JPH0326094B2 - - Google Patents
Info
- Publication number
- JPH0326094B2 JPH0326094B2 JP58207615A JP20761583A JPH0326094B2 JP H0326094 B2 JPH0326094 B2 JP H0326094B2 JP 58207615 A JP58207615 A JP 58207615A JP 20761583 A JP20761583 A JP 20761583A JP H0326094 B2 JPH0326094 B2 JP H0326094B2
- Authority
- JP
- Japan
- Prior art keywords
- slurry
- flue gas
- tank
- liquid
- liquid chamber
- 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
- 239000002002 slurry Substances 0.000 claims description 69
- 239000007788 liquid Substances 0.000 claims description 46
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 35
- 239000003546 flue gas Substances 0.000 claims description 35
- 229910052602 gypsum Inorganic materials 0.000 claims description 23
- 239000010440 gypsum Substances 0.000 claims description 23
- 238000006477 desulfuration reaction Methods 0.000 claims description 22
- 230000023556 desulfurization Effects 0.000 claims description 22
- 238000010521 absorption reaction Methods 0.000 claims description 20
- 239000006228 supernatant Substances 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 10
- 238000005192 partition Methods 0.000 claims description 8
- 239000006185 dispersion Substances 0.000 claims description 5
- 239000000834 fixative Substances 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims 3
- 239000011575 calcium Substances 0.000 description 16
- 150000001875 compounds Chemical class 0.000 description 11
- 239000013078 crystal Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- 239000002250 absorbent Substances 0.000 description 8
- 230000002745 absorbent Effects 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000007254 oxidation reaction Methods 0.000 description 7
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 6
- 235000010261 calcium sulphite Nutrition 0.000 description 6
- 239000003595 mist Substances 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 239000002562 thickening agent Substances 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 238000003892 spreading Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 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
- 238000007599 discharging Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000011505 plaster Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【発明の詳細な説明】
本発明は固形物を懸濁するスラリーを用いて排
煙中のSO2を吸収し、副生物として固体のイオウ
化合物を回収する湿式排煙脱硫装置に関するもの
である。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a wet flue gas desulfurization device that uses a slurry in which solids are suspended to absorb SO 2 in flue gas and recover solid sulfur compounds as by-products.
現在、排煙脱硫の主流をなしているものに
CaCO3やCa（OH）2を吸収剤として排煙脱硫を行
ない、亜硫酸カルシウムや硫酸カルシウム（石
膏）として回収するいわゆる湿式石灰法の排煙脱
硫装置があり、例えば、特開昭57−63117号公報
などの他、多くの刊行物に詳述されている通りで
ある。 Currently, the mainstream of flue gas desulfurization
There is a so-called wet lime method flue gas desulfurization device that desulfurizes flue gas using CaCO 3 or Ca(OH) 2 as an absorbent and recovers it as calcium sulfite or calcium sulfate (gypsum). This is detailed in many publications including official gazettes.
ここで、第１図によつて現在、工業的に広く採
用されている湿式石灰法による排煙脱硫装置を説
明する。 Here, with reference to FIG. 1, a flue gas desulfurization apparatus using a wet lime method, which is currently widely used industrially, will be explained.
SO2を含んだ排煙１は吸収塔本体２に導かる。
吸収塔本体２の下部にはCa化合物を懸濁したス
ラリーを受けるタンク３が設けてあり、撹拌機４
にてスラリーを撹拌して固形物の沈殿を防止す
る。Ca化合物を懸濁したスラリーは吸収塔循環
ポンプ５によつて塔頂に送られ、塔内に散布さ
れ、排煙と接触しながら流下し、再びタンク３に
戻る。スラリーと接触してSO2を除去された排煙
はミストエリミネーター６を通つて、浄化ガス７
として排出される。一方、タンク３へはSO2吸収
量に見合つてCaCO3やCa（OH）2のスラリーをラ
イン８により供給すると共に、吸収剤がSO2を吸
収して生成した亜硫酸カルシウムを含むスラリー
をライン９から酸化塔１０へ導く。酸化塔１０で
は底部に備えた気泡発生器１１から空気１２を吹
き込み、ライン１３から硫酸を供給して、亜硫酸
カルシウムを酸化して石膏にすると共に、未反応
のCaCO3やCa（OH）2を石膏に転化する。酸化塔
１０から出た石膏スラリーはライン１４を通つて
シツクナー１５に導かれ、濃縮石膏スラリーはラ
イン１６、タンク１７、ポンプ１８、遠心分離器
１９へ送られ、石膏２０を得ると共に過液はタ
ンク２１へ導かれ、ポンプ２２及びライン２３を
経由してシツクナー１５へ導かれる。一方、シツ
クナー１５の上澄液はライン２４からタンク２５
へ導かれ、ポンプ２６から、排煙脱硫装置内の例
えば吸収剤の調整用に使用されたり、排水された
りする。 Flue gas 1 containing SO 2 is led to the absorption tower main body 2.
A tank 3 is provided at the bottom of the absorption tower body 2 to receive the slurry in which Ca compounds are suspended.
Stir the slurry to prevent precipitation of solids. The slurry in which the Ca compound is suspended is sent to the top of the tower by the absorption tower circulation pump 5, spread inside the tower, flows down while coming into contact with flue gas, and returns to the tank 3 again. The flue gas from which SO 2 has been removed by contact with the slurry passes through a mist eliminator 6 and is purified gas 7.
It is discharged as. On the other hand, a slurry of CaCO 3 or Ca(OH) 2 is supplied to tank 3 through line 8 in accordance with the amount of SO 2 absorbed, and a slurry containing calcium sulfite produced by the absorbent absorbing SO 2 is supplied to tank 3 through line 9. from there to the oxidation tower 10. In the oxidation tower 10, air 12 is blown from a bubble generator 11 provided at the bottom, and sulfuric acid is supplied from a line 13 to oxidize calcium sulfite into gypsum, and remove unreacted CaCO 3 and Ca(OH) 2. Converts into plaster. The gypsum slurry coming out of the oxidation tower 10 is led to the thickener 15 through the line 14, and the concentrated gypsum slurry is sent to the line 16, tank 17, pump 18, and centrifugal separator 19 to obtain gypsum 20, and the filtrate is sent to the tank. 21 and then to the thickener 15 via a pump 22 and a line 23. On the other hand, the supernatant liquid of the thickener 15 is transferred from the line 24 to the tank 25.
The water is led to the pump 26 and used, for example, for adjusting an absorbent in the flue gas desulfurization equipment, or is drained.
本発明者らは、現在の排煙脱硫装置に含まれる
構成を簡単化して経済的にすぐれたものとするべ
く、鋭意研究を重ねて来た結果、CaCO3やCa
（OH）2の結晶とSO2との反応速度、SO2を吸収し
て生成する亜硫酸カルシウムの酸化反応速度、石
膏の沈降速度の各データに基づき、各々、別々の
工程をなす装置を別個に設けていた従来の装置構
成の基本的考え方を脱却し、吸収塔及び、吸収塔
タンクにSO2吸収、酸化、石膏沈殿濃縮、上澄液
回収の各操作を集約した、簡単化した本発明の装
置構成を完成するに到つたものである。 The inventors of the present invention have conducted extensive research in order to simplify the configuration included in current flue gas desulfurization equipment and make it economically superior .
Based on the data on the reaction rate of (OH) 2 crystals and SO 2 , the oxidation reaction rate of calcium sulfite produced by absorbing SO 2 , and the sedimentation rate of gypsum, we developed separate equipment for each process. The simplified method of the present invention breaks away from the basic concept of the conventional equipment configuration and consolidates the operations of SO 2 absorption, oxidation, gypsum precipitation concentration, and supernatant liquid recovery in the absorption tower and absorption tower tank. The device configuration has now been completed.
本発明の要旨は、SO2を含む排煙をSO2固定剤
を懸濁するスラリーと接触させてSO2を吸収する
湿式排煙脱硫装置に於いて、上記スラリー散布
手段を設けた吸収塔、該吸収塔に連通し、かつ
撹拌手段、SO2固定剤供給手段、前記スラリー散
布手段に連通するスラリー循環手段、下部のみが
スラリーと連通する仕切手段によつて区切られた
液室、及び排煙の組成に応じ要すれば酸化用ガス
分散手段を有するスラリー受けタンク、該液室
上部に設けられた上澄液排出手段、前記スラリ
ー循環手段より立ち上つて分岐したスラリー分岐
管、該スラリー分岐管に接続する石膏分離手
段、石膏分離手段より分離する分離液を前記液
室の下部に返送する配管、該返送管の下部でか
つ前記液室内に設けられた邪魔板よりなることを
特徴とする湿式排煙脱硫装置を提供するところに
ある。 The gist of the present invention is a wet flue gas desulfurization device that absorbs SO 2 by contacting flue gas containing SO 2 with a slurry in which an SO 2 fixative is suspended, an absorption tower provided with the above slurry dispersion means, A liquid chamber that communicates with the absorption tower and is separated by a stirring means, an SO 2 fixative supply means, a slurry circulation means that communicates with the slurry distribution means, a partition means whose lower part only communicates with the slurry, and exhaust gas. A slurry receiving tank having an oxidizing gas dispersion means if necessary depending on the composition of the slurry, a supernatant liquid discharge means provided at the upper part of the liquid chamber, a slurry branch pipe rising from the slurry circulation means and branching off, and the slurry branch pipe. A wet type characterized by comprising a gypsum separating means connected to the gypsum separating means, a pipe for returning the separated liquid separated from the gypsum separating means to the lower part of the liquid chamber, and a baffle plate provided at the lower part of the return pipe and inside the liquid chamber. The company provides flue gas desulfurization equipment.
本発明による湿式排煙脱硫装置の１実施例を第
２図によつて説明する。SO2を含んだ排煙１０１
は吸収塔本体１０２に導かれる。第２図では排煙
と吸収スラリーがいわゆる並流で接触する場合を
図示したが、第１図に示したような向流の気液接
触方式でもよい。 One embodiment of the wet flue gas desulfurization apparatus according to the present invention will be described with reference to FIG. Exhaust smoke containing SO 2 101
is guided to the absorption tower main body 102. Although FIG. 2 shows a case in which the flue gas and absorption slurry contact in a so-called parallel flow, a countercurrent gas-liquid contact method as shown in FIG. 1 may also be used.
吸収塔本体１０２の下部にはCa化合物を懸濁
したスラリーを受けるタンク１０３が設けてあ
り、撹拌機１０４にてスラリーを撹拌して固形物
の沈殿を防止する。Ca化合物を懸濁したスラリ
ーは吸収塔循環ポンプ１０５によつて塔頂に送ら
れ、スラリー散布装置１０６から塔内に散布され
排煙と接触しながら流下し再びタンク１０３に戻
る。スラリーと接触してSO2を除去された排煙は
ミストエリミネーター１０７を通つて、浄化ガス
１０８として排出される。一方、タンク１０３へ
はSO2吸収量に見合つてCaCO3やCa（OH）2のSO2
吸収剤を粉体貯蔵タンク１０９より供給する。吸
収剤であるCaCO3やCa（OH）2は水と懸濁したス
ラリーとしてタンク１０３へ供給することもでき
る。吸収剤がSO2を吸収して生成する亜硫酸カル
シウムは気液接触ゾーンでスラリーが酸性状態に
保たれる為、排煙中に含まれる酸素によつて酸化
され、石膏結晶に転化してしまう。しかし、排煙
中の酸素が少ない場合は酸化触媒のMn2+をタン
ク１０３へ添加するか、又は空気ノズル１１０か
ら酸素ガスを含む気体を供給すると、吸収された
SO2を石膏として固定化することができる。この
ようにタンク１０３ではCa化合物としての石膏
結晶が懸濁したスラリーが溜まるので、スラリー
排出口１１１と吸収塔循環ポンプ１０５を介して
スラリー散布装置１０６へ至る配管から石膏結晶
を含むスラリーを分岐管１１２で分取し、自動開
閉弁１２１でその分取量を調整しながら分離器１
１３へ導き石膏ケーキ１１４を得ると共に過液
はライン１１５からタンク１０３へ戻す。 A tank 103 for receiving slurry in which Ca compounds are suspended is provided at the bottom of the absorption tower main body 102, and the slurry is stirred by a stirrer 104 to prevent precipitation of solids. The slurry in which the Ca compound is suspended is sent to the top of the tower by an absorption tower circulation pump 105, and is spread into the tower from a slurry distribution device 106, flows down while coming into contact with flue gas, and returns to the tank 103 again. The exhaust gas from which SO 2 has been removed by contact with the slurry passes through a mist eliminator 107 and is discharged as purified gas 108. On the other hand, SO 2 such as CaCO 3 and Ca(OH) 2 is sent to the tank 103 in proportion to the amount of SO 2 absorbed .
Absorbent is supplied from a powder storage tank 109. The absorbent CaCO 3 or Ca(OH) 2 can also be supplied to the tank 103 as a slurry suspended in water. Since the slurry is kept in an acidic state in the gas-liquid contact zone, the calcium sulfite produced when the absorbent absorbs SO 2 is oxidized by the oxygen contained in the flue gas and converted into gypsum crystals. However, if the amount of oxygen in the flue gas is low, adding Mn 2+ as an oxidation catalyst to the tank 103 or supplying a gas containing oxygen gas from the air nozzle 110 will reduce the amount of oxygen absorbed.
SO 2 can be immobilized as plaster. In this way, slurry in which gypsum crystals as a Ca compound are suspended accumulates in the tank 103, so the slurry containing gypsum crystals is transferred from the pipe leading to the slurry distribution device 106 via the slurry discharge port 111 and the absorption tower circulation pump 105 into a branch pipe. 112, and the separator 1 adjusts the amount to be collected using the automatic on-off valve 121.
13 to obtain a gypsum cake 114, and the filtrate is returned to tank 103 through line 115.
タンク１０３の内部にはスラリー液面上から液
面下に亘つて、撹拌されているスラリーと隔離さ
れた液室１１６が形成されるように仕切壁１１７
を設け、仕切壁１１７の下端は開放させて、撹拌
機１０４によつて撹拌されたスラリーが仕切壁１
１７によつて仕切られた液室１１６の下部を互い
に流通し得るようにしてある。更に第２図には撹
拌されたスラリーの流動によつて、液室１１６内
の上澄液が乱されないように邪魔板１１８を設け
てある。液室１１６の上澄液は上澄液排出口１１
９とポンプ１２０を介して排出される。又、ライ
ン１１５より戻される過液は液室１１６の下部
に上方から下方に向つて流入するようにし石膏結
晶が上昇して来るのを防止する。更に石膏スラリ
ーを分取する分岐管１１２はスラリー散布装置１
０６に近い高位置に傾斜を持たせて取り付け、自
動開閉弁１２１によつて必要に応じてスラリーを
分取する。こうすることによつて自動開閉弁が閉
の時でも分岐管１１２内に石膏結晶の沈殿堆積に
よる詰まりが防止でき、また分離器１１３へは重
力で石膏スラリーが流下する為、液体運搬のエネ
ルギーが節減できる。 A partition wall 117 is installed inside the tank 103 to form a liquid chamber 116 that extends from above the slurry liquid level to below the liquid level and is isolated from the slurry being stirred.
The lower end of the partition wall 117 is opened so that the slurry stirred by the stirrer 104 can be passed through the partition wall 117.
The lower portions of the liquid chambers 116 partitioned by the liquid chambers 17 are made to be able to communicate with each other. Further, in FIG. 2, a baffle plate 118 is provided to prevent the supernatant liquid in the liquid chamber 116 from being disturbed by the flow of the stirred slurry. The supernatant liquid in the liquid chamber 116 is transferred to the supernatant liquid outlet 11
9 and pump 120. Further, the excess liquid returned from the line 115 flows downward from above into the lower part of the liquid chamber 116 to prevent gypsum crystals from rising. Further, a branch pipe 112 for separating the gypsum slurry is connected to the slurry spreading device 1.
The slurry is installed at a high position close to 06 with an inclination, and the slurry is separated as necessary using the automatic opening/closing valve 121. By doing this, even when the automatic on-off valve is closed, clogging due to gypsum crystal precipitation in the branch pipe 112 can be prevented, and since the gypsum slurry flows down to the separator 113 by gravity, the energy for transporting the liquid is saved. You can save money.
一般に湿式排煙脱硫装置ではミストエリミネー
ター１０７で捕集されたミスト中のCa化合物結
晶が付着堆積して、ガス流路を狭隘化しないよう
洗浄ノズル１２２から洗浄水が流入したり、更に
はポンプのシール水が流入する等、水が沢山使用
される。そしてこれらの水は、タンク１０３に溜
まつているスラリー濃度の外乱となる。スラリー
濃度の変化は湿式排煙脱硫装置の運転管理が不安
定になり種晶濃度変動に伴なうスケールトラブル
を誘発する。従来これらの問題は、解決されない
ままであり、特にCa化合物を懸濁したスラリー
を用いた湿式排煙脱硫装置のスケールの防止は重
要な課題であるが、本発明者らの研究によれば、
スケールトラブルの主因は水の流入によるスラリ
ー濃度変動にあることが分つた。 In general, in wet flue gas desulfurization equipment, Ca compound crystals in the mist collected by the mist eliminator 107 adhere and accumulate, causing cleaning water to flow in from the cleaning nozzle 122 to avoid narrowing the gas flow path, and even the pump A lot of water is used, such as seal water flowing in. These waters then disturb the slurry concentration stored in the tank 103. Changes in slurry concentration make the operational management of wet flue gas desulfurization equipment unstable and induce scale troubles due to fluctuations in seed crystal concentration. Conventionally, these problems have remained unsolved, and in particular, prevention of scale in wet flue gas desulfurization equipment using slurry in which Ca compounds are suspended is an important issue, but according to the research of the present inventors,
It was found that the main cause of scale trouble was slurry concentration fluctuation due to water inflow.
本発明装置においては上記の問題を湿式排煙脱
硫装置のタンクからCa化合物結晶を懸濁するス
ラリーを排出することと、同タンクからCa化合
物結晶濃度の低い上澄液を排出することの２つの
操作を同時に任意にしかも応答遅れがなく随意に
行なうことにより、湿式排煙脱硫装置のCa化合
物スラリー濃度を安定にコントロールすることが
可能となる。しかも、従来の湿式排煙脱硫装置に
比較して構成が簡単化された上に上述の効果が得
られる極めてすぐれた特徴がある。 The device of the present invention solves the above problem by two methods: discharging the slurry in which Ca compound crystals are suspended from the tank of the wet flue gas desulfurization device, and discharging the supernatant liquid with a low concentration of Ca compound crystals from the same tank. By performing the operations simultaneously and arbitrarily without delay in response, it becomes possible to stably control the Ca compound slurry concentration in the wet flue gas desulfurization equipment. Furthermore, compared to conventional wet flue gas desulfurization equipment, the structure is simplified and the above-mentioned effects can be obtained.
実施例
使用した装置は第２図に示す構成を有すもので
ある。EXAMPLE The apparatus used had the configuration shown in FIG.
石膏結晶を含むスラリーを溜めるタンク１０３
は1000mm×2000mmの断面を有し、液深さは2000mm
とした。吸収塔循環ポンプ１０５で50m3／ｈのス
ラリーを吸収塔１０２の塔頂のスラリー散布装置
１０６からスプレーし、塔内には合成樹脂製のグ
リツドを充填して気液並流方式で排煙3000Nm3／
ｈを処理し、入口SO21200ppmから出口
SO260ppmとなるまで脱硫した。タンク１０３へ
はCaCO3粉末を吸収剤として粉体貯蔵タンク１
０９からSO2吸収量に見合つて供給した。タンク
１０３の内部には内径が400mmで長さが2500mmの
下端が開放された円筒状の仕切壁１１７を取り付
けた。仕切壁１１７で囲まれた液室１１６から上
澄液を取り出すライン１１９からの上澄液流量
は、液室１１６内での平均上昇速度５ｍ／ｈ程度
とした時でも、上澄液は若干の固形物を浮遊して
いる程度のものが得られた。 Tank 103 for storing slurry containing gypsum crystals
has a cross section of 1000mm x 2000mm, and the liquid depth is 2000mm
And so. The absorption tower circulation pump 105 sprays slurry at a rate of 50 m 3 /h from the slurry spraying device 106 at the top of the absorption tower 102, and the tower is filled with a synthetic resin grid to exhaust smoke at 3000 Nm in a gas-liquid parallel flow system. 3 /
Process h and outlet from inlet SO 2 1200ppm
Desulfurization was carried out until SO 2 was 60ppm. Powder storage tank 1 is connected to tank 103 using CaCO 3 powder as an absorbent.
From 09 onwards, SO 2 was supplied in proportion to the amount of SO 2 absorbed. Inside the tank 103, a cylindrical partition wall 117 with an inner diameter of 400 mm and a length of 2500 mm and an open bottom end was installed. The supernatant liquid flow rate from the line 119 that takes out the supernatant liquid from the liquid chamber 116 surrounded by the partition wall 117 is such that even when the average rising speed in the liquid chamber 116 is about 5 m/h, the supernatant liquid is slightly A substance with only floating solids was obtained.
タンク１０３に溜まるCa化合物のスラリー濃
度を比重計にて検知しながらスラリー濃度を高め
る場合はライン１１９から上澄液を抜き出し、同
時に自動開閉弁１２１を閉として分岐管１１２か
らのスラリー分取を停止する。またスラリー濃度
を低くする場合はライン１１９からは同じく上澄
液をタンク１０３の液面レベルを保つべく抜き出
し乍ら、自動開閉弁１２１を開として分岐管１１
２から分離器１１３にスラリーを送り、石膏を分
離して後過液をライン１１５からタンク１０３
に戻した。かかる操作に依つて、タンク１０３の
スラリー濃度を１〜35重量％の領域に於ける所望
の濃度に管理運転できた。もちろんこの間SO2の
吸収剤であるCaCO3は粉体の状態で連続的にタ
ンク１０３に供給した。 When increasing the slurry concentration while detecting the slurry concentration of Ca compounds accumulated in the tank 103 with a hydrometer, the supernatant liquid is extracted from the line 119, and at the same time, the automatic opening/closing valve 121 is closed to stop the slurry collection from the branch pipe 112. do. In addition, when lowering the slurry concentration, the supernatant liquid is similarly extracted from the line 119 in order to maintain the liquid level in the tank 103, and the automatic opening/closing valve 121 is opened so that the branch pipe 11
The slurry is sent from line 115 to the separator 113 to separate the gypsum, and the filtrate is sent to the tank 103 from line 115.
I returned it to . Through such operations, the slurry concentration in tank 103 could be controlled to a desired concentration in the range of 1 to 35% by weight. Of course, during this time CaCO 3 which is an absorbent for SO 2 was continuously supplied to the tank 103 in the form of powder.
ライン１１９より抜き出す上澄液量はミストエ
リミネーター１０７の洗浄ノズル１２２から流入
する水と排煙への蒸発水とのバランスからタンク
１０３の液面が一定になるよう制御した。 The amount of supernatant liquid extracted from the line 119 was controlled so that the liquid level in the tank 103 would be constant based on the balance between the water flowing in from the cleaning nozzle 122 of the mist eliminator 107 and the evaporated water to the exhaust gas.
また自動開閉弁１２１を介して分離器１１３へ
送るスラリー流量は平均的に0.1〜１m3／ｈの範
囲で操作したので、スラリー散布装置１０６から
の噴射流量に殆んど影響を与えないものであつ
た。 Furthermore, since the slurry flow rate sent to the separator 113 via the automatic on-off valve 121 was operated within the range of 0.1 to 1 m 3 /h on average, it hardly affected the injection flow rate from the slurry spreading device 106. It was hot.
本実験で分離器１１３から排出された固形物の
組成はCaSO4・2H2O97wt％、CaCO30.5wt％、
その他2.5wt％であり亜硫酸カルシウムは検出さ
れなかつた。排煙中の酸素濃度が５〜８容量％含
まれていることから、吸収されたSO2が排煙中の
酸素によつて、グリツド充填気液接触域に於いて
全部酸化されてしまつた為、タンク１０３に設置
した空気ノズル１１０からはもはや空気を送風す
る必要はなかつた。 In this experiment, the composition of the solids discharged from the separator 113 was 97wt% CaSO 4 2H 2 O , 0.5wt% CaCO 3 ,
The other content was 2.5wt%, and no calcium sulfite was detected. Since the oxygen concentration in the flue gas is 5 to 8% by volume, all of the absorbed SO 2 was oxidized by the oxygen in the flue gas in the gas-liquid contact area filling the grid. It was no longer necessary to blow air from the air nozzle 110 installed in the tank 103.
以上の実験により本発明装置によれば従来の湿
式排煙脱硫装置では困難であつた吸収塔でのスラ
リー濃度の管理が、所望濃度に迅速に調整できる
ようになり、種晶濃度不足に依るスケールトラブ
ルや濃度過多に依る配管、弁類の摩損や閉塞のト
ラブルが解消できることを実証した。更に従来の
湿式排煙脱硫装置に設けられていた酸化塔、シツ
クナー及び過液タンクや上澄液タンクとそれら
設備に付帯するポンプ、弁、配管、計装器具など
が不要となり大幅な工程の簡略化を成し得ること
を実証した。 As a result of the above experiments, the device of the present invention makes it possible to quickly adjust the slurry concentration in the absorption tower to the desired concentration, which was difficult with conventional wet flue gas desulfurization devices. We have demonstrated that problems such as wear and tear and blockage of piping and valves caused by excessive concentration can be resolved. Furthermore, the oxidation tower, thickener, filtrate tank, supernatant tank, and associated pumps, valves, piping, instrumentation, etc. that were installed in conventional wet flue gas desulfurization equipment are no longer required, greatly simplifying the process. We have demonstrated that it is possible to achieve
第１図は従来から工業的に採用されている湿式
石灰法による排煙脱硫装置を示し、第２図は本発
明の湿式排煙脱硫装置の一実施例の構成図を示
す。
第２図において、１０１……排煙、１０２……
吸収塔本体、１０３……タンク、１０４……撹拌
機、１０５……吸収塔循環ポンプ、１０６……ス
ラリー散布装置、１０７……ミストエリミネータ
ー、１０８……浄化ガス、１０９……粉体貯蔵タ
ンク、１１０……空気ノズル、１１１……スラリ
ー排出口、１１２……分岐管、１１３……分離
器、１１４……石膏ケーキ、１１５……過液ラ
イン、１１６……液室、１１７……仕切壁、１１
８……邪魔板、１１９……上澄液排出口、１２０
……ポンプ、１２１……自動開閉弁、１２２……
洗浄ノズルである。
FIG. 1 shows a flue gas desulfurization system using a wet lime method that has been conventionally used industrially, and FIG. 2 shows a configuration diagram of an embodiment of the wet flue gas desulfurization system of the present invention. In Fig. 2, 101...exhaust smoke, 102...
Absorption tower body, 103... Tank, 104... Stirrer, 105... Absorption tower circulation pump, 106... Slurry spreading device, 107... Mist eliminator, 108... Purification gas, 109... Powder storage tank, 110...Air nozzle, 111...Slurry discharge port, 112...Branch pipe, 113...Separator, 114...Gypsum cake, 115...Liquid line, 116...Liquid chamber, 117...Partition wall, 11
8... Baffle plate, 119... Supernatant liquid outlet, 120
...Pump, 121...Automatic on-off valve, 122...
It is a cleaning nozzle.
Claims (1)
リーと接触させてSO2を吸収する湿式排煙脱硫装
置に於いて、上記スラリー散布手段を設けた吸
収塔、該吸収塔に連通し、かつ撹拌手段、SO2
固定剤供給手段、前記スラリー散布手段に連通す
るスラリー循環手段、下部のみがスラリーと連通
する仕切手段によつて区切られた液室、及び排煙
の組成に応じ要すれば酸化用ガス分散手段を有す
るスラリー受けタンク、該液室上部に設けられ
た上澄液排出手段、前記スラリー循環手段より
立ち上つて分岐したスラリー分岐管、該スラリ
ー分岐管に接続する石膏分離手段、石膏分離手
段より分離する分離液を前記液室の下部に返送す
る配管、該返送管の下部でかつ前記液室内に設
けられた邪魔板よりなることを特徴とする湿式排
煙脱硫装置。1. In a wet flue gas desulfurization equipment that absorbs SO 2 by bringing flue gas containing SO 2 into contact with a slurry in which an SO 2 fixative is suspended, an absorption tower provided with the slurry dispersion means described above, communicating with the absorption tower. and stirring means, SO 2
A fixative supply means, a slurry circulation means communicating with the slurry dispersion means, a liquid chamber separated by a partition means whose lower part only communicates with the slurry, and an oxidizing gas dispersion means if necessary depending on the composition of the flue gas. a slurry receiving tank, a supernatant liquid discharge means provided above the liquid chamber, a slurry branch pipe rising from the slurry circulation means and branching off, a gypsum separation means connected to the slurry branch pipe, and separation from the gypsum separation means. A wet flue gas desulfurization device comprising a pipe for returning the separated liquid to the lower part of the liquid chamber, and a baffle plate provided at the lower part of the return pipe and inside the liquid chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58207615A JPS6099329A (en) | 1983-11-07 | 1983-11-07 | Stack gas desulfurization apparatus by wet process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58207615A JPS6099329A (en) | 1983-11-07 | 1983-11-07 | Stack gas desulfurization apparatus by wet process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6099329A JPS6099329A (en) | 1985-06-03 |
| JPH0326094B2 true JPH0326094B2 (en) | 1991-04-09 |
Family
ID=16542719
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58207615A Granted JPS6099329A (en) | 1983-11-07 | 1983-11-07 | Stack gas desulfurization apparatus by wet process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6099329A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2505525B2 (en) * | 1988-04-08 | 1996-06-12 | 三菱重工業株式会社 | Gas-liquid contact treatment device for slurry |
| GB2296490B (en) * | 1994-05-11 | 1998-04-08 | Babcock Hitachi Kk | Wet-type flue gas desulfurization plant and method making use of a solid desulfurizing agent |
| CN103861431A (en) * | 2014-03-11 | 2014-06-18 | 贵州天下家政有限公司 | Primary treatment device for sulfuric acid tail gas |
| JP6526278B1 (en) * | 2018-03-23 | 2019-06-05 | 三菱日立パワーシステムズ株式会社 | Exhaust gas desulfurization system |
-
1983
- 1983-11-07 JP JP58207615A patent/JPS6099329A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6099329A (en) | 1985-06-03 |
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