JPH0147213B2 - - Google Patents
Info
- Publication number
- JPH0147213B2 JPH0147213B2 JP56059264A JP5926481A JPH0147213B2 JP H0147213 B2 JPH0147213 B2 JP H0147213B2 JP 56059264 A JP56059264 A JP 56059264A JP 5926481 A JP5926481 A JP 5926481A JP H0147213 B2 JPH0147213 B2 JP H0147213B2
- Authority
- JP
- Japan
- Prior art keywords
- adsorbent
- amount
- exhaust gas
- moving bed
- extracted
- 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
- 239000003463 adsorbent Substances 0.000 claims description 35
- 238000000034 method Methods 0.000 claims description 14
- 238000001179 sorption measurement Methods 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 5
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 claims 2
- 230000003647 oxidation Effects 0.000 claims 1
- 238000007254 oxidation reaction Methods 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 description 11
- 230000023556 desulfurization Effects 0.000 description 11
- 239000000446 fuel Substances 0.000 description 7
- 239000003208 petroleum Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 230000006378 damage Effects 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Description
【発明の詳細な説明】
この発明はボイラ等の燃焼装置から排出される
排ガス中の硫黄酸化物を吸着剤の移動層により除
去する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for removing sulfur oxides from exhaust gas discharged from a combustion device such as a boiler using a moving bed of adsorbent.
最近の燃料事情の変化に伴い、火力発電所用大
型ボイラをはじめとする各種燃焼装置においては
石油系燃料から石炭系燃料へと転換し、燃料の安
定供給、燃料費の低減を図る傾向にある。しかし
石炭は石油に比較して灰分、硫黄分の含有量がき
わめて多く、炭種によつても相違するが、灰分は
石油の200〜400倍、硫黄分は約２倍から６倍に達
し、しかも発熱量は低下する。このため石炭系の
燃料を使用する場合には石油系の燃料を使用する
場合に比較して大容量の集塵装置、脱硫装置が必
要となり装置の大型化、複雑化は避けられない。 With recent changes in the fuel situation, there is a trend to switch from petroleum-based fuels to coal-based fuels in various combustion devices, including large boilers for thermal power plants, in order to achieve a stable supply of fuel and reduce fuel costs. However, coal has extremely high ash and sulfur content compared to petroleum, and although it varies depending on the type of coal, the ash content is 200 to 400 times that of petroleum, and the sulfur content is about 2 to 6 times that of petroleum. Moreover, the amount of heat generated decreases. For this reason, when coal-based fuel is used, a larger capacity dust collector and desulfurization equipment are required than when petroleum-based fuel is used, making the equipment unavoidably larger and more complex.
排ガスの脱硫方法としては湿式と乾式とがある
が、このうち湿式脱硫は吸着設備を小型に形成で
きる反面、処理後の排ガス温度が低下して白煙を
発生するため排ガスの再加熱が必要で不経済であ
り、さらに脱硫処理により生じた排水によつて二
次公害を生ずる虞れもある。これに対して乾式脱
硫は装置が大型化する反面、排ガスの再加熱、排
水処理等の設備が不要であり経済的である。 There are two methods for desulfurizing exhaust gas: wet and dry.Of these, wet desulfurization allows the adsorption equipment to be made smaller, but on the other hand, the exhaust gas temperature drops after treatment and white smoke is generated, so the exhaust gas must be reheated. This is uneconomical, and there is also the possibility that secondary pollution may be caused by the wastewater generated by the desulfurization process. On the other hand, although dry desulfurization requires larger equipment, it is more economical because it does not require equipment for reheating exhaust gas or treating waste water.
乾式脱硫の一方法として吸着剤の移動層を形成
し、この移動層により硫黄酸化物（以下SOxと称
する）を吸着除去する方法があるが、この方法は
脱硫効率が高い反面次の如き問題がある。 One dry desulfurization method is to form a moving bed of adsorbent and use this moving bed to adsorb and remove sulfur oxides (hereinafter referred to as SO x ), but although this method has high desulfurization efficiency, it has the following problems. There is.
先ず、吸着剤は移動層中で物理的な破壊を受け
易く、移動層から排出される時点で相当量の吸着
剤が破壊され使用不能となる。このことは吸着剤
として通常高価な活性炭が使用されるため大きな
経済的損失となる。 First, the adsorbent is susceptible to physical destruction in the moving bed, and a considerable amount of the adsorbent is destroyed and becomes unusable upon being discharged from the moving bed. This results in a large economic loss since expensive activated carbon is usually used as the adsorbent.
次に吸着剤の移動速度は移動層を通過する排ガ
ス流量、排ガス中のSOx濃度、吸着剤の吸着能力
等を考慮して決定されるべきであるが、従来は必
ずしもこのことが十分に考慮されておらず、不必
要に速い速度で移動させて大量の吸着剤を破壊し
たり、反対に移動速度が遅過ぎて移動層中で吸着
状態が飽和状態となつて吸着効率を低下させる等
の問題があつた。 Next, the moving speed of the adsorbent should be determined by taking into account the flow rate of the exhaust gas passing through the moving bed, the SO x concentration in the exhaust gas, the adsorption capacity of the adsorbent, etc., but in the past, this has not always been taken into account sufficiently. If not, the adsorbent may be moved at an unnecessarily high speed, destroying a large amount of adsorbent, or, conversely, the moving speed may be too slow, causing the adsorption state to reach a saturated state in the moving bed and reducing adsorption efficiency. There was a problem.
さらに排ガス中のダストによる移動層の詰りも
重大な問題であり、ダストの詰りによる排ガス通
過量の低下は直ちに脱硫効率の低下につながるこ
とになる。 Furthermore, clogging of the moving bed due to dust in the exhaust gas is also a serious problem, and a decrease in the amount of exhaust gas passing due to the dust clogging immediately leads to a decrease in desulfurization efficiency.
この発明の目的は上述した問題点を除去し、吸
着剤の破壊を最少限に止め、しかも高い脱硫効率
を得ることのできる方法を提供することにある。 An object of the present invention is to provide a method which can eliminate the above-mentioned problems, minimize damage to the adsorbent, and obtain high desulfurization efficiency.
要するにこの発明は移動層の入口と出口の排ガ
スの差圧、排ガス中のSOx濃度、排ガス流入量等
を考慮して移動層からの吸着剤の抜き出し量を定
めることを特徴とする方法である。 In short, this invention is a method characterized by determining the amount of adsorbent extracted from the moving bed in consideration of the differential pressure between the exhaust gas at the inlet and outlet of the moving bed, the SOx concentration in the exhaust gas, the amount of exhaust gas flowing in, etc. .
以下この発明の一実施例を図面を参考に説明す
る。 An embodiment of the present invention will be described below with reference to the drawings.
第１図および第２図において、符号１は吸着塔
を示し、吸着塔１内には活性炭等から成る吸着剤
２の移動層が形成され、吸着塔１内を通過した吸
着剤２は下部のバルブ３を経てベルトコンベヤ４
により系外に移送され吸着物の脱離処理が施され
再使用される。なおバルブ３は吸着剤の破壊を少
くするためロータリバルブとしておくとよい。 In FIG. 1 and FIG. 2, reference numeral 1 indicates an adsorption tower, and a moving bed of adsorbent 2 made of activated carbon or the like is formed in the adsorption tower 1. Belt conveyor 4 via valve 3
The adsorbent is transferred to the outside of the system, subjected to desorption treatment, and reused. Note that the valve 3 is preferably a rotary valve in order to reduce damage to the adsorbent.
吸着塔１の排ガス入口側には排ガス流量を検知
する流量検知器５、SOxの殆んどを占めるSO2の
濃度を検知するSO2検知器６、圧力検知器７が、
また出口側には圧力検知器７ａ、SO2検知器６ａ
が各々配置してある。これら各検知器は記憶と指
令信号を発する制御箱８に回路接続しこれらの検
知信号を比較演算しバルブ３の開度およびモータ
９の調節によりベルトコンベヤ４の排出速度を適
正値に保持し、吸着塔１を通過する排ガスＧの脱
硫を良好な状態に保持する。 On the exhaust gas inlet side of the adsorption tower 1, there are a flow rate detector 5 for detecting the exhaust gas flow rate, an SO 2 detector 6 for detecting the concentration of SO 2 that accounts for most of the SO x , and a pressure detector 7.
In addition, there is a pressure detector 7a and an SO 2 detector 6a on the outlet side.
are arranged respectively. Each of these detectors is circuit-connected to a control box 8 that emits memory and command signals, and these detection signals are compared and calculated, and the discharge speed of the belt conveyor 4 is maintained at an appropriate value by adjusting the opening of the valve 3 and the motor 9. The desulfurization of the exhaust gas G passing through the adsorption tower 1 is maintained in a good state.
第２図は以上の操作を具体的に示すものであ
る。 FIG. 2 specifically shows the above operation.
先ずSO2検知器６および流量検知器５により検
知した吸着塔に流入する排ガスのSO2濃度１０お
よびガス流量１１により単位時間当りに処理すべ
きSO2の量を算定し、あらかじめ計算しておいた
吸着剤の単位時間当りの吸着剤X′（符号１２で示
す）により符号１３で示む吸着剤の抜き出し量の
基準値Ｘを定める。一方移動層にはダストが付着
して詰りが生ずるため、圧力検知器７および７ａ
で検知した差圧を移動層のドラフトロスとし、か
つこれを補正値１４とする。一方SO2検知器６ａ
により検知した出口排ガス（処理ガス）のSO2濃
度を補正値１５とし、両補正値１４、および１５
により前記基準値Ｘを補正して最終的に符号１６
で示す適正抜き出し量Ｋを定める。この適正移動
量Ｋに基づいて符号１７で示すバルブの開度OP
を定め、最終的にバルブ３の開度を調節する。 First, the amount of SO 2 to be treated per unit time is calculated from the SO 2 concentration 10 of the exhaust gas flowing into the adsorption tower detected by the SO 2 detector 6 and the flow rate detector 5 and the gas flow rate 11, and the amount of SO 2 to be treated per unit time is calculated in advance. A reference value X for the amount of adsorbent extracted, indicated by reference numeral 13, is determined by the amount of adsorbent X' (indicated by reference numeral 12) per unit time. On the other hand, since dust adheres to the moving layer and causes clogging, pressure detectors 7 and 7a
The differential pressure detected in is taken as the draft loss of the moving layer, and this is taken as the correction value 14. On the other hand, SO 2 detector 6a
The SO 2 concentration of the outlet exhaust gas (processed gas) detected by is set as the correction value 15, and both correction values 14 and 15
The reference value X is corrected by
Determine the appropriate extraction amount K shown by . Based on this appropriate movement amount K, the valve opening degree OP indicated by reference numeral 17
is determined, and the opening degree of the valve 3 is finally adjusted.
この発明を実施することにより吸着剤の吸着能
力と通過ガスのSOx濃度に対応して吸着剤の移動
速度が定められるので脱硫効率を高めることがで
きる。 By carrying out this invention, the movement speed of the adsorbent is determined in accordance with the adsorption capacity of the adsorbent and the SO x concentration of the passing gas, so that the desulfurization efficiency can be increased.
また不必要に速い速度で吸着剤を移動させるこ
とがないので吸着剤の破損を最少限に止めること
ができる。 Furthermore, since the adsorbent is not moved at an unnecessarily high speed, damage to the adsorbent can be minimized.
第１図はこの発明に係る方法を実施するための
脱硫塔の系統図、第２図はこの発明に係る方法の
演算状態を示す系統図である。
１…吸着塔、２……吸着剤、３……バルブ、１
１……排ガス流量、１３……吸着剤抜き出し量の
基準値、１４，１５……補正値、１６……吸着剤
抜き出し量の適正値。
FIG. 1 is a system diagram of a desulfurization tower for implementing the method according to the present invention, and FIG. 2 is a system diagram showing the calculation state of the method according to the present invention. 1...Adsorption tower, 2...Adsorbent, 3...Valve, 1
1...Exhaust gas flow rate, 13...Reference value of adsorbent extraction amount, 14, 15...Correction value, 16...Appropriate value of adsorbent extraction amount.
Claims (1)
着剤で除去する方法において、移動層入口と出口
間の排ガス圧力差と、移動層入口と出口の排ガス
中の硫黄酸化物濃度と、移動層入口ガス流量とに
より吸着剤抜き出し量を定め、この抜き出し量に
基づいて吸着塔からの吸着剤の抜き出し量を制御
することを特徴とする吸着剤抜き出し量制御方
法。 ２ 移動層入口の排ガス中の硫黄酸化物濃度と排
ガス流量により吸着剤抜き出し量の基準値を定
め、移動層出口の排ガス中の硫黄酸化物濃度と、
移動層入口と出口間の排ガス圧力差とを補正値と
して前記基準値を補正して適正抜き出し量を定め
ることを特徴とする特許請求の範囲第１項記載の
吸着剤抜き出し量制御方法。 ３ 吸着剤の抜き出しをロータリバルブにより行
うことを特徴とする特許請求の範囲第１項または
第２項記載の吸着剤抜き出し量制御方法。 ４ 吸着剤抜き出しをバルブとベルトコンベヤの
組み合せにより行なうことを特徴とする特許請求
の範囲第１項または第２項記載の吸着剤抜き出し
量制御方法。[Claims] 1. In a method for removing sulfur oxides in exhaust gas using an adsorbent forming a moving bed, the exhaust gas pressure difference between the inlet and outlet of the moving bed and the sulfur oxidation in the exhaust gas at the inlet and outlet of the moving bed are A method for controlling the amount of adsorbent extracted, characterized in that the amount of adsorbent extracted is determined based on the concentration of the adsorbent and the gas flow rate at the inlet of the moving bed, and the amount of adsorbent extracted from the adsorption tower is controlled based on the amount of extracted adsorbent. 2. Determine the standard value for the amount of adsorbent extracted based on the sulfur oxide concentration in the exhaust gas at the moving bed inlet and the exhaust gas flow rate, and determine the sulfur oxide concentration in the exhaust gas at the moving bed outlet,
2. The adsorbent extraction amount control method according to claim 1, wherein the appropriate extraction amount is determined by correcting the reference value using the exhaust gas pressure difference between the inlet and outlet of the moving bed as a correction value. 3. A method for controlling the amount of adsorbent withdrawn according to claim 1 or 2, characterized in that the adsorbent is withdrawn by a rotary valve. 4. A method for controlling the amount of adsorbent extracted according to claim 1 or 2, characterized in that the adsorbent is extracted by a combination of a valve and a belt conveyor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56059264A JPS57174125A (en) | 1981-04-21 | 1981-04-21 | Controlling method for removal rate of adsorbent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56059264A JPS57174125A (en) | 1981-04-21 | 1981-04-21 | Controlling method for removal rate of adsorbent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57174125A JPS57174125A (en) | 1982-10-26 |
| JPH0147213B2 true JPH0147213B2 (en) | 1989-10-12 |
Family
ID=13108332
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56059264A Granted JPS57174125A (en) | 1981-04-21 | 1981-04-21 | Controlling method for removal rate of adsorbent |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS57174125A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4604532B2 (en) * | 2004-03-24 | 2011-01-05 | Ｊｆｅスチール株式会社 | Exhaust gas treatment method and treatment apparatus |
| JP4634763B2 (en) * | 2004-09-02 | 2011-02-16 | 新日本製鐵株式会社 | Method of transporting exhaust gas treatment agent to exhaust gas treatment tank |
| JP4735353B2 (en) * | 2005-08-25 | 2011-07-27 | Ｊｆｅスチール株式会社 | Exhaust gas treatment method |
-
1981
- 1981-04-21 JP JP56059264A patent/JPS57174125A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57174125A (en) | 1982-10-26 |
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