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WO2011155830A1 - Procédé de conversion de minéraux de type silicate métallique en composés de silicium et composés métalliques - Google Patents

Procédé de conversion de minéraux de type silicate métallique en composés de silicium et composés métalliques Download PDF

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Publication number
WO2011155830A1
WO2011155830A1 PCT/NL2011/050408 NL2011050408W WO2011155830A1 WO 2011155830 A1 WO2011155830 A1 WO 2011155830A1 NL 2011050408 W NL2011050408 W NL 2011050408W WO 2011155830 A1 WO2011155830 A1 WO 2011155830A1
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WO
WIPO (PCT)
Prior art keywords
gpv
carbon dioxide
foregoing
channel
reactants
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/NL2011/050408
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English (en)
Inventor
Kees-Jan Leendert Rijnsburger
Paulus Carolus Mari Knops
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
PLAN B CO2
RIJNSBURGER HOLDING BV
Original Assignee
PLAN B CO2
RIJNSBURGER HOLDING BV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by PLAN B CO2, RIJNSBURGER HOLDING BV filed Critical PLAN B CO2
Priority to EP11726216.2A priority Critical patent/EP2580157A1/fr
Priority to AU2011262614A priority patent/AU2011262614B2/en
Publication of WO2011155830A1 publication Critical patent/WO2011155830A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/18—Carbonates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/20—Methods for preparing sulfides or polysulfides, in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/42—Sulfides or polysulfides of magnesium, calcium, strontium, or barium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/60—Preparation of carbonates or bicarbonates in general
    • 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
    • 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
    • C01B33/14—Colloidal silica, e.g. dispersions, gels, sols
    • C01B33/141—Preparation of hydrosols or aqueous dispersions
    • C01B33/142—Preparation of hydrosols or aqueous dispersions by acidic treatment of silicates
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/24—Magnesium carbonates

Definitions

  • the invention relates to a new method for converting metallic silicate minerals to silicon compounds and metal compounds via a conversion reaction.
  • silicate mineral The largest proportion of minerals by far in the earth's crust (about 90%) is a silicate mineral.
  • Each silicate mineral is built up of a lattice comprising silicate groups (Si04) and metals. Positively charged metal atoms are present in each lattice opposite the negative charge of each silicate group (4-) .
  • the type of lattice in which the silicate groups are arranged is subdivided into orthosilicates (isolated silicate groups), nesosilicates (chain of silicates) , phyllosilicates (silicates linked in sheets) and tectosilicates ⁇ 3-dimensional structure of silicates) .
  • orthosilicates isolated silicate groups
  • nesosilicates chain of silicates
  • phyllosilicates phyllosilicates linked in sheets
  • tectosilicates ⁇ 3-dimensional structure of silicates
  • silica or orthosilicic acid in particular are raw materials much used in industry.
  • various metal compounds which have economic importance as for instance intermediate product for metal extraction, can be separated in the form of a salt.
  • Serpentine a phyllosilicate
  • olivine a phyllosilicate
  • nesosilicate are silicates which comprise mainly magnesium as metal (and a lower content of iron) .
  • a conversion process for these magnesium silicates is known in which the mineral reacts with carbon dioxide in an autoclave under increased temperature and pressure to form magnesium (bi) carbonate and silicic acid as end product.
  • reaction ii and to even greater extent reaction iii, will predominate here.
  • a complete conversion of silicate mineral is obtained via these two reactions.
  • the invention has for its object to provide a method wherein the energy consumption is reduced and to achieve additional advantages.
  • the invention provides for this purpose a method for converting metallic silicate minerals to silicon compounds and metal compounds via a conversion reaction
  • the GPV comprises two channels having separate entries on the upper side of the GPV and which channels are mutually connected on the underside of the GPV,
  • a GPV is per se known from the American patient application US 2006/0086673 as a vertical, elongate, cylindrical vessel placed in the ground and having a length of several hundred metres.
  • This GPV is constructed from a central inner channel and an outer channel which encloses the inner channel.
  • Inner channel and outer channel are mutually connected on the underside of the GPV. Owing to this construction a flow introduced into the inner channel is carried to a lowest point inside the GPV and then carried upward through the outer channel to then leave the GPV.
  • the descending flow in the inner channel consists of a slurry of dispersed silicate minerals in water with a density of about 2 kg/litre a pressure increase of up to 20 bar can be achieved per 100 metre length of a GPV.
  • the flow From the lowest point inside the GPV the flow reverses and moves upward through the outer channel, leaving the GPV at the surface.
  • the entry flow is here usually carried with some overpressure into the GPV.
  • the first channel through which the descending flow is carried is preferably embodied as inner channel.
  • the second channel is preferably embodied as outer channel.
  • the whole GPV preferably has an overall length of between 500 and 800 metres, wherein the first channel and second channel have corresponding lengths.
  • the GPV provides a very efficient heat use.
  • the conditions can be chosen such that reaction products are formed substantially in the lowest part of the descending flow and the further part of the ascending flow so that more heat is created overall in the ascending flow. This makes the GPV eminently suitable for heat exchange.
  • the heat from the ascending flow can usefully be employed to heat the descending dispersion flow before it reaches the lowest point.
  • the outer channel can relinquish the formed heat to the inner channel via a separating wall which separates the inner channel from the outer channel.
  • the separating wall then functions as heat exchanger.
  • the reactants are introduced here at some point in the descending flow: this can be at the position of the entry on the upper side of the GPV, but can also be at some depth in the descending flow via a separate conduit. It is a further advantage in the method according to the invention for the solid particles of silicate minerals in dispersion to have an average diameter in the order of magnitude of 2-3 millimetres or smaller. This upper limit for the particle size is relatively high compared to the usual particle size for a reaction in an autoclave. In an autoclave a particle size is generally applied which is at least a factor of 100 smaller, and so lies in the order of magnitude of micrometres.
  • the content of the particles of silicate minerals in the dispersion preferably lies between 3% by weight and 30% by weight of the overall weight of the dispersion.
  • the process requires a minimum content in order to be economically attractive, while on the other it is a requirement that no undesired agglomerations of solid material, which can block or impede the dispersion flow, can take place in the dispersion.
  • the formed silicon compounds preferably comprise silica and/or
  • the formed metal compounds further comprise metal bicarbonates and/or metal carbonates.
  • Soluble metal bicarbonates are a good nutrient for oil-producing algae, such as determined seaweeds and algae. The bicarbonates thus form an attractive alternative to the introduction of carbon dioxide gas into the medium in which the algae are cultivated, in addition, metal carbonates have for instance an advantageous function as absorbent in solution for absorbing carbon dioxide, with the formation of bicarbonates.
  • the formed metal compounds more preferably comprise metal sulphides.
  • metal sulphides For the separation of valuable metals it is attractive to obtain for instance nickel and iron in sulphide form. The metal can then be extracted via known conversion reactions.
  • the silicate compounds and metal compounds formed during the conversion are separated from the slurry in usual ways, such as by filtration, precipitation or by applying a cyclone.
  • the metallic silicate minerals advantageously comprise olivine or serpentine. It has been demonstrated for these minerals that the operational costs for complete conversion thereof to silicate compounds and metal compounds can be halved per kilogram of starting material.
  • reactants are more preferably applied which are chosen from a group of acids comprising hydrochloric acid, sulphuric acid, carbon dioxide and bicarbonate.
  • acids comprising hydrochloric acid, sulphuric acid, carbon dioxide and bicarbonate.
  • carbon dioxide can react with silicate minerals in accordance with known reactions, several examples of which have been given in the introduction.
  • Hydrochloric acid and sulphuric acid are known acids which (usually as liquid) react with silicate minerals, wherein respectively metal chloride and metal sulphate are formed in addition to silica.
  • Bicarbonate in solution reacts with silicate minerals similarly to carbon dioxide.
  • the erosion of silicate particles in the descending dispersion flow can be further enhanced when gas bubbles are present in the flow which cause turbulent flows in the main flow.
  • This can be achieved by introducing a reactant in gas form into the descending dispersion flow. If no reactant in gas form is introduced it is possible to consider introducing an additional inert gas so that the enhancing effect of the gas bubbles is nevertheless
  • the operational costs of the process are further reduced.
  • one or more of the reactants are preferably added in gas form to the descending dispersion flow.
  • This has the effect of creating turbulence in the descending dispersion flow, whereby the erosion of the particles of silicate mineral is enhanced, with the above stated resulting advantages.
  • the heat transfer inside the GPV is improved by the presence of gas bubbles.
  • the addition of the reactants in gas form can for instance be performed via a conduit provided wholly or partially in the first channel. The gas is brought under a suitable pressure here so that at the position of the injection point a slight overpressure is created relative to the hydrostatic pressure prevailing there in the first channel .
  • the concentration of gas bubbles formed in the liquid flow must remain below a critical limit so that the gas bubbles do not accumulate into a large gas bubble which disrupts the continuity of the liquid flow. This is undesirable from the viewpoint of hydrodynamics, but also from the viewpoint of an optimal reaction surface area between the gas phase and the liquid phase.
  • the aim in practice is a gas content in the dispersion of between 10 and 50% by volume, preferably 20 to 40% by volume, for instance 30% by volume.
  • the gas phase has an intrinsically greater volume per quantity of reactant than the liquid phase, it is generally desirable, or even essential, to introduce the gaseous reactant distributed over the liquid flow ⁇ i.e.
  • the GPV comprises a heat exchanger, preferably a system of heat exchangers, and that with particular preference the heat exchanger herein comprises a water reservoir which encloses a part of the GPV as a casing and wherein a plurality of supply and discharge conduits for water are provided at different positions in the reservoir.
  • the heat exchanger is for instance provided round the GPV as a casing which is in heat-exchanging contact with the channels of the GPV so that surplus heat - i.e. heat which is not used in the exchange between the channels in the GPV - can be discharged externally.
  • the GPV advantageously comprises a system of heat exchangers which can be deployed actively at different heights of the GPV.
  • the temperature inside the GPV can thus be actively controlled so that an optimum temperature for the conversion reaction can be maintained along the column in the GPV. Maintaining an optimum temperature on the underside of the GPV ⁇ at the highest pressure) is for instance very desirable for the purpose of controlling the conversion reaction. An optimum temperature is moreover often desirable for the exit flow on the upper side.
  • the heat discharged by the heat exchanger (s) can be used in other processes, for instance to produce
  • the heat exchanger can optionally be used in reverse manner to supply heat to the GPV when heating of the slurry in the GPV is desired.
  • the invention relates to a conversion reaction in which carbon dioxide or a derivative form thereof is applied as reactant, wherein the silicate mineral functions as sequestering agent for carbon dioxide or a derivative thereof.
  • Sequestration in this context is a general term for storing carbon dioxide in a compound, whereby gaseous carbon dioxide is extracted from the atmosphere or release of formed carbon dioxide into the atmosphere is prevented.
  • the reactants comprise carbon dioxide and/or bicarbonate
  • the silicate mineral functions as sequestering agent for carbon dioxide and/or bicarbonate.
  • the reactants are introduced at some point in the descending flow: this can be at the position of the entry on the upper side of the GPV, but can also be via a separate conduit at some depth in the descending flow.
  • the metallic silicate minerals advantageously comprise: olivine or serpentine. With these minerals a reduction in operational costs can be achieved of about 50%. These minerals moreover have a high absorbing capacity for sequestration of carbon dioxide: about 1 kilogram of olivine is able to absorb or store 1.2 kilograms of carbon dioxide.
  • the reactants preferably comprise carbon dioxide and the carbon dioxide is added in gas form.
  • the carbon dioxide is preferably obtained from a regeneration of absorbent amines or from flue gas from a bioethanol plant.
  • the advantage hereof is that such carbon dioxide has a high concentration in gas form, which enhances the kinetics of the reaction. A high concentration of 80%, preferably 90% or higher, is generally desirable for good reaction kinetics.
  • flue gas from an ammonia plant can also be used.
  • the reactants comprise dissolved bicarbonate, this bicarbonate originating from the reaction of gaseous carbon dioxide with calcium carbonate and/or magnesium carbonate. This method provides the advantage that a concentrated flow of reactant can be supplied when use is made of a flue gas with a low
  • concentration of carbon dioxide for instance lower than 50% ⁇ .
  • the method thus provides a method for sequestration of carbon dioxide, wherein the heat produced can be utilized to form a concentrated gas flow of carbon dioxide prior to sequestration.
  • gaseous carbon dioxide is preferably added at different positions in the first channel of the GPV.
  • the silicate minerals have not yet reacted completely, whereby the capacity of the mineral has not been wholly utilized.
  • a complete reaction can still be achieved by feeding back unreacted material.
  • the unreacted particles have to be
  • the solid particles of silicate minerals advantageously have an average diameter in the order of magnitude of 2-3
  • Water that is salt water is advantageously applied in the invention.
  • the higher concentration of dissolved salts results in a higher ion activity being obtained in salt water, which has a positive effect on the conversion
  • Fig. 1 shows a cross-sectional schematic view of a GPV in which a method according to the invention is performed.
  • Fig. 2 shows a variant of the GPV of fig. 1, in which the heat exchanger is modified.
  • Figure 1 shows a GPV 1 with an inner channel 3 and an outer channel 5, separated from each other by the inner wall 7 which encloses inner channel 3.
  • the length of the GPV is in reality much greater than shown in the figure.
  • the flow direction inside the channels is shown with arrows.
  • a slurry of silicate mineral in water is introduced into inner channel 3 via entry 9.
  • An injection pipe 10 is inserted into inner channel 3 for the purpose of introducing reactant via entry 11, in this case gaseous carbon dioxide. Gas bubbles of carbon dioxide which are formed in the slurry are shown at the bottom end of pipe 10.
  • the ascending flow in outer channel 5 will consist largely of wholly converted silicate mineral, i.e. of separate silicate compounds and metal compounds.
  • the exiting flow 14 is further processed in order to separate and process the produced compounds. If desired, the flow direction inside the GPV can also be the other way round, provided the supply channels and discharge channels also take a reversed form.
  • the GPV has an insulating outer casing 16 to limit heat loss to the environment, although the insulating property is not always necessary in practice depending on the ground composition.
  • the outer casing Provided in the outer casing are two heat exchangers consisting of a spiral-shaped water conduit 18 through which water can be pumped from inlet 20 to outlet 22.
  • the heat exchangers are placed at different levels: one at the top and the other at the bottom. Depending on the reactions taking place in the GPV, surplus heat is created at one or both levels. As soon as this is detected (for instance using heat sensors (not shown) ) water is pumped through the heat exchanger and heat is thus extracted from the system. This heat can be used elsewhere in any desired manner as energy source for various processes, such as generating electricity.
  • the heat flow through the heat exchanger can otherwise also take place in the reverse direction, wherein heat is now carried to the GPV for the purpose of heating the reaction mixture in the GPV.
  • Figure 2 shows a GPV with similar parts as in figure 1, wherein the corresponding components have the same
  • the heat exchanger in fig. 2 consists of a water reservoir 30 filled with water.
  • a main conduit 32 with a valve 34 for water feed is connected to water reservoir 30.
  • Protruding into water reservoir 30 are three pipes 36 of different lengths and with a valve 38, which opens or closes the pipes and with which it is possible to switch between water discharge or water feed. Diverse combinations can thus be made of water flows between the outer ends of pipes 36.
  • a flow as indicated with arrows is optimal during use of the GPV wherein the reaction of olivine with C02 is in progress and sufficient heat is produced.
  • Water is introduced here into the reservoir via main conduit 32 and discharged via the shortest pipe 36 for the purpose of cooling discharge flow 14. Water is also
  • the heat exchange can be controlled with more variation during use of the GPV due to the arrangement of the heat exchanger according to figure 2.
  • Example 1
  • a GPV of one of the two types as shown above is applied with the following specifications:
  • the length of the GPV shaft is 600 m, the diameter of inner channel and outer channel respectively 20 cm and 30 cm.
  • the diameter can be in the order of magnitude of several metres.
  • a slurry of olivine particles of 2-3 mm in salt water is introduced at about 10 bar into the inner channel.
  • the density of the slurry is about 1.9 kg/litre.
  • the particles are slowly worn down by erosion.
  • Carbon dioxide gas (concentration: 90% partial
  • a complete conversion according to reaction ii) of olivine to magnesite (MgC03) takes about 2 hours at a pressure of 150 bar and a temperature of 185°C, and at a particle size of 75 pm.
  • This quantity of carbon dioxide is comparable to the emission of a.600 MW coal-fired power station.
  • the carbon dioxide gas is obtained in a concentration of 90% from the regeneration of amines which have absorbed carbon dioxide.
  • the energy obtained via the heat exchangers of the GPV is sufficient to carry out this regeneration, to produce sufficient carbon dioxide gas for the conversion reaction in the GPV.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Dispersion Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Treating Waste Gases (AREA)

Abstract

Procédé de conversion de minéraux de type silicate métallique en composés de silicium et composés métalliques par une réaction de conversion, ledit procédé étant caractérisé en ce que la réaction de conversion est mise en œuvre dans un réacteur sous pression opérant par gravité (GPV), comme suit : le GPV comprend deux canaux ayant des entrées séparées du côté supérieur du GPV, lesdits canaux étant reliés ensemble dans la partie basse du GPV, et une dispersion de particules solides des minéraux de type silicate est entraînée dans le GPV par un flux descendant, un ou plusieurs réactifs pour la réaction de conversion sont ajoutés à la dispersion, et les composés de silicium et les composés métalliques qui se sont formés lors de la réaction de conversion sont entraînés par un flux ascendant du GPV. Le procédé fournit un procédé de séquestration de dioxyde de carbone, la chaleur produite pouvant être utilisée pour former un flux gazeux concentré de dioxyde de carbone avant la séquestration.
PCT/NL2011/050408 2010-06-08 2011-06-08 Procédé de conversion de minéraux de type silicate métallique en composés de silicium et composés métalliques Ceased WO2011155830A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP11726216.2A EP2580157A1 (fr) 2010-06-08 2011-06-08 Procédé de conversion de minéraux de type silicate métallique en composés de silicium et composés métalliques
AU2011262614A AU2011262614B2 (en) 2010-06-08 2011-06-08 Method for converting metal comprising silicate minerals into silicon compounds and metal compounds

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL2004851 2010-06-08
NL2004851A NL2004851C2 (nl) 2010-06-08 2010-06-08 Werkwijze voor het omzetten van metaalhoudende silicaatmineralen tot siliciumverbindingen en metaalverbindingen.

Publications (1)

Publication Number Publication Date
WO2011155830A1 true WO2011155830A1 (fr) 2011-12-15

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Country Link
EP (1) EP2580157A1 (fr)
AU (1) AU2011262614B2 (fr)
NL (1) NL2004851C2 (fr)
WO (1) WO2011155830A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102021116491A1 (de) 2021-06-25 2022-12-29 Rheinisch-Westfälische Technische Hochschule Aachen, Körperschaft des öffentlichen Rechts Karbonatisierungsverfahren und Karbonatisierungsmischung
DE102023108019A1 (de) 2023-03-29 2024-10-02 Andreas Michael Bremen Reaktorsystem für ein Karbonatisierungsverfahren

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Publication number Priority date Publication date Assignee Title
US6068825A (en) * 1998-07-15 2000-05-30 Japan As Represented By Director General Of Agency Of Industrial Science And Technology Method for the preparation of a high-quality powder of amorphous silicic acid
WO2000046149A1 (fr) * 1999-02-03 2000-08-10 Italcementi S.P.A. Procede de preparation de silice a partir de silicate de calcium
WO2002048036A1 (fr) * 2000-11-02 2002-06-20 Silica Tech Ans Extraction de composes de silice et de magnesium a partir d'olivine
US20060086673A1 (en) 2004-10-27 2006-04-27 Titmas James A Gravity pressure vessel and related apparatus and methods
WO2007060149A1 (fr) * 2005-11-23 2007-05-31 Shell Internationale Research Maatschappij B.V. Procede de sequestration de dioxyde de carbone par carbonation minerale
WO2007069902A1 (fr) * 2005-11-24 2007-06-21 Institutt For Energiteknikk PROCEDE DE FABRICATION INDUSTRIELLE DE MgCO3 PUR A PARTIR D’UN TYPE DE PIERRE CONTENANT DE L’OLIVINE
WO2008101293A1 (fr) * 2007-02-20 2008-08-28 Hunwick Richard J Système, appareil et procédé de séquestration de dioxyde de carbone
WO2008142017A2 (fr) * 2007-05-21 2008-11-27 Shell Internationale Research Maatschappij B.V. Procédé de séquestration de dioxyde de carbone par carbonatation minérale
WO2009086551A1 (fr) * 2008-01-03 2009-07-09 The Trustees Of Columbia University In The City Of New York Systèmes et procédés permettant de renforcer in situ le taux de carbonatation de la péridotite
WO2010006242A1 (fr) * 2008-07-10 2010-01-14 Calera Corporation Production de compositions contenant du carbonate à partir d'un matériau comportant des silicates métalliques

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6068825A (en) * 1998-07-15 2000-05-30 Japan As Represented By Director General Of Agency Of Industrial Science And Technology Method for the preparation of a high-quality powder of amorphous silicic acid
WO2000046149A1 (fr) * 1999-02-03 2000-08-10 Italcementi S.P.A. Procede de preparation de silice a partir de silicate de calcium
WO2002048036A1 (fr) * 2000-11-02 2002-06-20 Silica Tech Ans Extraction de composes de silice et de magnesium a partir d'olivine
US20060086673A1 (en) 2004-10-27 2006-04-27 Titmas James A Gravity pressure vessel and related apparatus and methods
WO2007060149A1 (fr) * 2005-11-23 2007-05-31 Shell Internationale Research Maatschappij B.V. Procede de sequestration de dioxyde de carbone par carbonation minerale
WO2007069902A1 (fr) * 2005-11-24 2007-06-21 Institutt For Energiteknikk PROCEDE DE FABRICATION INDUSTRIELLE DE MgCO3 PUR A PARTIR D’UN TYPE DE PIERRE CONTENANT DE L’OLIVINE
WO2008101293A1 (fr) * 2007-02-20 2008-08-28 Hunwick Richard J Système, appareil et procédé de séquestration de dioxyde de carbone
WO2008142017A2 (fr) * 2007-05-21 2008-11-27 Shell Internationale Research Maatschappij B.V. Procédé de séquestration de dioxyde de carbone par carbonatation minérale
WO2009086551A1 (fr) * 2008-01-03 2009-07-09 The Trustees Of Columbia University In The City Of New York Systèmes et procédés permettant de renforcer in situ le taux de carbonatation de la péridotite
WO2010006242A1 (fr) * 2008-07-10 2010-01-14 Calera Corporation Production de compositions contenant du carbonate à partir d'un matériau comportant des silicates métalliques

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102021116491A1 (de) 2021-06-25 2022-12-29 Rheinisch-Westfälische Technische Hochschule Aachen, Körperschaft des öffentlichen Rechts Karbonatisierungsverfahren und Karbonatisierungsmischung
WO2022268789A1 (fr) 2021-06-25 2022-12-29 Rheinisch-Westfälische Technische Hochschule (Rwth) Aachen Procédé de carbonatation et mélange de carbonatation
DE102023108019A1 (de) 2023-03-29 2024-10-02 Andreas Michael Bremen Reaktorsystem für ein Karbonatisierungsverfahren
WO2024200557A1 (fr) 2023-03-29 2024-10-03 Bremen Andreas Michael Système de réacteur pour un procédé de carbonatation

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