US20100307388A1 - Flue gas purification plant - Google Patents

Flue gas purification plant Download PDF

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Publication number
US20100307388A1
US20100307388A1 US12/863,248 US86324809A US2010307388A1 US 20100307388 A1 US20100307388 A1 US 20100307388A1 US 86324809 A US86324809 A US 86324809A US 2010307388 A1 US2010307388 A1 US 2010307388A1
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US
United States
Prior art keywords
flue gas
filter device
dust
furnace
filter
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.)
Abandoned
Application number
US12/863,248
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English (en)
Inventor
Anton Secklehner
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.)
Scheuch GmbH
Original Assignee
Scheuch GmbH
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 Scheuch GmbH filed Critical Scheuch GmbH
Publication of US20100307388A1 publication Critical patent/US20100307388A1/en
Assigned to SCHEUCH GMBH reassignment SCHEUCH GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SECKLEHNER, ANTON
Abandoned legal-status Critical Current

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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
    • B01D53/34—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
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium 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

Definitions

  • the invention relates to a plant for purifying the flue gases from a furnace, including at least one selective reduction catalyst for reducing nitrogen oxides present in the flue gas, and/or at least one catalyst for reducing carbon monoxide from, particularly odor-forming, hydrocarbons or for removing ammonia, as well as a dust separation means, and a method for purifying the flue gases from a furnace by the selective catalytic reduction of nitrogen oxides by a reducing agent and a reduction catalyst as well as by dust separation.
  • the removal of nitrogen oxides, or denitrification, is usually carried out by reductive methods.
  • SNCR selective non-catalytic reduction
  • SCR selective catalytic reduction
  • the selective non-catalytic reduction is usually carried out at temperatures between 900° C. and 1100° C., with the reducing agent being directly fed into the furnace.
  • the selective catalytic reduction can be performed at distinctly lower temperatures, since the catalyst significantly reduces the activation energies required for the reducing reactions.
  • This method moreover, allows for a decrease of the reducing agent charge as compared to SNCR denitrification, where the reducing agent is used in a hyperstoichiometric amount, since practically no side reactions will occur.
  • the selective catalytic reduction differentiates between high-dust configurations and low-dust configurations.
  • high-dust configurations the denitrification of the flue gases takes place prior to dedusting, which is why the catalyst is subject to elevated wear.
  • This will, as a rule, result in reduced dwell times of the catalyst, and call for expensive measures, e.g., the use of special catalysts with suitable geometries of the flue gas channels extending through the catalyst bed as is, for instance, described in DE 296 23 503 U1 or DE 196 35 383 A1, or the use of catalysts that are capable of withstanding higher mechanical stresses caused, for instance, by the periodic shaking-off of the dust loads from the catalyst particles.
  • SCR selective catalytic reduction
  • the dust separation means is comprised of at least a first and a second filter device and the reduction catalyst is arranged between the first and second filter devices, as well as by method for purifying the flue gases from a furnace, in which the flue gases are supplied to a first dust separation prior to contacting the reduction catalyst, and the fine-dust purification of the flue gases is effected after the reduction of the nitrogen oxides.
  • the catalyst configuration for the removal of nitric oxides according to the invention offers the advantage that the flue gases need not be additionally heated for the denitrification reactions, but still have inherently sufficient energy contents, i.e. sufficiently high temperatures, to enable the operation of the catalyst. A reduction of fuels is thus feasible as compared to low-dust plants.
  • the first filter device can be arranged immediately following the furnace or a heat exchanger unit, viewed in the flow direction of the flue gases, such that the flue gases will enter the first filter unit at a very high temperature, whereby the temperature drop in this filter unit can be kept low—considered relatively—and the flue gases will leave the filter device at a temperature promoting the reduction of the nitrogen oxides on the catalyst.
  • a temperature of at least 250° C. is understood.
  • a desulfurization plant between the first filter device and the furnace, or a heat exchanger unit following thereupon, viewed in the flow direction of the flue gases, such that the sulfur content will at least be proportionally reduced and the risk of sulfur compounds depositing on the catalyst will be lowered.
  • the first filter device is comprised of an electric filter.
  • this filter can be operated at a high temperature and, on the other hand, this filter technology is already highly mature and electric filters are available, anyway, for instance, in cement production plants—dedusting formerly having been frequently performed with electric filters, yet the majority of those electric filters having been replaced with cloth filters due to tightened environmental regulations—and no additional investment costs will occur.
  • At least one raw material drying apparatus or raw material dry-grinding apparatus is arranged between the first filter device and the second filter device, in particular between the second filter device and the catalyst, viewed in the flow direction of the flue gases, such that the residual energy contents of the flue gases can be used for drying the raw materials which are, for instance, employed for the production of cement.
  • the flue gases leaving the catalyst bed will even be further cooled prior to entering the second filter device, which is preferably formed by a cloth filter, said second filter device thus being subjected to a reduced thermal stress even without applying additional cooling means.
  • the dust content of the flue gases in the first dust separation is preferably reduced to a maximum dust content of 3 g/Nm 3 , in particular 2.5 g/Nm 3 , for instance 1 g/Nm 3 , or a maximum dust content of 30 g/Nm 3 , respectively, if another pre-separation means, i.e. no electric filter, is used as said first filter device, since it has turned out that the efficiency of the plant can be enhanced by these maximum dust contents of the flue gases.
  • another pre-separation means i.e. no electric filter
  • the first dust separation at a temperature of the flue gas of at least 250° C. or at most 450° C., for instance at most 350° C., whereby, as already pointed out above, no special measures need to be taken to reduce the temperature drop in the first filter device, and the latter can hence be configured in a more cost-effective manner.
  • FIG. 1 illustrates a plant according to the invention in the form of a block diagram.
  • positional indications given in the description such as e.g. upstream, after or downstream, laterally etc., refer to the FIGURE actually described and illustrated and any positional change is to be analogously transferred to the new position.
  • FIG. 1 depicts a plant 1 for the production of cement clinker.
  • the nitrification plant according to the invention is not limited to its use in the cement industry, although this is the preferred variant embodiment. It is also possible to equip waste incineration plants, calorific power stations, etc. with the same.
  • the plant 1 comprises a furnace 2 in the form of a rotary kiln which is operated by a firing device 3 so as to produce cement clinker from known raw materials.
  • the gas purification plant comprises a first filter device 7 , a reduction catalyst 8 and a second filter device 9 .
  • the first filter device 7 is configured as an electric filter.
  • the flue gas entering the electric filter may optionally be pre-conditioned with water in order to increase the effectiveness of the electric filter.
  • a spray device 11 can be arranged in a supply line 10 leading to the first filter device 7 to spray water into the same.
  • the flue gas is diluted with with fresh air via a fresh-air duct 12 including a valve 13 , so as to enable an increase in the effectiveness of coarse dedusting through the electric filter.
  • a mixed gas can be supplied to the flue gas via a mixed-gas line 14 , for instance a gas derived from the furnace 2 , a so-called bypass gas, which can be drawn off the furnace 2 in the region of the heat exchanger unit 5 .
  • Appropriate conveying means 15 e.g. flue gas fans, can be arranged both in the mixed-gas line 14 and in the supply line 10 .
  • the dust content of the flue gas or crude gas is reduced by the first filter device 7 from 200 g/Nm 3 to 300 g/Nm 3 or 60 g/Nm 3 to 70 g/Nm 3 , respectively, to a maximum value of 3 g/Nm 3 and, preferably, 1 g/Nm 3 . It is also possible to reduce the dust content only to a maximum of 30 g/Nm 3 , if no electric filter but another pre-separation means is used as said first filter device 7 .
  • the first filter device 7 can be provided with a heat insulation suitable for such high temperatures so as to lower the decrease of the flue gas temperature.
  • the flue gas enters the reduction catalyst 8 , where the denitrification, i.e. the reaction of nitric oxides to nitrogen and water, takes place according to known reactions.
  • a reducing agent is fed to the pre-purified flue gas, using a reducing-agent feeder 16 .
  • the reducing agent is comprised of ammonia, as is known from the prior art.
  • the use of compounds containing ammonia or reducing agents releasing ammonia at elevated temperatures may also envisaged.
  • the reducing-agent feeder 16 may also be omitted if excess ammonia is present in the flue gas of the plant 1 , and, if there is insufficient ammonia, it is also possible to supplement the missing portion via the reducing-agent feeder 16 .
  • the catalyst may, for instance, be comprised of titanium dioxide or vanadium pentoxide or titanium oxide as the carrier and vanadium pentoxide as the active mass, optionally supplemented with tungsten oxide or mixed with other metal oxides.
  • these catalysts are known from the prior art so that any further discussion as to their geometries or pore structures can be obviated.
  • the supply of reducing agent again is, for instance, effected through spraying nozzles.
  • the reducing agent itself can be admixed to the flue gas up-stream of the catalyst, yet the reducing agent is preferably fed into or onto the catalyst bed.
  • the denitrified flue gas Via a line 17 , the denitrified flue gas—it should be noted here that by denitrified flue gas a flue gas is meant which, in terms of NO x , complies with the exhaust emission standards, e.g. the Austrian exhaust emission standards—reaches the second filter device 9 .
  • This second filter device 9 is configured as a bag filter comprising filter cloths or filter bags. Such bag filters are already known and used in the cement industry such that any further discussion can be obviated. By the aid of these filter cloths, the dust content of the flue gas is at least reduced to values complying with the exhaust emission standards.
  • a spray cooler 18 can be arranged upstream of the second filter device 9 to cool the flue gas prior to entering the second filter device 9 to a temperature, for instance a maximum temperature of 250° C., at which the thermal stress exerted on the filter cloth by the flue gas will be reduced.
  • the thus purified flue gases leave the plant 1 into the air via a stack 19 .
  • a conveying means 15 may again be arranged between the stack 19 and the second filter device 9 .
  • the residual energy contents of the flue gases leaving the reduction catalyst 8 are, however, preferably used to dry the raw materials used for cement production.
  • two drying mills 20 are illustrated in FIG. 1 , which are arranged between the reduction catalyst 8 and the second filter device 9 , viewed in the flow direction of the flue gases.
  • the two drying mills 20 are, in particular, arranged in parallel such that the denitrified flue gases will flow through the same either simultaneously or alternately.
  • Valves 21 - 24 are illustrated in FIG. 1 for the respective switching of the flow paths of the flue gases.
  • drying mills 20 in parallel with the direct introduction of the flue gases via line 17 into the second filter device 9 , to which end a valve 25 is again arranged in line 17 in order to enable switching between the flow directions via line 17 or via at least one of the drying mills 20 .
  • the drying mills 20 themselves are configured according to the prior art.
  • Another option is to supply fresh air via a fresh-air duct 26 to at least one of the drying mills 20 , a respective fresh-air valve 27 being arranged in the fresh-air duct 26 also in this case.
  • the denitrified flue gas will reach the second filter device 9 at a temperature of about 150° C.
  • Dust content of the flue gas leaving the furnace 2 and/or the heat exchanger 5 60 to 120 g/Nm 3
  • Dust content of the flue gas leaving the electric filter max. 3 g/Nm 3
  • Dust content of the flue gas at the entry into the bag filter less than 3 g/Nm 3 with direct introduction and about 100 g/Nm 3 with “mill operation”, respectively
  • Dust content of the flue gas when leaving the bag filter 10 mg/Nm 3
  • the dust content of the flue gas is practically not reduced in the reduction catalyst 8 . If, however, a dust precipitate does occur in the reduction catalyst 8 , this can be periodically cleaned, e.g. by purging with compressed air.
  • nitric oxides also the flue gas of carbon monoxide from, particularly odor-forming, hydrocarbons and/or the removal of ammonia from flue gases from combustion furnaces, particularly from plant 1 .
  • a separate catalyst can, if required, be arranged upstream or downstream of the denitrification catalyst, comprising, for instance, titanium-vanadium compounds which may be supplemented with palladium and/or platinum.
  • the denitrification catalyst comprising, for instance, titanium-vanadium compounds which may be supplemented with palladium and/or platinum.
  • the reduction catalyst 8 can be configured as a layered catalyst including several beds for the individual catalysts, or several catalysts can be separately arranged in the plant 1 or a respective flue gas purification plant, for instance, one behind the other in separate containers, viewed in the flow direction of the flue gases.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical & Material Sciences (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)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Electrostatic Separation (AREA)
  • Treating Waste Gases (AREA)
US12/863,248 2008-01-16 2009-01-15 Flue gas purification plant Abandoned US20100307388A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
ATGM31/2008 2008-01-16
AT0003108U AT10369U1 (de) 2008-01-16 2008-01-16 Rauchgasreinigungsanlage
PCT/AT2009/000010 WO2009089559A1 (de) 2008-01-16 2009-01-15 Rauchgasreinigungsanlage

Publications (1)

Publication Number Publication Date
US20100307388A1 true US20100307388A1 (en) 2010-12-09

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US12/863,248 Abandoned US20100307388A1 (en) 2008-01-16 2009-01-15 Flue gas purification plant

Country Status (7)

Country Link
US (1) US20100307388A1 (zh)
EP (1) EP2237861A1 (zh)
CN (1) CN101977668A (zh)
AT (1) AT10369U1 (zh)
BR (1) BRPI0907170A2 (zh)
RU (1) RU2484883C2 (zh)
WO (1) WO2009089559A1 (zh)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110104628A1 (en) * 2008-03-25 2011-05-05 Agc Glass Europe Glass melting furnace
US20120247371A1 (en) * 2011-04-04 2012-10-04 Thyssenkrupp Polysius Ag Method and installation for producing cement clinker
WO2013019393A1 (en) * 2011-07-29 2013-02-07 Flsmidth A/S Pollution control system for kiln exhaust
US20140087319A1 (en) * 2011-05-27 2014-03-27 Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH Method and Device for Producing Cement Clinker
US20160339381A1 (en) * 2014-01-27 2016-11-24 Thyssenkrupp Industrial Solutions Ag Method for heat-treating a material flow and for cleaning resulting exhaust gases
US9855527B2 (en) 2013-11-06 2018-01-02 Thyssenkrupp Industrial Solutions Ag Method for cleaning bypass gases of the cement or mineral industry, and system of the cement or mineral industry
CN108426263A (zh) * 2018-03-28 2018-08-21 清华大学 燃煤烟气处理系统
WO2021083426A3 (zh) * 2020-12-21 2021-11-11 苏州喜全软件科技有限公司 一种印染锅炉废气处理装置
CN114870620A (zh) * 2022-05-07 2022-08-09 北京京西燃气热电有限公司 一种柔性接触式密封装置
CN116747643A (zh) * 2023-08-24 2023-09-15 山西毅诚科信科技有限公司 一种新型水泥窑脱硝除尘装置

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DE102009022903A1 (de) * 2009-05-27 2010-12-09 Polysius Ag Verfahren und Anlage zur Wärmebehandlung von feinkörnigem Material
DE102010036647B3 (de) 2010-07-27 2012-01-19 Elex Cemcat Ag Rauchgasreinigungsanlage einer Zementklinkerproduktionsanlage
DE102011000564B4 (de) 2011-02-08 2013-05-02 Elex Cemcat Ag Verfahren und Anlage zur Herstellung von Zementklinker
AT510406B1 (de) * 2011-04-04 2012-04-15 Scheuch Gmbh Schlauchfilter zur reinigung staubbelasteter gase und injektordüse für ein solches schlauchfilter
DE102011001933B4 (de) 2011-04-08 2013-02-28 Elex Cemcat Ag Verfahren und Anlage zur Herstellung von Zementklinker und zur Reinigung der dabei entstehenden Abgase
DE102011050125B4 (de) * 2011-05-05 2019-04-18 Maerz Ofenbau Ag Rauchgasreinigungsanlage einer Zementklinkerproduktionsanlage
CN102935331A (zh) * 2011-08-15 2013-02-20 上海索菲玛汽车滤清器有限公司 用于还原废气中的氮氧化物的设备
CN102661667A (zh) * 2012-05-31 2012-09-12 河南中材环保有限公司 一种水泥窑炉脱硝、余热利用及除尘系统及方法
DE102013016701B4 (de) * 2013-10-08 2017-06-14 Khd Humboldt Wedag Gmbh Verfahren zur Entstickung von Bypassabgasen in einer Anlage zur Herstellung von Zementklinker und Anlage zur Herstellung von Zementklinker
PL3002051T4 (pl) * 2014-10-03 2020-07-27 General Electric Technology Gmbh Odpylacz użyteczny z reaktorem płuczkowym do oczyszczania spalin na sucho
DE102015202698B4 (de) 2015-02-13 2020-11-05 Maerz Ofenbau Ag Verfahren zur Reinigung von Abgasen bei der thermischen Aufarbeitung von Mineralstoffen
CN107781834A (zh) * 2016-08-30 2018-03-09 中国辐射防护研究院 一种废浸渍活性炭焚烧处理装置及方法
DE102016119695A1 (de) * 2016-10-17 2018-04-19 Thyssenkrupp Ag Verfahren und Anlage zur Reinigung von Vorwärmerabgasen einer Anlage der Zement- und/oder Mineralsindustrie
AT17408U1 (de) * 2021-03-24 2022-03-15 Scheuch Man Holding Gmbh Vorrichtung und Verfahren zur Herstellung von Zementklinker
CN113069920A (zh) * 2021-05-08 2021-07-06 中材萍乡水泥有限公司 一种水泥生产超低排放脱硝设备
CN114471108B (zh) * 2022-02-14 2022-12-27 北京科技大学 工业烟气同步脱碳脱硝及余热回收利用的装置

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US4307068A (en) * 1977-08-31 1981-12-22 Mitsubishi Jukogyo Kabushiki Kaisha Method and apparatus for treating an exhaust gas
US4744967A (en) * 1986-01-18 1988-05-17 Degussa Aktiengesellschaft Process for the purification of exhaust gases containing oxides of nitrogen and sulfur
US5259863A (en) * 1991-05-28 1993-11-09 Deutsche Babcock Anlagen Gmbh Method and apparatus for the incineration of garbage and refuse
US6395237B1 (en) * 2000-02-13 2002-05-28 The Babcock & Wilcox Company Circulating fluidized bed reactor with selective catalytic reduction
US20040042946A1 (en) * 2000-12-04 2004-03-04 Gilles Vicard Method and installation for purifying cement plant fumes
US7198698B1 (en) * 2001-05-02 2007-04-03 Air Control Techniques, P.C. Method of photochemically removing ammonia from gas streams
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Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9150446B2 (en) * 2008-03-25 2015-10-06 Agc Glass Europe Glass melting furnace
US20110104628A1 (en) * 2008-03-25 2011-05-05 Agc Glass Europe Glass melting furnace
US20120247371A1 (en) * 2011-04-04 2012-10-04 Thyssenkrupp Polysius Ag Method and installation for producing cement clinker
US9067827B2 (en) * 2011-04-04 2015-06-30 Thyssenkrupp Industrial Solutions Ag Method and installation for producing cement clinker
US9873635B2 (en) * 2011-05-27 2018-01-23 Sudbayerisches Portland-Zementwerk Gebr. Wiesbock & Co. Gmbh Method and device for producing cement clinker
US20140087319A1 (en) * 2011-05-27 2014-03-27 Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH Method and Device for Producing Cement Clinker
WO2013019393A1 (en) * 2011-07-29 2013-02-07 Flsmidth A/S Pollution control system for kiln exhaust
US9855527B2 (en) 2013-11-06 2018-01-02 Thyssenkrupp Industrial Solutions Ag Method for cleaning bypass gases of the cement or mineral industry, and system of the cement or mineral industry
US20160339381A1 (en) * 2014-01-27 2016-11-24 Thyssenkrupp Industrial Solutions Ag Method for heat-treating a material flow and for cleaning resulting exhaust gases
US9914093B2 (en) * 2014-01-27 2018-03-13 Thyssenkrupp Industrial Solutions Ag Method for heat-treating a material flow and for cleaning resulting exhaust gases
CN108426263A (zh) * 2018-03-28 2018-08-21 清华大学 燃煤烟气处理系统
WO2021083426A3 (zh) * 2020-12-21 2021-11-11 苏州喜全软件科技有限公司 一种印染锅炉废气处理装置
CN114870620A (zh) * 2022-05-07 2022-08-09 北京京西燃气热电有限公司 一种柔性接触式密封装置
CN116747643A (zh) * 2023-08-24 2023-09-15 山西毅诚科信科技有限公司 一种新型水泥窑脱硝除尘装置

Also Published As

Publication number Publication date
RU2010134000A (ru) 2012-02-27
CN101977668A (zh) 2011-02-16
RU2484883C2 (ru) 2013-06-20
BRPI0907170A2 (pt) 2017-06-06
EP2237861A1 (de) 2010-10-13
AT10369U1 (de) 2009-02-15
WO2009089559A1 (de) 2009-07-23

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