JPH0125625Y2 - - Google Patents
Info
- Publication number
- JPH0125625Y2 JPH0125625Y2 JP133184U JP133184U JPH0125625Y2 JP H0125625 Y2 JPH0125625 Y2 JP H0125625Y2 JP 133184 U JP133184 U JP 133184U JP 133184 U JP133184 U JP 133184U JP H0125625 Y2 JPH0125625 Y2 JP H0125625Y2
- Authority
- JP
- Japan
- Prior art keywords
- slurry liquid
- absorbent
- slurry
- flow rate
- amount
- 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
Links
- 239000002002 slurry Substances 0.000 claims description 87
- 239000007788 liquid Substances 0.000 claims description 78
- 230000002745 absorbent Effects 0.000 claims description 62
- 239000002250 absorbent Substances 0.000 claims description 62
- 238000010521 absorption reaction Methods 0.000 claims description 38
- 239000002253 acid Substances 0.000 claims description 27
- 238000006477 desulfuration reaction Methods 0.000 claims description 27
- 230000023556 desulfurization Effects 0.000 claims description 27
- 238000006386 neutralization reaction Methods 0.000 claims description 18
- 238000001514 detection method Methods 0.000 claims description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- 239000007789 gas Substances 0.000 description 27
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 229910052815 sulfur oxide Inorganic materials 0.000 description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 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
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Description
【考案の詳細な説明】
［考案の技術分野］
本考案は排ガスの硫黄酸化物を除去する湿式排
煙脱硫装置に係り、特に、吸収塔内に循環する吸
収剤スラリ液濃度を常時一定にして排ガス量、
SO2濃度の変動に対して安定した脱硫率を維持す
ることができる湿式排煙脱硫装置に関する。[Detailed Description of the Invention] [Technical Field of the Invention] The present invention relates to a wet flue gas desulfurization device for removing sulfur oxides from flue gas, and in particular, the present invention relates to a wet flue gas desulfurization device that removes sulfur oxides from flue gas, and in particular, a device that constantly maintains a constant concentration of absorbent slurry circulating in an absorption tower. Exhaust gas amount,
This invention relates to a wet flue gas desulfurization device that can maintain a stable desulfurization rate against fluctuations in SO 2 concentration.
［考案の技術的背景とその問題点］
一般に、ボイラ等から排出される排ガス中には
硫黄酸化物（以下SOxという）が含まれているこ
とから、公害防止の見地より脱硫処理がなされた
後、清浄ガスとして大気中へ放出している。[Technical background of the idea and its problems] Generally, the exhaust gas emitted from boilers etc. contains sulfur oxides (hereinafter referred to as SOx), so from the viewpoint of pollution prevention, after desulfurization treatment is performed, , released into the atmosphere as clean gas.
ここで、比較的脱硫率が良好なことから多く採
用されている湿式排煙脱硫装置を第１図に基づい
て説明する。図示する如く１は吸収塔であり、石
灰などの吸収剤を溶解した吸収剤スラリ液が下部
の吸収液タンク２から抜き出されてスラリ液循環
通路３を通つた後、塔内に噴霧される。そして、
この噴露液と排ガス４とを接触させて脱硫処理を
行なう。 Here, a wet flue gas desulfurization device, which is widely used because of its relatively good desulfurization efficiency, will be explained with reference to FIG. As shown in the figure, reference numeral 1 denotes an absorption tower, in which an absorbent slurry liquid in which an absorbent such as lime is dissolved is extracted from an absorption liquid tank 2 at the bottom, passes through a slurry liquid circulation passage 3, and is then sprayed into the tower. . and,
Desulfurization treatment is performed by bringing this sprayed liquid into contact with the exhaust gas 4.
そして、この脱硫処理に際しては、吸収塔１の
入口排ガス中のSO2濃度及び排ガス量をそれぞれ
SO2濃度計５、ガス流量計６で計測し、これらの
積により入口排ガス中のSO2量を算出し、そし
て、これに過剰率設定器７でSO2量を過剰にして
必要な吸収剤量設定値を算出している。 During this desulfurization treatment, the SO 2 concentration in the exhaust gas at the entrance of absorption tower 1 and the amount of exhaust gas are
The amount of SO 2 in the inlet exhaust gas is calculated by the product of the SO 2 concentration meter 5 and the gas flow meter 6, and the amount of SO 2 is increased using the excess rate setting device 7 to add the necessary absorbent. The amount setting value is being calculated.
一方、吸収塔１に供給されるスラリ濃度やスラ
リ流量はそれぞれスラリ液供給通路８に介設した
スラリ濃度計９やスラリ流量計１０で計測され、
これらの値に基づいて供給される吸収剤量を算出
している。 On the other hand, the slurry concentration and slurry flow rate supplied to the absorption tower 1 are measured by a slurry concentration meter 9 and a slurry flow meter 10 provided in the slurry liquid supply passage 8, respectively.
The amount of absorbent to be supplied is calculated based on these values.
そして、吸収剤制御器１１により、上記算出さ
れた吸収剤量が前記吸収剤量設定値に一致するよ
うにスラリ液制御弁１２の開度を制御して必要な
吸収剤量を吸収塔１へ供給するようになつてい
る。 Then, the absorbent controller 11 controls the opening degree of the slurry liquid control valve 12 so that the calculated absorbent amount matches the absorbent amount set value, and supplies the required amount of absorbent to the absorption tower 1. supply.
ところで、脱硫効率は排ガス量の変動、入口
SO2濃度の変動など排ガスの条件により高くなつ
たり低くなつたりするため、吸収塔１のスラリ液
中に残る吸収剤量は脱硫率が高いと少なくなり、
脱硫率が低いと多くなる傾向がある。 By the way, desulfurization efficiency depends on fluctuating gas amount and inlet
The amount of absorbent remaining in the slurry liquid in absorption tower 1 decreases when the desulfurization rate is high, as it increases or decreases depending on flue gas conditions such as fluctuations in SO 2 concentration.
It tends to increase when the desulfurization rate is low.
このため、吸収剤量が少ない時に、入口排ガス
量や入口SO2濃度が増した場合前述した如く、こ
れに見合つた量の吸収剤が吸収液タンク２に供給
されるものの、特に、このタンクの容量が大きい
とタンク内の吸収剤濃度が中々上昇せず、脱硫効
率が低下するという不都合が起つていた。 For this reason, when the amount of absorbent is small and the amount of inlet exhaust gas or the inlet SO 2 concentration increases, as mentioned above, a commensurate amount of absorbent will be supplied to the absorbent tank 2, but especially if this tank If the capacity is large, the concentration of the absorbent in the tank will not rise at all, resulting in a reduction in desulfurization efficiency.
また、この脱硫装置にあつてはガス流量計６や
SO2濃度計５のように余り精度のよくない計器を
使うため、タンクに供給する吸収剤量を的確に制
御できない場合があつた。 In addition, in this desulfurization equipment, the gas flow meter 6 and
Since less accurate instruments such as the SO 2 concentration meter 5 were used, there were cases in which it was not possible to accurately control the amount of absorbent supplied to the tank.
一方、上述した不都合を解消するため第２図に
示す如く、塔内を循環する吸収液のPH値をPH計１
３で測定し、これが一定値を維持するようにスラ
リ液制御弁１２で供給吸収剤量を制御することも
行なわれてはいるが、この場合には吸収液中に混
入した燃料中の不純物によりPH計１３の指示が鈍
くなつて吸収液中の吸収剤濃度に比例したPH値を
表示しなくなり、的確な濃度制御ができない場合
があつた。 On the other hand, in order to eliminate the above-mentioned inconvenience, as shown in Figure 2, the PH value of the absorption liquid circulating in the column was measured using a PH meter.
3, and the amount of absorbent supplied is controlled by the slurry liquid control valve 12 so that it is maintained at a constant value, but in this case, the amount of absorbent is There were cases in which the PH meter 13's indication became dull and did not display a PH value proportional to the absorbent concentration in the absorbent, making it impossible to accurately control the concentration.
本考案は以上のような問題点に着目し、これを
有効に解決すべく創案されたものである。 The present invention focuses on the above-mentioned problems and has been devised to effectively solve them.
［考案の目的］
本考案の目的は、吸収塔内に循環する吸収剤ス
ラリ液濃度を常時一定にして、排ガス量、SO2濃
度の変動に対して安定した脱硫率を維持すことが
できる湿式排煙脱流装置を提供するにある。[Purpose of the invention] The purpose of the invention is to develop a wet desulfurization method that can maintain a stable desulfurization rate against fluctuations in exhaust gas amount and SO 2 concentration by constantly keeping the concentration of the absorbent slurry circulating in the absorption tower constant. To provide a flue gas deflow device.
［考案の概要］
本考案は吸収塔内に使用する吸収液の一部を取
り出すと共に、これに酸を加えて中和する中和チ
ヤンバと、この中和チヤンバに流入するスラリ液
量を検出するスラリ液量検出手段と、上記中和チ
ヤンバに流入する酸の流量を検出する酸流量検出
手段と、これら各検出手段で得られるスラリ液量
と酸流量値とから吸収塔内に流れるスラリ液濃度
を算出すると共にこの算出値に基づいてスラリ液
制御弁の開度調整をして吸収塔に供給される吸収
剤スラリ液量を制御する供給吸収剤制御手段とを
備え、上記目的を達成するものである。[Summary of the invention] This invention includes a neutralization chamber that takes out a portion of the absorption liquid used in the absorption tower and neutralizes it by adding acid, and detects the amount of slurry liquid flowing into this neutralization chamber. A slurry liquid amount detection means, an acid flow rate detection means for detecting the flow rate of acid flowing into the neutralization chamber, and a concentration of the slurry liquid flowing into the absorption tower from the slurry liquid amount and acid flow rate value obtained by each of these detection means. and a supply absorbent control means for calculating the amount of absorbent slurry supplied to the absorption tower by adjusting the opening degree of the slurry liquid control valve based on the calculated value, and achieving the above object. It is.
［考案の実施例］
以下に、本考案の好適一実施例を添付図面に基
づいて詳述する。[Embodiment of the invention] A preferred embodiment of the invention will be described below in detail with reference to the accompanying drawings.
第３図は本考案に係る脱硫装置を示す概略平面
図である。 FIG. 3 is a schematic plan view showing the desulfurization apparatus according to the present invention.
図示する如く１は下部に吸収液タンク２を有す
る筒体状の吸収塔である。この吸収塔１の下部側
壁には排ガスを塔内に導入する排ガス入口１４が
設けられると共に、上部には清浄ガスを排出する
ためのガス出口１５が設けられている。 As shown in the figure, 1 is a cylindrical absorption tower having an absorption liquid tank 2 at the bottom. The lower side wall of the absorption tower 1 is provided with an exhaust gas inlet 14 for introducing exhaust gas into the tower, and the upper part is provided with a gas outlet 15 for discharging clean gas.
上記吸収液タンク２にはこれに吸収剤スラリ液
を供給するための配管（以下「スラリ液供給通
路」という）８が接続されている。ここに吸収剤
としては例えば石灰（石灰石、生石灰、消石灰な
ど）や水酸化マグネシウムなどのアルカリ剤が使
用される。 A pipe (hereinafter referred to as "slurry liquid supply passage") 8 is connected to the absorption liquid tank 2 for supplying an absorbent slurry liquid thereto. As the absorbent, for example, an alkaline agent such as lime (limestone, quicklime, slaked lime, etc.) or magnesium hydroxide is used.
このスラリ液供給通路８にはスラリ液の流量制
御を行なうスラリ液制御弁１２、スラリ液の流量
を計測するスラリ流量計１０及びスラリ液の濃度
を計測するスラリ濃度計９とがそれぞれ順次介設
されている。 A slurry liquid control valve 12 for controlling the flow rate of the slurry liquid, a slurry flow meter 10 for measuring the flow rate of the slurry liquid, and a slurry concentration meter 9 for measuring the concentration of the slurry liquid are successively installed in the slurry liquid supply passage 8. has been done.
また、吸収液タンク２からはスラリ液循環通路
３が延出されると共に途中に循環ポンプ１６を介
設してその先端は吸収塔１内の上部に設けた噴霧
ノズル１７に接続されており、タンク２から抜き
出した吸収剤スラリ液を吸収塔１の上部に移送す
ると共に、これを塔内に噴霧するようになつてい
る。 Further, a slurry liquid circulation passage 3 extends from the absorption liquid tank 2, and a circulation pump 16 is interposed in the middle, the tip of which is connected to a spray nozzle 17 provided at the upper part of the absorption tower 1. The absorbent slurry liquid extracted from the absorption tower 2 is transferred to the upper part of the absorption tower 1, and is sprayed into the tower.
スラリ液循環通路３にはこれに流れるスラリ液
の一部（少量）を取出すための本考案の特徴とす
る中和チヤンバ１８が取出通路１９を介して接続
されており、この取出通路１９には取出し量を計
測するための例えば流量計よりなるスラリ流量検
出手段２０と、この流量が略一定になるように流
量制御を行なう取出流量制御弁２１とがそれぞれ
順次介設されている。 A neutralization chamber 18, which is a feature of the present invention, is connected to the slurry circulation passage 3 via a take-out passage 19 for taking out a portion (a small amount) of the slurry flowing therein. A slurry flow rate detection means 20, such as a flow meter, for measuring the amount taken out, and a take-out flow rate control valve 21, which controls the flow rate so that the flow rate is approximately constant, are provided in sequence.
上記中和チヤンバ１８には例えばPH１以下の概
知濃度の硫酸、塩酸あるいは硝酸などの強酸をこ
れに供給するための酸供給通路２２が接続されて
おり、チヤンバ内のアルカリ剤スラリ液を強酸で
もつて中和すようになつている。この酸供給通路
２２には流量制御弁２３が介設されており、上記
中和チヤンバ１８に設けたPH計２４の検出値に基
づきこれが常時一定値を維持するように流量制御
を行なうようになつている。尚、中和反応完了時
のPH値は３〜５なのでこの間の値を任意に選択し
て設定値とする。 An acid supply passage 22 is connected to the neutralization chamber 18 for supplying a strong acid such as sulfuric acid, hydrochloric acid, or nitric acid with a known concentration of PH1 or less to the neutralization chamber 18. It is becoming more and more neutralizing. A flow rate control valve 23 is interposed in the acid supply passage 22, and the flow rate is controlled so that the value is always maintained at a constant value based on the detected value of the PH meter 24 provided in the neutralization chamber 18. ing. Incidentally, since the PH value at the completion of the neutralization reaction is between 3 and 5, a value between these values is arbitrarily selected and used as the set value.
また、この酸供給通路２２には例えば流量計よ
りなる酸流量検出手段２５が設けられており、こ
れを流れて中和反応に使用される酸量を計測し得
るようになつている。 Further, this acid supply passage 22 is provided with an acid flow rate detection means 25 consisting of, for example, a flowmeter, so that the amount of acid flowing through this and used for the neutralization reaction can be measured.
上記中和チヤンバ１８と吸収塔１との間には中
和されたスラリ液を再度吸収塔１内へ戻すための
導管２６が介設されている。 A conduit 26 is interposed between the neutralization chamber 18 and the absorption tower 1 for returning the neutralized slurry liquid into the absorption tower 1 again.
そして、前記酸流量検出手段２５にて検出され
た酸の流量値及び上記スラリ流量検出手段２０に
て検出された取出スラリ液の流量値はそれぞれ本
考案の特徴とする供給吸収剤制御手段２７へ伝達
され、前記吸収液タンク２へ供給するスラリ量す
なわち吸収剤量を制御するようになつている。具
体的には、この制御手段２７は上記酸流量検出手
段２５からの流量値とスラリ流量検出手段２０か
らの取出スラリ液の流量値とを比較演算処理して
中和チヤンバ１８内すなわちスラリ液循環通路３
内のスラリ液の濃度（吸収剤濃度）を算出する演
算部２８と、このスラリ液濃度の算出値を更に演
算処理して、この算出値がある一定値を維持する
ために吸収液タンク２内へ供給すべき必要吸収剤
量を算出し、この算出した必要吸収剤量をタンク
２へ供給すべく、前記スラリ液供給通路８に介設
したスラリ液制御弁１２の開度調整をして吸収剤
スラリ液量を制御する吸収剤制御部２９とにより
構成されている。スラリ液供給通路８内を移送さ
れる吸収剤量は従来例の通りスラリ流量計１０及
びスラリ濃度計９からの計測値に基づき演算部３
０にて算出され、上記吸収剤制御部２９へ伝達す
るようになつている。そして、この実際の吸収剤
量と上記必要吸収剤量との差分が前述の如くスラ
リ液制御弁１２の開度調整により補正するように
なつている。 The acid flow rate value detected by the acid flow rate detection means 25 and the flow rate value of the extracted slurry liquid detected by the slurry flow rate detection means 20 are respectively sent to the supply absorbent control means 27 which is a feature of the present invention. The amount of slurry, that is, the amount of absorbent supplied to the absorption liquid tank 2 is controlled. Specifically, the control means 27 compares and calculates the flow rate value from the acid flow rate detection means 25 and the flow rate value of the slurry liquid taken out from the slurry flow rate detection means 20, and controls the flow rate within the neutralization chamber 18, that is, the slurry liquid circulation. aisle 3
The calculation unit 28 calculates the concentration of the slurry liquid (absorbent concentration) in the absorbent tank 2, and the calculation unit 28 calculates the concentration of the slurry liquid (absorbent concentration) in the absorbent tank 2. The required amount of absorbent to be supplied to the tank 2 is calculated, and the opening degree of the slurry liquid control valve 12 interposed in the slurry liquid supply passage 8 is adjusted to supply the calculated required amount of absorbent to the tank 2. The absorption agent control section 29 controls the amount of agent slurry. The amount of absorbent transferred through the slurry liquid supply passage 8 is determined by the calculation unit 3 based on the measured values from the slurry flow meter 10 and the slurry concentration meter 9, as in the conventional example.
0 and is transmitted to the absorbent control section 29. The difference between the actual amount of absorbent and the required amount of absorbent is corrected by adjusting the opening of the slurry liquid control valve 12 as described above.
次に以上のように構成された本考案の作用につ
いて説明する。 Next, the operation of the present invention configured as above will be explained.
まず、吸収剤として石灰等を水に溶解すること
により生成した吸収剤スラリ液はスラリ液供給通
路８を介して吸収液タンク２内へ導入され、これ
によりスラリ液循環通路３を介して吸収塔１の上
部へ移送されて噴霧ノズル１７から塔内へ噴霧循
環される。 First, an absorbent slurry liquid generated by dissolving lime or the like in water as an absorbent is introduced into the absorption liquid tank 2 via the slurry liquid supply passage 8, and is then passed through the slurry circulation passage 3 into the absorption tower. It is transferred to the upper part of the tower 1 and circulated as a spray from the spray nozzle 17 into the tower.
そして、この噴霧された吸収液と排ガス入口１
４が導入されたSOx含有排ガス４とが接触して脱
硫処理がなされる。 Then, this sprayed absorption liquid and the exhaust gas inlet 1
4 is brought into contact with the SOx-containing exhaust gas 4 introduced therein, and a desulfurization process is performed.
ここで、循環スラリ液中の吸収剤濃度の測定を
行なうために、スラリ液循環通路３を流れるスラ
リ液の一部は取出通路１９を介してほぼ一定量ず
つ間欠的或いは連続的に中和チヤンバ１８内に取
出され、酸供給通路２２を介してこれに供給され
るH2SO4などの強酸と下記式のごとき中和反応
を生ずる。尚、下記式は吸収剤として炭酸カルシ
ウムを使用した場合の反応式である。 Here, in order to measure the absorbent concentration in the circulating slurry liquid, a portion of the slurry liquid flowing through the slurry liquid circulation passage 3 is sent to the neutralization chamber intermittently or continuously in approximately constant amounts via the take-out passage 19. 18 and supplied thereto via the acid supply passage 22, a neutralization reaction as shown in the following formula occurs with a strong acid such as H 2 SO 4 . Incidentally, the following formula is a reaction formula when calcium carbonate is used as an absorbent.
CaCO3＋H2SO4＋H2O
→CaSO4・2H2O＋CO2↑
スラリ液のPHが５〜７であるのに対し、この反
応のPHは３〜５であり、この間の予め定められた
設定値になるようにPH計２４の検出値に基づき酸
の流量制御弁２３が開度調節され、硫酸の流量が
制御される。この硫酸の使用量はチヤンバ内の微
小スラリ液中の吸収剤量に比例するので、酸流量
検出手段２５で検出された酸流量値と、スラリ液
検出手段２０で検出されたスラリ液量値との商
を、供給吸収剤制御手段２７の一部を構成する演
算部２８にて演算することによりチヤンバ或いは
循環通路３内のスラリ液中の吸収剤濃度（スラリ
液濃度）が求められる。そして、吸収剤制御部２
９にて上記吸収剤濃度検出値を更に演算すること
によりこの算出値がある一定値を維持するために
タンク２内へ供給すべき必要吸収剤量を算出し、
この算出値に基づいてスラリ液供給通路８に介設
したスラリ液制御弁１２の開度調整がなされて吸
収剤スラリ液量が制御される。この際、スラリ流
量計１０及びスラリ濃度計９からの計測値に基づ
き算出されたタンクへの供給吸収剤量が演算部３
０より吸収剤制御部２９へ常時伝達されており、
この実際の供給吸収剤量と上記必要吸収剤量との
差分を上述の如くスラリ液制御弁１２の開度調整
を行なうことにより増加させたり或いは減少させ
たりする。 CaCO 3 +H 2 SO 4 +H 2 O →CaSO 4・2H 2 O + CO 2 ↑ While the pH of the slurry liquid is 5 to 7, the PH of this reaction is 3 to 5, and the predetermined setting during this period is The opening of the acid flow control valve 23 is adjusted based on the detected value of the PH meter 24 so that the flow rate of sulfuric acid is controlled. Since the amount of sulfuric acid used is proportional to the amount of absorbent in the minute slurry liquid in the chamber, the acid flow rate value detected by the acid flow rate detection means 25 and the slurry liquid amount value detected by the slurry liquid detection means 20 are The absorbent concentration in the slurry liquid in the chamber or the circulation passage 3 (slurry liquid concentration) can be determined by calculating the quotient of the quotient in the calculation section 28 that constitutes a part of the supplied absorbent control means 27. Then, the absorbent control section 2
In step 9, the above detected absorbent concentration value is further calculated to calculate the required amount of absorbent to be supplied into the tank 2 in order to maintain this calculated value at a certain constant value,
Based on this calculated value, the opening degree of the slurry liquid control valve 12 provided in the slurry liquid supply passage 8 is adjusted to control the absorbent slurry liquid amount. At this time, the amount of absorbent to be supplied to the tank calculated based on the measured values from the slurry flow meter 10 and the slurry concentration meter 9 is calculated by the calculation unit 3.
0 to the absorbent control unit 29,
The difference between the actual amount of absorbent supplied and the required amount of absorbent is increased or decreased by adjusting the opening degree of the slurry liquid control valve 12 as described above.
これにより、スラリ液循環通路３内を循環して
排ガスと直接接触することになるスラリ液中の吸
収剤濃度を常時ある一定値に維持させることがで
きる。 Thereby, the absorbent concentration in the slurry liquid that circulates in the slurry liquid circulation passage 3 and comes into direct contact with the exhaust gas can be maintained at a certain constant value at all times.
このように、スラリ液循環通路３内のスラリ液
の一部を酸で中和させることによりPH計の指示が
燃料中の不純物のため鈍くなるPH５〜７の領域を
避けてPH計の指示が実際のPH値と一致するPH３〜
５の領域でPH計を使用し、そして、この中和滴定
に必要な硫酸（酸）量等から吸収剤濃度を求める
ようにしたので、従来例と異なり正確な吸収剤濃
度を計測することができる。 In this way, by neutralizing a portion of the slurry liquid in the slurry liquid circulation passage 3 with acid, the PH meter reading can be adjusted to avoid the PH5 to 7 range where the PH meter reading becomes dull due to impurities in the fuel. PH3~ which matches the actual PH value
A PH meter is used in the region 5, and the absorbent concentration is determined from the amount of sulfuric acid (acid) required for this neutralization titration, so unlike conventional methods, it is possible to accurately measure the absorbent concentration. can.
そして、この正確な吸収剤濃度に基づいてタン
ク内に供給すべく吸収剤量を制御するので、前述
の如く排ガスと直接接触することになるスラリ液
循環通路３内の吸収剤濃度を一定値に維持でき、
従つて排ガス量や排ガス中の含有SOx濃度の変動
に対しても安定した脱硫率を維持することがで
き、脱硫率の低下を防止することかできる。な
お、吸収液をスラリ液循環通路３のみから分岐し
なくても吸収液タンク２より微小量、小容量ポン
プで抜き出してもよい。 Since the amount of absorbent to be supplied into the tank is controlled based on this accurate absorbent concentration, the absorbent concentration in the slurry liquid circulation passage 3 that comes into direct contact with the exhaust gas is kept at a constant value as described above. can be maintained,
Therefore, a stable desulfurization rate can be maintained even with variations in the amount of exhaust gas and the concentration of SOx contained in the exhaust gas, and a decrease in the desulfurization rate can be prevented. Note that the absorption liquid does not have to be branched only from the slurry liquid circulation path 3, but may be extracted from the absorption liquid tank 2 in a very small amount using a small capacity pump.
［考案の効果］
以上要するに本考案によれば次のような優れた
効果を発揮することができる。[Effects of the invention] In summary, according to the present invention, the following excellent effects can be achieved.
(1) 排ガスと直接接触することになるスラリ液循
環通路内の吸収剤濃度を正確に検出することが
でき、従つて、この濃度を脱硫に最適な一定値
に常時維持させることができる。(1) It is possible to accurately detect the concentration of the absorbent in the slurry liquid circulation passage that comes into direct contact with the exhaust gas, and therefore it is possible to constantly maintain this concentration at a constant value that is optimal for desulfurization.
(2) 従つて、排ガス量や含有SOx濃度など排ガス
条件が変動しても脱硫率が低下することを防止
して安定した脱硫率を維持することができる。(2) Therefore, even if the exhaust gas conditions such as the amount of exhaust gas and the concentration of SOx contained fluctuate, the desulfurization rate can be prevented from decreasing and a stable desulfurization rate can be maintained.
(3) 従来使用した精度の悪いガス流量計やSO2濃
度計などの計器を使用しないので、前述のごと
き精密な濃度制御ができる。(3) Precise concentration control as mentioned above is possible because conventional instruments such as gas flow meters and SO 2 concentration meters, which have poor accuracy, are not used.
第１図は従来の湿式排煙脱硫装置を示す平面
図、第２図は従来の他の装置を示す概略平面図、
第３図は本考案の好適一実施例を示す平面図であ
る。
尚、図中１は吸収塔、２は吸収液タンク、３は
スラリ液循環通路、４は排ガス、８は配管（スラ
リ液供給通路）、１２はスラリ液制御弁、１８は
中和チヤンバ、２０はスラリ流量検出手段、２２
は酸供給通路、２４はPH計、２５は酸流量検出手
段、２０は供給吸収制御手段である。
Fig. 1 is a plan view showing a conventional wet flue gas desulfurization device, Fig. 2 is a schematic plan view showing another conventional device,
FIG. 3 is a plan view showing a preferred embodiment of the present invention. In the figure, 1 is an absorption tower, 2 is an absorption liquid tank, 3 is a slurry liquid circulation passage, 4 is an exhaust gas, 8 is a pipe (slurry liquid supply passage), 12 is a slurry liquid control valve, 18 is a neutralization chamber, 20 is slurry flow rate detection means, 22
24 is an acid supply passage, 24 is a PH meter, 25 is an acid flow rate detection means, and 20 is a supply and absorption control means.
Claims (1)
にスラリ液制御弁が介設された配管を通して吸収
塔に送り、この吸収塔において排ガスと接触させ
て脱硫処理する湿式排煙脱硫装置において、吸収
塔内に使用する吸収液の１部を取り出すと共にこ
れに酸を加えて中和する中和チヤンバと、上記中
和チヤンバに流入するスラリ液量を検出するスラ
リ液量検出手段と、上記中和チヤンバに流入する
酸の流量を検出する酸流量検出手段と、上記スラ
リ流量検出手段から得られるスラリ液量値と上記
酸流量検出手段から得られる酸流量値とを比較演
算処理して上記吸収塔内に流れるスラリ液濃度を
算出すると共に、この算出値に基づいて上記スラ
リ液制御弁の開度調整をして上記吸収塔内に流れ
る吸収剤スラリ液量を制御する供給吸収剤制御手
段とを備えたことを特徴とする湿式排煙脱硫装
置。 In wet flue gas desulfurization equipment, which uses a slurry liquid absorbent and sends this slurry liquid through a pipe with a slurry liquid control valve in the middle to an absorption tower, where it is brought into contact with flue gas for desulfurization treatment. a neutralization chamber that takes out a part of the absorption liquid used in the column and neutralizes it by adding acid; a slurry liquid amount detection means that detects the amount of slurry liquid flowing into the neutralization chamber; and the neutralization chamber. An acid flow rate detection means for detecting the flow rate of acid flowing into the chamber compares and calculates the slurry liquid volume value obtained from the slurry flow rate detection means and the acid flow rate value obtained from the acid flow rate detection means to detect the absorption tower. supply absorbent control means that calculates the concentration of the slurry liquid flowing into the absorption tower, and adjusts the opening degree of the slurry liquid control valve based on this calculated value to control the amount of absorbent slurry liquid flowing into the absorption tower. A wet flue gas desulfurization device characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP133184U JPS60115528U (en) | 1984-01-11 | 1984-01-11 | Wet flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP133184U JPS60115528U (en) | 1984-01-11 | 1984-01-11 | Wet flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60115528U JPS60115528U (en) | 1985-08-05 |
| JPH0125625Y2 true JPH0125625Y2 (en) | 1989-08-01 |
Family
ID=30473979
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP133184U Granted JPS60115528U (en) | 1984-01-11 | 1984-01-11 | Wet flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60115528U (en) |
-
1984
- 1984-01-11 JP JP133184U patent/JPS60115528U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60115528U (en) | 1985-08-05 |
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