WO1998003249A1 - Epurateur a filtre catalytique ceramique pour gaz de combustion - Google Patents

Epurateur a filtre catalytique ceramique pour gaz de combustion Download PDF

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Publication number
WO1998003249A1
WO1998003249A1 PCT/DK1997/000315 DK9700315W WO9803249A1 WO 1998003249 A1 WO1998003249 A1 WO 1998003249A1 DK 9700315 W DK9700315 W DK 9700315W WO 9803249 A1 WO9803249 A1 WO 9803249A1
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WO
WIPO (PCT)
Prior art keywords
flue gas
cleaning device
filter
catalyst
gas cleaning
Prior art date
Application number
PCT/DK1997/000315
Other languages
English (en)
Inventor
Vladimir Boscak
Original Assignee
Fls Miljø A/S
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 Fls Miljø A/S filed Critical Fls Miljø A/S
Priority to AU34347/97A priority Critical patent/AU3434797A/en
Publication of WO1998003249A1 publication Critical patent/WO1998003249A1/fr

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Classifications

    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/104—High temperature resistant (ceramic) type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices

Definitions

  • Flue gas cleaning device with catalytic ceramic filter Flue gas cleaning device with catalytic ceramic filter.
  • the present invention relates to a flue gas cleaning device of the type set forth in the introductory part of claim 1.
  • the standards for emissions from municipal, hazardous and clinical waste incineration plants cover several pollutants which can be divided into four categories: particulate mat- ter, acid gases, heavy metals and dioxins.
  • the cleaning of flue gases from waste incinerators is currently practised by the variety of generic and proprietary techniques for remo al of particulate matter and gaseous pollutants.
  • the most common techniques for particulate matter removal are fabric filters and electrostatic precipitators, while the gaseous pollutants are removed in the variety of dry, semi- dry and wet scrubbing techniques or their combination, using calcium or sodium reagents. More recently NO x is controlled by the Selective Non-Catalytic Reduction (SNCR) or the Selective Catalytic Reduction (SCR) .
  • SNCR Selective Non-Catalytic Reduction
  • SCR Selective Catalytic Reduction
  • the ceramic filters also called candle filters, can generally be divided into high and low density types.
  • the high density types are made primarily of the following com- pounds: quartz (Si0) , mullite (3 A1 2 0 3 x 2 Si0) , aluminium oxide (Al 2 0 t ) and silicon carbide (SiC) .
  • the low density types are typically made of alumina silica fibers. While the low density filters have a porosity of up to 90 % , the high density types have typical porosity of 40 %.
  • the low density filters are characterized by low weight and low pressure drop, but show low strength sensitivity toward moisture and corrosion, and are only applicable to medium high temperature.
  • the high density filters which are more relevant to this invention are characterized by high removal efficiency and applicability to high temperature.
  • the pressure drop through ceramic filter is dictated by pore size and filter wall thickness.
  • the relationship be- tween pressure drop and gas velocity changes with length of in-service time.
  • the change in pressure drop between subsequent filtering and cleaning cycles approaches zero as the total number of cycles increases, provided gas velocity remains constant.
  • ceramic filters After about 200 cycles, ceramic filters have been observed to reach an equilibrium. The point of equilibrium depends on process conditions, ceramic composition, particulate matter characteristics, etc.
  • NO in the flue gas can in general be controlled by the following methods:
  • SCR selective catalytic reduction
  • SNCR selective noncatalytic reduction
  • the degree of NO conversion depends on the temperature and amount of ammonia added. With increasing NHJNO,. ratio con- version increases but one should prevent NHj slippage. By using a suitable catalyst more than 90 ?> reduction of NO can be obtained at an NHJNO molar ratio of approximately one within the temperature range of 300-400 °C .
  • the carriers are typically based on the following compounds: titanium oxide, zeolite, iron oxide or activated carbon. Most commercial carriers use vanadium pentoxide as an active compound and titanium dioxide to disperse and support vanadia. They are monolithic in structure with a large number of parallel channels arranged in a honeycomb structure or in parallel plates. Plate types have generally higher resistance to erosion and deposition than honeycombs. The size of the channels depends on the flue gas particulate matter content and its characteristics. The carriers can be tailormade to meet specific requirements regarding thermal stability or low activity towards SO oxidation. The carriers are manufactured m standard elements, which can be assembled in large modules consisting of several elements facilitating the handling and installation of the catalyst carrier m the SCR reactor.
  • a filter medium for treating an exhaust gas has a catalyst layer for eliminating nitrogen oxides formed on the other side of a porous ceramic substrate from which the exhaust gas is discharged.
  • the filter medium may have a double-cylinder construction m which the catalyst layers formed on at least one side of an inner cylinder and the pre-coat layer and the solid material layer are formed on an outer side of an outer cylinder.
  • the object of the present invention is to provide a flue gas cleaning device which, in relation to the closest prior art, allows for an improved NO. removal efficiency relative to the flue gas flow through the filter.
  • Providing the catalyst in the pores inside the porous fil- ter structure allows for a more intimate contact betweeen the flue gas and the catalyst compared to devices where the flue gas flows parallel to a surface provided with a catalyst, and allows for a longer contact time compared to a device where the flue gas penetrates a layer of catalyst. This means that a combined particle and NO, removal unit with increased NO, removal efficiency and smaller dimensions than hitherto known is obtained. A simultaneous removal of dioxin, if present, is also obtained.
  • the porous structure has an essentially tubular shape where the first face extends along the outer circumference of the tube and the second face extends along the inner circumference of the tube.
  • a sup- porting structure e.g. in the form of axially extending ribs, can be provided between opposing parts of the second face .
  • a membrane consisting of ultra fine sintered ceramic powder, e.g. SiC, can be applied onto the filter element surface.
  • the invention further relates to a system for cleaning flue gas wherein at least one duct is provided for leading the flue gas from a combustion chamber to the filter device housing and wherein means for injecting ammonia into said duct are provided.
  • the system may further comprise in said duct means for injecting sorbent or reagent for bringing SO, HCl or HF on a particulate form in order to allow a removal of these par ⁇ ticles on the surface of the porous filter structure.
  • sorbent or reagent for bringing SO, HCl or HF on a particulate form in order to allow a removal of these par ⁇ ticles on the surface of the porous filter structure.
  • the invention still further relates to a method for cleaning flue gas by use of a device which is characterized m that ammonia is injected into the flue gas stream upstream of the device.
  • a sorbent or reagent for converting the flue gas content of SO,, HCl or HF to particulate form is injected into the flue gas stream upstream of the device m order to remove in the device these particles from the flue gas.
  • Acid gases are neutralized by in-duct injection of NaHC0 3 , Ca(OH) or other sodium- or cal- cium-based sorbents.
  • the resulting sodium or calcium salts are removed together with the particulate mat- ter ( fly-ash) m a CCF .
  • the invention also relates to a method of manufacturing a device as set forth above starting with a porous ceramic filter structure having a desired shape and pore size, which method includes
  • Figure 1 schematically shows m section a filter structure according to the invention attached to a supporting structure
  • Figure 2 schematically shows in section an enlarged view of a part of the filter structure of Figure 1
  • Figure 3 schematically shows a system utilizing a device according to the invention.
  • FIG. 1 represents the preferred embodiment of the cata- lytic ceramic filter (CCF) element 1 with a tubular shape and it illustrates one arrangement for holding the said element to the filter housing.
  • Filter element is closed with the flat plate 2 on one side and has a flat flange 3 on the other end which is sealed by ceramic gasket 4 be- tween clamp and spigot plate 5,6.
  • CCF arrangement will be given in the description of Figure 3.
  • two basic types of CCF can be used. If one desires low pressure drop and require- ments for N0 ⁇ removal are not very demanding, a thin wall filter element with internal suppport ribs can be used. If high NO (and dioxms) removal efficiencies are required and higher CCT pressure drops are of secondary importance, a thick wall filter element can be used. A thick wall ele- ment requires no supporting ribs.
  • Figure 2 shows the schematic close-up of CCF wall. This close-up illustrates the use of ultra-fine silicon carbide sintered powder layer 9 (membrane) at the outside face of the wall of the filter element. Its use is optional, while it has the benefit of serving as a barrier for very fine particulate matter it adds to the filter's pressure drop.
  • Figure 2 further shows a mono-molecular layer of SCR catalyst 10 attached to the sintered SiC powder.
  • the preferred formulation of the catalyst is vanadia supported by titania but in principle any SCR catalyst which can be prepared in solution for impregnation of SiC filter structure can be used.
  • SCR catalyst examples include: zeolites, bauxite, alumina, sodium aluminate, iron spinel, hematite, alunite, anataze, dawsonite, spinel, siderite, manganite, melite, gothite, azurite.
  • the flow path for the flue gas is indicated by arrows 11,12.
  • Figure 3 shows the preferred embodiment of the invention in a combustion-energy generating facility.
  • a combustion chamber 13 of a generic type is illustrated which in the case of fossil fuel power plant has either dry or wet bottom furnace with front wall, opposed wall, corner, tangential or other firing while in the case of waste incineration consist of grate furnace, rotary kiln or their combination.
  • Type of fuel fired in the combustion chamber dictates the composition of the flue gas and plays an important role in the selection of reagent for acid gas control in the CCF and its operating temperature.
  • the flue gas generated by combustion of fossil fuel namely coal or heavy oil
  • the flue gas from either municipal, hazardous or clinical waste incineration is characterized by high HCl concentration (in the order of thousands mg/Nm J ) , low to medium NO., concentration (in the order of hundreds of mg/Nm 3 ) , medium S0 2 concentration (low hundreds mg/Nm 3 ) , medium or low particulate matter load, medium or high heavy metals concentration and presence of dioxins in the order of tens ng TEQ/Nm J .
  • the clinical waste incinerators are characterized by very high dioxins content.
  • a boiler 15 is shown and thermal energy is recovered by high pressure 14 and low pressure 16 steam tubes e.g. for generation of electric power in a turbine.
  • flue gases exiting boiler or particulate matter control device with temperature of about
  • 300°C are introduced into reactor 18 or directly into the duct leading into CCF housing 27 comprising the filter 28 constituted by several filter devices 1 according to the invention.
  • the reactor is used in the case of high con- centration of acid gases or in the case where very high re- mova] efficiency is required.
  • the first step in flue gas cleaning is acid gas control. SO and HCl as well as HF are removed from the flue gas by neutralization with a dry alkali.
  • the selection of alkaline reagent is dictated by the concentration of acid gases and desired degree of removal. In the case of low concentration and low removal requirements, the preferred reagent is lime due to its relatively low cost.
  • a combination of the reagents can also be used.
  • HCl and particular HF are much easier removed than SO,.
  • the reactor is used preferentially the case of high SO concentration as is the case for the flue gases from fossil fuel combustion facilities.
  • the role of reactor is to provide intimate contact between reagent and acid gases so it may have some internals to enhance mass transfer.
  • the reagent is stored into silo 20 from where it is injected into reactor via pipe 19.
  • the reagent is transported pneumatically by the use of fan 21.
  • the reagent is injected directly into ductwork leading to CCF.
  • the removal of acid gases also takes place as the gas flows through the cake on CCF elements.
  • the products of acid gases neutralization are calcium or sodium salts which to ⁇ gether with unreacted reagent and fly ash are collected on the ceramic filter. The removal of residue takes place dur ⁇ ing the cleaning cycle.
  • Catalytic ceramic filter housing 27 is typically manufactured from mild steel plate of continuously welded and flanged construction and is designed to accomodate thermal expansion.
  • the catalytic ceramic filter elements are sealed against the spigot plate 5 by a clamping plate 6.
  • a ceramic gasket 4 is fitted between the spigot plate 5 and element flange 3 to ensure a good seal.
  • Each element is supported at the far end by support collars which form part of the filter casing.
  • the pipe 29 for compressed air run vertically down each row of elements passing through the filter case at the top of the filter housing and connecting to the diaphragm valves 24 and compressed air manifolds.
  • support ribs are used in the elements, it is essential that the hole for jet pulse air injection is located precisely above the center of the ele- ment.
  • air is in ⁇ jected via venturi 7 shown in Figure 1.
  • Pulse controller units and solenoid valves 30 enclosure, pre-wired, are also mounted on the filter top plate. The compressed gas is stored into a tank 31 connected to a pipe manifold.
  • Flanged inlets to the filter section are fitted to the top plate which provides "down flow" characteristics within the filter body thus assisting dust release in the hoppers.
  • the complete top section is mounted on a valley type hopper equipped with a rotary valve 32, screw conveyor and dust collection bin discharge arrangement 33.
  • the reaction chamber is designed to give a low velocity on each pass and give arduous route and dwell time for the gas flow, to en- sure a good contact between the reactant and gas.
  • the complete filter and hopper assembly is mounted on a substantial support structure, designed to give 1500 mm clearance under the rotary valve.
  • the new catalytic ceramic filter elements are conditioned during the first reverse pulse cleaning cycles. In this period a layer of dust builds up on the surface of elements resulting in an increase in pressure drop. Pressure drop equilibrium is reached rapidly after these initial cycles and afterwards the conditioned layer of dust provides for superefficient filtration.
  • the ceramic elements can easily handle high face velocities so sudden volume changes present no problem.
  • residue from CCF is not acceptable for deposit it can be treated 38 to meet desired specifications.
  • residue treatment one can employ resource recovery which depends on the reagent used. For example if reagent is calcium based, the resulting very soluble CaCl can be recovered in the evaporator and used as de-icing agent. The prevailing calcium sulfite can be oxidized to the high- grade gypsum for use in wall-board or cement production.
  • resource recovery can also employ recovery of sulfur through calcination and production of elemental sulfur via Claus process, production of sulfuric acid through oxidation of S0 2 to S0 3 and subsequent absorption and production of compressed S0 gas .
  • NO,- is reduced to nitrogen by reaction with ammonia in the presence of catalyst applied into CCF elements.
  • the ammonia stored as a liquid in a tank is first mixed with air in am- monia preparation device 25 and is then introduced into re ⁇ actor or directly into duct in front of CCF via injection nozzles 24 designed for good ammonia distribution.
  • the temperature of CCF is dictated by the composition of flue gases and desired removal efficiency. In the case of flue gas with high S0 2 and specifically SO.-, concentration as is mostly the case with fossil fuel combustion, a CCF temperature above 350°C is desired to prevent formation of solid ammonium disulfate which may plug the ceramic filter. In the case of low S0 3 concentration and low NO removal re- quirements CCF temperature can be below 300°C.
  • the dioxins formed on the fly ash through de-novo synthesis are oxidatively destroyed in the presence of SCR catalyst.
  • con- trol dioxins will also be adsorbed on said active carbon particles .
  • CCF temperature is relatively high, some more volatile heavy metals, namely mercury and cadmium, may be a problem.
  • a suitable sorbent may have to be added to the flue gas in front of CCF.
  • the sorbent stored in a silo 22 can via fan 23 be introduced into the same pipe where reagent is fed to the CCF system.
  • the suitable sorbent is for example active carbon as such or treated with phosphorus or sulfur. Sodium sulfid can also be used in particular if the mercury content is high.
  • the clean gas exiting CCF can be introduced into an optional economizer 34 where the heat can be recuperated by heating the water in the tubes 35.
  • the flue gas is preferentially moved through CCF via an induced draft fan 37 discharging the gas to a stack 36.
  • Binder Material: Urea-formaldehyde TABLE 1: CCF TESTS WITH FLUE GAS

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Biomedical Technology (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Filtering Of Dispersed Particles In Gases (AREA)

Abstract

La présente invention concerne un épurateur (1) pour gaz de combustion comprenant une structure filtrante poreuse. Cette structure, qui est caractérisée par une première face et une seconde face, les pores de la structure poreuse formant des passages pour le gaz de combustion entre la première face et la seconde face, est complétée par un matériau catalytique (10) qui est appliqué sur la surface des passages, et qui permet, en présence d'ammoniac, la réduction catalytique sélective du NOx. Ce principe permet d'accroître l'aptitude à l'élimination du NOx. L'invention concerne également un système d'épuration des gaz de combustion ainsi qu'un procédé d'épuration des gaz de combustion utilisant un tel dispositif pour l'élimination de tous les polluants contenus dans les gaz de combustion. L'invention concerne enfin un procédé de fabrication d'un tel dispositif.
PCT/DK1997/000315 1996-07-22 1997-07-18 Epurateur a filtre catalytique ceramique pour gaz de combustion WO1998003249A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU34347/97A AU3434797A (en) 1996-07-22 1997-07-18 Flue gas cleaning device with catalytic ceramic filter

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DK80496 1996-07-22
DK0804/96 1996-07-22

Publications (1)

Publication Number Publication Date
WO1998003249A1 true WO1998003249A1 (fr) 1998-01-29

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PCT/DK1997/000315 WO1998003249A1 (fr) 1996-07-22 1997-07-18 Epurateur a filtre catalytique ceramique pour gaz de combustion

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DE10034045A1 (de) * 2000-07-13 2002-01-31 Schumacher Umwelt Trenntech Keramisches Filterelement und Verfahren zu seiner Herstellung
WO2003055577A1 (fr) * 2001-12-29 2003-07-10 Pall Corporation Element filtrant
US6663839B2 (en) 2001-02-26 2003-12-16 Abb Lummus Global Inc. Radial flow gas phase reactor and method for reducing the nitrogen oxide content of a gas
US6706246B2 (en) 2001-02-26 2004-03-16 Abb Lummus Global Inc. System and method for the selective catalytic reduction of nitrogen oxide in a gas stream
US6821490B2 (en) 2001-02-26 2004-11-23 Abb Lummus Global Inc. Parallel flow gas phase reactor and method for reducing the nitrogen oxide content of a gas
WO2006037387A1 (fr) * 2004-09-30 2006-04-13 Pall Corporation Element poreux a activite catalytique
WO2013019393A1 (fr) * 2011-07-29 2013-02-07 Flsmidth A/S Système de régulation de la pollution pour une évacuation de four
US9108134B2 (en) 2011-08-05 2015-08-18 Pall Corporation Catalytic filter system
WO2016150464A1 (fr) * 2015-03-20 2016-09-29 Haldor Topsøe A/S Filtre à bougie en céramique catalysé et procédé de nettoyage de dégagement gazeux ou de gaz d'échappement
WO2016150465A1 (fr) * 2015-03-20 2016-09-29 Haldor Topsøe A/S Filtre à bougie en céramique catalysé et procédé de nettoyage des dégagements gazeux et des gaz d'échappement
WO2016110828A3 (fr) * 2015-02-13 2016-10-13 Dürr Systems GmbH Procédé et appareil pour accroître l'efficacité d'une combustion industrielle
TWI637781B (zh) * 2015-03-20 2018-10-11 丹麥商托普索公司 催化陶質心過濾器及清理製程排出或耗費氣體的方法
TWI637783B (zh) * 2015-03-20 2018-10-11 丹麥商托普索公司 經催化之陶瓷燭式過濾器及用於排氣或廢氣之清潔方法
WO2018197177A1 (fr) * 2017-04-26 2018-11-01 Haldor Topsøe A/S Procédé et système pour l'élimination de matière particulaire et de composés nocifs de gaz de combustion à l'aide d'un filtre céramique ayant un catalyseur scr
US10232352B2 (en) 2015-03-20 2019-03-19 Haldor Topsøe A/S Catalyzed ceramic candle filter and method of cleaning process off- or exhaust gases
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Publication number Priority date Publication date Assignee Title
EP0242488A1 (fr) * 1984-11-02 1987-10-28 Mitsubishi Jukogyo Kabushiki Kaisha Matière filtrante pour le traitement de gaz de fumée

Patent Citations (1)

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Publication number Priority date Publication date Assignee Title
EP0242488A1 (fr) * 1984-11-02 1987-10-28 Mitsubishi Jukogyo Kabushiki Kaisha Matière filtrante pour le traitement de gaz de fumée

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EP1772178A1 (fr) 2000-07-13 2007-04-11 Pall Corporation Bougie filtrant
DE10034045A1 (de) * 2000-07-13 2002-01-31 Schumacher Umwelt Trenntech Keramisches Filterelement und Verfahren zu seiner Herstellung
US8388898B2 (en) 2000-07-13 2013-03-05 Pall Corporation Ceramic filter element
US6663839B2 (en) 2001-02-26 2003-12-16 Abb Lummus Global Inc. Radial flow gas phase reactor and method for reducing the nitrogen oxide content of a gas
US6706246B2 (en) 2001-02-26 2004-03-16 Abb Lummus Global Inc. System and method for the selective catalytic reduction of nitrogen oxide in a gas stream
US6821490B2 (en) 2001-02-26 2004-11-23 Abb Lummus Global Inc. Parallel flow gas phase reactor and method for reducing the nitrogen oxide content of a gas
JP4807935B2 (ja) * 2001-12-29 2011-11-02 ポール・コーポレーション フィルタ要素
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