JPS6392B2 - - Google Patents
Info
- Publication number
- JPS6392B2 JPS6392B2 JP53096315A JP9631578A JPS6392B2 JP S6392 B2 JPS6392 B2 JP S6392B2 JP 53096315 A JP53096315 A JP 53096315A JP 9631578 A JP9631578 A JP 9631578A JP S6392 B2 JPS6392 B2 JP S6392B2
- Authority
- JP
- Japan
- Prior art keywords
- magnesium
- hydration
- concentration
- particle size
- hydration reaction
- 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
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 24
- 238000006703 hydration reaction Methods 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 19
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 19
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 18
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 16
- 239000000395 magnesium oxide Substances 0.000 claims description 15
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 12
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 12
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 9
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 8
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- 238000006477 desulfuration reaction Methods 0.000 claims description 5
- 230000023556 desulfurization Effects 0.000 claims description 5
- 150000002681 magnesium compounds Chemical class 0.000 claims description 5
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 4
- 239000002245 particle Substances 0.000 description 14
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 13
- 239000000347 magnesium hydroxide Substances 0.000 description 13
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 13
- 230000036571 hydration Effects 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000010304 firing Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 229910019440 Mg(OH) Inorganic materials 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- -1 chlorine ions Chemical class 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000000887 hydrating effect Effects 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000011812 mixed powder Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Description
【発明の詳細な説明】
本発明は、混式排煙脱硫方法の改良、さらに詳
しくいえば、マグネシウム化合物含有吸収液を用
いて排ガス中の亜硫酸ガスを除去する混式排煙脱
硫方法において、焼成炉排ガス洗浄液で再生酸化
マグネシウムの水和を行うことにより水和反応速
度を高めるとともに、生成水酸化マグネシウムの
粒径を小さくし、湿式ミルを不要とした改良方法
に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention aims to improve a mixed flue gas desulfurization method, and more specifically, in a mixed flue gas desulfurization method that uses an absorption liquid containing a magnesium compound to remove sulfur dioxide gas from flue gas, This invention relates to an improved method that increases the hydration reaction rate by hydrating recycled magnesium oxide with a furnace exhaust gas cleaning solution, reduces the particle size of the produced magnesium hydroxide, and eliminates the need for a wet mill.
水酸化マグネシウム、酸化マグネシウム、亜硫
酸マグネシウムなどのマグネシウム化合物が亜硫
酸ガスと反応する性質を利用して、排ガス中の亜
硫酸ガスを除去する方法はよく知られている。こ
の排煙脱硫方法では、亜硫酸ガスをマグネシウム
化合物との反応により生じる亜硫酸マグネシウム
や硫酸マグネシウムを乾燥後焼成して亜硫酸ガス
を回収するとともに酸化マグネシウムを得、次い
でこの酸化マグネシウムに水を加えて水和し水酸
化マグネシウムに変え、これを吸収剤として循環
再使用する。ところで、この再生水酸化マグネシ
ウムの吸収効果を高めるには、水和反応を十分に
行い、またこの反応で生じる水酸化マグネシウム
の粒径を小さくする必要がある。このため、従来
法においては湿式ミルで水酸化マグネシウムを摩
砕し、かつ大型の水和槽を用いて長時間の水和反
応を行わせる必要があつた。 A method of removing sulfur dioxide gas from exhaust gas by utilizing the property that magnesium compounds such as magnesium hydroxide, magnesium oxide, and magnesium sulfite react with sulfur dioxide gas is well known. In this flue gas desulfurization method, magnesium sulfite or magnesium sulfate produced by the reaction of sulfur dioxide gas with a magnesium compound is dried and calcined to recover sulfur dioxide gas and obtain magnesium oxide, and then water is added to this magnesium oxide to hydrate it. It is then converted into magnesium hydroxide, which is recycled and reused as an absorbent. By the way, in order to enhance the absorption effect of this regenerated magnesium hydroxide, it is necessary to sufficiently perform the hydration reaction and to reduce the particle size of the magnesium hydroxide produced in this reaction. For this reason, in the conventional method, it was necessary to mill the magnesium hydroxide using a wet mill and to carry out the hydration reaction for a long time using a large hydration tank.
本発明者らは、このような従来法における欠点
を克服し、水和反応時間を短縮するとともに粒径
の小さい水酸化マグネシウムを形成させる方法に
ついて鋭意研究を重ねた結果、水和反応の際に、
塩化マグネシウム含有焼成炉ガス洗浄廃液で希釈
した焼成物を用い、かつその硫酸マグネシウム濃
度及び処理温度を所定の範囲内に制御することに
よりその目的を達成しうることを見出し、この知
見に基づいて本発明をなすに至つた。 The present inventors have conducted intensive research on a method to overcome the drawbacks of conventional methods, shorten the hydration reaction time, and form magnesium hydroxide with a small particle size. ,
We discovered that the purpose could be achieved by using a fired product diluted with a waste fluid from cleaning furnace gas containing magnesium chloride, and by controlling the magnesium sulfate concentration and processing temperature within a predetermined range.Based on this knowledge, we developed this book. He came up with an invention.
すなわち、本発明は、亜硫酸ガス含有排ガスを
マグネシウム化合物含有吸収液で処理して脱硫
し、吸収液中に蓄積する亜硫酸マグネシウムを回
収し焼成して酸化マグネシウムとし、次いでこの
酸化マグネシウムを水和反応に付したのち、吸収
液中に循環し再使用する混式排煙脱硫方法におい
て、前記水和反応を、塩化マグネシウム濃度1500
〜5000ppm、硫酸マグネシウム濃度16重量％以下
の焼成炉ガス洗浄廃液を用い、40〜80℃の温度範
囲で行うことを特徴とする方法を提供するもので
ある。 That is, the present invention treats sulfite gas-containing exhaust gas with an absorption liquid containing a magnesium compound to desulfurize it, recovers the magnesium sulfite accumulated in the absorption liquid and burns it to produce magnesium oxide, and then subjects this magnesium oxide to a hydration reaction. In the mixed flue gas desulfurization method in which the mixture is recycled into the absorbent and reused, the hydration reaction is carried out at a magnesium chloride concentration of 1500.
The present invention provides a method characterized in that it is carried out at a temperature range of 40 to 80° C. using waste liquid from firing furnace gas cleaning with a magnesium sulfate concentration of 16% by weight or less and a magnesium sulfate concentration of 16% by weight or less.
次に、本発明方法を添付図面に従つて説明す
る。図面は本発明方法の実施態様の１例を示すフ
ローシートであるが、吸収塔１においては、水酸
化マグネシウム、亜硫酸マグネシウム及び硫酸マ
グネシウムを含むスラリーと排ガス中の亜硫酸ガ
スとが接触し、次の反応により亜硫酸ガスが除去
される。 Next, the method of the present invention will be explained with reference to the accompanying drawings. The drawing is a flow sheet showing an example of an embodiment of the method of the present invention. In the absorption tower 1, a slurry containing magnesium hydroxide, magnesium sulfite, and magnesium sulfate comes into contact with sulfur dioxide gas in the exhaust gas, and the following occurs. The reaction removes sulfur dioxide gas.
Mg（OH）2＋SO25H2O →MgSO3・6H2O
MgSO3＋SO2＋H2O→Mg（HSO3）2
Mg（HSO3）2＋Mg（OH）2＋4H2O
→2MgSO4・6H2O
Mg（OH）2＋SO3＋6H2O →MgSO4・7H2O
MgSO31/2O2＋7H2O →MgSO4・7H2O
これらの反応生成物及び未反応吸収剤は遠心分
離機２で母液から分けられ乾燥炉３で乾燥された
のち焼成炉４へ送られ、ここで約1000℃の温度に
加熱焼成され、次式に従つて濃度10〜12％の亜硫
酸ガスを回収するとともに酸化マグネシウムを再
生する。Mg(OH) 2 +SO 2 5H 2 O →MgSO 3・6H 2 O MgSO 3 +SO 2 +H 2 O→Mg(HSO 3 ) 2 Mg(HSO 3 ) 2 +Mg(OH) 2 +4H 2 O
→2MgSO 4・6H 2 O Mg(OH) 2 +SO 3 +6H 2 O →MgSO 4・7H 2 O MgSO 3 1/2O 2 +7H 2 O →MgSO 4・7H 2 O These reaction products and unreacted absorbent is separated from the mother liquor in a centrifuge 2, dried in a drying furnace 3, and then sent to a firing furnace 4, where it is heated and fired at a temperature of about 1000°C to produce sulfur dioxide gas with a concentration of 10 to 12% according to the following formula. and recover magnesium oxide.
MgSO3→MgO＋SO2↑
MgSO41/2Ｃ →MgO＋SO2↑＋1/2CO2↑
この焼成炉４で生成したMgOと未反応の
MgSO4の混合物は水和槽５へ送られる。他方、
焼成炉４の排ガスはサイクロン６を経て洗浄塔７
に送られ、ここで洗浄水タンク８から供給される
洗浄水と接触されたのち排出される。この洗浄水
中には、工業用水、燃焼重油、使用薬品などに含
有されている塩素イオンが長期間の運転により循
環洗浄水中に蓄積して生成した塩化マグネシウム
が含まれているので、これを水和槽５へ送り、塩
化マグネシウム濃度1500〜500ppm、硫酸マグネ
シウム濃度16重量％の反応液として用い、40〜80
℃の温度で次式の水和反応を行わせる。 MgSO 3 →MgO＋SO 2 ↑ MgSO 4 1/2C →MgO＋SO 2 ↑＋1/2CO 2 ↑ MgO generated in this firing furnace 4 and unreacted
The MgSO 4 mixture is sent to hydration tank 5. On the other hand,
The exhaust gas from the firing furnace 4 passes through the cyclone 6 and is sent to the cleaning tower 7.
There, it comes into contact with the wash water supplied from the wash water tank 8, and then is discharged. This cleaning water contains magnesium chloride, which is produced when chlorine ions contained in industrial water, combusted heavy oil, and used chemicals accumulate in the circulating cleaning water due to long-term operation. It was sent to tank 5 and used as a reaction solution with a magnesium chloride concentration of 1500 to 500 ppm and a magnesium sulfate concentration of 16% by weight.
The following hydration reaction is carried out at a temperature of °C.
MgO＋H2O→Mg（OH）2
このようにして、従来法の1/2〜1/3の反応時間
で粒径50μ以下の細かい水酸化マグネシウムを得
ることができる。 MgO + H 2 O → Mg (OH) 2 In this way, fine magnesium hydroxide with a particle size of 50μ or less can be obtained in 1/2 to 1/3 the reaction time of the conventional method.
本発明方法において水和に用いる焼成炉ガス洗
浄水中の塩化マグネシウム濃度は、1500〜
5000ppmの範囲にあることが必要であり、この濃
度が1500ppm未満では水和反応が遅くなるし、
5000ppmよりも高いと装置の腐食が著しく、使用
に耐えなくなる。また、この中の硫酸マグネシウ
ムの濃度は16重量％以下に制御することが必要で
あり、これよりも濃度が高いと高粘度の複塩の生
成を完全に抑制することが困難になる。 The concentration of magnesium chloride in the firing furnace gas cleaning water used for hydration in the method of the present invention is 1500 to
It needs to be in the range of 5000ppm, and if this concentration is less than 1500ppm, the hydration reaction will be slow.
If the concentration is higher than 5000ppm, the equipment will be severely corroded and will no longer be usable. Furthermore, the concentration of magnesium sulfate in this must be controlled to 16% by weight or less; if the concentration is higher than this, it will be difficult to completely suppress the formation of a high viscosity double salt.
さらに水和反応の際の温度は、水酸化マグネシ
ウムが最も安定に維持される40〜80℃の範囲で行
うことが必要であり、この温度が40℃未満では水
和効率が低下するし、80℃よりも高いと種々の複
塩の副生を免れがたい。 Furthermore, the temperature during the hydration reaction needs to be carried out in the range of 40 to 80 °C, where magnesium hydroxide is maintained most stably; if this temperature is lower than 40 °C, the hydration efficiency will decrease, If the temperature is higher than ℃, it is difficult to avoid the by-product of various double salts.
本発明方法は、反応速度を著しく短縮すること
ができ、また水和用の水の供給を省くことができ
る上に、生成する水酸化マグネシウムの粒径を小
さくできるので湿式ミルが不要となるなどの利点
を有する。 The method of the present invention can significantly shorten the reaction rate, eliminate the need for water supply for hydration, and reduce the particle size of the produced magnesium hydroxide, eliminating the need for a wet mill. It has the following advantages.
次に実施例により本発明をさらに詳細に説明す
る。 Next, the present invention will be explained in more detail with reference to Examples.
各例中における水酸化マグネシウムの平均粒径
は、光学顕微鏡により測定した粒径を算術平均し
たものである。 The average particle size of magnesium hydroxide in each example is the arithmetic mean of the particle sizes measured using an optical microscope.
実施例 １
図面に示す装置を用い、焼成炉から酸化マグネ
シウム2850Kgと硫酸マグネシウム150Kgの混合物
（平均粒径500μ）を水和槽に送り、また洗浄塔か
ら塩化マグネシウム1800ppm及び硫酸マグネシウ
ム６重量％を含む洗浄廃液10000Kgを水和槽に送
り、かきまぜながら45℃で４時間反応させた。Example 1 Using the equipment shown in the drawing, a mixture of 2850 kg of magnesium oxide and 150 kg of magnesium sulfate (average particle size 500 μ) was sent from the firing furnace to a hydration tank, and a mixture containing 1800 ppm of magnesium chloride and 6% by weight of magnesium sulfate was sent from the washing tower to a mixture containing 1800 ppm of magnesium chloride and 6% by weight of magnesium sulfate. 10,000 kg of washing waste liquid was sent to a hydration tank and reacted at 45°C for 4 hours while stirring.
この結果、平均粒径40μの水酸化マグネシウム
を90％の水和率で得た。 As a result, magnesium hydroxide with an average particle size of 40μ was obtained with a hydration rate of 90%.
比較例
焼成炉から生成する酸化マグネシウム2850Kg、
硫酸マグネシウム150Kgの混合粉体（平均粒子径
500μ）と水10000Kgを第１水和槽内で45℃で１時
間かきまぜて平均粒径260μの固体を含むスラリ
ーを得た。この処理をさらに３時間継続したが、
固体の平均粒径は100μ以下にならなかつた。前
記の平均粒径260μの固体を含むスラリーに水
1500Kgを加えながら10分間湿式ミルにて粉砕して
平均粒径40μとした後、第２水和槽に入れ45℃で
12時間反応させた結果、水和率は85％であり、実
施例１よりも低かつた。Comparative example: 2850 kg of magnesium oxide produced from a kiln,
Mixed powder of 150Kg of magnesium sulfate (average particle size
500μ) and 10,000Kg of water were stirred at 45°C for 1 hour in the first hydration tank to obtain a slurry containing solids with an average particle size of 260μ. This process was continued for another 3 hours,
The average particle size of the solids did not fall below 100μ. Add water to the slurry containing solids with an average particle size of 260μ.
Grind in a wet mill for 10 minutes while adding 1500 kg to give an average particle size of 40μ, then place in the second hydration tank and heat at 45℃.
As a result of reacting for 12 hours, the hydration rate was 85%, which was lower than in Example 1.
図面は本発明方法の実施態様の１例を示すフロ
ーシートであり、図中符号、１は吸収塔、４は焼
成炉、５は水和槽、７は洗浄塔である。
The drawing is a flow sheet showing an example of an embodiment of the method of the present invention, and the reference numeral 1 in the drawing is an absorption tower, 4 is a calcining furnace, 5 is a hydration tank, and 7 is a washing tower.
Claims (1)
含有吸収液で処理して脱硫し、吸収液中に蓄積す
る亜硫酸マグネシウムを回収し焼成して酸化マグ
ネシウムとし、次いでこの酸化マグネシウムを水
和反応に付したのち、吸収液中に循環し再使用す
る混式排煙脱硫方法において、前記水和反応を、
塩化マグネシウム濃度1500〜5000ppm、硫酸マグ
ネシウム濃度16重量％以下の焼成炉ガス洗浄廃液
を用いて、40〜80℃の温度範囲で行うことを特徴
とする方法。1 The exhaust gas containing sulfur dioxide is treated with an absorption liquid containing a magnesium compound to desulfurize it, the magnesium sulfite accumulated in the absorption liquid is recovered and calcined to form magnesium oxide, and then this magnesium oxide is subjected to a hydration reaction, and then absorbed. In a mixed flue gas desulfurization method that circulates in the liquid and reuses the hydration reaction,
A method characterized in that it is carried out at a temperature range of 40 to 80°C using a waste liquid for cleaning furnace gas with a magnesium chloride concentration of 1500 to 5000 ppm and a magnesium sulfate concentration of 16% by weight or less.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9631578A JPS5488870A (en) | 1978-08-08 | 1978-08-08 | Wet exhaust gas desulfurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9631578A JPS5488870A (en) | 1978-08-08 | 1978-08-08 | Wet exhaust gas desulfurization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5488870A JPS5488870A (en) | 1979-07-14 |
| JPS6392B2 true JPS6392B2 (en) | 1988-01-05 |
Family
ID=14161586
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9631578A Granted JPS5488870A (en) | 1978-08-08 | 1978-08-08 | Wet exhaust gas desulfurization method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5488870A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3751340B2 (en) * | 1995-08-22 | 2006-03-01 | 東洋エンジニアリング株式会社 | Exhaust gas desulfurization method |
| CN112090267A (en) * | 2020-09-23 | 2020-12-18 | 北京沃尔福环保科技有限公司 | Flue gas desulfurization process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4881771A (en) * | 1972-02-04 | 1973-11-01 | ||
| JPS4929433A (en) * | 1971-06-24 | 1974-03-15 |
-
1978
- 1978-08-08 JP JP9631578A patent/JPS5488870A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4929433A (en) * | 1971-06-24 | 1974-03-15 | ||
| JPS4881771A (en) * | 1972-02-04 | 1973-11-01 |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5488870A (en) | 1979-07-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4246245A (en) | SO2 Removal | |
| RO103174B1 (en) | Cleansing method of exhaust gas hot steam from a boiler installation or a cement kiln | |
| US7179438B2 (en) | Methods and apparatus for recovering gypsum and magnesium hydroxide | |
| JP2002293537A (en) | Method for manufacturing calcium carbonate | |
| JP4747382B1 (en) | Flue gas purification treatment method | |
| JPH0310575B2 (en) | ||
| CN102284238A (en) | Bialkali-method flue-gas desulphurization process | |
| US9764963B2 (en) | Method for the production of free flowing synthetic calcium fluoride and use thereof | |
| JPS593207B2 (en) | Gasly Yukara Sankaiou O Jiyokyosuru Hohou | |
| JPH06226042A (en) | Method for removal of sulfur dioxide from heated gaseous stream containing sulfur dioxide and for production of alpha type calcined gypsum | |
| EA002798B1 (en) | Process for bayer liquors causticisation and apparatus therefor | |
| US5085764A (en) | Process for upgrading coal | |
| US3961021A (en) | Method for removing sulfur dioxide from combustion exhaust gas | |
| JPH11509586A (en) | Separation of impurities from lime and lime sludge, and two-stage causticization of green liquor containing impurities such as silicon | |
| JPS6392B2 (en) | ||
| JPS6245394A (en) | Simultaneous removal of arsenic and silicon | |
| RU2740015C1 (en) | Method of cleaning off-gases from chlorine and sulfur oxide to obtain binder | |
| RU2694937C1 (en) | Method for obtaining silicon, aluminum and iron oxides under complex non-waste processing from bottom ash materials | |
| RU2624570C1 (en) | Method of processing of sodium-fluorine-carbon-containing waste of electrolytic production of aluminium | |
| RU2198842C2 (en) | Method of magnesium oxide producing | |
| RU2746731C1 (en) | Method of production of biocide, zinc oxide and magnesium and calcium chloride crystal hydrates from production waste | |
| JP6579317B2 (en) | Desalination method of incineration ash | |
| JPS5848490B2 (en) | Sansei Gas Nyoruchi Yuwahouhou | |
| RU2027669C1 (en) | Method of processing of energy coal ash to alumina and gypsum | |
| RU2572988C1 (en) | Method of obtaining calcium fluoride from fluorine-containing solutions |