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JP2012240034A - Flue gas desulfurization equipment provided with flue gas finishing desulfurization device, and exhaust gas treatment system using the same - Google Patents

Flue gas desulfurization equipment provided with flue gas finishing desulfurization device, and exhaust gas treatment system using the same Download PDF

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Publication number
JP2012240034A
JP2012240034A JP2011116094A JP2011116094A JP2012240034A JP 2012240034 A JP2012240034 A JP 2012240034A JP 2011116094 A JP2011116094 A JP 2011116094A JP 2011116094 A JP2011116094 A JP 2011116094A JP 2012240034 A JP2012240034 A JP 2012240034A
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desulfurization
slurry
flue gas
finishing
absorbent
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Naoyuki Kamiyama
直行 神山
Tatsuto Nagayasu
立人 長安
Takeshi Maeda
健 前田
Tetsu Ushiku
哲 牛久
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Mitsubishi Heavy Industries Ltd
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Priority to JP2011116094A priority Critical patent/JP2012240034A/en
Priority to PCT/JP2012/062206 priority patent/WO2012160998A1/en
Publication of JP2012240034A publication Critical patent/JP2012240034A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

PROBLEM TO BE SOLVED: To provide a flue gas desulfurization equipment provided with a flue gas finishing desulfurization device, and an exhaust gas treatment system using the same.SOLUTION: The flue gas desulfurization equipment includes a main desulfurization device 13 for removing a sulfur oxide from a combustion exhaust gas (exhaust gas) 11 by means of an absorbing liquid slurry (absorbing liquid slurry) 12 containing a calcium compound, a finishing desulfurization device 15 for further removing the sulfur oxide remaining in the desulfurized gas 14, from which the sulfur oxide has been removed in the main desulfurization device 13, until the concentration of the sulfur oxide is extremely low, and an absorbing liquid slurry supply means for supplying the absorbing liquid slurry 12 containing the calcium compound in a prescribed concentration to the finishing desulfurization device 15.

Description

本発明は、仕上げ排煙脱硫装置を供えた排煙脱硫設備及びこれを用いた排ガス処理システムに関する。   The present invention relates to a flue gas desulfurization facility provided with a finish flue gas desulfurization apparatus and an exhaust gas treatment system using the same.

排ガス処理システムの一例を図６に示す。図６に示すように、排ガス処理システム１０００においては、ボイラ（石炭焚ボイラ）１０１からの排ガス１１は、脱硝装置１０２で排ガス中の窒素酸化物（ＮＯｘ）を除去した後、まずエアヒータ１０３に導かれてボイラに供給される空気を加熱する。その後排ガスＧは、乾式の電気集塵機１０４に導入されて煤塵が除去される。次に、排ガス１１は、脱硫装置１０５に導入されて硫黄酸化物（ＳＯｘ）が除去される。その後、排ガス１１はＣＯ2回収装置１０６に導入されて、二酸化炭素を除去し、その後煙突１１１より浄化ガス１１２が大気に放出される（例えば、特許文献１参照）。 An example of the exhaust gas treatment system is shown in FIG. As shown in FIG. 6, in the exhaust gas treatment system 1000, the exhaust gas 11 from the boiler (coal-fired boiler) 101 is first introduced into the air heater 103 after nitrogen oxide (NOx) in the exhaust gas is removed by the denitration device 102. The air supplied to the boiler is heated. Thereafter, the exhaust gas G is introduced into a dry electric dust collector 104 to remove dust. Next, the exhaust gas 11 is introduced into the desulfurization apparatus 105 to remove sulfur oxides (SOx). Thereafter, the exhaust gas 11 is introduced into the CO 2 recovery device 106 to remove carbon dioxide, and then the purified gas 112 is released from the chimney 111 to the atmosphere (for example, see Patent Document 1).

脱硫と脱炭素を同時に処理する方法として種々の提案がある（特許文献２〜３）。   There are various proposals as methods for simultaneously treating desulfurization and decarbonization (Patent Documents 2 to 3).

特開平１１−１７９１４７号公報Japanese Patent Laid-Open No. 11-179147 特開平０６−８６９１１号公報Japanese Patent Laid-Open No. 06-86911 特開２００３−５３１３４号公報JP 2003-53134 A

しかしながら、脱硫装置１０５で脱硫した後に、ＣＯ2回収装置１０６を設置する場合、当該ＣＯ2回収装置１０６に許容量を超える硫黄酸化物や煤塵が残存すると、ＣＯ2吸収液として例えばアミン系吸収液を用いる場合、ＣＯ2吸収液（例えばアミン吸収液）中に蓄積され、或いは当該劣化相当分の吸収液をリクレーミングしたり、新液を補充したりする際にランニングコストが多く発生する、という問題がある。 However, when the CO 2 recovery device 106 is installed after desulfurization by the desulfurization device 105, if sulfur oxide or soot exceeding the allowable amount remains in the CO 2 recovery device 106, for example, an amine-based absorption liquid is used as the CO 2 absorption liquid. Is used, it is accumulated in the CO 2 absorbing liquid (for example, amine absorbing liquid), or the running cost is increased when reclaiming the absorbing liquid corresponding to the deterioration or replenishing the new liquid. There is.

よって、予め脱硫装置１０５で硫黄酸化物が除去された排ガス１１に対して、更に排ガス中の対象成分を極低濃度まで浄化できる仕上げ排煙脱硫装置を供えた排煙脱硫設備の出現が切望されており、これを備えた排ガス処理システムが考案されている。   Therefore, the appearance of a flue gas desulfurization facility provided with a finish flue gas desulfurization device that can further purify the target component in the exhaust gas to an extremely low concentration with respect to the exhaust gas 11 from which sulfur oxides have been previously removed by the desulfurization device 105 is eagerly desired. An exhaust gas treatment system equipped with this has been devised.

一方で仕上げ脱硫装置では入口排ガス中のＳ分吸収負荷が低くなり、仕上げ脱硫装置の入口排ガス中の水分が飽和状態で蒸発が促進され難い条件下で仕上げ脱硫装置の吸収液スラリ中の固体状の硫酸カルシウム成分、すなわち石膏粒子濃度が低くなる事から、スラリ中で硫酸イオンとカルシウムがイオンが反応する際に吸収塔内で壁面や構造物、配管等の表面上に石膏スケールが析出する事を防止するための種晶石膏粒子のスラリ中の含有濃度が不足し当該スケールが剥離し吸収液噴出ノズルを閉塞させる懸念がある。このため、例えば、前記の石膏スケールの設備部材への析出を防止できるスラリ中石膏濃度として５重量パーセント以上を保持とする事が望ましい。   On the other hand, in the final desulfurization apparatus, the S component absorption load in the inlet exhaust gas is low, and the solid state in the absorption liquid slurry of the final desulfurization apparatus is under the condition that the moisture in the inlet exhaust gas of the final desulfurization apparatus is saturated and evaporation is difficult to promote. The concentration of gypsum particles, that is, the concentration of gypsum particles in the slurry, causes gypsum scale to deposit on the surface of walls, structures, and piping in the absorption tower when sulfate ions react with calcium ions in the slurry. There is a concern that the concentration of the seed crystal gypsum particles in the slurry for preventing the ink is insufficient, the scale peels off, and the absorbing liquid ejection nozzle is blocked. For this reason, for example, it is desirable to maintain 5% by weight or more as the gypsum concentration in the slurry that can prevent the gypsum scale from being deposited on equipment members.

本発明は、前記問題に鑑み、当該石膏スケールの設備部材への析出を防止することができる仕上げ排煙脱硫装置を供えた排煙脱硫設備及びこれを用いた排ガス処理システムを提供することを課題とする。   In view of the above problems, the present invention provides a flue gas desulfurization facility provided with a finish flue gas desulfurization device capable of preventing the gypsum scale from being deposited on a facility member, and an exhaust gas treatment system using the same. And

上述した課題を解決するための本発明の第１の発明は、燃焼排ガスから硫黄酸化物を、カルシウム化合物を含む吸収液スラリにより除去する主脱硫装置と、該主脱硫装置で硫黄酸化物を除去した脱硫ガス中に残存する硫黄酸化物を極低濃度までさらに除去する仕上げ脱硫装置と、該仕上げ脱硫装置に所定濃度のカルシウム化合物を含む吸収液スラリをスケーリング防止用の種晶石膏源として供給する吸収液スラリ供給手段とを具備することを特徴とする排煙脱硫設備にある。   A first invention of the present invention for solving the above-mentioned problems is a main desulfurization device that removes sulfur oxide from combustion exhaust gas by an absorbent slurry containing a calcium compound, and sulfur oxide is removed by the main desulfurization device. A final desulfurization apparatus that further removes sulfur oxide remaining in the desulfurized gas to an extremely low concentration, and an absorbent slurry containing a calcium compound at a predetermined concentration is supplied to the final desulfurization apparatus as a seed crystal gypsum source for preventing scaling. An exhaust gas desulfurization facility comprising an absorbent slurry supply means.

第２の発明は、第１の発明において、前記吸収液スラリ供給手段が、前記主脱硫装置を循環する吸収液スラリ循環ラインと、該吸収液スラリ循環ラインから分岐され、循環する吸収液スラリの一部をスケーリング防止用の種晶石膏源として仕上げ脱硫装置に供給する吸収液スラリ供給ラインとを具備することを特徴とする排煙脱硫設備にある。   According to a second aspect of the present invention, in the first aspect, the absorbent slurry supply means includes an absorbent slurry circulating line that circulates through the main desulfurization device, and an absorbent slurry that is branched from the absorbent slurry circulating line and circulates. A flue gas desulfurization facility comprising an absorbent slurry supply line for supplying a part to a finishing desulfurization apparatus as a seed crystal gypsum source for preventing scaling.

第３の発明は、第１の発明において、前記吸収液スラリ供給手段が、前記主脱硫装置を循環する吸収液スラリ循環ラインと、該吸収液スラリ循環ラインから分岐され、循環する吸収液スラリの一部をスケーリング防止用の種晶石膏源として仕上げ脱硫装置に供給する吸収液スラリ供給ラインと、前記仕上げ脱硫装置内の吸収液スラリ濃度をスケーリング防止用の種晶石膏源として機能する所定設定値に調整する吸収液濃度調整手段と、を具備することを特徴とする排煙脱硫設備にある。   According to a third aspect of the present invention, in the first aspect, the absorbent slurry supply means includes an absorbent slurry circulation line that circulates through the main desulfurization device, and an absorbent slurry that divides and circulates from the absorbent slurry circulation line. Absorbing liquid slurry supply line that supplies a part of the seeding gypsum source for preventing scaling to the finishing desulfurization apparatus, and a predetermined set value that functions as a seeding gypsum source for preventing scaling of the absorbing liquid slurry concentration in the finishing desulfurization apparatus. And a flue gas desulfurization facility comprising an absorbent concentration adjusting means for adjusting the absorption liquid concentration.

第４の発明は、第１の発明において、前記吸収液スラリ供給手段が、前記主脱硫装置から抜き出した吸収液スラリから固液分離した石膏をスラリ化するスラリホッパと、該石膏スラリをスケーリング防止用の種晶石膏源として仕上げ脱硫装置に供給する石膏スラリ供給ラインとを具備することを特徴とする排煙脱硫設備にある。   According to a fourth invention, in the first invention, the absorbent slurry supply means is a slurry hopper for slurrying gypsum solid-liquid separated from the absorbent slurry extracted from the main desulfurization device, and for preventing scaling of the gypsum slurry. A flue gas desulfurization facility comprising a gypsum slurry supply line for supplying to a finishing desulfurization apparatus as a seed crystal gypsum source.

第５の発明は、第１乃至４のいずれか一つの発明において、前記仕上げ脱硫装置内に強アルカリを供給する強アルカリ供給手段を具備することを特徴とする排煙脱硫設備にある。   A fifth invention is the flue gas desulfurization facility according to any one of the first to fourth inventions, further comprising strong alkali supply means for supplying strong alkali into the finishing desulfurization apparatus.

第６の発明は、ボイラ等からの排ガス中の窒素酸化物を除去する脱硝装置と、窒素酸化物除去後のガス中の煤塵を除去する集塵機と、除塵後のガス中の硫黄酸化物を除去する脱硫装置と、この脱硫後の排ガス中に残存する硫黄酸化物を極低濃度までさらに除去する第１乃至５のいずれか一つの排煙脱硫設備と、浄化ガス中の二酸化炭素を回収するＣＯ2回収装置とを具備することを特徴とする排ガス処理システムにある。 The sixth invention is a denitration device that removes nitrogen oxides in exhaust gas from boilers, a dust collector that removes soot and dust in the gas after nitrogen oxide removal, and sulfur oxides in the gas after dust removal A desulfurization apparatus for removing the sulfur oxide remaining in the exhaust gas after the desulfurization to a very low concentration, and a CO 2 for recovering carbon dioxide in the purified gas. 2. An exhaust gas treatment system comprising a recovery device.

本発明によれば、仕上げ脱硫装置の吸収液スラリを所定硫酸カルシウム濃度とし種晶石膏として機能させることで、仕上げ脱硫装置内での石膏スケーリングの発生を防ぎ、安定した継続的な操業が可能となる。   According to the present invention, the absorbent slurry of the finishing desulfurization apparatus has a predetermined calcium sulfate concentration and functions as seed crystal gypsum, thereby preventing the occurrence of gypsum scaling in the finishing desulfurization apparatus and enabling stable and continuous operation. Become.

図１は、実施例１に係る排煙脱硫設備の概略図である。FIG. 1 is a schematic diagram of a flue gas desulfurization facility according to a first embodiment. 図２−１は、実施例２に係る排煙脱硫設備の概略図である。FIG. 2-1 is a schematic diagram of the flue gas desulfurization facility according to the second embodiment. 図２−２は、実施例２に係る他の排煙脱硫設備の概略図である。FIG. 2-2 is a schematic diagram of another flue gas desulfurization facility according to the second embodiment. 図３−１は、実施例３に係る排煙脱硫設備の概略図である。FIG. 3A is a schematic diagram of the flue gas desulfurization facility according to the third embodiment. 図３−２は、実施例３に係る他の排煙脱硫設備の概略図である。FIG. 3-2 is a schematic diagram of another flue gas desulfurization facility according to the third embodiment. 図３−３は、実施例３に係る他の排煙脱硫設備の概略図である。FIG. 3C is a schematic diagram of another flue gas desulfurization facility according to the third embodiment. 図３−４は、実施例３に係る他の排煙脱硫設備の概略図である。FIG. 3-4 is a schematic diagram of another flue gas desulfurization facility according to the third embodiment. 図４は、実施例４に係る排煙脱硫設備の概略図である。FIG. 4 is a schematic diagram of the flue gas desulfurization facility according to the fourth embodiment. 図５は、実施例５に係る排ガス処理システムの概略図である。FIG. 5 is a schematic diagram of an exhaust gas treatment system according to a fifth embodiment. 図６は、排ガス処理システムの一例を示す図である。FIG. 6 is a diagram illustrating an example of an exhaust gas treatment system.

以下、この発明につき図面を参照しつつ詳細に説明する。なお、この実施例により本発明が限定されるものではなく、また、実施例が複数ある場合には、各実施例を組み合わせて構成するものも含むものである。また、下記実施例における構成要素には、当業者が容易に想定できるもの、あるいは実質的に同一のものが含まれる。   Hereinafter, the present invention will be described in detail with reference to the drawings. In addition, this invention is not limited by this Example, Moreover, when there exists multiple Example, what comprises combining each Example is also included. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art or those that are substantially the same.

本発明による実施例に係る排煙脱硫設備について、図面を参照して説明する。図１は、実施例１に係る排煙脱硫設備の概略図である。
図１に示すように、排煙脱硫設備１０Ａは、燃焼排ガス（以下「排ガス」という）１１から硫黄酸化物を、カルシウム化合物を含む吸収液スラリ（以下吸収液スラリともいう）１２により除去する主脱硫装置１３と、該主脱硫装置１３で硫黄酸化物を除去した脱硫ガス１４中に残存する硫黄酸化物を極低濃度までさらに除去する仕上げ脱硫装置１５と、該仕上げ脱硫装置１５に所定濃度のカルシウム化合物を含む吸収液スラリ１２をスケーリング防止用の種晶石膏源として供給する吸収液スラリ供給手段とを具備するものである。なお、図１中、符号１９は主脱硫装置１３からの脱硫ガス１４を仕上げ脱硫装置１５側に供給する煙道を図示する。 A flue gas desulfurization facility according to an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of a flue gas desulfurization facility according to a first embodiment.
As shown in FIG. 1, the flue gas desulfurization facility 10 </ b> A mainly removes sulfur oxide from combustion exhaust gas (hereinafter referred to as “exhaust gas”) 11 with an absorption liquid slurry (hereinafter also referred to as absorption liquid slurry) 12 containing calcium compounds. A desulfurization unit 13, a finish desulfurization unit 15 that further removes sulfur oxide remaining in the desulfurization gas 14 from which sulfur oxides have been removed by the main desulfurization unit 13, and a predetermined concentration in the finish desulfurization unit 15. An absorbent slurry supply means for supplying an absorbent slurry 12 containing a calcium compound as a seed crystal gypsum source for preventing scaling. In FIG. 1, reference numeral 19 denotes a flue for supplying the desulfurization gas 14 from the main desulfurization device 13 to the finishing desulfurization device 15 side.

本実施例では、吸収液スラリ供給手段は、主脱硫装置１３を循環して噴霧ノズル１７より噴出流（液柱）１８を噴出させ、吸収液スラリ１２を循環させる吸収液スラリ循環ラインＬ1と、該吸収液スラリ循環ラインＬ1から分岐され、循環する吸収液スラリ１２の一部を仕上げ脱硫装置１５に供給する吸収液スラリ供給ラインＬ2とから構成されている。
なお、吸収液スラリ循環ラインＬ1には、吸収液スラリ１２の循環をする循環ポンプＰ1が介装されており、吸収液スラリ１２の循環量を制御装置２２により制御している。 In this embodiment, the absorbing liquid slurry supply means circulates the main desulfurization apparatus 13 plume from the spray nozzle 17 (liquid column) 18 is ejected, the absorbing solution slurry circulating line L 1 to circulate the absorption liquid slurry 12 The absorbent slurry supply line L 2 is branched from the absorbent slurry circulating line L 1 and supplies a part of the circulating absorbent slurry 12 to the finishing desulfurizer 15.
The absorption liquid slurry circulation line L 1 is provided with a circulation pump P 1 that circulates the absorption liquid slurry 12, and the amount of circulation of the absorption liquid slurry 12 is controlled by the controller 22.

仕上げ脱硫装置１５に供給された吸収液スラリ１２は、仕上げ脱硫装置１５内に設けられた噴霧ノズル１７より噴出流（液柱）１８を噴出させ、脱硫ガス１４と接触させることで脱硫ガス１４中に残存する硫黄酸化物をさらに除去し浄化ガス１４Ａとして、高深度脱硫を行っている。
なお、落下液はその底部側の貯留部１５ａに貯留される。
貯留された吸収液スラリ１２は、仕上げ脱硫装置１５に介装された抜き出しポンプＰ2及び、吸収液スラリ返送ラインＬ3により主脱硫装置１３に返送している。
なお、仕上げ脱硫装置１５の底部側の貯留部１５ａには液面を監視するレベル計２１が設けられ、その液面の水位を制御装置２２により制御している。 The absorbent slurry 12 supplied to the finishing desulfurization device 15 is spouted from the spray nozzle 17 provided in the finishing desulfurization device 15 and ejected from the sprayed stream (liquid column) 18 and brought into contact with the desulfurization gas 14. Sulfur oxide remaining in the catalyst is further removed to perform high-depth desulfurization as the purified gas 14A.
The falling liquid is stored in the storage portion 15a on the bottom side.
The stored absorbent slurry 12 is returned to the main desulfurizer 13 by the extraction pump P 2 interposed in the finishing desulfurizer 15 and the absorbent slurry return line L 3 .
In addition, a level meter 21 for monitoring the liquid level is provided in the storage portion 15 a on the bottom side of the finishing desulfurization device 15, and the water level of the liquid level is controlled by the control device 22.

すなわち、仕上げ脱硫装置１５に設けたレベル計２１で計測を行い、制御装置２２において、所定のレベル値に達していると判定したら、吸収液スラリ供給ラインＬ2に介装したバルブＶ1又は吸収液スラリ返送ラインＬ3に介装した抜き出しポンプＰ2を制御して、所定の水位を維持するようにしている。 That performs a measurement at the level gauge 21 provided in the finishing desulfurization unit 15, control the apparatus 22, when it is determined to have reached a predetermined level value, the valve V 1 or absorption interposed absorbing solution slurry supply line L 2 The extraction pump P 2 interposed in the liquid slurry return line L 3 is controlled to maintain a predetermined water level.

なお、主脱硫装置１３では、主脱硫装置１３の底部側の貯留部１３ａに貯留された吸収液スラリ１２は、吸収液スラリ抜き出しラインＬ4により、石膏脱水機３１に供給され、ここで固液分離されて石膏３２と脱水濾液３３とに分離される。
分離された脱水濾液３３は、別途排水３４として排水処理されている。なお、脱水濾液３３の一部は、主脱硫装置１３側へ脱水濾液返送ラインＬ5により、返送されて、主脱硫装置１３内での石膏濃度を所定濃度（例えば３０ｗｔ％程度）に制御している。 In the main desulfurization apparatus 13, the main desulfurization apparatus 13 absorbing liquid slurry 12 that has been stored in the storage unit 13a of the bottom side of the the absorbing solution slurry withdrawal line L 4, is fed to the gypsum dewatering machine 31, wherein the solid-liquid Separated into gypsum 32 and dehydrated filtrate 33.
The separated dehydrated filtrate 33 is drained separately as drainage 34. A part of the dehydrated filtrate 33 is returned to the main desulfurization device 13 side by the dehydrated filtrate return line L 5 , and the gypsum concentration in the main desulfurization device 13 is controlled to a predetermined concentration (for example, about 30 wt%). Yes.

本実施例によれば、仕上げ脱硫装置１５において、主脱硫装置１３から所定石膏濃度の吸収液スラリ１２を供給することで、主脱硫装置１３と仕上げ脱硫装置１５とにおいて、吸収液スラリ濃度が同じものが循環されるので、仕上げ脱硫装置１５内に供給する脱硫ガス１４の水分が飽和であっても、仕上げ脱硫装置１５の内部に供給される水（例えば入口ダクトやミストエリミネータの洗浄水等）により吸収液スラリ濃度が薄まることがなくなる。   According to the present embodiment, in the final desulfurization apparatus 15, the absorbent slurry slurry 12 having the predetermined gypsum concentration is supplied from the main desulfurization apparatus 13, so that the main liquid desulfurization apparatus 13 and the final desulfurization apparatus 15 have the same absorption liquid slurry concentration. Since the water is circulated, even if the water content of the desulfurization gas 14 supplied into the finishing desulfurization device 15 is saturated, water supplied into the finishing desulfurization device 15 (for example, cleaning water for an inlet duct or mist eliminator). As a result, the absorbent slurry concentration does not decrease.

この結果、仕上げ脱硫装置１５内での種晶石膏濃度が極端に薄いような設計条件とする場合に較べて、石膏付着核の場（表面積）が大きくなり、石膏過飽和度が小さくなり、仕上げ脱硫装置１５の壁面や構造物、配管等の表面上における石膏の成長が防止される。   As a result, the gypsum adhering nucleus field (surface area) is increased, the gypsum supersaturation level is reduced, and the final desulfurization is performed as compared with the design condition in which the seed crystal gypsum concentration in the finishing desulfurization apparatus 15 is extremely thin. The growth of gypsum on the surface of the wall surface of the device 15, the structure, the piping, etc. is prevented.

これに対し、仕上げ脱硫装置１５内での種晶石膏濃度が極端に薄い設計条件とする場合には、石膏付着核の場（表面積）が極めて小さくなる事で、石膏過飽和度が大きくなる可能性がある。この石膏過飽和度が大きくなると、仕上げ脱硫装置１５内の壁面や構造物、配管等の表面上に石膏が成長し、これが振動や発停時のヒートショック等で剥離し、このスケール片が循環液に混入し、吸収塔スプレーパイプ内部やノズルを閉塞させる結果、脱硫・除塵性能低下に至るおそれがある。   On the other hand, if the seed crystal gypsum concentration in the finishing desulfurization apparatus 15 is designed to be extremely thin, the gypsum supersaturation degree may increase because the gypsum adhering nucleus field (surface area) becomes extremely small. There is. When this gypsum supersaturation level increases, gypsum grows on the surface of the wall surface, structure, piping, etc. in the finishing desulfurization unit 15 and peels off due to vibration or heat shock at the time of starting and stopping. As a result, the desulfurization / dust removal performance may be degraded.

本発明では、主脱硫装置１３側と仕上げ脱硫装置１５側とを同一の濃度（例えば２０〜３０ｗｔ％）の吸収液スラリ１２を用いて共有することで、仕上げ脱硫装置１５におけるスケール発生を防止することができ、安定した継続的な脱硫操業が可能となる。   In the present invention, the main desulfurization device 13 side and the finish desulfurization device 15 side are shared by using the absorbent slurry 12 having the same concentration (for example, 20 to 30 wt%), thereby preventing scale generation in the finish desulfurization device 15. And a stable and continuous desulfurization operation becomes possible.

本発明による実施例に係る排煙脱硫設備について、図面を参照して説明する。図２−１及び図２−２は、実施例２に係る排煙脱硫設備の概略図である。なお、実施例１の構成部材と同一の部材については、同一の符号を付してその説明は省略する。
図２−１に示すように、実施例２に係る排煙脱硫設備１０Ｂは、主脱硫装置１３を循環する吸収液スラリの一部をスケーリング防止用の種晶石膏源として仕上げ脱硫装置１５に供給する吸収液スラリ供給ラインＬ2と、前記仕上げ脱硫装置１５内の吸収液スラリ濃度をスケーリング防止用の種晶石膏源として機能する所定設定値に調整する吸収液濃度調整手段と、を具備するものである。 A flue gas desulfurization facility according to an embodiment of the present invention will be described with reference to the drawings. FIGS. 2-1 and 2-2 are schematic views of the flue gas desulfurization facility according to the second embodiment. In addition, about the member same as the structural member of Example 1, the same code | symbol is attached | subjected and the description is abbreviate | omitted.
As shown in FIG. 2A, the flue gas desulfurization facility 10B according to the second embodiment supplies a part of the absorbent slurry circulating through the main desulfurization device 13 to the finishing desulfurization device 15 as a seed crystal gypsum source for preventing scaling. that the absorbing liquid slurry supply line L 2 which comprises a, and absorbing liquid concentration adjusting means for adjusting a predetermined setting value that serves the absorbing solution slurry concentration in the finishing desulfurization apparatus 15 as a seed crystal gypsum source for scaling prevention It is.

本実施例では、主脱硫装置１３から濃い吸収液スラリ（例えば所定石膏濃度２０〜３０ｗｔ％）のものを仕上げ脱硫装置１５に送液しつつ、仕上げ脱硫装置１５で測定する密度計２３の値を主脱硫装置１３からの供給バルブＶ1と連動させ、仕上げ脱硫装置１５における吸収液スラリの石膏濃度を、主脱硫装置１３の吸収液スラリ濃度の半分程度の所定濃度（例えば石膏濃度１０〜２０ｗｔ％）に調整している。
なお、仕上げ脱硫装置１５での循環した吸収液１２Ａは、仕上げ脱硫性能に寄与して落下し、底部側の貯留部１５ａに貯留される。 In this embodiment, the density of the density meter 23 measured by the finishing desulfurization device 15 is sent from the main desulfurization device 13 to the final desulfurization device 15 while supplying a thick absorbent slurry (for example, a predetermined gypsum concentration of 20 to 30 wt%). In conjunction with the supply valve V 1 from the main desulfurization device 13, the gypsum concentration of the absorbent slurry in the finishing desulfurization device 15 is set to a predetermined concentration (for example, a gypsum concentration of 10 to 20 wt%) that is about half of the absorption slurry concentration of the main desulfurization device 13. ).
In addition, the absorption liquid 12A circulated in the finishing desulfurization device 15 contributes to the finishing desulfurization performance and falls and is stored in the storage portion 15a on the bottom side.

ここで、仕上げ脱硫装置１５内を循環する吸収液スラリ１２Ａの密度計２３の密度（ρ）としては、石膏濃度が１０〜２０ｗｔ％程度の１．０６〜１．１５の範囲とするのが好ましい。   Here, the density (ρ) of the density meter 23 of the absorbent slurry 12A circulating in the finishing desulfurization apparatus 15 is preferably in the range of 1.06 to 1.15 where the gypsum concentration is about 10 to 20 wt%. .

なお、貯留された吸収液スラリ１２Ａ（所定石膏濃度１０〜２０ｗｔ％）は、吸収液スラリ返送ラインＬ3により主脱硫装置１３に返送している。
その際、仕上げ脱硫装置１５のレベル計２１と返送バルブＶ3とも連動させて仕上げ脱硫装置１５の液位を一定に保つようにしている。
なお、吸収液スラリ１２Ａは、吸収液スラリ循環ラインＬ10を介して仕上げ脱硫装置１５内を循環させている。 Incidentally, pooled absorption liquid slurry 12A (predetermined gypsum concentration 10-20 wt%) is returned to the main desulfurization apparatus 13 by the absorbing solution slurry return line L 3.
At that time, the level gauge 21 of the finishing desulfurization device 15 and the return valve V 3 are interlocked to keep the liquid level of the finishing desulfurization device 15 constant.
The absorption liquid slurry 12A is circulated through the finishing desulfurization unit 15 through the absorbing solution slurry circulating line L 10.

また、仕上げ脱硫装置１５に供給する貯留部１５ａの内部には、整流格子２４を設けている。これにより、仕上げ脱硫装置１５内に吹き出され、投入箇所でのスラリ密度の変動による不均一化を防止している。   In addition, a rectifying grid 24 is provided inside the reservoir 15 a that supplies the finishing desulfurization device 15. Thereby, it blows off in the finishing desulfurization apparatus 15, and prevents the nonuniformization by the fluctuation | variation of the slurry density in a charging location.

また、仕上げ脱硫装置１５内部には、攪拌機２５を設置して、仕上げ脱硫装置１５内部全体に攪拌力を行渡らせるようにしている。   In addition, a stirrer 25 is installed inside the finish desulfurization device 15 so that the stirring force is distributed throughout the finish desulfurization device 15.

ここで、排煙脱硫設備１０Ｂの設置初期乃至定期修繕後の再起動当初における吸収液スラリ１２は、主脱硫装置１３側において、所定最低濃度（例えば石膏濃度５ｗｔ％）の薄い濃度の吸収液スラリとした後、その薄い濃度の吸収液スラリ１２を仕上げ脱硫装置１５側に吸収液スラリ供給ラインＬ2を介して供給する。そして、排煙脱硫装置の運転を開始して、主脱硫装置１３では、石膏濃度を所定の例えば３０ｗｔ％とする。一方、仕上げ脱硫装置１５側では、目標の１０〜２０ｗｔ％に達した後には、その後、密度計２３によりその目標濃度を監視し、必要に応じて、バルブＶ1を操作して、仕上げ脱硫装置１５側へ濃い濃度の吸収液スラリ１２を供給するようにすればよい。 Here, the absorbent slurry 12 at the initial stage of installation of the flue gas desulfurization facility 10B or at the beginning of restart after periodic repair is a thin absorbent slurry having a predetermined minimum concentration (for example, a gypsum concentration of 5 wt%) on the main desulfurization device 13 side. after the supply through the absorbing solution slurry supply line L 2 to the desulfurization apparatus 15 side finishing absorption liquid slurry 12 of the low concentration. Then, the operation of the flue gas desulfurization apparatus is started, and the main desulfurization apparatus 13 sets the gypsum concentration to a predetermined value, for example, 30 wt%. On the other hand, in the finishing desulfurization unit 15 side, after reaching the 10-20 wt% of the goal, then the target density is monitored by the density meter 23, as required, by operating the valves V 1, finishing desulfurizer What is necessary is just to make it supply the absorption liquid slurry 12 of a deep density | concentration to 15 side.

また、本実施例では、図２−２に示す他の排煙脱硫設備１０Ｂのように、仕上げ脱硫装置１５内を循環する循環吸収液スラリ１２Ａの一部（※１）を、吸収液スラリ供給ラインＬ2に導入して、吸収液スラリの濃度を所定濃度とした後に、仕上げ脱硫装置１５内に供給するようにしてもよい。これにより例えば３０ｗｔ％という主脱硫装置１３からの濃い石膏濃度の吸収液スラリ１２の投入が防止され、投入箇所でのスラリ密度の変動による不均一化を抑制するようにしている。 Further, in this embodiment, as in the other flue gas desulfurization equipment 10B shown in FIG. 2-2, a part (* 1) of the circulating absorbent slurry 12A circulating in the finishing desulfurizer 15 is supplied to the absorbent slurry. It may be introduced into the line L 2 and supplied to the finishing desulfurization apparatus 15 after the concentration of the absorbent slurry is set to a predetermined concentration. Thereby, for example, the absorption liquid slurry 12 having a high gypsum concentration from the main desulfurization apparatus 13 of 30 wt% is prevented, and unevenness due to fluctuations in the slurry density at the input location is suppressed.

この際、薄め液として、濃度の調整を循環する吸収液スラリ１２Ａを用いても良く、これにより系内の水バランスが崩れることがないものとなる。   At this time, an absorbing liquid slurry 12A that circulates the concentration adjustment may be used as the diluting liquid, so that the water balance in the system is not lost.

本発明による実施例に係る排煙脱硫設備について、図面を参照して説明する。図３−１乃至図３−４は、実施例３に係る排煙脱硫設備の概略図である。
図３−１に示すように、実施例３に係る排煙脱硫設備１０Ｃ−１は、主脱硫装置１３から抜き出した吸収液スラリ１２から固液分離した石膏３２（※２）を石膏スラリ４１にスラリ化するスラリホッパ４２と、得られた石膏スラリ４１を仕上げ脱硫装置１５内に供給する石膏スラリ供給ラインＬ11とを具備するものである。 A flue gas desulfurization facility according to an embodiment of the present invention will be described with reference to the drawings. 3A to 3D are schematic views of the flue gas desulfurization facility according to the third embodiment.
As shown in FIG. 3A, the flue gas desulfurization facility 10 </ b> C- 1 according to the third embodiment uses gypsum 32 (* 2) separated from the absorbent slurry 12 extracted from the main desulfurizer 13 as a gypsum slurry 41. A slurry hopper 42 for slurrying and a gypsum slurry supply line L 11 for supplying the obtained gypsum slurry 41 into the finishing desulfurization apparatus 15 are provided.

この際、仕上げ脱硫装置１５の液密度を常時密度計２３で測定し、この値で投入する量を制御して、吸収液スラリ濃度を調節するようにしている。   At this time, the liquid density of the finishing desulfurization apparatus 15 is constantly measured by the density meter 23, and the amount of the charged liquid is controlled by adjusting the amount to be charged with this value.

本実施例では、石膏脱水機３１から分離された石膏３２を仕上げ脱硫装置に供給し、所定の石膏濃度とすることで、スケールの防止を図るようにしている。   In the present embodiment, the gypsum 32 separated from the gypsum dewatering machine 31 is supplied to the finishing desulfurization apparatus to obtain a predetermined gypsum concentration, thereby preventing scale.

図３−２は、実施例３に係る他の排煙脱硫設備の概略図である。
図３−２に示す排煙脱硫設備１０Ｃ−２においては、石膏３２以外に石灰石４４をスラリホッパ４２に投入し、これらの混合物である石膏・石灰石スラリ４５を仕上げ脱硫装置１５内にスラリ供給ラインＬ11により供給するようにしている。 FIG. 3-2 is a schematic diagram of another flue gas desulfurization facility according to the third embodiment.
In the flue gas desulfurization facility 10C-2 shown in FIG. 3-2, limestone 44 is put into the slurry hopper 42 in addition to the gypsum 32, and the gypsum / limestone slurry 45, which is a mixture of these, is put into the finishing desulfurization apparatus 15 with the slurry supply line L. 11 to supply.

図３−３は、実施例３に係る他の排煙脱硫設備の概略図である。
図３−３に示す排煙脱硫設備１０Ｃ−３においては、石膏脱水機３１で分離した石膏３２をベルトコンベヤにより投入ホッパ４６に直接粉体のまま供給し、粉体の石膏３２を直接仕上げ脱硫装置１５内に供給するようにしている。 FIG. 3C is a schematic diagram of another flue gas desulfurization facility according to the third embodiment.
In the flue gas desulfurization facility 10C-3 shown in FIG. 3C, the gypsum 32 separated by the gypsum dewatering machine 31 is directly supplied as powder to the input hopper 46 by a belt conveyor, and the powder gypsum 32 is directly finished and desulfurized. It is made to supply in the apparatus 15.

この際、仕上げ脱硫装置１５内を循環させる吸収液スラリ循環ラインＬ10をから一部分岐した分岐ラインＬ11より、吸収液スラリ４１を抜き出して投入ホッパ４６に供給してスラリー化させ、重力により仕上げ脱硫装置１５の底部に吸収液スラリ４１を供給している。この際、供給する石膏３２の量は、密度計２３と連動して吸収液スラリ４１の調整を図るようにしている。 In this case, the branch line L 11 that is partially branched from the absorption liquid slurry circulating line L 10 that circulates the inside finishing desulfurization unit 15, and supplies to the feeding hopper 46 by extracting absorbing solution slurry 41 is slurried, finished by gravity An absorbent slurry 41 is supplied to the bottom of the desulfurization device 15. At this time, the amount of gypsum 32 to be supplied is adjusted to the absorbent slurry 41 in conjunction with the density meter 23.

図３−４は、実施例３に係る他の排煙脱硫設備の概略図である。
図３−４に示す排煙脱硫設備１０Ｃ−４においては、排煙脱硫設備１０Ｃ−３において、投入ホッパ４６に、さらに粉体の石灰石４４を投入し、粉体の混合物（石膏３２、石灰石４４）４７を直接仕上げ脱硫装置１５内に直接供給するようにしている。
なお、石膏３２のみを投入ホッパ４６に投入して、石灰石４４を直接仕上げ脱硫装置１５内に直接供給するようにしてもよい。 FIG. 3-4 is a schematic diagram of another flue gas desulfurization facility according to the third embodiment.
In the flue gas desulfurization facility 10C-4 shown in FIG. 3-4, in the flue gas desulfurization facility 10C-3, the powder limestone 44 is further charged into the charging hopper 46, and the powder mixture (gypsum 32, limestone 44). 47) is directly supplied into the finishing desulfurization apparatus 15.
Note that only the gypsum 32 may be input to the input hopper 46 and the limestone 44 may be directly supplied into the finishing desulfurization apparatus 15.

本発明による実施例に係る排煙脱硫設備について、図面を参照して説明する。図４は、実施例３に係る排煙脱硫設備の概略図である。
図４に示すように、実施例４に係る排煙脱硫設備１０Ｄは、実施例１の排煙脱硫設備１０Ａにおいて、さらに仕上げ脱硫装置１５内に強アルカリ５２を、強アルカリ槽５１かアルカリ供給ラインＬ7を介して供給する強アルカリ供給手段を備えている。 A flue gas desulfurization facility according to an embodiment of the present invention will be described with reference to the drawings. FIG. 4 is a schematic view of the flue gas desulfurization facility according to the third embodiment.
As shown in FIG. 4, the flue gas desulfurization facility 10D according to the fourth embodiment is the same as the flue gas desulfurization facility 10A according to the first embodiment. Strong alkali supply means for supplying via L 7 is provided.

本実施例では、実施例１乃至３の仕上げ脱硫装置１５の内部の運転状態を正常に保つことを目的として、仕上げ脱硫装置１５で使用する吸収液スラリ１２のカルシウム化合物以外の吸収液の種類を適宜入れ替えたり、混合したりしている。   In this embodiment, for the purpose of maintaining the normal operation state of the finishing desulfurization apparatus 15 of Examples 1 to 3, the type of the absorbing liquid other than the calcium compound of the absorbing slurry 12 used in the finishing desulfurization apparatus 15 is selected. They are replaced or mixed as appropriate.

この切り替えは、オンラインもしくはオフラインで行うことが可能であり、その切替タイミングは、計器信号（基準条件での脱硫性能、石灰石の活性、基準ガス量における仕上げ脱硫装置ガス圧損等）を解析することで切替タイミングを決定するようにしている。   This switching can be performed online or offline, and the switching timing is determined by analyzing instrument signals (desulfurization performance under reference conditions, limestone activity, finish desulfurizer gas pressure loss at reference gas amount, etc.). The switching timing is determined.

吸収液スラリ１２としてカルシウム化合物の吸収液から、強アルカリ吸収液に切替える制御を制御手段２２で行い、バルブＶ4を開放した後、強アルカリ槽５１から強アルカリ５２をポンプＰ7により送給している。
この強アルカリ吸収液の使用によって、ガス境膜抵抗の低減を図り、脱硫性能を向上するようにしている。 From the absorption solution of the calcium compound as the absorbent liquid slurry 12 performs control to switch to the strong alkaline liquid absorbent with control means 22, after opening the valve V 4, the strongly alkaline 52 from strongly alkaline bath 51 feed by a pump P 7 feeds ing.
By using this strong alkali absorbing solution, the gas film resistance is reduced and the desulfurization performance is improved.

ここで、強アルカリ吸収液としては、ＮａＯＨ、Ｎａ2ＣＯ3、ＮａＨＣＯ3、Ｍｇ（ＯＨ）2等を用いることができるが、本発明はこれらに限定されるものではない。 Here, NaOH, Na 2 CO 3 , NaHCO 3 , Mg (OH) 2 or the like can be used as the strong alkali absorbing solution, but the present invention is not limited to these.

このような強アルカリ５２に切り替えることで、不具合発生時においても迅速に対応できることとなる。   By switching to such a strong alkali 52, it is possible to respond quickly even when a problem occurs.

本発明による実施例５に係る排ガス処理システムの概略構成図を図５に示す。
図５に示すように、実施例４に係る排ガス処理システム１００は、例えばボイラ１０１からの排ガス１１中の窒素酸化物を除去する脱硝装置１０２と、窒素酸化物除去後のガス中の熱を回収するエアヒータ１０３と、熱回収後のガス中の煤塵を除去する電気集塵機１０４と、除塵後のガス中の硫黄酸化物を除去する主脱硫装置１３と仕上げ脱硫装置１５とを具備する排煙脱硫装置と、浄化ガス１４Ａ中の二酸化炭素を回収するＣＯ2回収装置１０６と、ＣＯ2回収後の浄化ガス１１２を外部に排出する煙突１１１とを具備するものである。 FIG. 5 shows a schematic configuration diagram of an exhaust gas treatment system according to Embodiment 5 of the present invention.
As shown in FIG. 5, the exhaust gas treatment system 100 according to the fourth embodiment recovers the heat in the gas after removing the NOx removal device 102 that removes nitrogen oxide in the exhaust gas 11 from the boiler 101, for example. Flue gas desulfurization device comprising: an air heater 103 that performs the above operation, an electric dust collector 104 that removes dust in the gas after heat recovery, a main desulfurization device 13 that removes sulfur oxide in the gas after dust removal, and a final desulfurization device 15 And a CO 2 recovery device 106 that recovers carbon dioxide in the purified gas 14A, and a chimney 111 that discharges the purified gas 112 after CO 2 recovery to the outside.

よって、仕上げ排煙脱硫装置１５の後段側に設置されるＣＯ2回収装置１０６に供給される浄化ガス１１２は、硫黄酸化物の濃度が極めて少なくなるので、ＣＯ2回収装置１０６で循環して利用されるＣＯ2吸収液（例えばアミン吸収液）中における硫黄酸化物や煤塵の蓄積が少なくなり、劣化を抑制することができる。
この結果、ＣＯ2吸収液が劣化に起因するＣＯ2吸収性能の低下が少なくなり、安定してＣＯ2の回収を行うことができる。 Therefore, the purified gas 112 supplied to the CO 2 recovery device 106 installed on the rear stage side of the finish flue gas desulfurization device 15 has a very low concentration of sulfur oxide, and is circulated and used in the CO 2 recovery device 106. Accumulation of sulfur oxides and soot and dust in the CO 2 absorbing liquid (for example, amine absorbing liquid) is reduced, and deterioration can be suppressed.
As a result, reduction of CO 2 absorption performance of the CO 2 absorbing liquid due to the deterioration is reduced, it is possible to perform stable recovery of CO 2.

また、ＣＯ2吸収性能の低下を補うために、ＣＯ2吸収性能の追加供給の回数と供給量が少なくなると共に、ＣＯ2吸収性能の回復のためのリクレーミング頻度の増大がなくなり、排ガス処理システムにおけるランニングコストの削減を図ることができる。 Further, in order to compensate for the decrease of CO 2 absorption performance, the number of times the supply amount of the additional supply of CO 2 absorption performance is reduced, there is no increase in the reclaiming frequency for recovery of CO 2 absorption performance, in the exhaust gas treatment system Running costs can be reduced.

１０Ａ〜１０Ｄ 排煙脱硫設備
１１ 排ガス
１２ カルシウム化合物を含む吸収液スラリ（吸収液スラリ）
１３ 主脱硫装置
１４ 脱硫ガス
１５ 仕上げ脱硫装置
１００ 排ガス処理システム
１０１ ボイラ
１０２ 脱硝装置
１０３ エアヒータ
１０４ 電気集塵機
１０５ 脱硫装置
１０６ ＣＯ2回収装置
１１１ 煙突 10A to 10D Flue gas desulfurization equipment 11 Exhaust gas 12 Absorption liquid slurry containing calcium compound (absorption liquid slurry)
13 main desulfurization apparatus 14 desulfurized gas 15 finishing desulfurization unit 100 exhaust gas treatment system 101 boiler 102 denitration apparatus 103 air heater 104 electrostatic precipitator 105 desulfurizer 106 CO 2 recovering apparatus 111 chimney

Claims (6)

燃焼排ガスから硫黄酸化物を、カルシウム化合物を含む吸収液スラリにより除去する主脱硫装置と、
該主脱硫装置で硫黄酸化物を除去した脱硫ガス中に残存する硫黄酸化物を極低濃度までさらに除去する仕上げ脱硫装置と、
該仕上げ脱硫装置に所定濃度のカルシウム化合物を含む吸収液スラリをスケーリング防止用の種晶石膏源として供給する吸収液スラリ供給手段とを具備することを特徴とする排煙脱硫設備。 A main desulfurization device for removing sulfur oxides from combustion exhaust gas with an absorbent slurry containing a calcium compound;
A finish desulfurization apparatus that further removes sulfur oxide remaining in the desulfurization gas from which sulfur oxide has been removed by the main desulfurization apparatus to an extremely low concentration;
A flue gas desulfurization facility comprising: an absorbent slurry supply means for supplying an absorbent slurry containing a calcium compound at a predetermined concentration as a seed crystal gypsum source for preventing scaling to the finishing desulfurization apparatus. 請求項１において、
前記吸収液スラリ供給手段が、
前記主脱硫装置を循環する吸収液スラリ循環ラインと、
該吸収液スラリ循環ラインから分岐され、循環する吸収液スラリの一部をスケーリング防止用の種晶石膏源として仕上げ脱硫装置に供給する吸収液スラリ供給ラインとを具備することを特徴とする排煙脱硫設備。 In claim 1,
The absorbent slurry supply means is
An absorbent slurry circulation line that circulates through the main desulfurization unit;
A flue gas characterized by comprising an absorption liquid slurry supply line branched from the absorption liquid slurry circulation line and supplying a part of the circulating absorption liquid slurry to a finishing desulfurization apparatus as a seed crystal gypsum source for preventing scaling Desulfurization equipment. 請求項１において、
前記吸収液スラリ供給手段が、
前記主脱硫装置を循環する吸収液スラリ循環ラインと、
該吸収液スラリ循環ラインから分岐され、循環する吸収液スラリの一部をスケーリング防止用の種晶石膏源として仕上げ脱硫装置に供給する吸収液スラリ供給ラインと、
前記仕上げ脱硫装置内の吸収液スラリ濃度をスケーリング防止用の種晶石膏源として機能する所定設定値に調整する吸収液濃度調整手段と、を具備することを特徴とする排煙脱硫設備。 In claim 1,
The absorbent slurry supply means is
An absorbent slurry circulation line that circulates through the main desulfurization unit;
An absorption liquid slurry supply line which is branched from the absorption liquid slurry circulation line and supplies a part of the circulating absorption liquid slurry to the finishing desulfurization apparatus as a seed crystal gypsum source for preventing scaling;
Absorbent liquid desulfurization equipment, comprising: an absorbent concentration adjusting means for adjusting an absorbent slurry concentration in the finishing desulfurization apparatus to a predetermined set value that functions as a seed crystal gypsum source for preventing scaling. 請求項１において、
前記吸収液スラリ供給手段が、
前記主脱硫装置から抜き出した吸収液スラリから固液分離した石膏をスラリ化するスラリホッパと、
該石膏スラリを仕上げ脱硫装置にスケーリング防止用の種晶石膏源として供給する石膏スラリ供給ラインとを具備することを特徴とする排煙脱硫設備。 In claim 1,
The absorbent slurry supply means is
A slurry hopper for slurrying gypsum separated into solid and liquid from the absorbent slurry extracted from the main desulfurization device;
A flue gas desulfurization facility comprising a gypsum slurry supply line for supplying the gypsum slurry to a finishing desulfurization apparatus as a seed crystal gypsum source for preventing scaling. 請求項１乃至４のいずれか一つにおいて、
前記仕上げ脱硫装置内に強アルカリを供給する強アルカリ供給手段を具備することを特徴とする排煙脱硫設備。 In any one of Claims 1 thru | or 4,
A flue gas desulfurization facility comprising strong alkali supply means for supplying strong alkali into the finishing desulfurization apparatus. ボイラ等からの排ガス中の窒素酸化物を除去する脱硝装置と、窒素酸化物除去後のガス中の煤塵を除去する集塵機と、除塵後のガス中の硫黄酸化物を除去する脱硫装置と、この脱硫後の排ガス中に残存する硫黄酸化物を極低濃度までさらに除去する請求項１乃至５のいずれか一つの排煙脱硫設備と、浄化ガス中の二酸化炭素を回収するＣＯ2回収装置とを具備することを特徴とする排ガス処理システム。 A denitration device that removes nitrogen oxides in exhaust gas from boilers, a dust collector that removes soot and dust in the gas after removal of nitrogen oxides, a desulfurization device that removes sulfur oxides in the gas after dust removal, A flue gas desulfurization facility according to any one of claims 1 to 5, wherein the sulfur oxide remaining in the exhaust gas after desulfurization is further removed to an extremely low concentration, and a CO 2 recovery device for recovering carbon dioxide in the purified gas. An exhaust gas treatment system comprising:
JP2011116094A 2011-05-24 2011-05-24 Flue gas desulfurization equipment provided with flue gas finishing desulfurization device, and exhaust gas treatment system using the same Withdrawn JP2012240034A (en)

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