JPS6152730B2 - - Google Patents
Info
- Publication number
- JPS6152730B2 JPS6152730B2 JP54031549A JP3154979A JPS6152730B2 JP S6152730 B2 JPS6152730 B2 JP S6152730B2 JP 54031549 A JP54031549 A JP 54031549A JP 3154979 A JP3154979 A JP 3154979A JP S6152730 B2 JPS6152730 B2 JP S6152730B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- denitrification
- catalyst
- oxidation
- sintering furnace
- Prior art date
- Legal status (The legal status 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 status listed.)
- Expired
Links
- 239000003054 catalyst Substances 0.000 claims description 39
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 30
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 29
- 238000007254 oxidation reaction Methods 0.000 claims description 29
- 230000003647 oxidation Effects 0.000 claims description 28
- 238000005245 sintering Methods 0.000 claims description 22
- 229910052742 iron Inorganic materials 0.000 claims description 19
- 238000000034 method Methods 0.000 claims description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 32
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 230000001590 oxidative effect Effects 0.000 description 4
- 230000004913 activation Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 230000010718 Oxidation Activity Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000010953 base metal Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Description
〔産業上の利用分野〕
本発明は、焼結炉排ガスの脱硝方法に係り、特
にアンモニア接触還元法の改良に関する。
〔従来技術とその問題点〕
製鉄所の焼結炉排ガスの脱硝触媒としては、安
価で且つ廃触媒がそのまま焼結炉原料として使用
できる利点があることから鉄鉱石が使用されてい
る。しかし、鉄鉱石はそのままでは脱硝触媒とし
ては低活性であり、そのため、これを活性化する
必要がある。活性化の方法としては、Cu，Cr，
Ｖ，Ti，Al等の金属酸化物を添加しり、酸処理
する方法が開示されている。しかし、これらの活
性化方法は、調整、焼成、廃液処理等の複雑な工
程を含み、そのためのコスト上昇は免れることが
できない。
また、脱硝後の排ガスを熱交換器により熱回収
して未処理の排ガスを昇温する方法、ならびに焼
結炉排ガス中に含まれる一酸化炭素を触媒を使用
して酸化燃焼し、この燃焼熱で排ガスを昇温する
方法が先に提案されている。しかし、一酸化炭素
酸化触媒としては、従来からPt，Pd等の貴金属
系、Co，Mn，Cu，Ni，Zn，Fe，Cr，Cd等の卑
金属酸化物が使用されているが、これらの触媒
は、性能を維持するためには触媒の交換、補充が
不可欠になり、高価な触媒ではランニングコスト
が高くなる欠点を持つ。
本発明は上記事情に鑑みなされたものでその目
的とするところは、焼結炉原料としての鉄鉱石を
まず一酸化炭素酸化反応器に充填して酸化触媒と
して使用すると同時に脱硝触媒としての活性化を
行ない、次いでそれを脱硝反応器に充填して脱硝
触媒として再度使用することにより、安価に効率
よく脱硝を行うことができる焼結炉排ガスの脱硝
方法を提供しようとするものである。
〔問題点を解決するための手段および作用〕
すなわち本発明は、焼結炉排ガス中にアンモニ
アガスを吹込む工程と、前記排ガスを脱硝触媒を
充填した脱硝反応器に導入する工程と、前記脱硝
された排ガスを酸化触媒を充填した一酸化炭素酸
化反応器に導入する工程と、前記一酸化炭素の酸
化により昇温した排ガスにより未脱硝処理の排ガ
スを加熱する工程を包含する焼結炉排ガス脱硝方
法において、焼結炉原料としての鉄鉱石を一酸化
炭素酸化反応器に充填して酸化触媒として使用す
ると同時に脱硝触媒としての活性化を行ない、前
記一酸化炭素の酸化に使用したのちに排出する鉄
鉱石の一部を前記脱硝反応器に充填して脱硝触媒
として再度使用するようにしたものである。
〔実施例〕
本発明の詳細ならびに実施例を添付図面によつ
て説明する。第１図は本発明の工程図の一例であ
る。すなわち、焼結炉１において発生した排ガス
２は、電気集塵機３により除塵される。脱硫装置
４で排ガス２は通常石灰水等のシヤワーにより洗
浄されるので排ガス温度が著しく低下する。
一方、鉄鉱石を脱硝触媒とした脱硝反応に必要
な適温350〜450℃であるので、この温度まで排ガ
ス２を昇温しなければならない。この昇温のため
に排ガス２は熱交換器５に導入される。熱交換器
５により低温の脱硫排ガス２を昇温させる高温ガ
スとして後記一酸化炭素酸化反応器９より排出さ
れたガスを利用し、これと熱交換を行うものであ
つて、40〜60℃の脱硫排ガス２は熱交換後300〜
350℃に昇温する。300〜350℃に昇温した排ガス
２はブロアー６で昇圧された後、アンモニアガス
が添加され脱硝反応器８に導入される。この脱硝
反応器８に導入される排ガス２の温度が前記350
〜450℃に達しない場合には助燃炉７にて加熱昇
温される。脱硝反応器８では次の(1)式、(2)式また
は(3)式により排ガス中の窒素酸化物（以下NOx
と称する）が還元されて無害のN2となる。
NO＋NH3＋１／4O2→N2＋３／2H2O …(1)
3NO＋４／3NH3→７／6N2＋2H2O …(2)
NO＋NO2＋2NH3→2N2＋3H2O …(3)
次いで、脱硝された排ガス２は、一酸化炭素
（CO）酸化反応器９に導入される。焼結炉原料と
しての鉄鉱石を酸化触媒としたCO酸化反応に必
要な適温は350〜450℃である。焼結炉排ガス中に
は、容量にて0.5〜3.0％のCOを含有するので、
これを酸化してCO2とすることにより排ガスの昇
温が可能となる。例えば容量比でCO1％含有する
排ガスを酸化燃焼させることにより約80℃の温度
上昇が可能である。CO酸化反応器９により昇温
され、かつCO2となつて無害化された排ガス２
は、熱交換器５に導入されて、その保有熱を放熱
し、脱硫装置４を出て温度低下した排ガス２の加
熱に有効に利用した後大気中に放出される。
前記触媒としての鉄鉱石は、そのままでも高い
CO酸化活性を有するが、脱硝活性が低い。とこ
ろが、本発明者らは、脱硫後の排ガスの如く５〜
20ppmのSOxを含むガスに300〜500℃の温度条件
でさらすと、鉄鉱石表面の酸化鉄の一部が硫酸塩
化されCO酸化活性が時間とともに低下するが、
それとともに脱硝活性が急激に上昇するという特
性を有していることを見出した。本発明では、こ
の特性を利用して、焼結炉原料としての鉄鉱石
を、まずCO酸化反応器９に充填して酸化触媒と
して使用すると同時に上記の如くSOxにより脱硝
触媒としての活性化を行なう。次いでそれを脱硝
反応器８に充填して脱硝触媒として再度使用し、
脱硝触媒としての鉄鉱石の脱硝活性が最高活性の
70〜90％に低下した次点で、これを廃棄し、廃棄
した廃棄触媒はそのまま製鉄原料として焼結炉１
に送る。
なお、CO酸化反応器９を脱硝反応器８の前段
に設けることも考えられるが、鉄鉱石を触媒とし
て用いる場合、両反応に必要な適温は350〜450℃
と等しいために、CO酸化反応器９を脱硝反応器
８の前段に設けると、脱硝反応器８に導入される
排ガスの温度が、適温の上限となるか適温を上ま
わることとなり好ましくない。
実施例
第１表の容量比組成を有する100Nm3／Ｈの排
ガス流２を370℃に温度調整した後、約18N／
Ｈのアンモニアガスを添加し、これを５〜10mm粒
度の鉄鉱石を充填した固定床型反応器に導入し、
NOxの除去率およびCO酸化率を測定した。この
時の排ガスの空間速度SVは2000H-1であつた。こ
の試験結果は第２図に示すとおりである。
[Industrial Field of Application] The present invention relates to a method for denitrating sintering furnace exhaust gas, and particularly to improvements in an ammonia catalytic reduction method. [Prior art and its problems] Iron ore is used as a denitrification catalyst for sintering furnace exhaust gas in steel plants because it is inexpensive and has the advantage that the spent catalyst can be used as a raw material for the sintering furnace. However, iron ore as it is has low activity as a denitrification catalyst, so it is necessary to activate it. Activation methods include Cu, Cr,
A method is disclosed in which metal oxides such as V, Ti, Al, etc. are added and acid treatment is performed. However, these activation methods involve complicated steps such as adjustment, calcination, and waste liquid treatment, which inevitably increases costs. In addition, we have developed a method for recovering heat from denitrified exhaust gas using a heat exchanger to raise the temperature of untreated exhaust gas, as well as a method for oxidizing and burning carbon monoxide contained in sintering furnace exhaust gas using a catalyst. A method of increasing the temperature of exhaust gas was previously proposed. However, as carbon monoxide oxidation catalysts, noble metals such as Pt and Pd, and base metal oxides such as Co, Mn, Cu, Ni, Zn, Fe, Cr, and Cd have been used, but these catalysts In order to maintain performance, catalyst replacement and replenishment are essential, and expensive catalysts have the disadvantage of high running costs. The present invention was developed in view of the above circumstances, and its purpose is to first fill iron ore as a raw material in a sintering furnace into a carbon monoxide oxidation reactor and use it as an oxidation catalyst, and at the same time activate it as a denitrification catalyst. The object of the present invention is to provide a method for denitrating sintering furnace exhaust gas, which can perform denitration at low cost and efficiently by filling the denitration reactor with the denitration reactor and using it again as a denitration catalyst. [Means and effects for solving the problem] That is, the present invention includes a step of injecting ammonia gas into the sintering furnace exhaust gas, a step of introducing the exhaust gas into a denitrification reactor filled with a denitrification catalyst, and a step of injecting the ammonia gas into the sintering furnace exhaust gas. A sintering furnace exhaust gas denitrification process that includes the steps of introducing the denitrified exhaust gas into a carbon monoxide oxidation reactor filled with an oxidation catalyst, and heating the undenitrated exhaust gas with the flue gas whose temperature has been raised by the oxidation of the carbon monoxide. In the method, iron ore as a raw material for a sintering furnace is charged into a carbon monoxide oxidation reactor and used as an oxidation catalyst, and simultaneously activated as a denitrification catalyst, used for oxidizing the carbon monoxide, and then discharged. A portion of the iron ore is charged into the denitrification reactor and used again as a denitrification catalyst. [Example] Details and examples of the present invention will be explained with reference to the accompanying drawings. FIG. 1 is an example of a process diagram of the present invention. That is, the exhaust gas 2 generated in the sintering furnace 1 is removed by the electrostatic precipitator 3. In the desulfurization device 4, the exhaust gas 2 is usually washed with a shower of lime water or the like, so that the temperature of the exhaust gas is significantly lowered. On the other hand, since the appropriate temperature is 350 to 450°C, which is necessary for the denitrification reaction using iron ore as a denitrification catalyst, the temperature of the exhaust gas 2 must be raised to this temperature. For this temperature increase, the exhaust gas 2 is introduced into the heat exchanger 5. The heat exchanger 5 uses the gas discharged from the carbon monoxide oxidation reactor 9 described later as a high-temperature gas to raise the temperature of the low-temperature desulfurization exhaust gas 2, and performs heat exchange with this gas. Desulfurization exhaust gas 2 has a temperature of 300~ after heat exchange
Raise the temperature to 350℃. The exhaust gas 2 heated to 300 to 350°C is pressurized by a blower 6, and then ammonia gas is added thereto and introduced into the denitrification reactor 8. The temperature of the exhaust gas 2 introduced into this denitrification reactor 8 is 350°C.
If the temperature does not reach ~450°C, the temperature is increased in the auxiliary combustion furnace 7. In the denitrification reactor 8, nitrogen oxides (hereinafter NOx
) is reduced to harmless N2 . NO+NH 3 +1/4O 2 →N 2 +3/2H 2 O…(1) 3NO+4/3NH 3 →7/6N 2 +2H 2 O…(2) NO+NO 2 +2NH 3 →2N 2 +3H 2 O…(3) Next, The denitrified exhaust gas 2 is introduced into a carbon monoxide (CO) oxidation reactor 9. The appropriate temperature required for the CO oxidation reaction using iron ore as a sintering furnace raw material as an oxidation catalyst is 350 to 450°C. Sintering furnace exhaust gas contains 0.5 to 3.0% CO by volume, so
By oxidizing this to CO2 , it is possible to raise the temperature of the exhaust gas. For example, by oxidizing and burning exhaust gas containing 1% CO by volume, it is possible to raise the temperature by approximately 80°C. Exhaust gas 2 heated by the CO oxidation reactor 9 and turned into CO 2 and rendered harmless
is introduced into the heat exchanger 5, radiates its retained heat, and is effectively used to heat the exhaust gas 2, which exits the desulfurization device 4 and whose temperature has decreased, and is then released into the atmosphere. Iron ore as the catalyst is expensive even as it is.
It has CO oxidation activity but low denitrification activity. However, the present inventors discovered that the exhaust gas after desulfurization
When exposed to gas containing 20ppm SOx at a temperature of 300 to 500℃, some of the iron oxide on the surface of iron ore becomes sulfated, and CO oxidation activity decreases over time.
At the same time, it was found that the denitrification activity rapidly increases. In the present invention, taking advantage of this characteristic, iron ore as a raw material for the sintering furnace is first charged into the CO oxidation reactor 9 and used as an oxidation catalyst, and at the same time is activated as a denitrification catalyst by SOx as described above. . Then, it is charged into the denitrification reactor 8 and used again as a denitrification catalyst.
The denitrification activity of iron ore as a denitrification catalyst is the highest
When the runner-up rate decreased to 70-90%, it was discarded, and the discarded waste catalyst was used as raw material for steelmaking in sintering furnace 1.
send to It is also possible to install the CO oxidation reactor 9 before the denitrification reactor 8, but when iron ore is used as a catalyst, the appropriate temperature required for both reactions is 350 to 450°C.
Therefore, if the CO oxidation reactor 9 is installed before the denitrification reactor 8, the temperature of the exhaust gas introduced into the denitrification reactor 8 will reach the upper limit of the optimum temperature or exceed the optimum temperature, which is not preferable. EXAMPLE After temperature-adjusting the exhaust gas stream 2 of 100 Nm 3 /H with the volumetric composition shown in Table 1 to 370°C, about 18 N/H
Add H ammonia gas and introduce it into a fixed bed reactor filled with iron ore with a particle size of 5 to 10 mm.
The NOx removal rate and CO oxidation rate were measured. The space velocity SV of the exhaust gas at this time was 2000H -1 . The test results are shown in Figure 2.
上記実施例で明らかなとおり、本発明は焼結炉
排ガス中にアンモニアガスを吹込む工程と、前記
排ガスを脱硝触媒を充填した脱硝反応器に導入す
る工程と、前記脱硝された排ガスを酸化触媒を充
填した一酸化炭素酸化反応器に導入する工程と、
前記一酸化炭素の酸化により昇温した排ガスによ
り未脱硝処理の排ガスを加熱する工程を包含する
焼結炉排ガスの脱硝方法において、焼結炉原料と
しての鉄鉱石をまず一酸化炭素酸化反応器に充填
して酸化触媒として使用すると同時に脱硝触媒と
しての活性化を行ない、次いでそれを脱硝反応器
に充填して脱硝触媒として再度使用するようにし
たので、酸化触媒と脱硝触媒を同一物を使用でき
ることおよび鉄鉱石触媒の特別な脱硝活性化が不
要となることで触媒コスト安価に保持できると共
に脱硝の高効率化を収めることができる。
As is clear from the above examples, the present invention includes a step of injecting ammonia gas into the sintering furnace exhaust gas, a step of introducing the exhaust gas into a denitrification reactor filled with a denitrification catalyst, and a step of introducing the denitrified exhaust gas into the oxidation catalyst. a step of introducing the carbon monoxide into a carbon monoxide oxidation reactor filled with
In the denitrification method for sintering furnace exhaust gas, which includes the step of heating undenitrated exhaust gas with the exhaust gas whose temperature has increased due to the oxidation of carbon monoxide, iron ore as a raw material for the sintering furnace is first introduced into a carbon monoxide oxidation reactor. The same catalyst can be used as the oxidation catalyst and the denitrification catalyst because it is charged and used as an oxidation catalyst and activated as a denitration catalyst at the same time, and then it is charged into the denitration reactor and used again as the denitration catalyst. In addition, since no special denitrification activation of the iron ore catalyst is required, the cost of the catalyst can be kept low and denitrification efficiency can be increased.
第１図は本発明による方法の実施例を示す工程
図、第２図は本発明の固定床型反応器による実施
例における運転経過時間による鉄鋼石触媒の
NOx脱硝率およびCO酸化率の変化を示す相関図
である。
１…焼結炉、２…排ガス、３…脱硫装置、５…
熱交換器、８…脱硝反応器、９…酸化反応器。
FIG. 1 is a process diagram showing an example of the method according to the present invention, and FIG. 2 is a flowchart showing the changes in the iron ore catalyst according to the elapsed operating time in the example using the fixed bed reactor of the present invention.
FIG. 3 is a correlation diagram showing changes in NOx denitrification rate and CO oxidation rate. 1... Sintering furnace, 2... Exhaust gas, 3... Desulfurization equipment, 5...
Heat exchanger, 8... Denitrification reactor, 9... Oxidation reactor.
Claims (1)
程と、前記排ガスを脱硝触媒を充填した脱硝反応
器に導入する工程と、前記脱硝された排ガスを酸
化触媒を充填した一酸化炭素酸化反応器に導入す
る工程と、前記一酸化炭素の酸化により昇温した
排ガスにより未脱硝処理の排ガスを加熱する工程
を包含する焼結炉排ガスの脱硝方法において、前
記一酸化炭素酸化反応器に充填する酸化触媒とし
て焼結炉原料としての鉄鉱石を使用するととも
に、前記一酸化炭素の酸化に使用したのちに排出
する鉄鉱石の一部を前記脱硝反応器に充填して脱
硝触媒として再度使用することを特徴とする焼結
炉排ガスの脱硝方法。1 A step of injecting ammonia gas into the sintering furnace exhaust gas, a step of introducing the exhaust gas into a denitrification reactor filled with a denitrification catalyst, and a step of introducing the denitrified exhaust gas into a carbon monoxide oxidation reactor filled with an oxidation catalyst. and a step of heating undenitrated exhaust gas with the exhaust gas heated by the oxidation of carbon monoxide. Iron ore is used as a sintering furnace raw material, and a part of the iron ore discharged after being used to oxidize the carbon monoxide is charged into the denitrification reactor and used again as a denitrification catalyst. A method for denitrating sintering furnace exhaust gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3154979A JPS55124531A (en) | 1979-03-16 | 1979-03-16 | Denitrification of waste gas from sintering furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3154979A JPS55124531A (en) | 1979-03-16 | 1979-03-16 | Denitrification of waste gas from sintering furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55124531A JPS55124531A (en) | 1980-09-25 |
| JPS6152730B2 true JPS6152730B2 (en) | 1986-11-14 |
Family
ID=12334261
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3154979A Granted JPS55124531A (en) | 1979-03-16 | 1979-03-16 | Denitrification of waste gas from sintering furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS55124531A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3423744A1 (en) * | 1984-06-28 | 1986-01-09 | Bergwerksverband Gmbh, 4300 Essen | Process for separating out SO2 and NOx |
| US5078973A (en) * | 1985-01-30 | 1992-01-07 | Babcoco-Hitachi Kabushiki Kaisha | Apparatus for treating flue gas |
| CN1004990B (en) * | 1985-01-30 | 1989-08-16 | 巴布考克日立株式会社 | Apparatus for treating flue gas |
-
1979
- 1979-03-16 JP JP3154979A patent/JPS55124531A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55124531A (en) | 1980-09-25 |
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