WO1995016518A1 - Milieu de filtration ameliore comportant des niveaux eleves de permanganate et d'eau - Google Patents

Milieu de filtration ameliore comportant des niveaux eleves de permanganate et d'eau Download PDF

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Publication number
WO1995016518A1
WO1995016518A1 PCT/US1994/014316 US9414316W WO9516518A1 WO 1995016518 A1 WO1995016518 A1 WO 1995016518A1 US 9414316 W US9414316 W US 9414316W WO 9516518 A1 WO9516518 A1 WO 9516518A1
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Prior art keywords
permanganate
composition
media
approximately
water
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PCT/US1994/014316
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English (en)
Inventor
William G. England
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Purafil, Inc.
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Publication date
Application filed by Purafil, Inc. filed Critical Purafil, Inc.
Priority to CA002207689A priority Critical patent/CA2207689C/fr
Priority to AU14345/95A priority patent/AU1434595A/en
Publication of WO1995016518A1 publication Critical patent/WO1995016518A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
    • B01J20/0222—Compounds of Mn, Re
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B01J20/043—Carbonates or bicarbonates, e.g. limestone, dolomite, aragonite
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/06—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04
    • B01J20/08—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04 comprising aluminium oxide or hydroxide; comprising bauxite
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/3021—Milling, crushing or grinding
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
    • B01J20/3202—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the carrier, support or substrate used for impregnation or coating
    • B01J20/3204—Inorganic carriers, supports or substrates
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
    • B01J20/3231—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the coating or impregnating layer
    • B01J20/3234—Inorganic material layers
    • B01J20/3236—Inorganic material layers containing metal, other than zeolites, e.g. oxides, hydroxides, sulphides or salts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/11—Clays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • 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
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
    • B01J2220/56—Use in the form of a bed
    • 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
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
    • B01J2220/64—In a syringe, pipette, e.g. tip or in a tube, e.g. test-tube or u-shape tube

Definitions

  • the present invention relates generally to an improved composition and method for the removal of compounds having toxic or corrosive properties or disagreeable odors, especially sulfur containing compounds, from gaseous streams.
  • the invention more particularly relates to the use in filter beds of an improved solid filtration media comprising a substrate impregnated with elevated levels of potassium permanganate and water.
  • the media may also be impregnated with sodium bicarbonate.
  • the media is improved in that it has a substantially higher capacity for the removal of the above compounds from gas streams than the media of the prior art. Further, the media contains significantly higher levels of potassium permanganate and water than thought to be efficacious in the prior art.
  • Undesirable airborne compounds including sulfur compounds, ammonia, formaldehyde, urea, carbon monoxide, oxides of nitrogen, mercaptans, amines, and ethylene, occur in a number of environments, where most are primarily responsible for the presence of disagreeable odors, or irritating or toxic gases.
  • environments include petroleum treatment and storage areas, sewage treatment facilities, hospitals, morgues, anatomy laboratories, animal rooms, and pulp and paper production sites, among others.
  • These undesirable compounds may be bacterial breakdown products of higher organic compounds, or byproducts of industrial processes.
  • Hydrogen sulfide a colorless, toxic gas with a characteristic odor of rotten eggs, is produced in coal pits, gas wells, sulfur springs, and from decaying organic matter containing sulfur. Controlling emissions of this gas, particularly from municipal sewage treatment plants, has long been considered desirable. More recently, protecting electronic apparatus from the corrosive fumes of these compounds has become increasingly important. Further, H2S is flammable.
  • Ammonia also a colorless gas, possesses a distinctive, pungent odor and is a corrosive, alkaline gas. The gas is produced in animal rooms and nurseries and its control also has long been considered desirable.
  • Chlorine is a greenish-yellow gas with a suffocating odor.
  • the compound is used for bleaching fabrics, purifying water, treating iron, and other uses. Control of this powerful irritant is most desirable for the well-being of those who work with it or are otherwise exposed to it.
  • chlorine has a corrosive effect on electronic circuitry, stainless steel and the like.
  • Formaldehyde (“HCHO”) is a colorless gas with a pungent suffocating odor. It is present in morgues and anatomy laboratories, and because it is intensely irritating to mucous membranes, its control is desirable.
  • Carbon monoxide (“CO"), an odorless, colorless, toxic gas, is present in compressed breathing air. Oxygenation requirements for certain atmospheres, including those inhabited by humans, mandate its control. Oxides of nitrogen, including nitrogen dioxide (“N02”), nitric oxide (“NO”), and nitrous oxide (“N2O”), are compounds with differing characteristics and levels of danger to humans, with nitrous oxide being the least irritating oxide. Nitrogen dioxide, however, is a deadly poison. Control of pollution resulting from any of these oxides is desirable or necessary, depending on the oxide.
  • Mercaptans and amines including methyl mercaptan (“CH3SH”), butyl mercaptan (“C4H9SH”) and methyl amine (“CH5N”), are undesirable gases present in sewerage odor. The control of these gases is desired for odor control.
  • CH3SH methyl mercaptan
  • C4H9SH butyl mercaptan
  • CH5N methyl amine
  • Ethylene (“C2H4") is a colorless, flammable gas that is a simple asphyxiant which accelerates the maturation or decomposition of fruits, vegetables, and flowers. Control of this -compound prolongs the marketable life of such items.
  • the following approximate formulation is an example of a solid filtration media produced by the current state of the art: 69% activated alumina, 10% water, 4.5% potassium permanganate, and 17% sodium bicarbonate.
  • the above solid filtration media is widely known in the art to have approximately a 9% capacity for the uptake of hydrogen sulfide gas in a gas stream.
  • One specific example of a solid filtration media for the removal of undesirable compounds from gas streams is described in U.S. Patent No. 4,235,750.
  • the '750 patent discloses an apparatus and method for adsorbing ethylene and other gaseous contaminants, wherein the apparatus is a three-part container comprising permanganate impregnated alumina in one compartment, activated carbon in the second compartment, and a mixture of molecular sieves and activated silica gel in the third compartment.
  • the '750 patent discloses that the concentration of the aqueous potassium permanganate solution used to impregnate the alumina should be limited to one pound of permanganate dissolved in one gallon of water since if more is dissolved, the pores of the alumina will be clogged, therefore reducing its oxidizing capacity.
  • the potassium permanganate and water solution is applied to the substrate so that the dried, finished product contains about 4 to 5%, preferably 4.5% of potassium permanganate by weight of the finished product.
  • water is simply a diluent which will eventually be evaporated, and therefore, is not meaningful except as a vehicle for application of the potassium permanganate to the basic alumina substrate.
  • the product is deemed finished after a substantial portion of the free water has been evaporated.
  • the alumina is dried to remove 99% of the free water after the aqueous potassium permanganate solution has been applied to the alumina.
  • the '750 patent discloses a potassium permanganate impregnated alumina for the removal of undesirable compounds from fluid streams, the capacity of the impregnated alumina is limited.
  • the efficiency of the permanganate impregnated alumina of the '750 patent is limited as its optimal concentration of permanganate is 4.5%, and higher concentrations of permanganate results in the clogging of the pores of the substrate and therefore its oxidizing capacity being reduced. Accordingly, this filtration media would be limited to approximately a 9% capacity for the uptake of hydrogen sulfide gas in a gas stream. Therefore, this filtration media could not be efficiently used in small filter beds as larger quantities of the impregnated alumina must be used to compensate for its limited capacity.
  • the use of the impregnated alumina of the '750 patent would be more costly as the media would have to be replaced more frequently, thereby incurring the cost of more frequently purchasing the media and also incurring the cost of the additional labor required for its more frequent replacement.
  • the permanganate impregnated alumina of the '750 patent is limited in that the failures in the adsorption of contaminants in fluid streams which occur at the end of the useful life of the media would be more frequent due to the limited capacity of the media. Therefore, the media of the '750 patent could not practically be utilized in systems where the air quality is critical.
  • the substrate must be hydrophilic and the reaction must take place in normal ambient humidity.
  • the '399 patent teaches that the amount of water necessary to cause the oxidation reaction is supplied by a normal ambient humidity. There is no teaching or suggestion in the. '399 patent to elevate the amount of free water in the pellet. Further, there is no teaching or suggestion in the '399 patent to elevate the concentration of permanganate in the pellet above that obtained with the 5% aqueous solution of permanganate.
  • the potassium permanganate impregnated alumina pellets of the '399 patent are limited in that they have a limited capacity for removing undesired contaminants from gas streams.
  • the adsorbent was impregnated with a 5% aqueous solution of the permanganate and subsequently dried.
  • No particular concentration range of potassium permanganate or water is disclosed for the pellets of the '399 patent.
  • the potassium permanganate impregnated alumina of the '399 patent appears to have the same limitations as the potassium permanganate impregnated alumina of the '750 patent as discussed above.
  • U.S. Patent No. 3,226,332 teaches a method of producing granular activated alumina uniformly impregnated with a solid oxidizing agent, preferably potassium permanganate, for use in treating fluid streams.
  • This method includes the spray addition of the impregnate, wherein the impregnate solution is sprayed onto the dry combination being tumbled in a mixer thereby forming pellets which are later dried to remove a substantial portion of the remaining water.
  • the preferred impregnated concentration of potassium permanganate is 2.5%, by dry weight.
  • the '332 patent discloses a range of 0.5 to 10% of potassium permanganate, from about 2% to about 4% of potassium permanganate being preferred.
  • the '332 patent also discloses that the pellets are dried to remove at least a substantial portion of the uncombined (free) water.
  • the permanganate impregnated alumina of the '332 patent may contain approximately 0.5 to 10% potassium permanganate, the preferred range of potassium permanganate remains at from about 2% to about 4%. Accordingly, if the concentration of the potassium permanganate in the solid substrate is above 4%, it does not appear that the patentee expects any significant improvement over its capacity at a concentration of 4%. Also, the '332 patent does not teach elevating the amount of water remaining in the substrate. Further, there is no teaching in the '332 patent of how to avoid clogging of the pores of the substrate as expected from the high concentration of potassium permanganate.
  • the potassium impregnated alumina as taught in the '332 patent would be expected by one skilled in the art to be limited in its capacity for the removal of undesirable compounds from fluid streams, and therefor has the same shortcomings as the potassium impregnated alumina of the '750 patent as discussed above.
  • the adso ⁇ tivity of permanganate impregnated alumina is maximized when the concentration of the potassium permanganate impregnated in the alumina is approximately 4-5%. It is further taught that at concentrations above 5%, the potassium permanganate crystallizes and plugs the pores in the media, and therefore does not increase and may even decrease the adso ⁇ tivity of the media.
  • the present invention relates to an improved solid filtration media, method of preparing the same, and method of treating a fluid stream with the solid filtration media.
  • the improved solid filtration media comprises permanganate, water, and a substrate, such as activated alumina. Sodium bicarbonate may also be added.
  • the free water content is minimized, and the potassium permanganate concentration is maintained at approximately 4 to 5% to avoid pore-clogging problems.
  • the media of the present invention contains significantly higher levels of permanganate and water.
  • An improved efficiency of removal of compounds such as hydrogen sulfide is achieved by this media.
  • the improved media of the present invention has a hydrogen sulfide capacity of greater than approximately 15%, whereas the media produced by the current art has a maximum hydrogen sulfide capacity of approximately 9- 10%.
  • the present invention addresses an existing need in the prior art by providing a high efficiency, high capacity, low flammability permanganate impregnated substrate for the removal of undesirable contaminants from gas streams.
  • the present invention therefore provides a long lasting filtration media which needs to be replaced less frequently and therefore minimizes maintenance and replacement costs.
  • a high capacity filtration media which may be used in small filter beds, and therefore may allow the treatment of fluid streams where there are significant space limitations.
  • the present invention further provides methods of making and using the filtration media.
  • the filtration media of the present invention has a higher efficiency and capacity to remove certain undesired compounds from gaseous streams than do the media in the prior art.
  • the improved media of the present invention yields an equivalent capacity as activated carbon adsorbents.
  • the filtration media of the present invention is much less expensive, and is considerably less flammable than activated carbon adsorbents.
  • the present invention provides an filtration media comprising at least approximately 5% permanganate salt, at least 10% water, and a porous substrate, wherein these percentages are by weight of the composition.
  • the permanganate salt is potassium permanganate.
  • the porous substrate is selected from the group consisting of activated alumina, silica gel, zeolite, adsorbent clay, kaolin, and activated bauxite, the preferred porous substrate being alumina.
  • the improved solid filtration media of the present invention comprises between approximately 5 and 12% permanganate salt, between approximately 10 and 35% water, and a porous substrate, wherein the above percentages are by weight of the composition.
  • the composition further comprises sodium bicarbonate, wherein the sodium bicarbonate is between approximately 0 to 30%, and preferably is between 15 to 20% by weight.
  • the sodium bicarbonate enhances the retention of water in the solid filtration media.
  • the present invention also provides a method of preparing an improved filtration media composition.
  • This method comprises the steps of mixing water, a permanganate salt, and a substrate, and then forming the mixture into at least one cohesive porous unit.
  • the unit is then cured at a temperature of from about 100°F to about 200°F, until the concentration of water is at least about 10% by weight of the composition, and the concentration of the permanganate salt is at least about 5% by weight of the composition.
  • the method of the present invention comprises forming an aqueous solution comprising the permanganate salt and then mixing the aqueous solution with the porous substrate.
  • the method of the present invention comprises forming a dry mixture comprising the permanganate salt and the substrate, and then adding water to the dry mixture.
  • the method of the present invention comprises forming a dry mixture comprising the permanganate salt and the substrate, forming an aqueous solution comprising the permanganate salt, and then mixing the aqueous solution with the dry mixture.
  • sodium bicarbonate may be added either to the dry mixture, to the water, or to both in the method of preparing the filtration media.
  • the unit formed is cured until the concentration of water is from about 10 to about 30% by weight of the composition, and the concentration of the permanganate salt is from about 5 to about 12% by weight of the composition.
  • the unit formed is cured until the concentration of sodium bicarbonate is between 15 to 20% by weight.
  • Yet another aspect of the present invention is a method of treating a contaminated fluid stream with the improved solid filtration composition of the present invention. This method comprises contacting the contaminated fluid stream with the improved solid filtration composition.
  • the improved filtration media embodying the present invention, the method of its preparation, and the method of its use provide improved efficiency and capacity in removing contaminants from gas streams.
  • an object of the present invention to provide an improved solid filtration media for removing undesirable compounds from an air stream. It is another object of the present invention to provide a solid filtration media having a high efficiency in removing unwanted compounds from an air stream flowing over or through the media. It is yet another object of the present invention to provide a solid filtration media having a high ignition temperature, and therefore, limited flammability.
  • Fig. 1 is a graph representing the efficiency of removal of hydrogen sulfide by media comprising either 4.4% or 8.4% potassium permanganate, as described more fully in Example 7.
  • the present invention relates to an improved solid filtration media, method of preparing the same, and method of treating a fluid stream with the solid filtration media.
  • the improved solid filtration media comprises permanganate, water, and a substrate, such as activated alumina. Sodium bicarbonate may also be added.
  • the media contains significantly higher levels of permanganate and water than thought possible in the prior art.
  • An improved efficiency of removal of compounds is achieved by this media.
  • a preferred embodiment of this improved media has a hydrogen sulfide capacity of greater than approximately 15%, whereas the media produced by the current art has a maximum hydrogen sulfide capacity of approximately 9- 10%.
  • the present invention provides an improved filtration media comprising a substrate impregnated with high levels of both permanganate, and water.
  • the filtration media comprises at least approximately 5% permanganate salt, and at least 10% water, by weight of the composition.
  • the permanganate salt may be selected from the group consisting of, but not limited to, potassium permanganate ("KMn ⁇ 4"), sodium permanganate, magnesium permanganate, calcium permanganate, barium permanganate, and lithium permanganate.
  • the permanganate salt is potassium permanganate (Aldrich, Milwaukee, WL).
  • the concentration of the potassium permanganate is between approximately 5 and 12%, and preferably between 7 and 12%.
  • the porous substrate may be selected from the group consisting of, but not limited to, activated alumina ("AI2O3") (LaRoche Chemical, Baton Rouge, LA.), silica gels (J.M. Huber, Chemical Division, Havre De Grace, MD.), zeolites (Steel Head Specialty Minerals, Spokane, WA.), kaolin (Englehard Co ⁇ ., Edison, N.J.), adsorbent clays (Englehard Co ⁇ ., Edison, N.J.), and activated bauxite.
  • a preferred porous substrate is alumina.
  • the concentration of substrate in the filtration media is between 40 and 80%, and most preferably it is between 60 and 75% where the media does not contain sodium bicarbonate, and it is preferably between.40 and 60% where the media contains sodium bicarbonate.
  • the concentration of water in the filtration media is between approximately 10 and 35%, preferably between 20 and 25%.
  • concentration of free water in the filtration media may be altered by the conditions present, such as the humidity and the temperature, during its storage and use.
  • the improved solid filtration media of the present invention comprises between approximately 5 and 12% potassium permanganate, between approximately 10 and 35% water, and between approximately 40 and 80% alumina, by weight of the composition.
  • the improved solid filtration media comprises between approximately 7 and 12% potassium permanganate, between approximately 20 and 25% water, and between approximately 60 and 75% alumina, by weight.
  • the composition further comprises sodium bicarbonate ("NaHC ⁇ 3”) (Rhone-Poulenc, Chicago Heights, IL.), wherein the concentration of sodium bicarbonate is between approximately 0 to 30%, and preferably is between 15 to 20%, by weight.
  • the sodium bicarbonate enhances the retention of water in the filtration media.
  • the preferred concentration of alumina is between approximately 40 and 60%. It is to be understood that when referring to the relative weight of components, the water referred to in the present specification, examples, and tables is defined as the free water, and does not include the bound water in the substrate.
  • filtration media such as filtration media, adsorbent composition, and impregnated substrate are all interchangeable, and denote a substance which is capable of reducing or eliminating the presence of unwanted contaminants in fluid streams by the contact of such a substance with the fluid stream.
  • fluid is defined as a liquid or gas capable of flowing, and includes gaseous, aqueous, organic containing, and inorganic containing fluids.
  • the present invention also provides a method of preparing an improved solid filtration composition.
  • This method comprises the steps of mixing water, a permanganate salt, and a substrate, and then forming the mixture into at least one cohesive porous unit.
  • the unit is then cured at a temperature of from about 100 ⁇ F to about 200°F, until the concentration of water is at least about 10% by weight of the composition, and the concentration of the permanganate salt is at least about 5% by weight of the composition.
  • the size and shape of the cohesive porous unit is not critical to the present invention. Any size and shape of a porous unit known in the art to reduce or eliminate undesirable contaminants from fluid streams when in contact with the unit may be used in the present invention.
  • the porous unit is a nominal 1/8" diameter round pellet.
  • the method of the present invention preferably comprises forming an aqueous solution comprising the permanganate salt and then mixing the aqueous solution with the porous substrate.
  • the aqueous solution should be heated to approximately 160° to 200°F, and preferably to between approximately 180° to 190°F.
  • the method of the present invention comprises forming a dry mixture comprising the permanganate salt and the substrate, and then adding water to the dry mixture.
  • the method of the present invention comprises forming a dry mixture comprising the permanganate salt and the substrate, forming an aqueous solution comprising the permanganate salt, and then mixing the aqueous solution with the dry mixture.
  • sodium bicarbonate may be added either to the dry mixture, to the water, or to both in the above methods of preparing the filtration media.
  • the unit formed is cured until the concentration of water is from about 10 to about 30%, and most preferably between 20 and 25%, by weight of the composition, and the concentration of the permanganate salt is from about 5 to about 12% by weight of the composition, and most preferably between 7 and 12%.
  • the unit formed is preferably cured until the concentration of sodium bicarbonate is less than approximately 30%, and preferably between 15 to 20% by weight.
  • the media may be cured at approximately 130° to 140°F.
  • the presence of sodium bicarbonate allows for a lower curing temperature such as 130° to 140°F, in contrast to the prior art curing temperature of about 200°F.
  • the impregnation treatment of the activated starting material in accordance with the present invention has not been found to be critical with respect to the particular sequence in which the dry mix is impregnated with moisture and impregnates.
  • the above combinations may be mixed in any manner which effectively produces the desired filtration media. Impregnation may be carried out simply by immersing and soaking the solid combination in a volume of impregnate solution. Also, the impregnate solution may be passed through the combination rather than being used as a static immersion treatment.
  • a preferred method of impregnation is spray addition in which an impregnate solution is sprayed onto a dry combination being tumbled in a mixer. This method of impregnation has been described in U.S. Patent No. 3,226,332, which is herein inco ⁇ orated by reference. Other methods of impregnating the combinations would suggest themselves as equally appropriate, and these are included within the scope of the present invention.
  • the aqueous impregnate solution of potassium permanganate is sprayed onto a dry combination of sodium bicarbonate and a substrate, such as activated alumina.
  • a dry combination would contain between approximately 80 to 85% activated alumina, and between approximately 15 to 20% of sodium bicarbonate.
  • the concentration of the potassium permanganate may vary in the solution to be sprayed onto the dry combination.
  • an aqueous solution containing approximately 20% of potassium permanganate, at between approximately 160°F to 200 ⁇ F, and preferably at between 180° to 190°F should be sprayed on the dry combination being tumbled in a mixer.
  • a solution of approximately 25% potassium permanganate at between approximately 160°F to 200°F, and preferably at about 180°F to 190°F should be sprayed on the dry combination being tumbled in a mixer.
  • any concentration of permanganate in the aqueous solution which is effective to yield the composition of the present invention may be used.
  • the permanganate salt is either in the dry feed mixture or in both the aqueous solution and the dry feed mixture
  • any concentration of permanganate in the dry mixture and/or the aqueous solution which is effective to produce the composition of the present invention may be used.
  • the media may be used to fill perforated modules to be inserted into air ducts in a manner known in the art.
  • Yet another aspect of the present invention is a method of treating a contaminated fluid stream with the improved solid filtration composition of the present invention.
  • This method comprises contacting the contaminated fluid stream with the above improved solid filtration compositions.
  • Methods of treating gaseous or other fluid streams are well known in the art.
  • any method known in the art of treating fluid streams with the media of the present invention may be used.
  • the composition of the present invention is employed to remove undesired compounds from gas streams.
  • the concentration of these undesirable compounds in the gas streams is not considered critical to the process of the present invention, nor is the physical and chemical makeup of the gas stream from which it is desired to remove undesirable compositions considered critical.
  • the undesired compositions will be removed from air, especially from air admixed with effluent gas streams resulting from municipal waste treatment facilities, paper mills, petrochemical refining plants, morgues, hospitals, anatomy laboratories, and hotel facilities, and so forth.
  • the oxidizing conditions which may be important are generally that oxygen preferably be present in the gas stream being treated, at least in small amounts. This oxygen content is readily found in the gas stream, if air comprises a sufficient portion of the gas stream being treated. If oxygen is totally absent or present in insufficient amounts, oxygen may be independently introduced into the gas stream being treated. A number of factors affect the amount of oxygen which may be required for maximum removal of the contaminants in a gas stream in accordance with the present invention, including the concentration and absolute amount of compounds being removed from the gas stream being treated.
  • the process With respect to the amount of compound removed, it is believed that the following factors affect the process: the basic degree of attraction of the activated substrate for the compound; the pore structure and size of the substrate; the specific surface area of the substrate; the surface characteristics of the substrate; the amount of permanganate present; and the amount of water present.
  • the filtration media of the present invention is appropriately used alone in filter beds for the removal of undesirable compounds. It is also appropriate, however, to use the composition of the present invention in conjunction with filter beds containing other filtration media, and also in conjunction with mechanical or electrostatic filters. Any such additional filters may be placed either upstream (before the media of the present invention with respect to the effluent gas being treated) or downstream.
  • the above invention significantly increases the efficiency and capacity of impregnated porous substrates (filtration media) to remove certain undesired compounds from gaseous streams over the capacity of impregnated porous substrates of the prior art. Therefore, the lifetime of a specific quantity of the improved filtration media will be much longer than the same quantity of the currently available filtration media.
  • the extension of the lifetime of the filtration products will significantly reduce consumers' and businesses' purchasing, servicing, and installation costs. Also, the enhanced efficiency of the improved media allows for a new line of products which are compact versions of currently available units, but have the same performance as the larger, currently available units. The capability of creating significantly smaller filtration units is useful for providing efficacious air filtration in space-limited quarters which previously could not utilize the larger, currently available units.
  • the improved permanganate media is less expensive than other filtration media having a roughly equivalent capacity.
  • the media of the present invention has an — equivalent capacity as activated carbon adsorbents.
  • the media of the present invention is considerably less expensive than activated carbon adsorbents.
  • the filtration media of the present invention is safe as it is not flammable, in contrast to carbon containing filtration products.
  • This aspect of the present invention is significant to industries which manufacture or process flammable, fume producing materials, such as the petroleum industry for example.
  • the increase in the concentration of the potassium permanganate and water in the solid filtration media has greatly increased the media's capacity for removing contaminants from air streams.
  • the potassium permanganate impregnated alumina media of the prior art has a capacity for the removal of hydrogen sulfide of approximately 9-10%.
  • a composition of the present invention containing approximately 53% activated alumina, 23% water, 7% potassium permanganate, and 17% sodium bicarbonate has a hydrogen sulfide capacity of approximately 15 to 17%.
  • a prior art media which contained approximately 3.5-4.0% potassium permanganate, and 10-15% water, had a hydrogen sulfide capacity of approximately 7.5%.
  • the solid filtration media of the present invention which contained approximately 7% potassium permanganate, and 15-20% water, had a hydrogen sulfide capacity of 15.9%.
  • the efficacy tests were performed by challenging a known quantity of the selected solid filtration media with 1.0% hydrogen sulfide gas at a constant flow rate and monitoring the concentration of hydrogen sulfide in the gas stream exiting the solid filtration media. The accelerated efficacy test is fully described in Example 4.
  • Example 8 The results of a non-accelerated test for the determination of performance characteristics such as removal efficiency and capacity for removal of various gas-phase air filtration media are discussed in Example 8, and are graphically illustrated in Figure 1.
  • the efficiency tests were performed on a solid filtration media of the prior art, and on a solid filtration media of the present invention.
  • the media of the prior art comprised 4.4% potassium permanganate, 19.9% water, 17% sodium bicarbonate, and 58.7 % alumina.
  • the media of the present invention comprised 8.4% potassium permanganate, 24.4% water, 17% sodium bicarbonate, and 50.2% alumina.
  • Fig. 1 illustrates the efficiency of hydrogen sulfide removal of each of the media over an extended period of time. As can be seen from Fig.
  • the media of the present invention has a percent efficiency of hydrogen sulfide removal of 96% at 260 hours, 78% at 456 hours, and 54% at 600 hours.
  • the media of the prior art has a hydrogen sulfide removal efficiency of approximately 92% at 260 hours, 42% at 456 hours, and 15% at 600 hours.
  • the method of the efficiency test is fully described in Example 7.
  • the oxidative capability of the surface of the media is regenerated by the flow or migration of permanganate from the center of the media to the surface of the media while the products of the oxidation reactions flow or migrate from the surface of the media to the center of the media. It is also believed that the higher the concentration of permanganate at the surface of the media, the higher the capacity and efficiency of the media. Further, the fluidity of the permanganate solution directly affects the flow and thus the quantity of the permanganate reaching the surface of the media. Therefore, it is critical to maintain an elevated concentration of free water in the media so that the permangante solution maintains a high level of fluidity and readily flows to the surface of the media thereby maximizing the efficiency and capacity of the media. A liquid path thus should be established between the interior of the pores and the surface of the media. This is contrary to prior art theory which teaches a need for penetration of the gaseous contaminants into the pores of the substrate.
  • the high concentration of permanganate and the low concentration of water causes the permanganate to crystallize and clog the pores of the substrate thereby blocking the flow of permanganate to the surface of the media.
  • the crystallized permanganate remains in the center of the media and therefore cannot move to the surface of the media to oxidize contaminants.
  • the following examples will serve better to illustrate the composition, the treatment methods of the present invention, and the capacity for the removal of contaminants in gas streams produced thereby. It should be noted that the continuous flow systems described in several of the following examples all were operated at a relative humidity of 40-50%.
  • a 7% potassium permanganate impregnated alumina composition is prepared as follows: A dried feed mix is prepared by combining, by weight, 80 to 85% alumina, and 15 to 20% sodium bicarbonate. The dry feed mixture is sprayed with a heated aqueous potassium permanganate solution at 180 to 190°F while the dried feed mix is being tumbled in a tumble mill. The resulting pellets are then dried at 130 to HO , until the pellets contain about 20 to 25% free water.
  • the aqueous potassium permanganate solution should preferably contain approximately 20% potassium permanganate by weight. It is to be understood that the aqueous potassium permanganate solution is sprayed on to the dry feed mix while the dry mix is rolled in the pelletizing disk as described in U.S. Patent No. 3,226,332, inco ⁇ orated herein by reference.
  • a 10% potassium permanganate impregnated alumina composition is prepared as follows:
  • a dried feed mix is prepared by combining, by weight, 80 to 85% alumina, and 15 to 20% sodium bicarbonate.
  • the dry feed mixture is sprayed with a heated aqueous potassium permanganate solution at 180 to 190°F while the dried feed mix is being tumbled in a tumble mill.
  • the resulting pellets are then dried at 130 to 140°F in air, until the pellets contain about 20 to 25% free water.
  • the aqueous solution should preferably contain approximately 25% potassium permanganate, by weight. It is to be understood that the aqueous potassium permanganate solution is sprayed on to the dry feed mix while the dry mix is rolled in the pelletizing disk as described in U.S. Patent No. 3,226,332, inco ⁇ orated herein by reference.
  • Example 2 Using the method described in Example 1 or Example 2, the following compositions, by dry weight, may also be prepared: TABLE I: ComDOsition of Solid Filtration Media
  • the dry feed mix is prepared by mixing appropriate amounts of the substrate and the sodium bicarbonate together.
  • the dry feed mix is mixed in a tumbling mill with an appropriate amount of an aqueous potassium permanganate solution sprayed onto the dry feed mix while tumbling, in the manner described in U.S. Patent No. 3,226,332.
  • Curing is as in Example 1 or 2.
  • the cured pellets are a strong, non-dusting filter media suitable for placement in filter beds. They provide an efficient media for the reduction or elimination of many undesirable compounds.
  • Standard Accelerated Test Method for Capacity Determination of Gas-Phase Air Filtration Media The following is an accelerated test method to be used for determining the capacity of removal of various gas-phase air filtration media when subjected to a flowing gas stream containing high levels of contaminant(s). Low-level challenge testing of gas-phase air filtration media, whether full-scale or small-scale, usually takes long periods of time to obtain the desired results. The following method provides an accelerated test for determining the removal capacities of various media by exposing them to high levels of contaminants.
  • a known volume of media is placed in an adso ⁇ tion tube and exposed to a known concentration (usually 1% # vol. /vol.) of contaminant gas(es) in a tempered, humidified, clean air system.
  • the gas stream is calibrated to deliver a total flow rate of 1450 ⁇ 20 ml/min.
  • the removal capacity is calculated as the amount (in grams) of contaminant removed from the air stream per volume (cubic centimeters) of media at a 50 parts per million (“ppm”) breakthrough.
  • the air utilized must be tempered, humidified, clean, oil-free, and compressed. Accordingly, the air must be passed through a bed of activated carbon followed by a filter bed containing potassium permanganate impregnated alumina pellets.
  • Each filter bed should contain at least 300 ml. (18.3 cu. in.) of media for each liter per minute (0.035 cfm.) of air flow.
  • the media in each filter bed should be changed before each test.
  • Media samples are preferably obtained from unopened original manufacturer's shipping or storage containers chosen at random whenever possible. The entire container, whenever possible or practical, should be sampled by taking small amounts of media from throughout the container and combining them into one larger sample. The sample should be thoroughly mixed before being analyzed.
  • Guidance on sampling may be obtained from ASTM Standard E300, entitled Recommended Practice for Sampling Industrial Chemicals. If a test is to be run comparing media of the same size or different sizes, the sample collected may be screened through the appropriate sieves to sort the media by size.
  • an adso ⁇ tion tube which is a cylindrical tube where glass wool and/or beads are optionally placed below the media, and the media and optional glass wool or beads are supported by stainless steel mesh, a perforated slotted glass disc, or a perforated slotted ceramic disc positioned below the media and glass wool or beads.
  • the filled media tube is arranged such that a mixture of air and contaminated gas enters the bottom of the tube, flows through the glass wool or beads, flows through the filtration media, and is then analyzed by a gas analyzer. Leaks in the gas system should be checked for and eliminated before beginning the analysis of the sample. Rotameters, analyzers, recorders, etc. should be calibrated over appropriate ranges according to the manufacturer's instructions or other standard methods such as ASTM Standard D3195, before any media is introduced into the system. Also, air and gas flow requirements should be determined and checked against supply capabilities to assure proper air and gas flows to the system.
  • the adso ⁇ tion tube Once the adso ⁇ tion tube is in position, start the flow of the mixture of contaminated gas and air and record the time, or time the test using a stop watch. Continue the flow of the mixture of gas and air until a breakthrough of 50 ppm is observed or indicated by the gas analyzer. Record the time at breakthrough. It is preferable to use a gas analyzer capable of variable scale readouts to 0 ppm ( ⁇ 5 ppm), having specific or multiple gas capabilities.
  • K 1.52 for H2S, 2.86 for S ⁇ 2, 3.17 for C_2, 2.15 for CH3SH,
  • C Concentration of challenge gas in airstream, Volume %.
  • F Total stream flow rate, cc/min.
  • tb Time to 50 ppm breakthrough, minutes.
  • V Volume of the adso ⁇ tion tube media column, cc.
  • Table II summarizes the content and the capacity of various permanganate containing, solid filtration media.
  • Lot 01083-8 is currently available solid filtration media.
  • Table III summarizes the content and the capacity of solid filtration media produced by several different manufacturers.
  • Cams Chemical manufactured Lot 252 which contains no sodium bicarbonate, approximately 3.5 to 4% KMn ⁇ 4, and about 10 to 15% H2O.
  • Unisorb manufactured Mark II which contains no sodium bicarbonate, approximately 3.5 to 4% KMn ⁇ 4, and about 10 to 15% H2O.
  • the two media manufactured by Purafil are the improved solid filtration media of the present invention.
  • the two Purafil media contain approximately 5.4% KMn ⁇ 4 and 7.0% KMn ⁇ 4, respectively.
  • the following is a method of determining the performance characteristics (removal efficiency and capacity for removal) of various gas-phase air filtration media when subjected to flowing gas streams of known concentrations and velocities.
  • This test provides a basis for comparing the characteristics of different media.
  • the method is briefly summarized as follows: a weighed media sample is placed in a glass tube and exposed to a known concentration of contaminant gas(es) in a tempered, humidified, clean air stream. The inlet and outlet gas concentrations are measured and recorded for use in determining media efficiency and capacity.
  • the tests can be n until a media is exhausted or to a predetermined removal efficiency or percent capacity. All parameters are held constant, and all samples are n simultaneously (in parallel) until the test is completed. Operating parameters may be altered between tests to create simulated field conditions.
  • the air utilized must be tempered, humidified, clean, oil-free, and compressed. Accordingly, the air must be passed through a bed of activated carbon followed by a filter bed containing potassium permanganate impregnated alumina pellets.
  • Each filter bed should contain at least 300 ml. (18.3 cu. in.) of media for each liter per minute (0.035 cfm.) of air flow. The media in each filter bed should be changed before each test.
  • Media samples are preferably obtained from unopened original manufacturer's shipping or storage containers chosen at random if possible. The entire container, whenever possible or practical, should be sampled by taking small amounts of media from throughout the container and combining them into one larger sample. Also, the sample should be thoroughly mixed before being analyzed. Guidance on sampling may be obtained from ASTM Standard E300- entitled Recommended Practice For Sampling Industrial Chemicals. If a test is to be mn comparing media of the same size or different sizes, the sample collected may be screened through the appropriate sieves to sort the media by size.
  • an adso ⁇ tion tube which is a cylindrical tube having glass wool and/or beads optionally placed below the media, and the media and optional glass wool or beads being supported by stainless steel mesh, a perforated slotted glass disc, or a perforated slotted ceramic disc positioned below the media and glass wool or beads.
  • the amount of media placed in the tubes may be determined by filling the tube to the desired level of media while tamping gently to eliminate any dead space, removing the media from the tubes, weighing the media, and finally returning the media to the tube.
  • This alternative method eliminates the need to determine the density of the media as required when filling the tube volumetrically.
  • the filled media tubes are then arranged in parallel such that the gas-air mixture will simultaneously flow through all of the media tubes. Also placed in parallel with the filled media tubes is one empty tube for challenging gas concentration, relative humidity, and temperature monitoring.
  • Leaks in the gas system should be checked for and eliminated before beginning the analysis of the media samples. Also, rotameters, analyzers, recorders, etc. should be calibrated over appropriate ranges according to the manufacturer's instmctions or other standard methods such as ASTM Standard D3195, before any media is introduced into the system. Air and gas flow requirements should be determined and checked against supply capabilities to assure proper air and gas flows to the system.
  • each gas challenge concentration should be set separately before combining the flows and the challenge tube. Interferences, both in the gas stream and on the analyzers, caused by the combining of multiple gases should be determined beforehand.
  • the sample selector of the gas analyzer may optionally be set for sampling at predetermined intervals and durations.
  • the air/gas lines are then connected to the media tubes.
  • Purified and humidified air is then mixed with the predetermined quantity of contaminant gas, and then the mixture passes through the tubes and is then analyzed by a gas analyzer.
  • the filled media tubes are arranged such that the mixture of air and contaminated gas enters the bottom of the tube, flows through the glass wool or beads, flows through the filtration media, and is then analyzed by a gas analyzer.
  • At predetermined sampling intervals record the outlet gas concentrations starting with the first media tube and ending with the challenge tube for each set of readings. Allow the analyzers to equilibrate between each tube and to zero after the challenge tube.
  • n hours since test start (for cumulative weight %) or hours to test completion (for total weight %).
  • Clt challenge gas concentration (in ppm) at time "t.”
  • MW molecular weight of challenge gas.
  • V airflow rate (in ml/min).
  • W media sample weight (in gm).
  • Fig. 1 illustrates the efficiency of hydrogen sulfide removal of each of the media over an extended period of time.
  • the media comprising 8.4% potassium permanganate has a percent efficiency of hydrogen sulfide removal of 96% at 260 hours, 78% at 456 hours, and 54% at 600 hours.
  • the solid filtration media comprising 4.4% potassium permanganate has a hydrogen sulfide removal efficiency of approximately 92% at 260 hours, 42% at 456 hours, and 15% at 600 hours.
  • a dry feed mix is prepared by combining, by weight, 75 to 85% alumina, 7 to 12% finely divided potassium permanganate, and 10 to 20% sodium bicarbonate.
  • the dry feed mixture is sprayed with water while the dried feed mix is being tumbled in a tumble mill.
  • the resulting pellets are then dried at 130° to 140°F, until the pellets contain about 20 to 25% free water. It is to be understood that the dry feed mix is rolled in the pelletizing disc as described in U.S. Patent No. 3,226,332, while it is being sprayed with water.
  • the dry feed mix may contain less potassium permanganate, and the water which is sprayed on the dry feed mix may contain the corresponding amount of potassium permanganate to yield the same final concentration of potassium permanganate as when all of the potassium permanganate is in the dry feed mix.
  • the aqueous potassium permanganate solution preferably is to be heated to approximately 180° to 190°F.

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  • Chemical Kinetics & Catalysis (AREA)
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  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Filtering Materials (AREA)

Abstract

Milieu de filtration amélioré, son procédé de préparation et procédé de traitement d'un courant fluide par ce milieu. Dans l'une de ses variantes, le milieu amélioré comprend un substrat présentant des niveaux élevés de permanganate et d'eau, et plus précisément, il comporte un substrat poreux imprégné d'au moins environ 5 % de permanganate et d'au moins environ 10 % d'eau en poids. Dans une autre variante, il comporte de plus du bicarbonate de soude. On peut ainsi atteindre une plus grande efficacité dans l'élimination des composés indésirables tels que l'hydrogène sulfuré.
PCT/US1994/014316 1993-12-15 1994-12-14 Milieu de filtration ameliore comportant des niveaux eleves de permanganate et d'eau WO1995016518A1 (fr)

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CA002207689A CA2207689C (fr) 1993-12-15 1994-12-14 Milieu de filtration ameliore comportant des niveaux eleves de permanganate et d'eau
AU14345/95A AU1434595A (en) 1993-12-15 1994-12-14 Improved solid filtration media incorporating elevated levels of permanganate and water

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WO2008094480A3 (fr) * 2007-01-26 2008-10-30 Aaf Mcquay Inc Milieux de filtration ayant un réactif chimique

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GB1026904A (en) * 1962-04-13 1966-04-20 Kaiser Aluminium Chem Corp Improvements in or relating to activated alumina products
GB1029688A (en) * 1964-02-20 1966-05-18 American Cyanamid Co Solid oxidant and method for deodorizing air therewith
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JPH02198629A (ja) * 1989-01-25 1990-08-07 Toshiyuki Nakajima 吸着酸化剤
US5278112A (en) * 1992-11-13 1994-01-11 Fred Klatte Chemically impregnated zeolite and method for chemically impregnating and coating zeolite

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GB1026904A (en) * 1962-04-13 1966-04-20 Kaiser Aluminium Chem Corp Improvements in or relating to activated alumina products
GB1029688A (en) * 1964-02-20 1966-05-18 American Cyanamid Co Solid oxidant and method for deodorizing air therewith
US3957059A (en) * 1975-02-10 1976-05-18 Philip Morris Incorporated Smoking product and process
JPS60827A (ja) * 1983-06-20 1985-01-05 Nippon Chem Ind Co Ltd:The 空気浄化剤の製造方法
US4517111A (en) * 1984-01-16 1985-05-14 The Dow Chemical Company Absorbents for airborne formaldehyde
JPH02198629A (ja) * 1989-01-25 1990-08-07 Toshiyuki Nakajima 吸着酸化剤
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Publication number Priority date Publication date Assignee Title
WO2008094480A3 (fr) * 2007-01-26 2008-10-30 Aaf Mcquay Inc Milieux de filtration ayant un réactif chimique
JP2010516392A (ja) * 2007-01-26 2010-05-20 エーエーエフ マックアリー インコーポレイテッド 化学試薬を含むろ過媒体
US7906456B2 (en) 2007-01-26 2011-03-15 Aaf-Mcquay Inc. Filtration media having a chemical reagent
CN101626827B (zh) * 2007-01-26 2013-01-23 Aaf-麦克维尔公司 具有化学试剂的过滤介质
US8546298B2 (en) 2007-01-26 2013-10-01 Aaf-Mcquay Inc. Filtration media having a chemical reagent

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