JP2017176922A - Desulfurizing agent addition control method - Google Patents
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 24
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims abstract description 66
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 62
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 51
- 230000023556 desulfurization Effects 0.000 claims abstract description 51
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 5
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 claims description 64
- 238000012937 correction Methods 0.000 claims description 4
- 229910052815 sulfur oxide Inorganic materials 0.000 abstract description 7
- 239000007789 gas Substances 0.000 description 24
- 239000000428 dust Substances 0.000 description 13
- 239000010802 sludge Substances 0.000 description 8
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 7
- 229910052731 fluorine Inorganic materials 0.000 description 7
- 239000011737 fluorine Substances 0.000 description 7
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 159000000007 calcium salts Chemical class 0.000 description 6
- 238000002844 melting Methods 0.000 description 6
- 230000008018 melting Effects 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 235000011148 calcium chloride Nutrition 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- WBHQBSYUUJJSRZ-UHFFFAOYSA-M sodium bisulfate Chemical compound [Na+].OS([O-])(=O)=O WBHQBSYUUJJSRZ-UHFFFAOYSA-M 0.000 description 1
- 229910000342 sodium bisulfate Inorganic materials 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
本発明は、脱硫剤添加制御方法に関する。 The present invention relates to a desulfurization agent addition control method.
金属類を含むスラッジなどに適切な溶剤を加えて１３００〜１４００度の高温で加熱溶解し、銅や金・銀などの有価金属を回収することが行われている。スラッジを溶融炉で溶融した際に発生する排ガスには各種排出規制物質が含まれており、各排出規制物質の濃度を排出基準以下に浄化して排出する必要がある。 An appropriate solvent is added to sludge containing metals and dissolved at high temperature of 1300 to 1400 degrees to recover valuable metals such as copper, gold and silver. The exhaust gas generated when the sludge is melted in the melting furnace contains various emission control substances, and it is necessary to purify and discharge the concentration of each emission control substance below the emission standard.
特許文献１には、排出規制物質の１つであるフッ素の濃度を、排出基準を満たす濃度まで浄化処理する方法が開示されている。 Patent Document 1 discloses a method for purifying the concentration of fluorine, which is one of emission control substances, to a concentration that satisfies emission standards.
ところで、排出規制物質の１つに硫黄酸化物（ＳＯｘ）がある。一般に、排ガス中のＳＯｘは、排ガスに脱硫剤を添加することによって除去されるが、脱硫剤の添加量を脱硫工程後のＳＯｘの濃度に基づいて手動で決定した場合、その添加量が過剰になってしまうおそれがある。 Incidentally, sulfur oxide (SOx) is one of emission control substances. Generally, SOx in exhaust gas is removed by adding a desulfurizing agent to the exhaust gas. However, if the addition amount of the desulfurizing agent is manually determined based on the concentration of SOx after the desulfurization process, the addition amount is excessive. There is a risk of becoming.
本発明は上記の課題に鑑み、排ガス中のＳＯｘ濃度の排出基準を遵守しつつ、脱硫剤の使用量を低減する脱硫剤添加制御方法を提供すること目的とする。 In view of the above problems, an object of the present invention is to provide a desulfurization agent addition control method that reduces the amount of desulfurization agent used while complying with the emission standard of SOx concentration in exhaust gas.
本発明に係る脱硫剤添加制御方法は、脱硫剤の添加により排ガス中の硫黄酸化物（ＳＯｘ）を中和する脱硫工程において、前記脱硫工程後のＳＯｘ濃度に基づいて前記排ガスに添加する前記脱硫剤の添加量を制御する脱硫剤添加制御方法であって、Ｎ時間前のＳＯｘ濃度のＮ時間移動平均値と、現在のＳＯｘ濃度のＮ時間移動平均値との差分である第１差分と、前記Ｎ時間前に前記脱硫剤の添加量の算出に用いた制御値と、に基づいて、今回の制御値を算出し、前記今回の制御値に基づいて前記脱硫剤の添加量を決定する方法である。 The desulfurization agent addition control method according to the present invention is the desulfurization step of adding to the exhaust gas based on the SOx concentration after the desulfurization step in the desulfurization step of neutralizing sulfur oxide (SOx) in the exhaust gas by adding the desulfurization agent. A desulfurization agent addition control method for controlling the addition amount of the agent, the first difference being the difference between the N time moving average value of the SOx concentration before N hours and the N time moving average value of the current SOx concentration, A method of calculating the current control value based on the control value used to calculate the addition amount of the desulfurizing agent N hours before and determining the addition amount of the desulfurization agent based on the current control value It is.
この場合において、前記第１差分に所定の係数を乗算した値に、前記Ｎ時間前の制御値を加算することにより、前記今回の制御値を算出してもよい。 In this case, the current control value may be calculated by adding the control value N hours before to the value obtained by multiplying the first difference by a predetermined coefficient.
この場合において、ＳＯｘ濃度のＭ時間移動平均値が第１の閾値以上である場合、前記所定の係数に所定の値を加算してもよい。 In this case, when the M time moving average value of the SOx concentration is equal to or more than the first threshold value, a predetermined value may be added to the predetermined coefficient.
また、所定時間毎にＳＯｘ濃度の瞬時値を取得し、前記ＳＯｘ濃度の瞬時値が第２の閾値以上である場合、前記ＳＯｘ濃度の瞬時値と前記第２の閾値との差分である第２差分を更に用いて、前記今回の制御値を算出してもよい。 In addition, an instantaneous value of the SOx concentration is acquired every predetermined time, and when the instantaneous value of the SOx concentration is equal to or greater than a second threshold value, a second value that is a difference between the instantaneous value of the SOx concentration and the second threshold value is obtained. The current control value may be calculated by further using the difference.
この場合において、前記ＳＯｘ濃度の瞬時値に応じた補正係数を更に用いて、前記今回の制御値を算出してもよい。 In this case, the current control value may be calculated by further using a correction coefficient corresponding to the instantaneous value of the SOx concentration.
また、前記ＳＯｘ濃度の瞬時換算値が第３の閾値以下の場合、前記今回の制御値を固定値としてもよい。 Further, when the instantaneous conversion value of the SOx concentration is equal to or smaller than the third threshold value, the current control value may be a fixed value.
本発明に係る脱硫剤添加制御方法によれば、排ガス中のＳＯｘ濃度の排出基準を遵守しつつ、脱硫剤の使用量を低減することができる。 According to the desulfurization agent addition control method according to the present invention, the amount of desulfurization agent used can be reduced while complying with the emission standard for SOx concentration in exhaust gas.
図１は、スラッジの処理工程を表す工程図である。図１で例示するように、出発原料は金属類を含むスラッジである。 FIG. 1 is a process diagram showing a sludge treatment process. As illustrated in FIG. 1, the starting material is sludge containing metals.
（溶融工程）
溶融工程では、スラッジを溶融炉に投入し、焼却処理する。
(Melting process)
In the melting step, sludge is put into a melting furnace and incinerated.
（冷却工程）
冷却工程では、溶融炉からの高温の排ガスを廃熱ボイラーに導入し、３００℃以下に冷却する。
(Cooling process)
In the cooling step, high-temperature exhaust gas from the melting furnace is introduced into the waste heat boiler and cooled to 300 ° C. or lower.
（除塵工程）
除塵工程では、集塵機を用いて、排ガス中の塵を取り除く。この除塵工程によって、フッ素除去工程においてカルシウム塩との反応効率を上げることができる。集塵機はいずれのタイプでもよいが、大きさや処理能力の面から電気集塵機が好ましい。
(Dust removal process)
In the dust removal process, dust in the exhaust gas is removed using a dust collector. By this dust removal step, the reaction efficiency with the calcium salt can be increased in the fluorine removal step. Any type of dust collector may be used, but an electric dust collector is preferable in terms of size and processing capacity.
（フッ素除去工程）
フッ素除去工程では、排ガスにフッ素を除去するためのカルシウム塩を投入する。カルシウム塩としては生石灰、消石灰、塩化カルシウム、石膏、及び炭酸カルシウムの何れを使用してもよい。排ガスは、溶融炉にて生成した硫黄酸化物や窒素酸化物を含有する酸性ガスであることから、中和効果を有する塩基性の消石灰や炭酸カルシウムが好ましい。またカルシウム塩を投入する時には、活性炭に代表される炭素系吸着剤をも添加するとさらに清浄効果が期待される。
(Fluorine removal process)
In the fluorine removal step, a calcium salt for removing fluorine is introduced into the exhaust gas. As the calcium salt, any of quick lime, slaked lime, calcium chloride, gypsum, and calcium carbonate may be used. Since the exhaust gas is an acidic gas containing sulfur oxides and nitrogen oxides generated in a melting furnace, basic slaked lime and calcium carbonate having a neutralizing effect are preferable. In addition, when adding a calcium salt, if a carbon-based adsorbent typified by activated carbon is also added, a further cleaning effect is expected.
（回収工程１）
回収工程１では、投入されたカルシウム塩や活性炭が適当な集塵機、例えばバグフィルターにより分離回収される。回収物としてのカルシウム塩にはフッ素がフッ化カルシウムとして含有されている。
(Recovery process 1)
In the recovery step 1, the input calcium salt and activated carbon are separated and recovered by a suitable dust collector, for example, a bag filter. The recovered calcium salt contains fluorine as calcium fluoride.
（脱硫工程）
脱硫工程では、フッ素を除去した排ガスに、脱硫剤（例えば、ナトリウムの炭酸塩）を添加して硫黄酸化物（ＳＯｘ）を中和する。これは、排ガス中に酸成分、とくに硫黄酸化物（ＳＯｘ）が含まれていると後工程である脱硝工程において、脱硝触媒が被毒されることになり好ましくないからである。
(Desulfurization process)
In the desulfurization step, the sulfur oxide (SOx) is neutralized by adding a desulfurization agent (for example, sodium carbonate) to the exhaust gas from which fluorine has been removed. This is because if the exhaust gas contains an acid component, particularly sulfur oxide (SOx), the denitration catalyst is poisoned in the denitration process, which is a subsequent process, which is not preferable.
脱硫工程において、投入する脱硫剤は、一般的なＳＯｘ中和用試薬、例えば炭酸ナトリウム、炭酸水素ナトリウムなどでよい。例えば、市販の脱硫剤（旭硝子社製のアクレシア（登録商標）等）を使用することができる。その粒径は特に指定されないが、後述する回収工程２において粉塵を回収する集塵機の能力に応じて選択される。 In the desulfurization step, the desulfurizing agent to be added may be a general SOx neutralizing reagent such as sodium carbonate or sodium hydrogen carbonate. For example, a commercially available desulfurization agent (Acrecia (registered trademark) manufactured by Asahi Glass Co., Ltd.) can be used. The particle size is not particularly specified, but is selected according to the ability of the dust collector to collect dust in the collecting step 2 described later.
（回収工程２）
回収工程２では、脱硫工程で生じた粉塵、すなわち炭酸ナトリウムの中和反応により生じた硫酸ナトリウム、硫酸水素ナトリウム、亜硫酸ナトリウム等を固気分離する。なお、この分離された粉塵は、特に処理することなく水に溶解させた後、通常の排水処理工程に投入して排出することが可能である。
(Recovery process 2)
In the recovery process 2, the dust generated in the desulfurization process, that is, sodium sulfate, sodium hydrogen sulfate, sodium sulfite, and the like generated by the neutralization reaction of sodium carbonate are separated into solid and gas. The separated dust can be dissolved in water without any particular treatment and then discharged into a normal waste water treatment process.
（脱硝工程）
脱硝工程では、回収工程２により粉塵が除去された排ガスに、アンモニアを添加して脱硝触媒により窒素酸化物を取り除く。脱硝工程後の排ガスは、大気中に放出される。この脱硝工程は、脱硝触媒塔などを用いるなど、一般的に用いられる方法で行えばよい。なお、本実施形態では脱硝工程後、排ガス中に含まれるＳＯｘ濃度が分析計によって測定される。
(Denitration process)
In the denitration process, ammonia is added to the exhaust gas from which dust has been removed in the recovery process 2, and nitrogen oxides are removed by the denitration catalyst. The exhaust gas after the denitration process is released into the atmosphere. This denitration step may be performed by a generally used method such as using a denitration catalyst tower. In this embodiment, the SOx concentration contained in the exhaust gas is measured by an analyzer after the denitration process.
次に、上述したスラッジの処理工程のうち、脱硫工程において排ガスに添加される脱硫剤の添加量を制御する脱硫剤添加制御方法について説明する。脱硫剤添加量制御は、脱硫剤を排ガスに添加する脱硫剤添加装置に接続された制御装置により実行される。 Next, a desulfurization agent addition control method for controlling the amount of desulfurization agent added to the exhaust gas in the desulfurization step among the above-described sludge treatment steps will be described. The desulfurization agent addition amount control is executed by a control device connected to a desulfurization agent addition device that adds the desulfurization agent to the exhaust gas.
本実施形態において、制御装置は、脱硝工程後のＳＯｘ濃度の１時間移動平均値を排出基準未満の所定の範囲に収め、かつ、脱硫剤の使用量を低減するよう脱硫剤の添加量を制御する。脱硫剤の添加量の決定には、ＭＶ値を用いる。なお、ＭＶ値は、例えば、脱硫剤の添加弁の開放度等を制御するための指標であり、ＭＶ値と脱硫剤の添加量の相関は、事前に試験を行うことで求めることができる。なお、ＭＶ値は、脱硫剤の添加量の決定に用いられる制御値の一例である。 In the present embodiment, the control device controls the addition amount of the desulfurizing agent so that the one-hour moving average value of the SOx concentration after the denitration step falls within a predetermined range less than the emission standard and the amount of the desulfurizing agent is reduced. To do. The MV value is used to determine the addition amount of the desulfurizing agent. The MV value is an index for controlling the degree of opening of the desulfurization agent addition valve, for example, and the correlation between the MV value and the addition amount of the desulfurization agent can be obtained by conducting a test in advance. The MV value is an example of a control value used for determining the addition amount of the desulfurizing agent.
図２は、本実施形態にかかる脱硫剤添加制御方法を示すフローチャートである。図２の処理は、脱硫剤添加量制御が開始され、脱硫剤添加量制御が終了されるまで、所定時間おきに実行される。 FIG. 2 is a flowchart showing a desulfurization agent addition control method according to the present embodiment. The processing in FIG. 2 is executed at predetermined intervals until the desulfurization agent addition amount control is started and the desulfurization agent addition amount control is terminated.
まず、ステップＳ１１において、制御装置は、分析計から、脱硝工程後のＳＯｘ濃度の１時間移動平均値を取得する。なお、ＳＯｘ濃度の１時間移動平均値は、ＳＯｘ濃度のＭ時間移動平均値の一例である。 First, in step S11, the control device obtains a one-hour moving average value of the SOx concentration after the denitration process from the analyzer. The 1-hour moving average value of the SOx concentration is an example of the M-time moving average value of the SOx concentration.
次に、ステップＳ１３において、制御装置は、ステップＳ１１で取得したＳＯｘ濃度の１時間移動平均値が閾値Ｖ１以上か否かを判断する。 Next, in step S13, the control device determines whether or not the one-hour moving average value of the SOx concentration acquired in step S11 is equal to or greater than a threshold value V1.
ＳＯｘ濃度の１時間移動平均値が閾値Ｖ１以上の場合、ステップＳ１３の判断が肯定され、ステップＳ１４に移行する。なお、閾値Ｖ１は、第１の閾値の一例である。 If the one-hour moving average value of the SOx concentration is equal to or greater than the threshold value V1, the determination in step S13 is affirmed and the process proceeds to step S14. The threshold value V1 is an example of a first threshold value.
ステップＳ１４に移行すると、制御装置は、ＭＶ値の算出に使用する係数であるＧａｉｎに所定の値を加算する。所定の値は、ＳＯｘ濃度の移動平均値に基づいて決定される。 If transfering it to step S14, a control apparatus will add a predetermined value to Gain which is a coefficient used for calculation of MV value. The predetermined value is determined based on the moving average value of the SOx concentration.
一方、ステップＳ１３の判断が否定された場合、ステップＳ１４の処理をスキップして、ステップＳ１５に移行する。 On the other hand, if the determination in step S13 is negative, the process of step S14 is skipped and the process proceeds to step S15.
ステップＳ１５に移行すると、制御装置は、所定時間ごとに取得されるＳＯｘ濃度の瞬時値が閾値Ｖ２以上であるか否かを判断する。ＳＯｘ濃度の瞬時値は、測定によって求められる。なお、閾値Ｖ２は、第２の閾値の一例である。 If transfering it to step S15, a control apparatus will judge whether the instantaneous value of SOx density | concentration acquired for every predetermined time is more than threshold value V2. The instantaneous value of the SOx concentration is obtained by measurement. The threshold value V2 is an example of a second threshold value.
ＳＯｘ濃度の瞬時値が閾値Ｖ２未満である場合、ステップＳ１５の判断が否定され、ステップＳ１６に移行する。 If the instantaneous value of the SOx concentration is less than the threshold value V2, the determination in step S15 is negative and the process proceeds to step S16.
ステップＳ１６に移行すると、制御装置は、ＳＯｘ濃度の瞬時値が閾値Ｖ３以下であるか否か判断する。ここでの判断が否定された場合、ステップＳ１７に移行する。なお、閾値Ｖ３は、第３の閾値の一例である。 In step S16, the control device determines whether or not the instantaneous value of the SOx concentration is equal to or less than the threshold value V3. When judgment here is denied, it transfers to step S17. The threshold value V3 is an example of a third threshold value.
ステップＳ１７に移行すると、制御装置は、以下の式（１）により、ＭＶ値を算出する。 If transfering it to step S17, a control apparatus will calculate MV value by the following formula | equation (1).
ＭＶ＝Ｇａｉｎ×Δｘ＋Ｂｉａｓ＋ＭＶｘ （１） MV = Gain × Δx + Bias + MVx (1)
ここで、Δｘは、例えば、２時間前のＳＯｘ濃度の２時間移動平均値と現在のＳＯｘ濃度の２時間移動平均値との差分である。なお、ＳＯｘ濃度の移動平均値を算出する期間（時間）は、２時間に限定されるものではなく、２時間未満であっても、２時間以上であってもよい。ＳＯｘ濃度の移動平均値を算出する期間（時間）は、例えば、スラッジを溶融炉に投入する時間間隔に基づいて決定すればよい。２時間前のＳＯｘ濃度の２時間移動平均値と現在のＳＯｘ濃度の２時間移動平均値との差分は、Ｎ時間前のＳＯｘ濃度のＮ時間移動平均値と、現在のＳＯｘ濃度のＮ時間移動平均値との差分である第１差分の一例である。 Here, Δx is, for example, the difference between the 2-hour moving average value of the SOx concentration two hours ago and the 2-hour moving average value of the current SOx concentration. The period (time) for calculating the moving average value of the SOx concentration is not limited to 2 hours, and may be less than 2 hours or 2 hours or more. What is necessary is just to determine the period (time) which calculates the moving average value of SOx density | concentration based on the time interval which throws sludge into a melting furnace, for example. The difference between the 2-hour moving average value of the SOx concentration two hours ago and the 2-hour moving average value of the current SOx concentration is the N-hour moving average value of the SOx concentration N hours ago and the N-time movement of the current SOx concentration. It is an example of the 1st difference which is a difference with an average value.
Ｂｉａｓは定数である。ＭＶｘは、例えば、２時間前に制御装置により算出されたＭＶ値である。なお、本実施形態において、制御開始直後では、Δｘの値として、制御開始直後のタイミングで分析計から出力される、ＳＯｘ濃度の１時間移動平均値を使用する。また、制御開始直後は、ＭＶｘ＝０とする。 Bias is a constant. MVx is, for example, an MV value calculated by the control device two hours ago. In the present embodiment, immediately after the start of control, the 1-hour moving average value of the SOx concentration output from the analyzer at the timing immediately after the start of control is used as the value of Δx. Immediately after the start of control, MVx = 0.
ところで、ＳＯｘ濃度の瞬時値が閾値Ｖ３以下の場合、ステップＳ１６の判断が肯定され、ステップＳ１８に移行する。 By the way, when the instantaneous value of the SOx concentration is equal to or less than the threshold value V3, the determination in step S16 is affirmed, and the process proceeds to step S18.
ステップＳ１８に移行すると、制御装置は、ＭＶ＝固定値とする。 In step S18, the control device sets MV = fixed value.
ところで、ＳＯｘ濃度の瞬時値が閾値Ｖ２以上である場合、ステップＳ１５の判断が肯定され、ステップＳ１９に移行する。 By the way, when the instantaneous value of the SOx concentration is equal to or higher than the threshold value V2, the determination in step S15 is affirmed, and the process proceeds to step S19.
ステップＳ１９に移行すると、制御装置は、以下の式（２）により、ＭＶ値を算出する。 If transfering it to step S19, a control apparatus will calculate MV value by the following formula | equation (2).
ＭＶ＝補正係数×Ｇａｉｎ×Δｘ´
＋Ｇａｉｎ×Δｘ＋Ｂｉａｓ＋ＭＶｘ （２）
MV = correction coefficient × Gain × Δx ′
+ Gain × Δx + Bias + MVx (2)
ここで、Δｘ´は、ＳＯｘ濃度の瞬時値と閾値Ｖ２との差分（ＳＯｘ濃度の瞬時値−閾値Ｖ２）である。補正係数は、ＳＯｘ濃度の瞬時値に基づいて決定される値である。 Here, Δx ′ is the difference between the instantaneous value of SOx concentration and the threshold value V2 (instantaneous value of SOx concentration−threshold value V2). The correction coefficient is a value determined based on the instantaneous value of the SOx concentration.
続くステップＳ２１では、制御装置はステップＳ１７〜Ｓ１９のいずれかにおいて算出されたＭＶ値を所定の計算式に代入することによって、脱硫剤の添加量を決定し、脱硫剤を排ガスに添加する。 In subsequent step S21, the control device determines the addition amount of the desulfurizing agent by substituting the MV value calculated in any of steps S17 to S19 into a predetermined calculation formula, and adds the desulfurizing agent to the exhaust gas.
本実施形態によれば、２時間前のＳＯｘ濃度の２時間移動平均値と、現在のＳＯｘ濃度の２時間移動平均値との差分であるΔｘと、２時間前に脱硫剤の添加量の算出に用いたＭＶｘと、に基づいて、ＭＶ値を算出し、ＭＶ値に基づいて脱硫剤の添加量を決定するので、２時間前に算出された添加量の脱硫剤を排ガスに添加した結果を踏まえて今回の脱硫剤の添加量を決定できる。これにより、必要量以上の脱硫剤が排ガスに添加されるのを防止することができ、脱硫剤の添加量を低減することができる。 According to the present embodiment, Δx, which is the difference between the 2-hour moving average value of the SOx concentration two hours ago and the 2-hour moving average value of the current SOx concentration, and the addition amount of the desulfurization agent two hours ago are calculated. The MV value is calculated based on the MVx used in the above, and the addition amount of the desulfurization agent is determined based on the MV value. Therefore, the result of adding the addition amount of the desulfurization agent calculated two hours ago to the exhaust gas Based on this, the amount of desulfurization agent can be determined. Thereby, it is possible to prevent the desulfurizing agent beyond the required amount from being added to the exhaust gas, and to reduce the amount of desulfurizing agent added.
上述した脱硫剤添加量制御を１２ヶ月間実施したところ、ＳＯｘ濃度の１時間移動平均値の平均値は排出基準未満であり、脱硫剤の使用量は脱硝工程後のＳＯｘ濃度に基づいて手動で脱硫剤の添加量を決定した場合の使用量の約４割となった。以上の結果から、上述した脱硫剤添加制御方法により、排ガス中のＳＯｘ濃度の排出基準を遵守しつつ、脱硫剤の使用量を低減できることが明らかとなった。 When the above-described desulfurization agent addition amount control was performed for 12 months, the average value of the 1 hour moving average value of the SOx concentration was less than the emission standard, and the amount of desulfurization agent used was manually determined based on the SOx concentration after the denitration process. This was about 40% of the amount used when the amount of desulfurizing agent was determined. From the above results, it became clear that the use amount of the desulfurizing agent can be reduced by the above-described desulfurizing agent addition control method while complying with the emission standard of the SOx concentration in the exhaust gas.
以上、本発明の実施例について詳述したが、本発明は係る特定の実施例に限定されるものではなく、特許請求の範囲に記載された本発明の要旨の範囲内において、種々の変形・変更が可能である。 Although the embodiments of the present invention have been described in detail above, the present invention is not limited to such specific embodiments, and various modifications and changes can be made within the scope of the gist of the present invention described in the claims. It can be changed.
Claims (6)
Ｎ時間前のＳＯｘ濃度のＮ時間移動平均値と、現在のＳＯｘ濃度のＮ時間移動平均値との差分である第１差分と、前記Ｎ時間前に前記脱硫剤の添加量の算出に用いた制御値と、に基づいて、今回の制御値を算出し、前記今回の制御値に基づいて前記脱硫剤の添加量を決定する脱硫剤添加制御方法。 Desulfurization agent addition control for controlling the addition amount of the desulfurization agent added to the exhaust gas based on the SOx concentration after the desulfurization step in a desulfurization step of neutralizing sulfur oxide (SOx) in the exhaust gas by adding a desulfurization agent A method,
Used to calculate the first difference, which is the difference between the N-hour moving average value of the SOx concentration before N hours and the N-time moving average value of the current SOx concentration, and the addition amount of the desulfurizing agent before the N hours. A desulfurization agent addition control method for calculating a control value for this time based on the control value and determining an addition amount of the desulfurization agent based on the control value for the current time.
The desulfurization agent addition control method according to claim 4 or 5, wherein when the instantaneous value of the SOx concentration is equal to or less than a third threshold value, the current control value is a fixed value.
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