JPH03247509A - Production of gypsum from coke oven gas - Google Patents
Production of gypsum from coke oven gasInfo
- Publication number
- JPH03247509A JPH03247509A JP4369390A JP4369390A JPH03247509A JP H03247509 A JPH03247509 A JP H03247509A JP 4369390 A JP4369390 A JP 4369390A JP 4369390 A JP4369390 A JP 4369390A JP H03247509 A JPH03247509 A JP H03247509A
- Authority
- JP
- Japan
- Prior art keywords
- gypsum
- oxidation tower
- slurry
- value
- air blown
- 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.)
- Pending
Links
- 229910052602 gypsum Inorganic materials 0.000 title claims abstract description 56
- 239000010440 gypsum Substances 0.000 title claims abstract description 56
- 239000000571 coke Substances 0.000 title claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 title claims description 10
- 230000003647 oxidation Effects 0.000 claims abstract description 39
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 35
- 239000002002 slurry Substances 0.000 claims abstract description 32
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 14
- 239000001301 oxygen Substances 0.000 claims abstract description 14
- 238000002485 combustion reaction Methods 0.000 claims abstract description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000011593 sulfur Substances 0.000 claims abstract description 6
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 239000002699 waste material Substances 0.000 claims abstract description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 9
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 8
- LVGQIQHJMRUCRM-UHFFFAOYSA-L calcium bisulfite Chemical compound [Ca+2].OS([O-])=O.OS([O-])=O LVGQIQHJMRUCRM-UHFFFAOYSA-L 0.000 claims description 8
- 235000010260 calcium hydrogen sulphite Nutrition 0.000 claims description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 239000002245 particle Substances 0.000 abstract description 14
- 238000007664 blowing Methods 0.000 abstract description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 2
- 230000001105 regulatory effect Effects 0.000 abstract 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 abstract 1
- 235000011116 calcium hydroxide Nutrition 0.000 abstract 1
- 239000000920 calcium hydroxide Substances 0.000 abstract 1
- 235000010261 calcium sulphite Nutrition 0.000 abstract 1
- 230000001276 controlling effect Effects 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- -1 hydrogen calcium sulfite Chemical class 0.000 abstract 1
- 239000013078 crystal Substances 0.000 description 14
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
この発明は、コークス炉ガスから、商品価値の優れた石
膏を製造するための方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for producing gypsum with excellent commercial value from coke oven gas.
コークス炉において、石炭の乾留時に発生したコークス
炉ガスは、ガス中から、タール、軽油、アンモニア等を
副生品として回収した後、脱硫設備に送り込まれ、ガス
中に含有される硫化水素（Ｈａｓ）が除去される。Coke oven gas generated during carbonization of coal is sent to desulfurization equipment after recovering tar, light oil, ammonia, etc. as byproducts from the gas, and hydrogen sulfide (Has) contained in the gas is recovered. ) are removed.
この脱硫設備における脱硫処理によって生した、多量の
硫黄分を含む廃液は、燃焼炉に送られる。The waste liquid containing a large amount of sulfur produced by the desulfurization process in this desulfurization equipment is sent to a combustion furnace.
そして、燃焼炉において、廃液中に含有されている硫黄
分が燃焼される。このときに発生した燃焼排ガスは１石
膏製造設備に送られ、石膏製造設備において、燃焼排ガ
ス中の亜硫酸ガス（ＳＯＺ）と、亜硫酸ガスの濃度に見
合った量の水酸化カルシウム（Ｃａ （ＯＨ）２ ）と
の反応により石膏が製造される。Then, in the combustion furnace, the sulfur content contained in the waste liquid is burned. The combustion exhaust gas generated at this time is sent to the gypsum manufacturing facility 1, where the sulfur dioxide gas (SOZ) in the combustion exhaust gas and calcium hydroxide (Ca(OH)2) in an amount commensurate with the concentration of sulfur dioxide gas are extracted. ) to produce gypsum.
第４図は、石膏製造設備における石膏製造の概略工程図
である。第４図に示すように、燃焼炉からのＳＯ□を含
む燃焼排ガスを、吸収塔１において、燃焼排ガス中の亜
硫酸の濃度に見合った量の水酸化カルシウムを含有する
水酸化カルシウム液に吸収させて、亜硫酸水素カルシウ
ムスラリーとなす。FIG. 4 is a schematic process diagram of gypsum production in the gypsum production facility. As shown in Fig. 4, the combustion exhaust gas containing SO Then, make a calcium bisulfite slurry.
次いで、このようにして得られた亜硫酸水素カルシウム
スラリーを、タンク２を経て、酸化塔３に送り込む。Next, the calcium bisulfite slurry thus obtained is sent to the oxidation tower 3 via the tank 2.
このようにして、酸化塔３に送り込まれた亜硫酸水素カ
ルシウムスラリーは、塔内にその下部から吹き込まれる
空気により酸化されて、石膏スラリーとなる。このよう
にして生成した石膏スラリーは、シックナー４を経て石
膏分離機５に送られ、石膏分離機５において石膏６を分
離する。かくして、石膏６が製造される。In this way, the calcium hydrogen sulfite slurry sent to the oxidation tower 3 is oxidized by air blown into the tower from the lower part, and becomes gypsum slurry. The gypsum slurry thus generated is sent to a gypsum separator 5 via a thickener 4, where gypsum 6 is separated. In this way, plaster 6 is manufactured.
〔発明が解決しようとする課題〕
しかしながら、上述のようにしてコークス炉ガスから製
造された石膏の結晶の平均粒径は、１０〜２０μ膳であ
って小さい。このために、建材用、ボード用等の石膏と
して、商品価値が低い問題があった。[Problems to be Solved by the Invention] However, the average particle size of gypsum crystals produced from coke oven gas as described above is small, ranging from 10 to 20 μm. For this reason, there has been a problem that the commercial value of gypsum as a building material, board, etc. is low.
従って、この発明の目的は、コークス炉ガスから、結晶
の平均粒径が大きい、商品価値の優れた石膏を製造する
ための方法を提供することにある。Therefore, an object of the present invention is to provide a method for producing gypsum having a large average crystal grain size and excellent commercial value from coke oven gas.
本発明者等は、上述した問題を解決し、コークス炉ガス
から製造される結晶の平均粒径を大きくなし、その商品
価値を高めるための手段を開発すべく鋭意研究を重ねた
。その結果、酸化塔内において、亜硫酸水素カルシウム
スラリーに吹き込まれた空気中の酸素の溶解速度、即ち
、石膏（ＣａＳＯ４・２Ｈ２０）の析出速度を遅くなし
、過飽和度を小さくするように、酸化塔からの排ガス中
の酸素濃度および石膏スラリーのｐｌ（値に基いて、酸
化塔への空気の吹き込み量を制御すれば、石膏結晶の平
均粒径を大きくし得ることを知見した。The present inventors have conducted extensive research in order to solve the above-mentioned problems, increase the average particle size of crystals produced from coke oven gas, and develop means for increasing their commercial value. As a result, in the oxidation tower, the dissolution rate of oxygen in the air blown into the calcium bisulfite slurry, that is, the precipitation rate of gypsum (CaSO4.2H20), is slowed down, and the degree of supersaturation is reduced. It has been found that the average particle size of gypsum crystals can be increased by controlling the amount of air blown into the oxidation tower based on the oxygen concentration in the exhaust gas and the PL value of the gypsum slurry.
この発明は、上記知見に基づくものであって、コークス
炉ガスに脱硫処理を施し、脱硫処理によって生じた廃液
中の硫黄分を燃焼させ１次いで、燃焼によって生じた、
亜硫酸ガスを含む燃焼排ガスを、水酸化カルシウム液に
吸収させて亜硫酸水素カルシウムスラリーとなし、次い
で、前記亜硫酸水素カルシウムスラリーを酸化塔に導き
、前記酸化塔の下部から吹き込まれる空気と反応させて
石膏スラリーとなし、前記石膏スラリーを分離すること
により石膏を得る２石膏の製造方法において、
前記酸化塔への前記空気の吹き込み量を、前記酸化塔か
らの排ガス中の酸素濃度が最低値となり、且つ、前記石
膏スラリーのｐｌ（が急上昇する直前の値になるように
制御することに特徴を有するものである。This invention is based on the above knowledge, and involves desulfurizing coke oven gas, burning the sulfur content in the waste liquid produced by the desulfurization process, and then burning the sulfur content produced by the combustion.
The combustion exhaust gas containing sulfur dioxide gas is absorbed into a calcium hydroxide solution to form a calcium hydrogen sulfite slurry, and then the calcium hydrogen sulfite slurry is led to an oxidation tower and reacted with air blown from the lower part of the oxidation tower to form gypsum. 2. A method for producing gypsum in which gypsum is obtained by separating the gypsum slurry into a slurry, and the amount of air blown into the oxidation tower is adjusted such that the oxygen concentration in the exhaust gas from the oxidation tower is at its lowest value, and , the gypsum slurry is characterized in that it is controlled so that the pl() of the gypsum slurry becomes a value just before the value rises rapidly.
第１図は、第４図に示す酸化塔３への空気の吹き込み量
と、酸化塔３から排出される排ガス中の酸素濃度との関
係を示すグラフである。第１図から明らかなように、酸
化塔３から排出される排ガス中の酸素濃度は、酸化塔３
への空気の吹き込み量によって変動し、吹き込み量が２
，０ＯＯＮｒｎ’／Ｈ前後のときに約１０％の最低にな
る。FIG. 1 is a graph showing the relationship between the amount of air blown into the oxidation tower 3 shown in FIG. 4 and the oxygen concentration in the exhaust gas discharged from the oxidation tower 3. As is clear from FIG. 1, the oxygen concentration in the exhaust gas discharged from the oxidation tower 3 is
It varies depending on the amount of air blown into the
,0OONrn'/H, the lowest value is about 10%.
第２図は、酸化塔３への空気の吹き込み量と、酸化塔３
によって生成し排出された石膏スラリーのｐｌ（との関
係を示すグラフである。第２図から明らかなように、石
膏スラリーのｐＨは、酸化塔３への空気の吹き込み量に
よって変動し、吹き込み量が２．００ＯＮｒｎ’／）１
前後のときにｐＨは２．０となり、吹き込み量を前記値
以下にすると、ｐＨは急上昇する。Figure 2 shows the amount of air blown into the oxidation tower 3 and the amount of air blown into the oxidation tower 3.
This is a graph showing the relationship between the PL of the gypsum slurry generated and discharged by is 2.00ONrn'/)1
The pH becomes 2.0 between the two times, and when the amount of blowing is reduced to below the above value, the pH rises rapidly.
第３図は、酸化塔３への空気の吹き込み量と、石膏結晶
の平均粒径との関係を示すグラフである。FIG. 3 is a graph showing the relationship between the amount of air blown into the oxidation tower 3 and the average particle size of gypsum crystals.
上述した、酸化塔への空気の吹き込み量と、酸化塔から
排出される排ガス中の酸素濃度および石膏スラリーのｐ
Ｈ値との関係から、前記排ガス中の酸素濃度が最低値と
なり、且つ、石膏スラリーのｐＨが急上昇する直前の値
になるように、酸化塔への空気の吹き込み量を２，００
ＯＮｒｎ’／Ｈ前後に制御すると、第３図から明らかな
ように、石膏結晶の平均粒径は、約３５μｍになる。As mentioned above, the amount of air blown into the oxidation tower, the oxygen concentration in the exhaust gas discharged from the oxidation tower, and the p of the gypsum slurry
From the relationship with the H value, the amount of air blown into the oxidation tower was adjusted to 2,000 ml so that the oxygen concentration in the exhaust gas becomes the lowest value and the pH of the gypsum slurry reaches the value just before it suddenly rises.
When ONrn'/H is controlled to be around, the average particle size of the gypsum crystals becomes about 35 μm, as is clear from FIG.
上記第１〜第３図から、石膏結晶の粒径を、３５〜４０
μ園に高めるために必要な条件は、次の通りである。From the above figures 1 to 3, the particle size of the gypsum crystals is 35 to 40.
The conditions necessary to raise the level to μ-en are as follows.
酸化塔からの排ガス中の酸素濃度＝１０〜１２％、石膏
スラリーのｐＨ： １．８〜２．３、酸化塔への空気の
吹き込み量： １，８００〜２，５０ＯＮｍ１″／Ｈ即
ち、酸化塔への空気の吹き込み量が１ 、８０ＯＮ ｒ
ｎ’／Ｈ未満では、排ガス中の酸素濃度が１２％を超え
て高くなり、未反応のＣａ （ｏｓｏ、 ）ｚが出現し
、且つ、石膏スラリーのｐＨが２．３を超えて高くなる
結果、石膏結晶の平均粒径が約１５μ−以下に低下する
。Oxygen concentration in exhaust gas from the oxidation tower = 10-12%, pH of gypsum slurry: 1.8-2.3, amount of air blown into the oxidation tower: 1,800-2,50 ONm1''/H, that is, oxidation The amount of air blown into the tower is 1,80ON r
If it is less than n'/H, the oxygen concentration in the exhaust gas becomes higher than 12%, unreacted Ca(oso, )z appears, and the pH of the gypsum slurry becomes higher than 2.3. , the average particle size of the gypsum crystals is reduced to about 15 microns or less.
一方、酸化塔への空気の吹き込み量が２，５０ＯＮｍｉ
’／）ｌを超えると、同じく排ガス中の酸素濃度が１２
％を超えて高くなり、且つ１石膏スラリーのｐＨが１．
８未満に低くなる結果、石膏結晶の平均粒径が約２０μ
ｍ以下に低下する。On the other hand, the amount of air blown into the oxidation tower was 2,50ONmi.
'/) If the oxygen concentration in the exhaust gas exceeds 12
%, and the pH of 1 gypsum slurry is 1.
As a result, the average particle size of gypsum crystals is approximately 20μ.
m or less.
従って、酸化塔への空気の好ましい吹き込み量は、ｌ、
８００〜２，５０ＯＮｍ／Ｈの範囲内である。Therefore, the preferable amount of air blown into the oxidation tower is l,
It is within the range of 800 to 2,50 ONm/H.
次に、この発明の方法を実施例により説明する。Next, the method of the present invention will be explained using examples.
第４図に示す工程に従って、亜硫酸水素カルシウムスラ
リーを酸化塔に導き、この発明の方法により、第１表に
示す条件で酸化を行ない、石膏スラリーとなした。同表
に、石膏スラリーを分離して得た製品石膏の結晶の平均
粒径を示す。また、同表に、従来の酸化条件およびこれ
により得られた製品石膏の結晶の平均粒径を、併せて示
す。According to the steps shown in FIG. 4, the calcium bisulfite slurry was led to an oxidation tower, and oxidized according to the method of the present invention under the conditions shown in Table 1 to obtain a gypsum slurry. The same table shows the average particle size of crystals of product gypsum obtained by separating the gypsum slurry. The same table also shows the conventional oxidation conditions and the average particle size of the crystals of the product gypsum obtained thereby.
上記第１表から明らかなように、この発明の方法によれ
ば、従来に比べて、平均粒径が１．７〜２倍の結晶を有
する品質の優れた商品価値の高い石膏を製造することが
できた。As is clear from Table 1 above, according to the method of the present invention, it is possible to produce gypsum of excellent quality and high commercial value, which has crystals with an average particle size of 1.7 to 2 times that of the conventional method. was completed.
以上述べたように、この発明によれば、コークス炉ガス
から、結晶の平均粒径が大きい１品質の優れた商品価値
の高い石膏を製造することができる、工業上有用な効果
がもたらされる。As described above, according to the present invention, it is possible to produce gypsum of excellent quality and high commercial value, which has a large average grain size of crystals, from coke oven gas, which is an industrially useful effect.
第１図は酸化塔への空気の吹き込み量と酸化塔からの排
ガス中の酸素濃度との関係を示すグラフ、第２図は酸化
塔への空気の吹き込み量と石膏スラリーのｐＨとの関係
を示すグラフ、第３図は酸化塔への空気の吹き込み量と
石膏結晶の平均粒径との関係を示すグラフ、第４図は石
膏製造の概略工程図である。図面において、
１・・・吸収塔、 ２・・・タンク、−３・・・
酸化塔、 ４・・・シックナー５・・・石膏分離
機、
６
石膏。Figure 1 is a graph showing the relationship between the amount of air blown into the oxidation tower and the oxygen concentration in the exhaust gas from the oxidation tower, and Figure 2 shows the relationship between the amount of air blown into the oxidation tower and the pH of the gypsum slurry. FIG. 3 is a graph showing the relationship between the amount of air blown into the oxidation tower and the average particle size of gypsum crystals, and FIG. 4 is a schematic process diagram of gypsum production. In the drawings, 1...absorption tower, 2...tank, -3...
Oxidation tower, 4...thickener 5...gypsum separator, 6 gypsum.
Claims (1)
て生じた廃液中の硫黄分を燃焼させ、次いで、燃焼によ
って生じた、亜硫酸ガスを含む燃焼排ガスを、水酸化カ
ルシウム液に吸収させて亜硫酸水素カルシウムスラリー
となし、次いで、前記亜硫酸水素カルシウムスラリーを
酸化塔に導き、前記酸化塔の下部から吹き込まれる空気
と反応させて石膏スラリーとなし、前記石膏スラリーを
分離することにより石膏を得る、石膏の製造方法におい
て、 前記酸化塔への前記空気の吹き込み量を、前記酸化塔か
らの排ガス中の酸素濃度が最低値となり、且つ、前記石
膏スラリーのｐＨが急上昇する直前の値になるように制
御することを特徴とする、コークス炉ガスからの石膏の
製造方法。 ２、前記酸化塔への前記空気の吹き込み量を、１，８０
０〜２，５００Ｎｍ＾３／Ｈの範囲内とする、請求項１
に記載の方法。[Claims] 1. Desulfurization treatment is performed on coke oven gas, sulfur content in the waste liquid produced by the desulfurization treatment is burned, and then the combustion exhaust gas containing sulfur dioxide gas produced by the combustion is converted into calcium hydroxide solution. The calcium hydrogen sulfite slurry is then introduced into an oxidation tower and reacted with air blown from the lower part of the oxidation tower to form a gypsum slurry, and the gypsum slurry is separated. In a gypsum manufacturing method for obtaining gypsum, the amount of air blown into the oxidation tower is set to a value immediately before the oxygen concentration in the exhaust gas from the oxidation tower reaches its lowest value and the pH of the gypsum slurry suddenly increases. A method for producing gypsum from coke oven gas, the method comprising: 2. The amount of air blown into the oxidation tower is 1.80
Claim 1: Within the range of 0 to 2,500 Nm^3/H
The method described in.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4369390A JPH03247509A (en) | 1990-02-23 | 1990-02-23 | Production of gypsum from coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4369390A JPH03247509A (en) | 1990-02-23 | 1990-02-23 | Production of gypsum from coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH03247509A true JPH03247509A (en) | 1991-11-05 |
Family
ID=12670914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4369390A Pending JPH03247509A (en) | 1990-02-23 | 1990-02-23 | Production of gypsum from coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH03247509A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109876759A (en) * | 2019-04-09 | 2019-06-14 | 昆山宇顺环保科技有限公司 | Accelerate the method and device of Desulphurization sulfite calcium oxidation using low temperature waste gas |
-
1990
- 1990-02-23 JP JP4369390A patent/JPH03247509A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109876759A (en) * | 2019-04-09 | 2019-06-14 | 昆山宇顺环保科技有限公司 | Accelerate the method and device of Desulphurization sulfite calcium oxidation using low temperature waste gas |
| CN109876759B (en) * | 2019-04-09 | 2021-07-20 | 昆山宇顺环保科技有限公司 | Method and device for accelerating oxidation of calcium sulfite in desulfurized fly ash by using low-temperature waste gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4452766A (en) | Double alkali process for removal of sulfur dioxide from gas streams | |
| US7419643B1 (en) | Methods and apparatus for recovering gypsum and magnesium hydroxide products | |
| EP0604701B1 (en) | Method of sulfur dioxide removal from gaseous streams with alpha hemihydrate gypsum product formation | |
| US4876076A (en) | Process of desulfurization | |
| US4040803A (en) | Wet waste flue gas desulfurizing process using lime as absorbent | |
| JPH03247509A (en) | Production of gypsum from coke oven gas | |
| EP0448599A1 (en) | A lignin preparation and a method for its manufacture. | |
| US6572832B2 (en) | Method of removing sulfur dioxide from a gaseous stream in a wet scrubbing unit | |
| US3965242A (en) | Method for desulfurizing exhaust gas by alkali sulphite-gypsum process | |
| CA1162033A (en) | Process for removing sulfur dioxide from combustion exhaust gas | |
| JPH0141376B2 (en) | ||
| US4003986A (en) | Process for producing sulfur from sulfur dioxide or ammonium sulfites | |
| US6099816A (en) | Process for desulfurizing a sulfur-dioxide containing gas | |
| AU696509B2 (en) | Process for removing SO2 from gases which contain it, with direct production of elemental sulfur | |
| US4990315A (en) | Apparatus for desulfurization | |
| JPH03247510A (en) | Production of gypsum from coke oven gas | |
| CN113634113A (en) | Method for solving dehydration difficulty of desulfurized gypsum slurry | |
| US4526768A (en) | Process for producing sulphuric acid | |
| US3826819A (en) | Sulfuric acid purification process | |
| US4313924A (en) | Process for removal of sulfur dioxide from gas streams | |
| WO2019127305A1 (en) | Processing method for producing sodium sulfite product by so2 flue gas absorption and arsenic-removal purification using leaching solution of arsenic-containing industrial alkaline residue | |
| US4698219A (en) | Treatment of waste from iron ore reduction | |
| JP3645675B2 (en) | Exhaust gas desulfurization method | |
| JPS6265909A (en) | Method and apparatus for treating gas containing sulfur dioxide | |
| US2383427A (en) | Calcium stannate refining |