JPS6312655B2 - - Google Patents
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- Publication number
- JPS6312655B2 JPS6312655B2 JP55105007A JP10500780A JPS6312655B2 JP S6312655 B2 JPS6312655 B2 JP S6312655B2 JP 55105007 A JP55105007 A JP 55105007A JP 10500780 A JP10500780 A JP 10500780A JP S6312655 B2 JPS6312655 B2 JP S6312655B2
- Authority
- JP
- Japan
- Prior art keywords
- coal
- desulfurization
- agent
- desulfurizing agent
- desulfurization agent
- 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
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- 239000003795 chemical substances by application Substances 0.000 claims description 63
- 239000003245 coal Substances 0.000 claims description 51
- 230000003009 desulfurizing effect Effects 0.000 claims description 27
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 239000000567 combustion gas Substances 0.000 claims description 10
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 10
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 10
- 230000001590 oxidative effect Effects 0.000 claims description 5
- 230000003213 activating effect Effects 0.000 claims description 3
- 238000010000 carbonizing Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 description 48
- 230000023556 desulfurization Effects 0.000 description 48
- 239000007789 gas Substances 0.000 description 27
- 238000001179 sorption measurement Methods 0.000 description 14
- 238000003763 carbonization Methods 0.000 description 13
- 238000002485 combustion reaction Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 230000004913 activation Effects 0.000 description 10
- 238000003795 desorption Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 5
- 238000010301 surface-oxidation reaction Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical class 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Description
【発明の詳細な説明】
本発明は燃焼排ガス中の硫黄酸化物を吸着除去
するための脱硫剤を製造する方法に係り、特に、
この脱硫剤を石炭より製造する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for producing a desulfurizing agent for adsorbing and removing sulfur oxides in combustion exhaust gas, and in particular,
The present invention relates to a method for producing this desulfurization agent from coal.
一般に化石燃料には硫黄化合物が含まれてお
り、これを燃焼させた場合、硫黄化合物は硫黄酸
化物として燃焼排ガスに同伴する。環境保全の立
場から、この燃焼排ガス中の硫黄酸化物は除去し
なければならず、これまで種々の脱硫法が用いら
れて来た。これらの脱硫法の中に乾式脱硫法があ
る。 Fossil fuels generally contain sulfur compounds, and when burned, the sulfur compounds are entrained in the combustion exhaust gas as sulfur oxides. From the standpoint of environmental conservation, sulfur oxides in this combustion exhaust gas must be removed, and various desulfurization methods have been used so far. Among these desulfurization methods, there is a dry desulfurization method.
乾式脱硫法は、硫黄酸化物を含む排ガスを吸着
塔に通すことにより、硫黄酸化物を脱硫剤に吸着
させ、脱硫剤は脱着塔で加熱脱着再生するもので
ある。この為、脱硫剤は脱着塔、脱着塔間で循環
使用する。この循環使用によつて脱硫剤は機械的
な損耗を伴なう。また、脱硫剤中に硫黄酸化物は
希硫酸の状態で吸着されるので、脱硫剤の加熱脱
着再生を行うと脱硫剤から放出される二酸化硫黄
量の約1/2の二酸化炭素が飛散する。この為、二
酸化炭素の炭素源として、脱硫剤中の炭素が損耗
する。 In the dry desulfurization method, exhaust gas containing sulfur oxides is passed through an adsorption tower so that the sulfur oxides are adsorbed by a desulfurization agent, and the desulfurization agent is regenerated by thermal desorption in the desorption tower. For this reason, the desulfurizing agent is used in circulation between the desorption towers. This cyclic use causes mechanical wear and tear on the desulfurizing agent. Furthermore, since sulfur oxides are adsorbed in the desulfurization agent in the form of dilute sulfuric acid, when the desulfurization agent is thermally desorbed and regenerated, carbon dioxide that is about half the amount of sulfur dioxide released from the desulfurization agent is scattered. For this reason, carbon in the desulfurization agent is used up as a carbon source for carbon dioxide.
上記の理由から、乾式脱硫法は、運転中の脱硫
剤の損耗を充分に考慮する必要があり、一般に脱
硫剤として広く用いられて来た活性炭では高価す
ぎるという問題がある。 For the above reasons, in the dry desulfurization method, it is necessary to fully consider the wear and tear of the desulfurization agent during operation, and activated carbon, which has been widely used as a desulfurization agent, is generally too expensive.
本発明者等は、高価な活性炭の代替脱硫剤とし
て燃料石炭あるいは通常の石炭から脱硫剤を製造
し、それを用いた乾式脱硫プロセスを特願昭54−
34617号、特願昭54−59161号、特願昭54−62633
号、特願昭54−97203号、特願昭54−97205号、特
願昭54−97206号、特願昭54−100289号等に記述
して来た。 The present inventors produced a desulfurization agent from fuel coal or ordinary coal as an alternative desulfurization agent to expensive activated carbon, and developed a dry desulfurization process using the desulfurization agent in a patent application filed in 1972.
34617, patent application No. 54-59161, patent application No. 54-62633
It has been described in Japanese Patent Application No. 54-97203, Japanese Patent Application No. 54-97205, Japanese Patent Application No. 1972-97206, Japanese Patent Application No. 100289-1983, etc.
本発明の目的は上記した乾式脱硫プロセスに好
適な脱硫剤の製造方法を提供するにある。 An object of the present invention is to provide a method for producing a desulfurizing agent suitable for the above-mentioned dry desulfurization process.
上記の目的に沿う為に、本発明の脱硫剤の製造
方法は、石炭を乾留・賦活して脱硫剤を作るもの
において、乾留前あるいは乾留後の石炭に燃焼排
ガスを接触させて石炭あるいは乾留炭の表面を酸
化することを特徴とする。 In order to meet the above objectives, the method for producing a desulfurizing agent of the present invention is a method for producing a desulfurizing agent by carbonizing and activating coal, in which combustion exhaust gas is brought into contact with coal before or after carbonization, and coal or carbonized coal is It is characterized by oxidizing the surface.
以下、本発明を実施に基づいて説明する。 Hereinafter, the present invention will be explained based on implementation.
先ず、乾式脱硫法を第１図によつて説明する。 First, the dry desulfurization method will be explained with reference to FIG.
石炭専焼ボイラ１００で石炭１が焼燃すると燃
焼ガス２が発生する。燃焼ガス２は吸着塔１０１
に送り、ここで脱硫剤に燃焼ガス２中の硫黄酸化
物が吸着する。硫黄酸化物が除去された排ガス４
は集塵器（図示せず）で脱塵後大気に開放され
る。一方、硫黄酸化物を吸着した脱硫剤６は脱着
塔１０３に送り、400〜500℃の高温で加熱脱着再
生する。再生した脱硫剤７は分級器１０５に送
り、吸着塔１０１の通風圧力損失の要因となる微
粒子をとり除き、微粒子８はボイラ１００へ戻し
て燃料とする。また、再生脱硫剤１１は吸着塔１
０１に戻す。このようにして、脱硫剤は吸着塔１
０１と脱着塔１０３を循環使用する。この循環使
用によつて脱硫剤は分級器１０５で分級した微粒
子量と、脱着塔１０３で脱着する際に飛散するカ
ーボン量に当価な量だけの脱硫剤１３を補充す
る。 When coal 1 is burnt in coal-fired boiler 100, combustion gas 2 is generated. The combustion gas 2 is sent to the adsorption tower 101
The sulfur oxides in the combustion gas 2 are adsorbed by the desulfurizing agent. Exhaust gas 4 from which sulfur oxides have been removed
is released to the atmosphere after being removed by a dust collector (not shown). On the other hand, the desulfurizing agent 6 that has adsorbed sulfur oxides is sent to a desorption tower 103, where it is thermally desorbed and regenerated at a high temperature of 400 to 500°C. The regenerated desulfurizing agent 7 is sent to a classifier 105 to remove fine particles that cause ventilation pressure loss in the adsorption tower 101, and the fine particles 8 are returned to the boiler 100 to be used as fuel. In addition, the regenerated desulfurization agent 11 is supplied to the adsorption tower 1
Return to 01. In this way, the desulfurization agent is added to the adsorption tower 1.
01 and the desorption tower 103 are used in circulation. Through this circulation, the desulfurizing agent 13 is replenished in an amount equivalent to the amount of fine particles classified by the classifier 105 and the amount of carbon scattered during desorption in the desorption tower 103.
この脱硫剤１３は、燃料石炭１の一部２２、ま
たは、別途用意した一般石炭２３によつて作られ
る。これらの石炭は単独であるいは混合して使用
される。これらの脱硫剤用原料石炭２４を前処理
装置２００に導き、石炭燃焼ガス２の一部２７と
直接接触させる。前処理装置２００に導入するガ
スは冷却器２０５によつて冷却し、350〜500℃好
ましくは450℃の温度とする。石炭２４は装置２
００内に約30分間滞留させる。また、直接接触を
行つた後の燃焼ガス２９はボイラ１００に戻す。
前処理後の石炭２５は乾留塔２０１に導入し、
600〜800℃の温度で乾留する。乾留炭２６は賦活
塔２０２に導き、酸化性ガスと接触させて脱硫剤
１３の製造を完了する。賦活の際発生したガス３
１はボイラ１００あるいはその他の燃料として用
いる。 This desulfurizing agent 13 is made from a portion 22 of the fuel coal 1 or a separately prepared general coal 23. These coals may be used alone or in combination. These desulfurizing agent raw coals 24 are led to a pretreatment device 200 and brought into direct contact with a portion 27 of the coal combustion gas 2. The gas introduced into the pretreatment device 200 is cooled by a cooler 205 to a temperature of 350 to 500°C, preferably 450°C. Coal 24 is device 2
00 for approximately 30 minutes. Further, the combustion gas 29 after direct contact is returned to the boiler 100.
The pretreated coal 25 is introduced into a carbonization tower 201,
Carbonization at a temperature of 600-800℃. The carbonized coal 26 is guided to the activation tower 202 and brought into contact with an oxidizing gas to complete the production of the desulfurizing agent 13. Gas generated during activation3
1 is used as a boiler 100 or other fuel.
一方、脱着塔１０３で脱着したガス９は、
CO2、SO2、H2Oが主成分であり、このガスは硫
黄回収工程１０４に導入し、SO2を元素状硫黄１
０に環元する。一部副生するH2SはSO2に酸化し
て、吸着塔１０１の入口ガスに同伴させる。 On the other hand, the gas 9 desorbed in the desorption tower 103 is
CO 2 , SO 2 , and H 2 O are the main components, and this gas is introduced into a sulfur recovery step 104 where SO 2 is converted into elemental sulfur 1
Ring element to 0. Some of the by-produced H 2 S is oxidized to SO 2 and entrained in the inlet gas of the adsorption tower 101 .
第２図は同じ乾式脱硫プロセスにおいて、燃焼
ガス２の一部２７と石炭との接触を乾留後に行う
ようにした例を示す。図において、脱硫剤用原料
石炭２４は先ず乾留炉２０１に導入して乾留炭３
１とし、その後、接触反応塔２０３で燃焼ガス２
７と接触させることになる。表面酸化処理後の石
炭３２は賦活炉２０２へ送られ脱硫剤となる。 FIG. 2 shows an example in which a portion 27 of the combustion gas 2 is brought into contact with coal after carbonization in the same dry desulfurization process. In the figure, raw coal 24 for desulfurization agent is first introduced into a carbonization furnace 201, and carbonization coal 3
1, and then in the catalytic reaction tower 203, the combustion gas 2
This will bring it into contact with 7. Coal 32 after surface oxidation treatment is sent to activation furnace 202 and becomes a desulfurization agent.
以上述べる２つの実施例によれば、石炭あるい
は乾留炭を燃焼ガスと直接接触させることにより
石炭あるいは乾留炭の表面に酸化物ができ、しか
る後の賦活反応が著しく容易になり、細孔の発達
を促進させる。 According to the two embodiments described above, by bringing coal or carbonized coal into direct contact with combustion gas, oxides are formed on the surface of the coal or carbonized coal, and the subsequent activation reaction is significantly facilitated, resulting in the development of pores. promote.
また、石炭に前処理として表面酸化を施すより
乾留炭に表面酸化を施し賦活を行う方が、より賦
活効果が得られることが確認されている。 Furthermore, it has been confirmed that a more effective activation effect can be obtained by subjecting carbonized coal to surface oxidation for activation rather than by subjecting coal to surface oxidation as a pretreatment.
以下に、脱硫剤製造方法の具体的な実施例を示
す。 Specific examples of the desulfurizing agent manufacturing method are shown below.
まず、エルメロ炭を５〜10mmφに破砕し、これ
を乾留した。乾留は昇温速度２〜３℃／mmで700
℃まで昇温し、しかる後１時間保持した。また雰
囲気ガスN2とした。 First, Ermelo coal was crushed into pieces of 5 to 10 mm in diameter and carbonized. Carbonization is 700 at a heating rate of 2 to 3℃/mm.
The temperature was raised to .degree. C. and then maintained for 1 hour. In addition, the atmosphere gas was N2 .
冷却後乾留炭を取り出し、H2O11％、O26％、
SO21000ppm、残りをN2とした模擬排ガスを400
℃に加熱し、この模擬排ガスと乾留炭を約45分間
接触させ、しかる後乾留炭をH2O10％残りN2の
酸化性ガスを用い900℃で２時間接触させ、脱硫
剤Atを製造した。一方、模擬排ガスと接触処理
させない乾留炭をH2O10％、残りN2の酸化性ガ
スを用い900℃で２時間接触させ、脱硫剤ANを製
造し、前記脱硫剤を比較した。乾留炭に対して得
られる脱硫剤収率は脱硫剤Atの場合75.4wt％で
あるのに対して、脱硫剤ANの場合には、85.2wt
％となり、明らかに脱硫剤Atの製造工程におい
て賦活反応性が向上していることが判明した。以
上の脱硫剤At、ANについてSO2吸着能を調べる
と、脱硫剤Atの場合14.6（SO2・ｇ／100ｇ脱硫
剤）で、脱硫剤ANの場合9.7（SO2・ｇ／100ｇ脱
硫剤）となる。ここでSO2吸着能はSO22％、
H2O10％、O26％、N282％の模擬排ガスを100℃
一定で、３時間接触させた状態でのSO2吸着量と
して示した。両脱硫剤の脱硫剤収率が異なるの
で、一概にSO2吸着能の優劣の比較は難かしい
が、脱硫剤ANの脱硫剤収率を75.4wt％に換算し、
その時のSO2吸着能を調べると12.8％となり、脱
硫剤Atの前処理の効果が明らかである。 After cooling, take out the carbonized coal and add 11% H 2 O, 6% O 2 ,
400% simulated exhaust gas with SO 2 1000ppm and the rest N 2
℃, the simulated exhaust gas and carbonized coal were brought into contact for about 45 minutes, and then the carbonized carbon was brought into contact with an oxidizing gas containing 10% H 2 O and the rest N 2 at 900°C for 2 hours to produce a desulfurizing agent A t . did. On the other hand, a desulfurizing agent A N was produced by contacting carbonized coal, which was not subjected to contact treatment, with a simulated exhaust gas at 900° C. for 2 hours using an oxidizing gas consisting of 10% H 2 O and the remainder N 2 , and compared the desulfurizing agents. The desulfurization agent yield obtained for carbonized coal is 75.4wt% for desulfurization agent A t , while it is 85.2wt% for desulfurization agent A N.
%, and it was found that the activation reactivity was clearly improved in the manufacturing process of the desulfurizing agent A t . When examining the SO 2 adsorption capacity of the above desulfurizing agents A t and AN , it is 14.6 (SO 2 g/100g desulfurizing agent) for desulfurizing agent A t and 9.7 (SO 2 g/100 g desulfurizing agent) for desulfurizing agent A N. 100g desulfurization agent). Here, SO 2 adsorption capacity is SO 2 2%,
Simulated exhaust gas of 10% H2O , 6% O2 , 82% N2 at 100℃
It is shown as the amount of SO 2 adsorbed under a constant state of contact for 3 hours. Since the desulfurization agent yields of both desulfurization agents are different, it is difficult to make a general comparison between the superiority and inferiority of SO 2 adsorption ability, but the desulfurization agent yield of desulfurization agent A N was converted to 75.4wt%,
When the SO 2 adsorption capacity at that time was examined, it was 12.8%, which clearly shows the effect of the pretreatment with the desulfurization agent At .
一方、第１図の実施例に示した乾留する以前の
石炭と燃焼排ガスを接触させる効果を調べた。 On the other hand, the effect of bringing the combustion exhaust gas into contact with the coal before carbonization shown in the example of FIG. 1 was investigated.
石炭は前記のエルメロ炭を５〜10mmφに破砕分
級し、それを前記したH2O11％、O26％、
SO21000ppm、他N2の石炭燃焼排ガスの模擬排
ガスと400℃で約45分接触させ、しかる後に前記
乾留条件で乾留炭を作り、しかる後、前記賦活条
件で脱硫剤At′を製造した。得られる脱硫剤収率
は脱硫剤ANとほぼ同じで、SO2吸着能も僅かに
向上することが認められるものの、乾留した後、
石炭燃焼排ガスと接触させる前処理する方法に比
較してその効果は少ない。しかし、粘結性炭ある
いは弱粘結性炭から脱硫剤を製造する場合に、前
記したように石炭燃焼排ガスと接触させること
で、乾留時の溶着による問題を軽減できる特徴が
ある。 Coal was obtained by crushing and classifying the Ermelo coal into pieces of 5 to 10 mmφ and adding 11% H 2 O, 6% O 2 ,
It was brought into contact with simulated coal combustion exhaust gas containing 1000 ppm SO 2 and N 2 at 400°C for about 45 minutes, then carbonized coal was produced under the above carbonization conditions, and then desulfurization agent At' was produced under the above activation conditions. The yield of the desulfurization agent obtained is almost the same as that of the desulfurization agent A N , and although it is recognized that the SO 2 adsorption capacity is slightly improved, after carbonization,
This method is less effective than a pretreatment method that involves contact with coal combustion exhaust gas. However, when producing a desulfurization agent from caking coal or weakly caking coal, problems caused by welding during carbonization can be reduced by bringing it into contact with coal combustion exhaust gas as described above.
かかる前処理法において、石炭燃焼排ガスの温
度は150℃〜500℃の温度領域が可能であるが、温
度が低いとその表面酸化速度が速く、前処理時間
が長くなること、高温になると表面酸化速度が早
くなり調整が難かしくなるので好ましくは前処理
の温度は350℃から400℃が最も好ましい。 In this pretreatment method, the temperature of the coal combustion exhaust gas can range from 150℃ to 500℃, but the lower the temperature, the faster the surface oxidation rate and the longer pretreatment time; the higher the temperature, the more the surface oxidation occurs. Preferably, the pretreatment temperature is most preferably 350°C to 400°C, since the speed becomes faster and adjustment becomes difficult.
一方、本発明の効果は、乾留あるいは賦活を行
うのに、石炭燃焼排ガスを導入し、適宜な滞留時
間、温度を調整することで発揮できることは明ら
かである。 On the other hand, it is clear that the effects of the present invention can be achieved by introducing coal combustion exhaust gas and adjusting the residence time and temperature appropriately for carbonization or activation.
また、石炭燃焼排ガスに若干の空気あるいは酸
素が添加されても本発明の効果は発揮できる。 Further, even if a small amount of air or oxygen is added to the coal combustion exhaust gas, the effects of the present invention can be exhibited.
本発明によれば、乾式排煙脱硫装置の脱硫剤を
製造するのに、石炭を破砕した石炭あるいは乾留
炭と石炭専焼ボイラの燃焼排ガスを350〜400℃の
温度で直接接触させることで、しかる後の賦活反
応を容易した脱硫剤製造プロセスであるから、石
炭専焼ボイラのオンサイトでの脱硫剤製造プロセ
スとして適し、安価な脱硫剤が製造でき、かつ吸
着能の高い脱硫剤が製造できる。 According to the present invention, a desulfurizing agent for a dry flue gas desulfurization device can be produced by directly bringing crushed coal or carbonized coal into direct contact with combustion exhaust gas from a coal-fired boiler at a temperature of 350 to 400°C. Since this is a desulfurization agent production process that facilitates the subsequent activation reaction, it is suitable as an on-site desulfurization agent production process for coal-fired boilers, and allows the production of inexpensive desulfurization agents as well as desulfurization agents with high adsorption capacity.
第１図は、本発明の実施例を適用した乾式脱硫
プロセスを示す図、第２図は他の実施例を適用し
た乾式脱硫プロセスを示す図である。
１３……脱硫剤、２４……脱硫剤用原料石炭、
２５，３１……乾硫炭、１００……石炭専焼ボイ
ラ、１０１……吸着塔、１０２……脱じん器、１
０３……吸着塔、１０４……硫黄回収工程、１０
５……分級器、１０６……活性炭あるいは脱硫剤
製造装置、２００……石炭前処理装置、２０１…
…乾留炉、２０２……賦活炉、２０３……接触反
応塔、２０５……冷却器あるいは加熱器。
FIG. 1 is a diagram showing a dry desulfurization process to which an embodiment of the present invention is applied, and FIG. 2 is a diagram showing a dry desulfurization process to which another embodiment is applied. 13...Desulfurization agent, 24...Coal material for desulfurization agent,
25, 31... Dry sulfur coal, 100... Coal-fired boiler, 101... Adsorption tower, 102... Dust remover, 1
03...Adsorption tower, 104...Sulfur recovery process, 10
5...Classifier, 106...Activated carbon or desulfurization agent manufacturing device, 200...Coal pretreatment device, 201...
... Carbonization furnace, 202 ... Activation furnace, 203 ... Contact reaction tower, 205 ... Cooler or heater.
Claims (1)
剤を石炭を乾留後に乾留炭を賦活して作るように
した脱硫剤の製造方法において、前記石炭の乾留
工程の前あるいは後に前記燃焼ガスの一部によつ
て原料石炭もしくは乾留炭を表面酸化させ、その
後に賦活を行うことを特徴とする脱硫剤の製造方
法。1. In a method for producing a desulfurizing agent that adsorbs and removes sulfur oxides from combustion gas, the desulfurizing agent is produced by activating carbonized coal after carbonizing coal, in which one of the combustion gases is removed before or after the carbonizing step of coal. A method for producing a desulfurizing agent, which is characterized by surface oxidizing raw material coal or carbonized coal, and then activating it.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10500780A JPS5730548A (en) | 1980-08-01 | 1980-08-01 | Preparation of desulfurizing agent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10500780A JPS5730548A (en) | 1980-08-01 | 1980-08-01 | Preparation of desulfurizing agent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5730548A JPS5730548A (en) | 1982-02-18 |
| JPS6312655B2 true JPS6312655B2 (en) | 1988-03-22 |
Family
ID=14396009
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10500780A Granted JPS5730548A (en) | 1980-08-01 | 1980-08-01 | Preparation of desulfurizing agent |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5730548A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2684156B2 (en) * | 1994-05-06 | 1997-12-03 | 呉羽テック株式会社 | Bonding method for hot carpet |
-
1980
- 1980-08-01 JP JP10500780A patent/JPS5730548A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5730548A (en) | 1982-02-18 |
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