WO1996014919A1 - Method of treating process or flue gases containing halogenous compounds - Google Patents

Method of treating process or flue gases containing halogenous compounds Download PDF

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Publication number
WO1996014919A1
WO1996014919A1 PCT/FI1995/000626 FI9500626W WO9614919A1 WO 1996014919 A1 WO1996014919 A1 WO 1996014919A1 FI 9500626 W FI9500626 W FI 9500626W WO 9614919 A1 WO9614919 A1 WO 9614919A1
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WO
WIPO (PCT)
Prior art keywords
reactor
cooled
process gases
circulating
temperature
Prior art date
Application number
PCT/FI1995/000626
Other languages
French (fr)
Inventor
Matti Hiltunen
Vesa Jokelainen
Kurt Westerlund
Original Assignee
Foster Wheeler Energia Oy
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Publication date
Application filed by Foster Wheeler Energia Oy filed Critical Foster Wheeler Energia Oy
Priority to AU38735/95A priority Critical patent/AU3873595A/en
Publication of WO1996014919A1 publication Critical patent/WO1996014919A1/en

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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
    • B01D53/02—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 by adsorption, e.g. preparative gas chromatography
    • B01D53/06—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 by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—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 by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B01D53/12—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 by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
    • 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
    • B01D53/70—Organic halogen compounds
    • 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
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • 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
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • 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
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Dispersion Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)

Abstract

The present invention relates to a method of treating different chlorine-containing materials, such as waste, and of biosludges at a high temperature of above 830 °C and of cooling generated process gases in order to minimize the amount of polyhalogenated aromatic compounds in the generating process gases. The process gases are cooled below 400 °C in the presence of a certain reagent. The cooling is preferably carried out in a circulating fluidized bed reactor.

Description

METHOD OF TREATING PROCESS OR FLUE GASES CONTAINING HALOGENOUS COMPOUNDS
The present invention relates to a method of cooling various process gases in order to minimize the amount of polyhalogenous compounds, such as dioxins and furans, in the gas emissions.
More accurately the present invention relates to a method of treating various materials containing halogenized hydrocarbon compounds, such as wastes, biosludges or metal oxide concentrates at a high temperature. The materials are heated or combusted in the presence of oxygen-containing gas so that the halogenized hydro- carbon compounds harmful to the environment, which the materials possibly contain, decompose, in order to cool the generated process gases, in order to minimize the amount of polyhalogenous compounds, such as dioxins and furans, harmful to the environment, in the gas emissions.
When combusting municipal waste, but also when combusting biosludges and in the smelting house processes, it has been acknowledged that the chlorine-containing environmental poisons are a problem. Polychlorinated aromatic compounds classified as superpoisons, such as coplanar PCB, polychlorinated aromatic compounds and polychlorinated furans, have been noted to be generating a lot both in the municipal waste incinerating plants as well as in industrial biomass incinerating plants. Dioxins have also been found in the flue gases of metal smelting houses. These chlorine compounds are very toxic both for animals and for human beings, cause genetic damage and will also be carsinogenic. Toxic compounds spread to the environment mostly with fly dust.
It has been said that the lower the temperature is and the shorter the retention time is in the combustion, the more supertoxins generate. The combustion at 500-700β has been proved to be especially liable for th generation of polychlorinated dioxins and furans. Thi has led to the conclusion that the combustion should tak place at a higher temperature and with a long retentio time for destroying the supertoxins. On the other hand it has also been suggested that the wastes can safely b disposed by incinerating at relatively low temperatures if the flue gases are post-combusted at such a hig temperature that, for example, dioxin and furan toxin are destroyed.
It is, however, not always possible to provide temperature suitable for eliminating supertoxins in th actual process or post-combustion. Moreover, it has als been found that the supertoxins are easily reformed i the later stages of the process, and also after post combustion.
Dioxins are formed, for example, in flue gases, b synthesization from chlorine compounds in the presence o carbon, water and oxygen at favourable temperatures. I has been noted that a substantial portion of the dioxin of the fly ash is formed by a so called "de nov synthesis" only after post-combusting in the hea exchangers and in the stack, because the "de nov synthesis" of the dioxins to a large extent depends o the temperature and the temperature of 250-400°C i especially suitable for this kind of synthesis. Effort have been made, by as complete a combustion as possible by a high combustion temperature and by a long retentio time to produce fly ash containing as little carbon a possible, whereby the synthesis will be prevented. B separating metals from the wastes, it has been attempte to decrease the amount of polychlorinated aromats in th flue gases. US patent specification 4,762,074 suggests the incineration of wastes containing pre-stages of toxic dioxins and furans with oxygenated air at a high temperature of at least 1200° in order to decompose the toxins. A highly excessive amount of oxygen is at the same time used for maintaining the amount of nitrogen oxides, which increase at high temperatures, at an acceptable level.
Swedish patent specification SE 453 777 discloses a method, of combusting solid waste in a reactor in a bubbling fluidized bed at a temperature below 9*00βC. The temperature of flue gases is raised in the reactor above the actual fluidized bed to at least 950°C by adding secondary air and by insulating the walls of the reactor. The temperature of the flue gases is maintained at a level of above 950°C for a period of time required by the decomposition of hydrocarbons and dioxins by leading the flue gases through an uncooled gas channel. The gases are cooled prior to the heat exchangers by injecting air or flue gases to the gases.
US patent specification 4,794,871 discloses a two- or three-stage method, in which waste is first treated in a rotatable drum at a temperature of 500°C maximum and the solid waste formed thereby is treated at the temperature of at least 500βC, preferably 500-1000°C, for destroying toxic substances. The flue gases from both treatment stages are combined and combusted at such a high temperature that the toxic compounds in the gases are completely decomposed.
Swedish patent application SE 8406090-4 discloses a method, in which environmentally harmful wastes containing chlorinated hydrocarbons are incinerated substoichimetrically at a temperature of at least 1200°C. The combustion takes place as plasma incineration. According to the patent application, the reformation o the toxic compounds may be prevented so that the flu gases which have first been cooled to 350-700βC ar brought into contact with lime in order to• separat chlorine from the gases. Chlorine separatio advantageously takes place so that the gases are supplie through a vertical reactor filled with lime. At lo temperatures the polychlorinated aromats are, however, produced rapidly before the chlorine has become bound t lime, so by utilizing this method it is not possible t achieve the desired result.
Decomposing toxic polyhalogens by a two-stage catalyti treatment has been suggested, for example, in US paten specification 4,983,366. In the method the gases ar first brought through an oxidizing catalytic crackin stage and secondly through a catalytic post-combustio stage.
Finnish patent specification FI 88364 suggests cooling of gas in two subsequent circulating fluidized bed reactors, whereby hot gases are cooled in a first fluidized be reactor so that the temperature of gases is still, afte cooling, above 400°C and in a second fluidized be reactor so that the temperature of gases rapidly decreases below the temperature range of 250-400°C. This specification also discloses the use of a catalyst fo the first stage, i.e. temperature range of > 400°C. Thi kind of arrangement has several disadvantages. Tw subsequent circulating beds cause, for example, hig operating costs due to, for example, pressure losses.
Finnish patent specification FI 83290 suggests cooling o gases in a circulating fluidized bed reactors, whereb the gases generating in grate combustion at a temperatur > 830°C are rapidly cooled in a circulating fluidized be reactor below 250°c. The rapid cooling required her across a large temperature range set great demands to the circulating fluidized bed reactor, for example, the amount of circulating bed material must be very large, in order for the cooling to be realized.
The purpose of the present invention is to bring about a method solving the problems of the prior art, by means of which method the gas emissions are minimized. The purpose of the present invention is to bring about a method of minimizing polyhalogenated hydrocarbon compound emissions in plants generating hot process or flue gases.
A characteristic feature of the method in accordance with the present invention is that - the generated process gases are cooled to a temperature of below 400°C in a circulating fluidized bed reactor, in which reactor
- reagent agent is mixed with process gas in the reactor for minimizing the amount of polyhalogen compounds in the gas emissions, such as dioxins and furans, harmful to the environment; and
- circulating bed material particles are separated in a particle separator from process gas and are cooled and recirculated to the reactor.
In some combustion processes unscreened environmentally harmful wastes are incinerated in grate combustion and the generated process gases are first heated for at least 1-2 seconds at > 1000βC in order to destroy environmentally harmful chlorinated hydrocarbons.
According to an embodiment of the invention, process gases can be thereafter cooled, for example, in combustion processes, so that flue gases are cooled in the presence of reagent agent, in direct contact with gases, below 400°C, preferably below 300°C. The cooling takes place preferably in a circulating fluidized bed reactor, in which it is possible to carry out a very rapid cooling, even more than 1000°C per second. The flue gases may thus be cooled practically speaking immediately to below 400βC. When combining rapid cooling with the impact of a reagent agent the entrance of polyhaiogenated aromatic compounds to the atmosphere is prevented.
The gases are preferably directly led from the combustion process to the fluidized bed reactor, whereby the gases are substantially not cooled between the combustion process and the fluidized bed reactor. If the temperature of the gases is very high after the combustion process, it is possible to cool the gases before introducing them into the fluidized bed reactor, so as to optimize the operation of the fluidized bed reactor.
Contrary to the cooling of gas in a circulating fluidized bed reactor rapidly to below 250'C, suggested in patent specification FI 83290, it is possible according to the invention, by using a suitable reagent agent, to achieve even better emission reductions. By utilizing the reagent agent the cooling may reach, contrary to the knowledge of the prior art, a temperature range of 250-400°C, which is very favourable for the regeneration of dioxins, and the emissions still remain very low. According to the invention, the cooling is carried out to 400-250°C preferably<300°C by utilizing a special reagent agent as bed material.
The reagent agent forms in steady state typically > 50%, but preferably > 75% of the circulating bed material. Thus, in addition to cooling, an efficient and sufficient effect of the reagent agent is obtained in the process gases.
The reagent agent is preferably CaC03, CaO, CaS04, Ca(OH)2, MgC03, MgO, MgS04, Mg(0H)2, BaC03, Bao, BaS04, Ba(0H)2/ or mixtures thereof. Also some other Ca-, Ba- or Mg-compound may act on the reduction of emissions advantageously.
It is also possible to add agents to the circulating bed material, which either act on the chlorine, fluorine and sulphur compounds in the flue gases or absorb these compounds to remove them from the gases. At the same time, it is possible to separate a substantial portion of the heavy metals in the flue gases, melting and evaporating at low temperatures, such as Hg, As, Zn, Cd, Pb and Sn, and their compounds, by condensing them to the circulating bed material in a cooling reactor. 'Particles can be removed from the circulation of the cooling reactor either continuously or at intermittently, in order to remove harmful recoverable substances from the circulation. New particles are added correspondingly to maintain the circulating bed material.
According to a second embodiment of the present invention municipal wastes or industrial biosludges may be advantageously incinerated in a circulating fluidized bed reactor at the temperature of 830-1000βc, whereby the above mentioned supertoxins in the wastes or sludges principally decompose. The flue gases are cooled in the presence of catalyst advantageously below 400°C. The cooling takes place in a circulating fluidized bed reactor, in which it is possible to effect a very rapid cooling, even more than 1000°C per second. The flue gases may thus be cooled practically speaking immediately below 400°c. By combining rapid cooling with the effect of a reagent agent the entrance of polyhalogenated aromatic compounds to the atmosphere is minimized.
The invention may be applied also to other flue gases containing chlorine compounds and possibly small amounts of carbon and oxygen, in which flue gases polychlorinated aromatic compounds are generated at higher temperatures. The circulating fluidized bed is a very advantageo embodiment for the method in accordance with the prese invention, because in the circulating fluidized b reactor hot gases, which are introduced into the react preferably as fluidizing gas, cool very rapidly alrea in the mixing chamber when mixing with cooler circulati particles. The cooling velocity in the mixing chamber generally > 500 βC/s, preferably above 1000 βC/s. Wh necessary, fluidized bed coolers cooling the circulati material, i.e. also reagent agent may be arranged i communication with the circulating bed reactor. In th circulating bed the mixing of gas and reagent agent is very efficient, whereby also the content of harmfu substances reduces efficiently by utilizing th circulating bed. Also the circulation of the reagen agent, reutilization, may be utilized very efficiently i the circulating bed arrangement.
It is also possible to add agents acting on the chlorine fluorine and sulphur compounds included in the flue gase or which absorb these compounds in order to remove the from the gases. At the same time it is possible t separate a substantial portion of the heavy metal smelting and evaporating at low temperatures, such as Hg As, Zn, Cd, Pb and Sn and their compounds, b condensating them to the circulating bed material in th cooling reactors. Particles may be removed eithe continuously or at intervals from the circulation of th cooling reactor in order to remove harmful material o material to be recovered from the circulation. Ne particles are respectively added to maintain th circulating bed material constant.
The invention is described below with reference to th enclosed schematic drawing. The figure illustrates a circulating fluidized bed reactor 2 cooling flue gases arranged to follow a waste incinerator 4. Wastes are supplied to a furnace 6 of the combustor through an opening 8. The wastes flow along a grate 10 to the lower part of the furnace and burn. Air is supplied through a grate to the furnace. The flue gases rise upwards in the furnace shaft 12, to which it is possible to arrange also additional burners to ensure complete combustion and the decomposition of environmentally harmful materials.
The upper part of the furnace shaft is provided with a cooling fluidized bed reactor 2, to which hot flue gases are supplied. The reactor 2 comprises a mixing chamber 14 and a particle separator 16. The lower part of the mixing chamber is provided with a gas inlet opening 18, through which hot gas flows to the mixing chamber operating at the same time as fluidizing gas in the reactor. The mixing chamber is also provided with a return duct 24, through which cooled solid particles are supplied to the mixing chamber. Cold particles are supplied to the mixing chamber so much that in large amounts they rapidly cool the flue gases below 400°C. According to the invention, the bed material used is reagent material, preferably comprising Ca-, Ba, or Mg-compounds such as CaO, CaCO^ or MgO. Suddenly, it has been noted that the use of Ca-, Ba-, or Mg-compounds as bed material reduces especially dioxin emissions considerably without the need to cool the gases to an unnecessary low temperature.
This will offer considerable advantages to the method in accordance with the present invention compared to the prior art:
- a smaller required cooling capacity is necessary for dimensioning the apparatus;
- the amount of the circulating bed material may be smaller, which leads to reduced operating costs; - a higher mixing temperature of gases and solid material enables a higher final temperature in the heat exchange;
- toxic materials are removed almost completely from the gas phase, whereby a good dust separation secures almost insignificant emissions;
- the circulating bed minimizes the need of reagent by efficient mixing and circulating reagent;
- wearing in the reactor is minimized especially by utilizing Ca-compound due to its non-abrasiveness.
The reagent agent preferably used are CaC03, CaO, CaS0 , Ca(OH)2, MgC03, MgO, MgS04, Mg(OH)2, BaC03, BaO, BaS04, Ba(OH)2, or a mixture of the above mentioned. Especially a Ca-compound is advantageous, because it is a commercially available, non-toxic compound. Moreover, as it is mentioned above, the wearing effect thereof in the circulating fluidized bed reactor is very small.
The upper part of the mixing chamber continues as a cooling portion 34, in which gases and solid particles are cooled together prior to the separation of particles from the gases. The particles may be advantageously cooled also after the particle separator in a separate particle cooler 28. The flue gases are withdrawn from the reactor through a duct 36.
The particle cooler is preferably a fluidized bed cooler, to which fluidizing gas is supplied by means of members 38. In the fluidizing bed the solid material entering from the particle separator 16 is fluidized and it is cooled by means of heat surfaces 32 arranged to the fluidized bed. In the separator the separated solid material may be led by means of members 40 also directly to the mixing chamber through channel 22. Members 40 are preferably a non-mechanical arrangement for guiding solid material. Solid material containing reagent may also be removed from the process through a conduit 30, whereby it is cooled. New material is supplied through conduit 42. A fluidized bed cooler may also be an integrated part of the reactor, whereby solid material may be transferred, if necessary, directly from the chamber 14 to the cooler 28.
The cooling reactor 2 may be applied also to follow a normal rotatable combustion furnace or grate combustion furnace or other kind of combustion furnace.
The present invention is described below by means of an example from test runs. The method in accordance with the invention was applied to an apparatus in accordance with the figure, in which apparatus municipal waste was incinerated in a grate boiler. The results were as shown in the enclosed table.
PCDD/PCDF measured total content
PRIOR TO AFTER MIXING
TREATMENT TREAT¬ TEMPE¬
BED MATERIAL [ng/m3n] MENT RATURE (ng/m3n] [°C]
SILICA SAND 1150 140 400
LIMESTONE 1150 27 400
SILICA SAND 1150 72 300
LIMESTONE 1150 16 300
According to the results, the measured total dioxin/furan emissions at the mixing temperature 400°C when using sand is approximately 87%, whereas when using limestone the emission reduction is even about 97%. Correspondingly, when using sand at the mixing temperature 300°C th reduction of dioxin/furan emissions is approximately 93%, whereas with the limestone the emission reduction is eve 99%. This shows unquestionably the advantage of the us of limestone: even at the temperature of 400βC th reduction of the dioxin/furan emissions is larger tha when using silica sand at the temperature of 300βC. Th total emissions in the above described mean the emissio both in the gas and in the solid material. The reductio of gas emissions is still more efficient: by utilizin the method in accordance with the invention th dioxin/furan content of gases after the treatment is onl 0.004 - 0.006 ng/m3n TE, which is in view of toxicity standardized value.
While the invention has been herein shown and describe in what is presently conceived to be the most practica and preferred embodiment thereof, it will be apparent t those of ordinary skill in the art that man modifications may be made thereof within the scope o invention, which scope is to be accorded the broades interpretation of the appended claims so as to encompas all equivalent methods and processes.

Claims

1. Method of treating various materials containing halogenized hydrocarbon compounds, such as wastes, biosludges or metal oxide concentrates at a high temperature, whereby
- the materials are heated or combusted at a temperature
> 830°C in the presence of oxygen-containing gas so that the halogenized hydrocarbon compounds harmful to the environment, which the materials possibly contain, decompose, in order to minimize the amount of polyhalogenous compounds, such as dioxins and furans, harmful to the environment, in the gas emissions, characterized by
- the generated process gases being cooled to a temperature in the range of 400°C to 250°C in a circulating fluidized bed reactor, in which reactor
- reagent agent is mixed with the process gas in the reactor for minimizing the amount of polyhalogen compounds in the gas emissions, such as dioxins and furans, harmful to the environment; and
- circulating bed material particles are separated in a particle separator from process gas and are cooled and recirculated to the reactor.
2. Method according to claim 1, characterized by the reagent agent being a Ca-, Ba- or Mg-compound.
3. Method according to claim 1 or 2, characterized by the reagent agent being one of or a mixture of following: CaC03, CaO, CaS04, Ca(0H)2, MgC03, MgO, MgS04, Mg(OH)2, BaC03, BaO, BaS04, Ba(0H) .
4. Method according to claim 1, characterized by the process gases generated being cooled to a temperature in the range Of 300°C - 250°C.
5. Method according to claim 1, characterized bv the reagent agent forming > 50% of the circulating bed material in the circulating fluidized bed reactor.
6. Method according to claim 5, characterized bv the reagent agent forming > 75 % of the circulating bed material.
7. Method according to claim l, characterized by circulating bed material particles being cooled in a heat exchanger before being separated from the process gases.
8. Method according to claim 1, characterized by circulating bed material particles being cooled in a heat exchanger after being separated from the process gases.
9. Method according to claim 1, characterized bv the process gases being cooled at a velocity of > 1000°C/s.
10. Method according to claim 1, characterized bv the materials being heated for at least 1 - 2 seconds at >
830°C.
11. Method according to claim 10, characterized bv the heating or the combustion of materials in the presence of oxygen-containing gas taking place in a grate furnace and process gases generated being heated to > 1000°C.
12. Method according to claim 1, characterized by the process gases being introduced uncooled into the circulating fluidized bed.
PCT/FI1995/000626 1994-11-16 1995-11-14 Method of treating process or flue gases containing halogenous compounds WO1996014919A1 (en)

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FI945402A FI945402A (en) 1994-11-16 1994-11-16 A process for treating process or flue gases containing halogen compounds
FI945402 1994-11-16

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2785976A1 (en) 1998-11-17 2000-05-19 Air Liquide WASTE COMBUSTION PROCESS FOR REDUCING DIOXIN EMISSIONS
EP1078675A2 (en) * 1999-08-27 2001-02-28 Praxair Technology, Inc. Fluid separation process and separation system therefor
WO2007069990A1 (en) * 2005-12-16 2007-06-21 Mölnlycke Health Care Ab Method for perforating heat meltable material

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988008741A1 (en) * 1987-05-08 1988-11-17 A. Ahlstrom Corporation Method and apparatus for treating process gases
WO1990014559A1 (en) * 1989-05-18 1990-11-29 A. Ahlstrom Corporation Treatment of process gases containing halogenous compounds
DE4034498A1 (en) * 1990-09-06 1992-03-12 Metallgesellschaft Ag METHOD FOR SEPARATING HEAVY METALS AND DIOXINES FROM COMBUSTION EXHAUST GASES
EP0529243A1 (en) * 1991-08-09 1993-03-03 A.Ahlstrom Corporation Method of treating process gases or flue gases containing halogenous compounds
WO1995018667A1 (en) * 1994-01-06 1995-07-13 University Of Waterloo Prevention of formation and destruction of organohalogen compounds in incineration of waste materials

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988008741A1 (en) * 1987-05-08 1988-11-17 A. Ahlstrom Corporation Method and apparatus for treating process gases
WO1990014559A1 (en) * 1989-05-18 1990-11-29 A. Ahlstrom Corporation Treatment of process gases containing halogenous compounds
DE4034498A1 (en) * 1990-09-06 1992-03-12 Metallgesellschaft Ag METHOD FOR SEPARATING HEAVY METALS AND DIOXINES FROM COMBUSTION EXHAUST GASES
EP0529243A1 (en) * 1991-08-09 1993-03-03 A.Ahlstrom Corporation Method of treating process gases or flue gases containing halogenous compounds
WO1995018667A1 (en) * 1994-01-06 1995-07-13 University Of Waterloo Prevention of formation and destruction of organohalogen compounds in incineration of waste materials

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2785976A1 (en) 1998-11-17 2000-05-19 Air Liquide WASTE COMBUSTION PROCESS FOR REDUCING DIOXIN EMISSIONS
EP1078675A2 (en) * 1999-08-27 2001-02-28 Praxair Technology, Inc. Fluid separation process and separation system therefor
EP1078675A3 (en) * 1999-08-27 2002-06-26 Praxair Technology, Inc. Fluid separation process and separation system therefor
WO2007069990A1 (en) * 2005-12-16 2007-06-21 Mölnlycke Health Care Ab Method for perforating heat meltable material

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AU3873595A (en) 1996-06-06
FI945402A0 (en) 1994-11-16
FI945402A (en) 1996-05-17

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