WO2001019497A1 - Verfahren zum behandeln von gasen aus einer sinteranlage - Google Patents
Verfahren zum behandeln von gasen aus einer sinteranlage Download PDFInfo
- Publication number
- WO2001019497A1 WO2001019497A1 PCT/EP2000/008950 EP0008950W WO0119497A1 WO 2001019497 A1 WO2001019497 A1 WO 2001019497A1 EP 0008950 W EP0008950 W EP 0008950W WO 0119497 A1 WO0119497 A1 WO 0119497A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- sintering
- sintering plant
- hot zone
- partial
- zone
- Prior art date
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
- B01D53/38—Removing components of undefined structure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
- B01D53/70—Organic halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
Definitions
- the present invention relates to a method for extracting and treating gases from a sintering plant.
- Sintering or agglomeration is the process of making fine ores into pieces for use in the blast furnace.
- a sinter mixture i.e. a fine ore mixture and a fuel
- a sintering belt i.e. a conveyor belt designed as a grate
- the sintered belt with the applied mixture also called the sintered bed, runs over a larger number of suction boxes. Air is drawn through the sintered bed through these suction boxes.
- An ignition furnace which is located above the first suction box, ignites the sinter mixture. The fire migrates from top to bottom through the sinter bed when the other suction boxes are passed over.
- the added fuel When burned, the added fuel generates a temperature which is just sufficient to soften the fine ore on its surface, so that the fine ore mixture bakes into a sinter cake.
- the combustion gases generated during sintering are extracted with the combustion air via the suction boxes.
- the sintering systems are usually equipped in such a way that the suction boxes are connected to a blower via an electrostatic filter (in some cases also a fabric filter), which generates the vacuum required under the sintering belt to draw the required combustion air through the sintering bed.
- the cleaned gas mixture is then discharged from the blower into the atmosphere via a chimney.
- a catalyst is used, which has already proven itself in waste incineration plants for the dioxin separation. In the waste incineration plants, this catalyst destroys the dioxin without leaving any residue. When operating such a catalyst in a sintering plant, however, it has been found that the dioxin destruction in the catalyst is often disturbed and sometimes does not take place at all. This is mainly due to the low gas temperatures (sometimes below 100 ° C).
- activated carbon or hearth furnace coke is injected into the exhaust gas stream together with calcium hydroxide behind the electrostatic precipitator. The activated carbon binds the dioxin, the calcium hydroxide is required to make the process inert.
- activated carbon / stove coke is blown directly into the electrostatic filter.
- the dioxin separation can be achieved to the desired extent and whether, due to the additional dust load, the electrostatic filter does not have even higher dust permeability.
- the object of the present invention is therefore to propose a method with which the exhaust gas problem of a sintering plant can be solved more effectively, simply and economically.
- the temperature in the sintering bed is relatively low from the ignition area to approximately the middle of the plant.
- the temperature in the sintered bed only increases significantly from the middle of the system.
- a more effective, simple and economical treatment of the exhaust gases of the sintering plant is achieved in that the extracted gases are no longer extracted and treated as a total flow as before, but the gases from the cold zone and the gases from the hot zone of the sintering plant are separated Partial flows are suctioned off and treated.
- dioxin measurements on existing sintering plants have shown that only very small amounts of dioxin are produced in the cold zone.
- the partial stream sucked separately from the cold zone therefore has only an extremely low dioxin load and does not need to be subjected to a treatment to reduce the dioxin content. Larger amounts of dioxin are only released in the exhaust gases from the hot zone and extracted with the partial stream from the hot zone. If this second partial flow is to be subjected to a treatment to reduce the dioxin content, it should be noted that by separating the partial flow from the cold zone, the temperature of the partial flow from the hot zone naturally increases above the mixing temperature of the total flow, which has a positive effect, for example Effectiveness of a dioxin separation in the catalyst affects. In conclusion, it should be noted that the exhaust gas problem of the sintering plant is generally simplified by the separate extraction of the gases from the cold and hot zone becomes. A more specific and thus more effective gas treatment can be carried out, with the lower gas quantities in the partial streams also achieving economic advantages.
- the partial flow from the cold zone of the sintering plant is advantageously only dedusted. Since only very small amounts of dioxin are present in the partial stream originating from the cold zone, it is e.g. it is not necessary to subject this partial flow to a treatment to reduce the dioxin content.
- the dedusting of the partial stream from the cold zone of the sintering plant is preferably carried out in one or more electrostatic filters. Because of a higher H 2 0 concentration in the cold zone, because of the lower one
- Dust separation in electrostatic filters can be significantly improved.
- the partial stream from the hot zone of the sintering plant is advantageously first dedusted and then subjected to a treatment to reduce the dioxin content.
- the dedusting of the partial stream from the hot zone of the sintering plant is preferably carried out in a fabric filter or cloth filter, which is particularly effective with fine dusts in relatively dry gas mixtures.
- the dioxin content is preferably reduced in a catalyst.
- a catalyst can be used which enables very good dioxin separation in waste incineration plants. Only the partial flow, from the hot zone of the sintering plant, in which substantial amounts of dioxin are released, is recorded and led to the catalyst. Since the partial flow treated in the catalyst has a sufficiently high temperature, the dioxin is destroyed without residue in the catalyst.
- the partial flow from the hot zone of the sintering plant can also be heated upstream of the catalytic converter.
- the additional heating can advantageously be carried out, for example, by burning the CO gas contained in this partial stream, preferably in a CO catalyst. This results in an even higher gas temperature, which further improves the dioxin separation in the catalyst.
- the partial flow from the hot zone of the sintering plant is preferably additionally subjected to a treatment in order to reduce the NO x content.
- This treatment for the purpose of reducing the NO x content advantageously comprises injecting NH 3 into the partial stream from the hot zone of the sintering plant. Indeed, at the temperatures of the partial flow from the hot zone, NO x reacts well with NH 3 .
- the partial stream from the hot zone preferably has a mixing temperature of more than 200 ° C. and the partial stream from the cold zone has a mixing temperature of less than 100 ° C. Indeed, at temperatures above 200 ° C, the catalyst should be able to destroy the dioxin without residue, and at temperatures below 100 ° C, the dioxin content in the exhaust gas from the sintering plant should be negligible.
- the dioxin content in the partial flow from the cold zone is preferably less than 0.5 ng / Nm 3 .
- Partial streams are preferably approximately the same size.
- FIG. 1 a schematic side view of a sintering plant
- FIG. 2 a schematic plan view of a sintering plant
- FIG. 3 a section AA through the sintering plant shown in FIG. 2
- FIG. 4 a graph of the volume flow of the exhaust gases of both zones
- FIG .5 a graph of the temperature of the exhaust gases of both zones
- Fig. 6 a graph of the dioxin content of the exhaust gases of both zones
- FIG. 1 shows a sintering plant 10 with a sintering belt 12, a bunker
- the sintering belt 12 transports the applied sintering mixture 20, also called the sintering bed, via the suction boxes W1-W22 to the discharge 18. Air is sucked through the sintering bed via these suction boxes W1-W22.
- the added fuel During combustion, the added fuel generates a temperature which is just sufficient to soften the fine ore on its surface, so that the sintered mixture bakes to form a sintered cake 22.
- the combustion gases generated during sintering are extracted with the combustion air via the suction boxes W1-W22.
- the suction boxes W1-W22 are divided into two separate groups.
- a first group comprises the suction boxes W1-W12, which are assigned to a so-called cold zone 36 of the sintering plant.
- a second group includes the suction boxes W13-W22, which are assigned to a so-called hot zone 38 of the sintering plant.
- FIGS. 4-6 each show the mean values of size (volume flow), temperature and dioxin content for the two partial flows for different subdivisions of the suction boxes W1-W22 between the two groups.
- the values for the partial flow from the first group are shown with dots and are entered under the ordinal number x of the last suction box of the first group.
- the values for the partial flow from the second group are shown with triangles and are entered under the ordinal number x of the suction box of the second group.
- Fig. 4 shows the size of the two partial flows in kNm 3 / h, i.e. under standard conditions. It can be seen that when the suction boxes W12 and W13 are separated, the two partial flows are approximately the same size. In other words, the partial flow from the cold zone and the partial flow from the hot zone have essentially the same size under standard conditions at the above-defined boundary between the cold and the hot zone.
- Fig. 5 shows the temperature of the two partial flows in ° C. It can be seen that if the suction boxes W12 and W13 are separated, the temperature of the partial flow from the cold zone is 73 ° C (see abscissa 12), while the temperature of the partial flow from the hot zone is 220 ° C (see abscissa 13), is significantly higher. If, as in the systems known to date, the exhaust gases are not separated into two partial streams, the temperature of the total stream is approximately 140 ° C. (see abscissa 1 or 22). If the suction boxes W12 and W13 are separated, the temperature of the partial flow from the hot zone is consequently higher by approximately 80 ° C.
- FIG. 6 shows the dioxin content of the two partial flows in ng based on a Nm 3 of gas. It can be seen that when the suction boxes W12 and W13 are separated, the dioxin content of the partial flow from the cold zone is 0.10 ng / Nm 3 (see abscissa 12), while the dioxin content of the partial flow from the hot zone is 3.74 ng / Nm 3 (see Abscissa 13), which is significantly higher. In other words, the dioxin content in the partial flow from the cold zone is negligible and does not pose any problems for the environment.
- the suction boxes W1-W12 are connected to a by means of a suction line 28
- Blower 24 connected, which draws the partial flow from the cold zone 36.
- an electrostatic filter 32 which dedusts the partial flow from the cold zone. The latter then reaches the atmosphere via a chimney 40.
- the partial flow from the cold zone 36 has a minimal dioxin content (0.10 ng / Nm 3 ), so that treatment to reduce the dioxin content is not necessary.
- the suction boxes W13-W22 are connected by means of a suction line 30 to a separate fan 26 which draws the partial flow out of the hot zone 38.
- a fabric filter 34 which dedusts the partial flow from the hot zone 38.
- the partial flow from the hot zone 38 has a relatively high dioxin content (3.74ng / Nm 3 ), this partial flow must be subjected to a treatment to reduce the dioxin content in a catalyst 42.
- the high temperature of the exhaust gases from the hot zone 38 (average temperature: 220 ° C.) enables a very good, residue-free dioxin separation in the catalyst 42.
- the partial flow from the hot zone 38 can now reach the atmosphere via the chimney 40.
- the dioxin separation in the catalyst 42 can be further improved by additional heating of the partial flow from the hot zone 38.
- the CO gas contained in the partial stream is burned in an upstream CO catalyst 44.
- Deposition can be made.
- Catalyst 42 NH 3 48 injected into the partial flow from the hot zone 38.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Filtering Of Dispersed Particles In Gases (AREA)
- Incineration Of Waste (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE50002769T DE50002769D1 (de) | 1999-09-13 | 2000-09-13 | Verfahren zum behandeln von gasen aus einer sinteranlage |
AU76550/00A AU7655000A (en) | 1999-09-13 | 2000-09-13 | Method of treating gases issued from a sintering plant |
EP00965993A EP1227874B1 (de) | 1999-09-13 | 2000-09-13 | Verfahren zum behandeln von gasen aus einer sinteranlage |
AT00965993T ATE244050T1 (de) | 1999-09-13 | 2000-09-13 | Verfahren zum behandeln von gasen aus einer sinteranlage |
CA002383840A CA2383840C (en) | 1999-09-13 | 2000-09-13 | Method of treating gases issued from a sintering plant |
US10/090,018 US6749822B2 (en) | 1999-09-13 | 2002-02-28 | Process for treatment of gases from a sintering plant |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
LU90439 | 1999-09-13 | ||
LU90439A LU90439B1 (de) | 1999-09-13 | 1999-09-13 | Verfahren zum Behandeln von Gasen aus einer Sinteranlage |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/090,018 Continuation US6749822B2 (en) | 1999-09-13 | 2002-02-28 | Process for treatment of gases from a sintering plant |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2001019497A1 true WO2001019497A1 (de) | 2001-03-22 |
Family
ID=19731834
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2000/008950 WO2001019497A1 (de) | 1999-09-13 | 2000-09-13 | Verfahren zum behandeln von gasen aus einer sinteranlage |
Country Status (10)
Country | Link |
---|---|
US (1) | US6749822B2 (de) |
EP (1) | EP1227874B1 (de) |
AT (1) | ATE244050T1 (de) |
AU (1) | AU7655000A (de) |
CA (1) | CA2383840C (de) |
DE (1) | DE50002769D1 (de) |
ES (1) | ES2204696T3 (de) |
LU (1) | LU90439B1 (de) |
TW (1) | TW480187B (de) |
WO (1) | WO2001019497A1 (de) |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6039130A (ja) * | 1983-08-12 | 1985-02-28 | Nippon Kokan Kk <Nkk> | 焼結排ガスの潜熱回収方法 |
EP0567964A2 (de) * | 1992-04-28 | 1993-11-03 | Mitsubishi Jukogyo Kabushiki Kaisha | Verfahren zur Entstickung von Abgasen |
BE1008097A6 (fr) * | 1994-02-28 | 1996-01-16 | Centre Rech Metallurgique | Procede de destruction des oxydes d'azote des fumees d'agglomeration des minerais de fer. |
DE4431939C1 (de) * | 1994-09-08 | 1996-01-18 | Steag Ag | Verfahren und Anordnung zur Wärmebehandlung von schüttfähigem Behandlungsgut |
EP0895049A1 (de) * | 1997-07-24 | 1999-02-03 | Siemens Aktiengesellschaft | Sinteranlage |
EP0908222A1 (de) * | 1997-09-16 | 1999-04-14 | Siemens Aktiengesellschaft | Verfahren zur Niedertemperaturminderung von Dioxinen in einem Abgas einer technischen Anlage |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5254519A (en) * | 1990-02-22 | 1993-10-19 | Engelhard Corporation | Catalyst composition containing platinum and rhodium components |
-
1999
- 1999-09-13 LU LU90439A patent/LU90439B1/de active
- 1999-12-03 TW TW088121153A patent/TW480187B/zh not_active IP Right Cessation
-
2000
- 2000-09-13 WO PCT/EP2000/008950 patent/WO2001019497A1/de active IP Right Grant
- 2000-09-13 DE DE50002769T patent/DE50002769D1/de not_active Expired - Lifetime
- 2000-09-13 CA CA002383840A patent/CA2383840C/en not_active Expired - Fee Related
- 2000-09-13 AT AT00965993T patent/ATE244050T1/de active
- 2000-09-13 EP EP00965993A patent/EP1227874B1/de not_active Expired - Lifetime
- 2000-09-13 ES ES00965993T patent/ES2204696T3/es not_active Expired - Lifetime
- 2000-09-13 AU AU76550/00A patent/AU7655000A/en not_active Abandoned
-
2002
- 2002-02-28 US US10/090,018 patent/US6749822B2/en not_active Expired - Fee Related
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6039130A (ja) * | 1983-08-12 | 1985-02-28 | Nippon Kokan Kk <Nkk> | 焼結排ガスの潜熱回収方法 |
EP0567964A2 (de) * | 1992-04-28 | 1993-11-03 | Mitsubishi Jukogyo Kabushiki Kaisha | Verfahren zur Entstickung von Abgasen |
BE1008097A6 (fr) * | 1994-02-28 | 1996-01-16 | Centre Rech Metallurgique | Procede de destruction des oxydes d'azote des fumees d'agglomeration des minerais de fer. |
DE4431939C1 (de) * | 1994-09-08 | 1996-01-18 | Steag Ag | Verfahren und Anordnung zur Wärmebehandlung von schüttfähigem Behandlungsgut |
EP0895049A1 (de) * | 1997-07-24 | 1999-02-03 | Siemens Aktiengesellschaft | Sinteranlage |
EP0908222A1 (de) * | 1997-09-16 | 1999-04-14 | Siemens Aktiengesellschaft | Verfahren zur Niedertemperaturminderung von Dioxinen in einem Abgas einer technischen Anlage |
Non-Patent Citations (1)
Title |
---|
PATENT ABSTRACTS OF JAPAN vol. 009, no. 166 (C - 290) 11 July 1985 (1985-07-11) * |
Also Published As
Publication number | Publication date |
---|---|
LU90439B1 (de) | 2001-03-14 |
TW480187B (en) | 2002-03-21 |
DE50002769D1 (de) | 2003-08-07 |
ATE244050T1 (de) | 2003-07-15 |
CA2383840C (en) | 2008-11-18 |
US20020119067A1 (en) | 2002-08-29 |
EP1227874B1 (de) | 2003-07-02 |
EP1227874A1 (de) | 2002-08-07 |
ES2204696T3 (es) | 2004-05-01 |
US6749822B2 (en) | 2004-06-15 |
CA2383840A1 (en) | 2001-03-22 |
AU7655000A (en) | 2001-04-17 |
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