EP0241496A1 - Procede d'elimination simultanee de so 2? et de no x? contenus dans des gaz de fumee - Google Patents

Procede d'elimination simultanee de so 2? et de no x? contenus dans des gaz de fumee

Info

Publication number
EP0241496A1
EP0241496A1 EP86905803A EP86905803A EP0241496A1 EP 0241496 A1 EP0241496 A1 EP 0241496A1 EP 86905803 A EP86905803 A EP 86905803A EP 86905803 A EP86905803 A EP 86905803A EP 0241496 A1 EP0241496 A1 EP 0241496A1
Authority
EP
European Patent Office
Prior art keywords
scrubber
washing
nox
gas
washing liquid
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Withdrawn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
EP86905803A
Other languages
German (de)
English (en)
Inventor
Heinrich IGELBÜSCHER
Heinrich Gresch
Heribert Dewert
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.)
Holter Heinz Dipl-Ing
Original Assignee
Holter Heinz Dipl-Ing
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 DE19853536312 external-priority patent/DE3536312A1/de
Priority claimed from DE19853537949 external-priority patent/DE3537949A1/de
Priority claimed from DE19853537948 external-priority patent/DE3537948A1/de
Priority claimed from DE19853538136 external-priority patent/DE3538136A1/de
Priority claimed from DE19853540973 external-priority patent/DE3540973A1/de
Priority claimed from DE19853541323 external-priority patent/DE3541323A1/de
Priority claimed from DE19853541471 external-priority patent/DE3541471A1/de
Priority claimed from DE19853543843 external-priority patent/DE3543843A1/de
Priority claimed from DE19853545190 external-priority patent/DE3545190A1/de
Priority claimed from DE19853546112 external-priority patent/DE3546112A1/de
Priority claimed from DE19853546122 external-priority patent/DE3546122A1/de
Application filed by Holter Heinz Dipl-Ing filed Critical Holter Heinz Dipl-Ing
Publication of EP0241496A1 publication Critical patent/EP0241496A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • C04B11/00—Calcium sulfate cements
    • C04B11/05—Calcium sulfate cements obtaining anhydrite, e.g. Keene's cement
    • 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
    • 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
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • 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
    • B01D53/60—Simultaneously removing sulfur oxides and 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
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/20—Halides
    • C01F11/24—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/46—Sulfates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/46—Sulfates
    • C01F11/464—Sulfates of Ca from gases containing sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/48—Sulfites
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • the invention relates to a method for single or multi-stage simultaneous SO2 and NOx separation from flue gases in a wet process.
  • the object of the invention is to improve such a method in such a way that it can be carried out with comparatively little effort, the maximum value prescribed by the authorities still being significantly below.
  • SO2 absorbed in the process which is precipitated as lime as CaSO3 / CaSO4 x 2H2O solid, no longer to be oxidized to CaSO4 x 2H2O via an oxidizer, but rather to the washing liquid stream of a prewash stage for the oxidation of the CaSO3 amount by means of Add oxygen to the amount of flue gas at a pH in the wash solution of pH 2 - 2.5.
  • the solid is passed to the scrubber or laundry sump of the prewash stage and contacted with the washing liquid at a corresponding pH value (pH 1-1.5) until the corresponding amount of SO2 is released, which is used to react the Siraultan washing of SO2 / NOx in which washer is needed.
  • SO2 and NOx be fed from the raw gas to a first scrubber that the SO2 is washed out by sodium sulfite (in the washing water) with the formation of sodium bisulfite (NaI-ISO3) and the gas freed from SO2, but loaded with NOx, is fed to a second scrubber, that in the second scrubber an iron EDTA washing solution, which is enriched with SO2 rich gas, is used for NOx scrubbing and pure gas is produced, which is released, the washing liquid from the first scrubber being transferred to a crystallizer from which sodium sulfate is released.
  • the SO2 rich gas generated in the process is handed over to its use, with partial quantities being introduced into the second scrubber to reduce the NOx compounds and the iron chelate complex compound.
  • a portion of the wash solution is passed from the second scrubber to thermal decomposition at about 650 degrees C to destroy U.S. compounds, with the amounts of SO2 released being sent to the scrubber and sodium sulfate being rejected from the process.
  • the raw gas which is enriched in particular with HCl and KF, is freed of HCl and / or HF in a pre-washer and SO2 and NOx in a first washer simultaneously with a specific washing solution , which is provided with an iron-EDTA complex, is washed.
  • a specific washing solution which is provided with an iron-EDTA complex
  • the washing liquid treated reducing in the circulation container quantity is transferred to the quantity of washing liquid for simultaneous SO2 and NOx washing.
  • the SO2 which has been freed of NOx and partially required to reduce NOx, and which was extracted from the raw gas, passes into a second scrubber as SO2-contaminated gas. It is washed with sodium sulfite SO2 and a part of it is discharged into the circulation tank.
  • the gas freed from SO2 and NOx leaves the process as clean gas.
  • a part of the first scrubber is fed as a washing liquid to a crystallization evaporator, from which SO2 rich gas is released.
  • Sodium sulfate is released from the crystallization evaporator.
  • the evaporation residue of the crystallization evaporator is transferred to thermal decomposition as a partial quantity and the SO2 released in the process is fed to the first scrubber or added to the SO2 rich gas.
  • Sodium sulfate is removed from the thermal decomposition.
  • a portion of the crystallization evaporator, which is not fed to the thermal decomposition, is returned to the first scrubber.
  • an anhydrite-shaped solid product is obtained, which is used as an economic good, preferably in underground mining as a dam building material.
  • a portion of the filtrate is supplied to an evaporation from a dewatering station downstream of the gravity separator.
  • the NS salts are decomposed separately at approx. 650 degrees and fed to the simultaneous washer.
  • the solids calcium sulfate and sulfite are thermally decomposed separately at approx. 750 degrees Celsius. After the decomposition, an anhydrite-like building material without alkali falls salt on.
  • washing liquid with an iron chelate compound without the addition of a chloride wash in used a single scrubber, the washing liquid is fed in portions to an electrolysis, in which the iron III is reduced to iron II and at the same time the current is driven so that the alkali metal chloride is practically split and decomposed to chlorine gas, the chlorine gas being collected and one Recycling can be supplied and the alkali hydroxide is used for washing SO2 from the flue gas.
  • pre-scrubber is added to the actual SO2 and NOx scrubbing to remove the acidic components HCl, HF etc. to wash out beforehand.
  • the salt load that is inevitably generated in the pre-washer must not usually be handed over to a river or an outflow, but must be evaporated and used for other purposes or sent to a landfill.
  • the gypsum which is processed into mining building materials or other building materials, for example, often has to be provided with an additional chloride addition in order to have the appropriate properties. Often the gypsum also has to be put into interim storage, in order to then correspond to the Chlorine levels are subjected to further processing.
  • the raw gas scrubbing in one Prewashing takes place, which is operated with an acidic pH, in which chlorides are washed out of the raw gas stream and in a postwashing unit downstream of the prewashing unit, into which SO2 and / or NOx is washed, the absorbents for washing SO2 and NOx being fed to the postwashing unit and the product obtained from the post-scrubber, consisting of not fully oxidized CaSO3 / CaSO4, is pumped into the pre-scrubber and a good oxidation and good mixture of the chlorides
  • gypsum can only be marketed with minor traces of calcium.
  • Chloride can be used as a dust binder in mining, for example.
  • the iron-II resistance in the Fe-EDTA complex is considerably more stable. It is therefore proposed according to the invention that the amount of manganese in the iron (II) salts should be kept at 0.05%, calculated on a dry basis, and the usual 0.14% dry basis. Wash-out degrees of better than 10% at 0.05% in the iron II salt over 0.14% in the iron II salt, measured dry, were achieved.
  • the washing liquid is enriched with an Fe concentration of 5 - 6.5 g / l, in which case the Fe-II content must be greater than 90% with a washing-out degree of more than 2 g / l washing solution and with a washing-out degree of 80% approximately with less than 2 g / l washing solution, whereby the total content of Fe-II and Fe-III must be kept at 5 - 6.5 g / l.
  • carboxylic acids preferably formic acid, citric acid and tartaric acid, contribute to the substantial improvement of the conductivity.
  • reducing agents are added to the iron chelation process in order to convert iron III back into iron II.
  • a reducing agent is often used, which is in powder form or in glycolized paste.
  • the powder form is usually difficult to handle and convey.
  • the pumpable mass of glycol interferes with the water treatment process.
  • FIG. 1 shows a method with gypsum production and SO2 release
  • FIG. 2 shows a process with the end product sodium sulfate
  • FIG. 3 shows a method for cleaning flue gases with high SO2 loads
  • FIG. 4 shows a method with recovery of valuable materials
  • Figure 5 shows a process for combustion products with a very high chlorine content
  • Figure 6 shows a process with gypsum discharge and calcium chloride extraction.
  • 1 denotes the pre-washer, which is operated acidic, preferably with a pH between 1-2, for washing HCl and HF. SO2 / NOx is washed out simultaneously in the main scrubber 2.
  • the value Fabric recovery with a gypsum precipitation stage is denoted by 3.
  • the precipitated mixture consisting of CaSOS, CaSO4 and traces of pure CaO, is fed to the pre-scrubber I via the outlet 4.
  • pre-washer 1 Due to the acidic pH value, pre-washer 1 and in the subsequent sump the mixture of CaSO4 and CaSO3 is oxidized to CaSO4 x 2H2O by the excess oxygen additionally contained in the raw gas.
  • the missing amount of SO2, which is required for the reaction of the SO2 / NOx-Sinultan wash, is so far acidified in the prewash for HCl / HF by lowering the pH value and the residence time of the mixture of CaSO3 / CaSO4 in the laundry sump so increased that by decomposing CaSO3 enough SO2 is released to allow the reactions in the simultaneous washer 2 to proceed safely.
  • 11 denotes the first scrubber for the SO2 and NOx raw gas intake.
  • the first scrubber 11 only SO2 is separated off over a sodium sulfite solution, with the formation of sodium bisulfite (NaHSO3).
  • the gas, cleaned of SO2 is washed in the second scrubber 12 with an EDTA solution which is mixed with sulfite and / or additional formate solutions.
  • the SO2 and NOx-cleaned gas leaves the washing zone via outlet 13.
  • SO2 pure gas is expelled from the sodium bisulfite wash solution from the first scrubber 11 at the temperature mentioned, which leaves the process via the outlet 16 as rich gas.
  • Sodium sulfate (Na2SO4) is discharged from the crystallizer 15 via the outlet 20.
  • a portion of the SO2 rich gas is introduced into the second scrubber 12 via outlet 14 to reduce Fe-III to Fe-II and reduce NOx to nitrogen from Sul uat.
  • the N / S salts formed are burned at about 650 ° C. and the residue sodium sulfate is released via the outlet 18.
  • the released SO2 is transferred to the first scrubber 11 via the outlet 19.
  • the raw gas 21, which is enriched in particular with HCl and HF, is freed of HCl and / or HF in a pre-scrubber 22.
  • SO2 and NOx are washed simultaneously with a specific washing solution which is provided with an iron-EDTA complex.
  • Part of the amount of washing liquid 24 in circulation is transferred to a circulation container 25, into which reducing agents 26 are added as required.
  • the amount of washing liquid treated in a reducing manner in the circulation tank 25 is transferred via a line 27 to the washing liquid amount for the simultaneous washing SO2 and NOx.
  • the SO2 that has been freed from NOx and partially required to reduce NOx and that was extracted from the raw gas goes into the second scrubber 29 as SO2-contaminated gas 28.
  • SO2 is washed with sodium sulfite and a portion is discharged into the circulation container 25.
  • a portion 31 is fed from the first washer 23 to the crystallization evaporator 32 as washing liquid. SO2 rich gas is released from these via outlet 33.
  • the evaporation residue 35 is a subset of a thermal decomposition 36 and the released SO2 is fed to the first scrubber 23 or the SO2 rich gas outlet 33.
  • sodium sulfate is also removed from the thermal decomposition.
  • 41 denotes the incoming raw gas which is introduced into the scrubber 42 of the simultaneous washing.
  • 43 is the EDTA addition, which opens into the washer 42.
  • the scrubber 42 is followed by a lime precipitate 45, into which the addition 44 of lime hydrate and reducing agents is also carried out.
  • the sulfur dioxide is supplied to the lime precipitate 45 after the simultaneous washing.
  • the solid precipitated with lime as calcium sulfite-calcium sulfate enters the gravity separator 46 as a suspension, which can be designed as a double-jacket sink separator.
  • the Separator 46 is followed by a dewatering station 47 and this in turn is followed by a thermal decomposition 50.
  • a partial amount of the filtrate from the dewatering station 47 enters an evaporation 49.
  • the raw gas which is introduced into the pre-scrubber 62 is denoted 61.
  • the raw gas is washed with an acidic pH, preferably below pH 5.
  • the SO2 and / or SO2 and NOx scrubber 63 is preferably operated above pH 5.
  • the clean gas leaves the scrubber 63 via the chimney 64.
  • the mixture removed from the scrubber 63, which originates from the lime suspension used in the scrubber 63, is designated by 65. This consists of CaSO3 / CaSO4 that is not completely oxidized. This is pumped into the pre-washer 62 via the line 66.
  • 71 denotes the upstream chloride spray tower, which is followed by the actual flue gas scrubber 72.
  • 72 a drum vacuum filter with gypsum washing station is designated and with 74 the return of the gypsum washing water into the spray and quench absorber 71.
  • the salts 75 obtained are drawn off below the spray and quench absorber 71.
  • the discharged, washed raw gypsum is designated 76.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Geology (AREA)
  • Biomedical Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Ceramic Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Treating Waste Gases (AREA)

Abstract

Procédé d'élimination simultanée de SO2 et de NOx contenus dans des gaz de fumée en une ou plusieurs étapes par voie humide. Le but de l'invention consiste à améliorer un procédé de ce genre de telle sorte qu'il puisse être exécuté avec un coût relativement minime, en obtenant en outre des valeurs sensiblement inférieures aux valeurs maximales prescrites par les autorités. A cet effet, le SO2 absorbé pendant le procédé, précipité par de la chaux sous forme de CaSO3/CaSO4 x 2H2O solide n'est plus oxydé par un oxydant pour devenir du CaSO4 x 2H2O mais est ajouté à l'état solide au courant de liquide de lavage d'un étage de prélavage à des fins d'oxydation de la quantité de CaSO3 par l'oxygène de la quantité de gaz de fumée, la solution de lavage ayant un pH compris entre 2 et 2,5. La matière solide est transmise au laveur ou au bassin de lavage de l'étage de prélavage et maintenue en contact avec le liquide de lavage, avec un pH correspondant (1 à 1,5) jusqu'à ce que la quantité de SO2 nécessaire à la réaction de lavage simultané de SO2/NOx dans le laveur soit libérée.
EP86905803A 1985-10-11 1986-10-08 Procede d'elimination simultanee de so 2? et de no x? contenus dans des gaz de fumee Withdrawn EP0241496A1 (fr)

Applications Claiming Priority (22)

Application Number Priority Date Filing Date Title
DE19853536312 DE3536312A1 (de) 1985-10-11 1985-10-11 Simultane so(pfeil abwaerts)2(pfeil abwaerts)/no(pfeil abwaerts)x(pfeil abwaerts)-abscheidung in waessriger phase mit gipserzeugung und so(pfeil abwaerts)2(pfeil abwaerts)-freisetzung in der vorwaschstufe
DE3536312 1985-10-11
DE19853537948 DE3537948A1 (de) 1985-10-25 1985-10-25 Simultane so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-verfahren zur reinigung von rauchgasen, die insbesondere mit hohen so(pfeil abwaerts)2(pfeil abwaerts)-belastungen versehen sind
DE3537949 1985-10-25
DE19853537949 DE3537949A1 (de) 1985-10-25 1985-10-25 So(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-gasreinigungsanlage mit endprodukt natriumsulfat
DE3537948 1985-10-25
DE19853538136 DE3538136A1 (de) 1985-10-26 1985-10-26 Wertstoffrueckgewinnung aus der simultanen so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-waschung von vorzugsweise rauchgasen hinter kraftwerken
DE3538136 1985-10-26
DE19853540973 DE3540973A1 (de) 1984-12-24 1985-11-19 Simultane so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-abscheidung bei rauchgasen, die mit hohem no(pfeil abwaerts)x(pfeil abwaerts) und hcl belastet sind
DE3540973 1985-11-19
DE3541323 1985-11-22
DE19853541323 DE3541323A1 (de) 1985-11-22 1985-11-22 So(pfeil abwaerts)2(pfeil abwaerts)-waschung hinter verbrennungsanlagen mit rohgips als endprodukt
DE3541471 1985-11-23
DE19853541471 DE3541471A1 (de) 1985-11-23 1985-11-23 So(pfeil abwaerts)2(pfeil abwaerts)- und/oder so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-waesche mit vorgesetzter calciumchlorid-gewinnung
DE3543843 1985-12-12
DE19853543843 DE3543843A1 (de) 1985-07-13 1985-12-12 Verfahren zur simultanen waschung von so(pfeil abwaerts)2(pfeil abwaerts) und no(pfeil abwaerts)x(pfeil abwaerts) aus rauchgasen durch einsatz manganarmer additive
DE3545190 1985-12-20
DE19853545190 DE3545190A1 (de) 1985-12-20 1985-12-20 Verfahren zur herstellung von wertprodukten hinter einer rauchgasentschwefelung
DE3546112 1985-12-24
DE3546122 1985-12-24
DE19853546112 DE3546112A1 (de) 1984-12-24 1985-12-24 Simultane so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-abscheidung durch einsatz einer elektrolyse unter beachtung der leitfaehigkeit der waschloesung
DE19853546122 DE3546122A1 (de) 1985-12-24 1985-12-24 Verfahren zur reduktionsmittelzugabe bei der simultanen so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-abscheidung

Publications (1)

Publication Number Publication Date
EP0241496A1 true EP0241496A1 (fr) 1987-10-21

Family

ID=27581482

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86905803A Withdrawn EP0241496A1 (fr) 1985-10-11 1986-10-08 Procede d'elimination simultanee de so 2? et de no x? contenus dans des gaz de fumee

Country Status (2)

Country Link
EP (1) EP0241496A1 (fr)
WO (1) WO1987002269A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2948335B2 (ja) * 1991-01-22 1999-09-13 三菱重工業株式会社 高性能排煙脱硫方法
US7405069B2 (en) 2002-04-08 2008-07-29 Akzo Nobel N.V. Method for removing a nitrogen oxide from a gas
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