JPS6244734Y2 - - Google Patents
Info
- Publication number
- JPS6244734Y2 JPS6244734Y2 JP7772082U JP7772082U JPS6244734Y2 JP S6244734 Y2 JPS6244734 Y2 JP S6244734Y2 JP 7772082 U JP7772082 U JP 7772082U JP 7772082 U JP7772082 U JP 7772082U JP S6244734 Y2 JPS6244734 Y2 JP S6244734Y2
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- spray header
- absorption
- absorption liquid
- circulation tank
- 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
- 238000010521 absorption reaction Methods 0.000 claims description 65
- 239000007788 liquid Substances 0.000 claims description 49
- 239000007921 spray Substances 0.000 claims description 42
- 239000007789 gas Substances 0.000 claims description 24
- 238000006477 desulfuration reaction Methods 0.000 claims description 21
- 230000023556 desulfurization Effects 0.000 claims description 21
- 230000002745 absorbent Effects 0.000 claims description 7
- 239000002250 absorbent Substances 0.000 claims description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- 239000003546 flue gas Substances 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 10
- 235000019738 Limestone Nutrition 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 5
- 235000010216 calcium carbonate Nutrition 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 239000006028 limestone Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052602 gypsum Inorganic materials 0.000 description 4
- 239000010440 gypsum Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 239000011575 calcium Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
Description
【考案の詳細な説明】
本考案は湿式排煙脱硫装置に係り、特に排ガス
中の亜硫酸ガスの除去性能および経済性を向上す
るに好適なように吸収塔循環液の供給方法を改善
した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, and in particular, a desulfurization device with an improved absorption tower circulating liquid supply method suitable for improving the removal performance and economic efficiency of sulfur dioxide gas in the flue gas. It is related to.
第１図は、従来の湿式脱硫装置の一例として石
灰石・石膏法における吸収塔およびその循環系統
を示すものである。 FIG. 1 shows an absorption tower and its circulation system in a limestone/gypsum method as an example of a conventional wet desulfurization apparatus.
被処理ガスは冷却塔１に導入され、ここで冷却
塔循環液と接触し、ガスの冷却および除じんが行
なわれた後、ミストエリミネータ２を経て吸収塔
３に送られる。該吸収塔３では、その下部に設け
られた循環タンク４に保有されている吸収液が吸
収塔循環ポンプ５および循環ライン６を経て複数
段のスプレヘツダ７に供給され、各スプレヘツダ
に取付けられたスプレノズルより吸収塔３内に噴
霧されて、冷却塔１から送られてきた排ガスと接
触し、排ガス中のSO2の吸収除去が行なわれる。
処理されたガスは、吸収塔１の頂部に設けられた
デミスタ８を経て吸収塔３から排出される。 The gas to be treated is introduced into the cooling tower 1, where it comes into contact with the cooling tower circulating liquid, and after the gas is cooled and dust removed, it is sent to the absorption tower 3 via the mist eliminator 2. In the absorption tower 3, the absorption liquid held in the circulation tank 4 provided at the lower part of the absorption tower 3 is supplied to the multi-stage spray header 7 via the absorption tower circulation pump 5 and the circulation line 6, and the spray nozzle attached to each spray header. The SO 2 is then sprayed into the absorption tower 3 and comes into contact with the exhaust gas sent from the cooling tower 1, where SO 2 in the exhaust gas is absorbed and removed.
The treated gas is discharged from the absorption tower 3 through a demister 8 provided at the top of the absorption tower 1.
循環タンク４内の吸収液は、吸収剤である石灰
石（CaCO3）とSO3の反応生成物である亜硫酸石
灰（CaSO3・1/2H2O）と、その一部が排ガス中
のO2で酸化されて生成する石膏（CaSO4・
2H2O）および未反応の過剰のCaCO3がある割合
で存在するスラリであり、そのPHは通常5.8〜6.0
程度の値に維持される。 The absorption liquid in the circulation tank 4 contains limestone (CaCO 3 ) which is an absorbent and lime sulfite (CaSO 3 1/2H 2 O) which is a reaction product of SO 3 and a part of which is O 2 in the exhaust gas. Gypsum ( CaSO4・
2H2O ) and unreacted excess CaCO3 are present in a certain proportion, and its PH is usually 5.8-6.0
The value is maintained at a certain level.
SO2との反応によつて消費されるCaCO3は、吸
収SO2量に応じてライン９より吸収塔下部循環タ
ンク４に補給される。また、反応生成物はライン
１０より必要量抜き出され、CaSO3・1/2H2Oの
酸化などが行なわれた後、副生石膏として回収さ
れる。 CaCO 3 consumed by the reaction with SO 2 is replenished to the circulation tank 4 at the bottom of the absorption tower via line 9 in accordance with the amount of SO 2 absorbed. Further, a required amount of the reaction product is extracted from the line 10, and after oxidation of CaSO 3 .1/2H 2 O, etc., is recovered as by-product gypsum.
一方、ライン６より供給される循環液量および
スプレヘツダ７の段数は、要求される脱硫率に応
じて適切に選定される。また、循環タンク４に対
しては、上記した吸収液PHを維持するために必要
な容量が決定される。 On the other hand, the amount of circulating fluid supplied from the line 6 and the number of stages of the spray header 7 are appropriately selected depending on the required desulfurization rate. Further, for the circulation tank 4, the capacity required to maintain the above-mentioned absorption liquid PH is determined.
一般に、このような吸収塔の脱硫性能は、入口
SO2濃度、吸収液PH、液ガス比およびスプレヘツ
ダ段数に関係し、次のような特性を有している。 Generally, the desulfurization performance of such an absorption tower depends on the inlet
It is related to the SO 2 concentration, absorption liquid PH, liquid-gas ratio, and number of spray header stages, and has the following characteristics.
(1) 入口SO2濃度が高くなるにつれて、同一の脱
硫率を維持するためには、液ガス比およびスプ
レヘツダ段数を多くする必要があり、循環ポン
プ動力および吸収塔の塔高が増加する。(1) As the inlet SO 2 concentration increases, in order to maintain the same desulfurization rate, it is necessary to increase the liquid-gas ratio and the number of spray header stages, which increases the circulation pump power and the height of the absorption tower.
(2) 吸収液PHを高めるにつれて、脱硫率は上昇す
る。ただし、循環タンクの容量および吸収液中
の未反応CaCO3の割合を増加する必要があ
り、これに伴なつて、塔高および石灰石消費量
ならびに反応生成物抜き出し液中の未反応
CaCO3の中和用硫酸消費量が増加する。(2) As the absorbent pH increases, the desulfurization rate increases. However, it is necessary to increase the capacity of the circulation tank and the proportion of unreacted CaCO 3 in the absorption liquid, and accordingly, the column height and limestone consumption as well as the unreacted CaCO 3 in the reaction product withdrawal liquid must be increased.
Sulfuric acid consumption for neutralizing CaCO3 increases.
(3) 液ガス比を高めるにつれて、脱硫率は上昇す
る。ただし、循環ポンプ動力が増加する。(3) As the liquid-gas ratio increases, the desulfurization rate increases. However, the circulation pump power increases.
(4) 同一液ガス比においても、スプレヘツダ段数
を増すにつれて脱硫率は上昇する。ただし、塔
高が増加する。(4) Even at the same liquid-gas ratio, the desulfurization rate increases as the number of spray header stages increases. However, the tower height will increase.
上記した従来技術の吸収塔において、高SO2濃
度および高効率の処理を行なうためには、装置な
らびに運転費のコストアツプは避けられない。 In order to achieve high SO 2 concentration and high efficiency treatment in the conventional absorption tower described above, an increase in equipment and operating costs is unavoidable.
また、循環タンク４における液の滞留時間を長
くすることにより、未反応CaCO3の割合を少な
くして同じPHを維持することができるが、タンク
容量がますます大きくなり、定期点検などでタン
クを空にするための系外排液槽が過大となり、ス
ペースならびに土建費のアツプにつながる。 In addition, by increasing the residence time of the liquid in the circulation tank 4, it is possible to reduce the proportion of unreacted CaCO 3 and maintain the same pH, but as the tank capacity becomes larger and larger, the tank must be removed during periodic inspections, etc. The external drainage tank for emptying becomes too large, leading to an increase in space and construction costs.
本考案の目的は、上記した従来技術の欠点を改
善し、装置の合理化を図ることができるように吸
収塔循環液の供給方法を改善した湿式脱硫装置を
提供することにある。 An object of the present invention is to provide a wet desulfurization apparatus in which the method for supplying circulating liquid to an absorption tower is improved so that the above-mentioned drawbacks of the prior art can be improved and the apparatus can be rationalized.
本考案は、上記の目的を達成するために、複数
段のスプレヘツダを分割し、上段側にPHの高い吸
収液を、また下段側にPHの低い吸収液を供給する
ようにして吸収塔の脱硫性能の向上を図つたもの
で、これに対応させて、吸収塔下部の循環タンク
と連結して補助循環タンクを設置し、ここに
CaCO3を補給して循環液のPHを高め、上段側ス
プレヘツダに供給するようにしたものである。 In order to achieve the above objective, the present invention divides the multi-stage spray header and supplies absorbent liquid with high PH to the upper stage and absorbent liquid with low PH to the lower stage to desulfurize the absorption tower. The aim was to improve performance, and in response to this, an auxiliary circulation tank was installed connected to the circulation tank at the bottom of the absorption tower.
CaCO 3 is replenished to increase the pH of the circulating fluid, which is then supplied to the upper spray header.
以下に本考案を実施例により詳細に説明する。 The present invention will be explained in detail with reference to examples below.
第２図は本考案の一実施例を示す吸収塔循環系
統であり、第１図と同一の箇所は同一符号で示
す。 FIG. 2 shows an absorption tower circulation system showing an embodiment of the present invention, and the same parts as in FIG. 1 are designated by the same symbols.
被処理ガスは、冷却塔１に導入され、冷却およ
び除じんが行なわれた後、ミストエリミネータ２
を経て吸収塔３の下部よりその内部に入り、上段
側スプレヘツダ１７および下段側スプレヘツダ１
３のノズルより噴霧された吸収液と接触し、排ガ
ス中のSO2が吸収除去された後、デミスタ８を経
て吸収塔３の頂部より排出される。 The gas to be treated is introduced into the cooling tower 1, where it is cooled and dust removed, and then passed through the mist eliminator 2.
The upper spray header 17 and the lower spray header 1 enter the interior of the absorption tower 3 from the lower part through the
After coming into contact with the absorption liquid sprayed from the nozzle 3 and absorbing and removing SO 2 in the exhaust gas, it is discharged from the top of the absorption tower 3 via the demister 8.
一方、吸収塔循環液は、吸収塔下部循環タンク
４より下段側スプレヘツダ用循環ポンプ１１およ
び循環ライン１２を経て下段側スプレヘツダ１３
に供給される。また、循環液の一部は、連絡管１
８を経て補助循環タンク１４に流入し、上段側ス
プレヘツダ用循環ポンプ１５および循環ライン１
６を経て上段側スプレヘツダ１７に供給される。 On the other hand, the absorption tower circulating liquid is passed from the absorption tower lower circulation tank 4 to the lower spray header circulation pump 11 and the circulation line 12 to the lower spray header 13.
is supplied to In addition, some of the circulating fluid is
8 to the auxiliary circulation tank 14, and the circulation pump 15 for the upper spray header and the circulation line 1.
6 and is supplied to the upper spray header 17.
補助循環タンク１４には、吸収SO2量に応じた
CaCO3スラリがライン９より供給される。ま
た、吸収塔３で除去されたSO2は前記した反応生
成物となり、ライン１０より必要量抜き出され
る。 In the auxiliary circulation tank 14, there is a
CaCO 3 slurry is supplied from line 9. Further, the SO 2 removed in the absorption tower 3 becomes the above-mentioned reaction product, and is extracted in a required amount from the line 10.
循環タンク４および１４における吸収液のPH値
に関しては、次のような実験式が得られている。 Regarding the pH value of the absorption liquid in the circulation tanks 4 and 14, the following empirical formula has been obtained.
PH＝−log〔Ｈ+〕 ……(1)
〔Ｈ+〕＝Ｋ・Ｒ／Ｖ・Ｃ１／Ｃ２ ……(2)
ここで、
〔Ｈ+〕：水素イオン濃度（ｇイオン／）
Ｋ：係数
Ｒ：吸収SO2量（kmol／ｈ）
Ｖ：タンクの保有液量（）
C1：〔Ca2+〕〓
C2：〔CaCO3〕〓
〔Ca2+〕：吸収液中のカルシウムイオン
濃度（ｇイオン／）
〔CaCO3〕：吸収液中の炭酸カルシウム
濃度（wt％）
α，β：定数
Ｒ＝ガス量×SO2濃度×脱硫率 ……(3)
なお、通常行なわれる操作条件の下では、
〔Ca2+〕は0.015gイオン／程度でほぼ一定であ
るため、C1はほぼ一定の値となる。 PH=-log [H + ] ...(1) [H + ]=K・R/V・C 1 /C 2 ...(2) Here, [H + ]: Hydrogen ion concentration (g ions/) K: coefficient R: amount of SO2 absorbed (kmol/h) V: amount of liquid held in the tank () C 1 : [Ca 2+ ] C 2 : [CaCO 3 ] Calcium ion concentration (g ions/) [CaCO 3 ]: Calcium carbonate concentration in absorption liquid (wt%) α, β: Constant R = gas amount x SO 2 concentration x desulfurization rate ... (3) Note that this is usually performed Under operating conditions,
[Ca 2+ ] is approximately constant at about 0.015 g ion/so that C 1 is approximately constant.
一方、〔CaCO3〕は、吸収液中に存在する未反
応CaCO3の割合に関係し、(2)式の他の条件が一
定であれば、この割合を多くするにつれてPHが漸
次上昇する。もし、第１図のように、吸収塔下部
循環タンク４のみの場合において、このような操
作を行なうとすれば、ライン１０よりの抜き出し
液中の未反応CaCO3量が多くなり、これを中和
するための硫酸消費量が増加することになり、運
転費のアツプを来たすので望ましくない。このた
め、通常、循環タンク４に補給されるCaCO3
は、吸収SO2の当量比に対し５〜10％程度の過剰
範囲に抑えられている。すなわち、通常の操作条
件の下では、(2)式のC2によつてPHを高める効果
は小さい。 On the other hand, [CaCO 3 ] is related to the proportion of unreacted CaCO 3 present in the absorption liquid, and if the other conditions in equation (2) are constant, the PH gradually increases as this proportion increases. If such an operation is carried out in the case of only the circulation tank 4 at the bottom of the absorption tower as shown in Fig. 1, the amount of unreacted CaCO 3 in the liquid extracted from the line 10 will increase, and this will have to be This is not desirable because the amount of sulfuric acid consumed for oxidation increases, which increases operating costs. For this reason, CaCO 3 that is normally replenished into the circulation tank 4
is suppressed to an excess of about 5 to 10% relative to the equivalent ratio of absorbed SO 2 . That is, under normal operating conditions, the effect of increasing the PH by C 2 in formula (2) is small.
吸収塔循環液のPHは、PHと脱硫性能の関係なら
びにPHとCaCO3過剰率など、総合的な見地よ
り、通常、5.8〜6.0程度で運転される。 The PH of the absorption tower circulating liquid is normally operated at about 5.8 to 6.0 from a comprehensive standpoint, such as the relationship between PH and desulfurization performance, and the PH and CaCO 3 excess rate.
このようなPH値を維持するためには、(2)式にお
いて、ＲとＶはほぼ比例関係にあり、(3)式に示す
ように、SO2濃度あるいは脱硫率が高くなるにつ
れてＲの値が大となるため、循環タンク４の保有
液量Ｖも大きくしなければならない。 In order to maintain such a PH value, in equation (2), R and V have a nearly proportional relationship, and as shown in equation (3), the value of R increases as the SO 2 concentration or desulfurization rate increases. Since this increases, the amount of liquid V held in the circulation tank 4 must also be increased.
一方、第２図のように、吸収塔下部循環タンク
４に補給循環タンク１４を付設すれば、補助循環
タンク１４においては、次のような関係よりPHを
高める効果を有している。すなわち、吸収塔下部
循環タンク４において、PHが5.8〜6.0程度に維持
された吸収液のうち、上段側スプレヘツダ１７に
供給される液量だけ、連絡管１８を経て補助循環
タンク１４に流入する。仮りに、上段側スプレヘ
ツダ１７と下段側スプレヘツダ１３に供給する液
量が同じであるとした場合、(2)式のＲの1/2が補
助循環タンク１４に流入することになる。また、
該タンク１４には。Ｒ×（1.05〜1.1）に相当する
当量のCaCO3がライン９より供給されるため、
該タンク内の未反応CaCO3の割合が増加する。
したがつて、(2)式の関係より、該タンク１４のPH
は高め易く、かつ、必要なPH上昇分に応じて該タ
ンク１４の保有液量Ｖを適当に選定すればよいこ
とになる。試算例によれば、該タンク１４の保有
液量を吸収塔下部循環タンク４の1/2にしてもPH
は0.4程度上昇させることができる。 On the other hand, if a make-up circulation tank 14 is attached to the absorption tower lower circulation tank 4 as shown in Fig. 2, the auxiliary circulation tank 14 has the effect of raising the pH due to the following relationship. That is, of the absorption liquid in the absorption tower lower circulation tank 4, whose pH is maintained at about 5.8 to 6.0, only the amount of liquid supplied to the upper spray header 17 flows into the auxiliary circulation tank 14 via the connecting pipe 18. If the amount of liquid supplied to the upper spray header 17 and the lower spray header 13 is the same, 1/2 of R in equation (2) flows into the auxiliary circulation tank 14. Also,
The tank 14 is supplied with an amount of CaCO3 equivalent to R x (1.05 to 1.1) through the line 9,
The proportion of unreacted CaCO3 in the tank increases.
Therefore, from the relationship of equation (2), the pH of the tank 14 is
According to a trial calculation example, even if the amount of liquid held in the tank 14 is half that of the absorption tower lower circulation tank 4, the pH
can be increased by about 0.4.
したがつて、この場合を例にとれば、上段側ス
プレヘツダ１７にはPHが6.2〜6.4程度に高められ
た吸収液を供給することができる。これは、吸収
塔３のスプレ部でのSO2濃度が下段側から上段側
になるにつれて低下するため、稀薄なSO2濃度の
部分にPHの高い吸収液を噴霧することを意味する
ものであり、SO2の吸収能を向上させる効果があ
る。すなわち、スプレノズルより噴霧された液滴
によるSO2の吸収は、液滴の気液界面を介して物
質移動が行なわれるものであり、ヘンリーの法則
に従つてSO2の液中への溶解は、ガス側と液側の
SO2分圧差に関係し、吸収液のPHが高いと液中の
SO2分圧が低下するため、ガス中のSO2濃度が低
い（分圧が低い）部分においても物質移動が促進
されるためである。 Therefore, taking this case as an example, the upper spray header 17 can be supplied with an absorption liquid whose pH has been increased to about 6.2 to 6.4. This means that the SO 2 concentration in the spray section of the absorption tower 3 decreases from the lower stage side to the upper stage side, so the absorption liquid with a high PH is sprayed into the area with a dilute SO 2 concentration. , has the effect of improving SO 2 absorption capacity. In other words, the absorption of SO 2 by the droplets sprayed from the spray nozzle is due to mass transfer via the gas-liquid interface of the droplets, and according to Henry's law, the dissolution of SO 2 into the liquid is as follows: gas side and liquid side
SO 2Related to the partial pressure difference, if the pH of the absorption liquid is high, the
This is because the SO 2 partial pressure decreases, so mass transfer is promoted even in areas where the SO 2 concentration in the gas is low (low partial pressure).
第２図において、補助循環タンクを複数、直列
に連結して吸収液のPHを順次高め、それぞれのタ
ンクよりスプレヘツダの上、中、下段の如く供給
するようにすることも、本考案の他の実施例の一
つである。このようにすることによつて、下段ス
プレヘツダ側から上段スプレヘツダ側に向つて、
すなわち、SO2濃度の高い方から低い方に向つて
吸収塔内に噴霧される吸収液のPHを次第に上昇さ
せ、総合効率を高めることができる。また、循環
タンク１基当りの保有液量を少なくすることがで
き、定期検査などでタンクを空にする場合、順次
切替えて行くことによつて大きな系外排水槽を必
要としない効果を有する。 In FIG. 2, it is also possible to connect a plurality of auxiliary circulation tanks in series to increase the pH of the absorption liquid in sequence, and to supply the liquid from each tank to the upper, middle, and lower stages of the spray header. This is one example. By doing this, from the lower spray header side to the upper spray header side,
That is, the pH of the absorption liquid sprayed into the absorption tower can be gradually increased from the higher SO 2 concentration to the lower SO 2 concentration, thereby increasing the overall efficiency. In addition, the amount of liquid held per circulation tank can be reduced, and when the tanks are emptied during periodic inspections, by sequentially switching over, a large external drainage tank is not required.
第３図は、湿式脱硫装置において、液ガス比、
吸収液のPH、スプレ段数と脱硫率の関係を示す一
例であるが、従来の方法によれば、各スプレヘツ
ダに同一PHの吸収液を供給しているため、図中の
Ａ点に相当するのに対し、本考案の方法によれ
ば、各スプレヘツダからの吸収液のPH平均値を上
昇させることができ、次のような効果がある。 Figure 3 shows the liquid-gas ratio,
This is an example showing the relationship between the pH of the absorption liquid, the number of spray stages, and the desulfurization rate.According to the conventional method, the absorption liquid with the same pH is supplied to each spray header, so the point corresponding to point A in the figure On the other hand, according to the method of the present invention, it is possible to increase the average pH value of the absorption liquid from each spray header, and the following effects are achieved.
(1) 同一の液ガス比とすれば、脱硫率はＢ点まで
上昇する。(1) If the liquid-gas ratio is the same, the desulfurization rate increases to point B.
(2) 同一の脱硫率で比較すれば、液ガス比はＣ点
まで減少する。すなわち、循環ポンプの動力を
減じることができ、この割合に比例して消費電
力の低減が図れる。また、スプレ段数も低減で
きる。(2) If compared at the same desulfurization rate, the liquid-gas ratio decreases to point C. That is, the power of the circulation pump can be reduced, and the power consumption can be reduced in proportion to this ratio. Moreover, the number of spray stages can also be reduced.
(3) さらに、高効率になるにつれて、従来技術で
はスプレ段数および液ガス比の増加が必要とな
るが、本考案では液ガス比をわずか増加させる
のみで対処することができ、装置の建設費およ
び運転費を低減することができる。(3) Furthermore, as efficiency increases, conventional technology requires an increase in the number of spray stages and the liquid-gas ratio, but with the present invention, this can be achieved by only slightly increasing the liquid-gas ratio, reducing equipment construction costs. and operating costs can be reduced.
第１図は、従来の湿式脱硫装置の一例としての
石灰石・石膏法における吸収塔およびその循環系
統を示す図、第２図は、本考案の一実施例を示す
吸収塔循環系統説明図、第３図は、湿式脱硫装置
において、液ガス比、吸収液のPH、スプレ段数と
脱硫率の関係の一例を示す図である。
図において、１……冷却塔、２……ミストエリ
ミネータ、３……吸収塔、４……吸収塔下部循環
タンク、５……吸収塔循環ポンプ、６……循環ラ
イン、７……スプレヘツダ、８……デミスタ、９
……石灰石スラリ供給ライン、１０……吸収液抜
き出しライン、１１……下段側スプレヘツダ用循
環ポンプ、１２……下段側スプレヘツダ用循環ラ
イン、１３……下段側スプレヘツダ、１４……補
助循環タンク、１５……上段側スプレヘツダ用循
環ポンプ、１６……上段側スプレヘツダ用循環ラ
イン、１７……上段側スプレヘツダ、１８……連
絡管。
Fig. 1 is a diagram showing an absorption tower and its circulation system in the limestone/gypsum method as an example of a conventional wet desulfurization equipment, and Fig. 2 is an explanatory diagram of the absorption tower circulation system showing an embodiment of the present invention. FIG. 3 is a diagram showing an example of the relationship between the liquid-gas ratio, the pH of the absorption liquid, the number of spray stages, and the desulfurization rate in a wet desulfurization apparatus. In the figure, 1...Cooling tower, 2...Mist eliminator, 3...Absorption tower, 4...Absorption tower lower circulation tank, 5...Absorption tower circulation pump, 6...Circulation line, 7...Spray header, 8 ...Demister, 9
... Limestone slurry supply line, 10 ... Absorbent extraction line, 11 ... Circulation pump for lower spray header, 12 ... Circulation line for lower spray header, 13 ... Lower spray header, 14 ... Auxiliary circulation tank, 15 ...Circulation pump for upper spray header, 16...Circulation line for upper spray header, 17... Upper spray header, 18... Communication pipe.
Claims (1)
吸収液を噴霧する複数段のスプレヘツダを内部に
設けた吸収塔と該吸収塔の下部に設けた吸収液循
環タンクとを備えた型の湿式排煙脱硫装置におい
て、前記吸収液循環タンクに直列に連結した一つ
以上の補助吸収液循環タンクを付設すると共に該
補助吸収液循環タンク内の吸収液のPHを順次前記
吸収液循環タンク内の吸収液のPHより高くし、か
つ、前記複数段のスプレヘツダを前記循環タンク
の数に対応させて上下に分割し、PHの高い吸収液
を前記スプレヘツダの上段側に、PHの低い吸収液
を前記スプレヘツダの下段側に前記循環タンクか
ら供給するようにしたことを特徴とする湿式排煙
脱硫装置。 A type of wet smoke flue gas equipped with an absorption tower equipped with a multi-stage spray header inside which sprays an absorption liquid for absorbing and removing sulfur dioxide gas from exhaust gas, and an absorption liquid circulation tank installed at the bottom of the absorption tower. In the desulfurization equipment, one or more auxiliary absorption liquid circulation tanks connected in series to the absorption liquid circulation tank are attached, and the pH of the absorption liquid in the auxiliary absorption liquid circulation tank is sequentially adjusted to the absorption liquid in the absorption liquid circulation tank. and the multi-stage spray header is divided into upper and lower parts corresponding to the number of circulation tanks, and the absorbent liquid with a high pH is placed in the upper side of the spray header, and the absorbent liquid with a low pH is placed in the upper side of the spray header. A wet flue gas desulfurization device characterized in that the lower stage side is supplied from the circulation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7772082U JPS58183231U (en) | 1982-05-28 | 1982-05-28 | Wet flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7772082U JPS58183231U (en) | 1982-05-28 | 1982-05-28 | Wet flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58183231U JPS58183231U (en) | 1983-12-06 |
| JPS6244734Y2 true JPS6244734Y2 (en) | 1987-11-27 |
Family
ID=30086971
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7772082U Granted JPS58183231U (en) | 1982-05-28 | 1982-05-28 | Wet flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58183231U (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60119919U (en) * | 1984-01-19 | 1985-08-13 | バブコツク日立株式会社 | Wet flue gas desulfurization equipment |
| JP2011194296A (en) * | 2010-03-18 | 2011-10-06 | Ihi Corp | Flue gas desulfurization equipment |
-
1982
- 1982-05-28 JP JP7772082U patent/JPS58183231U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58183231U (en) | 1983-12-06 |
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