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WO2001066233A1 - Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene - Google Patents

Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene Download PDF

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Publication number
WO2001066233A1
WO2001066233A1 PCT/EP2001/002612 EP0102612W WO0166233A1 WO 2001066233 A1 WO2001066233 A1 WO 2001066233A1 EP 0102612 W EP0102612 W EP 0102612W WO 0166233 A1 WO0166233 A1 WO 0166233A1
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WO
WIPO (PCT)
Prior art keywords
catalyst
reactor
dust
exhaust gas
addition
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/EP2001/002612
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German (de)
English (en)
Inventor
Gurudas Samant
Gerd Sauter
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.)
Individual
Original Assignee
Individual
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
Priority claimed from DE2000111325 external-priority patent/DE10011325A1/de
Priority claimed from DE2000111327 external-priority patent/DE10011327A1/de
Application filed by Individual filed Critical Individual
Priority to US10/030,198 priority Critical patent/US20030157007A1/en
Priority to CA002391710A priority patent/CA2391710C/fr
Priority to AU52170/01A priority patent/AU5217001A/en
Priority to EP01925398A priority patent/EP1244511A1/fr
Publication of WO2001066233A1 publication Critical patent/WO2001066233A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • 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
    • 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
    • F23J2215/10—Nitrogen; Compounds thereof
    • F23J2215/101—Nitrous oxide (N2O)
    • 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 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices

Definitions

  • the currently most frequently used process is the SCR process (Selective Catalytic Reduction).
  • Ammonia or compounds containing ammonium are introduced into the reaction chamber containing the catalyst and the nitrogen oxides in the flue gas are converted into nitrogen and water vapor .
  • sulfuric acid and ammonium hydrogen sulfate are formed in the case of SO 2 -containing exhaust gases.
  • the formation of sulfuric acid and ammonium hydrogen sulfate is undesirable since they cause considerable corrosion problems in the system parts which are connected downstream of the reactor usually with S0 2 -containing exhaust gases, separate desulfurization plants switched on before the SCR process, which works on the principle of Dry or wet flue gas desulphurization plant (REA) work.
  • REA Dry or wet flue gas desulphurization plant
  • the exhaust gas is cooled and reheated for the subsequent SCR process, which is the case in most power plants and waste incineration plants.
  • Such processes are associated with high costs and the formation of CaSO 3 in accordance with the reaction CaO + SO 2 ⁇ CaSO 3 cannot be avoided.
  • the presence of CaSO 3 in landfill materials is environmentally hazardous.
  • EP-A-0 671 201 describes a method for separating sulfur trioxide and for denitrification - in particular in waste incineration plants - whereby ammonia or ammonium-containing compounds in the flue gas stream before a heat exchanger package, preferably before the last heat exchanger package, or before the flue gas purification into the flue gas be introduced so that the catalytic denitrification of the dedusted flue gases is then operated in the low temperature range, in particular between 100 ° C. and 280 ° C.
  • the aim is to reduce the SO 3 concentration upstream of the SCR reactor by forming ammonium sulfate.
  • the disadvantage of this process is that not only are ammonium sulfate aerosols formed, but also ammonium hydrogen sulfate, which is later deposited on the catalysts.
  • the ammonium sulfate aerosols are difficult to dedust in downstream filter devices, so that the environment is considerably polluted.
  • a separate scrubber is required for SO 2 removal.
  • the flue gas has to be heated up again after the scrubber, which cannot be done by heat exchange alone.
  • an additional firing e.g. B. surface burner with natural gas required.
  • Disadvantages are high investment and operating costs.
  • the production of cement includes the extraction and preparation of the raw materials, the burning of the raw material mixture consisting essentially of limestone, clay and silica to cement clinker in an oven and joint grinding of the clinker with ground materials, e.g. B. CaSO 4 , to cement.
  • ground materials e.g. B. CaSO 4
  • approx. 97% of cement clinker is burned in rotary kilns that are heated with natural gas, oil, coal dust or secondary fuels.
  • gas temperatures 1,800 ° C to 2,000 ° C
  • firing material temperatures 1,350 ° C to 1,500 ° C are reached, which are necessary for the formation of cement clinker.
  • the raw meal is preheated either in the rotary kiln itself or in a separate preheater, which preferably consists of several cyclones arranged one behind the other.
  • the hot exhaust gases from the rotary kiln flow through the cyclones from bottom to top.
  • the raw meal is added to the exhaust gases before the top cyclone.
  • the dust is separated from the gas in the individual cyclones and in again before the next cyclone suspended the gas flow. In this way, the raw meal is heated.
  • the exhaust gas After leaving the top cyclone, the exhaust gas still has temperatures of 300 ° C to 400 ° C and has a dust content of 50 - 100 g / m 3 N , r . With an exhaust gas quantity of, for example, approx.
  • the dust separation in the cyclones is between 80% and 95%.
  • the remaining heat content of the dust-containing exhaust gases is used in the grinding plant for raw meal drying.
  • the dust from the filter system of the grinding plant is called raw meal and is the starting material for the clinker process. If the grinding system fails or comes to a standstill, the exhaust gas after the last cyclone is not passed over the grinding system, but cooled down via an evaporative cooler and then dedusted in a separate filter system. This means direct operation without utilizing the heat content in the grinding system.
  • the exhaust gases can also contain carbon monoxide, hydrocarbons, halogen compounds, which must also be removed.
  • DE-A-196 35 385 provides a process for the denitrification of waste gases resulting from the production of cement, in which the waste gases, which have dust contents of more than 5 g / m 3 N f , in a titanium oxide-containing catalyst with a hydraulic Diameters from 6.8 mm to 30 mm are used and these with an exhaust gas velocity of more than 3 m / s i. B. flow through.
  • This is a denitrification of dust-containing exhaust gases from the cement industry using a titanium-containing catalyst.
  • Such a method is also described in DE-A-296 15 192.
  • the V 2 O 5 content in the catalytic converter is limited due to the formation of ammonium bisulfate if the SO 2 content in the exhaust gas is high.
  • the application EP-AI-0 534 087 A1 describes a process for removing nitrogen oxides from exhaust gases, in which alcohol is added to the exhaust gas before it enters the catalyst in order to reduce the conversion from SO 2 to SO 3 .
  • the aforementioned prior art does not include the simultaneous catalytic decomposition of sulfur and nitrogen oxides contained in exhaust gases, but only the denitrification of exhaust gases with a low sulfur oxide content.
  • a reduction catalyst with injection-side injection of reactant immediately after the furnace, that is, before Dedusting is arranged.
  • the reduction catalytic converter is arranged shortly after the furnace, ie in front of the cyclone heat exchanger, since the cyclone heat exchanger also acts as a dedusting apparatus in addition to being a heat exchanger.
  • the reduction reactor is not arranged immediately after the furnace, but after the cyclone heat exchanger, ie after the partial dedusting in the cyclones.
  • ammonia or urea metering takes place directly in front of the reduction reactor.
  • an even distribution of the ammonia is not guaranteed.
  • a high ammonia slip is to be expected due to the streak formation of the ammonia in the reduction catalyst.
  • this device is not suitable for the simultaneous separation of sulfur and nitrogen oxides.
  • the invention has for its object to develop a method for simultaneous desulfurization and denitrification without the formation of ammonium sulfate or ammonium bisulfate, in which the degradation of NO x to N 2 and H 2 O and SO 2 to CaSO 4 in one and the same Reactor takes place.
  • This object is achieved in that the treatment of the exhaust gases containing sulfur and nitrogen oxides in the presence and / or with the addition of one or more substances selected from the group of free oxides, carbonates, hydroxides of calcium, magnesium, sodium and potassium in a reactor is carried out with solid catalysts and during the treatment the operating conditions of the gas flow in the free reaction space in accordance with Froude's key figures in the area
  • This advantage is based on the fact that the catalytic treatment not only converts NO x to nitrogen and water vapor, but also converts SO 2 to SO 3 and incorporates it in the presence of free oxides, carbonates, hydroxides of calcium, magnesium, sodium and potassium becomes.
  • the formation of ammonium sulfates, ammonium bisulfates or sulfuric acid is suppressed.
  • These incorporated sulfates of calcium, magnesium, sodium and potassium can be very easily in a downstream filter system, e.g. B. a hose or electrostatic precipitator can be separated and used.
  • a preferred embodiment of the invention is the use of honeycomb and or plate catalysts which, in addition to titanium dioxide and tungsten, contain more than 0.5% by weight of vanadium pentoxide. This increases the catalytic conversions of NO x SO x .
  • a particularly preferred embodiment of the invention is that the catalysts preferably contain 2% to 8% vanadium pentoxide. With this mode of operation, levels of denitrification and desulfurization of over 95% are achieved.
  • a further preferred embodiment is the treatment in the presence and / or with the addition of one or more substances selected from the group of free oxides, carbonates, hydroxides of calcium, magnesium, sodium and potassium, with an average grain size d 50 between 5 ⁇ m and 100 microns.
  • the sulfur oxides are removed very quickly with little consumption of additives.
  • the costs are preferably minimized by the treatment in the presence and / or with the addition of one or more substances selected from the group of free oxides, carbonates, hydroxides of calcium, since calcium compounds are more economical compared to alkali compounds.
  • the calcium compounds are present in large quantities before dedusting before dedusting. So an arrangement of the reactor before dedusting d. H. between heat exchanger tower and grinding plant advantageous.
  • NH 3 -releasing compounds such as (NH 4 ) 2 SO 4 , (NH 4 ) 2 CO 3 , (NH 4 ) HCO 3 , (COONH 3 ) 2 H 2 O, HCOONH 4 , NH 3 , NH 4 , are used as reducing agents OH, H 2 O-CO-NH 2 , NH 2 CN, Ca (CN) 2 , NaOCN, C 2 H 4 N 4 , C 3 H 6 N 6 and NH 3 -containing wastewater from photochemical plants, individually or in groups , before entering the catalytic reactor in gaseous, liquid or solid state at several points in the flue gas stream in the temperature range between 200 ° C and 1000 ° C.
  • a preferred embodiment consists in that NH 3 -releasing compounds in the form of dilute aqueous solutions, preferably in the temperature range between 300 ° C. and 550 ° C., are introduced into the flue gas stream as the reducing agent.
  • the water vapor partial pressure in the reaction chamber is increased and the sulfur incorporation is thus improved.
  • a particularly preferred embodiment of the invention is the presence or addition of one or more substances, selected from the group of free oxides, carbonates, hydroxides of calcium, magnesium, sodium and potassium, in the flue gas stream before the addition of NH 3 -releasing compounds.
  • one or more substances selected from the group of free oxides, carbonates, hydroxides of calcium, magnesium, sodium and potassium, in the flue gas stream before the addition of NH 3 -releasing compounds.
  • the formation of ammonium bisulfate, ammonium sulfate and sulfuric acid is completely suppressed.
  • the flow can flow from the top or from the bottom.
  • a particularly preferred embodiment of the invention is that the reactor equipped with the catalysts can be flowed in alternately from above and from below. Due to this alternating flow, the reactor can easily be kept clean of dust-containing waste gases and the blockage of the channels by dust can be avoided. Furthermore, the lifetime of the catalysts can be increased by changing the flow of the reactor.
  • a further preferred embodiment of the invention is that the reactor equipped with a catalyst can be used in addition to the breakdown of sulfur and nitrogen oxides for the breakdown of halogen compounds, halogenated organic compounds, hydrocarbons and CO.
  • a preferred embodiment of the invention is that the reactor equipped with a catalyst for the decomposition of sulfur and nitrogen oxides in dust-containing exhaust gases in the chemical and metallurgical as well as in the cement and lime industry, in power plants and in waste incineration plants in the process flow in the temperature range between 200 ° C and 500 ° C can be used without additional preheating of the exhaust gas.
  • a further embodiment according to the invention is the device for the treatment of exhaust gas containing dust and oxygen.
  • the drawings show examples of the device for carrying out the method, which are explained in more detail below. They show schematically: ⁇ Fig. 1 shows an arrangement of the device in the cement industry
  • ⁇ • Fig. 2 shows a device for the cement industry
  • Fig. 1 shows the arrangement of the device according to the invention in a cement plant with a rotary kiln for clinker production.
  • the SCR reactor with catalyst modules and dust blowers is arranged in the flow direction after the suspended gas cyclone heat exchanger, consisting of the interconnected cyclones Z21 to Z24.
  • the suspended gas cyclone heat exchanger consisting of the interconnected cyclones Z21 to Z24.
  • NH 3 -releasing compounds several points A, B, C, D and E are provided in the temperature range from 300 ° C to 1000 ° C. Dosing points A, B and C are preferred for dosing ammonia, ammonia solution or urea solution.
  • the dosing points D and E are preferred.
  • the calcium-containing raw meal is fed in between the cyclones Z1 and Z2.
  • the exhaust gas is either passed to the chimney in the case of combined operation via the raw material mill and the dedusting device, or passed to the chimney in the case of direct operation via the evaporative cooler and the dedusting device.
  • Fig. 2 shows a device with gas flow from bottom to top, from top to bottom and alternately from below and from above.
  • NH 3 -releasing compounds In the event of a malfunction or the SCR reactor is shut off, the addition of NH 3 -releasing compounds is stopped and discharged either to the raw material mill or to the evaporative cooler via a bypass, ie via line F via the WT blower. Flaps M2, M4, M6 remain open and flaps M3, M1, M8, M7 and M5 are closed.
  • the cold air damper M9 is intended to control the exhaust gas temperature upstream of the SCR reactor.
  • the line E and the flaps M1, M8 and M7 are superfluous and the device is therefore only provided with an SCR reactor, bypass line F and the flaps M3, M4, M5, M6.
  • two individual flaps can be equipped with a switch flap.
  • the WT blower can be installed shortly after the cyclone heat exchanger, depending on space requirements and design.
  • the SCR reactor is provided, for example, with five catalyst layers with modules for SO x and NO x degradation and one catalyst layer with modules for hydrocarbon and carbon monoxide degradation.
  • the number of catalyst layers can be changed depending on the proportion of SO x , NO x , hydrocarbons and carbon monoxide.
  • the catalytic converter elements or catalytic converter modules are provided with wear protection or wear grids made of hard metal or ceramic on the gas side against erosion of dust-containing exhaust gases. With alternating gas flow from above and below, wear protection of approx. 5 - 20 mm is attached on both sides.
  • dust blowers are provided for each catalyst layer on the gas side. With alternating gas flow during operation from above and below, the dust blowers are provided on both sides. The air for the dust blower is heated to approx. 250 ° C before entering the reactor.
  • Fig. 3 shows the arrangement of the device according to the invention for power plants between the boiler and air preheater.
  • Additives e.g. B. Ca (OH) 2 , are added after the boiler and before the NHOH metering.
  • Fig. 4 shows the gas flow from below or from above or alternately from below and above analogous to the description in Fig. 2 for cement plants. Compared to In cement plants, the exhaust gas in power plants is led to the chimney after the SCR reactor via air preheaters and dedusting devices.
  • a system according to FIG. 2 is installed in a cement plant with an exhaust gas volume of 100,000 m 3 N tr / h. Experiments with partial gas flows of 3,000 - 10,000 m 3 N tr are carried out. Before being fed into the reactor, the raw gas has the following composition:
  • NO x content 1 500 mg m 3 N tr
  • Dust content 8 000 mg / m 3 N , r
  • the density of the gas is calculated based on the gas composition.
  • the dust content before entering the reactor (mainly CaO and Ca (OH) 2 ) is 8,000 mg / m 3 N tr .
  • the determined grain density of the dust is 3.1 kg / m 3 . Based on these data and operating conditions, a gas velocity of 6.5 m / s is determined in accordance with Froude's key figures.
  • the content of active component (e.g. V 2 O 5 ) in the catalysts is 0.1%, 0.3%, 1%, 3% and 5%.
  • Gaseous NH 3 is added as a reducing agent before entering the reactor with a stoichiometer, ie a molar ratio NH ⁇ NO x of 0.85.
  • a steel grille made of stainless steel is attached to the module of the catalyst as wear protection before the dust-containing exhaust gas enters.
  • the gas components NO x , SO x , NH 3 , CO, CO 2 and H 2 O are continuously measured before and after the reactor using a MCS-100 multicomponent analyzer.
  • the NH 3 content in the exhaust gas is ⁇ 1 mg / m 3 N. t . , , , The analyzes of the dust after the catalyst show no formation of ammonium sulfate, ammonium hydrogen sulfate or CaS0 3 .
  • the SO x content is bound as CaSO.
  • no dust deposits are found in the reactor or in the catalyst channels in these experiments.

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

Abstract

L'invention concerne un procédé et un dispositif pour le traitement catalytique d'effluents gazeux contenant des oxydes de soufre et d'azote et également de la poussière et de l'oxygène résultant de processus chimiques ou de la combustion de combustibles fossiles par exemple de combustibles de centrales ou secondaires, tels que des ordures ou des boues résiduaires, ou bien provenant d'usines de production de verre ou de ciment. Selon ledit procédé, les effluents gazeux sont libérés de leurs oxydes de soufre et d'azote en présence et/ou avec addition d'au moins une substance sélectionnée parmi les oxydes libres, les carbonates et les hydroxydes de calcium, magnésium, sodium et potassium, dans un réacteur comportant un catalyseur solide, à une température comprise dans la plage 200 DEG C - 500 DEG C.
PCT/EP2001/002612 2000-03-10 2001-03-08 Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene Ceased WO2001066233A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US10/030,198 US20030157007A1 (en) 2000-03-10 2001-03-08 Method and device for the catalytically treating exhaust gas containing dust and oxygen
CA002391710A CA2391710C (fr) 2000-03-10 2001-03-08 Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene
AU52170/01A AU5217001A (en) 2000-03-10 2001-03-08 Method and device for catalytically treating exhaust gas containing dust and oxygen
EP01925398A EP1244511A1 (fr) 2000-03-10 2001-03-08 Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE2000111325 DE10011325A1 (de) 2000-03-10 2000-03-10 Verfahren und Vorrichtung zur katalytischen Behandlung von Schwefel-und Stickoxiden enthaltenden staub -und sauerstoffhaltigen Abgasen
DE10011327.7 2000-03-10
DE2000111327 DE10011327A1 (de) 2000-03-10 2000-03-10 Verfahren und Vorrichtung zur katalytischen Behandlung von Schwefel-und Stickoxide enthaltenden staub-und sauerstoffhaltigen Abgasen eines Zement-Drehrohrofens
DE10011325.7 2000-03-10

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Publication Number Publication Date
WO2001066233A1 true WO2001066233A1 (fr) 2001-09-13

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PCT/EP2001/002612 Ceased WO2001066233A1 (fr) 2000-03-10 2001-03-08 Procede et dispositif de traitement catalytique d'effluents gazeux contenant de la poussiere et de l'oxygene

Country Status (4)

Country Link
EP (1) EP1244511A1 (fr)
AU (1) AU5217001A (fr)
CA (1) CA2391710C (fr)
WO (1) WO2001066233A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005039997A1 (de) * 2005-08-24 2007-03-01 Samant, Gurudas, Dr. Verfahren und Vorrichtung zur Reinigung von SCR-Reaktoren im Zementdrehrohrofen
WO2007104785A3 (fr) * 2006-03-15 2008-01-24 Cemag Anlagenbau Dessau Gmbh Production de clinker
CN1844747B (zh) * 2006-04-28 2010-04-21 合肥水泥研究设计院 水泥回转窑和焚烧炉联合处理城市生活垃圾的系统及其应用
CN101857350A (zh) * 2010-06-04 2010-10-13 合肥水泥研究设计院 水泥窑废气间接干化处理和利用污泥装置及工艺方法
WO2016113049A1 (fr) * 2015-01-14 2016-07-21 Thyssenkrupp Industrial Solutions Ag Procédé de réduction des oxydes d'azote dans les effluents gazeux d'une installation de traitement à flux entrainé dérivé et installation de traitement à flux entrainé
WO2017012880A1 (fr) * 2015-07-23 2017-01-26 Thyssenkrupp Industrial Solutions Ag Procédé et installation de fabrication de clinker de ciment ou d'autres produits minéraux, et de dénitruration de gaz de dérivation
EP3299080A1 (fr) * 2016-09-26 2018-03-28 HeidelbergCement AG Procédé de contrôle du taux d'ammoniac dans les gaz de combustion de cément et usine de cément avec émission d'ammoniac contrôlée

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0161470A1 (fr) * 1984-04-05 1985-11-21 Linde Aktiengesellschaft Procédé et dispositif pour éliminer des substances gazeuses indésirables d'un gaz de fumée
EP0211458A1 (fr) * 1985-07-20 1987-02-25 Rolf Dr. Graf Procédé pour éliminer de la matière nocive de gaz de fumée
EP0682974A2 (fr) * 1994-05-19 1995-11-22 Metallgesellschaft Ag Procédé pour la dénitration d'un gaz d'échappement
WO1997009112A1 (fr) * 1995-09-08 1997-03-13 Elex Ag Installation d'epuration des gaz de fumee
EP0791389A1 (fr) * 1996-02-20 1997-08-27 ERC Emissions-Reduzierungs-Concepte GmbH Dispositif catalyseur, notamment pour une chaudière à trois passages
EP0826408A1 (fr) * 1996-08-31 1998-03-04 Katalysatorenwerke Hüls GmbH Procédé pour l'élimination réductrice d'oxydes d'azote dans des gaz effluents provenant de la fabrication de ciment et contenant des poussières
EP0885649A1 (fr) * 1997-06-20 1998-12-23 Von Roll Umwelttechnik AG Procédé et dispositif pour la dénitration de gaz d'échappement provenant de la combustion

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0161470A1 (fr) * 1984-04-05 1985-11-21 Linde Aktiengesellschaft Procédé et dispositif pour éliminer des substances gazeuses indésirables d'un gaz de fumée
EP0211458A1 (fr) * 1985-07-20 1987-02-25 Rolf Dr. Graf Procédé pour éliminer de la matière nocive de gaz de fumée
EP0682974A2 (fr) * 1994-05-19 1995-11-22 Metallgesellschaft Ag Procédé pour la dénitration d'un gaz d'échappement
WO1997009112A1 (fr) * 1995-09-08 1997-03-13 Elex Ag Installation d'epuration des gaz de fumee
EP0791389A1 (fr) * 1996-02-20 1997-08-27 ERC Emissions-Reduzierungs-Concepte GmbH Dispositif catalyseur, notamment pour une chaudière à trois passages
EP0826408A1 (fr) * 1996-08-31 1998-03-04 Katalysatorenwerke Hüls GmbH Procédé pour l'élimination réductrice d'oxydes d'azote dans des gaz effluents provenant de la fabrication de ciment et contenant des poussières
EP0885649A1 (fr) * 1997-06-20 1998-12-23 Von Roll Umwelttechnik AG Procédé et dispositif pour la dénitration de gaz d'échappement provenant de la combustion

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005039997A1 (de) * 2005-08-24 2007-03-01 Samant, Gurudas, Dr. Verfahren und Vorrichtung zur Reinigung von SCR-Reaktoren im Zementdrehrohrofen
WO2007104785A3 (fr) * 2006-03-15 2008-01-24 Cemag Anlagenbau Dessau Gmbh Production de clinker
CN1844747B (zh) * 2006-04-28 2010-04-21 合肥水泥研究设计院 水泥回转窑和焚烧炉联合处理城市生活垃圾的系统及其应用
CN101857350A (zh) * 2010-06-04 2010-10-13 合肥水泥研究设计院 水泥窑废气间接干化处理和利用污泥装置及工艺方法
WO2016113049A1 (fr) * 2015-01-14 2016-07-21 Thyssenkrupp Industrial Solutions Ag Procédé de réduction des oxydes d'azote dans les effluents gazeux d'une installation de traitement à flux entrainé dérivé et installation de traitement à flux entrainé
KR20170104466A (ko) * 2015-01-14 2017-09-15 티센크루프 인더스트리얼 솔루션스 아게 동반 유동 처리 플랜트의 배기 가스 중의 질소 산화물을 환원시키는 방법, 및 동반 유동 처리 플랜트
KR101977521B1 (ko) 2015-01-14 2019-05-10 티센크루프 인더스트리얼 솔루션스 아게 동반 유동 처리 플랜트의 배기 가스 중의 질소 산화물을 환원시키는 방법, 및 동반 유동 처리 플랜트
WO2017012880A1 (fr) * 2015-07-23 2017-01-26 Thyssenkrupp Industrial Solutions Ag Procédé et installation de fabrication de clinker de ciment ou d'autres produits minéraux, et de dénitruration de gaz de dérivation
EP3299080A1 (fr) * 2016-09-26 2018-03-28 HeidelbergCement AG Procédé de contrôle du taux d'ammoniac dans les gaz de combustion de cément et usine de cément avec émission d'ammoniac contrôlée
WO2018054756A1 (fr) * 2016-09-26 2018-03-29 Heidelbergcement Ag Procédé de régulation de la teneur en ammoniac dans un gaz d'échappement de ciment et installation de ciment à émission d'ammoniac contrôlée

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CA2391710C (fr) 2007-05-22
AU5217001A (en) 2001-09-17
EP1244511A1 (fr) 2002-10-02

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