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WO2004073600A2 - Procede et appareil de fabrication de silice precipitee a partir de cendre de balle de riz - Google Patents

Procede et appareil de fabrication de silice precipitee a partir de cendre de balle de riz Download PDF

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Publication number
WO2004073600A2
WO2004073600A2 PCT/IN2004/000047 IN2004000047W WO2004073600A2 WO 2004073600 A2 WO2004073600 A2 WO 2004073600A2 IN 2004000047 W IN2004000047 W IN 2004000047W WO 2004073600 A2 WO2004073600 A2 WO 2004073600A2
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WO
WIPO (PCT)
Prior art keywords
silica
rice husk
novel process
manufacture
precipitated silica
Prior art date
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Ceased
Application number
PCT/IN2004/000047
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English (en)
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WO2004073600A3 (fr
Inventor
Hanasoge Suryanarayana Avadani Mukunda
Srinivasaiah Dasappa
Palkat Joseph Paul
Dibbur Nagesh Rao Subbukrishna
Nagamangala Krishnaiyengar Sriranga Rajan
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Indian Institute of Science IISC
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Indian Institute of Science IISC
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Priority to JP2006502649A priority Critical patent/JP4537379B2/ja
Publication of WO2004073600A2 publication Critical patent/WO2004073600A2/fr
Publication of WO2004073600A3 publication Critical patent/WO2004073600A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1806—Stationary reactors having moving elements inside resulting in a turbulent flow of the reactants, such as in centrifugal-type reactors, or having a high Reynolds-number
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/0066—Stirrers
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B33/00—Silicon; Compounds thereof
    • C01B33/113—Silicon oxides; Hydrates thereof
    • C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
    • C01B33/18—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof
    • C01B33/187—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof by acidic treatment of silicates
    • C01B33/193—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof by acidic treatment of silicates of aqueous solutions of silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
    • B01F27/191—Stirrers with two or more mixing elements mounted in sequence on the same axis with similar elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
    • B01F27/192—Stirrers with two or more mixing elements mounted in sequence on the same axis with dissimilar elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/02—Apparatus characterised by their chemically-resistant properties
    • B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
    • B01J2219/0277—Metal based

Definitions

  • This invention relates to a novel process and apparatus for the manufacture of Precipitated Silica from Rice Husk Ash.
  • silica SiO 2 Process for the production of precipitated silica SiO 2 from rice husk ash having multiple applications in the filed of rubbers and plastics, paints, toothpaste, catalysts, carrier agent, insulation, stabilizing and desiccants.
  • the process for silica precipitation is novel, wherein the chemicals used are regenerated making it a closed loop operation.
  • the extraction process through digestion, precipitation and regeneration are done based on the application specifics, so as to get the required particle size and densities.
  • the present invention related generally to silica and more precisely to a novel process of obtaining silica from rice husk ash by precipitation using carbon dioxide for the process of precipitation.
  • the process has three stages i.e. digestion of rice husk, precipitation of silica from soluble silicate and regeneration of caustic solution and the final left over is used as activated carbon without involving any further processing.
  • Rice husk or paddy husk - an agricultural residue is available abundantly in rice producing countries. India alone produces approximately 12 million tons of rice husk annually. Rice husk is generally not advocated as cattle feed because of low cellulose and other sugar contents in it. Furfural and rice bran oil are extracted from rice husk. Rice husk is used by industries as fuel in boilers and for power generation. Rick husk has a high ash content varying from 18-20%. Silica is the major constituent of rice husk ash. High silica (SiO 2 ) content in rice husk ash is economically feasible to extract silica, which has wide market. The process also addresses the issue of appropriate disposal of rice husk ash. The strength of this novel process of extracting silica through precipitation is that with minor changes in the chemical composition the end product silica could be used for all the following application.
  • Stabilizing eg of beer, silicon rubbers
  • Non eutrophic water softening eg "builder” materials in washing.
  • the global scenario on production and consumption pattern of precipitated silica is around 6,75,000 M.T/annum according to 1994 reports.
  • the global market and demand for speciality silicas which includes Precipitated silica, silica gel, fumed silica and colloidal silica, reached and estimated value of $1.7 million.
  • the global market for speciality silicas is expected to grow at a rate of roughly 4.0 % a year (in real terms, excluding significant inflation) exceeding $2 billion in that year.
  • Synthetic amorphous silica for the industrial applications are produced in four different forms.
  • It contains three-dimensional network or aggregated silica particles of colloidal dimension.
  • the pores are filled with water. It is generally prepared in acidic conditions.
  • Precipitated silica is powder obtained by coagulation of particles from aqueous solution under the influence of appropriate electrolyte concentration.
  • the present patent is specific to the category Conventionally Precipitated Silica is manufactured by of fusion silica sand and sodium carbonate at high temperatures of around 1400 °C and the sodium silicate obtained is precipitated using acid mainly, sulphuric acid.
  • the conventional process and other process using sodium silicate obtained from rice husk ash involves acid (i.e., sulphuric acid) precipitation of the sodium silicate to produce Precipitated Silica.
  • Sodium sulphate is a waste that is generated and this liquid effluent requires elaborate treatment to meet emission standards.
  • the process requires effluent treatment plant for treating sodium sulphate. This calls for additional financial implications and any carelessness in treating the effluent would damage the environment.
  • Figure 1 is the block diagram illustrating the flow chart of the Digestion step of the present invention
  • Figure 2 is the block diagram illustrating the flow chart of the Precipitation step of the present invention
  • Figure 3 is the block diagram illustrating the flow chart of the Regeneration step of the present invention
  • Figure 4 illustrates a typical Silica Digester used in the process of the present invention
  • Figure 5 illustrates a typical Silica Precipitator used in the process of the present invention
  • Figure 6 illustrates a typical Regenerator used in the process of the present invention
  • the silica precipitation technology developed by us is a novel process for silica precipitation where the chemicals used are regenerated making it a closed loop operation.
  • Successful studies for extraction of silica (Chemical and Physical properties of the precipitated silica is given in Table 3) on laboratory scale carried out also meet the industrial requirements. Further studies carried out for suitable application of the undigested ash obtained after extraction, finds application in water treatment plants with or without any further processing as activated carbon.
  • Rice husk ash has a silica content of around 80 % - 90 % most of which is in amorphous nature, depending on the temperature of combustion. This silica can be extracted economically by the proposed process, which meets the requirements of the various industries. This novel process consists of three steps namely;
  • Digestion refers to extraction of the insoluble silica present in the ash to soluble salt in the form of sodium silicate.
  • the required quantity of sodium hydroxide (ratio varying from 1:1 to 1:4 with respect to dry ash) is dissolved in water and the ash is added after the temperature of the caustic reaches greater than 95°C.
  • Digestion studies were carried out at various temperatures in order to optimize the same. Digestion temperature of around 95°C was decided, as the optimum because of the higher silica recovery as can be seen in Table 1.
  • the digestion is carried out at this temperature for a period of lhr, which is the optimum time established by the experimental results as decrease in the time decreases the silica extracted and further increase in time of digestion hardly increases the yield obtained, which is evident from the experimental results given in Table 2.
  • Precipitation is the process in which the soluble sodium silicate reacts with carbon dioxide to form silicon dioxide. This is the crucial step to obtain the precipitated silica of required specifications, by varying the parameters. Sparging of required carbon dioxide was done with and without pressure and it was observed that the silica produced during the process created blockade of sparger holes when the carbon dioxide pressure was less than of 1.75 kg/cm 2 (gauge), which posed problems during the final stages in the form of uncontrollable flow rate of carbon dioxide producing silica of different properties each time. During this step the various parameters like temperature, flow of carbon dioxide and silica concentration in the sodium silicate solution play vital role in obtaining silica of different types.
  • silica concentrations in the sodium silicate solution ranging from 2.5 % to 10.0 % were tried for precipitation.
  • the variation of parameters results in silica of different quality. It was observed that silica concentration in the range of 4.5 % to 6.0% were suitable for producing the silica required by most of the industries. Higher and lower silica concentrations than the above range produced silica of higher density, in addition to the difficulties in handling the slurry during precipitation at higher concentrations.
  • Precipitation was carried out at various temperatures and it was observed that lower temperatures produced gel like silica with high density. It was also observed that the rate of carbonation affected the density of the silica produced, the density increasing with increasing flow rate.
  • the variation in the surface area can be controlled by the amount of carbonation, which is indicated by the determination of carbonate and bicarbonate at the end of precipitation.
  • Precipitation was also carried out with a mixture of air and carbon dioxide at different individual percentages. Similar properties of precipitated silica produced with pure carbon dioxide were obtained. These experiments were carried out to use the industrial flue gases, which contain carbon dioxide in the range of 10 - 15 %. Precipitation was also carried out at various Na 2 O: SiO 2 ratios. CHEMICAL SCHEMATIC REPRESENTATION OF PRECIPITATED SILICA USING RICE HUSK ASH:
  • the two main requirements for the silica produced are; 1. Surface area. 2. Tap density.
  • Controlling factors a. Surface Area: i. Surface area also depends upon the quality of mixing that takes place inside the precipitator, which varies with the agitator used. The surface area is low ( ⁇
  • Tap Density of the material is the density of the powder when a fixed quantity of the silica powder is tapped in a standard closed measuring cylinder till the volume of the powder remains constant and does not decrease with further tapings.
  • the tap density of the material is dependent on the ration of initial caustic to carbon dioxide flow rate as indicated in the figure below.
  • Regeneration of the solution is the conversion of sodium carbonate to sodium hydroxide by the use of Calcium hydroxide.
  • the regenerated sodium hydroxide is used for digestion of the fresh ash.
  • Calcium hydroxide can be either purchased from the market and the resulting calcium carbonate can be sold at the market or the calcium carbonate can be heated at around 850°C for converting it to calcium oxide which when comes in contact with water becomes calcium hydroxide. This depends on the market value of each product and the costs involved for either processing or purchasing.
  • the calcium carbonate obtained can be heated to 850°C upon which it breaks up into calcium oxide and carbon dioxide.
  • the carbon dioxide obtained is used for precipitation of silica from sodium silicate.
  • the calcium oxide is then used for regeneration.
  • the Apparatus consists of three parts i.e a digester, a precipitator and a regenerator for carrying out the three main steps of the present invention.
  • Each one is provided with a main reaction vessel 1, with a lid 2 and a flange 3 through which an agitator 4 is placed inside the reaction vessel 1.
  • the flange 3 has an outside diameter of 600mm and an inner diameter of 400mm and is made of stainless steel.
  • the flange 3 is provided with necessary holes 5 for placing bolts and nuts.
  • the agitator 4 is provided with two propellers 6.
  • a condenser 7, a temperature measurement slot 8 and feed inlets 9 & 10 are provided. The feed inlets are used to send the necessary reactants to the reaction vessel.
  • a ball value 11 is provided for product evacuation and drain value 12 is provided for sampling.
  • the reaction vessel and the lid are fully insulated with high quality ceramic wool insulation 13 with 0.5mm stainless sheet cladding.
  • the height of the liquid from the bottom of the vessel will be up to level marked 14.
  • the precipitator is additionally equipped with a sparger 15 through the inlet 10, for carbon dioxide. Through the inlet 16 of the sparger 15, a working pressure of > 1.75kg/cm 2 is applied to prevent blockade of sparger holes 17, by precipitated silica. In most of the experiments the hole dia was adjusted to let in the carbon dioxide or mixture of carbon dioxide & air at a velocity of > 400 m/s.
  • the agitator used in the precipitator has a paddle 18.
  • the length/Diameter of all the vessels is in the ratio of 2: 1.
  • Source of Silica is replenishable. It has been mentioned earlier in this document that all rice-producing countries have abundant quantity of rice husk. India alone produces about 12 million tons of rice husk every year.
  • the resultant material was dried in a hot air forced draft tray drier at 110°C.
  • Dried silica was ground using a high-speed grinder.
  • the surface area of silica produced with such was in the range of 150 - 200 m 2 /gm and the tap density of the material was in the range of 160 -220 kg/m 3 .
  • the ratio of Na2O:SiO2 was around 1:1.8.
  • Example 2 The conditions remained identical to example 1 except for usage of only Paddle type agitator (2 Nos) at the bottom and the middle portion of the vessel. Usage of this reduced the precipitation time by around 15 %.
  • the surface area of silica produced with such a procedure was in the range of 50 - 90 m 2 /gm and the tap density of the material was in the range of 160 -220 kg/m 3 .
  • Dried silica was ground using a high speed grinder. Propeller type agitators (2 Nos) at bottom and middle portion of the vessel and a Paddle type agitator was used in the top to ensure good mixing.
  • the surface area of silica produce with such a procedure was in the range of 150 - 200 m 2 /gm and the tap density of the material was in the range of 80 - 120 kg/m 3 .
  • the ratio of Na 2 O:SiO 2 was 1:3. The results of the experiments are given in Table 4.
  • the resultant material was dried in a hot air forced draft tray drier at 110°C.
  • Dried silica was ground using a high speed grinder.
  • the surface area of silica produce with such procedure was in the range of 300 - 350 m2/gm and the tap density of the material was in the range of 220 - 260 kg/m 3 .
  • the ratio of Na 2 O:SiO 2 was around 1:1.8.
  • Table 5 The results of five experiments carried out with the above conditions are given Table 5.
  • Dried silica was ground using a high speed grinder. Propeller type agitators (2 Nos) at bottom and middle portion of the vessel and a Paddle type agitator was used in the top to ensure good mixing.
  • the surface area of silica produce with such a procedure was in the range of 200 - 260 m 2 /gm and the tap density of the material was in the range of 100 - 140 kg/m 3 .
  • the ratio of Na 2 O:SiO 2 was around 1:1.75.
  • Table 6 The results of the experiments are given Table 6.
  • Dried silica was ground using a high speed grinder. Propeller type agitators (2 Nos) at bottom and middle portion of the vessel and a Paddle type agitator was used in the top to ensure good mixing.
  • the surface area of silica produced was 220 m 2 /gm and the tap density of the material was 510 kg/m 3 .
  • the ratio of Na 2 O:SiO 2 was around 1:1.9.
  • Appearance Precipitated Silica is a white free flowing powder. It is a very finely divided silica, in which the degree of polymerization is limited by the preparation technique

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Silicon Compounds (AREA)

Abstract

L'invention concerne un procédé destiné à la fabrication de silice précipitée à partir de cendre de balle de riz, ayant une aire comprise entre 400 et 500m2/g et une densité après tassement comprise entre 80 et 600kg/m3, pouvant être utilisée dans le domaine des caoutchoucs et des plastiques, des peintures, des pâtes dentifrices, des catalyseurs, des agents de transport, des isolements, des agents de stabilisation et des desséchants. Le processus de précipitation de la silice est nouveau, les substances chimiques utilisées étant régénérées, ce qui permet d'obtenir une opération en circuit fermé. Le procédé d'extraction par digestion, précipitation et régénération est réalisé sur la base de l'application voulue, pour obtenir les dimensions granulométriques et les densités souhaitées.
PCT/IN2004/000047 2003-02-18 2004-02-18 Procede et appareil de fabrication de silice precipitee a partir de cendre de balle de riz Ceased WO2004073600A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2006502649A JP4537379B2 (ja) 2003-02-18 2004-02-18 籾殻の灰から沈降シリカを製造するプロセスおよび装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN134CH2003 2003-02-18
IN134/MAS/2003 2003-02-18

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WO2004073600A3 WO2004073600A3 (fr) 2004-11-04

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Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7279147B2 (en) * 2005-05-25 2007-10-09 Selma Turkay Method of producing an adsorbent from rice hull ash
JP2009522264A (ja) * 2005-12-30 2009-06-11 ジェイ・エム・ヒューバー・コーポレーション 生物起源のシリカ材料を含む歯磨剤
WO2010135791A1 (fr) * 2009-05-29 2010-12-02 Radici Plastics Ltda Utilisation de la cendre de balle de riz dans des composés de polyamide
WO2011100811A1 (fr) * 2010-02-18 2011-08-25 Radici Plastics Ltda Utilisation de la cendre de coque de riz dans des composés (polypropylène)
WO2012020938A3 (fr) * 2010-08-13 2012-05-18 충남대학교산학협력단 Procédé pour préparer simultanément une silice de pureté élevée ayant une structure fine et des fibres
WO2012153897A1 (fr) * 2011-05-12 2012-11-15 충남대학교 산학협력단 Procédé de dérivation de silice et silicium très purs et poreux à partir de balles de riz
US20150068916A1 (en) * 2013-09-11 2015-03-12 King Fahd University Of Petroleum And Minerals Catalyst for electrochemical dechlorination of hydrocarbons
AU2013242721B2 (en) * 2012-03-26 2015-12-03 Sunshine Kaidi New Energy Group Co., Ltd. Method utilizing industrial flue gas for removing metal ions from rice hulls
WO2017042011A1 (fr) * 2015-09-09 2017-03-16 Compagnie Industrielle De La Matiere Vegetale - Cimv Procédé pour l'extraction de la silice
EP3156368A1 (fr) * 2015-10-15 2017-04-19 Rhodia Operations Nouveau procédé de préparation de silicate, nouveau procédé de préparation de silice précipitée
EP3088360A4 (fr) * 2013-12-25 2017-07-26 Zhongying Changjiang International New Energy Investment Co. Ltd. Procédé de production de dioxyde de silicium nanométrique et de carbonate de calcium nanométrique à l'aide de cendres de balle de riz et de gaz de combustion d'une centrale électrique à biomasse
WO2017179070A1 (fr) * 2016-04-14 2017-10-19 Indian Institute Of Science Procédé et système de génération de silice précipitée haute performance à partir de cendres de balle de riz
CN108217664A (zh) * 2018-03-16 2018-06-29 湖州长鑫电工材料有限公司 一种硅微粉选择性絮凝提纯用装置
CN108529635A (zh) * 2018-03-22 2018-09-14 益海（佳木斯）粮油工业有限公司 一种提升生物质白炭黑性能的稻壳原料
WO2018167682A1 (fr) * 2017-03-14 2018-09-20 Tata Chemicals Limited Procédé de préparation de verre soluble à partir de cendre de balle de riz
WO2018167646A1 (fr) * 2017-03-14 2018-09-20 Tata Chemicals Limited Procédé de préparation de silicate de sodium à partir de cendre de balles de riz
WO2018167648A1 (fr) * 2017-03-14 2018-09-20 Tata Chemicals Limited Procédé de préparation de silice à partir de cendre de balle de riz
CN108854906A (zh) * 2018-06-22 2018-11-23 安徽志成机械科技有限公司 一种节能散热型反应釜
US10479691B2 (en) 2014-04-01 2019-11-19 Rapas Corporation Method for recovering silica from silica-containing plant body using titanium oxide
CN110575801A (zh) * 2018-06-11 2019-12-17 河南骏化发展股份有限公司 用于双盐复分解法制备白炭黑的多功能交变载荷反应釜
WO2022050901A1 (fr) * 2020-09-04 2022-03-10 Agency For Science, Technology And Research Procédé de production de silice purifiée
CN115159529A (zh) * 2022-08-15 2022-10-11 锦洋高新材料股份有限公司 一种以工业二氧化硅固废物为原料经沉淀法制备白炭黑的方法
US11873218B2 (en) 2018-03-02 2024-01-16 Pörner Ingenieurgesellschaft M.B.H. Sustainable silicates and methods for their extraction
WO2024089003A1 (fr) 2022-10-28 2024-05-02 Rhodia Operations Procédé de préparation de silicate à partir de cendres végétales comprenant de la silice cristalline à l'aide d'un sel contenant un anion multivalent
EP4365230A1 (fr) 2022-11-02 2024-05-08 The Goodyear Tire & Rubber Company Silice traitée par un agent de couplage et polyéthylène glycol pour une composition de caoutchouc
WO2025180682A1 (fr) * 2024-02-29 2025-09-04 Unilever Ip Holdings B.V. Composition de soin buccal

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WO2005077828A1 (fr) * 2004-02-13 2005-08-25 Garry Robert Nunn Silice biogene soluble et ses applications
KR100982032B1 (ko) 2009-12-29 2010-09-13 한국건설기술연구원 왕겨를 이용한 펠렛의 제조방법
CN102212219B (zh) * 2011-04-06 2013-05-08 江南大学 一种用作橡胶填料的稻壳基碳/硅复合物及其制备方法
CN104692388A (zh) * 2013-12-05 2015-06-10 沈阳宜盛瓷新型材料有限公司 一种用稻壳制备高纯纳米三维多孔结构硅的方法
CN104368291B (zh) * 2014-09-29 2016-05-25 佛山市南海万兴材料科技有限公司 一种用于生产包裹色料的酸洗装置
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JP7069604B2 (ja) * 2017-08-28 2022-05-18 味の素株式会社 沈降シリカの製造法
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