WO2000078435A1 - Method and apparatus for desulphurisation of exhaust gases - Google Patents

Method and apparatus for desulphurisation of exhaust gases Download PDF

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Publication number
WO2000078435A1
WO2000078435A1 PCT/EP2000/005880 EP0005880W WO0078435A1 WO 2000078435 A1 WO2000078435 A1 WO 2000078435A1 EP 0005880 W EP0005880 W EP 0005880W WO 0078435 A1 WO0078435 A1 WO 0078435A1
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WO
WIPO (PCT)
Prior art keywords
raw meal
extracted
exhaust gases
ground
calcined raw
Prior art date
Application number
PCT/EP2000/005880
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French (fr)
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WO2000078435B1 (en
Inventor
Kent Thomsen
Soren Hundebol
Original Assignee
F L Smidth & Co A/S
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Priority to AU55347/00A priority Critical patent/AU760533B2/en
Priority to CA002375001A priority patent/CA2375001A1/en
Priority to PL00352274A priority patent/PL352274A1/en
Priority to EP00940402A priority patent/EP1200176B1/en
Priority to AT00940402T priority patent/ATE238093T1/en
Application filed by F L Smidth & Co A/S filed Critical F L Smidth & Co A/S
Priority to DE60002339T priority patent/DE60002339T2/en
Priority to BR0011761-7A priority patent/BR0011761A/en
Priority to JP2001504490A priority patent/JP2003502143A/en
Priority to KR1020017016217A priority patent/KR20020019093A/en
Priority to MXPA01012573A priority patent/MXPA01012573A/en
Priority to DK00940402T priority patent/DK1200176T3/en
Publication of WO2000078435A1 publication Critical patent/WO2000078435A1/en
Publication of WO2000078435B1 publication Critical patent/WO2000078435B1/en

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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
    • 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
    • B01D53/83—Solid phase processes with moving reactants

Definitions

  • the present invention relates to a method and apparatus for desulphurisation of exhaust gases from a cement making plant by bonding gaseous sulphur dioxide to calcium-containing cement raw meal which is extracted from the calcination stage of the plant and subsequently brought into contact with the exhaust gases as a sulphur- absorbing reactant.
  • a method of this kind is known from US-A-4,634,583.
  • the disadvantage of this known method is its low rate of efficiency. This is due to the fact that the particle size of the calcined raw meal which is introduce into the exhaust gases is relatively large, causing its surface area to be reduced correspondingly. Therefore, this known method requires much more raw meal than is theoretically required, leading to an unnecessary waste of heat since the extracted raw meal is cooled from a temperature range between 850 and 950° to a temperature range of 220 - 250°C. It is the object of the present invention to provide a method and apparatus by means of which the mentioned disadvantage is reduced.
  • this object is achieved by a method of the kind mentioned in the introduction and being characterized in that the extracted raw meal is slaked and ground prior to being brought into contact with the exhaust gases.
  • An improvement of the thermal economy is thereby obtained by reducing the quantity of raw meal required for the desulphurisation process. This is ascribable to the fact that by subjecting the raw meal to slaking and grinding, the fineness of the raw meal will be improved, thereby enhancing the efficiency of the desulphurisation process. Tests conducted have indicated that a reduction of the particle size of the reactant will enhance the rate of efficiency of the desulphurisation process.
  • the extracted, calcined raw meal is subjected to minimum 80 per cent slaking, and preferably full-scale slaking.
  • the percentage of slaking is determined to be equal to (1 - free CaO after slaking/free CaO before slaking) x 100, where free CaO is reported on an ignition-loss free basis as is conventional.
  • the extracted, calcined raw meal is ground to an average particle size of less than 5 ⁇ m, preferably of less than 3 ⁇ m.
  • the invention also includes apparatus for desulphurisation of exhaust gases from a cement making plant, having means for slaking and for grinding the extracted raw meal prior to bringing it into contact with the exhaust gases.
  • SO 2 is formed by partial oxidation for example of FeS 2 , at around 550 °C. Furthermore, the highest efficiency of desulphurisation when using extracted raw meal is achieved at high temperatures. It is therefore preferred that the extracted, calcined raw meal is introduced into the exhaust gas stream at a location immediately after, viewed in the direction of flow of the exhaust gases, SO 2 has been formed by partial combustion of the sulphide constituents in the raw materials. In a traditional cement making plant comprising a preheater with five cyclone stages, the formation of SO 2 from sulphide- containing raw materials will typically take place in the inlet duct for the third cyclone stage and in that cyclone stage itself.
  • the extracted raw meal is introduced into the exhaust gases in the exhaust gas discharge duct from the third cyclone stage or at a subsequent location.
  • SO 2 measuring equipment will be used to establish exactly where SO 2 is formed, with the decision concerning the location of the point of introduction being made accordingly.
  • the extracted, calcined raw meal in a flash pipe is introduced into a stream of mixed air and water causing it to be slaked, that the slaked raw meal is separated in a separating mechanism, and is subsequently conveyed to and ground in a mill.
  • the airstream from the flash pipe is used to convey the slaked and ground, calcined raw meal from the mill to the point of introduction.
  • the overriding objective of the present invention is to remove the SO 2 originating from the raw materials because the SO 2 formed from the fuels in the hotter parts of the kiln system is effectively bonded to CaO and converted into CaSO 4 which is a solid which will be a constituent component of the finished clinker.
  • Figurel shows a traditional cement making plant where the method according to the invention is used.
  • FIG. 2 shows an especially preferred embodiment of the invention.
  • Figure 1 a cement making plant which comprises a cyclone preheater
  • the plant is run in accordance with traditional operating principles which involves raw material being introduced at an inlet 9 in the inlet duct to the first cyclone stage 1 a of the cyclone preheater and heated, calcined and burned into clinker by first being directed through the preheater 1 , the calciner 4 and subsequently through the kiln 3 in counterflow with hot exhaust gases which are formed at, respectively, a burner 11 in the rotary kiln 3 and burners 13 in the calciner 4. The burned clinker is subsequently cooled in the clinker cooler 5.
  • some of the hot, calcined raw meal is extracted from the fifth stage separating cyclone 1 e of the preheater 1 by means of a dosing mechanism 15 which is designed for extracting a controlled stream of material.
  • the stream of material thus extracted is directed to a slaking and grinding apparatus 17 of any suitable kind.
  • a slaking and grinding apparatus 17 of any suitable kind.
  • this could be a ball mill, a vertical mill, a ring roller mill or a roller press to which water (H 2 O) is added, possibly in vaporized form.
  • the apparatus 17, as shown in Fig. 2 comprises a riser pipe or flash pipe 17a with a subsequent separating cyclone 17b and a mill 17c.
  • the extracted, calcined raw meal is introduced into an ascending stream of mixed air and water, thereby causing the raw meal to be slaked.
  • the air is supplied by means of a fan 16 and the water is supplied via an opening 20.
  • the slaked, but still substantially dry, calcined raw meal is subsequently separated in the separating cyclone 17b from where it is conveyed, if convenient via an intermediate bin (not shown) to the mill 17c wherein it is ground to the desired particle size.
  • the now slaked and ground, calcined raw meal is conveyed, possibly via a scoop device, to an entrance opening 19 which is provided in the outlet duct 21 of the third cyclone stage 1c.
  • the raw meal is conveyed pneumatically via a duct 18 by means of the airstream from the flash pipe.
  • calcium oxide (CaO) and calcium hydroxide (Ca(OH) 2 ) will react with the SO 2 present in the exhaust gases and will be converted into calcium sulphite CaSO 3 and/or calcium sulphate CaSO 4 .
  • These solids may be a constituent part of the clinker in similarity with other constituent components of the raw materials.
  • the slaked and ground, calcined raw meal may either be conveyed direct to the entrance opening 19 or it may be conveyed to an intermediate bin, not shown, wherefrom it may subsequently be led by means of a dosing means to the entrance opening.
  • the actual introduction of the material may take place using a special lance which is capable of dispersing the slaked and ground, calcined raw meal across the entire cross-sectional area of the duct 21 in order to optimize the efficiency of the desulphurisation process.

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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)
  • Disintegrating Or Milling (AREA)
  • Sampling And Sample Adjustment (AREA)

Abstract

Described is a method and apparatus for desulphurisation of exhaust gases from a cement making plant by bonding gaseous sulphur dioxide to calcium-containing cement raw meal which is extracted from the calcination stage (4) of the plant and subsequently brought into contact with the exhaust gases as a sulphur-absorbing reactant. The specific method slaking and grinding the extracted raw meal prior to it being brought into contact with the exhaust gases. By this method and apparatus an improvement of the thermal economy, is obtained by reducing the quantity of raw meal required for the desulphurisation process. This is ascribable to the fact that by subjecting the raw meal to slaking and grinding, the fineness of the raw meal will be improved, thereby enhancing the efficiency of the desulphurisation process.

Description

METHOD AND APPARATUS FOR DESULPHURISATION OF EXHAUST GASES
The present invention relates to a method and apparatus for desulphurisation of exhaust gases from a cement making plant by bonding gaseous sulphur dioxide to calcium-containing cement raw meal which is extracted from the calcination stage of the plant and subsequently brought into contact with the exhaust gases as a sulphur- absorbing reactant.
A method of this kind is known from US-A-4,634,583. The disadvantage of this known method is its low rate of efficiency. This is due to the fact that the particle size of the calcined raw meal which is introduce into the exhaust gases is relatively large, causing its surface area to be reduced correspondingly. Therefore, this known method requires much more raw meal than is theoretically required, leading to an unnecessary waste of heat since the extracted raw meal is cooled from a temperature range between 850 and 950° to a temperature range of 220 - 250°C. It is the object of the present invention to provide a method and apparatus by means of which the mentioned disadvantage is reduced.
According to the invention this object is achieved by a method of the kind mentioned in the introduction and being characterized in that the extracted raw meal is slaked and ground prior to being brought into contact with the exhaust gases. An improvement of the thermal economy is thereby obtained by reducing the quantity of raw meal required for the desulphurisation process. This is ascribable to the fact that by subjecting the raw meal to slaking and grinding, the fineness of the raw meal will be improved, thereby enhancing the efficiency of the desulphurisation process. Tests conducted have indicated that a reduction of the particle size of the reactant will enhance the rate of efficiency of the desulphurisation process.
It is preferred that a substantial amount of the calcium oxide (CaO) contained in the extracted raw meal is converted into calcium hydroxide (Ca(OH)2), due to the greater capability of the latter to bond sulphur dioxide (SO2). According to the invention it is therefore preferred that the extracted, calcined raw meal is subjected to minimum 80 per cent slaking, and preferably full-scale slaking. The percentage of slaking is determined to be equal to (1 - free CaO after slaking/free CaO before slaking) x 100, where free CaO is reported on an ignition-loss free basis as is conventional.
Since a reduction in the particle size of the reactant will raise the efficiency of the desulphurisation process, it is further preferred that the extracted, calcined raw meal is ground to an average particle size of less than 5 μm, preferably of less than 3 μm. The invention also includes apparatus for desulphurisation of exhaust gases from a cement making plant, having means for slaking and for grinding the extracted raw meal prior to bringing it into contact with the exhaust gases.
It is particularly in cases where sulphides, such as pyrite (FeS2), are incorporated in the raw materials that the exhaust gases from the cement making plant contains SO2.
SO2is formed by partial oxidation for example of FeS2, at around 550 °C. Furthermore, the highest efficiency of desulphurisation when using extracted raw meal is achieved at high temperatures. It is therefore preferred that the extracted, calcined raw meal is introduced into the exhaust gas stream at a location immediately after, viewed in the direction of flow of the exhaust gases, SO2 has been formed by partial combustion of the sulphide constituents in the raw materials. In a traditional cement making plant comprising a preheater with five cyclone stages, the formation of SO2 from sulphide- containing raw materials will typically take place in the inlet duct for the third cyclone stage and in that cyclone stage itself. In such a plant it is preferred that the extracted raw meal is introduced into the exhaust gases in the exhaust gas discharge duct from the third cyclone stage or at a subsequent location. In actual practice, SO2 measuring equipment will be used to establish exactly where SO2 is formed, with the decision concerning the location of the point of introduction being made accordingly.
It is preferred that the extracted, calcined raw meal in a flash pipe is introduced into a stream of mixed air and water causing it to be slaked, that the slaked raw meal is separated in a separating mechanism, and is subsequently conveyed to and ground in a mill.
It is further preferred that the airstream from the flash pipe is used to convey the slaked and ground, calcined raw meal from the mill to the point of introduction. The overriding objective of the present invention is to remove the SO2originating from the raw materials because the SO2 formed from the fuels in the hotter parts of the kiln system is effectively bonded to CaO and converted into CaSO4 which is a solid which will be a constituent component of the finished clinker.
In the following the invention will be explained in further detail with reference to the accompanying diagrammatical drawings, in which:-
Figurel shows a traditional cement making plant where the method according to the invention is used; and
Figure. 2 shows an especially preferred embodiment of the invention.
In Figure 1 is seen a cement making plant which comprises a cyclone preheater
1 with five cyclones 1a to 1e, a calciner 4, a rotary kiln 3 and a clinker cooler 5. The plant is run in accordance with traditional operating principles which involves raw material being introduced at an inlet 9 in the inlet duct to the first cyclone stage 1 a of the cyclone preheater and heated, calcined and burned into clinker by first being directed through the preheater 1 , the calciner 4 and subsequently through the kiln 3 in counterflow with hot exhaust gases which are formed at, respectively, a burner 11 in the rotary kiln 3 and burners 13 in the calciner 4. The burned clinker is subsequently cooled in the clinker cooler 5.
In accordance with the method of the invention, some of the hot, calcined raw meal is extracted from the fifth stage separating cyclone 1 e of the preheater 1 by means of a dosing mechanism 15 which is designed for extracting a controlled stream of material. The stream of material thus extracted is directed to a slaking and grinding apparatus 17 of any suitable kind. For example, this could be a ball mill, a vertical mill, a ring roller mill or a roller press to which water (H2O) is added, possibly in vaporized form. In an especially preferred embodiment of the invention the apparatus 17, as shown in Fig. 2, comprises a riser pipe or flash pipe 17a with a subsequent separating cyclone 17b and a mill 17c. In this embodiment the extracted, calcined raw meal is introduced into an ascending stream of mixed air and water, thereby causing the raw meal to be slaked. The air is supplied by means of a fan 16 and the water is supplied via an opening 20. The slaked, but still substantially dry, calcined raw meal is subsequently separated in the separating cyclone 17b from where it is conveyed, if convenient via an intermediate bin (not shown) to the mill 17c wherein it is ground to the desired particle size.
From the apparatus 17 the now slaked and ground, calcined raw meal is conveyed, possibly via a scoop device, to an entrance opening 19 which is provided in the outlet duct 21 of the third cyclone stage 1c. In the embodiment shown in Fig. 2, the raw meal is conveyed pneumatically via a duct 18 by means of the airstream from the flash pipe.
After being introduced into the exhaust gases, calcium oxide (CaO) and calcium hydroxide (Ca(OH)2) will react with the SO2 present in the exhaust gases and will be converted into calcium sulphite CaSO3 and/or calcium sulphate CaSO4. These solids may be a constituent part of the clinker in similarity with other constituent components of the raw materials.
The slaked and ground, calcined raw meal may either be conveyed direct to the entrance opening 19 or it may be conveyed to an intermediate bin, not shown, wherefrom it may subsequently be led by means of a dosing means to the entrance opening. The actual introduction of the material may take place using a special lance which is capable of dispersing the slaked and ground, calcined raw meal across the entire cross-sectional area of the duct 21 in order to optimize the efficiency of the desulphurisation process.

Claims

1. A method for desulphurisation of exhaust gases from a cement making plant by bonding gaseous sulphur dioxide to calcium-containing cement raw meal which is extracted from the calcination stage (4) of the plant and subsequently brought into contact with the exhaust gases as a sulphur-absorbing reactant, characterized in that the extracted raw meal is slaked and ground (17) prior to being brought into contact with the exhaust gases.
2. A method according to claim 1 , characterized in that the extracted, calcined raw meal is subjected to a minimum of 80 per cent slaking.
3. A method according to claim 1 or claim 2, characterized in that the extracted, calcined raw meal is subjected to full-scale slaking.
4. A method according to any of claims 1 to 3, characterized in that the extracted, calcined raw meal is ground to an average particle size of less than 5 μm.
5. A method according to claim 4, characterized in that the extracted, calcined raw meal is ground to an average particle size of less than 3 μm.
6. A method according to any of claims 1 to 5, characterized in that the extracted, calcined raw meal is introduced into the exhaust gas stream at a location (19), viewed in the direction of flow of the exhaust gases, immediately after SO2 has been formed by partial combustion of the sulphide constituents in the raw materials.
7. A method according to any of claims 1 to 6, characterized in that the extracted, calcined raw meal is introduced into a stream of mixed air and water in a flash pipe (17a), causing it to be slaked, that the slaked raw meal is separated in a separating mechanism (17b), and is subsequently conveyed to and ground in a mill (17c).
8. A method according to claim 7, characterized in that the airstream from the flash pipe (17a) is used to convey the slaked and ground, calcined raw meal from the mill (17c) to the point of introduction (19) into the exhaust gases.
9. An apparatus for desulphurisation of exhaust gases from a cement making plant by a method of bonding gaseous sulphur dioxide to calcium-containing cement raw meal which is extracted from the calcination stage (4) of the plant and subsequently brought into contact with the exhaust gases as a sulphur-absorbing reactant, characterized by means (17) for slaking and for grinding the extracted raw meal prior to bringing it into contact with the exhaust gases.
10. Apparatus according to claim 9, characterized by means (18) for introducing the extracted, calcined raw meal into the exhaust gas stream at a location (19), viewed in the direction of flow of the exhaust gases, immediately after SO2 has been formed by partial combustion of the sulphide constituents in the raw materials.
11. Apparatus according to claim 9 or claim 10, characterized in that the means for slaking the extracted, calcined raw meal includes a flash pipe (17a).
12. Apparatus according to claim 1 1 , characterized in that the means for slaking the extracted, calcined raw meal includes a separating mechanism (17b).
13. Apparatus according to claim 1 1 or claim 12, characterized in that the means for grinding the extracted, calcined raw meal includes a grinding mill (17c).
14. Apparatus according to claim 13, characterized in that a duct (18) is used to provide an airstream from the flash pipe (17a) to convey the slaked and ground, calcined raw meal from the mill (17c) to the point of introduction (19) into the exhaust gases.
15. A cement making plant having apparatus according to any of claims 9 to 14.
16. A cement making plant according to claim 15, including a five-stage preheater, characterized in that the slaked and ground raw meal is introduced into the exhaust gases immediately prior to the third stage (1c) of the preheater (1 ).
PCT/EP2000/005880 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases WO2000078435A1 (en)

Priority Applications (11)

Application Number Priority Date Filing Date Title
DK00940402T DK1200176T3 (en) 1999-06-18 2000-06-16 Process and apparatus for desulfurizing flue gas
BR0011761-7A BR0011761A (en) 1999-06-18 2000-06-16 Discharge gas desulphurisation method and apparatus
PL00352274A PL352274A1 (en) 1999-06-18 2000-06-16 Method of and apparatus for desulphurization of exhaust gas
EP00940402A EP1200176B1 (en) 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases
AT00940402T ATE238093T1 (en) 1999-06-18 2000-06-16 METHOD AND DEVICE FOR DESULFURIZATION OF EXHAUST GASES
AU55347/00A AU760533B2 (en) 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases
DE60002339T DE60002339T2 (en) 1999-06-18 2000-06-16 METHOD AND DEVICE FOR DESULFURING EXHAUST GASES
CA002375001A CA2375001A1 (en) 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases
JP2001504490A JP2003502143A (en) 1999-06-18 2000-06-16 Exhaust gas desulfurization method and apparatus
KR1020017016217A KR20020019093A (en) 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases
MXPA01012573A MXPA01012573A (en) 1999-06-18 2000-06-16 Method and apparatus for desulphurisation of exhaust gases.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DKPA199900867 1999-06-18
DK199900867 1999-06-18

Publications (2)

Publication Number Publication Date
WO2000078435A1 true WO2000078435A1 (en) 2000-12-28
WO2000078435B1 WO2000078435B1 (en) 2001-02-08

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Country Status (17)

Country Link
EP (1) EP1200176B1 (en)
JP (1) JP2003502143A (en)
KR (1) KR20020019093A (en)
CN (1) CN1142815C (en)
AT (1) ATE238093T1 (en)
AU (1) AU760533B2 (en)
BR (1) BR0011761A (en)
CA (1) CA2375001A1 (en)
CZ (1) CZ20014584A3 (en)
DE (1) DE60002339T2 (en)
DK (1) DK1200176T3 (en)
ES (1) ES2198321T3 (en)
MX (1) MXPA01012573A (en)
PL (1) PL352274A1 (en)
PT (1) PT1200176E (en)
WO (1) WO2000078435A1 (en)
ZA (1) ZA200109636B (en)

Cited By (4)

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WO2002028512A1 (en) * 2000-10-05 2002-04-11 F.L. Smidth A/S Method for reducing the sox emission from a plant for manufacturing cement clinker and such plant
WO2005042429A1 (en) * 2003-10-29 2005-05-12 F.L. Smidth A/S Method and plant for preheating particulate or pulverulent material
WO2005100247A1 (en) * 2004-04-16 2005-10-27 Flsmidth A/S Method and apparatus for hydration of a particulate or pulverulent material containing cao, hydrated product, and use of the hydrated product
WO2008074048A1 (en) * 2006-12-21 2008-06-26 Knoch, Kern & Co. Kg Reduction of the content of offgases in the production of cement clinker

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CN104474894B (en) * 2014-11-20 2019-01-25 王在仕 A kind of cyclone cylinder dry fume catalytic desulfurization device and technique
JP6494469B2 (en) * 2015-08-07 2019-04-03 太平洋セメント株式会社 Operation method of cement baking equipment
CN105536506A (en) * 2016-01-27 2016-05-04 西安建筑科技大学 Online kiln exit gas self-desulfuration method and system
CN105771616A (en) * 2016-01-27 2016-07-20 西安建筑科技大学 Method and system for on-line removal of SO2 in kiln tail flue gas by using raw material powder
CN105771618A (en) * 2016-03-23 2016-07-20 天津水泥工业设计研究院有限公司 Waste gas desulfurization and sulfur fixation structure for cement industry
CN106731645A (en) * 2017-03-09 2017-05-31 徐州贝克福尔节能环保技术有限公司 The facility and method of a kind of preheater inside self-loopa desulfurization
CN108097028A (en) * 2017-12-26 2018-06-01 重庆市新嘉南建材有限责任公司 Spontaneous desulfurizer and method
CN108525505A (en) * 2018-06-25 2018-09-14 禹州市灵威水泥熟料有限公司 A kind of cement clean manufacturing efficient combination desulfurization technology
CN109499295A (en) * 2018-12-29 2019-03-22 米凯利科技（北京）有限公司 Dry method desulfuration system
JP7326448B2 (en) * 2019-08-01 2023-08-15 太平洋エンジニアリング株式会社 Method for producing desulfurizing agent and method for desulfurizing exhaust gas from cement kiln

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EP0228111A1 (en) * 1985-12-18 1987-07-08 Metallgesellschaft Ag Process for the removal of noxious matter from waste gases
DE3643143A1 (en) * 1986-11-05 1988-05-11 Krupp Polysius Ag Process for removing pollutants from exhaust gases
WO1993010884A1 (en) * 1991-11-25 1993-06-10 F.L. Smidth & Co. A/S Method for reducing the sulphur dioxide content in the flue gas from a clinker production plant and apparatus for carrying out the method
EP0845443A1 (en) * 1996-11-29 1998-06-03 E. Schwenk Baustoffwerke Kg Process for removing sulfur dioxide from the exhaust gases of a furnace installation

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US4634583A (en) * 1984-01-07 1987-01-06 Klockner-Humboldt-Deutz Ag Method for the desulfurization of flue gas of a firing system
EP0228111A1 (en) * 1985-12-18 1987-07-08 Metallgesellschaft Ag Process for the removal of noxious matter from waste gases
DE3643143A1 (en) * 1986-11-05 1988-05-11 Krupp Polysius Ag Process for removing pollutants from exhaust gases
WO1993010884A1 (en) * 1991-11-25 1993-06-10 F.L. Smidth & Co. A/S Method for reducing the sulphur dioxide content in the flue gas from a clinker production plant and apparatus for carrying out the method
EP0845443A1 (en) * 1996-11-29 1998-06-03 E. Schwenk Baustoffwerke Kg Process for removing sulfur dioxide from the exhaust gases of a furnace installation

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002028512A1 (en) * 2000-10-05 2002-04-11 F.L. Smidth A/S Method for reducing the sox emission from a plant for manufacturing cement clinker and such plant
US6902714B2 (en) 2000-10-05 2005-06-07 F. L. Smidth A/S Method for reducing the SO2 emission from a plant for manufacturing cement clinker and such plant
KR100779326B1 (en) 2000-10-05 2007-11-27 에프엘스미쓰 에이/에스 Method for reducing the sox emission from a plant for manufacturing cement clinker and such plant
WO2005042429A1 (en) * 2003-10-29 2005-05-12 F.L. Smidth A/S Method and plant for preheating particulate or pulverulent material
US7384475B2 (en) 2003-10-29 2008-06-10 F. L. Smidth A/S Method and plant for preheating particulate or pulverulent material
WO2005100247A1 (en) * 2004-04-16 2005-10-27 Flsmidth A/S Method and apparatus for hydration of a particulate or pulverulent material containing cao, hydrated product, and use of the hydrated product
US7595037B2 (en) 2004-04-16 2009-09-29 Flsmidth A/S Method and apparatus for hydration of a particulate or pulverulent material containing CaO, hydrated product, and use of hydrated product
CN1942400B (en) * 2004-04-16 2010-11-10 Fl史密斯公司 Method and apparatus for hydration of a particulate or pulverulent material containing cao, hydrated product, and use of the hydrated product
WO2008074048A1 (en) * 2006-12-21 2008-06-26 Knoch, Kern & Co. Kg Reduction of the content of offgases in the production of cement clinker

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CA2375001A1 (en) 2000-12-28
DK1200176T3 (en) 2003-06-02
PT1200176E (en) 2003-08-29
ZA200109636B (en) 2002-11-22
BR0011761A (en) 2002-03-05
DE60002339D1 (en) 2003-05-28
PL352274A1 (en) 2003-08-11
CZ20014584A3 (en) 2002-04-17
CN1142815C (en) 2004-03-24
AU760533B2 (en) 2003-05-15
JP2003502143A (en) 2003-01-21
ATE238093T1 (en) 2003-05-15
MXPA01012573A (en) 2004-06-22
ES2198321T3 (en) 2004-02-01
CN1356922A (en) 2002-07-03
WO2000078435B1 (en) 2001-02-08
AU5534700A (en) 2001-01-09
EP1200176A1 (en) 2002-05-02
DE60002339T2 (en) 2004-01-22
EP1200176B1 (en) 2003-04-23
KR20020019093A (en) 2002-03-09

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