JPS6031817A - Wet flue gas desulfurization method - Google Patents
Wet flue gas desulfurization methodInfo
- Publication number
- JPS6031817A JPS6031817A JP58140503A JP14050383A JPS6031817A JP S6031817 A JPS6031817 A JP S6031817A JP 58140503 A JP58140503 A JP 58140503A JP 14050383 A JP14050383 A JP 14050383A JP S6031817 A JPS6031817 A JP S6031817A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- absorbent
- slurry
- gypsum
- 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
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 19
- 230000023556 desulfurization Effects 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 10
- 239000003546 flue gas Substances 0.000 title claims description 10
- 230000002745 absorbent Effects 0.000 claims abstract description 34
- 239000002250 absorbent Substances 0.000 claims abstract description 34
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 30
- 239000010440 gypsum Substances 0.000 claims abstract description 30
- 239000002002 slurry Substances 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 238000010521 absorption reaction Methods 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 32
- 239000006227 byproduct Substances 0.000 claims description 4
- 150000007514 bases Chemical class 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 abstract 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 12
- 238000002485 combustion reaction Methods 0.000 description 6
- 229910000019 calcium carbonate Inorganic materials 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000007664 blowing Methods 0.000 description 4
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 4
- 235000010261 calcium sulphite Nutrition 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- -1 calcium basic compound Chemical class 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 210000003127 knee Anatomy 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、ＳＯ，含有排ガスから８０２を除去する排煙
脱硫方法において高脱硫率、高純度石膏の副生を同時に
達成する改良された湿式排煙脱硫方法に関するものであ
る。すなわち、吸収剤としてカルシウム塩基性化合物を
含むスラリーを使用し、排ガス中のＳＯ２を除去すると
ともに石１ｆを副生する方法において、単一の吸収塔を
使用し、排ガスの性状に応じて、最適な液ガス比、吸収
剤スラリーの吸収基液滞留時間を設定し、かつ、吸収液
スラリーｐＨを４〜６とすることによシ、高脱硫率を得
ると同時に、吸収液スラリーから直接高純度石膏を回収
することを特徴とするものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an improved wet flue gas desulfurization method that simultaneously achieves a high desulfurization rate and the by-product of high-purity gypsum in a flue gas desulfurization method for removing SO and 802 from flue gas containing it. be. In other words, in a method that uses a slurry containing a calcium basic compound as an absorbent to remove SO2 from exhaust gas and produce stone 1f as a by-product, a single absorption tower is used and the optimal By setting a suitable liquid-gas ratio, absorption base liquid residence time of the absorbent slurry, and adjusting the pH of the absorbent slurry to 4 to 6, a high desulfurization rate can be obtained, and at the same time, high purity can be obtained directly from the absorbent slurry. It is characterized by recovering gypsum.
従来、炭酸カルシウム、水酸化カルシウムｆｚどを、吸
収剤として、ＳＯ３と反応させ、得られた亜硫酸カルシ
ウムを酸化して石膏（硫酸カルシウム）を回収する方法
がなされているが、高脱硫率を得るためには、下記（１
）、 （２）式で示される吸収反応を２塔以上の吸収装
置で行なわせ、かつ、高純度石膏を回収するためには、
吸収装置とは別個に設けた、（３）式で系される反応を
行なう酸化装置を必要とし、この酸化装置において空気
吹込、硫酸添加等の方法にょシ高純度石膏が得られてい
た。Conventionally, calcium carbonate, calcium hydroxide fz, etc. are used as absorbents to react with SO3, and the resulting calcium sulfite is oxidized to recover gypsum (calcium sulfate), but this method achieves a high desulfurization rate. In order to do so, follow the steps below (1)
), In order to carry out the absorption reaction shown by formula (2) in two or more absorption units and to recover high-purity gypsum,
An oxidizing device that carries out the reaction expressed by equation (3), which is provided separately from the absorption device, is required, and high-purity gypsum can be obtained in this oxidizing device using methods such as air blowing and addition of sulfuric acid.
０ａＯＯａ ＋ ＢＯ２＋Ａｌｌ →ｏａｓｏ、−４Ｈ
！ｏ＋ｏｏ２＋ムｑ・・・（１）
０ａ（ＯＨ）２ ＋ＳＯ２＋Ａｑ −＋ ０ａＳＯ３−
％Ｈ２０＋Ａｑ・・・（２）
ＯａＳＯｓ・’ＡＨｚＯ＋’、４０ｚ＋Ａｑ−＋０ａＳ
Ｏ４・２Ｈ２０−１−Ａｑ・・・（３）
吸収装置本体では、（３）式が、副反応として起シうる
が、生成する石膏の量は、酸化装置を省略できるほど十
分ではなく、吸収装置において高脱硫率・高純度石膏の
生成の両者を同時に満足することはできなかった。0aOOa + BO2+All → oaso, -4H
! o+oo2+muq...(1) 0a(OH)2 +SO2+Aq −+ 0aSO3−
%H20+Aq...(2) OaSOs・'AHzO+', 40z+Aq-+0aS
O4.2H20-1-Aq... (3) In the absorber itself, equation (3) may occur as a side reaction, but the amount of gypsum produced is not sufficient to omit the oxidizer, and the absorption It was not possible to simultaneously satisfy both a high desulfurization rate and the production of high-purity gypsum using the equipment.
これを達成する方法として、吸収装置への空気吹込によ
シ両者を満足させる方法が発明されているが、この場合
においても、吸収塔への空気吹込装置が別途必要である
。As a method for achieving this, a method has been invented that satisfies both requirements by blowing air into the absorption device, but even in this case, a separate air blowing device into the absorption tower is required.
本発明者らは、従来の石灰−石膏法による排煙脱硫の欠
点を解消すべく鋭童研究した結果、これら従来法に対し
、酸化装置を設けることなく、また、吸収塔への空気吹
込なしに、単一の吸収塔だけで、高脱硫率・高純度石膏
生成を同時に達する仁とができる、簡略化された経済的
な方法を提供するものである。The present inventors conducted extensive research to resolve the drawbacks of flue gas desulfurization using the conventional lime-gypsum method. In addition, it provides a simplified and economical method that can simultaneously achieve high desulfurization efficiency and high purity gypsum production using only a single absorption tower.
すなわち、本発明は８０２１０００ ｐｐｍ以下、０２
４チ以上を含む排ガスから日ｏ２を除去し、石膏を副生
ずる吸収塔１塔方式湿式排煙脱硫方法において、吸収剤
としてＯａ 塩基性化合物ス：７Ｕ−を用い、吸収塔に
おいて、液ガス比１３ｔ／６１”以上、液滞留時間１３
Ｈｒ以上、吸収液スラリーｐＨ４〜６とすることにょシ
、高脱硫率を得ると同時に、吸収液スラリーから直接高
純度石膏を回収することを特徴とする湿式排煙脱硫方法
を提供するものである。That is, the present invention has a content of 8021000 ppm or less, 02
In the wet flue gas desulfurization method using one absorption tower, which removes O2 from the flue gas containing more than 4% and produces gypsum as a by-product, Oa basic compound 7U- is used as the absorbent, and the liquid-gas ratio is reduced in the absorption tower. 13t/61” or more, liquid residence time 13
To provide a wet flue gas desulfurization method characterized by obtaining a high desulfurization rate by adjusting the pH of the absorbent slurry to 4 to 6 and recovering high-purity gypsum directly from the absorbent slurry. .
本発明による方法は、単一の吸収塔からなる８０１吸収
装置（必要に応じて吸収液スラリーを濃縮するスラリー
濃縮装置）、吸収液スラリーより石膏を分離する石膏分
離装置、スラリー濃縮装置よりの上澄液ある％Ａ＃ｉ石
膏分離工程よシの分＠戸液とカルシウム塩基性化合物を
混合する吸収剤調合装置、これらを順次結ぶ配管および
吸収剤調合装置と吸収装置を結ぶ配管よ多構成される。The method according to the present invention includes an 801 absorption device consisting of a single absorption tower (slurry concentrator for concentrating the absorbent slurry as necessary), a gypsum separation device for separating gypsum from the absorbent slurry, and an upper layer of the slurry concentrator. The gypsum separation process with clear liquid consists of a multi-layer system including an absorbent blending device that mixes the liquid and a calcium basic compound, piping that connects these in sequence, and piping that connects the absorbent blending device and the absorption device. Ru.
以下、本発明の方法を実施するのに適する装置の一例を
添付の第１図にしたがって説明する。An example of an apparatus suitable for carrying out the method of the present invention will be described below with reference to the accompanying FIG. 1.
処理すべきｓｏ２を含有する排ガス１は、排ガス性状に
応じた吸収液滞留時間を有する液留部をもつ吸収塔２に
導入される。吸収塔２において排ガスは、ポンプ３によ
り多段のスプレーから噴霧嘔れる吸収液スラリーによｊ
ｐｓｏ、を除去され、流路４より煙突５へ送られ大気中
へ放出される。吸収液スラリーｐＨけ、吸収剤調合装置
６よシ、ポンプ７から流路８で吸収塔へ送られる吸収剤
スラリー流量を調節することによ如ｐＨ＝４〜６に調整
される。吸収液スラリーの一部は、流路？よ〕濃縮装置
１０へ送られ、濃縮嘔れたスラリーは、ポンプ１１で流
路１２よ如石膏分離装置１Ｓへ送られ、石膏１４を分離
する。濃縮装置１０の上澄液は、流路１５よシ吸収剤調
合装置６へ送られ、吸収剤１６と混合することにより、
吸収剤スラリーの調合が行なわれる。上澄液の一部は排
水１７として放出される。石膏分離装置１３のろ液は流
路１Ｂよシ濃縮装置１０へ戻される。The exhaust gas 1 containing SO2 to be treated is introduced into an absorption tower 2 having a liquid distillation section having an absorption liquid residence time depending on the exhaust gas properties. In the absorption tower 2, the exhaust gas is converted into absorption liquid slurry sprayed from multi-stage sprays by a pump 3.
pso is removed, sent to the chimney 5 through the flow path 4, and released into the atmosphere. The pH of the absorbent slurry is adjusted to between 4 and 6 by adjusting the flow rate of the absorbent slurry sent from the absorbent blending device 6 and the pump 7 to the absorption tower via the channel 8. Is part of the absorption liquid slurry a flow path? The concentrated slurry sent to the concentrator 10 is sent to the gypsum separation device 1S via the flow path 12 by the pump 11, where the gypsum 14 is separated. The supernatant liquid of the concentrator 10 is sent to the absorbent blending device 6 through the channel 15, and mixed with the absorbent 16, thereby
An absorbent slurry is prepared. A portion of the supernatant liquid is discharged as waste water 17. The filtrate from the gypsum separator 13 is returned to the concentrator 10 through the channel 1B.
第２図は従来の吸収塔２塔方式によるフローを示し、第
１図と共通する装置は同一番号で示しである。このフロ
ーでは第１図の場合と比べてｐＨ調整槽１８、酸化装置
（酸化塔１９、空気２０、酸化空気ファン２１）、硫酸
設備（硫酸２２、硫酸タンク２６、ｐＨメーター２４）
等を余分に必要としている。FIG. 2 shows the flow of a conventional two-absorption tower system, and devices common to those in FIG. 1 are designated by the same numbers. In this flow, compared to the case in Figure 1, there is a pH adjustment tank 18, an oxidation device (oxidation tower 19, air 20, oxidation air fan 21), sulfuric acid equipment (sulfuric acid 22, sulfuric acid tank 26, pH meter 24).
etc. are needed extra.
以上よシ本発明において用りられる装置では、建設コス
トで約５０％、ランニングコストで約５％のコストの軽
減が可能である。In summary, with the device used in the present invention, it is possible to reduce the construction cost by about 50% and the running cost by about 5%.
以下本発明を具体例によって説明する。The present invention will be explained below using specific examples.
比較例
重油燃焼排ガスを対象として、従来法の吸収塔２塔方式
の場合の試験結果を示す。Comparative Example Test results are shown for a conventional two-absorption tower system using heavy oil combustion exhaust gas.
■処理対象排ガス二重油燃焼排ガス
■処理ガス量 ： １０００１ｍ”／Ｈ■吸収塔型式
ニスプレー塔型式（向流）第１吸収塔 ５５０■φＸス
０００■Ｈ（スプレー２段）第２ ｔｔ ５５０■φＸ
Ｉ０，０００■Ｈ（スプｖ−４段）■吸収剤 ：炭酸カ
ルシウム
■吸収剤供給量 ：吸収Ｓｏ２に対して１．０２〜１．
０３倍当量
従来の吸収塔を二基用いる方法（吸収塔への空気吹込熱
）においては比較例に示す如く吸収塔出口吸収液スラリ
ー固形分中には多量の亜硫酸カルシウムが残存している
。■Exhaust gas to be treated Dual oil combustion exhaust gas ■Processed gas amount: 10001 m”/H ■Absorption tower type
Nispray tower type (countercurrent) 1st absorption tower 550■φX 000■H (spray 2 stages) 2nd tt 550■φX
I0,000 ■H (Spv-4 stage) ■Absorbent: Calcium carbonate ■Absorbent supply amount: 1.02 to 1.
In the conventional method using two absorption towers (air blowing heat into the absorption tower), a large amount of calcium sulfite remains in the solid content of the absorbent slurry at the exit of the absorption tower, as shown in the comparative example.
従って、高純度石膏を得るためには、亜硫酸カルシウム
を石膏化する酸化装置が必要となる道理である。あるい
は、吸収塔出口吸収液スラリー中において、亜硫酸カル
シウムを残存させないためには、吸収塔への空気吹込が
必要となってくるものである。Therefore, in order to obtain high-purity gypsum, an oxidation device for turning calcium sulfite into gypsum is required. Alternatively, in order to prevent calcium sulfite from remaining in the absorbent slurry at the outlet of the absorption tower, it is necessary to blow air into the absorption tower.
これに対し、本発明者らは、単一の吸収塔を使用する場
合、吸収塔での石膏生成率（吸収除去された８０２が石
膏に転化される割合）は、次の関係式で示されることを
見出した。On the other hand, the present inventors found that when a single absorption tower is used, the gypsum production rate in the absorption tower (the rate at which 802 absorbed and removed is converted to gypsum) is expressed by the following relational expression: I discovered that.
Ｙ 二石膏生成率 （−）
０２：ガス中の酸素濃度（−）
ＦＢ（）、 ：ガス中の８０２濃度（ｐｐｍ）Ｌ ：循
環液量 （ｍ”Ｈ）
Ｌ ＝ Ｌ／Ｇ Ｘ Ｇ
ＶＧ：液ガス比（ｍｕｍ３）
Ｇ ：処理ガスｆｉｔ（ｒｙ＋”／Ｈ）Ｈ−Ｔ ：吸収
基液滞留時間（Ｈｒ）
［５Ｏｚｌ：吸収Ｓｏ、量 （ｋｇ−ｍｏｔ／Ｈ）Ｋ
： １１〜 ＩＩＬ４
α ： １１８〜１．０
βニーα１〜α５
γ：１〜ｔ２
θ：α２〜１．０
但し、吸収液スラリーｐＨ＝＝４〜６
実施例１
重油燃焼排ガスを対象として、本発明の方法を適用した
場合の試験結果を示す。Y Gypsum production rate (-) 02: Oxygen concentration in gas (-) FB (), : 802 concentration in gas (ppm) L: Circulating fluid amount (m”H) L = L/G X G VG: Liquid-gas ratio (mum3) G: Processing gas fit (ry+”/H) H-T: Absorption base liquid residence time (Hr) [5Ozl: Absorption So, amount (kg-mot/H) K
: 11 to IIL4 α : 118 to 1.0 β knee α1 to α5 γ: 1 to t2 θ: α2 to 1.0 However, absorption liquid slurry pH==4 to 6 Example 1 This study was conducted on heavy oil combustion exhaust gas. The test results obtained when the method of the invention is applied are shown.
■処理対象排ガス：重油燃焼排ガス
■処理ガス景 ： １０００ ａｍ”／ｎ■吸収塔型式
ニスプレー塔（向流）
５５０■φ×１５．０００閤Ｈ（スプレー６段）
■吸収剤 ：炭酸カルシウム
■吸収剤供給ｔ ：吸収Ｓｏ２に対して１．０２〜１．
０５倍当量
すなわち、実施例からは、単一の吸収塔を使用する場合
ｓｏ、１１１度が低く、”ｘｍ度、液ガス比、吸収基液
滞留時間が大きいほど石膏化が進むことが示されており
、少なくともＥＩＯｓ１０００ｐｐｍ以下、０１４％以
上を含む排ガスに対しては、液ガス比ｉ ｓ １７ｍ”
以上、吸収塔液滞留時間１５Ｈｒ以上、吸収液スラリー
ｐＨ＝４〜６とすることによシ、吸収浴出ロ吸収液スラ
リー中固形分は、９５憾以上の高純度石膏となしうるも
のである。そして、この条件下においては９５−以上の
高脱硫率も同時に達成されている。■Exhaust gas to be treated: Heavy oil combustion exhaust gas ■Processed gas view: 1000 am”/n ■Absorption tower type Nispray tower (countercurrent) 550 ■φ x 15.000 mm (6 spray stages) ■Absorbent: Calcium carbonate ■Absorption Agent supply t: 1.02 to 1.0 for absorbed So2.
In other words, the examples show that when a single absorption tower is used, so and 111 degrees are low, and the larger the xm degree, liquid-gas ratio, and absorption base liquid residence time, the more gypsumization progresses. For exhaust gas containing at least 1000ppm or less of EIOs and 0.14% or more, the liquid gas ratio is 17m"
As described above, by setting the absorption tower liquid residence time to 15 hours or more and the absorption liquid slurry pH to 4 to 6, the solid content in the absorption liquid slurry coming out of the absorption bath can be made into high purity gypsum of 95% or more. . Under these conditions, a high desulfurization rate of 95 or more was simultaneously achieved.
また、実施例１と比較例を比較すると、同様の排ガス性
状、運転条件において、脱硫性能は、ともに９５係以上
の高脱硫率を達成してφるものの、吸収塔出口吸収液ス
ラリー中の固形分中の石膏割合は、吸収塔２塔方式では
、非常に低い値である。すなわち、前述した石膏生成率
を示す関係式は、吸収塔１塔の場合において成立するも
のであシ、吸収塔２塔方式からは考えられないものであ
る。In addition, when comparing Example 1 and Comparative Example, under similar exhaust gas properties and operating conditions, both achieved a high desulfurization rate of 95 coefficients or higher in terms of desulfurization performance. The proportion of gypsum in the two absorption towers is a very low value. That is, the above-mentioned relational expression indicating the gypsum production rate holds true in the case of one absorption tower, and cannot be considered from a two-absorption tower system.
下記実施例２，３に本発明の方法を石炭燃焼排ガス分対
象として適用した場合について示す。Examples 2 and 3 below show cases in which the method of the present invention is applied to coal combustion exhaust gas.
実施例２
■処理対象排ガス：石炭専焼排ガス
■処理ガス量 ：５５４０口ＯＮｍ３Ａ１１■吸収塔型
式 ニスプレー塔（向流）
９、 ７ ｍφ Ｘ ５ ５．５ ｍＨ■吸収剤 ：炭
酸カルシウム
■吸収剤供給ｔ ：吸収ｓｏ２に対して１．０５倍当量
実施例３
■処理対象排ガス二石炭専焼排ガス
■処理ガス量 ：１．３３６，００ＯＮｍ３７ｎ湿■吸
収塔型式 ニスプレー塔（向流）
１４、Ｏｍφ×３五ｉｍＨ
■吸収剤 ：炭酸カルシウム
■吸収剤供給量 ：吸収ＳＯ，に対して１．０５倍当量
以上の如く、実施例２．３よシ、本発明の方法による効
果は明らかである。Example 2 ■ Exhaust gas to be treated: Coal combustion exhaust gas ■ Processing gas amount: 5540 ports ONm3A11 ■ Absorption tower type Nispray tower (countercurrent) 9, 7 mφ x 5 5.5 mH ■ Absorbent: Calcium carbonate ■ Absorbent supply t : 1.05 times equivalent to absorbed SO2 Example 3 ■ Exhaust gas to be treated Two coal-fired exhaust gas ■ Processing gas amount: 1.336,00 ON m37n wet ■ Absorption tower type Nispray tower (countercurrent) 14, Omφ x 35 imH (1) Absorbent: Calcium carbonate (2) Absorbent supply amount: 1.05 times or more equivalent to absorbed SO, as in Examples 2 and 3, the effects of the method of the present invention are clear.
第１図は本発明の方法を実施するのに適する装置の一例
を示す概念図、第２図は従来法における装置の概念図を
示す。
１：排ガス、２：吸収塔、３：吸収塔循環ポンプ、４：
煙道、５：煙突、６：吸収剤調合タンク、７：吸収剤供
給ポンプ、８．？、１２゜１５．１８：配管、１０ニス
ラリ−濃縮装置、１１：ポンプ、１Ｓ：固液分離装置、
１４：石膏、１６：吸収剤、１７：排水、１８ ： ｐ
Ｈ調整槽、１９二酸化塔、２０：空気、２に酸化空気フ
ァン、２２：硫酸、２３：硫酸タンク、２４ ： ｐＨ
メーター
代理人 内 １） 明
代理人 萩 原 亮 −FIG. 1 is a conceptual diagram showing an example of an apparatus suitable for implementing the method of the present invention, and FIG. 2 is a conceptual diagram of an apparatus in a conventional method. 1: Exhaust gas, 2: Absorption tower, 3: Absorption tower circulation pump, 4:
flue, 5: chimney, 6: absorbent preparation tank, 7: absorbent supply pump, 8. ? , 12゜15.18: Piping, 10 Nis slurry concentrator, 11: Pump, 1S: Solid-liquid separation device,
14: Plaster, 16: Absorbent, 17: Drainage, 18: p
H adjustment tank, 19 Dioxide tower, 20: Air, 2: Oxidizing air fan, 22: Sulfuric acid, 23: Sulfuric acid tank, 24: pH
Meter Agents 1) Akira Agent Ryo Hagiwara −
Claims (1)
スから８０．を除去し、石膏を副生ずる吸収塔１塔方式
湿式排煙脱硫方法において、吸収剤としてＯａ塩基性化
合物スラリーを用い、吸収塔において、液ガス比ｉ３ｔ
／＠”以上、液滞留時間１３Ｈｒ 以上、吸収液スラＩ
）−ｐＨ４〜６とすることによシ、高脱硫率を得ると同
時に、吸収液スラリーから直接高純度石膏を回収するこ
とを特徴とする湿式排煙脱硫方法。80.80% from exhaust gas containing less than 8021000 ppm and more than 0.024%. In the wet flue gas desulfurization method using one absorption tower and producing gypsum as a by-product, Oa basic compound slurry is used as an absorbent, and the liquid-to-gas ratio i3t is
/@” or more, liquid residence time 13Hr or more, absorption liquid slug I
) - A wet flue gas desulfurization method characterized by obtaining a high desulfurization rate by adjusting the pH to 4 to 6 and at the same time recovering high purity gypsum directly from the absorbent slurry.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58140503A JPS6031817A (en) | 1983-08-02 | 1983-08-02 | Wet flue gas desulfurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58140503A JPS6031817A (en) | 1983-08-02 | 1983-08-02 | Wet flue gas desulfurization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6031817A true JPS6031817A (en) | 1985-02-18 |
| JPH0355172B2 JPH0355172B2 (en) | 1991-08-22 |
Family
ID=15270151
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58140503A Granted JPS6031817A (en) | 1983-08-02 | 1983-08-02 | Wet flue gas desulfurization method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6031817A (en) |
-
1983
- 1983-08-02 JP JP58140503A patent/JPS6031817A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0355172B2 (en) | 1991-08-22 |
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