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WO1996016722A1 - Method for separating gaseous pollutants from hot process gases - Google Patents

Method for separating gaseous pollutants from hot process gases Download PDF

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Publication number
WO1996016722A1
WO1996016722A1 PCT/SE1995/001403 SE9501403W WO9616722A1 WO 1996016722 A1 WO1996016722 A1 WO 1996016722A1 SE 9501403 W SE9501403 W SE 9501403W WO 9616722 A1 WO9616722 A1 WO 9616722A1
Authority
WO
WIPO (PCT)
Prior art keywords
mixer
dust
process gases
supplied
burnt lime
Prior art date
Application number
PCT/SE1995/001403
Other languages
French (fr)
Inventor
Stefan Åhman
Nils Bringfors
Original Assignee
ABB Fläkt 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
Priority to PL95320426A priority Critical patent/PL320426A1/en
Priority to CZ971574A priority patent/CZ157497A3/en
Priority to EP95939455A priority patent/EP0804273A1/en
Priority to HU9800501A priority patent/HU220402B/en
Priority to AU41264/96A priority patent/AU692014B2/en
Priority to UA97063196A priority patent/UA52592C2/en
Priority to SI9520141A priority patent/SI9520141A/en
Priority to RU97111848A priority patent/RU2147919C1/en
Priority to MD97-0166A priority patent/MD1020C2/en
Application filed by ABB Fläkt AB filed Critical ABB Fläkt AB
Priority to EE9700215A priority patent/EE04049B1/en
Priority to CA002205995A priority patent/CA2205995C/en
Priority to BR9509831A priority patent/BR9509831A/en
Priority to RO97-00951A priority patent/RO115421B1/en
Priority to SK661-97A priority patent/SK66197A3/en
Priority to JP51717096A priority patent/JP3640674B2/en
Publication of WO1996016722A1 publication Critical patent/WO1996016722A1/en
Priority to FI972233A priority patent/FI972233A7/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
    • B01D53/46—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
    • 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

Definitions

  • the present invention relates to a method for sepa ⁇ rating gaseous pollutants, such as sulphur dioxide, from hot process gases, such as flue gases, in which method the process gases are passed through a contact reactor, in which a particulate absorbent material, which is reac ⁇ tive with the gaseous pollutants, is introduced in mois ⁇ tened state into the process gases for converting the gaseous pollutants into separable dust, whereupon the process gases are passed through a dust separator, in which dust is separated from the process gases and from which the cleaned process gases are discharged, part of the dust separated in the dust separator being passed to a mixer, in which it is mixed and supplied with water so as to be moistened, whereupon it is recirculated as ab- sorbent material by being introduced into the process gases together with an addition of fresh absorbent.
  • a contact reactor in which a particulate absorbent material, which is reac ⁇ tive with the gaseous pollutants, is introduced in mois ⁇ tened state into the process gases for
  • the above-described method for separating gaseous pollutants from hot process gases is known from e.g. SE 8504675-3 and SE 8904106-5.
  • use is preferably made of slaked lime (calcium hydroxide) in particle form as fresh absorbent.
  • This absorbent is mixed with dust which has been separated from the process gases in the dust separator, whereupon the mixture is supplied with water to be introduced, in moistened state, into the flue gases in the contact reac ⁇ tor.
  • the slaked lime is comparatively expensive, and so various experiments have been made to use burnt lime (calcium oxide) instead, which is considerably less ex ⁇ pensive.
  • the object of the present invention is to provide a method for separating gaseous pollutants from hot process gases, in which the slaked lime can be replaced by burnt lime, without necessitating an expensive, separate plant for slaking the burnt lime.
  • this object is achieved by a method which is of the type mentioned by way of in- troduction and is characterised in that burnt lime is added as fresh absorbent, and that the major part of the dust separated in the dust separator is supplied to and discharged from the mixer in a substantially continuous flow, the dust being kept so long in the mixer and being recirculated so many times that the total residence time of the burnt lime in the mixer in moistened state is suf ⁇ ficiently long for the burnt lime to have time to react substantially completely with water supplied to the mixer and form slaked lime.
  • the fresh absorbent in the form of burnt lime is supplied preferably to the mixer, but it may also be added to that part of the dust separated in the dust separator which is supplied to the mixer. Alternatively, the burnt lime can be introduced directly into the flue gases in the contact reactor.
  • An air flow is suitably supplied to the mixer in order to fluidise the dust mixed therein and thus improve the mixture.
  • FIG. 1 Schematically illustrates a plant for cleaning flue gases from a coal-fired central heating plant, the cleaning plant being provided with equipment for carrying out the method according to the present invention.
  • the drawing schematically illustrates a plant for cleaning flue gases from a coal-fired central heating plant 1, said flue gases containing dust, such as fly ash, and gaseous pollutants, such as sulphur dioxide.
  • a preheating device 2 is arranged to transmit heat from the hot flue gases to combustion air, which via a duct 2a is supplied to the central heating plant 1 by means of a fan 3.
  • the hot flue gases are conveyed through a duct 4 to a dust separator 5, which in the embodiment shown is an electrostatic precipitator having three successive preci- pitator units, through which the flue gases are passed to be cleaned.
  • the flue gases cleaned in this manner are via a duct 6 passed to a flue gas fan 7, which via a duct 8 feeds them on to a chimney 9 to be emitted into the at ⁇ mosphere.
  • the dust separator can also be a bag filter.
  • the duct 4 comprises a vertical portion which forms a contact reactor 10.
  • a mixer 11 communicates with the contact reactor 10 in the lower part thereof.
  • the mixer 11 introduces a particulate absorbent material, which is reactive with the gaseous pollutants in the flue gases, in moistened state into the flue gases in the lower part of the contact reactor 10. This absorbent material con ⁇ verts the gaseous pollutants into dust, which is separat ⁇ ed in the precipitator 5.
  • the dust particles separated in the precipitator 5 are collected in the hoppers 12 of the precipitator units.
  • the major part of the collected dust particles is recirculated in the system in a manner which will be described in detail below.
  • the remainder of the collect ⁇ ed dust particles are transported away in a manner which will not be described in detail, for instance by means of a worm conveyor.
  • the mixer 11 is of the type as described in SE- 9404104-3.
  • the mixer 11 has essentially the shape of a double-bottom box. Between the two bottoms, the upper of which consists of a tensioned fluidising cloth 13 of polyester, there is a chamber 14, to which air for fluidising the particulate absorbent material in the mixer 11 is conducted through an air supply conduct 15.
  • Water is supplied to the mixer 11 through a water supply conduit 16 and nozzles 17, which are arranged in the upper portion of the mixer.
  • the particulate material which is to be mixed is supplied to the mixer 11 through two material inlets 18 and 19 at the inlet end of the mixer.
  • the mixer 11 further comprises a mechanical mixing mechanism 20 consisting of two cooperating, parallel agi ⁇ tators (of which only one is shown in the drawing), each having a horizontal shaft and, mounted thereon, a plura- lity of inclined elliptic plates.
  • the outlet end of the mixer 11 extends into the contact reactor 10 in order to continuously supply thereto through an overflow 21 well- mixed, moistened absorbent material.
  • That part of the dust particles collected in the hoppers 12 of the precipitator units which is to be recirculated in the system is supplied to the mixer 11 through the inlet 19.
  • Particulate burnt lime (calcium oxide) is supplied to the mixer 11 through the inlet 18 to be mixed with the dust particles supplied through the inlet 19.
  • the mixture is moistened with water supplied through the nozzles 17.
  • Water is supplied through the nozzles 17 also in order to slake the burnt lime supplied to the mixer 11.
  • the mixer produces a homogeneously moistened, homogeneous mixture of material particles, which are, through the overflow 21 of the mixer 11, continuously supplied to the contact reactor 10 as absorbent material.
  • the residence time of the material particles in the mixer 11 is in the order of 5-60 s, especially 10-20 s.
  • the residence time as stated above (10-20 s) of the material particles in the mixer 11, i.e. the time during which the lime particles are in moistened state, is in- sufficient for the burnt lime to have time to react com ⁇ pletely with the water added for slaking and form slaked lime. Such a reaction is relatively slow and takes seve ⁇ ral minutes.
  • the Exam- pie states the conditions prevailing at points A, B and C in the drawing, i.e. in the duct 4 before the mixer 11, in the reactor 10 after the mixer 11 at the inlet of the precipitator 5 and at the outlet of the precipitator 5, respectively.
  • the dust at A is substantially fly ash, whereas the dust at B is fly ash and absorbent material.
  • the particulate absorbent mate ⁇ rial including the burnt lime, which is being slaked, is thus circulated on the average about 35 times (1.0 x 103,933 / 2,930 * 35) in the system before being discharged at D.
  • the total residence time of the absor ⁇ bent material in the mixer 11 thus is 350-700 s, i.e. in the order of 6-12 min, which is sufficient for the burnt lime to have time to be slaked.
  • the total consumption of water in the above Example is 3,366 1/h, of which 152 1/h is required for the slak ⁇ ing of lime.
  • the moisture content of the absorbent material discharged from the mixer 11 is about 6%.
  • the moisture con ⁇ tent can, according to the composition of the mixture, suitably be varied in the range 2-15%.
  • the circulation number will, by analogy with that stated above, be about 110 (0.980 x 103,993 / 930 * 110), which in turn yields a residence time of 1,100-2,200 s, i.e. in the order of 18-37 min.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

Hot process gases are passed through a contact reactor (10), in which a particulate absorbent material, which is reactive with gaseous pollutants in the gases, is introduced into the gases to convert the gaseous pollutants into separable dust. The process gases are then passed through a dust separator (5). The major part of the dust separated in the dust separator (5) is passed to a mixer (11), in which it is mixed and moistened, whereupon it is recirculated as absorbent material by being introduced, together with fresh absorbent, into the process gases. Burnt lime is added as fresh absorbent. The dust is kept so long in the mixer and recirculated so many times that the total residence time of the burnt lime in the mixer in moistened state is sufficiently long for the burnt lime to react substantially completely with water supplied to the mixer and form slaked lime.

Description

METHOD FOR SEPARATING GASEOUS POLLUTANTS FROM HOT PROCESS GASES
The present invention relates to a method for sepa¬ rating gaseous pollutants, such as sulphur dioxide, from hot process gases, such as flue gases, in which method the process gases are passed through a contact reactor, in which a particulate absorbent material, which is reac¬ tive with the gaseous pollutants, is introduced in mois¬ tened state into the process gases for converting the gaseous pollutants into separable dust, whereupon the process gases are passed through a dust separator, in which dust is separated from the process gases and from which the cleaned process gases are discharged, part of the dust separated in the dust separator being passed to a mixer, in which it is mixed and supplied with water so as to be moistened, whereupon it is recirculated as ab- sorbent material by being introduced into the process gases together with an addition of fresh absorbent.
The above-described method for separating gaseous pollutants from hot process gases is known from e.g. SE 8504675-3 and SE 8904106-5. According to these two docu- ments, use is preferably made of slaked lime (calcium hydroxide) in particle form as fresh absorbent. This absorbent is mixed with dust which has been separated from the process gases in the dust separator, whereupon the mixture is supplied with water to be introduced, in moistened state, into the flue gases in the contact reac¬ tor. The slaked lime is comparatively expensive, and so various experiments have been made to use burnt lime (calcium oxide) instead, which is considerably less ex¬ pensive. In these experiments, a plant had to be used, in which the burnt lime has first been slaked, i.e. the calcium oxide has been caused to react with water to form calcium hydroxide, before being introduced into the cleaning process. Such a lime slaking plant is expensive, which means that the expected profit when changing from slaked lime to burnt lime failed to appear.
The object of the present invention is to provide a method for separating gaseous pollutants from hot process gases, in which the slaked lime can be replaced by burnt lime, without necessitating an expensive, separate plant for slaking the burnt lime.
According to the invention, this object is achieved by a method which is of the type mentioned by way of in- troduction and is characterised in that burnt lime is added as fresh absorbent, and that the major part of the dust separated in the dust separator is supplied to and discharged from the mixer in a substantially continuous flow, the dust being kept so long in the mixer and being recirculated so many times that the total residence time of the burnt lime in the mixer in moistened state is suf¬ ficiently long for the burnt lime to have time to react substantially completely with water supplied to the mixer and form slaked lime. The fresh absorbent in the form of burnt lime is supplied preferably to the mixer, but it may also be added to that part of the dust separated in the dust separator which is supplied to the mixer. Alternatively, the burnt lime can be introduced directly into the flue gases in the contact reactor.
An air flow is suitably supplied to the mixer in order to fluidise the dust mixed therein and thus improve the mixture.
The invention will now be described in more detail with reference to the accompanying drawing, which schema¬ tically illustrates a plant for cleaning flue gases from a coal-fired central heating plant, the cleaning plant being provided with equipment for carrying out the method according to the present invention. The drawing schematically illustrates a plant for cleaning flue gases from a coal-fired central heating plant 1, said flue gases containing dust, such as fly ash, and gaseous pollutants, such as sulphur dioxide. A preheating device 2 is arranged to transmit heat from the hot flue gases to combustion air, which via a duct 2a is supplied to the central heating plant 1 by means of a fan 3.
The hot flue gases are conveyed through a duct 4 to a dust separator 5, which in the embodiment shown is an electrostatic precipitator having three successive preci- pitator units, through which the flue gases are passed to be cleaned. The flue gases cleaned in this manner are via a duct 6 passed to a flue gas fan 7, which via a duct 8 feeds them on to a chimney 9 to be emitted into the at¬ mosphere. The dust separator can also be a bag filter.
The duct 4 comprises a vertical portion which forms a contact reactor 10. A mixer 11 communicates with the contact reactor 10 in the lower part thereof. The mixer 11 introduces a particulate absorbent material, which is reactive with the gaseous pollutants in the flue gases, in moistened state into the flue gases in the lower part of the contact reactor 10. This absorbent material con¬ verts the gaseous pollutants into dust, which is separat¬ ed in the precipitator 5.
The dust particles separated in the precipitator 5 are collected in the hoppers 12 of the precipitator units. The major part of the collected dust particles is recirculated in the system in a manner which will be described in detail below. The remainder of the collect¬ ed dust particles are transported away in a manner which will not be described in detail, for instance by means of a worm conveyor.
The mixer 11 is of the type as described in SE- 9404104-3. Thus, the mixer 11 has essentially the shape of a double-bottom box. Between the two bottoms, the upper of which consists of a tensioned fluidising cloth 13 of polyester, there is a chamber 14, to which air for fluidising the particulate absorbent material in the mixer 11 is conducted through an air supply conduct 15. Water is supplied to the mixer 11 through a water supply conduit 16 and nozzles 17, which are arranged in the upper portion of the mixer. The particulate material which is to be mixed, is supplied to the mixer 11 through two material inlets 18 and 19 at the inlet end of the mixer. The mixer 11 further comprises a mechanical mixing mechanism 20 consisting of two cooperating, parallel agi¬ tators (of which only one is shown in the drawing), each having a horizontal shaft and, mounted thereon, a plura- lity of inclined elliptic plates. The outlet end of the mixer 11 extends into the contact reactor 10 in order to continuously supply thereto through an overflow 21 well- mixed, moistened absorbent material.
That part of the dust particles collected in the hoppers 12 of the precipitator units which is to be recirculated in the system is supplied to the mixer 11 through the inlet 19. Particulate burnt lime (calcium oxide) is supplied to the mixer 11 through the inlet 18 to be mixed with the dust particles supplied through the inlet 19. The mixture is moistened with water supplied through the nozzles 17. Water is supplied through the nozzles 17 also in order to slake the burnt lime supplied to the mixer 11. Owing to the construction of the mecha¬ nical mixing mechanism 20 and the fluidisation of the material particles supplied to the mixer 11, the mixer produces a homogeneously moistened, homogeneous mixture of material particles, which are, through the overflow 21 of the mixer 11, continuously supplied to the contact reactor 10 as absorbent material. The residence time of the material particles in the mixer 11 is in the order of 5-60 s, especially 10-20 s.
The residence time as stated above (10-20 s) of the material particles in the mixer 11, i.e. the time during which the lime particles are in moistened state, is in- sufficient for the burnt lime to have time to react com¬ pletely with the water added for slaking and form slaked lime. Such a reaction is relatively slow and takes seve¬ ral minutes.
The invention will now be described in more detail with the aid of the theoretical Example below. The Exam- pie states the conditions prevailing at points A, B and C in the drawing, i.e. in the duct 4 before the mixer 11, in the reactor 10 after the mixer 11 at the inlet of the precipitator 5 and at the outlet of the precipitator 5, respectively.
A B C
Gas flow (Nm3/h) 100,000 103,993 103, ,993 Gas temperature ( cC) 125 65 65 S02 concentration (ppm) 1,150 280 172 Dust concentration (g/Nm3) 20 1,000 < 0. ,03
The dust at A is substantially fly ash, whereas the dust at B is fly ash and absorbent material.
At D, 2,930 kg of dust are discharged per hour, 2,000 kg being fly ash.
In this Example, the particulate absorbent mate¬ rial, including the burnt lime, which is being slaked, is thus circulated on the average about 35 times (1.0 x 103,933 / 2,930 * 35) in the system before being discharged at D. The total residence time of the absor¬ bent material in the mixer 11 thus is 350-700 s, i.e. in the order of 6-12 min, which is sufficient for the burnt lime to have time to be slaked.
The total consumption of water in the above Example is 3,366 1/h, of which 152 1/h is required for the slak¬ ing of lime. When this amount of water is consumed, the moisture content of the absorbent material discharged from the mixer 11 is about 6%. However, the moisture con¬ tent can, according to the composition of the mixture, suitably be varied in the range 2-15%.
If, in the above Example, the fly ash content of the flue gases at point A is zero, i.e. the discharge at D is 930 kg/h, the circulation number will, by analogy with that stated above, be about 110 (0.980 x 103,993 / 930 * 110), which in turn yields a residence time of 1,100-2,200 s, i.e. in the order of 18-37 min.

Claims

1. A method for separating gaseous pollutants, such as sulphur dioxide, from hot process gases, such as flue gases, in which method the process gases are passed through a contact reactor (10), in which a particulate absorbent material, which is reactive with the gaseous pollutants, is introduced in moistened state into the process gases for converting the gaseous pollutants into separable dust, whereupon the process gases are passed through a dust separator (5), in which dust is separated from the process gases and from which the cleaned process gases are discharged, part of the dust separated in the dust separator (5) being passed to a mixer (11), in which it is mixed and supplied with water so as to be moisten¬ ed, whereupon it is recirculated as absorbent material by being introduced into the process gases together with an addition of fresh absorbent, c h a r a c t e r i s e d in that burnt lime is added as fresh absorbent, and that the major part of the dust separated in the dust separator (5) is supplied to and discharged from the mixer (11) in a substantially continuous flow, the dust being kept so long in the mixer and being recirculated so many times that the total residence time of the burnt lime in the mixer (11) in moistened state is sufficiently long for the burnt lime to have time to react substantially com¬ pletely with water supplied to the mixer and form slaked lime.
2. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is supplied to the mixer (11).
3. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is added to that part of the dust separated in the dust separator ( 5) which is supplied to the mixer (11).
4. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is introduced directly into the flue gases in the contact reactor (10).
5. The method as claimed in any one of the preceding claims, c h a r a c t e r i s e d in that an air flow is supplied to the mixer (11) in order to fluidise the dust mixed therein.
PCT/SE1995/001403 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases WO1996016722A1 (en)

Priority Applications (16)

Application Number Priority Date Filing Date Title
MD97-0166A MD1020C2 (en) 1994-11-28 1995-11-24 Method for separating gaseous polluants from hot process gases
EP95939455A EP0804273A1 (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
HU9800501A HU220402B (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
AU41264/96A AU692014B2 (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
UA97063196A UA52592C2 (en) 1994-11-28 1995-11-24 Method of separation of gas polluant from hot process gases
SI9520141A SI9520141A (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
RU97111848A RU2147919C1 (en) 1994-11-28 1995-11-24 Method of separating gaseous impurities from hot process gases
PL95320426A PL320426A1 (en) 1994-11-28 1995-11-24 Method of removing gaseous pollutants from hot process gases
EE9700215A EE04049B1 (en) 1994-11-28 1995-11-24 A method for the separation of gaseous pollutants from thermal process gases
CZ971574A CZ157497A3 (en) 1994-11-28 1995-11-24 Method of separating gaseous contaminants from hot processing gases
CA002205995A CA2205995C (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
BR9509831A BR9509831A (en) 1994-11-28 1995-11-24 Method for the separation of gaseous pollutants from hot process gases
RO97-00951A RO115421B1 (en) 1994-11-28 1995-11-24 Process for the separation of gaseous pollutants from hot flue gases in heating installations
SK661-97A SK66197A3 (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases
JP51717096A JP3640674B2 (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from heat treatment gas
FI972233A FI972233A7 (en) 1994-11-28 1997-05-27 Method for separating gaseous pollutants from hot process gases

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE9404105A SE504440C2 (en) 1994-11-28 1994-11-28 Ways to separate gaseous pollutants from hot process gases
SE9404105-0 1994-11-28

Publications (1)

Publication Number Publication Date
WO1996016722A1 true WO1996016722A1 (en) 1996-06-06

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SE1995/001403 WO1996016722A1 (en) 1994-11-28 1995-11-24 Method for separating gaseous pollutants from hot process gases

Country Status (20)

Country Link
EP (1) EP0804273A1 (en)
JP (1) JP3640674B2 (en)
KR (1) KR100384589B1 (en)
CN (1) CN1080137C (en)
AU (1) AU692014B2 (en)
BR (1) BR9509831A (en)
CZ (1) CZ157497A3 (en)
EE (1) EE04049B1 (en)
FI (1) FI972233A7 (en)
HU (1) HU220402B (en)
MD (1) MD1020C2 (en)
PL (1) PL320426A1 (en)
RO (1) RO115421B1 (en)
RU (1) RU2147919C1 (en)
SE (1) SE504440C2 (en)
SI (1) SI9520141A (en)
SK (1) SK66197A3 (en)
UA (1) UA52592C2 (en)
WO (1) WO1996016722A1 (en)
ZA (1) ZA959876B (en)

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EP0882490A1 (en) * 1997-06-05 1998-12-09 ALOIS SCHEUCH GESELLSCHAFT m.b.H. Method of purifying pollutant containing gases
WO1999059704A1 (en) * 1998-05-18 1999-11-25 ABB Fläkt AB Method and apparatus for cleaning flue gases
WO2001032296A1 (en) * 1999-11-03 2001-05-10 Foster Wheeler Energia Oy Method and apparatus for binding pollutants in flue gas
JP2002518168A (en) * 1998-06-24 2002-06-25 エービービー フラクト アクチボラグ Flue gas cleaning method
JP3395036B2 (en) 1997-10-06 2003-04-07 日立造船株式会社 Method and apparatus for removing acid gas from exhaust gas
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WO2004026443A1 (en) 2002-09-20 2004-04-01 Alstom Technology Ltd Method and device for separating gaseous pollutants from hot process gases by absorption and a mixer for moistening particulate dust
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DE102007045751B4 (en) * 2006-10-24 2010-01-21 Scheuch Gmbh Apparatus and method for moistening a sorbent
US7766997B2 (en) 2007-12-21 2010-08-03 Alstom Technology Ltd Method of reducing an amount of mercury in a flue gas
US7850936B2 (en) 2008-02-18 2010-12-14 Alstom Technology Ltd Dry sulfur dioxide (SO2) scrubbing
EP2457637A1 (en) 2010-11-24 2012-05-30 Alstom Technology Ltd Method of cleaning a carbon dioxide rich flue gas and a boiler system
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US8728211B2 (en) 2012-03-30 2014-05-20 Alstom Technology Ltd Nozzle for spraying liquid and a mixer comprising the nozzle
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CN105617851A (en) * 2016-03-16 2016-06-01 中国科学院城市环境研究所 Efficient dual-tower semi-dry process desulfurization method and device
WO2019048582A1 (en) 2017-09-06 2019-03-14 S.A. Lhoist Recherche Et Developpement Process for treating flue gases in cds flue gas treatment

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UA52592C2 (en) 2003-01-15
MD1020C2 (en) 1999-07-31
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SK66197A3 (en) 1997-10-08
SE9404105L (en) 1996-05-29
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PL320426A1 (en) 1997-09-29
BR9509831A (en) 1997-09-30
HU220402B (en) 2002-01-28
JPH10509914A (en) 1998-09-29
FI972233A0 (en) 1997-05-27
EE04049B1 (en) 2003-06-16
JP3640674B2 (en) 2005-04-20
CN1080137C (en) 2002-03-06
SE504440C2 (en) 1997-02-10
ZA959876B (en) 1996-07-15
EP0804273A1 (en) 1997-11-05
AU692014B2 (en) 1998-05-28
RU2147919C1 (en) 2000-04-27
FI972233A7 (en) 1997-05-27
CZ157497A3 (en) 1997-11-12
CN1167450A (en) 1997-12-10
HUT77637A (en) 1998-06-29
SI9520141A (en) 1997-10-31

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