WO1996023577A1 - Regeneration of carbonate minerals used in gas purification processes - Google Patents

Regeneration of carbonate minerals used in gas purification processes Download PDF

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Publication number
WO1996023577A1
WO1996023577A1 PCT/SE1996/000074 SE9600074W WO9623577A1 WO 1996023577 A1 WO1996023577 A1 WO 1996023577A1 SE 9600074 W SE9600074 W SE 9600074W WO 9623577 A1 WO9623577 A1 WO 9623577A1
Authority
WO
WIPO (PCT)
Prior art keywords
granules
carbonate
working process
rotor
mill
Prior art date
Application number
PCT/SE1996/000074
Other languages
French (fr)
Inventor
Lars LIDSTRÖM
Original Assignee
Senea Miljöteknik Ab
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 Senea Miljöteknik Ab filed Critical Senea Miljöteknik Ab
Priority to PL96321320A priority Critical patent/PL321320A1/en
Priority to AU46374/96A priority patent/AU4637496A/en
Publication of WO1996023577A1 publication Critical patent/WO1996023577A1/en
Priority to FI973141A priority patent/FI973141A/en

Links

Classifications

    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B01J20/043—Carbonates or bicarbonates, e.g. limestone, dolomite, aragonite
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28002—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their physical properties
    • B01J20/28004—Sorbent size or size distribution, e.g. particle size
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3433—Regenerating or reactivating of sorbents or filter aids other than those covered by B01J20/3408 - B01J20/3425
    • 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
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
    • B01J2220/56—Use in the form of a bed

Definitions

  • the present invention relates to a method of regenerating carbonate granules used in gas purification plants, for instance mineral granules rich in limestone, such as lime ⁇ stone and dolomite in accordance with the preamble of Claim 1.
  • the limestone granules are passed to a separation zone where they are regenerated and cleaned mechanically with the aid of a rotating drum which causes the limestone granules to rub against one another and therewith wear away the surface coatings on the granules.
  • This abrasion results in separation of the surface coating, although only after a relatively long granule residence time in the separation zone.
  • the fine-grain material rubbed from the granules can then be sieved and subsequently dumped.
  • the object of the present invention is to provide a novel and improved technique for removing chemical compounds that have formed on the mineral surfaces, therewith to enable essen ⁇ tially optimal use of regenerated carbonate granules in a simple and economic manner.
  • Coatings that are formed by chemical reaction with compounds in the gas being cleaned can be relatively hard and the energy input needs to be rela- tively high in order to clean the carbonate granules effec ⁇ tively.
  • SO ⁇ -compounds for instance, can be relatively hard and the energy input needs to be rela- tively high in order to clean the carbonate granules effec ⁇ tively.
  • coating separation can be controlled and guided in a completely different fashion with the aid of different procedures, as described below with reference to the modus operandi of the mill.
  • the energy input per unit volume of attrition or grinding space is very large in comparison with the energy input of rotating drums, meaning that the mill installation requires relatively little space for the same energy input.
  • the mill can be constructed on both a small and a large scale to no detriment, and the carbonate granules that have been cleaned of their coatings in the mill can be recycled to the gas purification plant with optimal results both with regard to the degree of separation and to a suitable particle-size distribution.
  • the contaminated material is transported through an agitated mill in a dry system, which is preferred in this case, with the aid of gravitational forces.
  • the rate at which the contaminated material passes through the mill can be varied by commensurate adjustment of the devices that feed the mineral granules into the mill and the devices that discharge said minerals therefrom.
  • the attrition principle to which the invention refers can also be characterized as containing an intrinsic dynamic classification function, which contributes towards effective separation of the chemical compounds that form on the surfaces of the granules.
  • Smaller granules will, in princi ⁇ ple, move more quickly through the mill than larger granules. Since sulphur compounds are adsorbed on the surfaces of the granules, the amount of substances that coat the granules per unit of surface area is essentially the same on both large and small granules in the present context. In follows from this that larger granules will have a slightly greater abrading effect than smaller granules.
  • the illustrated plant includes a gas cleansing vessel 1 which includes a filling or bed of carbonate granules having a size of approximately 5-10 mm.
  • the fresh, unused mineral granules are fed to the upper part of the vessel through the medium of feeder means, as indicated by arrow 2, and used, contaminated granules are discharged from the lower part of the vessel through the medium of discharge means 3.
  • a given proportion of the discharged granules can be returned to the gas cleansing plant without separating the contaminated coatings from the granules, as indicated by the material flow 4.
  • the devices referenced 1-4 are not embraced by the invention, and are merely shown to provide a better under ⁇ standing of the invention.
  • the proportion of carbonate granules that are to be de-coated are passed down into a vessel 5.
  • the supply of mineral granules to an agitating, stationary mill is regulated with the aid of a feeder 6, which is preferably a screw feeder.
  • the mineral granules are led to the mill 7, which in the present case is an agitated mill in which abrading and attrition are achieved by virtue of agitating the mineral granules, indicated at 7', with the aid of a highspeed, movable rotor 7" provided with rods 7 .
  • the grinding and attrition effect is thus achieved by pressure and shear forces and by movement between the carbonate granules themselves, said forces being generated by means of the aforesaid rotor or agitator, which will normally rotate at a speed of about 80 rpm and deliver a high power per unit of mill volume.
  • the desired degree of abrasion and attrition of the carbonate granules in the mill 7 can be adapted to the requirements placed on the gas cleansing capacity of the thus regenerated material, i.e. by increasing or decreasing the quantity of sieved fine-fraction. This is also an important factor, since carbonate minerals can have mutually different hardnesses, different sulphur adsorption capacities, etc., which may require corrections in order to achieve suitable process properties.
  • the mill 7 may be provided conveniently with a speed regula ⁇ tor which will enable the desired energy outtake from the mill to be controlled in a simple manner.
  • the energy consumed per unit of weight of processed material controls the amount of fine-fraction formed when working the material.
  • the amount of energy consumed per unit of weight is also a function of the level of the medium in the mill with a rotor that includes a given number of outwardly projecting ele ⁇ ments, suitably rods.
  • energy consumption can also be regulated by decreasing or increasing the level of the mineral granules in the mill 7, thereby increasing or decreasing the number of rods 7" ' that come into contact with the mill charge.
  • the balance between abrading and grinding the granules can be influenced in accordance with the particular requirements prevailing in each individual case, by appropriate configura ⁇ tion of the grinding tools, i.e. the rods, or by appropriate selection of the spacing therebetween.
  • the extent to which the carbonate granules 7' are abraded and/or ground is determined partly by the amount of sulphur to be adsorbed, partly to the cleanliness requirement of these granules subsequent to the regeneration process, and partly by the requirement to perform the granule regeneration process in a manner in which the delivery of fresh material will compensate for the amount of separated material as far as possible.
  • this inter ⁇ play will result in the gas resistance in the sulphur- cleansing vessel to be held as constant as possible, by taking appropriate measures in accordance with the afore- going. From an economical aspect, it is also important to keep material separation to the lowest possible level, so as to avoid unnecessary losses of carbonate material.
  • the discharge of material from the mill 7 and delivery of the material to a sieve or screen 9 is regulated with the aid of a discharge feeder 8, suitably a disc feeder.
  • the screen 9 separates a fine-fraction 10 containing the impurities, said fine-fraction normally corresponding to 5% of the weight of carbinate granules, while oversize granules 11 captured by the sieve are returned to the sulphur cleansing process.
  • the sieve 9 may have two or three tiers. A two or three tier sieve will enable the separation and possible abrasion of an intermediate fraction 12 of selected particle size. In some cases, this may be an appropriate procedure in maintaining the desired average granule size in the sulphur cleansing plant, which is preferred with regard to obtaining suitable resistance to the gases that flow through the vessel 1.

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

Abstract

There is described a method of regenerating carbonate granules used in a gas cleansing plant in which gas to be cleansed flows through a bed of carbonate granules, e.g. mineral granules rich in limestone and having an approximate size of 5-10 mm, by removing from said granules surface coatings formed by impurities, such as SOx-impurities, in the gas cleansing process. The granules removed from the bed ar worked mechanically in a manner which subjects the granules to pressure forces and shear forces. The mechanical working process is effected by the mutal infuence of the carbonate granules on one another in a mill (7) having a rotor (7') provided with outwardly projecting elements (7'''), said elements transmitting the energy of rotor motion to the carbonate granules (7'), whereafter regenerated carbonate granules having an approximate size of 5-10 mm are separated from the thus worked material and returned to the bed.

Description

Regeneration of carbonate minerals used in gas purification processes
The present invention relates to a method of regenerating carbonate granules used in gas purification plants, for instance mineral granules rich in limestone, such as lime¬ stone and dolomite in accordance with the preamble of Claim 1.
It is known to use one or more magazines which contain a bed of SOχ-absorbent substances, such as limestone, in conjunc¬ tion with the burning of sulphurous fuels in order to extract sulphur from the flue gases; see for instance SE-B-442 777 and WO 94/08697 in this regard. Flue gases pass through the bed of SOχ-absorbent substance and are cleansed by virtue of the reaction of sulphur contaminants with and their adsorp¬ tion on the surfaces of the limestone granules, such as to form a coating on the granules. After the bed has passed through a cooling zone, the limestone granules are passed to a separation zone where they are regenerated and cleaned mechanically with the aid of a rotating drum which causes the limestone granules to rub against one another and therewith wear away the surface coatings on the granules. This abrasion results in separation of the surface coating, although only after a relatively long granule residence time in the separation zone. The fine-grain material rubbed from the granules can then be sieved and subsequently dumped.
The object of the present invention is to provide a novel and improved technique for removing chemical compounds that have formed on the mineral surfaces, therewith to enable essen¬ tially optimal use of regenerated carbonate granules in a simple and economic manner.
To this end it is proposed that in a regeneration method of the kind defined in the introduction the carbonate granules are processed in the manner defined in the characterizing clause of Claim 1, i.e. by using an agitated mill in which the carbonate granules being regenerated themselves act as grinding medium such as to remove the chemical compounds from the surfaces of the carbonate granules. This technique finds its major use in the cleansing of sulphur-containing gases.
Coatings that are formed by chemical reaction with compounds in the gas being cleaned, such as SOχ-compounds for instance, can be relatively hard and the energy input needs to be rela- tively high in order to clean the carbonate granules effec¬ tively. In order to achieve effective cleaning of the granules in a rotating drum, it is necessary for the granules to remain in the drum for a relatively long period of time, and it is not clear to which extent the surfaces coated with SOχ-compounds and the non-coated surfaces are both worn away in the process. Neither does this technique enable the degree of abrasion to be varied other than by extending the resi¬ dence time of the granules in the drum, this latter solution only marginally influencing the extent to which the granules are abraded.
When using an agitated mill with the carbonate granules as the grinding medium, coating separation can be controlled and guided in a completely different fashion with the aid of different procedures, as described below with reference to the modus operandi of the mill.
In agitated mills, the energy input per unit volume of attrition or grinding space is very large in comparison with the energy input of rotating drums, meaning that the mill installation requires relatively little space for the same energy input. The mill can be constructed on both a small and a large scale to no detriment, and the carbonate granules that have been cleaned of their coatings in the mill can be recycled to the gas purification plant with optimal results both with regard to the degree of separation and to a suitable particle-size distribution. The contaminated material is transported through an agitated mill in a dry system, which is preferred in this case, with the aid of gravitational forces. The rate at which the contaminated material passes through the mill can be varied by commensurate adjustment of the devices that feed the mineral granules into the mill and the devices that discharge said minerals therefrom.
The attrition principle to which the invention refers can also be characterized as containing an intrinsic dynamic classification function, which contributes towards effective separation of the chemical compounds that form on the surfaces of the granules. Smaller granules will, in princi¬ ple, move more quickly through the mill than larger granules. Since sulphur compounds are adsorbed on the surfaces of the granules, the amount of substances that coat the granules per unit of surface area is essentially the same on both large and small granules in the present context. In follows from this that larger granules will have a slightly greater abrading effect than smaller granules.
Tests have shown that when grinding mineral products, it is not only the physical processes associated with mechanical degradation that occur. The structure, surface properties and reaction tendency of the material also changes. In addition to producing newly formed surfaces and newly formed partic¬ les, the amount of energy delivered to the carbonate minerals also gives rise to a broken-lattice surface structure in which the microcrack density is such as to increase reactivi- ty beyond that which can be explained by the size of the individual granules or particles. This can be observed with the aid of different measuring methods, such as differential thermoanalysis, X-ray analysis or nuclear magnetic resonance.
Further characteristic features of the invention are set forth in the depending claims. The invention will now be described with reference to the accompanying drawing which illustrates very schematically an exemplifying embodiment of a plant at which the inventive method can be carried out.
The illustrated plant includes a gas cleansing vessel 1 which includes a filling or bed of carbonate granules having a size of approximately 5-10 mm. The fresh, unused mineral granules are fed to the upper part of the vessel through the medium of feeder means, as indicated by arrow 2, and used, contaminated granules are discharged from the lower part of the vessel through the medium of discharge means 3. A given proportion of the discharged granules can be returned to the gas cleansing plant without separating the contaminated coatings from the granules, as indicated by the material flow 4. The devices referenced 1-4 are not embraced by the invention, and are merely shown to provide a better under¬ standing of the invention.
The proportion of carbonate granules that are to be de-coated are passed down into a vessel 5. The supply of mineral granules to an agitating, stationary mill is regulated with the aid of a feeder 6, which is preferably a screw feeder.
Thus, the mineral granules are led to the mill 7, which in the present case is an agitated mill in which abrading and attrition are achieved by virtue of agitating the mineral granules, indicated at 7', with the aid of a highspeed, movable rotor 7" provided with rods 7 . The grinding and attrition effect is thus achieved by pressure and shear forces and by movement between the carbonate granules themselves, said forces being generated by means of the aforesaid rotor or agitator, which will normally rotate at a speed of about 80 rpm and deliver a high power per unit of mill volume.
The desired degree of abrasion and attrition of the carbonate granules in the mill 7 can be adapted to the requirements placed on the gas cleansing capacity of the thus regenerated material, i.e. by increasing or decreasing the quantity of sieved fine-fraction. This is also an important factor, since carbonate minerals can have mutually different hardnesses, different sulphur adsorption capacities, etc., which may require corrections in order to achieve suitable process properties.
The mill 7 may be provided conveniently with a speed regula¬ tor which will enable the desired energy outtake from the mill to be controlled in a simple manner. The energy consumed per unit of weight of processed material controls the amount of fine-fraction formed when working the material.
The amount of energy consumed per unit of weight is also a function of the level of the medium in the mill with a rotor that includes a given number of outwardly projecting ele¬ ments, suitably rods. Thus, energy consumption can also be regulated by decreasing or increasing the level of the mineral granules in the mill 7, thereby increasing or decreasing the number of rods 7" ' that come into contact with the mill charge.
The balance between abrading and grinding the granules can be influenced in accordance with the particular requirements prevailing in each individual case, by appropriate configura¬ tion of the grinding tools, i.e. the rods, or by appropriate selection of the spacing therebetween.
The extent to which the carbonate granules 7' are abraded and/or ground is determined partly by the amount of sulphur to be adsorbed, partly to the cleanliness requirement of these granules subsequent to the regeneration process, and partly by the requirement to perform the granule regeneration process in a manner in which the delivery of fresh material will compensate for the amount of separated material as far as possible. In this regard, it is important that this inter¬ play will result in the gas resistance in the sulphur- cleansing vessel to be held as constant as possible, by taking appropriate measures in accordance with the afore- going. From an economical aspect, it is also important to keep material separation to the lowest possible level, so as to avoid unnecessary losses of carbonate material.
If a balance with regard to gas resistance cannot be achieved by adding fresh material or by increased working of the material, it may also be necessary to remove an intermediate fraction when this fraction is found to have been increased to an extent at which it is able to influence the gas resistance in the reactor.
The discharge of material from the mill 7 and delivery of the material to a sieve or screen 9 is regulated with the aid of a discharge feeder 8, suitably a disc feeder. The screen 9 separates a fine-fraction 10 containing the impurities, said fine-fraction normally corresponding to 5% of the weight of carbinate granules, while oversize granules 11 captured by the sieve are returned to the sulphur cleansing process. The sieve 9 may have two or three tiers. A two or three tier sieve will enable the separation and possible abrasion of an intermediate fraction 12 of selected particle size. In some cases, this may be an appropriate procedure in maintaining the desired average granule size in the sulphur cleansing plant, which is preferred with regard to obtaining suitable resistance to the gases that flow through the vessel 1.
In the case of applications where separation places no particular requirements on the accuracy of the sieving process it may suffice with internal screening of the material in the mill 7. This is achieved by mounting a screening plate 13 on the mill bottom, and discharging the aforesaid larger granules 14 from the mill through a grating 15 in the mill mantle. It will be understood that the invention is not restricted to the aforedescribed and illustrated methods and procedures and that the invention can be implemented in any desired manner within the scope of the following claims.

Claims

C l a i m s
1. A method of regenerating carbonate granules used in a gas cleansing plant in which gas to be cleansed flows through a bed of carbonate granules, e.g. mineral granules rich in limestone and having an approximate size of 5-10 mm, by removing from said granules surface coatings that are formed by impurities, such as S0χ-impurities, in the gas cleansing process, wherein the granules are removed from the bed and worked mechanically such as to subject the granules to pressure forces and shear forces, characterized in that the mechanical working process is effected by the mutual influ¬ ence of the carbonate granules on one another in a mill (7) having a rotor (7") provided with outwardly projecting elements ( T ' ' ) , said elements transmitting the energy of rotor motion to the carbonate granules (7'), whereafter regenerated carbonate granules having an approximate size of 5-10 mm are separated from the thus worked material and returned to the bed.
2. A method according to Claim 1, characterized in that the granule working process is controlled by adjusting the level of carbonate granules in the mill (7).
3. A method according to Claim 1 or Claim 2, characterized in that the granule working process is controlled by adjust¬ ing the speed of the rotor (7").
4. A method according to any one of Claims 1-3, characterized by using a rotor (7") whose outwardly projecting elements
(7'") have the form of rods.
5. A method according to any one of Claims 1-4, characterized in that the granule working process is controlled by an appropriate choice of the number of rods (7' ' ' ) on the rotor (7").
6. A method according to any one of claims 1-5, characterized in that the granule working process is controlled by an appropriate choice of the dimensions of the individual rods (7'").
7. A method according to any one of claims 1-6, characterized in that the granule working process is effected so that the removed coatings will be at most 5% of the weight of the carbonate granules.
8. A method according to any one of Claims 1-7, characterized in that the product obtained by the working process is sieved into two or three fractions (10, 11, 12).
9. A method according to any one of Claims 1-8, characterized in that an intermediate product (12) obtained after the working process is subjected to a certain degree of grinding after sieving.
PCT/SE1996/000074 1995-01-30 1996-01-24 Regeneration of carbonate minerals used in gas purification processes WO1996023577A1 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
PL96321320A PL321320A1 (en) 1995-01-30 1996-01-24 Method of regenerating carbonate minerals used in gas purification processes
AU46374/96A AU4637496A (en) 1995-01-30 1996-01-24 Regeneration of carbonate minerals used in gas purification processes
FI973141A FI973141A (en) 1995-01-30 1997-07-29 Regeneration of carbonate minerals used in gas purification processes

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE9500323-2 1995-01-30
SE9500323A SE510535C2 (en) 1995-01-30 1995-01-30 Methods of regenerating used carbonate grains during gas purification

Publications (1)

Publication Number Publication Date
WO1996023577A1 true WO1996023577A1 (en) 1996-08-08

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Application Number Title Priority Date Filing Date
PCT/SE1996/000074 WO1996023577A1 (en) 1995-01-30 1996-01-24 Regeneration of carbonate minerals used in gas purification processes

Country Status (6)

Country Link
AU (1) AU4637496A (en)
CZ (1) CZ229897A3 (en)
FI (1) FI973141A (en)
PL (1) PL321320A1 (en)
SE (1) SE510535C2 (en)
WO (1) WO1996023577A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19962734A1 (en) * 1999-12-23 2001-06-28 Wolf Dieter Hamisch Removal of gaseous boron trifluoride and pretreatment of process waste gas involves spraying with water or aqueous solution to form boron oxide and hydrogen fluoride and optionally condense water and acid
EP2011558A1 (en) * 2007-05-16 2009-01-07 Babcock Noell GmbH Facility and method for removing contaminants from exhaust gas
KR101298727B1 (en) * 2011-06-28 2013-08-21 현대제철 주식회사 Purification apparatus using adsorption and filtration and method for back washing of the purification apparatus

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE442777B (en) * 1984-03-16 1986-01-27 Lennart Karlsson DEVICE FOR AIR CONDITIONING AND PURIFICATION OF GAS, primarily ROCKS
US4710365A (en) * 1982-08-28 1987-12-01 Rheinisch-Westfalisches Elektrizitatswerk Aktiengesellschaft Process for the dry removal of sulfur dioxide from flue gas
WO1990009226A1 (en) * 1989-02-15 1990-08-23 Imatran Voima Oy Process and equipment for cleaning of flue gases
SE500037C2 (en) * 1992-10-22 1994-03-28 Svenska Energinaet Miljoetekni Method for purifying SO 7x] containing flue gases
WO1995006512A1 (en) * 1993-09-03 1995-03-09 Lidstroem Lars Joergen Flue gas purification

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4710365A (en) * 1982-08-28 1987-12-01 Rheinisch-Westfalisches Elektrizitatswerk Aktiengesellschaft Process for the dry removal of sulfur dioxide from flue gas
SE442777B (en) * 1984-03-16 1986-01-27 Lennart Karlsson DEVICE FOR AIR CONDITIONING AND PURIFICATION OF GAS, primarily ROCKS
WO1990009226A1 (en) * 1989-02-15 1990-08-23 Imatran Voima Oy Process and equipment for cleaning of flue gases
SE500037C2 (en) * 1992-10-22 1994-03-28 Svenska Energinaet Miljoetekni Method for purifying SO 7x] containing flue gases
WO1995006512A1 (en) * 1993-09-03 1995-03-09 Lidstroem Lars Joergen Flue gas purification

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19962734A1 (en) * 1999-12-23 2001-06-28 Wolf Dieter Hamisch Removal of gaseous boron trifluoride and pretreatment of process waste gas involves spraying with water or aqueous solution to form boron oxide and hydrogen fluoride and optionally condense water and acid
EP2011558A1 (en) * 2007-05-16 2009-01-07 Babcock Noell GmbH Facility and method for removing contaminants from exhaust gas
KR101298727B1 (en) * 2011-06-28 2013-08-21 현대제철 주식회사 Purification apparatus using adsorption and filtration and method for back washing of the purification apparatus

Also Published As

Publication number Publication date
PL321320A1 (en) 1997-12-08
AU4637496A (en) 1996-08-21
SE9500323D0 (en) 1995-01-30
FI973141A0 (en) 1997-07-29
SE9500323L (en) 1996-07-31
CZ229897A3 (en) 1998-02-18
FI973141A (en) 1997-07-29
SE510535C2 (en) 1999-05-31

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