EP3154664A1 - Installation composée d'un dispositif de traitement produisant des fumées, d'un catalyseur d'oxydation et d'un catalyseur de réduction, ainsi que procédé de traitement des fumées dans une telle installation - Google Patents

Installation composée d'un dispositif de traitement produisant des fumées, d'un catalyseur d'oxydation et d'un catalyseur de réduction, ainsi que procédé de traitement des fumées dans une telle installation

Info

Publication number
EP3154664A1
EP3154664A1 EP15729778.9A EP15729778A EP3154664A1 EP 3154664 A1 EP3154664 A1 EP 3154664A1 EP 15729778 A EP15729778 A EP 15729778A EP 3154664 A1 EP3154664 A1 EP 3154664A1
Authority
EP
European Patent Office
Prior art keywords
exhaust gas
temperature
catalyst
reduction
oxidation catalyst
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.)
Withdrawn
Application number
EP15729778.9A
Other languages
German (de)
English (en)
Inventor
Franz-Josef Zurhove
Melanie Flaßpöhler
Timo Stender
Kathrin Rohloff
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.)
Maerz Ofenbau AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
Elex Cemcat AG
ThyssenKrupp Industrial Solutions AG
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 Elex Cemcat AG, ThyssenKrupp Industrial Solutions AG filed Critical Elex Cemcat AG
Publication of EP3154664A1 publication Critical patent/EP3154664A1/fr
Withdrawn legal-status Critical Current

Links

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
    • B01D53/869—Multiple step processes
    • 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
    • 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
    • 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
    • B01D53/864—Removing carbon monoxide or hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • 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
    • B01D2251/2065—Ammonium hydroxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/902—Multilayered catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/904—Multiple catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories

Definitions

  • the invention relates to a system comprising a treatment device for the mechanical and / or thermal treatment of an inorganic material which generates exhaust gas, with an oxidation catalyst adjoining the treatment device in the flow direction of the exhaust gas and with a reduction catalytic converter adjoining the oxidation catalytic converter in the flow direction of the exhaust gas.
  • the invention further relates to a method for treating the exhaust gas in such a plant.
  • a generic system is used for example in the production of cement clinker.
  • the cement raw meal is preheated before being introduced into a rotary kiln in a material preheater, which is usually designed as a four- to six-stage cyclone preheater, by the exiting the rotary kiln exhaust gas.
  • the exhaust gas is usually cooled down to a temperature of between 250 ° C and 400 ° C.
  • a suitable exhaust gas temperature may be required to be in a suitable temperature range for (high) pollutant reduction.
  • Such an adjustment of the exhaust gas temperature upstream of the exhaust gas treatment device can take place by various measures, such as, for example, a water application, a heat exchanger with heat supply or removal, or an addition of another gas flow with a different temperature. If, for example, an increase in the exhaust gas temperature takes place after the material preheater, this can be achieved by an additional heat supply, for example, by means of an auxiliary heater, for example in the form of burners or a combustion chamber can be achieved.
  • DE 197 20 205 A1 further discloses the possibility of a combination of the reduction catalyst with an oxidation catalyst connected downstream thereof, as a result of which organic compounds and, in particular, furans and dioxins are to be removed from the exhaust gas at the same time.
  • a device for the treatment of exhaust gases from, for example, a plant for cement clinker production has become known.
  • the device comprises a multilayer catalyst having at least three successively arranged catalyst layers with at least partially different lengths.
  • the first of the layers is designed as an oxidation catalyst, while a supply device for an ammonia-containing reducing agent first connects to this first catalyst layer.
  • the invention has the object underlying to provide an advantageous possibility for the exhaust gas treatment of a treatment device for mechanical and / or thermal treatment of an inorganic material and in particular derived from a cement clinker furnace exhaust gas.
  • This object is achieved by means of a system according to claim 1 and a method according to claim 9.
  • Advantageous embodiments of the system according to the invention and advantageous embodiments of the method according to the invention are the subject of the other claims and will become apparent from the following description of the invention.
  • the invention is based on the finding that in a reversal of the order of reduction catalyst and oxidation catalyst compared to the known from DE 197 20 205 AI device for exhaust gas treatment can achieve relevant advantages that can overcompensate the disadvantages associated with the reversal disadvantages.
  • the exhaust gas should be supplied to the two types of catalyst with a temperature optimally adapted as far as possible in order to achieve high reduction rates for the respective pollutants. It can be assumed in principle that the reduction rates for carbon monoxide and / or organic hydrocarbons in an oxidation catalyst and for organic hydrocarbons in a reduction catalyst increase with increasing temperature of the exhaust gas. For a reduction of carbon monoxide in an oxidation catalyst results in a minimum temperature of 180 ° C, for example, from the guideline VDI 3476. Is also a relevant reduction of organic hydrocarbons provided, this usually requires higher exhaust gas temperatures, for example, at least 360 ° C.
  • the exhaust gas temperature in the oxidation catalyst should be at least 400 ° C.
  • Another advantage of higher exhaust gas temperatures in an oxidation catalyst is the markedly slower deactivation of the oxidation catalyst.
  • Such high exhaust gas temperatures can lead to its rapid deactivation in a reduction catalyst, such as an SCR catalyst.
  • a reduction catalyst such as an SCR catalyst.
  • this problem would still by the exothermic oxidation of the pollutants in the oxidation catalyst be reinforced, which could lead to a further increase in the temperature of the exiting the oxidation catalyst exhaust gas.
  • the temperature of the exhaust gas entering the reduction catalyst should be limited.
  • the temperature influencing device arranged upstream of the oxidation catalytic converter preferably effects a heating of the exhaust gas.
  • the temperature-influencing device arranged between the oxidation catalytic converter and the reduction catalytic converter preferably effects a cooling of the exhaust gas.
  • the method according to the invention makes it possible to set the temperatures of the exhaust gas entering the catalytic converters as optimally as possible.
  • CO carbon monoxide
  • C x H y organic hydrocarbons
  • NO x nitrogen oxides
  • the exhaust gas should advantageously be supplied to the reduction catalyst at a maximum of 420 ° C., preferably 400 ° C., and particularly preferably 380 ° C.
  • the temperature of the exhaust gas fed to the reduction catalytic converter should advantageously not fall below 150 ° C., preferably 180 ° C. and particularly preferably 220 ° C.
  • the oxidation catalyst and / or the reduction catalyst may be single or multi-layered.
  • Several similar catalyst (lag) s can also be connected in parallel in the exhaust line of the system.
  • the configuration of the temperature influencing device (s) may be arbitrary.
  • an increase in temperature for the exhaust gas is to be achieved by means of the temperature-influencing device (s)
  • this can be based in particular on a combustion (ie the burning of a fuel with the primary or exclusive objective of the heat input into the exhaust gas), an admixture of a fluid, in particular a gas, based on a higher temperature compared to the local temperature of the exhaust gas, and / or a heat exchange with any heat exchange medium.
  • a combustion ie the burning of a fuel with the primary or exclusive objective of the heat input into the exhaust gas
  • an admixture of a fluid, in particular a gas based on a higher temperature compared to the local temperature of the exhaust gas, and / or a heat exchange with any heat exchange medium.
  • the temperature-influencing device may comprise a heater, an admixing device for a fluid, in particular a gas (for example another exhaust gas or a cooling gas of the system), and / or a heat exchanger.
  • a gas for example another exhaust gas or a cooling gas of the system
  • a temperature reduction for the exhaust gas is to be achieved by means of the temperature-influencing device (s)
  • this can be based, in particular, on admixing a gas with a lower temperature compared to the local temperature of the exhaust gas, an admixing of a medium evaporating at the relevant temperatures, preferably water or a watery one Solution, and / or a heat exchange with any heat exchange medium based.
  • the temperature-influencing device may for this purpose comprise an admixing device for a fluid, in particular a gas or water or an aqueous solution, and / or a heat exchanger.
  • the Temperaturbeeinfiussungsvoriques (s) is / are preferably controllable with regard to the temperature influence on the exhaust gas and particularly preferably adjustable so that the most accurate and changing circumstances (in particular temperature and composition of the exhaust gas on entering the temperature influencing device) adjustable adjustment of the temperature of Exhaust gas for the entry into the downstream of the temperature influencing device following oxidation and / or reduction catalyst can take place.
  • a temperature influencing device is provided, in a preferred embodiment of such a system according to the invention that by means of a common heat exchanger or by means of a heat exchanger of the temperature influencing devices using a transfer medium, a heat transfer Exhaust gas downstream of the oxidation catalyst is carried out on exhaust gas upstream of the oxidation catalyst.
  • the temperature-influencing device of the system according to the invention arranged upstream of the oxidation catalytic converter can comprise a material preheater arranged between the treatment device and the oxidation catalytic converter, in which heat is transferred from the exhaust gas to the material. Adjusting the temperature of the exhaust gas entering the oxidation catalyst may then be achieved in that the heat exchange of the exhaust gas with the preheated material is adjustable and in particular controllable.
  • the material preheater may comprise one or more heat exchanger stages, wherein a first feed for the material is arranged in the direction of passage of the material through the material preheater in front of a heat exchanger stage, a second supply for the material relative to the direction of passage of the material through the material preheater , is arranged behind this heat exchanger stage and a control device for the adapted distribution of the material to the first supply and the second supply is provided.
  • the control device may preferably be formed as a control device, which uses as a controlled variable, for example, the temperature of the exhaust gas to be set or an exhaust gas composition upstream and / or downstream of the oxidation catalyst (and optionally also of the reduction catalyst).
  • a metering device for a particular ammonia-containing reducing agent (in particular liquid or gaseous) is preferably provided.
  • the metering device can advantageously be arranged between the oxidation catalytic converter and the reduction catalytic converter, as a result of which exposure of the oxidation catalytic converter to the reducing agent can be avoided.
  • the metering device can advantageously also function as a temperature-influencing device in that the metered reducing agent extracts heat energy from the exhaust gas by evaporation.
  • a metered addition of an aqueous ammonia solution can be provided.
  • a means for dust removal for the oxidation catalyst and / or the reduction catalyst prevented by the deposition of dust on elements of the catalyst device and / or already deposited dust can be removed again.
  • This device for dust removal can, for example, in the form of a known dust blower, in particular, be designed for use in cement processing plant designed dust blower.
  • the integration of one or more facilities for dust removal in the system according to the invention may be useful, in particular due to the amounts of dust contained in the exhaust gas, when a dust filter in the flow direction of the exhaust gas to the catalysts and consequently the exhaust gas is dedusted only downstream of the reduction catalyst.
  • the dust content in the exhaust gas up to the dust filter can be up to 100 g / Nm 3 or even more, at least when cement clinker is fired by means of the treatment device.
  • a basically advantageous dust filter can also be integrated elsewhere in the exhaust system of the system according to the invention, in particular upstream of the oxidation catalytic converter.
  • the plant according to the invention is particularly suitable for the production and / or processing of material (s) of the basic industry, in particular of raw materials of the mining industry and concrete of cement clinker, lime and minerals.
  • the plant according to the invention may also comprise other plants or plant components which do not serve the treatment of an inorganic material.
  • a temperature influencing device which is designed in the form of an admixer or a heat exchanger, a component and in particular a guided in the component material or fluid flow of a non-plant equipment or apparatus, such as the power plant industry (especially combustion of materials (especially raw materials, but also eg waste) for the production of electrical energy).
  • These installations or devices that are not in use may serve, for example, for drying, torrefaction and / or pyrolysis of, in particular, a carbonaceous material or fluid stream Influencing the temperature of the exhaust gas upstream of the oxidation catalyst and / or of the reduction catalyst does not have to be geared to achieving the highest possible rate of reduction. Rather, a reduction to the extent that statutory emissions regulations are met, can be provided. In this case, a lower than maximum possible reduction can be accepted in order to keep, for example, the temperature load for the system components and in particular the catalysts and / or additional fuel sales, for example in one or more designed as a heater temperature influencing devices, within limits.
  • FIG. 1 shows a plant according to the invention in a schematic representation
  • Fig. 2 a plant according to the invention for the production of cement clinker in a schematic representation.
  • FIG. 1 shows in a greatly simplified manner a plant according to the invention with a treatment device 1 for the mechanical and / or thermal treatment of an inorganic material 2 and with an exhaust gas line connected downstream of the treatment device 1 in which exhaust gas discharged from the treatment device 1 is cleaned; ie there is a reduction in the concentrations of certain pollutants in the exhaust gas.
  • the exhaust gas line comprises - in the flow direction of the exhaust gas - a first temperature influencing device 3, an oxidation catalyst 4, a second temperature influencing device 5 and a reduction catalyst 6.
  • the treatment device 1, the material to be treated 2 and a fuel 7 is supplied.
  • the treatment of the material 2 takes place thermally by burning the fuel 7 in the treatment device 1.
  • the resulting exhaust gas is further heated in the first temperature influencing device 3 to a temperature of, for example, about 440 ° C. This allows high rates of reduction for the concentrations of both carbon monoxide and organic hydrocarbons in the first
  • the first temperature influencing device 3 may for example comprise a heat exchanger, through which a heat transfer from any other fluid, for example, the exhaust gas downstream of the oxidation catalyst 4 and upstream of the reduction catalyst 6, takes place on the exhaust gas.
  • the first temperature-influencing device 3 may also comprise a heater 8, by which a further heating of the exhaust gas can take place in addition to that by the heat exchanger.
  • a heater 8 is particularly useful when the heat transfer in the heat exchanger is not sufficient to heat the exhaust reliably to the desired temperature.
  • the heat input into the exhaust gas by a heater 8 on the fuel turnover is well regulated.
  • the temperature of the exiting from the oxidation catalyst 4 exhaust gas is too high for the subsequent reduction catalyst 6. Therefore, it is provided to cool the exhaust gas in the second temperature influencing device 5 to at most about 380 ° C.
  • This may be, for example, in addition to an optional cooling by a heat exchange with the exhaust gas upstream of the oxidation catalyst 4 - by injecting an aqueous ammonia solution take place, wherein the heat energy required for the evaporation of the solution is removed from the exhaust gas.
  • the ammonia of the solution also serves as a reducing agent for the reduction in the concentrations of nitrogen oxides in the exhaust gas taking place in the reduction catalytic converter 6.
  • FIG. 2 shows a system of the invention corresponding to FIG. 1 that has a substantially more concrete design.
  • This is for the production of cement clinker, which is in a treatment apparatus in the form of a rotary kiln 9 from cement raw meal, fired.
  • the finely ground cement raw meal which comprises organic constituents, is dispersed into hot fuel gases which originate from the rotary kiln 9 and from an optional calciner 10, wherein the organic constituents are expelled from the cement raw meal and incompletely combusted.
  • the rotary kiln 9 based on the passage direction of the material (2) (cement raw meal or cement clinker), a material preheater 11 upstream in the form of a multi-stage cyclone preheater with integrated calciner 10.
  • the material preheater 11 the cement raw meal is flowed through in several stages by the exhaust gas originating from the rotary kiln 9 and entrained and then separated again from the exhaust gas stream in a cyclone of the respective preheater stage.
  • the cyclone preheater has, as usual, a vertical structure, so that the cement raw meal, as far as it is entrained by the exhaust gas flow, is primarily moved counter to the direction of gravity and falls after separation in the cyclone due to gravity to the next preheater stage.
  • Other common types of material preheaters such as staged residence time reactors, are also possible.
  • the cement raw meal is fed via a cement raw meal task 12 in the system and fed to the material preheater 11.
  • the material preheater 11 also serves as the first temperature influencing device 3 of the system according to the invention.
  • a division of the cement raw meal takes place on a first supply 13, which, based on the direction of the passage of the Cement raw meal through the material preheater 11, in front of the first (here uppermost) heat exchanger stage 14 is arranged, and a second supply 15.
  • the introduced via this first feed 4 in the material preheater 2 cement raw meal thus increases in heat exchange with the exhaust gas in this first heat exchanger stage 14 (FIG. and also all other heat exchanger stages).
  • the second cement raw meal feeder 15 is located behind the first heat exchanger stage 14, based on the direction of passage of the cement raw meal through the material preheater 11.
  • the introduced via this second supply 15 in the material preheater 11 cement raw meal thus does not participate in a heat exchange with the exhaust gas in the first heat exchanger stage 14, but in all other heat exchanger stages. If a portion of the cement raw meal does not pass through all the heat exchanger stages, the total heat transfer from the exhaust to the material to be preheated will remain below a plant specific and operating parameter dependent maximum, which will affect both the temperature of the preheated cement raw meal and the temperature of the exhaust leaving the material preheater 11.
  • the sizes of the cement raw meal streams introduced into the material preheater 11 via the first supply 13 and the second supply 15 can be adjusted via a control device 16. This consequently allows an adapted adjustment of the temperature of the exhaust gas leaving the material preheater 11, which is subsequently supplied to an exhaust gas treatment device 17.
  • the control device 16 is designed as a control device that regulates the sizes of the introduced via the first supply 13 and the second supply 15 in the material preheater 11 cement raw meal flows in response to a measured temperature of the entering into the exhaust treatment device 17 exhaust gas such that the measured Exhaust gas temperature is in a desired temperature range.
  • This target temperature range is chosen with regard to the highest possible reduction rate for pollutants by means of a multi-layer oxidation catalyst 4 of the exhaust treatment device 17 and is for example between about 360 ° C and about 440 ° C, depending on the specific exhaust gas composition.
  • the oxidation catalyst 4 is followed by a multilayer reduction catalyst 6.
  • This is based on the principle of selective catalytic reduction of particular nitrogen oxides.
  • the exhaust gas in a known manner upstream of the reduction catalyst 6 (and downstream of the oxidation catalyst 4) is added a reducing agent in the form of ammonium hydroxide, which is distinguished from (the also possible use of) urea as a reducing agent, in particular by a shorter evaporation path.
  • decomposition would release carbon monoxide from urea, which should be avoided.
  • the nitrogen oxides are reduced with the ammonia to nitrogen and water and organic hydrocarbons still contained in the exhaust gas are further reduced.
  • the oxidation catalyst 4 and the reduction catalyst 6 are integrated in the same housing 18 of the exhaust treatment device 17.
  • the temperature of the exhaust gas leaving the oxidation catalytic converter 4 is too high for a permanent admission of the reduction catalytic converter 6.
  • the system therefore has as a second temperature influencing device 5 a cooling device for the exhaust gas to be introduced into the reduction catalytic converter 6.
  • This cooling device is in the form of a metering device 19 for water, which is formed integrally with a metering device 20 for the ammonium hydroxide. A mixture of ammonium hydroxide and water is thus introduced via a common nozzle device 21 in the exhaust gas stream.
  • the introduced water evaporates in the exhaust gas stream and thereby removes this heat energy, which leads to a decrease in temperature of the entire, then the evaporated water and ammonium hydroxide exhaust gas stream.
  • the temperature of the exhaust gas entering the reduction catalytic converter 6 is limited to preferably a maximum of 380 ° C.
  • the integral metering device has no return.
  • the adapted, and in particular with respect to the maximum heat exchange performance of the material preheater 11 reduced heat exchange of the exhaust gas to the preheating cement raw meal not only affects the temperature of the entering into the exhaust treatment device 17 exhaust gas but also the temperature of entering the rotary kiln 9 cement raw meal.
  • this temperature of the preheated cement raw meal can be relatively low, but this can be compensated by an increased fuel turnover in one or more, serving as heat generating devices burners (not shown) of the rotary kiln 9 or - if available - the calciner 10.
  • the fuel conversion and thus the heat input in the rotary kiln 9 and in the exhaust gas can be adjusted by means of a control device or regulated a control device.
  • the temperature of the exhaust gas entering the exhaust gas treatment device 17 may represent a controlled variable for the fuel conversion. Alternatively or additionally, other parameters may also serve as a controlled variable, for example a gas temperature in the optional calciner 10 of the system.
  • a precalcination of the already preheated in the cyclone preheater cement raw meal can be done, which is then finished in the rotary kiln 9 ready for cement clinker.
  • For heating and deacidification of the cement raw meal in the precalcining in the calciner 10 are removed from the rotary kiln 9 exhaust (and heated cooling air from a rotary kiln 9 (with respect to the direction of passage of the cement clinker) downstream clinker cooler 22, which is supplied via a Tertiär Kunststoff 23 to the calciner 10
  • the separation of the precalcined in the calciner 10 material from the exhaust gas and / or the cooling air takes place in the cyclone of the last heat exchanger stage of the material preheater 11th Reference numerals:

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Ceramic Engineering (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Ecology (AREA)
  • Environmental Sciences (AREA)
  • Public Health (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Chimneys And Flues (AREA)

Abstract

L'invention concerne une installation composée d'un dispositif de traitement (1) destiné au traitement mécanique et/ou thermique d'un matériau inorganique (2) et produisant des fumées, d'un catalyseur d'oxydation (4) situé dans le prolongement du dispositif de traitement (1) dans le sens d'écoulement des fumées et d'un catalyseur de réduction (6) situé dans le prolongement du catalyseur d'oxydation (4) dans le sens d'écoulement des fumées. Selon l'invention, ladite installation comprend un dispositif de régulation de température (3, 5) destiné à influer sur la température des fumées en amont du catalyseur d'oxydation (4) et/ou entre le catalyseur d'oxydation (4) et le catalyseur de réduction (6).
EP15729778.9A 2014-06-10 2015-06-08 Installation composée d'un dispositif de traitement produisant des fumées, d'un catalyseur d'oxydation et d'un catalyseur de réduction, ainsi que procédé de traitement des fumées dans une telle installation Withdrawn EP3154664A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014108153.6A DE102014108153A1 (de) 2014-06-10 2014-06-10 Anlage mit einer ein Abgas erzeugenden Behandlungsvorrichtung, einem Oxidations- und einem Reduktionskatalysator sowie Verfahren zur Behandlung des Abgases in einer solchen Anlage
PCT/EP2015/062729 WO2015189154A1 (fr) 2014-06-10 2015-06-08 Installation composée d'un dispositif de traitement produisant des fumées, d'un catalyseur d'oxydation et d'un catalyseur de réduction, ainsi que procédé de traitement des fumées dans une telle installation

Publications (1)

Publication Number Publication Date
EP3154664A1 true EP3154664A1 (fr) 2017-04-19

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP15729778.9A Withdrawn EP3154664A1 (fr) 2014-06-10 2015-06-08 Installation composée d'un dispositif de traitement produisant des fumées, d'un catalyseur d'oxydation et d'un catalyseur de réduction, ainsi que procédé de traitement des fumées dans une telle installation

Country Status (4)

Country Link
US (1) US20170157560A1 (fr)
EP (1) EP3154664A1 (fr)
DE (1) DE102014108153A1 (fr)
WO (1) WO2015189154A1 (fr)

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US11007479B2 (en) * 2017-04-26 2021-05-18 Haldor Topsoe A/S Method and system for the removal of particulate matter and noxious compounds from flue-gas using a ceramic filter with an SCR catalyst

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DE102014108154A1 (de) * 2014-06-10 2015-12-17 Elex Cemcat Ag Verfahren zur Abgasbehandlung und Anlage mit einer Abgasbehandlungsvorrichtung
DE102016121301A1 (de) * 2016-11-08 2018-05-09 Thyssenkrupp Ag Anlage und Verfahren zur Reinigung eines Abgases einer Bearbeitungsvorrichtung der Zement-, Kalk- oder Mineralsindustrie
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