JPH0716580B2 - Dry flue gas desulfurization method - Google Patents
Dry flue gas desulfurization methodInfo
- Publication number
- JPH0716580B2 JPH0716580B2 JP60227797A JP22779785A JPH0716580B2 JP H0716580 B2 JPH0716580 B2 JP H0716580B2 JP 60227797 A JP60227797 A JP 60227797A JP 22779785 A JP22779785 A JP 22779785A JP H0716580 B2 JPH0716580 B2 JP H0716580B2
- Authority
- JP
- Japan
- Prior art keywords
- tower
- flue gas
- water
- gas desulfurization
- recovery system
- 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 - Lifetime
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】 （関連技術分野） 本発明は乾式排煙脱硫方法の改良に関するものである。TECHNICAL FIELD The present invention relates to an improvement in a dry flue gas desulfurization method.
（従来技術） 従来は、脱離塔出口には、サイクロン集塵器の様な簡単
でしかもダストのみしか除去できない集塵器が設置され
ていた。しかもこれはダスト捕集効率が悪く、塩安（NH
4Cl）、硫安（NH4）2SO4）はそのまま通過し、次の副生
品回収系へ流入されるという状態であった。(Prior Art) Conventionally, a dust collector that is simple and can remove only dust, such as a cyclone dust collector, was installed at the exit of the desorption tower. Moreover, this has poor dust collection efficiency,
4 Cl) and ammonium sulphate (NH 4 ) 2 SO 4 ) passed through as they were and flowed into the next by-product recovery system.
（発明が解決しようとする問題点） 従来型乾式脱硫装置では、乾式脱硫プロセスにおける副
生品回収系の構成機器および／また配管がNH4Clや（N
H4）2SO4或いは活性炭粉等によって閉塞したり、回収副
生品内へ上記物質が混入し、回収副生品の純度を落すと
いう問題があったが、本発明はこのような問題を解決し
ようとするものである。(Problems to be Solved by the Invention) In the conventional dry desulfurization equipment, the components and / or the piping of the by-product recovery system in the dry desulfurization process are NH 4 Cl or (N
H 4 ) 2 SO 4 or activated carbon powder or the like clogs, or the above substances are mixed into the recovered by-product, which reduces the purity of the recovered by-product, but the present invention has such problems. It is something to solve.
（発明の解決手段） 脱離塔４と副生品回収系との間に水スプレー6aとこれに
続く充填塔6bよりなる洗浄塔６を設置し、該洗浄塔６で
脱離ガス中の不純物を除去したのち副生品回収系に送る
ようにし、かつ洗浄塔パージ水を温水気化器11に導きこ
れを蒸発させ、該蒸気を吸着塔入口及び／または出口煙
道に導き、排煙脱硫装置にて再利用可能にした。(Means for Solving the Invention) A cleaning tower 6 comprising a water spray 6a and a subsequent packing tower 6b is installed between the desorption tower 4 and a by-product recovery system, and impurities in the desorbed gas are contained in the cleaning tower 6. After being removed, the cleaning tower purged water is introduced into the hot water vaporizer 11 to evaporate it, and the vapor is introduced into the adsorption tower inlet and / or outlet flue to produce a flue gas desulfurization device. Made reusable.
（実施例） 副生品として硫黄で回収する場合を述べると、１はボイ
ラーで、該ボイラーの排煙は吸着塔２を経て煙突３から
大気中に排出される。(Example) As for the case of recovering sulfur as a by-product, 1 is a boiler, and the smoke emitted from the boiler is discharged from the chimney 3 to the atmosphere through the adsorption tower 2.
４は脱離塔で、この脱離塔４を出た脱離ガスはNH4Cl、
（NH4）2SO4、HFを1,000〜10,000ppm程度含んでいる。
又この他に活性炭粉を１〜3g/Nm3程度含んでいる。脱離
ガスはダクト５を経て、洗浄塔６でまず水スプレー6aと
接触し、NH4Cl、（NH4）2SO4、HF等が洗浄されてこれら
物質の含有率が０〜10ppmまで低減される。又含有され
ているSO2はほとんど水に溶けないため、そのまま純度
の高いSO2リッチガスとして充填塔6bを経て後段の硫黄
回収系７に送られる。4 is a desorption tower, and the desorption gas leaving this desorption tower 4 is NH 4 Cl,
Contains (NH 4 ) 2 SO 4 and HF in the range of 1,000 to 10,000 ppm.
In addition to this, it also contains about 1 to 3 g / Nm 3 of activated carbon powder. The desorbed gas passes through the duct 5 and first comes into contact with the water spray 6a in the washing tower 6 to wash NH 4 Cl, (NH 4 ) 2 SO 4 , HF, etc., and the content of these substances is reduced to 0 to 10 ppm. To be done. Further, since the contained SO 2 is almost insoluble in water, it is sent as it is to the sulfur recovery system 7 in the subsequent stage via the packed column 6b as a highly pure SO 2 rich gas.
洗浄塔６の前段では水スプレー6aに直接脱離ガスが接触
するので、ガス温度も下げ、後段のラシヒリング等が充
填されている充填塔6b内で気液接触して完全にNH4Cl、
（NH4）2SO4等が除去される。Since the desorbed gas comes into direct contact with the water spray 6a in the front stage of the washing tower 6, the gas temperature is also lowered, and gas-liquid contact is made completely in the packed tower 6b filled with Raschig rings and the like in the rear stage to complete NH 4 Cl,
(NH 4 ) 2 SO 4 etc. are removed.
又脱離ガス中には30〜40％のH2Oが含まれているが、充
填塔6bで凝縮除去される。かくして充填塔の出口では、
約70〜80℃のガス温度となっている。The desorbed gas contains 30 to 40% of H 2 O, which is condensed and removed in the packed column 6b. Thus, at the exit of the packed tower,
The gas temperature is about 70-80 ° C.
充填塔6bにて精製されたSO2リッチの脱離ガスは硫黄回
収系７に送られ、高純度の硫黄として回収される。残っ
たテールガスは焼却炉８で焼却される。The SO 2 rich desorbed gas purified in the packed column 6b is sent to the sulfur recovery system 7 and is recovered as high-purity sulfur. The remaining tail gas is incinerated in the incinerator 8.
洗浄塔６ではポンプ10によって洗浄水が循環されるが、
洗浄水槽９内のPH値等の増加によって適時補給水が注入
されるようになっている。The washing water is circulated by the pump 10 in the washing tower 6,
Make-up water is injected at appropriate times by increasing the PH value in the cleaning water tank 9.
又洗浄水槽９の水位によって、洗浄水は温水気化器11に
パージ排出される。温水気化器11で蒸気と間接熱交換
し、ドレーンを蒸発させて、該蒸気は吸着塔２の入口又
は出口側へ戻され再利用されるようになっている。Further, the cleaning water is purged and discharged to the warm water vaporizer 11 depending on the water level in the cleaning water tank 9. The hot water vaporizer 11 indirectly exchanges heat with the vapor to evaporate the drain, and the vapor is returned to the inlet or outlet of the adsorption tower 2 for reuse.
なお、回収副生品として硫黄回収の場合を示している
が、すでに確立されている硫酸等を回収する場合にも本
技術を適用することができるのは自明のことである。Although the case of sulfur recovery is shown as the recovery by-product, it is obvious that the present technology can be applied to the case of recovering already established sulfuric acid and the like.
（効果） １）従来、乾式脱硫プロセスに於ては不純物（NH4Cl、
（NH4）2SO4、HF、HCl、NH3等）を含んだSO2リッチ脱離
ガスがそのまま副生品回収系に送られ、構成機器および
／また配管の閉塞や腐触等の種々のトラブルの原因とな
っていた。これに対し、本発明の如く、脱離塔と副生品
回収系との間に洗浄塔を設ることにより、構成機器およ
び／また配管の閉塞がなくなり、副生品回収系の安全運
転が可能となった。又不純物とともに活性炭粉などのダ
ストも洗浄塔で除去するので、純度の高い副生品が回収
系で回収できる。(Effect) 1) Conventionally, in the dry desulfurization process, impurities (NH 4 Cl,
The SO 2 rich desorbed gas containing (NH 4 ) 2 SO 4 , HF, HCl, NH 3 etc. is sent to the by-product recovery system as it is, and various components such as blockage and corrosion of component equipment and / or piping Was causing trouble. On the other hand, by providing a washing tower between the desorption tower and the byproduct recovery system as in the present invention, the blockage of the component equipment and / or the piping is eliminated, and the safe operation of the byproduct recovery system is achieved. It has become possible. Further, since dust such as activated carbon powder is removed together with impurities in the washing tower, a highly pure by-product can be recovered by the recovery system.
２）洗浄水排水を温水気化器に導き蒸発させるので、排
水処理設備を要せず、又温水気化器で発生した蒸気を吸
着塔入口にもどした場合、NH3蒸気がこの蒸気中に存在
している為、アンモニアの使用量が低減でき、脱硫、脱
硝効率をあげることができる。かつまた、温度が低下し
水分が増加するので脱硫効率を一段と上昇させることが
できる。2) Since the wash water drainage is introduced to the hot water vaporizer and vaporized, no waste water treatment equipment is required, and when the steam generated in the hot water vaporizer is returned to the adsorption tower inlet, NH 3 vapor is present in this vapor. Therefore, the amount of ammonia used can be reduced, and desulfurization and denitration efficiency can be improved. Moreover, since the temperature decreases and the water content increases, the desulfurization efficiency can be further increased.
図は本発明に係る実施例に示す硫黄を回収する排煙脱硫
プロセスを示す図。 図において； １……ボイラー、２……吸着塔 ３……煙突、４……脱離塔 ５……ダクト、６……洗浄塔 6a……水スプレー、6b……充填塔 ７……硫黄回収系 ８……（テーブルガスの）焼却炉 ９……洗浄水槽、10……ポンプ 11……温水気化器FIG. 1 is a diagram showing a flue gas desulfurization process for recovering sulfur shown in an example according to the present invention. In the figure; 1 ... Boiler, 2 ... Adsorption tower 3 ... Chimney, 4 ... Desorption tower 5 ... Duct, 6 ... Washing tower 6a ... Water spray, 6b ... Packing tower 7 ... Sulfur recovery System 8 …… Incinerator (of table gas) 9 …… Washing water tank, 10 …… Pump 11 …… Hot water vaporizer
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/34 ＺＡＢ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Office reference number FI technical display location B01D 53/34 ZAB
Claims (1)
プレー（6a）とこれに続く充填塔（6b）よりなる洗浄塔
（６）を設置し、該洗浄塔（６）で脱離ガス中の不純物
を除去したのち副生品回収系に送るようにし、かつ洗浄
塔パージ水を温水気化器（11）に導きこれを蒸発させ、
該蒸気を吸着塔入口及び／または出口煙道に導き、排煙
脱硫装置にて再利用可能にしたことを特徴とする乾式排
煙脱硫方法。1. A washing tower (6) comprising a water spray (6a) and a packed tower (6b) following the water spray (6a) is installed between the desorption tower (4) and the by-product recovery system. After removing impurities in the desorbed gas in 6), it is sent to the by-product recovery system, and the cleaning tower purge water is introduced into the warm water vaporizer (11) to evaporate it.
A dry flue gas desulfurization method, characterized in that the vapor is guided to an inlet and / or an outlet flue of the adsorption tower so that it can be reused in a flue gas desulfurization apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60227797A JPH0716580B2 (en) | 1985-10-15 | 1985-10-15 | Dry flue gas desulfurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60227797A JPH0716580B2 (en) | 1985-10-15 | 1985-10-15 | Dry flue gas desulfurization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6287227A JPS6287227A (en) | 1987-04-21 |
| JPH0716580B2 true JPH0716580B2 (en) | 1995-03-01 |
Family
ID=16866538
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60227797A Expired - Lifetime JPH0716580B2 (en) | 1985-10-15 | 1985-10-15 | Dry flue gas desulfurization method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0716580B2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102350175B (en) * | 2011-07-15 | 2013-12-25 | 攀钢集团有限公司 | Multistage desorption system for desulphurization solution |
| CN103979766A (en) * | 2014-05-26 | 2014-08-13 | 南京理工大学 | Indirect sludge drying tail gas treatment device and treatment method thereof |
| CN111256147A (en) * | 2020-03-16 | 2020-06-09 | 李智 | Domestic waste pyrolysis gasification incineration grate furnace and its treatment system |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3944006A (en) * | 1974-08-15 | 1976-03-16 | Outboard Marine Corporation | Endless cleated track |
| JPS55147132A (en) * | 1979-05-04 | 1980-11-15 | Sumitomo Heavy Ind Ltd | Method for reducing so2 in waste gas to sulfur |
-
1985
- 1985-10-15 JP JP60227797A patent/JPH0716580B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6287227A (en) | 1987-04-21 |
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