EP0716677A1 - Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene - Google Patents

Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene

Info

Publication number
EP0716677A1
EP0716677A1 EP94926229A EP94926229A EP0716677A1 EP 0716677 A1 EP0716677 A1 EP 0716677A1 EP 94926229 A EP94926229 A EP 94926229A EP 94926229 A EP94926229 A EP 94926229A EP 0716677 A1 EP0716677 A1 EP 0716677A1
Authority
EP
European Patent Office
Prior art keywords
gas
sulfur
temperature
mercury
sulfuric acid
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Withdrawn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
EP94926229A
Other languages
German (de)
English (en)
Inventor
Jürgen RITTER
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.)
FPR HOLDING AG
Original Assignee
FPR HOLDING 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
Priority claimed from DE4333039A external-priority patent/DE4333039C2/de
Priority claimed from DE4404997A external-priority patent/DE4404997A1/de
Application filed by FPR HOLDING AG filed Critical FPR HOLDING AG
Publication of EP0716677A1 publication Critical patent/EP0716677A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • 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
    • B01D53/75—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G13/00—Compounds of mercury
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon

Definitions

  • the invention relates to a method for cleaning an essentially oxygen-free, flammable gas which contains, inter alia, H 2 S, Hg, dioxins and furans.
  • synthesis gases which contain, inter alia, H 2 S, Hg, dioxins and furans.
  • a known example of such a synthesis gas is the gas which arises during the pyrolysis of the waste treatment process from the company Thermoselect and which, as a result, is used as a conversion gas or the like. This gas is obtained at a temperature of about 1200 ° C and is cooled down to 90 ° C by the Pfei ⁇ fen water cooling according to the Thermoselect method. This shock cooling is carried out to prevent deNovo synthesis of dioxins and furans decomposed at 1200 ° C. Not inconsiderable amounts of heavy metals accumulate in the cooling water. Together with a subsequent gas scrubbing, considerable amounts of waste water are generated, the treatment of which is not without problems.
  • the gas washes carried out serve in particular to separate H 2 S, HC1 and Hg from the synthesis gas.
  • Plant for the production of sulfuric acid which is operated at a temperature that destroys dioxins and furans and allows the mercury to be separated.
  • the process according to the invention is essentially based on the fact that with a suitable adsorbent, in particular with a suitably doped activated carbon, for example with iodide ions is doped, in the same step H 2 S, Hg and the dioxins and furans can be removed virtually completely from the synthesis gas.
  • the synthesis gas emerging from the adsorber is thus freed from the contaminations mentioned and can - possibly after separation of hydrochloric acid and possibly one
  • Elimination of further pollutants in a manner known per se - are supplied to electricity generation or another utilization.
  • the loaded adsorbent of the adsorber is regenerated.
  • An activated carbon can be doped again after regeneration.
  • the removal of the H 2 S from the synthesis gas is preferably carried out by adsorption catalysis, in which the reaction products sulfur and water are formed from H 2 S under the action of oxygen, which is expediently metered in before the adsorber.
  • the resulting elemental sulfur is adsorbed on the inner surface of the activated carbon.
  • the water is removed in the form of water vapor with the gas.
  • oxygen to the energy-rich gas takes place in such a small amount that there is no risk of explosion.
  • Small amounts of the H 2 S react with the metered oxygen to form S0 2 , which is catalytically converted to sulfuric acid on the activated coke, so that in addition to that mainly adsorbed sulfur in the pore structure of the activated coke also contains small amounts of sulfuric acid.
  • the circulation of the selected activated carbon between adsorption, regeneration and reuse in the adsorption is relatively low because the activated carbon up to can be loaded at a rate of a good 1 kg S per kg activated carbon.
  • the activated carbon consumption due to abrasion is correspondingly low
  • the rich gas obtained during the regeneration is oxidized. It is achieved that S0 2 is formed from the adsorbed sulfur.
  • the S0 2 -containing, oxidized rich gas is passed into a plant for the production of sulfuric acid, which is operated at a temperature which destroys dioxins and furans and allows the mercury to be separated off.
  • Such a plant for the production of sulfuric acid is the nitrogen oxide-sulfuric acid plant known for this purpose from DE 41 27 075 A1, the denitrification tower of which is hot, i.e. is operated at a temperature of> .60 ° C.
  • the denitration tower In this denitration tower, any dioxins and furans formed by DeNovo synthesis are safely split into harmless constituents, under conditions which preclude DeNovo synthesis.
  • the mercury is converted to mercury sulfate by sulfuric acid containing nitrosylsulfuric acid. By adding a thiosulfate, the mercury sulfate is converted to mercury sulfide (HgS) and precipitated.
  • HgS mercury sulfide
  • the process known for the processing of exhaust gases which is based on the adsorption of pollutants and the sulfuric acid production by the Fattinger process, is therefore used for a completely different type, namely oxygen-free synthesis gas, which is a sulfur component has at least predominantly H 2 S.
  • oxygen-free synthesis gas which is a sulfur component has at least predominantly H 2 S.
  • the adsorbent is regenerated, preferably by using an inert gas with a temperature of> 500 ° C., the preferred temperature of which is around 650 ° C.
  • Regeneration at this temperature has the advantage over the known extraction of the sulfur with the aid of solvents that the mercury is also desorbed with every regeneration. This creates a relatively evenly composed desorption gas. Oxygen is supplied to this desorption gas for oxidation. In this way, the composition of the gas constituents can be converted so that the Fattir-jer process can now also be used for the originally completely different pollutant composition.
  • the advantages of the unproblematic mercury separation and the definite destruction of the dioxins and furans which can be achieved with the Fattinger process can therefore also be achieved for the starting composition of the gas under consideration here.
  • the sulfur and mercury contained in the desorption gas are condensed out and stored temporarily.
  • This sulfur / mercury intermediate product can then be burned in precisely metered amounts, so that the sulfuric acid plant can be offered a constant amount of S0 2 in a constant concentration.
  • This procedure has the advantage that the regeneration and the sulfuric acid plant can be operated separately from the synthesis gas cleaning plant. This ensures high availability of synthesis gas cleaning.
  • the desorption gas which in addition to desorbed elemental sulfur also contains S0 2 from the desorption of sulfuric acid and HgS, can be passed through a condensation stage in which S and HgS are condensed out.
  • the desorption gas which then still contains S0 2 , can be metered into the combustion chamber for the combustion of sulfur.
  • Other sulfur compounds still contained in the desorption gas which may form in the activated carbon regeneration, are also converted to SO 2 at the temperature of approx. 800 ° C. in the combustion chamber.
  • the emerging behind the combustion chamber S0 2 -rich which also includes the resulting by desorption of sulfuric S0 2, then passes expediently a known Reichgaswasehe before it gets out of the sulfuric acid plant zu ⁇ .
  • An essential feature of the method according to the invention is that the gas introduced into the adsorber has a temperature of>. 100 ° C. This has the consequence that any Cooling water used to cool down the hot combustible gas from its starting temperature is contained in vapor form in the synthesis gas and passes through the adsorber in this form. The steam does not affect the desulfurization of the synthesis gas.
  • An advantage of this procedure is that the evaporated cooling water only condenses out after practically all pollutants have been removed by the adsorber and any filter.
  • the dry adsorption process according to the invention allows cooling, for example in a quench tower which does not require an excess of water, to about 110 to 120 ° C., that is to say the temperature at which the gas preferably enters the adsorber.
  • the synthesis gas should preferably pass through a filter. Mineral components and heavy metals already in solid form at the respective temperature can be separated in this filter and can be glazed to a non-elutable substance.
  • a bag filter is preferably used for this. In the present case, bag filters can be used economically up to 250 ° C. It is therefore possible according to the invention to cool the gas down to a temperature of up to 250 ° C. and to filter out the mineral constituents and solid heavy metals at this temperature.
  • the subsequent cooling to the preferred 110 to 120 ° C can be carried out with a heat exchanger, so that the residual energy of the gas can be obtained in a usable form.
  • the heavy metals and heavy metal compounds separated in the bag filter As an alternative to melting the heavy metals into a glass melt, it is possible to pass the heavy metals and heavy metal compounds separated in the bag filter through a small wash in which the water-soluble chlorides are separated off. The remaining heavy metals and heavy metal compounds can then be further processed.
  • the wash water obtained in small quantities is known in ter cleaned and introduced together with the excess water that accumulates in the gas cooling in a receiving water or channel.
  • a heat exchanger for example in the form of a waste heat boiler, is used to recover and fully utilize the energy contained in the hot synthesis gas, with which steam and electrical energy is generated from it via a turbine.
  • the heat exchanger is made of corrosion-resistant special steel or lined with conventional materials.
  • the synthesis gas obtained at approximately 1200 ° C. can be cooled to approximately 900 ° C. or below, preferably with synthesis gas cooled down to approximately 120 ° C.
  • the synthesis gas can also be passed through a quartz bulk filter before the entry into the waste heat boiler, for example at 850 ° C. to 900 ° C., for the early separation of the mineral substances.
  • the synthesis gas is cooled down to approx. 280 ° C, then preferably in a graphite heat exchanger further to approx. 150 ° C.
  • a bag filter can be used to separate the heavy metals and possibly also the mineral substances behind the graphite heat exchanger.
  • the gas is cooled down with a further heat exchanger to the inlet temperature in the adsorber to 110 to 120 ° C.
  • the synthesis gas which arises from the gasification of waste, for example, often contains other sulfur compounds, such as COS and CS 2 , in addition to H 2 S.
  • other sulfur compounds such as COS and CS 2
  • there is one Sulfur-free exhaust gas is required so that all sulfur components should be removed from the synthesis gas.
  • This is achieved according to the invention using the method according to the invention if a catalytic conversion of the sulfur-containing constituents into adsorbable sulfur configurations, preferably H 2 S, is carried out before the adsorption.
  • the adsorptive sulfur configurations can then be adsorbed in the adsorption stage, together with the H 2 S contained in the synthesis gas anyway.
  • the catalytic conversion is preferably carried out by using a particularly doped activated carbon through which the synthesis gas flows in a fixed bed reactor.
  • the conversion of COS and CS 2 to H 2 S represents a purely catalytic, ie not an adsorptive process.
  • the process according to the invention can thus also be used if the synthesis gas originally contains non-adsorbable sulfur-containing constituents.
  • the synthesis gas usually has a temperature of approximately 1200 to 1400 ° C. and emerges from the high-temperature reactor. It is subjected to gas cooling and passes through a filter for the separation of mineral components and heavy metals in solid form. Mercury is not separated from this filter, since it is still in gaseous form in the synthesis gas.
  • the gas prepared in this way contains non-adsorbable sulfur-containing constituents, such as COS or CS 2 , and if these sulfur constituents are to be completely removed from the gas, the gas passes through a fixed bed filled with an activated carbon catalyst, formed from a fixed bed filled with doped activated carbon ⁇ reactor in which the non-adsorbable sulfur-containing constituents, such as in particular COS and / or CS 2 , are converted into H 2 S.
  • the converted H 2 S together with the H 2 S contained in the synthesis gas anyway, can be separated off in the following adsorber together with Hg, dioxins and furans as well as residual dust.
  • the gas thus cleaned passes into an HCl scrubber, in which the HC1 is recovered and then concentrated to salable hydrochloric acid.
  • the purified synthesis gas is used in a suitable manner, for example by combustion for electricity purposes.
  • the resulting exhaust gas is denitrified and can be led outside through a chimney.
  • the synthesis gas which is produced, for example, by the gasification of domestic waste according to the Thermoselect method, already brings with it a high water content at 1200 ° C., which comes from the waste used.
  • the synthesis gas In order to use the synthesis gas as an energy source after it has been cleaned, it is cooled and dried. net and largely freed from this water.
  • the water is slightly acidic and otherwise practically free of pollutants and can therefore be discharged into a drain or sewer system after neutralization without further treatment.
  • cooling water is used to cool the synthesis gas from 1200 to 1400 ° C to a lower temperature, this can be recovered in the HCl scrub or in the gas cooling and can be reused as cooling water with practically no pollutants.
  • the synthesis gas is not cooled down with water in a quench tower, but rather the energy contained in the hot synthesis gas is recovered as usable energy in a waste heat boiler and a downstream graphite heat exchanger, then a part of the water contained in the waste can be released into the synthesis gas reached, can be used for the production of hydrochloric acid.
  • the hydrochloric acid absorbed in the HCl scrubber can be known
  • the deposited in the filter mineral components and solid heavy metals can be melted down to a eluierbe operatingn melt product in a known method • was ⁇ to.
  • the non-meltable heavy metals and heavy metal compounds such as cadmium (Cd) separate and can be recovered.
  • the activated carbon in the adsorber is removed from the adsorber and fed to a regeneration which preferably works with hot inert gas of about 650 ° C.
  • sulfur and mercury are desorbed in the form of mercury and removed with the desorption gas.
  • the regenerated activated carbon gets back into the adsorber, if necessary after renewed doping.
  • the also adsorbed dioxins and furans are among the Conditions of thermal regeneration largely destroyed. If small portions are desorbed without being destroyed, they reach the rich gas with the desorption gas and are destroyed in the sulfuric acid plant.
  • the regenerated activated carbon Before the regenerated activated carbon is returned to the adsorber, it is passed through a sieving / screening. Fine components such as activated carbon undersize and dust are separated in it and returned to the raw waste.
  • the desorption gas which leaves the regenerator at about 450 ° C., is mixed with air and the sulfur contained in the desorption gas is oxidized with the atmospheric oxygen to SO 2 .
  • the rich gas essentially contained in S0 2 is cooled and dedusted and then subjected to rich gas washing.
  • the main separation of mercury takes place there.
  • the wash water which may still contain traces of residual pollutants, is sprayed into the hot synthesis gas at a suitable point. There it evaporates and reaches the gas cleaning system in gaseous form with the synthesis gas to be cleaned.
  • the S0 2 rich gas is used for the production of sulfuric acid in a salable form.
  • Residual mercury is deposited in the sulfuric acid plant as mercury. It is combined with the sulfur condensed out after the regeneration and decomposed when the sulfur is burned.
  • the Hg is released as metallic mercury and the sulfur contained in the HgS is oxidized to S0 2 . This procedure ultimately only produces metallic mercury, which is also precipitated as metallic mercury in the rich gas scrubber, which serves as a mercury sink, and can be removed as a valuable substance.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

On peut laver un gaz combustible pratiquement exempt d'oxygène contenant H2S, Hg, des dioxines et des furanes, entre autres, en procédant aux étapes suivantes: on fait passer le gaz, à une température égale ou supérieure à 100 DEG C, à travers un adsorbant, afin d'en séparer en même temps pratiquement la totalité de H2S, Hg, des dioxines et des furanes; on régénère l'adsorbant chargé; on oxyde le gaz de désorption obtenu pendant la régénération afin de former du SO2; on introduit le gaz oxydé de désorption dans une installation de préparation d'acide sulfurique exploitée à une température qui détruit les dioxines et les furanes et qui permet de séparer le mercure. De préférence, on évite la formation d'effluents pollués lors du refroidissement du gaz avec de l'eau.
EP94926229A 1993-09-03 1994-09-01 Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene Withdrawn EP0716677A1 (fr)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
DE4329752 1993-09-03
DE4329752 1993-09-03
DE4333039A DE4333039C2 (de) 1993-09-03 1993-09-30 Verfahren zum Reinigen eines im wesentlichen sauerstofffreien, brennbaren Gases
DE4333039 1993-09-30
DE4404997 1994-02-17
DE4404997A DE4404997A1 (de) 1993-09-30 1994-02-17 Verfahren zum Reinigen eines im wesentlichen sauerstofffreien, brennbaren Gases
PCT/EP1994/002901 WO1995006699A1 (fr) 1993-09-03 1994-09-01 Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene

Publications (1)

Publication Number Publication Date
EP0716677A1 true EP0716677A1 (fr) 1996-06-19

Family

ID=27205510

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94926229A Withdrawn EP0716677A1 (fr) 1993-09-03 1994-09-01 Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene

Country Status (2)

Country Link
EP (1) EP0716677A1 (fr)
WO (1) WO1995006699A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8828900B2 (en) 2011-04-08 2014-09-09 Toyota Jidosha Kabushiki Kaisha Exhaust gas purification catalyst

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3019830B1 (fr) * 2014-04-14 2017-11-24 Gdf Suez Procede et dispositif de traitement d'un gaz de synthese provenant d'une etape de gazeification de biomasse

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR85066E (fr) * 1964-01-07 1965-06-04 Aquitaine Petrole Procédé de récupération de composés sulfurés gazeux contenus en faibles concentrations dans les gaz résiduaires et fumées
DE1224865B (de) * 1964-02-05 1966-09-15 Metallgesellschaft Ag Verfahren zur Abscheidung von Schwefelwasserstoff aus Gasgemischen
US4045371A (en) * 1974-05-07 1977-08-30 Exxon Research And Engineering Company Process for preparing a gas desulfurization sorbent
JPS5919728B2 (ja) * 1976-03-24 1984-05-08 バブコツク日立株式会社 硫化水素含有ガスの処理法
DE4127075A1 (de) * 1991-08-16 1993-02-18 Nymic Anstalt Verfahren zum reinigen von belasteten abgasen von verbrennungsanlagen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9506699A1 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8828900B2 (en) 2011-04-08 2014-09-09 Toyota Jidosha Kabushiki Kaisha Exhaust gas purification catalyst

Also Published As

Publication number Publication date
WO1995006699A1 (fr) 1995-03-09

Similar Documents

Publication Publication Date Title
EP0553337B1 (fr) Procede d'epuration des gaz d'evacuation charges d'installations d'incineration
DE3629817C2 (fr)
EP1997549B1 (fr) Procédé et dispositif de nettoyage catalytique de gaz biogènes ou anthropogènes contenant du méthane
EP0819233A1 (fr) Procede et dispositif de traitement thermique de dechets
DE4012887C2 (fr)
EP0123856B1 (fr) Procédé d'élimination ou d'isolation de polluants de gaz d'échappement
EP0596911A1 (fr) Procedee de lavage de gaz de fumee fortement contamines avec du mercure.
DE2948305C2 (de) Verfahren zum trockenen Reinigen von quecksilberhaltigen Gasen, insbesondere Abgasen, thermischer Prozesse
DE3706131A1 (de) Verfahren zur entfernung von schadstoffen aus rauchgas
EP0716677A1 (fr) Procede de lavage d'un gaz combustible pratiquement exempt d'oxygene
DE4333039C2 (de) Verfahren zum Reinigen eines im wesentlichen sauerstofffreien, brennbaren Gases
DE4404997A1 (de) Verfahren zum Reinigen eines im wesentlichen sauerstofffreien, brennbaren Gases
DE3602710C2 (fr)
WO1999015277A1 (fr) Procede pour revaloriser des automobiles usagees
DE4102557A1 (de) Verfahren zur herstellung von adsorbensmaterial mit katalytischen eigenschaften
DE4447583A1 (de) Verfahren zur Entfernung von Schadstoffen aus Verbrennungsabgasen
DE4024303C1 (en) Carburation of carbonaceous materials - by pyrolytic decomposition, putting impurities through low viscosity bath made of old molten glass
DE19638584C2 (de) Verfahren zur Abscheidung von Staub aus einem staubhaltigen und wasserdampfhaltigen Abgas in einem filtrierenden Abscheider
DE4425471A1 (de) Verfahren zum Reinigen von Abgasen
DE4406460C2 (de) Verfahren zur Reinigung eines Vergasungsgases aus der Vergasung von Abfall- und Reststoffen
DE4342669A1 (de) Verfahren und Vorrichtung zur Verwertung eines bei einer Vergasung von Kohlenstoff enthaltenden Materialien anfallenden Gases und darin enthaltener Verunreinigungen
DE4422924C2 (de) Verfahren zur Reinigung eines Abgasstromes aus einer Verbrennungsanlage
WO1993004765A1 (fr) Procede d'epuration des gaz de fumee
DE3541447A1 (de) Verfahren zur verringerung der schwefelemission von kohlegefeuerten kraftwerken
DE9410363U1 (de) Vorrichtung zur Reinigung eines Abgasstromes aus einer Verbrennungsanlage

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19960301

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE FR GB IT LI NL

17Q First examination report despatched

Effective date: 19960604

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Withdrawal date: 19961203