EP0804271A1 - PROCEDE D'EPURATION DE GAZ DE COMBUSTION AVEC DES CATALYSEURS AU DeNOx A DES TEMPERATURES INFERIEURES A 150o C - Google Patents

PROCEDE D'EPURATION DE GAZ DE COMBUSTION AVEC DES CATALYSEURS AU DeNOx A DES TEMPERATURES INFERIEURES A 150o C

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Publication number
EP0804271A1
EP0804271A1 EP96902926A EP96902926A EP0804271A1 EP 0804271 A1 EP0804271 A1 EP 0804271A1 EP 96902926 A EP96902926 A EP 96902926A EP 96902926 A EP96902926 A EP 96902926A EP 0804271 A1 EP0804271 A1 EP 0804271A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
deno
catalysts
combustion gases
dust
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Withdrawn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
EP96902926A
Other languages
German (de)
English (en)
Inventor
Peter Dransfeld
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Publication of EP0804271A1 publication Critical patent/EP0804271A1/fr
Withdrawn legal-status Critical Current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
    • F23J15/02—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
    • 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
    • B01D53/8659—Removing halogens or halogen compounds
    • B01D53/8662—Organic halogen compounds
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/92—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • 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 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F23J2215/301—Dioxins; Furans
    • 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
    • F23J2215/60—Heavy metals; 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 invention relates to a method for the reduction of chlorosulfonic organic products of incomplete combustion and of Queck ⁇ silver in combustion exhaust gases under oxidative conditions DA, by in that at a temperature below 150 ° C with a De O x catalyst in the combustion exhaust gases Contact brings.
  • PIC Products of Incomplete Combustion
  • Part of these PIC's are organohalogen compounds (chlorobenzenes, chlorophenols, polychlorinated biphenyls, polyhalogenated (chlorine, bromine) dibenzodioins and dibenzofurans etc.). These compounds are toxic, are extremely difficult to degrade and are therefore harmful to the environment, with late damage in particular being feared.
  • the polyhalogenated dibenzodioxins and dibenzofurans (hereinafter collectively and briefly referred to as "dioxins *) are of particular importance with regard to the potential health risk of emissions from incineration plants.
  • EP-A 559 071 describes a process with which dioxins are adsorbed on a catalyst in a first stage at temperatures from 100 to 150 ° C. and in a second stage at a temperature which is at least 50 ° C. higher, in particular at more than 300 ° C can be reduced.
  • the catalytic stage for the removal of dioxins is operated, for example, after the stage of the aqueous flue gas scrubbing, a great deal of energy is required in order to heat the flue gases from below 100 ° C. to the working temperature of the catalyst.
  • elemental mercury present in the flue gas is oxidized catalytically, but the mercury compounds that arise in the process, such as HgO, HgCl or HgS0, are retained less due to their vapor pressure, the higher the working temperature of the catalyst, so that an additional separation stage for the mercury compounds is needed.
  • incineration plants such as domestic waste and special waste incineration plants are currently equipped with cloth filters. These filters are usually operated at temperatures between 100 to 145 ° C.
  • An adsorbing filter auxiliary layer is applied to the filters to reduce dioxin emissions.
  • wear which usually consists of a dusty lime / coke or lime / activated carbon mixture. This mixture has to be made expensive for this purpose and disposed of after use at high cost and with a high level of safety.
  • the lime content in the mixture is approximately 70% to 98%.
  • the lime further reduces the trace concentrations of acidic noxious gases such as HC1, HBr and S0 2 to a certain extent, it essentially serves to inertize the combustible or even explosive coal dust.
  • flammable adsorbent increases the amount and cost of the material to be disposed of.
  • handling flammable or explosive materials also requires expensive safety precautions.
  • non-combustible mineral materials can also be used. These have a lower adsorption capacity for dioxins compared to coal, so that ultimately comparable amounts have to be disposed of.
  • the mineral materials known so far for dioxin adsorption often have the further disadvantage that they are not suitable for the adsorption of heavy metals, in particular elemental mercury.
  • Oxygen is generally sufficient as an oxidizing agent.
  • Other oxidizing agents such as H 2 0 are usually not required.
  • the process is therefore carried out in such a way that sufficient oxygen is present so that the oxygen sorption outweighs the sorption 0 of possibly added reducing substances such as NH 3 , CH or H 2 S, for example 0 2 6%, NH 3 ⁇ 30 ppm .
  • a 0 2 content of 0.5 to 21, preferably 3 to 21, in particular 6 to 12% by volume is used.
  • the dwell time ⁇ is to be understood as the time in which the catalyst is exposed to oxidative conditions at the selected operating temperature.
  • the period during which the catalyst 0 is in contact with the organochlorine products of incomplete combustion can be shorter than the residence time ⁇ in the two-stage process described below.
  • the weight-average grain diameter pso measured according to DIN 66 111, is between 1 and 200 ⁇ , preferably 5 to 150 and in particular 10 and
  • weight-average grain diameter is between 10 and 5000 ⁇ m, preferably 50 and 3000 ⁇ m and in particular 100 and 2000 ⁇ m. This can hardly be achieved, for example, by conventional grinding processes.
  • the ratio of the specific inner surface according to BET Fi, sp to the specific enveloping geometric surface F u , sp of the catalyst can be important in some cases. Then it is advantageous if the specified ratio of specific BET surface area to specific enveloping surface area is selected such that it obeys the exponential equation (2):
  • Fi'sp specific inner surface of the catalyst used measured according to BET, for example DIN 66 132 in m 2 / g F u
  • sp specific enveloping geometric surface of the catalyst used in m 2 / g, which is wetted by the fluid becomes. This area can be calculated directly in the case of catalyst bodies with a defined geometry. In the case of beds of spherical catalysts, for example, it is the ball surface that can be calculated from the ball diameter, divided by the weight of the catalyst bed.
  • F u , S p is determined in a corresponding manner from the particle size distribution and the generally known form factor in a manner known to the person skilled in the art (see, for example, Perry's Chemical Engineer's Handbook 6th ed. Section 4, » Reactor Design: Basic Principles and Data “and Section 5; Davidson Clift, Harrison” Fluidization “2nd ed. (1985) Academic Press; M. Leva” Fluidization “McGraw-Hill (1959)).
  • kads mass transfer coefficient gas-catalyst surface in m / s. It can be determined in a known manner according to equation (3).
  • the temperature-dependent diffusion coefficient D is determined in a known manner (see, for example, VDI Warmth Atlas, 4th edition, 1988, Da 32 / Da 33) and is, for example, at 130 ° C. for tetrachlorodibenzodioxin 0.094 cm 2 / s, for hexachlorodibenzodioxins 0.087 cm 2 / s, for octachlorodibenzodioxins 0.082 cm 2 / s and for hexachlorodibenzofurans 0.088 cm 2 / s.
  • the catalyst is usually used in arrangements such as fixed bed, moving bed, rotor adsorber, fluidized bed, circulating fluidized bed or in particular filter layer, for example in a cloth filter, if appropriate with internal or external dust recycling under oxidative conditions with the combustion. exhaust gas and thus brought into contact with the organochlorine products of incomplete combustion.
  • the catalyst dust is advantageously mixed into the combustion exhaust gases by means of suitable apparatuses such as compressed air injectors in the exhaust gas duct.
  • the flow rate here is usually 10 to 30 m / s and is turbulent, so that the catalyst, like the ash contained in the exhaust gas, practically does not settle. Its concentration is usually 50 to 500, preferably 100 to 300 mg / m 3 .
  • the catalyst dust is filtered out of the flue gas, for example using conventional cloth filters. Good results are achieved if the filtered-out catalyst is partially, for example 50 to 95%, returned to the exhaust gas in order to increase the contact and residence time.
  • the method according to the invention can also be carried out in two stages.
  • the catalyst is loaded with the incomplete combustion of the organochlorine products and regenerated in a second step under oxidative conditions.
  • the loaded catalyst can be filtered out of the flue gas by, for example, cyclones or cloth filters and discharged in a silo where the second step (regeneration) takes place under oxidative conditions.
  • the residual oxygen of the combustion gases or additionally introduced atmospheric oxygen can be used for regeneration, for example.
  • the loading step can be carried out under oxidative conditions. However, this is not absolutely necessary.
  • both steps can be operated at the same temperature.
  • the duration of the regeneration ⁇ (seconds) in the second step is often chosen in accordance with the above relation (1).
  • DeNO ⁇ catalysts have been known for a long time and are used for the catalytic reduction of nitrogen oxides NO x with ammonia in nitric acid plants and large combustion plants.
  • the DeNO x catalysts and their manufacture are described, for example, in VDI Report No. 730, 1989, pages 121 to 156, and in
  • DeNO ⁇ catalysts of the titanium oxide type, iron oxide or zeolite type, which may contain conventional donors come into consideration.
  • Titanium oxide catalysts are preferred, in particular those with a titanium oxide content of> 70% by weight, based on the total weight of the catalyst.
  • the modified DeNOx catalysts are those which additionally contain nickel, chromium, copper and / or cobalt oxides as donors. They are contained in an amount of 0.1 to 10% by weight, preferably 0.5 to 5% by weight, based on the total weight of the catalyst.
  • Catalysts containing donor tungsten oxide (WO 3 ), molybdenum oxide (MOO 3 ) and / or in particular vanadium oxide (V 2 ⁇ 5 > are particularly preferred.
  • the type and amount of the additives are chosen so that the conversion rate mentioned and the Degradation rate can be increased.
  • the amount of donors is generally at least 0.5% by weight, preferably 1 to 20% by weight.
  • compositions for catalysts used according to the invention are
  • M0O3 0 to 5%, preferably 0 to 4%
  • fillers e.g. glass fiber, clay, possibly SO 4 .
  • the catalysts generally have the following data:
  • Pore volume 100 to 400 mm 3 / g BET surface area: 20 to 100 m 2 / g according to the pore radius: 50 to 200 A.
  • DeNO x catalysts ie exhausted for denitrification
  • these catalysts are particularly preferred.
  • a particular advantage of the process according to the invention is that it can also be used to reduce the mercury content in combustion exhaust gases at the same time to reduce chlorine-organic products from incomplete combustion.
  • Mercury is reduced particularly well if there is a comparatively large amount of sulfur dioxide (10 to 100 mg / Nm 3 ) in the flue gas.
  • Particularly good mercury reduction properties are achieved if 5 to 50 parts by weight of VOs and / or W0 3 are added to 100 parts by weight of the above-mentioned catalyst compositions.
  • the S0 concentration in the flue gas before the cloth filter was 4 mg / m 3 .
  • the dioxin concentration was determined according to known methods in the flue gas before and after the cloth filter and in the removed filter dust.
  • the concentration after the cloth filter was always below 0.1 ng / m 3 .
  • a dioxin balance around the cloth filter with the catalytically active filter auxiliary layer was created from the measured flue gas and filter dust mass flows. The one in the filter dust discharge The dioxin concentration measured only made up 7% of the concentration to be expected on the basis of the balance.
  • Mercury was determined using the method described by Braun, Metzger, Vogg in Rubbish and Waste 18, pages 62 to 71 and pages 89 to 95 (1986) (see also Braun, Metzger Chemosphere 16, page 821 ff (1987)). The method allows a separate determination of elemental mercury (H g ) and mercury compounds (HgVerb)
  • the sulfur dioxide concentration in the flue gas upstream of the cloth filter was 45 mg / m 3 in this case.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (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

Un procédé permet de réduire dans des conditions d'oxydation la teneur en produits chlorés organiques de gaz d'échappement qui résultent d'une combustion imparfaite. Le procédé se caractérise en ce que l'on met les gaz d'échappement en contact avec un catalyseur au DeNOx à une température inférieure à 150 °C.
EP96902926A 1995-02-11 1996-01-26 PROCEDE D'EPURATION DE GAZ DE COMBUSTION AVEC DES CATALYSEURS AU DeNOx A DES TEMPERATURES INFERIEURES A 150o C Withdrawn EP0804271A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE1995104597 DE19504597A1 (de) 1995-02-11 1995-02-11 Verfahren zur Reinigung von Verbrennungsabgasen mit DeNO¶x¶-Katalysatoren bei Temperaturen unterhalb von 150 DEG C
DE19504597 1995-02-11
PCT/EP1996/000320 WO1996024433A1 (fr) 1995-02-11 1996-01-26 PROCEDE D'EPURATION DE GAZ DE COMBUSTION AVEC DES CATALYSEURS AU DeNOx A DES TEMPERATURES INFERIEURES A 150 °C

Publications (1)

Publication Number Publication Date
EP0804271A1 true EP0804271A1 (fr) 1997-11-05

Family

ID=7753736

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96902926A Withdrawn EP0804271A1 (fr) 1995-02-11 1996-01-26 PROCEDE D'EPURATION DE GAZ DE COMBUSTION AVEC DES CATALYSEURS AU DeNOx A DES TEMPERATURES INFERIEURES A 150o C

Country Status (3)

Country Link
EP (1) EP0804271A1 (fr)
DE (1) DE19504597A1 (fr)
WO (1) WO1996024433A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0908221A1 (fr) * 1997-09-16 1999-04-14 Siemens Aktiengesellschaft Catalyseur et procédé pour la réduction des dioxines à basse température
EP0908222A1 (fr) * 1997-09-16 1999-04-14 Siemens Aktiengesellschaft Procédé pour la réduction à température basse des dioxines dans un gaz d'échappement d'une installation technique
DE19745043A1 (de) * 1997-10-11 1999-04-15 Katalysatorenwerke Huels Gmbh Verfahren zur Zerstörung von organischen Halogenverbindungen in staubhaltigen Gasen bei niedriger Temperatur
JP4570783B2 (ja) * 1998-11-09 2010-10-27 アルギロン ゲゼルシャフト ミット ベシュレンクテル ハフツング ハロゲン化炭化水素を低減するための触媒体及びその方法

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
HUT60937A (en) * 1989-10-06 1992-11-30 Babcock Anlagen Ag Method for separating orgqnic combustion products originating because of imperfect firing particularly from the exhaust gas of burning apparatus
DE4206599A1 (de) * 1992-03-03 1993-09-09 Basf Ag Metalle und/oder oxide enthaltende katalysatorelemente und verfahren zum oxidativen abbau von cyclischen organischen verbindungen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9624433A1 *

Also Published As

Publication number Publication date
WO1996024433A1 (fr) 1996-08-15
DE19504597A1 (de) 1996-08-14

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