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WO1998024733A1 - Preparation de cendres volantes selon un procede par voie humide - Google Patents

Preparation de cendres volantes selon un procede par voie humide Download PDF

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Publication number
WO1998024733A1
WO1998024733A1 PCT/US1997/022010 US9722010W WO9824733A1 WO 1998024733 A1 WO1998024733 A1 WO 1998024733A1 US 9722010 W US9722010 W US 9722010W WO 9824733 A1 WO9824733 A1 WO 9824733A1
Authority
WO
WIPO (PCT)
Prior art keywords
carbon
fly ash
fraction
microspheres
particles
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/US1997/022010
Other languages
English (en)
Inventor
Clinton W. Pike
Jerry L. Heavilon
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.)
Jtm Industries Inc
Boral Materials LLC
Original Assignee
Jtm Industries Inc
ISG Resources Inc
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 Jtm Industries Inc, ISG Resources Inc filed Critical Jtm Industries Inc
Priority to AU55143/98A priority Critical patent/AU5514398A/en
Publication of WO1998024733A1 publication Critical patent/WO1998024733A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B18/00—Use of agglomerated or waste materials or refuse as fillers for mortars, concrete or artificial stone; Treatment of agglomerated or waste materials or refuse, specially adapted to enhance their filling properties in mortars, concrete or artificial stone
    • C04B18/04—Waste materials; Refuse
    • C04B18/06—Combustion residues, e.g. purification products of smoke, fumes or exhaust gases
    • C04B18/08—Flue dust, i.e. fly ash
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/91—Use of waste materials as fillers for mortars or concrete

Definitions

  • This invention relates to the beneficiation of fly ash and more particularly to the wet process for removing a high purity carbon and providing an enhanced reactive pozzolan.
  • the coal-fired utility companies produce fly ash as a by-product from the combustion of pulverized coal and, in many instances, including petroleum coke.
  • the material making up the fly ash includes primarily devolotized mineral matter which had been trapped or loosely associated with the coal and incombustible components and elements of the coal, and also of the petroleum coke where that fuel is present.
  • the fly ash also contains discrete carbon rich particles which have not been completely combusted, due to the inefficiency of the boiler design or other related conditions.
  • Fly ash as collected throughout the United States can have carbon contents of as little as about 0.5% up to 20% or more. Fly ashes may be utilized as an acceptable mineral admixture for use in portland cement concrete under the standards set out in ASTM C-618 which limits loss on ignition (LOI) to 6%.
  • the LOI value generally equates to the carbon content of the fly ashes.
  • carbon content is known to be undesirable in any case because its presence changes the demand for air entraining admixtures that are used to entrain air into concrete. Carbon causes an undesirable reduction in the entrained air, and in many countries, entrained air is the only real protection which concrete has against the freeze-thaw/wet-dry phenomena.
  • This invention relates to a wet process for beneficiating fly ash and providing a relatively high purity carbon.
  • the carbon content is predominately devolatized and exhibits a porous surface area with pore sizes up to 20 microns. As a result, this carbon has a very high total surface area.
  • An important aspect of the method of this invention includes the recognition of the cause of degradation of carbon purity and the value of such entrapped particles, and provides processing steps which free the particles from the carbon flotation fraction by attrition scrubbing and by reflotation of such fraction into a carbon fraction of reduced size and enhanced purity, and an underflow fraction of extremely fine sub-micron spheres which may be combined with the pozzolan fraction to increase pozzolanic activity.
  • a further benefit to the process is the fact that the carbon is broken down into even a finer particle size with increased surface area, so that the carbon product can be more competitive as a filler for products such as rubber and plastic, and as a purifying agent for aqueous filters and the like.
  • the combined fly ash fraction is treated and dried in such a way that the end product is essentially free of combined agglomerations and clumps greater than 325 mesh.
  • the handling and drying process of this invention not only prevents the coarseness which has been the result of conventional drying but maintains the pozzolanic activity of the product by assuring the freeness of even the smallest particles. This is accomplished by feeding the dewatered and combined pozzolan fractions through an enclosed dryer system including a screw-type feed with a heated blade or blades. This drying in such a heated blade-type conveyor controls the escape of volatiles and provides a means by which any remaining volatile organic compounds (VOC) may be properly collected and handled.
  • VOC volatile organic compounds
  • the enhanced dried pozzolan is subjected to a final disaggregation in a high speed type mixer which has the energy necessary to separate the agglomerations into individuals particles so that the final product is essentially free of clumps which would prevent it from passing through a 325 mesh screen.
  • the pozzolan fraction may also be enhanced by adding an alumina clay and/or lime in the mixer to increase early and overall strength of a cementitious product, as set out in co-owned U.S. patent of Styron et al. 5,484,480.
  • Such additive, in aggregate, may comprise between about 3 to 5% by weight of the enhanced pozzolan.
  • the invention may be considered as a method of making an enhanced pozzolan from fly ash containing carbon, in which the carbon is in the form of carbon particles which contain non-carbon fly ash microspheres, including the steps of screening the fly ash to obtain a screened ash which is free of larger particles, such as in the size of about +50 mesh or more.
  • This step has the advantage of removing scoria, larger ferrite particles, and particles which have fused together to form hard clumps. These types of particles interfere with the pozzolan reaction by not contributing to the cementitious reaction and because scoria is porous and has a high surface area and negatively impacts any chemical reaction by retaining surface modifiers which may be added.
  • pre-screening substantially reduces the demand for conditioning chemicals which are required in the subsequent flotation steps.
  • Water is added to the screened fly ash to form a fly ash slurry and flotation and conditioning chemicals may be added at that time.
  • the conditioned fly ash is then applied to flotation tanks from which a carbon rich fraction and a non-carbon pozzolan fraction are separated.
  • the carbon rich fraction described above, contains impurities primarily in the form of tiny microspheres in the porous surface which impurities have significant value for the final pozzolan product.
  • microspheres are removed, in substantial part, by delivering the carbon rich fraction to an attrition mill or other commutation equipment in which the carbon flotation fraction is subjected to conditions in which a substantial portion of the microspheres are released from the remaining carbon particles.
  • the carbon particles are broken down into even smaller particles increasing the surface area of the carbon fraction.
  • further flotation reagents are re-added thereby forming a carbon rich slurry which contains freed microspheres.
  • a particularly effective and preferred method of breaking down the carbon rich fraction includes applying the fraction to an attrition mill in which a counter flow caused by opposing impellers, combined with steel or ceramic scrubbing balls in the liquid matrix, the balls operate to increase the impingement contact with the particles.
  • Such attrition scrubbing also reduces the size of the carbon component, thereby facilitation floatation separation from the matrix.
  • This carbon rich slurry is then floated in a second bank of flotation cells and a second carbon rich fraction and a second pozzolanic non- carbon fraction is formed, consisting primarily of tiny microspheres.
  • the second non-carbon fraction may then be combined with the first pozzolanic fraction to form an enhanced pozzolan which may then be dewatered and dried.
  • the second carbon fraction forms an improved carbon product.
  • the preferred drying procedure comprises applying the combined wet fraction to a heated screw-type linear dryer for driving off water and volatiles, thereby having less than 0.3% moisture non-carbon product.
  • This product in spite of the agitation received in the screw-type dryer, may yet contain small agglomerations of weakly bonded together fly ash particles which may exceed the opening of a 325 mesh screen.
  • the dried product from the linear screw-type conveyor is preferably applied to a high speed mixer which frees up any bonds between such particles and breaks up agglomerations to provide a final pozzolan which consists of a non-carbon fraction of fly ash combined with the microspheres extracted from the carbon rich fraction.
  • the pozzolan may be further enhanced by the addition of lime and/or an alkaline clay, as explained above.
  • a further object of the invention is to provide a super enhanced pozzolan by separating microspheres as small as 1 micron or less from the matrix of a carbon rich flotation fraction and recombining such microspheres into the non-carbon fraction and similarly providing an enhanced carbon fraction which has been reduced in size and from which has been extracted a non-carbon impurity.
  • a still further object of the invention is to provide a wet-type enhancement process for carbon laden fly ash which is economical to practice and which provides a valuable useful end products.
  • a source of dry fly ash having a carbon content is illustrated at 10.
  • This source may have been electrostatically collected from a public utilities electric power generation station, for example, and may contain a significant component of carbon particles, usually in excess of 6%, and for some fly ashes may exceed 20%.
  • a first desirable step in the beneficiation of such fly ash is to remove that portion of the source 10 which exceeds about 50 mesh by screening on a dry or a wet screen 11. This screening step has the effect of removing larger aggregates, clumps, and scoria commonly contained in raw fly ash and which would provide an undesirable load on the system and on the reagents which are required in the flotation processes.
  • the underflow from the screen 11 is directed into a conditioner or blender in which process water is added to provide a relatively high consistency slurry of fly ash and water in the order of about 65% solids.
  • the conditioner 12 provides a thorough mixing and blending of the screened ash, and flotation reagents are added at this stage.
  • the conditioning in the conditioner 12 need only extend until there has been a thorough mixing and blending of the solids with the liquid and reagents suitable for application to a first bank of flotation cells.
  • the combined conditioned ash and reagents are then withdrawn from the conditioner 12 by a slurry pump 14 and applied to the inlet of a bank 15 of flotation cells 15a-15d. While four cells are shown, more or fewer may be used depending upon the capacity required. Also, at this time, dilution process water is added to reduce the relatively high consistency to a consistency ideal for proper flotation.
  • the solids content is influenced by particle size, the percentage of carbon content, the retention time, and the pH. Typically, the solids content will be in a range of about 5 to 20% solids.
  • the process water used at the bank 15 of flotation cells and at the conditioner 12 may be recycled from a system clarifier common to the various thickener and dryer positions within the system, with suitable make-up water added as required at the clarifier.
  • the mixture of conditioned and screened fly ash, flotation reagents, and dilution water is agitated and aerated, according to conventional flotation practice in the cell bank 15 to form a first carbon rich flotation fraction at the top and a non-carbon fraction at the bottom.
  • the non-carbon fraction, following flotation, is removed on a line 16 for further thickening and processing.
  • the first carbon rich floatation fraction from the cells 15 in line 17 consists primarily of carbon and other elements which have attached to the froth. This fraction is applied to an attrition mill 20.
  • the carbon rich fraction is, in affect, a carbon which is contaminated with a non-carbon component.
  • the carbon particles tend to be porous and vesicular, and have entrapped within them and/or bonded to them non-carbon particles primarily in the form of very small microspheres, in the order of one micron or less in size.
  • This microsphere component may comprise a substantial portion of the mass of the fraction such as in the range of approximately 20% to 40%.
  • a particularly useful attrition mill 20 is a two-stage attrition scrubber of the kind commonly used in clay processing operations, such as the variable pitch axial flow two-stage Attrition Scrubber made by Denver Equipment Company, Div. of the Denver Solo group of companies, Colorado springs, Colorado 80901.
  • the preferred attrition mill employs helix variable- pitch reversed pitched impellers 20A,20B mounted in pairs on common parallel shafts to provide counterflow between the opposing impellers.
  • the attrition process is augmented by the inclusion of ceramic or steel balls 20C in the matrix, steel balls being preferred, to enhance particle breakdown by impingement of particles between the balls. It has been found that the balls significantly increase particle size reduction and surface area. At the same time, the microspheres are released from entrapment.
  • the percentage of such recovered non-carbon solids in the first carbon floatation fraction typically may run between about 25 to 35% of the total weight of the solids.
  • the preferred attrition mill with ceramic or metals balls as a grinding media has been found to operate over a wide range of matrix consistencies or percentages of solid material.
  • the first float may be taken directly from the cells 15 and applied to the mill 20 without pre-thickening although pre-thickening could be inserted, if desired.
  • floatation reagents may be added in the mill 20 so that the conditioner will come into intimate contact with the carbon particles.
  • the addition of grinding balls in the mill 20 has a significant effect on the increase in the specific surface area of the carbon component.
  • a preferred loading of grinding balls consists of the use of between about 25 to 40 percent displacement, by volume, by balls in the diameter of about between one-quarter and three-eighths of an inch into matrix, which balls are retained within the mill 20 by a retention screen at the outlet.
  • about 310 pounds of steel balls are used in an approximately two cubic foot diameter attrition mill of the kind described above and shown at reference numeral 20 and the through-put rate at about 16 percent solids, may be in the order of about nine gallons per minute.
  • the carbon-rich fraction following scrubbing in the mill 20 is diluted as necessary and applied to a second bank 22 of flotation cells, illustrated as comprising cells 22a-22d. Obviously, these cells may be of considerably lower capacity than the cells of bank 15 since the quantity of product handled may be anywhere between 10% to 30% of the original input to bank 15.
  • the milled carbon rich fraction may be diluted with process water and further reagents may be added at the cells 22. The dilution is to a solids consistency which is most efficient for further separation, in the order of about 5 to 10%.
  • a second carbon rich fraction is formed since the froth has a purity substantially greater than that of the first fraction, while a second non-carbon fraction is formed consisting primarily of fly ash microspheres released from the first carbon fraction, as an underflow from the cells.
  • the increased fineness of the carbon component facilitates its flotation.
  • the non-carbon fraction from the cells is removed on a line 24 for further processing.
  • the feed float on line 17 to the mill in a particular instance was measured as having a specific surface area (CM 2 CM 3 ) of 9,888.
  • the carbon overflow from the bank 22 produced a specific surface area of 11,942, indicating an increase in surface area of about 18 percent over milling without using steel balls.
  • the second carbon rich fraction is, therefore, of relatively high purity, and is applied to a thickener 25 where it is thickened to a consistency of approximately 50%, and applied by pump 26 to a final drum-type filter 27 and further thickened. Then it is dried in an enclosed linear heated flighting screw- type dryer 30 for storage in a container 32.
  • the heated flighting screw-type dryer 30 may be a thermal processor sold under the HOLO-FLIGHT trademark by Denver Equipment Company, Colorado Springs, Colorado 80901. Filtrate from the thickener 25 and filter 27 is returned to the clarifier.
  • the underflow fractions from lines 16 and 24 are combined and dried, see Fig. IB.
  • the product may be applied to a thickener 40 where a substantial portion of the fluid content is removed to provide a thickened pozzolan, and to collect the cenospheres.
  • the cenospheres rise to the surface, in the thickener vat, in which the fly ash component and microspheres are allowed to settle to the bottom. If the cenospheres are collected at the thickener effluent, they may be collected as a float in the clarifier.
  • the underflow from the thickener 40 may be applied by a slurry pump 41 to a drum-type filter 44 in which further liquid content is removed and the contents are then preferably applied to a delumper 45.
  • the delumper 45 is a moderate speed mixer which reduces the larger aggregations of the material when it is in a partially dried state from the drum-type filter such as wet sand.
  • This product is then delivered to a linear heated screw-type processor 50 which may also be a HOLO-FLIGHT thermal processor with heated screw vanes and heated walls.
  • the screw vanes re hollow and the vanes and walls may be oil heated, such as by oil at 600° F.
  • the pozzolan product will leave the processor 50 at about 390° F and at a moisture content of less than 0.3%.
  • This enclosed processor releases a water fraction as well as any volatile organic compounds (VOCs) and controls their release for proper disposal.
  • the dried product is delivered at the elevated temperature from the thermal processor 50 to a high speed pin-type mixer 52.
  • the output from the linear processor or dryer 50 is a fine product but may contain aggregations of weakly bonded ash particles which are not capable of passing through a 325 mesh screen.
  • the high speed pin-type mixer 52 breaks down these weak bonds and frees the particles one from the other. This is particularly advantageous since the pozzolan is enhanced by the microspheres from the second flotation step, and these microspheres must be free of bonds to provide the maximum pozzolanic activity.
  • supplemental materials may be added such as an alkaline clay as described in the previously referenced U.S. patent no. 5,484,480 and/or lime to produce the final product and stored in a receptacle or container 55.
  • the reagents which are added to effectuate the frothing and collecting functions preferably consist of a combined frother and collector, although these elements may be separately added.
  • the frother/collector reagent may consist of the non-aromatic reagent S-8259 of Cytec Industries Inc., Five Garret Mountain Plaza, West Paterson. New Jersey 07424, comprising a emulsion of a hydrotreated light petroleum distillate, CAS registration number 064742-478 and a sulfonic acid, petroleum, sodium salt, CAS registration number 68608-26-4, which will further include a suitable frothing agent such as "Aerofroth" 88, CAS registration number 104-76-7 or frother S-7904, provided by Cytec Industries Inc., identified above.
  • collectors may be used are described in Australian Patent 572344 granted September 29, 1988 and include a suitable oil such as crystal free neutral oil or fuel or, an acid or an acid ester, as described in the examples, and a sulfonated hydrocarbon compound, as described in the examples.
  • this non-aeromatic reagent S-8259 is preferred for VOC control.
  • the reagent dosage may be about 2 to 3 lbs. per ton in the primary floatation which includes about 2 lbs. of frother such as S-7904 or aerofroth 88 and about ⁇ to 1 lb. of collector.
  • the amount of reagents may be decreased to about 1 to 1 14 lbs. per ton including about l ⁇ lb. per ton of frother and about Vi to 1 lb. per ton of collector.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Ceramic Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Civil Engineering (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention porte sur un procédé de fabrication d'un ciment pouzzolanique amélioré, à partir de cendres volantes ayant une importante teneur en carbone. Ce procédé consiste à tamiser (11) la cendre volante brute et à utiliser des agents de conditionnement, appliquer la cendre sur un premier ensemble de cuves de flottation (15) de façon à retirer une fraction riche en carbone et une fraction sans carbone, soumettre la fraction riche en carbone à broyeur par frottement (20) de façon à fractionner les particules de carbone et libérer des microsphères piégées dans les vésicules de carbone, appliquer la fraction riche en carbone broyée sur un second banc de cellules de flottation (22) et séparer une seconde fraction riche en carbone contenant des particules de carbone fractionnées et des particules de carbone dont la taille a été réduite, et une seconde fraction sans carbone contenant principalement des microsphères de cendres volantes, combiner les fractions sans carbone et les sécher dans un séchoir du type séchoir à hélice chauffé (30) et briser toute agglomération de particules formant un ciment pouzzolanique réactif de cendres volantes qui contient une partie appréciable de particules fines comprenant des microsphères.
PCT/US1997/022010 1996-12-04 1997-12-03 Preparation de cendres volantes selon un procede par voie humide Ceased WO1998024733A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU55143/98A AU5514398A (en) 1996-12-04 1997-12-03 Wet process fly ash beneficiation

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US76004696A 1996-12-04 1996-12-04
US08/760,046 1996-12-04

Publications (1)

Publication Number Publication Date
WO1998024733A1 true WO1998024733A1 (fr) 1998-06-11

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6630022B2 (en) * 1999-05-12 2003-10-07 Granite Rock Company Mechanical activation of granitic powders
WO2005110945A1 (fr) * 2004-05-13 2005-11-24 Procedo Enterprises Etablissement Systeme de traitement de matieres cementeuses composites a faibles emissions de dioxyde de carbone
US7975940B2 (en) 2009-03-31 2011-07-12 Staker & Parson Companies Systems and methods for reducing the particle size of a pozzolan
US8152080B2 (en) 2009-03-31 2012-04-10 Staker & Parson Companies Systems and methods for reducing the particle size of a pozzolan
KR101166276B1 (ko) 2004-05-13 2012-07-17 프로세도 엔터프라이스 에스따블리스망 이산화탄소 배출이 감소된 복합 시멘트 물질 제조용 공정시스템
WO2013057471A1 (fr) * 2011-10-20 2013-04-25 Rocktron Mineral Services Ltd Valorisation des cendres volantes
US8496750B2 (en) * 2009-03-31 2013-07-30 Staker & Parson Companies Method for reducing the particle size of a pozzolan
CN110252246A (zh) * 2019-07-01 2019-09-20 河南城建学院 一种粉煤灰空心微珠为模板乙酸钾盐基多孔碳吸附材料及其制备方法和应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3328180A (en) * 1964-06-24 1967-06-27 Mcdowell Wellman Eng Co Method of making light-weight aggregate from fly ash
US4121945A (en) * 1976-04-16 1978-10-24 Amax Resource Recovery Systems, Inc. Fly ash benificiation process
US4426282A (en) * 1981-02-16 1984-01-17 Kryolitselskabet Oresund A/S Process for the separation of coal particles from fly ash by flotation
US4652433A (en) * 1986-01-29 1987-03-24 Florida Progress Corporation Method for the recovery of minerals and production of by-products from coal ash

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3328180A (en) * 1964-06-24 1967-06-27 Mcdowell Wellman Eng Co Method of making light-weight aggregate from fly ash
US4121945A (en) * 1976-04-16 1978-10-24 Amax Resource Recovery Systems, Inc. Fly ash benificiation process
US4426282A (en) * 1981-02-16 1984-01-17 Kryolitselskabet Oresund A/S Process for the separation of coal particles from fly ash by flotation
US4652433A (en) * 1986-01-29 1987-03-24 Florida Progress Corporation Method for the recovery of minerals and production of by-products from coal ash

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6630022B2 (en) * 1999-05-12 2003-10-07 Granite Rock Company Mechanical activation of granitic powders
WO2005110945A1 (fr) * 2004-05-13 2005-11-24 Procedo Enterprises Etablissement Systeme de traitement de matieres cementeuses composites a faibles emissions de dioxyde de carbone
AU2005243810B2 (en) * 2004-05-13 2009-03-12 Procedo Enterprises Etablissement Processing system for manufacturing of composite cementitious materials with reduced carbon dioxide emissions
RU2370474C2 (ru) * 2004-05-13 2009-10-20 Проседо Энтерпрайзес Этаблиссман Технологическая установка для производства композитных цементирующих материалов с уменьшенным выделением двуокиси углерода
KR101166276B1 (ko) 2004-05-13 2012-07-17 프로세도 엔터프라이스 에스따블리스망 이산화탄소 배출이 감소된 복합 시멘트 물질 제조용 공정시스템
US7975940B2 (en) 2009-03-31 2011-07-12 Staker & Parson Companies Systems and methods for reducing the particle size of a pozzolan
US8152080B2 (en) 2009-03-31 2012-04-10 Staker & Parson Companies Systems and methods for reducing the particle size of a pozzolan
US8496750B2 (en) * 2009-03-31 2013-07-30 Staker & Parson Companies Method for reducing the particle size of a pozzolan
WO2013057471A1 (fr) * 2011-10-20 2013-04-25 Rocktron Mineral Services Ltd Valorisation des cendres volantes
CN110252246A (zh) * 2019-07-01 2019-09-20 河南城建学院 一种粉煤灰空心微珠为模板乙酸钾盐基多孔碳吸附材料及其制备方法和应用

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Publication number Publication date
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