JPH0658104U - Power plant with fluidized bed furnace - Google Patents
Power plant with fluidized bed furnaceInfo
- Publication number
- JPH0658104U JPH0658104U JP14593U JP14593U JPH0658104U JP H0658104 U JPH0658104 U JP H0658104U JP 14593 U JP14593 U JP 14593U JP 14593 U JP14593 U JP 14593U JP H0658104 U JPH0658104 U JP H0658104U
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- exhaust
- gas
- exhaust gas
- heat recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
(57)【要約】
【目的】 加圧流動床ボイラプラント等の流動床炉を備
えた発電プラントにおいて、脱硝効果を維持しつつ、排
ガス中のＳＯ3 がアンモニアと作用して酸性硫安（ＮＨ
4 ＨＳＯ4 ）が発生することを抑制する。
【構成】 流動床炉（加圧流動床ボイラ１）、同流動床
炉の生成ガスで駆動されるガスタービン８、及びガスタ
ービン８の出口に接続された排ガス系統２３に設置され
た脱硝装置１２と排熱回収熱交換器を備えた流動床炉を
備えた発電プラントにおいて、排ガス系統２３に上流側
の第１の排熱回収熱交換器１０と下流側の排熱回収熱交
換器１１を設け、両熱交換器１０，１１の間に脱硝装置
１２を配置した。また、脱硝装置１２の入口ガス温度を
温度計４０で検出し、給水バイパス系統１６の流量制御
弁１３を制御して、第１の排熱回収熱交換器１０の熱吸
収量を制御して、脱硝装置１２の入口ガス温度を一定に
保持するようにした。
(57) [Summary] [Purpose] In a power plant equipped with a fluidized bed furnace, such as a pressurized fluidized bed boiler plant, SO 3 in the exhaust gas acts on ammonia while maintaining the denitration effect, and acidic ammonium sulfate (NH
4 HSO 4 ) is suppressed. [Structure] A denitration device 12 installed in a fluidized bed furnace (pressurized fluidized bed boiler 1), a gas turbine 8 driven by generated gas of the fluidized bed furnace, and an exhaust gas system 23 connected to an outlet of the gas turbine 8. In a power plant equipped with a fluidized bed furnace equipped with an exhaust heat recovery heat exchanger, an exhaust gas system 23 is provided with an upstream first exhaust heat recovery heat exchanger 10 and a downstream exhaust heat recovery heat exchanger 11. A denitration device 12 is arranged between the heat exchangers 10 and 11. Further, the inlet gas temperature of the denitration device 12 is detected by the thermometer 40, the flow control valve 13 of the feed water bypass system 16 is controlled, and the heat absorption amount of the first heat recovery heat exchanger 10 is controlled. The inlet gas temperature of the denitration device 12 was kept constant.
Description
【０００１】[0001]
本考案は、脱硝装置でのＳＯ3 への転換率を低減させることができるようにし た加圧流動床ボイラプラント、ガス化コンバインドプラント等の流動床炉を備え た発電プラントに関する。The present invention relates to a power plant equipped with a fluidized bed furnace, such as a pressurized fluidized bed boiler plant or a gasification combined plant, capable of reducing the conversion rate of SO 3 in a denitration device.
【０００２】[0002]
従来の脱硝装置を装備した石炭焚ボイラ又は油焚ボイラにおいては、燃焼排ガ スを排出する煙突の前に脱硫装置又は電気集じん器を装備することによって、燃 焼ガス中のＳＯ3 と脱硝装置からの残留アンモニアの化学反応にって発生する酸 性硫安（ＮＨ4 ＨＳＯ4 ）を完全に除去することが可能であった。In a coal-fired boiler or oil-fired boiler equipped with a conventional denitration device, SO 3 in the combustion gas and denitration are installed by equipping the desulfurization device or the electric precipitator before the chimney that discharges the combustion exhaust gas. It was possible to completely remove the acidic ammonium sulfate (NH 4 HSO 4 ) generated by the chemical reaction of residual ammonia from the equipment.
【０００３】 しかし、燃焼ガスによって駆動されるガスタービンを装備した加圧流動床ボイ ラプラントでは、加圧流動床ボイラ内で脱硫が可能なために脱硫装置を設置して いない。また、全体のプラント効率を向上させる観点から、煙突よりの排出ガス 温度を極力低下させるために、排熱回収熱交換器が装備されている。However, in a pressurized fluidized bed boiler plant equipped with a gas turbine driven by combustion gas, a desulfurizer is not installed because desulfurization is possible in the pressurized fluidized bed boiler. Also, from the viewpoint of improving the overall plant efficiency, an exhaust heat recovery heat exchanger is equipped to reduce the temperature of the exhaust gas from the stack as much as possible.
【０００４】 従来の前記加圧流動床ボイラプラントを、図４に示す。１は加圧容器２を備え た加圧流動床ボイラであって、同加圧流動床ボイラ１内には、石炭・石灰石供給 システム３から石炭と石灰石が供給され、また供給空気系統２１を経て後述する 空気圧縮機からの空気が供給され、石炭・石灰石及び空気によって加圧流動床ボ イラ１内に加圧流動層が形成され、石炭が燃焼すると共に石灰石によって燃焼ガ ス中の脱硫が行われる。FIG. 4 shows the conventional pressurized fluidized bed boiler plant. Reference numeral 1 is a pressurized fluidized bed boiler equipped with a pressurized container 2. In the pressurized fluidized bed boiler 1, coal and limestone are supplied from a coal / limestone supply system 3 and also via a supply air system 21. Air from an air compressor, which will be described later, is supplied, and a pressurized fluidized bed is formed in the pressurized fluidized bed boiler 1 by the coal, limestone, and air, and coal burns and limestone desulfurizes the combustion gas. Be seen.
【０００５】 一方、加圧流動床ボイラ１内には、給水系統２５から水が供給される伝熱管４ ａが装備されており、同伝熱管４ａ内で発生した蒸気は、主蒸気系統２６ａを経 て発電機３１に直結された蒸気タービン３２の駆動用主蒸気として蒸気タービン ３２へ供給され、また蒸気タービン３２から抽気された蒸気は、加圧流動床ボイ ラ１内の伝熱管４ｂへ供給されて再熱された上再熱蒸気系統２６ｂを経て蒸気タ ービン３２へ再び供給される。On the other hand, the pressurized fluidized bed boiler 1 is equipped with a heat transfer tube 4a to which water is supplied from a water supply system 25, and steam generated in the heat transfer tube 4a is fed to the main steam system 26a. After that, the steam is supplied to the steam turbine 32 as the main steam for driving the steam turbine 32 directly connected to the generator 31, and the steam extracted from the steam turbine 32 is supplied to the heat transfer tube 4b in the pressurized fluidized bed boiler 1. The reheated steam is supplied to the steam turbine 32 through the reheated steam system 26b.
【０００６】 加圧流動床ボイラ１で発生した燃焼ガスは、同加圧流動床ボイラ１内のサイク ロン５及び同加圧流動床ボイラ１外の高温脱じん装置６で脱じんされた上、高温 ガス系統２２を経て発電機７と空気圧縮機９に直結されたガスタービン８へ供給 されて同ガスタービン８を駆動する。空気圧縮機９で発生した圧力空気は、前記 のように空気系統２１を経て加圧流動床ボイラ１内へ供給され、また、その１部 は石炭・石灰石供給システム３の搬送用空気として利用される。The combustion gas generated in the pressurized fluidized bed boiler 1 is dedusted by a cyclone 5 in the pressurized fluidized bed boiler 1 and a high temperature dedusting device 6 outside the pressurized fluidized bed boiler 1, and It is supplied to the gas turbine 8 directly connected to the generator 7 and the air compressor 9 via the high temperature gas system 22, and drives the gas turbine 8. The compressed air generated in the air compressor 9 is supplied into the pressurized fluidized bed boiler 1 through the air system 21 as described above, and a part of the compressed air is used as the carrier air of the coal / limestone supply system 3. It
【０００７】 前記ガスタービン８の出口を煙突１８に接続する低温ガス系統２３には、アン モニア（ＮＨ3 ）を排ガス中に注入し、かつ、脱硝触媒が充填された脱硝装置１ ２及び同脱硝装置１２の下流側に排熱回収熱交換器１１が設置されており、ガス タービン８を出た排ガスは、脱硝及び熱回収が行われた上煙突１８から排出され る。In the low temperature gas system 23 connecting the outlet of the gas turbine 8 to the chimney 18, ammonia (NH 3 ) is injected into the exhaust gas, and a denitration device 12 and a denitration device which are filled with a denitration catalyst. An exhaust heat recovery heat exchanger 11 is installed on the downstream side of the device 12, and the exhaust gas discharged from the gas turbine 8 is exhausted from the upper chimney 18 where denitration and heat recovery have been performed.
【０００８】 前記蒸気タービン３２を出た蒸気は、復水器２３で凝縮されて復水となり、復 水ポンプ３５で加圧され、給水加熱器３４で加熱され復水系統２４を経て給水ポ ンプ３６に入り、同給水ポンプ３６で加圧された水は、給水系統２５へ入り前記 排熱回収熱交換器１１で排ガスと熱交換して加熱された上、加圧流動床ボイラ１ 内の前記伝熱管４ａへ供給される。The steam exiting the steam turbine 32 is condensed in a condenser 23 to become condensed water, pressurized by a condensate pump 35, heated by a feed water heater 34, and passed through a condensate system 24 to a feed water pump. The water that has entered 36 and has been pressurized by the water supply pump 36 enters the water supply system 25 and is heated by exchanging heat with the exhaust gas in the exhaust heat recovery heat exchanger 11 and then in the pressurized fluidized bed boiler 1. It is supplied to the heat transfer tube 4a.
【０００９】[0009]
前記の従来の加圧流動床ボイラプラントにおいては、排熱回収熱交換器１１に よって熱回収されて排ガスの温度が低下して煙突１８から排出されるが、このよ うに排ガスの温度が低下することに伴なって、排ガスに含まれるＳＯ3 と脱硝装 置１２からの残留アンモニア（ＮＨ3 ）が反応して酸性硫安（ＮＨ4 ＨＳＯ4 ） がミスト状態で排ガス中に析出してくる。この酸性硫安の発生量を抑えるために は、脱硝装置における脱硝触媒によるＳＯ2 のＳＯ3 への転換率を極力低減させ る必要があるが、従来は有効な手段がなかった。In the above-mentioned conventional pressurized fluidized bed boiler plant, heat is recovered by the exhaust heat recovery heat exchanger 11 and the temperature of the exhaust gas lowers and is discharged from the chimney 18. However, the temperature of the exhaust gas lowers in this way. Accompanying this, SO 3 contained in the exhaust gas reacts with residual ammonia (NH 3 ) from the denitration device 12, and acidic ammonium sulfate (NH 4 HSO 4 ) precipitates in the exhaust gas in the mist state. In order to suppress the amount of generated acidic ammonium sulfate, it is necessary to reduce the conversion rate of SO 2 to SO 3 by the denitration catalyst in the denitration device as much as possible, but heretofore no effective means has been available.
【００１０】 この問題を解決する一つの対策として、従来のボイラと同様に、ガスタービン 出口の下流側に電気集じん器を装備することも考えられるが、加圧流動床ボイラ はコンバインドプラントであるためガスタービンの排出側に電気集じん器をつけ ると、単にコストが上昇するだけでなくガスタービンの排気圧力が上昇してガス タービンの出力が低下する。この結果、プラント効率も低下するという問題があ った。As one measure to solve this problem, it is conceivable to equip an electrostatic precipitator on the downstream side of the gas turbine outlet as in the conventional boiler, but the pressurized fluidized bed boiler is a combined plant. Therefore, if an electric precipitator is attached to the discharge side of the gas turbine, not only the cost will increase, but also the exhaust pressure of the gas turbine will increase and the output of the gas turbine will decrease. As a result, there was a problem that the plant efficiency was also reduced.
【００１１】 本考案は、以上の問題点を解決することができる流動床炉発電プラントを提供 しようとするものである。The present invention is intended to provide a fluidized bed reactor power plant that can solve the above problems.
【００１２】[0012]
（１） 本考案は、流動床炉、前記流動床炉の生成ガスで駆動されるガスタービ ン、及び前記ガスタービンの出口に接続された排ガス系統に設置された排熱回収 熱交換器とアンモニアが注入された排ガスが流過する脱硝触媒が充填された脱硝 装置を備えた流動床炉を備えた発電プラントにおいて、前記ガスタービンの出口 に接続された排ガス系統に上流側の第１排熱回収熱交換器と下流側の第２の排熱 回収熱交換器を設け、前記排ガス系統の前記両排熱回収熱交換器の間に脱硝装置 を設置したことを特徴とする。 (1) The present invention provides a fluidized bed furnace, a gas turbine driven by the gas produced by the fluidized bed furnace, and an exhaust heat recovery heat exchanger and ammonia installed in an exhaust gas system connected to the outlet of the gas turbine. In a power plant equipped with a fluidized bed furnace equipped with a denitration device filled with a denitration catalyst through which the injected exhaust gas flows, the first exhaust heat recovery heat upstream of the exhaust gas system connected to the outlet of the gas turbine. An exchanger and a second exhaust heat recovery heat exchanger on the downstream side are provided, and a denitration device is installed between the both exhaust heat recovery heat exchangers of the exhaust gas system.
【００１３】 （２）また、本考案は、前記（１）の流動床炉を備えた発電プラントにおいて 、前記脱硝装置の入口の排ガスの温度を検出する温度計及び前記温度計の信号に よって制御され前記第１の排熱回収熱交換における排ガスからの熱吸収量を制御 する手段を設けたことを特徴とする。(2) Further, in the present invention, in a power plant equipped with the fluidized bed furnace of (1), a thermometer for detecting the temperature of the exhaust gas at the inlet of the denitration device and control by a signal of the thermometer. Means for controlling the amount of heat absorbed from the exhaust gas in the first exhaust heat recovery heat exchange is provided.
【００１４】[0014]
前記のように、排ガスの温度が低下すると、脱硝装置出口の残留アンモニアと 排ガス中のＳＯ3 とが反応して酸性硫安が発生して析出するために、この酸性硫 安の発生，析出を避けるためには、脱硝装置におけるＳＯ2 からのＳＯ3 への転 換率を小さく抑える必要がある。このためには、図３に示すように、脱硝装置に おけるガス温度を低くすることが望ましい。一方、脱硝装置におけるガス温度を あまり低くすると、脱硝触媒の量を多くする必要があり、かつ、反応温度以下の ガス温度とした時には脱硝作用が消滅することとなる。As mentioned above, when the temperature of the exhaust gas decreases, the residual ammonia at the outlet of the denitration device reacts with SO 3 in the exhaust gas to generate and precipitate ammonium ammonium sulfate, so avoid the generation and precipitation of this ammonium sulfate. Therefore, it is necessary to suppress the conversion rate from SO 2 to SO 3 in the denitration device to be small. For this purpose, as shown in FIG. 3, it is desirable to lower the gas temperature in the denitration device. On the other hand, if the gas temperature in the denitration device is too low, it is necessary to increase the amount of denitration catalyst, and the denitration action disappears when the gas temperature is lower than the reaction temperature.
【００１５】 前記（１）の本考案では、脱硝装置の上流側に適当な熱吸収量をもつ第１の排 熱回収熱交換器を設け、脱硝装置へ流入するガスタービンよりの排ガスを適当な 温度に下げることによって、脱硝装置においては、ＳＯ2 からＳＯ3 への転換率 を小さく抑えると共に必要な脱硝作用が行われる。このように、ＳＯ3 の含有量 が少く、かつ、脱硝作用を受けた排ガスは、脱硝装置から第２の排熱回収熱交換 器へ流入してその排熱が回収される。第２の排熱回収熱交換器を出る排ガスの温 度は低下しているが、前記のようにＳＯ3 の含有量は少いために、これが残留ア ンモニアと反応して酸性硫安を発生することが抑制される。In the present invention of (1) above, a first exhaust heat recovery heat exchanger having an appropriate heat absorption amount is provided on the upstream side of the denitration device, and the exhaust gas from the gas turbine flowing into the denitration device is appropriately disposed. By lowering the temperature, in the denitration apparatus, the conversion rate from SO 2 to SO 3 is kept small and the required denitration action is performed. As described above, the exhaust gas having a low SO 3 content and subjected to the denitration action flows from the denitration device into the second exhaust heat recovery heat exchanger to recover the exhaust heat. Although the temperature of the exhaust gas exiting the second heat recovery heat exchanger is low, the SO 3 content is low as described above, and this reacts with residual ammonia to generate acidic ammonium sulfate. Is suppressed.
【００１６】 前記（２）の本考案では、前記（１）の本考案において、脱硝装置の入口の排 ガスの温度を温度計によって検出し、この信号によって、第１排熱回収熱交換器 の熱吸収量が制御される。これによって、プラント負荷の変動等があっても、脱 硝装置内の排ガスの温度が所定の値、即ち、前記のように脱硝作用を充分に行う と共にＳＯ2 からＳＯ3 への変換率を低く抑えることができるような値に保持さ れる。In the invention of (2) above, in the invention of (1) above, the temperature of the exhaust gas at the inlet of the denitration device is detected by a thermometer, and this signal is used to detect the temperature of the first exhaust heat recovery heat exchanger. The amount of heat absorption is controlled. As a result, even if the plant load fluctuates, the temperature of the exhaust gas in the denitration device will reach the specified value, that is, the denitration effect will be sufficient as described above and the conversion rate from SO 2 to SO 3 will be low. It is held at a value that can be suppressed.
【００１７】[0017]
本考案の一実施例を、図１に示す。本実施例は、図４に示す加圧流動床ボイラ プラントと同様な構成をもつ加圧流動床ボイラプラントであり、以下、相違する 点について説明する。なお、図１において対応する部分には図４におけると同じ 符号が付せられている。 One embodiment of the present invention is shown in FIG. The present embodiment is a pressurized fluidized bed boiler plant having the same configuration as the pressurized fluidized bed boiler plant shown in FIG. 4, and the differences will be described below. The corresponding parts in FIG. 1 are designated by the same reference numerals as in FIG.
【００１８】 ガスタービン８の出口に接続された低温ガス系統２３には、上流側に第１の排 熱回収熱交換器１０、下流側に第２の排熱回収熱交換器１１が設けられ、前記低 ガス系統２３の両熱交換器１０，１１の間には、アンモニアが注入された排ガス が流過する脱硝触媒が充填された脱硝装置１２が設けられている。The low temperature gas system 23 connected to the outlet of the gas turbine 8 is provided with a first exhaust heat recovery heat exchanger 10 on the upstream side and a second exhaust heat recovery heat exchanger 11 on the downstream side, Between the heat exchangers 10 and 11 of the low gas system 23, there is provided a denitration device 12 filled with a denitration catalyst through which exhaust gas injected with ammonia flows.
【００１９】 給水ポンプ３６に接続された給水系統２５は、先ず第２の排熱回収熱交換器１ １を通り、次いで第１の排熱回収熱交換器１０を通った上、加圧流動床ボイラ１ の伝熱管４ａに供給されるようになっている。The water supply system 25 connected to the water supply pump 36 first passes through the second exhaust heat recovery heat exchanger 11 and then the first exhaust heat recovery heat exchanger 10 and then the pressurized fluidized bed. The heat is transferred to the heat transfer tube 4a of the boiler 1.
【００２０】 前記給水系統２５の第１及び第２の排熱回収熱交換器１０，１１の間から流量 調整弁１３をもつ給水バイパス系統１６が分岐し、同給水バイパス系統１６は第 １の排熱回収熱交換器１０をバイパスして同熱交換器１０の出口側に設けられた 流量調整弁１４の下流側で給水系統に２５に合流している。A water supply bypass system 16 having a flow rate adjusting valve 13 branches from between the first and second exhaust heat recovery heat exchangers 10 and 11 of the water supply system 25, and the water supply bypass system 16 has a first exhaust heat recovery system. It bypasses the heat recovery heat exchanger 10 and joins the water supply system 25 downstream of the flow rate adjusting valve 14 provided on the outlet side of the heat exchanger 10.
【００２１】 ４０は脱硝装置１２の入口側の排ガス温度を検出する温度計であり、その信号 はガス温度制御器４１に入力され、同制御器４１の信号によって前記流量調整弁 １３，１４が制御されるようになっている。Reference numeral 40 is a thermometer for detecting the temperature of the exhaust gas at the inlet side of the denitration device 12, the signal of which is input to the gas temperature controller 41, and the flow rate adjusting valves 13 and 14 are controlled by the signal of the controller 41. It is supposed to be done.
【００２２】 本実施例では、適当な熱吸収量をもつ第１の排熱回収熱交換器１０において、 排ガスと給水との間に熱交換が行われて排ガスの温度が降下し、排ガスは、充分 な脱硝作用を行うことができると共にＳＯ2 からのＳＯ3 の転換率を低く抑える ことができる温度で脱硝装置１２へ流入する。In the present embodiment, in the first exhaust heat recovery heat exchanger 10 having an appropriate heat absorption amount, heat exchange is performed between the exhaust gas and the feed water, the temperature of the exhaust gas drops, and the exhaust gas is It flows into the denitration device 12 at a temperature at which a sufficient denitration action can be performed and the conversion rate of SO 3 from SO 2 can be suppressed to a low level.
【００２３】 脱硝装置１２で脱硝され、かつ、ＳＯ3 の発生を抑えられた排ガスは、第２の 排熱回収熱交換器１１で給水との間に熱交換を行って更に温度を下げた上、脱硝 され、かつ、酸性硫安（ＮＨ4 ＨＳＯ4 ）の発生，析出がない状態で煙突１８か ら排出される。The exhaust gas that has been denitrified by the denitration device 12 and has suppressed the generation of SO 3 undergoes heat exchange with the feed water by the second exhaust heat recovery heat exchanger 11 to further lower the temperature. After being denitrified, and without generating or depositing acidic ammonium sulfate (NH 4 HSO 4 ), it is discharged from the stack 18.
【００２４】 また、プラント負荷の減低下等によって、脱硝装置１２へ流入する排ガスの温 度が低下した時には、温度計４０の信号によってガス温度制御器４１は流量調整 弁１４の開度を減ずると共に流量調整弁１３を開く。これにより、給水の一部は 給水バイパス系統１６を経て流れることとなり、第１の排熱回収熱交換器１０を 流れる給水流量が減少し、これによって、同熱交換器１０の熱吸収量が調整され 、脱硝装置１２に流入する排ガスの温度を適正な値に保つ。このようにして、本 実施例では、プラント負荷の変動等があっても、脱硝装置１２へ流入する排ガス の温度を常に適正な値に保持し、ＳＯ2 のＳＯ3 への転換を抑えながら充分な脱 硝を行うことができる。なお、本実施例において、第１の排熱回収熱交換器１０ における排ガス温度の低下は、通常のプラント負荷において５０℃程度とするの が望ましい。When the temperature of the exhaust gas flowing into the denitration device 12 decreases due to a decrease in the plant load or the like, the signal from the thermometer 40 causes the gas temperature controller 41 to decrease the opening degree of the flow control valve 14. The flow rate adjusting valve 13 is opened. As a result, a part of the water supply flows through the water supply bypass system 16, and the flow rate of the water supply flowing through the first exhaust heat recovery heat exchanger 10 is reduced, whereby the heat absorption amount of the heat exchanger 10 is adjusted. Then, the temperature of the exhaust gas flowing into the denitration device 12 is maintained at an appropriate value. In this way, in this embodiment, the temperature of the exhaust gas flowing into the denitration device 12 is always kept at an appropriate value even if there is a fluctuation in the plant load, and the conversion of SO 2 to SO 3 is suppressed while being sufficient. Denitration can be performed. In the present embodiment, it is desirable that the temperature of the exhaust gas in the first exhaust heat recovery heat exchanger 10 is lowered to about 50 ° C. under a normal plant load.
【００２５】 本実施例と図４に示す従来のプラントにおける脱硝装置の入口ガス温度とＳＯ 2 →ＳＯ3 転換率のプラント出力に対する関係を図２に示す。同図２においては 、本実施例は本考案として示されている。図２に示すように、本実施例において は、従来のプラントに比して脱硝装置の入口ガス温度を５０℃程度低くしており 、また、ＳＯ3 転換率はプラント出力以下に拘らず従来のプラントに比して著し く低くすることができる。The inlet gas temperature and SO of the denitration device in this example and the conventional plant shown in FIG. 2 → SO3The relationship between conversion rate and plant output is shown in FIG. In FIG. 2, this embodiment is shown as the present invention. As shown in FIG. 2, in the present embodiment, the inlet gas temperature of the denitration device is lower by about 50 ° C. than in the conventional plant, and the SO3The conversion rate can be markedly lower than that of conventional plants regardless of plant output or less.
【００２６】 なお、本実施例は加圧流動床ボイラを用いたプラントに係るが、本考案では、 常圧の流動床ボイラを用いることもでき、また、本考案は、ガス化炉の高温生成 ガスによってガスタービンを駆動するプラント等流動床炉を備えた発電プラント にひろく適用することができる。In addition, although the present embodiment relates to a plant using a pressurized fluidized bed boiler, a fluidized bed boiler at normal pressure can be used in the present invention, and the present invention is directed to high temperature generation of a gasification furnace. It can be widely applied to a power plant equipped with a fluidized bed furnace such as a plant that drives a gas turbine with gas.
【００２７】[0027]
以上詳述したように、本考案は登録請求の範囲の請求項１及び２に記載の構成 を具備することによって、脱硝装置入口の排ガス温度を最適値にすることができ るので、脱硝触媒量又は触媒の種類を変更することなく充分な脱硝を行うことが できると共に、ＳＯ2 のＳＯ3 への転換率を低く保つことが可能となる。これに より、脱硝装置から排出される残留アンモニアと排ガス中に含まれるＳＯ3 とが 低温度域で反応することによって発生しバイジンとして取扱われる酸性硫安を大 幅に減少することができ、環境対策上有効である。As described above in detail, the present invention can optimize the exhaust gas temperature at the inlet of the denitration device by providing the configurations described in claims 1 and 2 of the registration claim, and therefore the denitration catalyst amount Alternatively, sufficient denitration can be performed without changing the type of catalyst, and the conversion rate of SO 2 to SO 3 can be kept low. As a result, it is possible to greatly reduce the amount of acidic ammonium sulfate that is generated as a result of reaction between residual ammonia discharged from the denitration equipment and SO 3 contained in the exhaust gas in the low temperature range and is treated as virgin. It is very effective.
【図１】本考案の一実施例の系統図である。FIG. 1 is a system diagram of an embodiment of the present invention.
【図２】同実施例と従来の加圧流動床ボイラプラントの
脱硝装置入口ガス温度とＳＯ2→ＳＯ3 転換率のプラン
ト出力に対する関係を示すグラフである。FIG. 2 is a graph showing a relationship between a denitration unit inlet gas temperature and a SO 2 → SO 3 conversion rate of the same example and a conventional pressurized fluidized bed boiler plant with respect to a plant output.
【図３】脱硝装置における入口ガス温度とＳＯ3 転換率
の関係を示すグラフである。FIG. 3 is a graph showing a relationship between an inlet gas temperature and a SO 3 conversion rate in a denitration device.
【図４】従来の加圧流動床ボイラプラントの系統図であ
る。FIG. 4 is a system diagram of a conventional pressurized fluidized bed boiler plant.
１ 加圧流動床ボイラ ２ 加圧容器 ３ 石炭・石灰石供給システム ４ａ，４ｂ 伝熱管 ７ 発電機 ８ ガスタービン ９ 空気圧縮機 １０ 第１の排熱回収熱交換器 １１ 第２の排熱回収熱交換器 １２ 脱硝装置 １３，１４ 流量調整弁 １６ 給水バイパス系統 ２３ 低温ガス系統 ２５ 給水系統 ３１ 発電機 ３２ 蒸気タービン ４０ 温度計 ４１ ガス温度制御器 1 Pressurized Fluidized Bed Boiler 2 Pressurized Container 3 Coal / Limestone Supply System 4a, 4b Heat Transfer Tube 7 Generator 8 Gas Turbine 9 Air Compressor 10 First Exhaust Heat Recovery Heat Exchanger 11 Second Exhaust Heat Recovery Heat Exchange 12 Denitration equipment 13, 14 Flow rate control valve 16 Water supply bypass system 23 Low temperature gas system 25 Water supply system 31 Generator 32 Steam turbine 40 Thermometer 41 Gas temperature controller
Claims (2)
動されるガスタービン、及び前記ガスタービンの出口に
接続された排ガス系統に設置された排熱回収熱交換器と
アンモニアが注入された排ガスが流過する脱硝触媒が充
填された脱硝装置を備えた流動床炉を備えた発電プラン
トにおいて、前記ガスタービンの出口に接続された排ガ
ス系統に上流側の第１の排熱回収熱交換器と下流側の第
２の排熱回収熱交換器を設け、前記排ガス系統の前記両
排熱回収熱交換器の間に脱硝装置を設置したことを特徴
とする流動床炉を備えた発電プラント。1. An exhaust heat recovery heat exchanger installed in a fluidized bed furnace, a gas turbine driven by generated gas of the fluidized bed furnace, and an exhaust gas system connected to an outlet of the gas turbine, and ammonia are injected. In a power plant equipped with a fluidized bed furnace equipped with a denitration device filled with a denitration catalyst through which exhaust gas flows, a first exhaust heat recovery heat exchange upstream of the exhaust gas system connected to the outlet of the gas turbine Plant and a second exhaust heat recovery heat exchanger on the downstream side, and a denitration device is installed between both of the exhaust heat recovery heat exchangers of the exhaust gas system, the power plant having a fluidized bed furnace .
出する温度計及び前記温度計の信号によって制御され前
記第１の排熱回収熱交換における排ガスからの熱吸収量
を制御する手段を設けたことを特徴とする請求項１に記
載の流動床炉を備えた発電プラント。2. A thermometer for detecting the temperature of the exhaust gas at the inlet of the denitration device and means for controlling the amount of heat absorbed from the exhaust gas in the first exhaust heat recovery heat exchange controlled by a signal from the thermometer. A power plant comprising the fluidized bed furnace according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1993000145U JP2583428Y2 (en) | 1993-01-07 | 1993-01-07 | Power plant with pressurized fluidized bed boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1993000145U JP2583428Y2 (en) | 1993-01-07 | 1993-01-07 | Power plant with pressurized fluidized bed boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0658104U true JPH0658104U (en) | 1994-08-12 |
| JP2583428Y2 JP2583428Y2 (en) | 1998-10-22 |
Family
ID=11465866
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1993000145U Expired - Lifetime JP2583428Y2 (en) | 1993-01-07 | 1993-01-07 | Power plant with pressurized fluidized bed boiler |
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| Country | Link |
|---|---|
| JP (1) | JP2583428Y2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014514491A (en) * | 2011-03-30 | 2014-06-19 | エミテック ゲゼルシヤフト フユア エミツシオンステクノロギー ミツト ベシユレンクテル ハフツング | Exhaust purification device for watercraft and method of operating the exhaust purification device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60122604U (en) * | 1984-01-20 | 1985-08-19 | 株式会社日立製作所 | Combined power plant |
| JPS60216010A (en) * | 1984-04-11 | 1985-10-29 | Toshiba Corp | Combined cycle plant |
| JPS6433417A (en) * | 1987-07-29 | 1989-02-03 | Mitsubishi Heavy Ind Ltd | Exhaust gas heat recovering system with denitrating device |
| JPH04272410A (en) * | 1991-02-28 | 1992-09-29 | Hitachi Ltd | Pressurized fluid layer boiler power generating plant |
-
1993
- 1993-01-07 JP JP1993000145U patent/JP2583428Y2/en not_active Expired - Lifetime
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60122604U (en) * | 1984-01-20 | 1985-08-19 | 株式会社日立製作所 | Combined power plant |
| JPS60216010A (en) * | 1984-04-11 | 1985-10-29 | Toshiba Corp | Combined cycle plant |
| JPS6433417A (en) * | 1987-07-29 | 1989-02-03 | Mitsubishi Heavy Ind Ltd | Exhaust gas heat recovering system with denitrating device |
| JPH04272410A (en) * | 1991-02-28 | 1992-09-29 | Hitachi Ltd | Pressurized fluid layer boiler power generating plant |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014514491A (en) * | 2011-03-30 | 2014-06-19 | エミテック ゲゼルシヤフト フユア エミツシオンステクノロギー ミツト ベシユレンクテル ハフツング | Exhaust purification device for watercraft and method of operating the exhaust purification device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2583428Y2 (en) | 1998-10-22 |
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