JP5773687B2 - Seawater flue gas desulfurization system and power generation system - Google Patents

Seawater flue gas desulfurization system and power generation system Download PDF

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JP5773687B2
JP5773687B2 JP2011042962A JP2011042962A JP5773687B2 JP 5773687 B2 JP5773687 B2 JP 5773687B2 JP 2011042962 A JP2011042962 A JP 2011042962A JP 2011042962 A JP2011042962 A JP 2011042962A JP 5773687 B2 JP5773687 B2 JP 5773687B2
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seawater
flue gas
gas desulfurization
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exhaust gas
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JP2012179521A5 (en
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貴志 吉元
貴志 吉元
晴治 香川
晴治 香川
裕 中小路
裕 中小路
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三菱日立パワーシステムズ株式会社
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/20Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/50Sulfur oxides
    • B01D53/501Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/72Treatment of water, waste water, or sewage by oxidation
    • C02F1/74Treatment of water, waste water, or sewage by oxidation with air
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01KSTEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K9/00Plants characterised by condensers arranged or modified to co-operate with the engines
    • F01K9/003Plants characterised by condensers arranged or modified to co-operate with the engines condenser cooling circuits
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00Methods of steam generation characterised by form of heating method
    • F22B1/02Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/02Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2252/00Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10Inorganic absorbents
    • B01D2252/103Water
    • B01D2252/1035Sea water
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08Seawater, e.g. for desalination
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00Treatment devices
    • F23J2219/40Sorption with wet devices, e.g. scrubbers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15041Means for absorbing SOx using seawater

Description

本発明は、石炭焚き、原油焚き及び重油焚き等の工業燃焼設備等から排出される排ガス中の硫黄酸化物を、海水を用いて脱硫する海水排煙脱硫システムおよび発電システムに関する。   The present invention relates to a seawater flue gas desulfurization system and a power generation system that use seawater to desulfurize sulfur oxides in exhaust gas discharged from industrial combustion facilities such as coal burning, crude oil burning, and heavy oil burning.

石炭や原油等を燃料とする発電プラントにおいて、石炭等の化石燃料を燃焼することでボイラから排出される燃焼排気ガス(以下、「排ガス」と呼ぶ)には硫黄酸化物(SOx)など硫黄分が含まれる。そのため、排ガスは、脱硫処理され、排ガス中に含まれている二酸化硫黄(SO2)等のSOxを除去してから大気に放出される。このような脱硫処理方法として、石灰石石膏法、スプレードライヤー法及び海水法等がある。 In a power plant using coal or crude oil as fuel, combustion exhaust gas (hereinafter referred to as “exhaust gas”) discharged from a boiler by burning fossil fuel such as coal contains sulfur content such as sulfur oxide (SOx). Is included. Therefore, the exhaust gas is subjected to a desulfurization treatment, and after removing SOx such as sulfur dioxide (SO 2 ) contained in the exhaust gas, it is released to the atmosphere. Examples of such a desulfurization method include a limestone gypsum method, a spray dryer method, and a seawater method.

発電所などは大量の冷却水を必要とするため海に面した場所に建設される場合が多い。そのため、脱硫処理に要する稼動コストを抑えることなどの観点から、海水を排ガス中の硫黄酸化物を吸収する吸収液として利用して脱硫を行う海水脱硫を用いた海水排煙脱硫装置が提案されている。   Power plants are often constructed in locations facing the sea because they require a large amount of cooling water. For this reason, a seawater flue gas desulfurization apparatus using seawater desulfurization that performs desulfurization using seawater as an absorbing liquid that absorbs sulfur oxide in exhaust gas has been proposed from the viewpoint of suppressing the operating cost required for the desulfurization treatment. Yes.

海水排煙脱硫装置は、略円筒のような筒形状又は角形状を縦置きにした脱硫塔(吸収塔)の内部に海水及びボイラ排ガスを供給し、海水を吸収液として気液接触させることでSOxを除去している。脱硫塔内で吸収剤として使用した脱硫後の海水(硫黄分吸収海水)は、たとえば、上部が開放された長い水路(Seawater Oxidation Treatment System;SOTS)内を流れ、海水と混合して希釈されて排出される。硫黄分吸収海水は、水路の一部の底面に設置したエアレーション装置から流出される微細気泡によって脱炭酸(爆気)される(例えば、特許文献1〜3参照)。   Seawater flue gas desulfurization equipment supplies seawater and boiler exhaust gas into a desulfurization tower (absorption tower) that has a cylindrical shape or a rectangular shape such as a substantially cylindrical shape placed vertically, and makes seawater gas-liquid contact as an absorption liquid. SOx is removed. The desulfurized seawater (sulfur content-absorbing seawater) used as an absorbent in the desulfurization tower flows, for example, in a long water channel (Seawater Oxidation Treatment System; SOTS) with an open top, and is mixed with seawater and diluted. Discharged. The sulfur-absorbing seawater is decarboxylated (explosion) by fine bubbles flowing out from an aeration apparatus installed on a part of the bottom of the water channel (see, for example, Patent Documents 1 to 3).

海水排煙脱硫装置では、海水を用いて脱硫を行う場合、脱硫塔内に供給される排ガスと脱硫塔の外部に排出される排ガスとの比から求められる排ガスの脱硫率は、所定値(例えば、90%程度)となるように調整している。   In the seawater flue gas desulfurization apparatus, when desulfurization is performed using seawater, the desulfurization rate of the exhaust gas obtained from the ratio of the exhaust gas supplied into the desulfurization tower and the exhaust gas discharged outside the desulfurization tower is a predetermined value (for example, , About 90%).

特開2006−055779号公報JP 2006-055779 A 特開2009−028570号公報JP 2009-028570 A 特開2009−028572号公報JP 2009-028572 A

海水を用いて脱硫を行う場合、海水のアルカリ度、海水温度、海水のpH、脱硫した海水中に含まれる硫酸イオン(SO4 2-)濃度などの海水性状に応じて、排ガスの脱硫率が所定値(例えば、90%程度)よりも高くなる場合がある。 When desulfurization is performed using seawater, the desulfurization rate of exhaust gas depends on the seawater properties such as the alkalinity of seawater, seawater temperature, seawater pH, and the concentration of sulfate ion (SO 4 2- ) contained in the desulfurized seawater. It may be higher than a predetermined value (for example, about 90%).

海水を脱硫塔内に供給する際、海水の供給量の調整はポンプを運転する台数を変更して制御を行なうようにしているため、脱硫塔内に供給する海水の供給量の微調整は困難である。そのため、排ガスの脱硫率が所定値よりも高くなった場合、排ガスの脱硫率の微調整が困難である、という問題がある。   When supplying seawater into the desulfurization tower, adjustment of the seawater supply volume is controlled by changing the number of pumps operated, so fine adjustment of the seawater supply volume supplied into the desulfurization tower is difficult. It is. Therefore, when the desulfurization rate of exhaust gas becomes higher than a predetermined value, there is a problem that fine adjustment of the desulfurization rate of exhaust gas is difficult.

本発明は、前記課題に鑑み、排ガスの脱硫率の調整を容易に行うことができる海水排煙脱硫システムおよび発電システムを提供することを課題とする。   In view of the above problems, an object of the present invention is to provide a seawater flue gas desulfurization system and a power generation system that can easily adjust the desulfurization rate of exhaust gas.

上述した課題を解決するための本発明の第1の発明は、排ガスと海水とを気液接触して前記排ガスを洗浄する排煙脱硫吸収塔と、前記排煙脱硫吸収塔の後流側に設けられ、硫黄分を含んだ硫黄分吸収海水を希釈用の海水と希釈混合する希釈混合槽と、前記海水を前記排煙脱硫吸収塔に供給する海水供給ラインと、前記海水供給ラインから分岐され、希釈海水を供給する希釈海水供給ラインと、希釈海水の分岐部の後流側で、前記海水供給ラインから第1の分岐部で分岐され、前記希釈混合槽に余剰海水を供給する第1の余剰海水分岐配管と、前記排煙脱硫吸収塔内の前記海水供給ラインの第2の分岐部で、該海水供給ラインから分岐され、前記希釈混合槽に余剰海水を供給する第2の余剰海水分岐配管と、を備えると共に、排煙脱硫吸収塔に供給される排ガス中の入口SO 2 濃度と出口SO 2 濃度との比(出口SO 2 濃度/入口SO 2 濃度)と、硫黄分吸収海水の海水性状とに基づいて第1余剰海水分岐配管、第2余剰海水分岐配管から抜き出される余剰海水の量を調整することで、前記排煙脱硫吸収塔内の前記海水の噴霧量を調節することを特徴とする海水排煙脱硫システムである。 The first invention of the present invention for solving the above-mentioned problems is a flue gas desulfurization absorption tower that cleans the flue gas by contacting the exhaust gas and seawater in a gas-liquid manner, and a downstream side of the flue gas desulfurization absorption tower. A diluting / mixing tank for diluting and mixing sulfur-absorbing seawater containing sulfur with seawater for dilution, a seawater supply line for supplying the seawater to the flue gas desulfurization absorption tower, and branched from the seawater supply line A first diverted seawater supply line for supplying dilute seawater and a diverted seawater branching section downstream from the seawater supply line at the first diverging section to supply surplus seawater to the dilution mixing tank A second surplus seawater branch that is branched from the seawater supply line at the second branch of the seawater supply line in the flue gas desulfurization absorption tower and supplies the surplus seawater to the dilution mixing tank And a flue gas desulfurization absorption tower. The ratio of the inlet SO 2 concentration and the outlet SO 2 concentration in the exhaust gas to be fed (the outlet SO 2 concentration / inlet SO 2 concentration), the first surplus seawater branch pipes on the basis of the seawater properties of sulfur absorbing seawater, the The seawater flue gas desulfurization system is characterized in that the amount of the seawater sprayed in the flue gas desulfurization absorption tower is adjusted by adjusting the amount of surplus seawater extracted from the 2 surplus seawater branch piping .

第2の発明は、第1の発明において、前記余剰海水分岐配管の分岐部は、前記海水供給ラインに設けられる海水送給ポンプの後流側に設けられることを特徴とする海水排煙脱硫システムである。   A second aspect of the present invention is the seawater flue gas desulfurization system according to the first aspect, wherein the branch portion of the surplus seawater branch pipe is provided on the downstream side of the seawater feed pump provided in the seawater supply line. It is.

第3の発明は、第1または第2の発明において、前前記排煙脱硫吸収塔、前記希釈混合槽および前記酸化槽が同一槽で構成されることを特徴とする海水排煙脱硫システムである。   A third invention is the seawater flue gas desulfurization system according to the first or second invention, wherein the flue gas desulfurization absorption tower, the dilution mixing tank, and the oxidation tank are configured in the same tank. .

第4の発明は、ボイラと、前記ボイラから排出される排ガスを蒸気発生用の熱源として使用すると共に、発生した蒸気を用いて発電機を駆動する蒸気タービンと、第1から第3の何れか1つの発明の海水排煙脱硫システムとを有し、前記蒸気タービンで凝縮した水を回収し、循環させる復水器と、前記ボイラから排出される排ガスの脱硝を行う排煙脱硝装置と、前記排ガス中の煤塵を除去する集塵装置と、前記排ガスと熱交換器内を循環する熱媒体とを熱交換する熱回収器と、前記排ガスと海水とを気液接触して前記排ガスを洗浄する排煙脱硫吸収塔から排出される浄化ガスと前記熱媒体とを熱交換して、前記浄化ガスを再加熱する再加熱器とを含む熱交換器と、前記海水排煙脱硫システムで脱硫された浄化ガスを外部へ排出する煙突との少なくとも1つを有することを特徴とする発電システムである。   A fourth invention uses a boiler, a steam turbine that uses exhaust gas discharged from the boiler as a heat source for generating steam, drives a generator using the generated steam, and any one of first to third A seawater flue gas desulfurization system of one invention, recovering and circulating the water condensed by the steam turbine, a flue gas denitration device for denitrating exhaust gas discharged from the boiler, A dust collector that removes dust in the exhaust gas, a heat recovery unit that exchanges heat between the exhaust gas and a heat medium circulating in the heat exchanger, and the exhaust gas and seawater are in gas-liquid contact to clean the exhaust gas. Heat exchange between the purified gas discharged from the flue gas desulfurization absorption tower and the heat medium, and a reheater for reheating the purified gas, and desulfurized by the seawater flue gas desulfurization system Little with chimney that discharges purified gas to the outside A power generation system characterized by having Kutomo one.

本発明によれば、排ガスの脱硫率の調整を容易に行うことができる。   According to the present invention, it is possible to easily adjust the desulfurization rate of exhaust gas.

図1は、本発明の実施例1に係る海水排煙脱硫システムの構成を示す概略図である。FIG. 1 is a schematic diagram illustrating a configuration of a seawater flue gas desulfurization system according to a first embodiment of the present invention. 図2は、排ガスの脱硫率を調整する運転方法の一例を示す図である。FIG. 2 is a diagram illustrating an example of an operation method for adjusting the exhaust gas desulfurization rate. 図3は、本発明の実施例2に係る発電システムの構成を示す概略図である。FIG. 3 is a schematic diagram illustrating a configuration of a power generation system according to Embodiment 2 of the present invention.

以下、本発明につき図面を参照しつつ詳細に説明する。なお、下記の実施例により本発明が限定されるものではない。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、実質的に同一のもの、いわゆる均等の範囲のものが含まれる。さらに、下記実施形態で開示した構成要素は適宜組み合わせることが可能である。   Hereinafter, the present invention will be described in detail with reference to the drawings. In addition, this invention is not limited by the following Example. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art, those that are substantially the same, and those in a so-called equivalent range. Furthermore, the constituent elements disclosed in the following embodiments can be appropriately combined.

本発明による実施例1に係る海水排煙脱硫システムについて、図面を参照して説明する。図1は、海水排煙脱硫システムの構成を示す概略図である。図1に示すように、本実施例に係る海水排煙脱硫システム10は、排煙脱硫吸収塔11と、希釈混合槽12と、酸化槽13とを有する。   A seawater flue gas desulfurization system according to Example 1 of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram showing the configuration of a seawater flue gas desulfurization system. As shown in FIG. 1, the seawater flue gas desulfurization system 10 according to the present embodiment includes a flue gas desulfurization absorption tower 11, a dilution mixing tank 12, and an oxidation tank 13.

海水21は海22からポンプ23により海水供給ラインL11に汲み上げられ、一部の海水21aはポンプ24により海水供給ラインL12を介して排煙脱硫吸収塔11に供給され、他の残りの海水21bは希釈海水供給ラインL13を介して希釈混合槽12に供給される。海水21は、海22からポンプ23により直接汲み上げた海水を用いているが、本発明はこれに限定されるものではなく、図示しない復水器から排出される海水21の排液などを用いるようにしてもよい。   The seawater 21 is pumped from the sea 22 to the seawater supply line L11 by the pump 23, a part of the seawater 21a is supplied to the flue gas desulfurization absorption tower 11 by the pump 24 via the seawater supply line L12, and the other remaining seawater 21b is It is supplied to the diluted mixing tank 12 through the diluted seawater supply line L13. As the seawater 21, seawater pumped directly from the sea 22 by the pump 23 is used, but the present invention is not limited to this, and the seawater 21 drained from a condenser (not shown) is used. It may be.

排煙脱硫吸収塔11は、排ガス25と海水21aとを気液接触して排ガス25を浄化する塔である。排煙脱硫吸収塔11では、海水21aは噴霧ノズル26より上方に液柱状に噴出させ、排ガス25と海水供給ラインL12を介して供給される海水21aとを気液接触させて、排ガス25中の硫黄分の脱硫を行っている。本実施例では、噴霧ノズル26は、上方に液柱状に噴出させる噴霧ノズルであるが、これに限定されるものではなく、下方にシャワー状に噴霧するようにしてもよい。   The flue gas desulfurization absorption tower 11 is a tower that purifies the exhaust gas 25 by gas-liquid contact between the exhaust gas 25 and the seawater 21a. In the flue gas desulfurization absorption tower 11, the seawater 21a is ejected in a liquid column shape above the spray nozzle 26, and the exhaust gas 25 and the seawater 21a supplied via the seawater supply line L12 are brought into gas-liquid contact. Desulfurization of sulfur is performed. In the present embodiment, the spray nozzle 26 is a spray nozzle that ejects upward in the form of a liquid column, but is not limited thereto, and may be sprayed downward in the form of a shower.

即ち、排煙脱硫吸収塔11において排ガス25と海水21aとを気液接触させて、下記式(I)に示すような反応を生じさせ、排ガス25中のSO2などの形態で含有されているSOxなどの硫黄分を海水21aに吸収させ、排ガス25中の硫黄分を、海水21aを用いて除去している。
SO2(G) + H2O → H2SO3(L) → HSO3 - + H ・・・(I)
That is, the exhaust gas 25 and seawater 21a are brought into gas-liquid contact in the flue gas desulfurization absorption tower 11 to cause a reaction as shown in the following formula (I), and are contained in the form of SO 2 or the like in the exhaust gas 25. The sulfur content such as SOx is absorbed by the seawater 21a, and the sulfur content in the exhaust gas 25 is removed using the seawater 21a.
SO 2 (G) + H 2 O → H 2 SO 3 (L) → HSO 3 + H + (I)

この海水脱硫により海水21aと排ガス25との気液接触により発生したH2SO3が解離して水素イオン(H+)が海水21a中に遊離するためpHが下がり、硫黄分吸収海水27には多量の硫黄分が吸収される。このため、硫黄分吸収海水27は硫黄分を高濃度に含んでいる。このとき、硫黄分吸収海水27のpHとしては、例えば3〜6程度となる。そして、排煙脱硫吸収塔11で硫黄分を吸収した硫黄分吸収海水27は、排煙脱硫吸収塔11の塔底部に貯留される。排煙脱硫吸収塔11の塔底部に貯留された硫黄分吸収海水27は、硫黄分吸収海水排出ラインL14を介して希釈混合槽12に送給される。希釈混合槽12で硫黄分吸収海水27は希釈混合槽12に供給される海水21bと混合され、希釈される。 Due to this seawater desulfurization, H 2 SO 3 generated by the gas-liquid contact between the sea water 21 a and the exhaust gas 25 is dissociated and hydrogen ions (H + ) are released into the sea water 21 a, so that the pH is lowered. A large amount of sulfur is absorbed. For this reason, the sulfur-absorbing seawater 27 contains a high concentration of sulfur. At this time, the pH of the sulfur-absorbing seawater 27 is about 3 to 6, for example. And the sulfur content absorption seawater 27 which absorbed the sulfur content in the flue gas desulfurization absorption tower 11 is stored in the tower bottom part of the flue gas desulfurization absorption tower 11. The sulfur-absorbing seawater 27 stored at the bottom of the flue gas desulfurization absorption tower 11 is fed to the dilution mixing tank 12 via the sulfur-absorbing seawater discharge line L14. In the dilution / mixing tank 12, the sulfur-absorbing seawater 27 is mixed with the seawater 21b supplied to the dilution / mixing tank 12 and diluted.

また、排煙脱硫吸収塔11で脱硫された浄化ガス29は浄化ガス排出通路L15を介して大気中に放出される。   Further, the purified gas 29 desulfurized in the flue gas desulfurization absorption tower 11 is released into the atmosphere through the purified gas discharge passage L15.

また、海水供給ラインL12には、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22が設けられている。第1の余剰海水分岐配管L21は、海水供給ラインL12のポンプ24と排煙脱硫吸収塔11との間の第1の分岐部28Aで海水供給ラインL12と連結している。また、第2の余剰海水分岐配管L22は、排煙脱硫吸収塔11内の海水供給ラインL12の第2の分岐部28Bと連結している。第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22から抜き出された余剰海水21cは、希釈混合槽12に送給される。第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22には、調節弁V11、V12が設けられ、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22から抜き出される余剰海水21cの量を調整している。 The seawater supply line L12 is provided with a first surplus seawater branch pipe L21 and a second surplus seawater branch pipe L22 . The first surplus seawater branch pipe L21 is connected to the seawater supply line L12 at the first branch portion 28A between the pump 24 of the seawater supply line L12 and the flue gas desulfurization absorption tower 11. The second surplus seawater branch pipe L22 is connected to the second branch portion 28B of the seawater supply line L12 in the flue gas desulfurization absorption tower 11. The surplus seawater 21c extracted from the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 is supplied to the dilution mixing tank 12. The first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 are provided with control valves V11 and V12, and are extracted from the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22. The amount of surplus seawater 21c to be discharged is adjusted.

第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22により海水供給ラインL12から海水21aの一部を余剰海水21cとして抜き出すことで、排煙脱硫吸収塔11に供給される海水21aの量を容易に調整することができるため、排煙脱硫吸収塔11における排ガス25の脱硫率の調整を容易に行うことができる。また、ポンプ24の吐出圧が抑えられるため、海水21aを排煙脱硫吸収塔11に供給する動力を低減することができる。更に、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cは希釈混合槽12に供給されるため、硫黄分吸収海水27を混合し、硫黄分吸収海水27中のSO2濃度を低減することができることから、希釈混合槽12中の硫黄分吸収海水27中に含まれるSO2が大気中に再飛散することを低減することができる。 Seawater 21a supplied to the flue gas desulfurization absorption tower 11 by extracting a part of seawater 21a as surplus seawater 21c from the seawater supply line L12 by the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22. Therefore, the desulfurization rate of the exhaust gas 25 in the flue gas desulfurization absorption tower 11 can be easily adjusted. Moreover, since the discharge pressure of the pump 24 is suppressed, the power for supplying the seawater 21a to the flue gas desulfurization absorption tower 11 can be reduced. Furthermore, since the surplus seawater 21c extracted to the 1st surplus seawater branch piping L21 and the 2nd surplus seawater branch piping L22 is supplied to the dilution mixing tank 12, the sulfur content absorption seawater 27 is mixed and sulfur content absorption is carried out. Since the SO 2 concentration in the seawater 27 can be reduced, it is possible to reduce the SO 2 contained in the sulfur-absorbing seawater 27 in the dilution mixing tank 12 from being re-scattered into the atmosphere.

排ガス25の脱硫率は、排煙脱硫吸収塔11に供給される排ガス25中の入口SO2濃度と出口SO2濃度との比(出口SO2濃度/入口SO2濃度)や硫黄分吸収海水27の海水性状に基づいて第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cの量により調整される。 The desulfurization rate of the exhaust gas 25 is determined by the ratio of the inlet SO 2 concentration and the outlet SO 2 concentration in the exhaust gas 25 supplied to the flue gas desulfurization absorption tower 11 (outlet SO 2 concentration / inlet SO 2 concentration) or the sulfur content absorbing seawater 27. Is adjusted by the amount of surplus seawater 21c extracted to the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22.

本実施例において、海水性状とは、硫黄分吸収海水27のアルカリ度、海水温度、pH、SO4濃度などをいう。アルカリ度とは、炭酸(H2CO3)、炭酸イオン(CO3 2-)、炭酸水素イオン(HCO3 -)、OH-、有機酸や弱酸の塩(ケイ酸、リン酸、ホウ酸)などの酸を消費する成分の含有量である。排ガス25の脱硫率を硫黄分吸収海水27の海水性状に基づいて第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cの量を調整する場合には、硫黄分吸収海水27のアルカリ度、海水温度、pH、SO4濃度の少なくとも1つ以上に基づいて調整される。中でも海水性状としては、アルカリ度(HCO3 -)に基づいて調整するのが好ましい。 In this embodiment, the seawater property refers to the alkalinity, seawater temperature, pH, SO 4 concentration, etc. of the sulfur-absorbing seawater 27. Alkalinity refers to carbonate (H 2 CO 3 ), carbonate ion (CO 3 2− ), bicarbonate ion (HCO 3 ), OH , organic acid or weak acid salt (silicic acid, phosphoric acid, boric acid) It is content of the component which consumes acids, such as. When adjusting the amount of surplus seawater 21c to be extracted to the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 based on the seawater properties of the sulfur-absorbing seawater 27, the desulfurization rate of the exhaust gas 25 is adjusted. The sulfur content-absorbing seawater 27 is adjusted based on at least one of alkalinity, seawater temperature, pH, and SO 4 concentration. Among them, the seawater properties are preferably adjusted based on alkalinity (HCO 3 ).

排煙脱硫吸収塔11には、排ガス25の入口および出口には、排ガス25の入口SO2濃度および出口SO2濃度を測定するためのSO2濃度計が設けられている。また、排煙脱硫吸収塔11には、硫黄分吸収海水27の海水温度、pH、SO4濃度を測定するための温度計、pH測定器、SO4濃度計を設ける。 In the flue gas desulfurization absorption tower 11, SO 2 concentration meters for measuring the inlet SO 2 concentration and the outlet SO 2 concentration of the exhaust gas 25 are provided at the inlet and outlet of the exhaust gas 25. Further, the flue gas desulfurization absorption tower 11 is provided with a thermometer, a pH measuring device, and an SO 4 concentration meter for measuring the seawater temperature, pH, and SO 4 concentration of the sulfur-absorbing seawater 27.

図2は、排ガス25の脱硫率を調整する運転方法の一例を示す図である。図2に示すように、排煙脱硫吸収塔11における排ガス25の脱硫率および硫黄分吸収海水27の海水性状を求める(ステップS11)。排ガス25の脱硫率が所定の閾値(例えば、設定値+α)以上か否かを判断する(ステップS12)。ここで、本実施例において、脱硫率の所定の閾値とは、例えば、排煙脱硫吸収塔11が、通常、脱硫に必要とされる所定の設定値(例えば、脱硫率が90%)と余分α(例えば、脱硫率が数%)との和の値をいう。   FIG. 2 is a diagram illustrating an example of an operation method for adjusting the desulfurization rate of the exhaust gas 25. As shown in FIG. 2, the desulfurization rate of the exhaust gas 25 and the seawater properties of the sulfur-absorbing seawater 27 in the flue gas desulfurization absorption tower 11 are obtained (step S11). It is determined whether or not the desulfurization rate of the exhaust gas 25 is equal to or greater than a predetermined threshold (for example, a set value + α) (step S12). In this embodiment, the predetermined threshold value of the desulfurization rate is, for example, a predetermined set value (for example, the desulfurization rate is 90%) that the flue gas desulfurization absorption tower 11 normally requires for desulfurization. The sum of α and (for example, the desulfurization rate is several percent).

排ガス25の脱硫率が所定の閾値(例えば、設定値+α)以上の場合には、硫黄分吸収海水27の海水性状と排ガス25の脱硫率とから海水21aの噴霧に必要な噴霧量を算出する(ステップS13)。海水21aの噴霧に必要な噴霧量に基づいて調節弁V11、V12の開度を算出する(ステップS14)。算出された調節弁V11、V12の開度に基づいて調節弁V11、V12の開閉度を調整する(ステップS15)。   When the desulfurization rate of the exhaust gas 25 is equal to or greater than a predetermined threshold (for example, set value + α), the spray amount necessary for spraying the seawater 21a is calculated from the seawater properties of the sulfur-absorbing seawater 27 and the desulfurization rate of the exhaust gas 25. (Step S13). The opening degree of the control valves V11 and V12 is calculated based on the spray amount necessary for spraying the seawater 21a (step S14). Based on the calculated opening of the control valves V11, V12, the degree of opening / closing of the control valves V11, V12 is adjusted (step S15).

算出された調節弁V11、V12の開度に基づいて調節弁V11、V12の開閉度を調整することで、排煙脱硫吸収塔11に供給される海水21aの量を調整することができるため、噴霧ノズル26から噴霧される海水21aの噴霧量を容易に調整することができる。これにより、上述の通り、排煙脱硫吸収塔11において、排ガス25の脱硫率の調整を容易に行うことができる。   Since the amount of seawater 21a supplied to the flue gas desulfurization absorption tower 11 can be adjusted by adjusting the degree of opening and closing of the control valves V11 and V12 based on the calculated opening of the control valves V11 and V12, The spray amount of the seawater 21a sprayed from the spray nozzle 26 can be easily adjusted. Thereby, as above-mentioned, in the flue gas desulfurization absorption tower 11, adjustment of the desulfurization rate of the waste gas 25 can be performed easily.

また、本実施例においては、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22は、希釈混合槽12と連結し、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22から抜き出された余剰海水21cは希釈混合槽12に送給するようにしているが、抜き出された余剰海水21cの供給先は希釈混合槽12に限定されるものではなく、排煙脱硫吸収塔11の塔底部に送給するようにしてもよいし、酸化槽13へ直接送給するようにしてもよい。また、抜き出された余剰海水21cは、希釈混合槽12と排煙脱硫吸収塔11の塔底部との両方に送給するようにしてもよいし、酸化槽13と排煙脱硫吸収塔11の塔底部との両方に送給するようにしてもよい。さらに、抜き出された余剰海水21cは、希釈混合槽12、酸化槽13および排煙脱硫吸収塔11の塔底部に送給するようにしてもよい。 In this embodiment, the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 are connected to the dilution mixing tank 12, and the first surplus seawater branch pipe L21 and the second surplus seawater. Although the surplus seawater 21c extracted from the branch pipe L22 is fed to the dilution mixing tank 12, the supply destination of the extracted surplus seawater 21c is not limited to the dilution mixing tank 12, You may make it send to the tower bottom part of the flue gas desulfurization absorption tower 11, and you may make it send directly to the oxidation tank 13. FIG. Further, the extracted surplus seawater 21c may be supplied to both the dilution mixing tank 12 and the tower bottom of the flue gas desulfurization absorption tower 11, or the oxidation tank 13 and the flue gas desulfurization absorption tower 11 may be supplied. You may make it send to both a tower bottom part. Further, the extracted surplus seawater 21c may be supplied to the dilution mixing tank 12, the oxidation tank 13, and the tower bottoms of the flue gas desulfurization absorption tower 11.

希釈混合槽12は、排煙脱硫吸収塔11の後流側に設けられ、硫黄分を含んだ硫黄分吸収海水27を希釈用の海水21bと希釈・混合する槽である。希釈混合槽12において、排煙脱硫吸収塔11で排ガス25中の硫黄分を海水21aと接触させて海水脱硫することによって生じた硫黄分を含んだ硫黄分吸収海水27を海水21bと混合・希釈する。硫黄分吸収海水27を海水21bと混合し、希釈することで、希釈混合槽12内の硫黄分吸収希釈海水31のpHを上昇させ、SO2ガスの再放散を防ぐことができる。また、希釈混合槽12においてSO2が放散され、外部に漏洩するのを防止することで、刺激臭を放つのを防止することができる。 The dilution mixing tank 12 is a tank that is provided on the downstream side of the flue gas desulfurization absorption tower 11 and dilutes and mixes the sulfur-absorbing seawater 27 containing sulfur with the seawater 21b for dilution. In the dilution and mixing tank 12, the sulfur-absorbing seawater 27 containing the sulfur content generated by bringing the sulfur content in the exhaust gas 25 into contact with the seawater 21a and desulfurizing the seawater in the flue gas desulfurization absorption tower 11 is mixed and diluted with the seawater 21b. To do. By mixing and diluting the sulfur-absorbing seawater 27 with the seawater 21b, the pH of the sulfur-absorbing diluted seawater 31 in the dilution mixing tank 12 can be raised, and re-emission of SO 2 gas can be prevented. Further, by preventing SO 2 from being diffused and leaking outside in the dilution / mixing tank 12, it is possible to prevent emission of an irritating odor.

そして、硫黄分吸収希釈海水31は、希釈混合槽12の下流側に設けられている酸化槽13に送給される。酸化槽13は、希釈混合槽12の下流側に設けられ、硫黄分吸収希釈海水31の水質回復処理を行う曝気装置(エアレーション装置)32を有する槽である。   And the sulfur content absorption dilution seawater 31 is sent to the oxidation tank 13 provided in the downstream of the dilution mixing tank 12. FIG. The oxidation tank 13 is a tank that is provided on the downstream side of the dilution mixing tank 12 and has an aeration apparatus (aeration apparatus) 32 that performs water quality recovery processing of the sulfur content absorption diluted seawater 31.

曝気装置32は、空気33を供給する酸化用空気ブロア34と、空気33を送給する散気管35と、空気33を酸化槽13内の硫黄分吸収希釈海水31に供給する酸化空気用ノズル36とを有するものである。酸化用空気ブロア34により外部の空気33が散気管35を介して酸化空気用ノズル36から酸化槽13内に送り込まれ、下記式(II)のような酸素の溶解を生じる。酸化槽13において硫黄分吸収希釈海水31中の硫黄分が空気33と接触して下記式(III)〜(V)のような亜硫酸水素イオン(HSO3 -)の酸化反応と、重炭酸イオン(HCO3 -)の脱炭酸反応とを生じ、硫黄分吸収希釈海水31は水質回復され、水質回復海水37となる。
2(G) → O2(L)・・・(II)
HSO3 - + 1/2O2 → SO4 2- + H ・・・(III)
HCO3 - + H → CO2(G) + H2O ・・・(IV)
CO3 2- +2H → CO2(G) + H2O ・・・(V)
The aeration apparatus 32 includes an oxidizing air blower 34 that supplies air 33, an air diffuser 35 that supplies the air 33, and an oxidizing air nozzle 36 that supplies the air 33 to the sulfur content absorption diluted seawater 31 in the oxidation tank 13. It has. The external air 33 is sent from the oxidizing air nozzle 36 into the oxidation tank 13 through the air diffusion pipe 35 by the oxidizing air blower 34, and the oxygen is dissolved as shown in the following formula (II). In the oxidation tank 13, the sulfur content in the sulfur content absorption diluted seawater 31 comes into contact with the air 33, and an oxidation reaction of bisulfite ions (HSO 3 ) as shown in the following formulas (III) to (V) and bicarbonate ions ( HCO 3 ) decarboxylation reaction occurs, and the sulfur content absorption diluted seawater 31 is recovered in water quality to become water quality recovered seawater 37.
O 2 (G) → O 2 (L) (II)
HSO 3 + 1 / 2O 2 → SO 4 2− + H + (III)
HCO 3 + H + → CO 2 (G) + H 2 O (IV)
CO 3 2- + 2H + → CO 2 (G) + H 2 O (V)

これにより、硫黄分吸収希釈海水31のpHを上昇させると共に、CODを低減することができ、水質回復海水37のpH、溶存酸素濃度、CODを海水放流可能なレベルとして放出することができる。また、酸化槽13で硫黄分吸収希釈海水31の水質回復を行う際にガスが発生しても、この発生するガスはSO2環境基準濃度を満たすようにして酸化槽13で放散させることができる。水質回復海水37は海水排出ラインL31を介して海22へ放流される。 Thereby, while raising the pH of the sulfur content absorption dilution seawater 31, COD can be reduced and the pH of the water quality recovery seawater 37, dissolved oxygen concentration, and COD can be discharge | released as a seawater dischargeable level. Further, even when gas is generated when the water content of the sulfur component absorption diluted seawater 31 is recovered in the oxidation tank 13, the generated gas can be diffused in the oxidation tank 13 so as to satisfy the SO 2 environmental standard concentration. . The water quality recovery seawater 37 is discharged to the sea 22 through the seawater discharge line L31.

このように、本実施例に係る海水排煙脱硫システム10は、排煙脱硫吸収塔11に供給される排ガス25の入口SO2濃度と出口SO2濃度との比および硫黄分吸収海水27のアルカリ度に基づいて第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cの量を調整することで、噴霧ノズル26から噴霧される海水21aの噴霧量を調整して排ガス25の脱硫率の調整を容易に行うことができる。また、海水21aを排煙脱硫吸収塔11に供給する動力を低減することができる。更に、余剰海水21cを希釈混合槽12中の硫黄分吸収海水27に混合することで、硫黄分吸収海水27中のSO2濃度を低減することができる。このため、屋外開放型の酸化槽13に流れた硫黄分吸収海水27を酸化処理し水質回復を行う際、排煙脱硫吸収塔11において吸収したSO2が希釈混合槽12において放散され、SO2ガスが外部に漏洩するのを防止し、刺激臭を放つのを防止することができる。 As described above, the seawater flue gas desulfurization system 10 according to the present embodiment is configured such that the ratio of the inlet SO 2 concentration and the outlet SO 2 concentration of the exhaust gas 25 supplied to the flue gas desulfurization absorption tower 11 and the alkali of the sulfur content absorption seawater 27. The spray amount of the seawater 21a sprayed from the spray nozzle 26 is adjusted by adjusting the amount of the surplus seawater 21c extracted to the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 based on the degree. It is possible to easily adjust the desulfurization rate of the exhaust gas 25. Moreover, the motive power which supplies the seawater 21a to the flue gas desulfurization absorption tower 11 can be reduced. Further, by mixing a surplus seawater 21c in sulfur absorption seawater 27 in the diluted mixing tank 12, it is possible to reduce the SO 2 concentration of sulfur in the absorbing seawater 27. Therefore, when performing the oxidation treatment water recovered sulfur absorbing seawater 27 flows into the oxidation tank 13 of the outdoor open, SO 2 absorbed in flue gas desulfurization absorber tower 11 is dissipated in the dilution mixing tank 12, SO 2 Gas can be prevented from leaking to the outside, and an irritating odor can be prevented.

したがって、本実施例に係る海水排煙脱硫システム10によれば、排ガス25の安定した脱硫率を維持しつつ、安全性および信頼性の高い海水排煙脱硫装置を提供することができる。   Therefore, according to the seawater flue gas desulfurization system 10 according to the present embodiment, it is possible to provide a seawater flue gas desulfurization device with high safety and reliability while maintaining a stable desulfurization rate of the exhaust gas 25.

また、本実施例においては、排煙脱硫吸収塔11で海水脱硫に用いた海水21aの処理をする海水排煙脱硫システムについて説明したが、本発明はこれに限定されるものではない。海水排煙脱硫装置は、例えば各種産業における工場、大型、中型火力発電所などの発電所、電気事業用大型ボイラ又は一般産業用ボイラ、製鉄所、精錬所等から排出される排ガス中に含まれる硫黄酸化物を海水脱硫する海水排煙脱硫装置にも適用することができる。   Moreover, in the present Example, although the seawater flue gas desulfurization system which processes the seawater 21a used for seawater desulfurization with the flue gas desulfurization absorption tower 11 was demonstrated, this invention is not limited to this. Seawater flue gas desulfurization equipment is included in exhaust gas discharged from factories in various industries, power plants such as large and medium-sized thermal power plants, large boilers for electric utilities or general industrial boilers, steelworks, smelters, etc. The present invention can also be applied to a seawater flue gas desulfurization apparatus that desulfurizes sulfur oxides.

また、本実施例においては、排煙脱硫吸収塔11、希釈混合槽12および酸化槽13は各々別々の槽として独立しており、排煙脱硫吸収塔11と希釈混合槽12と酸化槽13とを連結するようにしているが、本実施例はこれに限定されるものではなく、排煙脱硫吸収塔11、希釈混合槽12および酸化槽13を一体として一つの槽で構成してもよいし、希釈混合槽12と酸化槽13とを一体として一つの槽で構成するようにしてもよい。   In the present embodiment, the flue gas desulfurization absorption tower 11, the dilution mixing tank 12 and the oxidation tank 13 are independent as separate tanks, and the flue gas desulfurization absorption tower 11, the dilution mixing tank 12, the oxidation tank 13, and the like. However, the present embodiment is not limited to this, and the flue gas desulfurization absorption tower 11, the dilution mixing tank 12, and the oxidation tank 13 may be integrated into a single tank. The dilution mixing tank 12 and the oxidation tank 13 may be integrated into a single tank.

本発明の実施例2に係る発電システムについて、図面を参照して説明する。本実施例に係る発電システムに適用される海水排煙脱硫システムには、実施例1に係る海水排煙脱硫システムが用いられる。なお、実施例1と同様の部材については、同一符号を付してその説明は省略する。   A power generation system according to Embodiment 2 of the present invention will be described with reference to the drawings. The seawater flue gas desulfurization system according to the first embodiment is used for the seawater flue gas desulfurization system applied to the power generation system according to the present embodiment. In addition, about the member similar to Example 1, the same code | symbol is attached | subjected and the description is abbreviate | omitted.

図3は、本発明の実施例2に係る発電システムの構成を示す概略図である。図3に示すように、本実施例に係る発電システム40は、ボイラ41と、蒸気タービン42と、復水器43と、排煙脱硝装置44と、集塵装置45と、海水排煙脱硫システム10とを有するものである。尚、本実施例において、上述のように、硫黄分吸収海水とは、海水排煙脱硫システム10においてSO2など硫黄分を吸収した使用済み海水をいう。 FIG. 3 is a schematic diagram illustrating a configuration of a power generation system according to Embodiment 2 of the present invention. As shown in FIG. 3, a power generation system 40 according to this embodiment includes a boiler 41, a steam turbine 42, a condenser 43, a flue gas denitration device 44, a dust collector 45, and a seawater flue gas desulfurization system. 10. In the present embodiment, as described above, the sulfur-absorbing seawater means used seawater that has absorbed sulfur such as SO 2 in the seawater flue gas desulfurization system 10.

ボイラ41は、油タンクまたは石炭ミルなどから供給される燃料46を空気予熱器(AH)47で予熱された空気48と共にバーナ(不図示)から噴射して燃焼させる。外部から供給される空気48は押込みファン49により空気予熱器47に送給され予熱される。燃料46と空気予熱器47で予熱された空気48とは前記バーナに供給され、燃料46はボイラ41で燃焼される。これにより、蒸気タービン42を駆動するための蒸気50を発生する。   The boiler 41 injects and burns fuel 46 supplied from an oil tank or a coal mill from a burner (not shown) together with air 48 preheated by an air preheater (AH) 47. The air 48 supplied from the outside is supplied to the air preheater 47 by the pushing fan 49 and preheated. The fuel 46 and the air 48 preheated by the air preheater 47 are supplied to the burner, and the fuel 46 is burned by the boiler 41. Thereby, the steam 50 for driving the steam turbine 42 is generated.

ボイラ41内で燃焼して発生する排ガス51は排煙脱硝装置44に送給される。また、排ガス51は復水器43から排出される水52と熱交換し、蒸気50を発生する熱源として使用される。蒸気タービン42はこの蒸気50を用いて発電機53を駆動している。そして、復水器43は蒸気タービン42で凝縮した水52を回収し、再びボイラ41に戻し、循環させている。   The exhaust gas 51 generated by combustion in the boiler 41 is sent to the flue gas denitration device 44. Further, the exhaust gas 51 is used as a heat source for exchanging heat with the water 52 discharged from the condenser 43 and generating steam 50. The steam turbine 42 uses this steam 50 to drive the generator 53. The condenser 43 collects the water 52 condensed by the steam turbine 42 and returns it to the boiler 41 for circulation.

ボイラ41から排出された排ガス51は排煙脱硝装置44内で脱硝され、空気予熱器47で空気48と熱交換した後、集塵装置45に送給され、排ガス51中の煤塵を除去する。そして、集塵装置45で除塵された排ガス51は、誘引ファン55により海水排煙脱硫システム10内に供給される。この時、排ガス51は熱交換器56で、海水排煙脱硫システム10で脱硫され排出される浄化ガス29と熱交換された後、海水排煙脱硫システム10内に供給される。また、排ガス51は熱交換器56で浄化ガス29と熱交換することなく海水排煙脱硫システム10に直接供給するようにしてもよい。   The exhaust gas 51 discharged from the boiler 41 is denitrated in the flue gas denitration device 44, exchanges heat with the air 48 by the air preheater 47, and then fed to the dust collector 45 to remove the dust in the exhaust gas 51. The exhaust gas 51 removed by the dust collector 45 is supplied into the seawater flue gas desulfurization system 10 by the induction fan 55. At this time, the exhaust gas 51 is heat-exchanged by the heat exchanger 56 with the purified gas 29 desulfurized and discharged by the seawater flue gas desulfurization system 10 and then supplied into the seawater flue gas desulfurization system 10. Further, the exhaust gas 51 may be directly supplied to the seawater flue gas desulfurization system 10 without exchanging heat with the purified gas 29 by the heat exchanger 56.

また、熱交換器56は、熱回収器と、再加熱器とを含むものであり、前記熱回収器と前記再加熱器との間を熱媒体が循環している。前記熱回収器は、空気予熱器47と集塵装置45との間に設けられ、ボイラ41から排出される排ガス51と前記熱媒体とを熱交換する。前記再加熱器は、排煙脱硫吸収塔11の後流側に設けられ、排煙脱硫吸収塔11から排出される浄化ガス57と前記熱媒体とを熱交換して、浄化ガス29を再加熱する。   The heat exchanger 56 includes a heat recovery device and a reheater, and a heat medium circulates between the heat recovery device and the reheater. The heat recovery unit is provided between the air preheater 47 and the dust collector 45 and exchanges heat between the exhaust gas 51 discharged from the boiler 41 and the heat medium. The reheater is provided on the downstream side of the flue gas desulfurization absorption tower 11, and exchanges heat between the purified gas 57 discharged from the flue gas desulfurization absorption tower 11 and the heat medium to reheat the purified gas 29. To do.

海水排煙脱硫システム10は、上述の実施例1に係る海水排煙脱硫装置である。すなわち、海水排煙脱硫システム10は、排煙脱硫吸収塔11と、希釈混合槽12と、酸化槽13と、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22とを有するものである。 The seawater flue gas desulfurization system 10 is the seawater flue gas desulfurization apparatus according to the first embodiment. That is, the seawater flue gas desulfurization system 10 includes a flue gas desulfurization absorption tower 11, a dilution and mixing tank 12, an oxidation tank 13, a first surplus seawater branch pipe L21, and a second surplus seawater branch pipe L22. Is.

海水排煙脱硫システム10では、上述の通り、排ガス51中に含有されている硫黄分を海22から汲み上げられた海水21を用いて海水脱硫を行っている。また、海水21は海22からポンプ23により汲み上げられ、復水器43で熱交換した後、一部の海水21aは海水供給ラインL12を介してポンプ24により海水排煙脱硫システム10に送給される。また、残りの海水21bは海水供給ラインL13を介して希釈混合槽12の上流側に送給される。海水排煙脱硫システム10において排ガス51と海水21aとを気液接触させて、排ガス51中の硫黄分を海水21aに吸収している。硫黄分を吸収した硫黄分吸収海水27は排煙脱硫吸収塔11から希釈混合槽12の上流側に送給され、海水21bと混合し、希釈される。   In the seawater flue gas desulfurization system 10, as described above, seawater desulfurization is performed using the seawater 21 pumped up from the sea 22 by the sulfur content contained in the exhaust gas 51. Further, the seawater 21 is pumped from the sea 22 by the pump 23 and heat exchange is performed by the condenser 43, and then a part of the seawater 21a is sent to the seawater flue gas desulfurization system 10 by the pump 24 via the seawater supply line L12. The The remaining seawater 21b is fed to the upstream side of the dilution / mixing tank 12 via the seawater supply line L13. In the seawater flue gas desulfurization system 10, the exhaust gas 51 and the seawater 21a are brought into gas-liquid contact, and the sulfur content in the exhaust gas 51 is absorbed by the seawater 21a. The sulfur-absorbing seawater 27 that has absorbed the sulfur is fed from the flue gas desulfurization absorption tower 11 to the upstream side of the dilution mixing tank 12, mixed with the seawater 21b, and diluted.

また、海水排煙脱硫システム10で浄化された排ガス51は、浄化ガス29となって浄化ガス排出通路L15を介して煙突57から外部に排出される。   Further, the exhaust gas 51 purified by the seawater flue gas desulfurization system 10 becomes the purified gas 29 and is discharged outside from the chimney 57 through the purified gas discharge passage L15.

本実施例では、海水排煙脱硫システム10は、海水供給ラインL12に第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22を設けている。第1の余剰海水分岐配管L21は海水供給ラインL12のポンプ24と排煙脱硫吸収塔11との間で海水供給ラインL12と連結している。また、第2の余剰海水分岐配管L22は排煙脱硫吸収塔11内の海水供給ラインL12と連結している。第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22から抜き出された余剰海水21cは希釈混合槽12に送給される。第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22により海水供給ラインL12から海水21aの一部を余剰海水21cとして抜き出すことで、排煙脱硫吸収塔11に供給される海水21aの量を調整し、排煙脱硫吸収塔11における排ガス51の脱硫率の調整を行う。排ガス25の脱硫率は、上述の通り、排煙脱硫吸収塔11に供給される排ガス51中の入口SO2濃度と出口SO2濃度との比(出口SO2濃度/入口SO2濃度)や硫黄分吸収海水27のアルカリ度に基づいて第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cの量により調整される。よって、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22により海水供給ラインL12から海水21aの一部を抜き出す量を容易に調整できるため、排煙脱硫吸収塔11に供給される海水21aの量を容易に調整することができる。このため、排煙脱硫吸収塔11における排ガス51の脱硫率の調整を容易に行うことができる。また、ポンプ24の吐出圧が抑えられるため、海水21aを排煙脱硫吸収塔11に供給する動力を低減することができる。 In the present embodiment, the seawater flue gas desulfurization system 10 includes a first surplus seawater branch pipe L21 and a second surplus seawater branch pipe L22 in the seawater supply line L12. The first surplus seawater branch pipe L21 is connected to the seawater supply line L12 between the pump 24 of the seawater supply line L12 and the flue gas desulfurization absorption tower 11. Further, the second surplus seawater branch pipe L22 is connected to the seawater supply line L12 in the flue gas desulfurization absorption tower 11. The surplus seawater 21c extracted from the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 is supplied to the dilution mixing tank 12. Seawater 21a supplied to the flue gas desulfurization absorption tower 11 by extracting a part of seawater 21a as surplus seawater 21c from the seawater supply line L12 by the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22. And the desulfurization rate of the exhaust gas 51 in the flue gas desulfurization absorption tower 11 is adjusted. As described above, the desulfurization rate of the exhaust gas 25 is determined by the ratio of the inlet SO 2 concentration and the outlet SO 2 concentration in the exhaust gas 51 supplied to the flue gas desulfurization absorption tower 11 (outlet SO 2 concentration / inlet SO 2 concentration) and sulfur. The amount of surplus seawater 21c extracted to the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22 is adjusted based on the alkalinity of the partial absorption seawater 27. Accordingly, the amount of the seawater 21a extracted from the seawater supply line L12 can be easily adjusted by the first surplus seawater branch pipe L21 and the second surplus seawater branch pipe L22, so that it is supplied to the flue gas desulfurization absorption tower 11. The amount of seawater 21a to be adjusted can be easily adjusted. For this reason, adjustment of the desulfurization rate of the exhaust gas 51 in the flue gas desulfurization absorption tower 11 can be easily performed. Moreover, since the discharge pressure of the pump 24 is suppressed, the power for supplying the seawater 21a to the flue gas desulfurization absorption tower 11 can be reduced.

また、海22から汲み上げられた海水21は復水器43で熱交換した後、海水排煙脱硫システム10に送給し、海水脱硫に用いているが、海22から汲み上げた海水21を復水器43で熱交換させずに海水排煙脱硫システム10に直接送給し、海水脱硫に用いるようにしてもよい。   The seawater 21 pumped from the sea 22 is heat-exchanged by the condenser 43 and then sent to the seawater flue gas desulfurization system 10 for use in seawater desulfurization. The seawater 21 pumped from the sea 22 is condensed into water. Instead of heat exchange in the vessel 43, it may be directly fed to the seawater flue gas desulfurization system 10 and used for seawater desulfurization.

希釈混合槽12で硫黄分吸収海水27を海水21bと混合し、希釈された硫黄分吸収希釈海水31は、酸化槽13に送給され、酸化槽13で硫黄分吸収希釈海水31を水質回復し、水質回復海水37とする。酸化槽13で得られた水質回復海水37は、pH、溶存酸素濃度、CODを海水放流可能なレベルとして酸化槽13から海水排出ラインL32を介して海22へ放流される。   The sulfur-absorbing seawater 27 is mixed with the seawater 21b in the dilution / mixing tank 12, and the diluted sulfur-absorbing / diluting seawater 31 is supplied to the oxidation tank 13 to recover the water content of the sulfur-absorbing diluted seawater 31 in the oxidation tank 13. Water quality recovery seawater 37. The water quality recovery seawater 37 obtained in the oxidation tank 13 is discharged from the oxidation tank 13 to the sea 22 via the seawater discharge line L32 with pH, dissolved oxygen concentration, and COD at a level at which seawater can be discharged.

また、海水供給ラインL11から海水21の一部を、希釈海水供給ラインL13を介して酸化槽13内の水質回復海水37の後流側に供給するようにしてもよい。これにより、水質回復海水37を更に希釈することができる。これにより、水質回復海水37のpHを上昇させ、海水排液のpHを海水近くにまで上昇させ、海水排液のpHの排水基準(pH6.0以上)を満たすと共に、CODを低減することができ、水質回復海水37のpH、CODを海水放流可能なレベルとして放出することができる。   Further, a part of the seawater 21 may be supplied from the seawater supply line L11 to the downstream side of the water quality recovery seawater 37 in the oxidation tank 13 via the diluted seawater supply line L13. Thereby, the water quality recovery seawater 37 can be further diluted. As a result, the pH of the water quality recovery seawater 37 is increased, the pH of the seawater drainage liquid is increased to near the seawater, the drainage standard for the pH of the seawater drainage liquid (pH 6.0 or higher) is satisfied, and COD is reduced. It is possible to release the pH and COD of the water quality recovery seawater 37 as a level at which seawater can be discharged.

このように、本実施例に係る発電システム40によれば、排煙脱硫吸収塔11において排ガス51の脱硫率の調整を容易に行うことができると共に、海水21aを排煙脱硫吸収塔11へ供給する動力を低減しランニングコストの抑制を図ることができる。また、第1の余剰海水分岐配管L21、第2の余剰海水分岐配管L22に抜き出される余剰海水21cは希釈混合槽12に供給され、硫黄分吸収海水27中のSO2濃度を低減することができることから、希釈混合槽12中の硫黄分吸収海水27中に含まれるSO2が大気中に再飛散することを低減することができる。したがって、排ガス51の安定した脱硫率を維持しつつ、安全性および信頼性の高い発電システムを提供することができる。 Thus, according to the power generation system 40 according to the present embodiment, it is possible to easily adjust the desulfurization rate of the exhaust gas 51 in the flue gas desulfurization absorption tower 11, and supply the seawater 21a to the flue gas desulfurization absorption tower 11. The driving power can be reduced and the running cost can be suppressed. The first surplus seawater branch pipe L21, the excess seawater 21c withdrawn to a second surplus seawater branch pipe L 22 is supplied to the dilution mixing tank 12, reducing the SO 2 concentration of sulfur in the absorbing seawater 27 Therefore, it is possible to reduce the re-scattering of SO 2 contained in the sulfur-absorbing seawater 27 in the dilution mixing tank 12 into the atmosphere. Therefore, it is possible to provide a power generation system with high safety and reliability while maintaining a stable desulfurization rate of the exhaust gas 51.

また、本実施例に係る海水排煙脱硫装置10は、各種産業における工場、大型、中型火力発電所などの発電所、電気事業用大型ボイラ又は一般産業用ボイラ等から排出される排ガス中に含まれる硫黄酸化物を海水脱硫することで生じる硫黄分吸収溶液中の硫黄分の除去に利用することができる。   In addition, the seawater flue gas desulfurization apparatus 10 according to the present embodiment is included in exhaust gas discharged from factories in various industries, power plants such as large and medium-sized thermal power plants, large boilers for electric utilities, or general industrial boilers. It can be used for removal of sulfur content in the sulfur content absorption solution produced by desulfurizing the sulfur oxide.

10 海水排煙脱硫システム
11 排煙脱硫吸収塔
12 希釈混合槽
13 酸化槽
21、21a、21b 海水
21c 余剰海水
22 海
23、24 ポンプ
25、51 排ガス
26 噴霧ノズル
27 硫黄分吸収海水
28A 第1の分岐部
28B 第2の分岐部
29 浄化ガス
31 硫黄分吸収希釈海水
32 曝気装置(エアレーション装置)
33 空気
34 酸化用空気ブロア
35 散気管
36 酸化空気用ノズル
37 水質回復海水
40 発電システム
41 ボイラ
42 蒸気タービン
43 復水器
44 排煙脱硝装置
45 集塵装置
46 燃料
47 空気予熱器(AH)
48 空気
49 押込みファン
50 蒸気
52 水
53 発電機
55 誘引ファン
56 熱交換器
57 煙突
L11、L12 海水供給ライン
L13 希釈海水供給ライン
L14 硫黄分吸収海水排出ライン
L15 浄化ガス排出通路
L21 第1の余剰海水分岐配管
L22 第2の余剰海水分岐配管
L31、L32 海水排出ライン
DESCRIPTION OF SYMBOLS 10 Seawater flue gas desulfurization system 11 Flue gas desulfurization absorption tower 12 Dilution mixing tank 13 Oxidation tank 21, 21a, 21b Seawater 21c Surplus seawater 22 Sea 23, 24 Pump 25, 51 Exhaust gas 26 Spray nozzle 27 Sulfur content absorption seawater 28A 1st Branch portion 28B Second branch portion 29 Purified gas 31 Sulfur content absorption diluted seawater 32 Aeration device (aeration device)
33 Air 34 Oxidizing air blower 35 Aeration pipe 36 Oxidizing air nozzle 37 Water quality recovery seawater 40 Power generation system 41 Boiler 42 Steam turbine 43 Condenser 44 Flue gas denitration device 45 Dust collector 46 Fuel 47 Air preheater (AH)
48 Air 49 Push-in fan 50 Steam 52 Water 53 Generator 55 Induction fan 56 Heat exchanger 57 Chimney L11, L12 Seawater supply line L13 Diluted seawater supply line L14 Sulfur component absorption seawater discharge line L15 Purified gas discharge passage L21 First surplus seawater Branch pipe L22 Second surplus seawater branch pipe L31, L32 Seawater discharge line

Claims (4)

  1. 排ガスと海水とを気液接触して前記排ガスを洗浄する排煙脱硫吸収塔と、
    前記排煙脱硫吸収塔の後流側に設けられ、硫黄分を含んだ硫黄分吸収海水を希釈用の海水と希釈混合する希釈混合槽と、
    前記海水を前記排煙脱硫吸収塔に供給する海水供給ラインと、
    前記海水供給ラインから分岐され、希釈海水を供給する希釈海水供給ラインと、
    希釈海水の分岐部の後流側で、前記海水供給ラインから第1の分岐部で分岐され、前記希釈混合槽に余剰海水を供給する第1の余剰海水分岐配管と、
    前記排煙脱硫吸収塔内の前記海水供給ラインの第2の分岐部で、該海水供給ラインから分岐され、前記希釈混合槽に余剰海水を供給する第2の余剰海水分岐配管と、を備えると共に、
    排煙脱硫吸収塔に供給される排ガス中の入口SO 2 濃度と出口SO 2 濃度との比(出口SO 2 濃度/入口SO 2 濃度)と、硫黄分吸収海水の海水性状とに基づいて第1余剰海水分岐配管、第2余剰海水分岐配管から抜き出される余剰海水の量を調整することで、前記排煙脱硫吸収塔内の前記海水の噴霧量を調節することを特徴とする海水排煙脱硫システム。
    A flue gas desulfurization absorption tower that cleans the exhaust gas by gas-liquid contact between the exhaust gas and seawater;
    A dilution mixing tank that is provided on the downstream side of the flue gas desulfurization absorption tower and dilutes and mixes sulfur-absorbing seawater containing sulfur with seawater for dilution;
    A seawater supply line for supplying the seawater to the flue gas desulfurization absorption tower;
    A diluted seawater supply line branched from the seawater supply line and supplying diluted seawater;
    A first surplus sea water branch pipe that is branched from the sea water supply line at the first branch part on the downstream side of the dilute sea water branch part and supplies surplus sea water to the dilution mixing tank;
    A second branch section of the seawater supply line in the flue gas desulfurization absorption tower and a second surplus seawater branch pipe branched from the seawater supply line and supplying surplus seawater to the dilution and mixing tank; ,
    Based on the ratio of the inlet SO 2 concentration to the outlet SO 2 concentration in the exhaust gas supplied to the flue gas desulfurization absorption tower (the outlet SO 2 concentration / the inlet SO 2 concentration) and the seawater properties of the sulfur-absorbing seawater. The seawater flue gas desulfurization characterized by adjusting the spray amount of the seawater in the flue gas desulfurization absorption tower by adjusting the amount of surplus seawater drawn from the surplus seawater branch pipe and the second surplus seawater branch pipe system.
  2. 請求項1において、
    前記余剰海水分岐配管の分岐部は、前記海水供給ラインに設けられる海水送給ポンプの後流側に設けられることを特徴とする海水排煙脱硫システム。
    In claim 1,
    The seawater flue gas desulfurization system, wherein a branch portion of the surplus seawater branch pipe is provided on a downstream side of a seawater feed pump provided in the seawater supply line.
  3. 請求項1または2において、
    前記排煙脱硫吸収塔、前記希釈混合槽および前記酸化槽が同一槽で構成されることを特徴とする海水排煙脱硫システム。
    In claim 1 or 2,
    A seawater flue gas desulfurization system, wherein the flue gas desulfurization absorption tower, the dilution mixing tank, and the oxidation tank are configured in the same tank.
  4. ボイラと、
    前記ボイラから排出される排ガスを蒸気発生用の熱源として使用すると共に、発生した蒸気を用いて発電機を駆動する蒸気タービンと、
    請求項1から3の何れか1つの海水排煙脱硫システムとを有し、
    前記蒸気タービンで凝縮した水を回収し、循環させる復水器と、
    前記ボイラから排出される排ガスの脱硝を行う排煙脱硝装置と、
    前記排ガス中の煤塵を除去する集塵装置と、
    前記排ガスと熱交換器内を循環する熱媒体とを熱交換する熱回収器と、前記排ガスと海水とを気液接触して前記排ガスを洗浄する排煙脱硫吸収塔から排出される浄化ガスと前記熱媒体とを熱交換して、前記浄化ガスを再加熱する再加熱器とを含む熱交換器と、
    前記海水排煙脱硫システムで脱硫された浄化ガスを外部へ排出する煙突との少なくとも1つを有することを特徴とする発電システム。
    With a boiler,
    Using the exhaust gas discharged from the boiler as a heat source for steam generation, and a steam turbine for driving a generator using the generated steam;
    A seawater flue gas desulfurization system according to any one of claims 1 to 3,
    A condenser for collecting and circulating the water condensed in the steam turbine;
    A flue gas denitration device for denitrating exhaust gas discharged from the boiler;
    A dust collector for removing the dust in the exhaust gas;
    A heat recovery unit that exchanges heat between the exhaust gas and a heat medium that circulates in the heat exchanger; and a purified gas discharged from a flue gas desulfurization absorption tower that cleans the exhaust gas by gas-liquid contact between the exhaust gas and seawater; A heat exchanger including a reheater that exchanges heat with the heat medium and reheats the purified gas;
    A power generation system comprising at least one of a chimney for discharging the purified gas desulfurized by the seawater flue gas desulfurization system to the outside.
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