JPH02293017A - Treatment of exhaust gas containing so2 and hf - Google Patents
Treatment of exhaust gas containing so2 and hfInfo
- Publication number
- JPH02293017A JPH02293017A JP1113650A JP11365089A JPH02293017A JP H02293017 A JPH02293017 A JP H02293017A JP 1113650 A JP1113650 A JP 1113650A JP 11365089 A JP11365089 A JP 11365089A JP H02293017 A JPH02293017 A JP H02293017A
- Authority
- JP
- Japan
- Prior art keywords
- slurry tank
- absorption liquid
- exhaust gas
- slurry
- absorption
- 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.)
- Granted
Links
- 238000010521 absorption reaction Methods 0.000 claims abstract description 71
- 239000002002 slurry Substances 0.000 claims abstract description 65
- 239000007788 liquid Substances 0.000 claims abstract description 54
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 19
- 230000002745 absorbent Effects 0.000 claims abstract description 7
- 239000002250 absorbent Substances 0.000 claims abstract description 7
- 238000000034 method Methods 0.000 claims description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 9
- 239000001569 carbon dioxide Substances 0.000 claims description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 abstract description 14
- 230000000694 effects Effects 0.000 abstract description 9
- 229910000019 calcium carbonate Inorganic materials 0.000 abstract description 8
- 235000010216 calcium carbonate Nutrition 0.000 abstract description 7
- 239000000428 dust Substances 0.000 abstract description 6
- 230000002411 adverse Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 31
- 239000003513 alkali Substances 0.000 description 7
- 230000007423 decrease Effects 0.000 description 5
- 238000000354 decomposition reaction Methods 0.000 description 4
- 239000010440 gypsum Substances 0.000 description 4
- 229910052602 gypsum Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 159000000000 sodium salts Chemical class 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 241000726103 Atta Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003657 drainage water Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000006748 scratching Methods 0.000 description 1
- 230000002393 scratching effect Effects 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、排ガスの処理方法に関し、特に石炭燃焼排ガ
スのようなＳＯ２とＨＰを含むｌＩ−ガスの湿式？処理
方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for treating exhaust gas, and in particular to a wet treatment method for lI-gas containing SO2 and HP, such as coal combustion exhaust gas. Regarding processing method.
（従来の技術〕
一般に知られている湿式石灰法による排煙脱硫法を実施
する場合、排ガス中には有害成分としてＳＯｘの他にＨ
Ｆが含まれる場合がある。石炭燃焼排ガス中に存在する
各成分の１例を示すと、ＳＯｘが約１０００ｐｐｍ、Ｈ
Ｆが約４０ｐｐｍ−ごある．このような排ガスをＣａＣ
ＯｔをＳＯ■吸収剤として湿式排ガス処理塔で処理する
と次のような反応が生ずる。(Prior art) When carrying out the flue gas desulfurization method using the generally known wet lime method, the flue gas contains H as a harmful component in addition to SOx.
F may be included. To give an example of each component present in coal combustion exhaust gas, SOx is about 1000 ppm, H
There is approximately 40 ppm of F. Such exhaust gas is converted into CaC
When Ot is treated as an SO2 absorbent in a wet exhaust gas treatment tower, the following reaction occurs.
ＣａＣＯｔ ＋ Ｓｏｌ−＋ＣａＳＯｚ ＋Ｃｏ２（１
）ＣａＣＯｚ＋２｝ＩＦ−ＣａＦｚ＋ＣＯ２＋ｌｌｚＯ
（２）〔発明が解決しようとする課題］
ところが、排ガス中にダストが多く含まれている場合、
このダスト中に含まれるＡ！成分が溶解し、ガス中から
のＨＦと反応してＡＩのフッ素化合物（以下八ＩＦｘで
示す）を生成し、このＡＩＦｘは石灰石（ＣａＣＯｓ）
の溶解作用を妨害することが知られている（特開昭５５
−１６７０２３号参照）。CaCOt+Sol-+CaSOz+Co2(1
) CaCOz+2}IF-CaFz+CO2+llzO
(2) [Problem to be solved by the invention] However, when the exhaust gas contains a lot of dust,
A contained in this dust! The components dissolve and react with HF from the gas to produce AI fluorine compounds (hereinafter referred to as IFx), and this AIFx is limestone (CaCOs).
It is known that the dissolving action of
-167023).
またこのために、塩基性ナトリウム塩のような強アルカ
リを添加して不具合を防止する方法が上記の特許公開公
報に示されている。For this purpose, the above-mentioned patent publication discloses a method of adding a strong alkali such as a basic sodium salt to prevent this problem.
従って、ＳＯ．とＨＦを含む排ガスを処理するに当たり
、ＨＦＩに見合った塩基性ナトリウム塩を添加してやれ
ば、ＡｆｆｉＦｘに起因する不具合の無い排ガス処理方
法として有効であることが伺い知れる．しかし、この方
法はＣａＣＯ，以外に強アルカリを吸収剤として、相当
看消費するためにランニングコストの上昇及び注入設備
コストの追加等を招く欠点があった。さらに、供給され
たナトリウムが、吸収液中に溶存して存在するため、排
水量を減少させようとすると、吸収液中のナトリウムの
濃度が増加し、石膏として回収しようとする場合、回収
石膏の純度が低下するおそれがある．また、強アルカリ
化合物をパルス的に添加し、吸収液のｐＨを一時的に上
昇させる事により、八ｌＰｘに起因する不具合を防止す
る方法も知られている．（特開昭６０−１２２０２９号
参照）．ただし、この場合には、説硫性能が低下してか
ら回復するまで、短時間ではあるが脱硫性能が低下する
おそれがある。Therefore, SO. It can be seen that when treating exhaust gas containing AffiFx and HF, adding a basic sodium salt commensurate with the amount of HFI is effective as an exhaust gas treatment method without the problems caused by AffiFx. However, this method uses a strong alkali as an absorbent in addition to CaCO, and has the disadvantage of increasing running costs and adding injection equipment costs because it is consumed considerably. Furthermore, since the supplied sodium exists dissolved in the absorption liquid, if an attempt is made to reduce the amount of drainage water, the concentration of sodium in the absorption liquid will increase, and if an attempt is made to recover it as gypsum, the purity of the recovered gypsum will increase. may decrease. It is also known to prevent problems caused by 8lPx by adding a strong alkaline compound in pulses to temporarily raise the pH of the absorption liquid. (Refer to Japanese Patent Application Laid-open No. 122029/1983). However, in this case, there is a risk that the desulfurization performance will decrease, albeit for a short period of time, from when the desulfurization performance decreases until it recovers.
ところが、本発明者らは、上記不具合の無い排ガス処理
方法の堤供を目的として、検討を進めたところ、排ガス
吸収塔に供給するＣａＣＯ．を含む吸収液を保存するス
ラリータンクを２基設け、該吸収液を第二のスラリータ
ンクから排ガス吸収塔に供給し、該吸収塔から第一のス
ラリータンクに送り、該第一のスラリータンクから前記
第二のスラリータンクに送る順路で吸収液を循環し、か
つ前記第一のスラリータンクの吸収液中に空気を吸込み
、かつ、前記第二のスラリータンクに空気を供給するこ
とにより、該第二のスラリータンク内の吸収液のｐｌｌ
を５．５〜６．５に維持すると共に前記第一のスラリー
クンク内の吸収液中の炭酸ガスを放敗させることにより
、ＡｆＦｘによるＣａＣＯユの溶解阻害の不具合を無く
し、高純度の石膏を回収できる本発明の排ガス処理方法
を得るに至った。However, the present inventors conducted studies with the aim of providing an exhaust gas treatment method free of the above-mentioned problems, and found that CaCO. Two slurry tanks are provided to store an absorption liquid containing . By circulating the absorption liquid in the route to the second slurry tank, sucking air into the absorption liquid in the first slurry tank, and supplying air to the second slurry tank, the second slurry tank is supplied with air. PLL of absorption liquid in the second slurry tank
By maintaining the ratio between 5.5 and 6.5 and eliminating the carbon dioxide in the absorption liquid in the first slurry tank, the problem of inhibition of dissolution of CaCO by AfFx is eliminated, and high-purity gypsum is recovered. The present inventors have succeeded in obtaining the exhaust gas treatment method of the present invention.
本発明では、上記の通り、吸収剤としてＣａＣＯ３を用
い、該吸収液を排ガス吸収塔へ供給する第二のスラリー
タンクに空気を供給することによりｐＨを５．５から６
．５にコントロールし、排ガス吸収塔から吸収液が送ら
れる第一のスラリータンクの吸収液中に空気を吹き込み
、該吸収液中の炭素ガスを放散させ、吸収液を第二のス
ラリータンクから排ガス吸収塔及び第一のスラリータン
クを経て第二のスラリータンクに循環させるようにして
いる．従来から、４４Ｆｘを分解するためには、前記の
塩基性ナトリウム塩の他に各種の強アルカリ化合物が促
案されている．これは、ＡｊＰｘの構成要素である＾Ｅ
が、アルカリにより固相に移行するためである。In the present invention, as described above, CaCO3 is used as an absorbent, and the pH is adjusted from 5.5 to 6 by supplying air to the second slurry tank that supplies the absorption liquid to the exhaust gas absorption tower.
．． 5, air is blown into the absorption liquid in the first slurry tank to which the absorption liquid is sent from the exhaust gas absorption tower to diffuse carbon gas in the absorption liquid, and the absorption liquid is transferred from the second slurry tank to absorb exhaust gas. The slurry is circulated through the tower and the first slurry tank to the second slurry tank. Conventionally, in order to decompose 44Fx, various strong alkaline compounds have been proposed in addition to the above-mentioned basic sodium salt. This is a component of AjPx ^E
This is because the alkali causes the transition to the solid phase.
本発明者等は、＾ＩＦｘの分解するｐＨｌ域について更
に検討を進めたところ、分解にはｐｌ＋を５．５から６
．５に維持することが効果的であることを見いだし足。The present inventors further investigated the pH range in which IFx decomposes, and found that pl+ is 5.5 to 6 for decomposition.
．． I found it effective to keep it at 5 feet.
さらにスラリー中の溶存炭酸ガスを放散することにより
ＡｆＦｘｆｉ度の低いスラリーでは吸収剤のＣａＣＯ＊
のみをアルカリ源としてｐｌｌが上記ＡｆｆｉＦｘ分解
ｐ Ｉｆ ｉＪ域まで上昇することを見い出した。Furthermore, by dissipating the dissolved carbon dioxide in the slurry, in slurries with low AfFxfi, the absorbent CaCO*
It has been found that pll increases to the above-mentioned AffiFx decomposition p If iJ range using only as an alkali source.
またｐＨを上げて一旦ＡｊＦｘを分解しても、ｐＨが低
下するとＡｆＦｘとして再溶解しＣａＣＯ３の活性を阻
害し易いことを見いだした。Furthermore, it has been found that even if AjFx is once decomposed by increasing the pH, when the pH decreases, it is easily redissolved as AfFx and inhibits the activity of CaCO3.
上記事実に基づき、本発明者等は、ＣａＣＯ，の供給方
法と炭酸ガス放散用空気の供給方法について鋭意検討し
た結果、排ガス吸収塔へ供給するＣａＣＯ３を含む吸収
液を保有するスラリータンクを２基設け、吸収液は第二
のスラリータンクから該吸収塔へ供給し、該吸収塔から
第一のスラリータンクに送り、該第一のスラリータンク
から前記第二のスラリータンクに送る順路で循環し、前
記第一のスラリータンクの吸収液に酸化用空気を送り、
前記第二のスラリータンクには炭酸ガス放散用の空気を
供給することにより第二のタンク中のスラリーのｐＨを
、５．５から６．５に制御する方法を見いだした。Based on the above facts, the inventors of the present invention have conducted intensive studies on the supply method of CaCO and the supply method of air for dispersing carbon dioxide gas, and have constructed two slurry tanks that hold the absorption liquid containing CaCO3 to be supplied to the exhaust gas absorption tower. provided, the absorption liquid is supplied from a second slurry tank to the absorption tower, from the absorption tower to the first slurry tank, and from the first slurry tank to the second slurry tank. Sending oxidizing air to the absorption liquid in the first slurry tank,
A method was found to control the pH of the slurry in the second tank from 5.5 to 6.5 by supplying air for carbon dioxide gas diffusion to the second slurry tank.
即ち、第二のスラリータンク内では次式のとうり吸収液
中に含まれる炭酸ガスを放散させＣａＣＯ ，の溶解を
促進してｐｌ＋を上昇させる．ＣａＣ０３＋ Ｈ ”
＝Ｃａｚ″″＋ＩＩＣＯ３− −−−−−−−−（
３）｝ＩＣＯ＊− ＝ＯＩＩ− ＋ＣＯ！↑ −・−
・−−一−−−−−−−−−−− （４）？Ｏ■の放散
が促進されるほど（３） （４）式の右辺への反応が促
進されｐ１１が上昇するが、吸収液ｐｌｌを６．５以上
にするためには過剰の空気を供給することになり、ラン
ニングコスト上昇を招くことから得策ではなく、かつ、
ＡｆＦｘの分解にも効果を及ぼすことはない．また、吸
収液ｐｌ１が５．５を下回るとＡｆｆｉＦｘの分解が不
充分となる。以上のことから、第二のスラリータンクの
吸収液ｐｕを５．５から６．５に制？Ｉｌ１することに
より安定したＣａＣＯ＋の反応性を維持できることが分
かった．
また、本発明では排ガス中に同伴されるＡｆｔ’ｘの発
生源（即ちダスト及び１１Ｆ）量が変動しても第二スラ
リータンク中の吸収液のｐｌ＋を常に所定領域となるよ
う空気供給量を調整することで安定運転可能であるが、
ＡｆｆｉＦｘの発生源が大きく増大した場合、又は何ら
かの誤掻作により吸収液のｐ｝Ｉが低下し吸収液中に＾
ｆｆｉＦｘが増大した場合には、ＣＯ，放散用の空気の
みでは吸収液のｐＨを所定領域に維持することが困難と
なる場合がある．このような場合には、ＣＯｔ放散用の
空気に加えてＣａ （０１１） ！のような強アルカリ
を第二スラリータンク中に間欠または連続的に供給し、
ｐｌ＋を所定の領域に維持することが有効である。That is, in the second slurry tank, carbon dioxide contained in the absorption liquid is diffused according to the following formula, promoting dissolution of CaCO 2 and increasing pl+. CaC03+H”
=Caz″″+IICO3− −−−−−−−−(
3)}ICO*- =OII- +CO! ↑ −・−
・−−1−−−−−−−−−−− (4)? The more the dissipation of O■ is promoted, the more the reaction to the right side of equations (3) and (4) is promoted and p11 increases, but in order to make the absorption liquid pll more than 6.5, excessive air must be supplied. This is not a good idea as it will lead to an increase in running costs, and
It also has no effect on the decomposition of AfFx. Furthermore, if the absorption liquid pl1 is less than 5.5, the decomposition of AffiFx will be insufficient. Based on the above, it is possible to control the absorption liquid PU in the second slurry tank from 5.5 to 6.5. It was found that stable CaCO+ reactivity could be maintained by Il1. In addition, in the present invention, even if the amount of Aft'x generation sources (i.e., dust and 11F) entrained in the exhaust gas changes, the air supply amount is adjusted so that the pl+ of the absorption liquid in the second slurry tank is always within a predetermined range. Stable operation is possible by adjusting the
When the source of AffiFx increases significantly, or due to some kind of accidental scratching, the p}I of the absorption liquid decreases and ^^ is added to the absorption liquid.
When ffiFx increases, it may become difficult to maintain the pH of the absorption liquid within a predetermined range using only CO and air for dispersion. In such cases, in addition to air for COt dissipation, Ca (011)! Supplying a strong alkali such as intermittently or continuously into the second slurry tank,
It is useful to maintain pl+ in a predetermined region.
この場合においても炭酸ガス敢敗用の空気の供給は、強
アルカリ添加量の大幅な低減する効果を持つ。In this case as well, the supply of air for eliminating carbon dioxide gas has the effect of significantly reducing the amount of strong alkali added.
（実施例） 本発明の一実施例を第１図によって説明する。(Example) An embodiment of the present invention will be described with reference to FIG.
小型微粉炭焚き（図示なし）からの俳ガスを、２００ｍ
３Ｎ／ｈ分取し、第１図に示す本発明による排ガス処理
法によって処理した。被処理排ガスの温度は、熱交換器
（図示なし）によって人口温度１１０゜Ｃ、ダスト濃度
はバグフィルター（図示なし）により約２００ｓ＋ｇ／
＋”Ｎに調整されているゆ入口ＳＯｚｆｉ度１；ｔ１２
００ｐｐｍ、ｔｌＦｆｉ度ｉ！５３ｐｐｍ Ｔ！ アッ
た．
被処理排ガスは、ライン３により吸収塔５に導入され、
Ｓｏｗ及びＨＦがガス中より除去された後ライン４より
排出される．吸収塔５下には、吸収液を保有する第一の
スラリータンク１と第二のスラリータンク２の２基のス
ラリータンクが設けられ、吸収液は第二のスラリータン
ク２から吸収液ボンプ６により吸収塔５に送られ、吸収
塔５から第一のスラリータンクｌに送り、第一のスラリ
ータンク１から第二のスラリータンク２に送る順路で循
環される。Gas from a small pulverized coal fire (not shown) is distributed over 200m.
3N/h was fractionated and treated by the exhaust gas treatment method according to the present invention shown in FIG. The temperature of the exhaust gas to be treated is controlled to 110°C by a heat exchanger (not shown), and the dust concentration is controlled to about 200s+g/g by a bag filter (not shown).
The inlet SOzfi degree adjusted to +”N is 1; t12
00ppm, tlFfi degree i! 53ppm T! Atta. The waste gas to be treated is introduced into the absorption tower 5 through the line 3,
After Sow and HF are removed from the gas, it is discharged from line 4. Below the absorption tower 5, there are two slurry tanks, a first slurry tank 1 and a second slurry tank 2, which hold absorption liquid, and the absorption liquid is transferred from the second slurry tank 2 to an absorption liquid pump 6. The slurry is sent to the absorption tower 5, from the absorption tower 5 to the first slurry tank 1, and from the first slurry tank 1 to the second slurry tank 2, where it is circulated.
吸収液としてのＣａＣＯｓスラリーは、ライン７よリス
ラリータンク１に供給されており、この際のＣａＣＯｓ
スラリー供給流量は、吸収塔より排出されるライン４の
ガス中のＳｏｔ濃度が５０９９ｆｉとなるように濃度調
節計９を介して回節弁８によって自動調節される。CaCOs slurry as an absorption liquid is supplied to reslurry tank 1 through line 7, and at this time CaCOs
The slurry supply flow rate is automatically adjusted by the adjustment valve 8 via the concentration controller 9 so that the Sot concentration in the gas in the line 4 discharged from the absorption tower becomes 5099fi.
一方、Ｃｏｔ放散用空気は、ライン１０より第二のスラ
リータンク２内の吸収液中に供給され、空気の供給ｉ量
は、スラリータンク２から吸収塔５に送られる吸収液の
ｐＨが５．７となるようにρＨｉｌｌ節計１２を介して
１１節弁１１によって自動調整される。On the other hand, the Cot diffusion air is supplied from the line 10 into the absorption liquid in the second slurry tank 2, and the amount of air supplied is such that the pH of the absorption liquid sent from the slurry tank 2 to the absorption tower 5 is 5. It is automatically adjusted by the 11-node valve 11 via the ρHill meter 12 so that the value becomes 7.
また、第一のスラリータンクｌには一定量の酸化用空気
がラインｌ３により導入される．吸収液ボンプ６により
吸収塔５に供給される吸？液の一部はラインｌ４より抜
き出される．以上の条件にて、定常運転を実施したとこ
ろ出口ガス中のＳＯ！は６０ｐρ一で安定に運転でき、
第一のスラリータンク１の吸収液ｐｌｌは５．２であっ
た．また、吸収液中のＣａＣＯｓ４度は、０．０６ｍｏ
ｌ／ ｌとなり、ＣａＣＯ３の反応性は良好であり、亜
硫酸カルシウムの存在しないことも確認した。Further, a certain amount of oxidizing air is introduced into the first slurry tank l through a line l3. The absorption liquid supplied to the absorption tower 5 by the absorption liquid pump 6? A portion of the liquid is extracted from line l4. When steady operation was carried out under the above conditions, SO in the outlet gas! can be operated stably with 60 pρ,
The absorbent pll in the first slurry tank 1 was 5.2. In addition, CaCOs 4 degrees in the absorption liquid is 0.06 mo
It was confirmed that the reactivity of CaCO3 was good and that calcium sulfite was not present.
この吸収液中のＡ２、Ｆｉｌ１度を測定したところそれ
ぞれ１．３ａ＋ｇ＃！、２０＋ｇｇ／ ４２の微量であ
った。When A2 and Fil1 degrees in this absorption liquid were measured, each was 1.3a+g#! , 20+gg/42.
本実施例の酸化用及びＣＯ．放散用空気の供給量比は
Ｃｏｔ放散用／ ｆｃＯｔ放敗用士酸化用］ ＝０．２
０となった。For oxidation and CO. The supply amount ratio of air for dissipation is Cot dispersion/fcOt dissipation air oxidation] = 0.2
It became 0.
（比較例）
前記実施例と同一の装置、ガス条件にて、ＣＯ！放散用
空気の供給を停止して運転した。(Comparative example) Using the same equipment and gas conditions as in the above example, CO! The system was operated with the supply of air for dissipation stopped.
即ち、第１図にて、ライン１０から第二のスラリータン
ク２へ供給していたＣＯ■放散用空気を停止した。That is, in FIG. 1, the CO2 dispersion air that was being supplied from the line 10 to the second slurry tank 2 was stopped.
本比較例では、運転開始以降次第にスラリータンクｌ及
び２の吸収液ｐｌ＋が低下し、最終的にスラリータンク
１及び２の吸収液ｐ｝ｌはそれぞれ４．５４．８となっ
た。In this comparative example, the absorption liquid pl+ in slurry tanks 1 and 2 gradually decreased after the start of operation, and finally the absorption liquid p}l in slurry tanks 1 and 2 became 4.54.8, respectively.
吸収液中のＣａＣＯ３ｉ１度は０．２０ｍｏｌ／ ｌと
なり、前記実施例に比べＣａＣＯｓの反応性が著しく低
下した．この吸収液口液中のＡ１、Ｆｆｉ度はそれぞれ
５０ｍｇ／ｊ！ ， １５０Ｂ／ １であった。The CaCO3i1 degree in the absorption liquid was 0.20 mol/l, and the reactivity of CaCOs was significantly lower than in the previous example. The A1 and Ffi degrees in this absorption liquid oral fluid are each 50mg/j! , 150B/1.
［発明の効果］
以上説明したように、本発明は、Ｓｏｗと旺を含む排ガ
スをＣａＣＯ１を含む吸収液によって排ガス吸収塔によ
って処理するに当たり、排ガス中のＨＦとダストに起因
する悪影響を除外し、ＣａＣＯ＋の活性を維持してＳＯ
ｔとＨＦを有効に吸収することができ、かつ、高価なＣ
ａ（０１１）ｔ等の強アルカリの添加量を不要にするか
その量を著しく低減できると共に、高純度の石膏を回収
することができる．[Effects of the Invention] As explained above, the present invention eliminates the adverse effects caused by HF and dust in the exhaust gas when treating the exhaust gas containing Sow and Oxygen in an exhaust gas absorption tower with an absorption liquid containing CaCO1, Maintaining CaCO+ activity and SO
C that can effectively absorb T and HF and is expensive.
It is possible to eliminate or significantly reduce the amount of strong alkali such as a(011)t added, and to recover high-purity gypsum.
第１図は本発明の一実施例を示すフロー図である。
２・・・第二のスラリータンク、
５・・・吸収塔、 ６・・・吸収液ボンブ、７
・・・吸収液のライン、 ８・・・調節弁、９・・・
濃度調節計、 １１・・・調節弁、１２・・・１１
１調節計、 １０． １３・・・空気のライン
。FIG. 1 is a flow diagram showing one embodiment of the present invention. 2... Second slurry tank, 5... Absorption tower, 6... Absorption liquid bomb, 7
...Absorbing liquid line, 8...Control valve, 9...
Concentration controller, 11...control valve, 12...11
1 controller, 10. 13...Air line.
Claims (1)
ガス吸収塔に供給される吸収剤としてＣａＣＯ＿３を含
む吸収液を用い、該吸収液を、第二のスラリータンクか
ら排ガス吸収塔に供給し、該排ガス吸収塔から第一のス
ラリータンクに送り、該第一のスラリータンクから前記
第二のスラリータンクに送る順路で循環させ、かつ、空
気を前記第二のスラリータンクに供給して該第二のスラ
リータンク内の吸収液ｐＨを５．５から６．５に維持す
ると共に、前記第一のスラリータンク内の吸収液中にも
空気を吹き込み該吸収液中の炭酸ガスを放散させること
を特徴とするＳＯ＿２とＨＦを含む排ガスの処理方法。In treating the exhaust gas containing SO_2 and HF, an absorption liquid containing CaCO_3 is used as an absorbent to be supplied to the exhaust gas absorption tower, and the absorption liquid is supplied from the second slurry tank to the exhaust gas absorption tower, and the exhaust gas is The second slurry is supplied from the absorption tower to the first slurry tank and circulated in the order from the first slurry tank to the second slurry tank, and air is supplied to the second slurry tank to prepare the second slurry. The pH of the absorption liquid in the tank is maintained from 5.5 to 6.5, and air is also blown into the absorption liquid in the first slurry tank to diffuse carbon dioxide gas in the absorption liquid. A method for treating exhaust gas containing SO_2 and HF.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1113650A JP2738954B2 (en) | 1989-05-08 | 1989-05-08 | Method for treating exhaust gas containing SO2 and HF |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1113650A JP2738954B2 (en) | 1989-05-08 | 1989-05-08 | Method for treating exhaust gas containing SO2 and HF |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02293017A true JPH02293017A (en) | 1990-12-04 |
| JP2738954B2 JP2738954B2 (en) | 1998-04-08 |
Family
ID=14617645
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1113650A Expired - Fee Related JP2738954B2 (en) | 1989-05-08 | 1989-05-08 | Method for treating exhaust gas containing SO2 and HF |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2738954B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5779999A (en) * | 1995-12-29 | 1998-07-14 | Marsulex Environmental Technologies, Llc | Method for scrubbing flue gases |
| WO1999017863A1 (en) * | 1996-04-08 | 1999-04-15 | Nkk Corporation | Wet type exhaust gas desulfurization method |
| EP1201290A4 (en) * | 1999-07-19 | 2002-09-04 | Ebara Corp | Apparatus and method for cleaning acidic gas |
| EP1366797A2 (en) * | 1997-11-11 | 2003-12-03 | Mitsubishi Heavy Industries, Ltd. | A wet gas processing method and the apparatus using the same |
| JP2006326430A (en) * | 2005-05-24 | 2006-12-07 | Kawasaki Plant Systems Ltd | Absorbing tower for flue gas desulfurization apparatus |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5898126A (en) * | 1981-12-03 | 1983-06-10 | Ishikawajima Harima Heavy Ind Co Ltd | Desulfurization of stack gas |
| JPS60122029A (en) * | 1983-12-05 | 1985-06-29 | Mitsubishi Heavy Ind Ltd | Disposition of waste gas |
-
1989
- 1989-05-08 JP JP1113650A patent/JP2738954B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5898126A (en) * | 1981-12-03 | 1983-06-10 | Ishikawajima Harima Heavy Ind Co Ltd | Desulfurization of stack gas |
| JPS60122029A (en) * | 1983-12-05 | 1985-06-29 | Mitsubishi Heavy Ind Ltd | Disposition of waste gas |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5779999A (en) * | 1995-12-29 | 1998-07-14 | Marsulex Environmental Technologies, Llc | Method for scrubbing flue gases |
| WO1999017863A1 (en) * | 1996-04-08 | 1999-04-15 | Nkk Corporation | Wet type exhaust gas desulfurization method |
| EP1366797A2 (en) * | 1997-11-11 | 2003-12-03 | Mitsubishi Heavy Industries, Ltd. | A wet gas processing method and the apparatus using the same |
| EP1366797A3 (en) * | 1997-11-11 | 2004-01-07 | Mitsubishi Heavy Industries, Ltd. | A wet gas processing method and the apparatus using the same |
| EP1201290A4 (en) * | 1999-07-19 | 2002-09-04 | Ebara Corp | Apparatus and method for cleaning acidic gas |
| JP2006326430A (en) * | 2005-05-24 | 2006-12-07 | Kawasaki Plant Systems Ltd | Absorbing tower for flue gas desulfurization apparatus |
| JP4734537B2 (en) * | 2005-05-24 | 2011-07-27 | 川崎重工業株式会社 | Absorption tower of flue gas desulfurization equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2738954B2 (en) | 1998-04-08 |
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