JP6709523B2 - Oxygen-fired boiler equipment - Google Patents

Oxygen-fired boiler equipment Download PDF

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JP6709523B2
JP6709523B2 JP2015202154A JP2015202154A JP6709523B2 JP 6709523 B2 JP6709523 B2 JP 6709523B2 JP 2015202154 A JP2015202154 A JP 2015202154A JP 2015202154 A JP2015202154 A JP 2015202154A JP 6709523 B2 JP6709523 B2 JP 6709523B2
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輝俊 内田
輝俊 内田
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本発明は、酸素燃焼ボイラ設備に関するものである。 The present invention relates to oxyfuel boiler equipment.

近年の石油及び天然ガスの需要の増大に伴う価格高騰等の情勢から、微粉炭焚ボイラを用いた石炭火力発電設備が重要な役割を占めるようになってきている。従来の微粉炭焚ボイラには、空気を燃焼用ガスとした空気燃焼ボイラが一般に使用されてきた。 Due to the recent situation such as soaring prices accompanying the increasing demand for oil and natural gas, coal-fired power generation facilities using pulverized coal-fired boilers have come to play an important role. As a conventional pulverized coal burning boiler, an air combustion boiler using air as a combustion gas has been generally used.

石炭燃焼それ自体には、石油・天然ガス燃焼と比較してＣＯ2排出量が多いという問題点があるため、石炭火力への依存比率の上昇に伴うＣＯ2排出量増大は、地球温暖化防止の観点から、回避しなければならない重要な課題である。 Coal combustion itself has a problem that CO 2 emission is larger than that of oil/natural gas combustion. Therefore, the increase in CO 2 emission due to the increase in the dependency ratio on coal-fired thermal power can prevent global warming. From the perspective of, it is an important issue that must be avoided.

又、空気燃焼ボイラでは、燃料である微粉炭の搬送用ガス及び燃焼用ガスとして空気が用いられるが、その組成は約八割が窒素、約二割が酸素である。これにより、排ガス中に多量の窒素が含まれることになるため、排ガスから窒素及びＣＯ2を分離回収する作業が面倒になるという問題がある。 Further, in an air-fired boiler, air is used as a carrier gas and a combustion gas for pulverized coal which is a fuel, and its composition is about 80% nitrogen and about 20% oxygen. As a result, a large amount of nitrogen is contained in the exhaust gas, which causes a problem that the work of separating and recovering nitrogen and CO 2 from the exhaust gas becomes troublesome.

そこで、大気中へのＣＯ2排出量を大幅に削減できる手法として、酸素燃焼ボイラが注目され、その開発が進められている。 Therefore, an oxyfuel boiler has attracted attention as a method capable of significantly reducing CO 2 emission into the atmosphere, and its development is being promoted.

前記酸素燃焼ボイラでは、微粉炭を燃やす酸素燃焼ボイラから排出される排ガスの大半を煙道の中途から抜き出し、この抜き出した排ガスと酸素製造装置で製造した酸素とを混合して酸素濃度を調整した燃焼用ガスを前記酸素燃焼ボイラに供給するようにした排ガス再循環方式が採用されている。この排ガス再循環方式の酸素燃焼ボイラによれば、排ガス中に窒素が含まれず、排出される最終的な排ガスのＣＯ2濃度が飛躍的に高まり、よって、排ガスからのＣＯ2の分離回収作業が容易になる。 In the oxyfuel boiler, most of the exhaust gas discharged from the oxyfuel boiler that burns pulverized coal is extracted from the middle of the flue, and the extracted exhaust gas and oxygen produced by the oxygen production device are mixed to adjust the oxygen concentration. An exhaust gas recirculation system is adopted in which combustion gas is supplied to the oxyfuel boiler. According to this oxyfuel combustion boiler of the exhaust gas recirculation system, nitrogen is not contained in the exhaust gas, and the CO 2 concentration of the final exhaust gas that is discharged is dramatically increased, so that the CO 2 separation and recovery work from the exhaust gas can be performed. It will be easier.

尚、酸素燃焼ボイラと関連する一般的技術水準を示すものとしては、例えば、特許文献１がある。 In addition, as a thing showing the general technical level relevant to an oxyfuel boiler, there exists patent document 1, for example.

特開２０１４−５９１０４号公報JP, 2014-59104, A

ところで、前記酸素燃焼ボイラにおける酸素燃焼運転時には、前記排ガスを微粉炭の搬送用ガスとしても再循環させるようになっている。このため、石炭を微粉砕するミルに接続される微粉炭管中の水分が高くなり、酸露点（亜硫酸ガスが硫酸となって結露する温度）が下がって腐食の可能性が高まる。又、前記微粉炭管中の水分が高くなると、微粉炭の充分な乾燥ができなくなり、搬送や燃焼にも悪影響が出るため、前記微粉炭の搬送用ガスの再循環ライン途中に脱水装置が設けられ、ミルでの微粉炭の乾燥性を高めるようになっている。 By the way, during the oxyfuel combustion operation in the oxyfuel boiler, the exhaust gas is recirculated as a pulverized coal carrier gas. For this reason, the water content in the pulverized coal pipe connected to the mill for pulverizing coal becomes high, the acid dew point (the temperature at which sulfurous acid gas turns into sulfuric acid and dew) is lowered, and the possibility of corrosion increases. Further, if the water content in the pulverized coal pipe becomes high, the pulverized coal cannot be dried sufficiently, which adversely affects transportation and combustion.Therefore, a dehydrator is installed in the recirculation line of the pulverized coal transportation gas. It is designed to improve the dryness of pulverized coal in the mill.

一方、前記酸素燃焼ボイラにおける空気燃焼運転時には、前記微粉炭の搬送用ガスとして空気が用いられるため、該空気は前記脱水装置を通過させずに迂回させるようになっている。ここで、前記脱水装置は非常に圧力損失の高い機器であるため、空気燃焼運転時と酸素燃焼運転時とで、搬送用ガスの流通系統における圧力損失の合計が大きく変わってくる。これにより、押込通風機を容量の大きいものにしなければならなくなると共に、酸素燃焼運転時に再循環させる排ガスが燃焼用ガスの流通系統にばかり流れることを防止すべく、前記脱水装置と同等の流通抵抗を付与するためのダンパ等の追加機器を燃焼用ガスの流通系統に設けることが必要となっていた。 On the other hand, during the air combustion operation in the oxyfuel boiler, since air is used as a carrier gas for the pulverized coal, the air is bypassed without passing through the dehydrator. Here, since the dehydrator is a device having a very high pressure loss, the total pressure loss in the distribution system of the carrier gas greatly changes between the air combustion operation and the oxyfuel operation. As a result, the forced draft fan must have a large capacity, and in order to prevent the exhaust gas to be recirculated during oxyfuel combustion from flowing only to the distribution system of the combustion gas, a flow resistance equivalent to that of the dehydration device. It has been necessary to provide an additional device such as a damper for providing the combustion gas in the distribution system of the combustion gas.

本発明は、上記従来の問題点に鑑みてなしたもので、押込通風機の大容量化を阻止して、流通抵抗を付与するための追加機器を不要とし得る酸素燃焼ボイラ設備を提供しようとするものである。 The present invention has been made in view of the above conventional problems, and it is an object of the present invention to provide an oxyfuel boiler facility that can prevent the increase in capacity of a forced draft fan and eliminate the need for an additional device for imparting flow resistance. To do.

本発明は、ボイラから排出される排ガスを燃料の燃焼用ガスとして再循環させる排ガス再循環ラインに押込通風機が設けられた酸素燃焼ボイラ設備であって、
前記排ガスを前記押込通風機と並列に設けられる一次通風機の作動により燃料の搬送用ガスとして再循環させる分岐排ガス再循環ラインを備え、
脱水装置は、前記一次通風機の入側の分岐排ガス再循環ラインに設けられ、
前記一次通風機の入側の分岐排ガス再循環ラインに、前記脱水装置の入側の排ガスによって前記脱水装置の出側の排ガスを加熱する加熱器が設けられる酸素燃焼ボイラ設備にかかるものである。
The present invention is an oxyfuel boiler facility in which a forced draft fan is provided in an exhaust gas recirculation line for recirculating exhaust gas discharged from a boiler as combustion gas for fuel,
A branch exhaust gas recirculation line for recirculating the exhaust gas as a gas for carrying fuel by the operation of a primary fan provided in parallel with the forced draft fan;
The dehydrator is provided in the branch exhaust gas recirculation line on the inlet side of the primary fan,
The present invention relates to an oxyfuel boiler facility in which a heater for heating the exhaust gas on the outlet side of the dehydrator by the exhaust gas on the inlet side of the dehydrator is provided in the branch exhaust gas recirculation line on the inlet side of the primary fan.

前記酸素燃焼ボイラ設備においては、前記排ガス再循環ラインにより再循環される燃焼用ガスに酸素を供給する酸素製造装置を備え、該酸素製造装置からの酸素を、再循環される排ガスに対し前記押込通風機の入側で混合するよう構成することが好ましい。 In the oxyfuel boiler equipment, an oxygen production device for supplying oxygen to the combustion gas recirculated by the exhaust gas recirculation line is provided, and oxygen from the oxygen production device is pushed into the recirculated exhaust gas. It is preferable that the mixing is performed on the inlet side of the fan.

本発明の酸素燃焼ボイラ設備によれば、押込通風機の大容量化を阻止して、流通抵抗を付与するための追加機器を不要とし得るという優れた効果を奏し得る。 According to the oxyfuel boiler equipment of the present invention, it is possible to obtain an excellent effect that an increase in capacity of the forced draft fan is prevented and an additional device for imparting flow resistance may be unnecessary.

本発明の酸素燃焼ボイラ設備の参考例を示す全体概要構成図であって、酸素燃焼運転時の状態を示す図である。It is a whole schematic block diagram which shows the reference example of the oxyfuel boiler equipment of this invention, and is a figure which shows the state at the time of oxyfuel combustion operation. 本発明の酸素燃焼ボイラ設備の参考例における空気燃焼運転時の状態を示す全体概要構成図である。It is the whole outline lineblock diagram showing the state at the time of air combustion operation in the reference example of the oxyfuel boiler equipment of the present invention. 本発明の酸素燃焼ボイラ設備の参考例の変形例を示す全体概要構成図であって、酸素燃焼運転時の状態を示す図である。It is a whole schematic block diagram which shows the modification of the reference example of the oxyfuel boiler equipment of this invention, and is a figure which shows the state at the time of oxyfuel combustion operation. 本発明の酸素燃焼ボイラ設備の実施例を示す全体概要構成図であって、酸素燃焼運転時の状態を示す図である。It is a whole schematic block diagram which shows the Example of the oxyfuel boiler equipment of this invention, Comprising: It is a figure which shows the state at the time of oxyfuel operation. 本発明の酸素燃焼ボイラ設備の実施例における空気燃焼運転時の状態を示す全体概要構成図である。It is the whole outline lineblock diagram showing the state at the time of air combustion operation in the example of the oxyfuel boiler equipment of the present invention. 本発明の酸素燃焼ボイラ設備の実施例の変形例を示す全体概要構成図であって、酸素燃焼運転時の状態を示す図である。A general outline configuration diagram showing a modification of the embodiment of the oxyfuel combustion boiler facility of the present invention, showing a state during oxyfuel combustion operation. 一般的な酸素燃焼ボイラ設備の一例を示す全体概要構成図であって、酸素燃焼運転時の状態を示す図である。It is a whole schematic block diagram which shows an example of general oxyfuel boiler equipment, and is a figure showing the state at the time of oxyfuel operation. 一般的な酸素燃焼ボイラ設備の一例における空気燃焼運転時の状態を示す全体概要構成図である。It is the whole outline lineblock diagram showing the state at the time of air combustion operation in an example of general oxyfuel boiler equipment.

以下、本発明の実施の形態を添付図面を参照して説明する。 Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings.

図１及び図２は本発明の酸素燃焼ボイラ設備の参考例である。 1 and 2 are reference examples of the oxyfuel boiler equipment of the present invention.

図１及び図２に示す酸素燃焼ボイラ設備は、ボイラ１と、ミル２と、予熱器３，４と、排ガスクーラ５と、脱塵装置６と、誘引通風機７（ＩＤＦ）と、排ガスライン８と、排ガス再循環ライン８Ｒと、押込通風機９（ＦＤＦ）と、酸素製造装置１０とを備えている。 The oxyfuel boiler equipment shown in FIGS. 1 and 2 includes a boiler 1, a mill 2, preheaters 3 and 4, an exhaust gas cooler 5, a dust removing device 6, an induction fan 7 (IDF), and an exhaust gas line. 8, an exhaust gas recirculation line 8R, a forced draft fan 9 (FDF), and an oxygen production device 10.

前記ボイラ１は、燃料を燃焼用ガスにより燃焼させて蒸気を発生し、排ガスを排ガスライン８へ排出するようになっている。前記ミル２は、前記燃料としての石炭を微粉砕するようになっている。前記予熱器３は、前記ミル２へ導入される搬送用ガスを前記ボイラ１から排出される排ガスによって予熱するようになっている。前記予熱器４は、前記ボイラ１から排出される排ガスによって前記燃焼用ガスを予熱するようになっている。前記排ガスクーラ５は、前記予熱器４を通過した排ガスを冷却するようになっている。前記脱塵装置６は、バグフィルタ或いは電気集塵機であって、前記排ガスクーラ５で冷却された排ガス中の煤塵を捕集するようになっている。前記排ガス再循環ライン８Ｒは、前記脱塵装置６で煤塵が捕集された排ガスを前記誘引通風機７と押込通風機９の作動により前記ボイラ１の燃焼用ガス及び微粉炭の搬送用ガスとして再循環させるようになっている。前記酸素製造装置１０は、図１に示す如く、前記ボイラ１の燃焼用ガスとして再循環される排ガスに酸素を供給するようになっている。 The boiler 1 burns fuel with a combustion gas to generate steam, and discharges exhaust gas to an exhaust gas line 8. The mill 2 finely pulverizes coal as the fuel. The preheater 3 preheats the carrier gas introduced into the mill 2 with the exhaust gas discharged from the boiler 1. The preheater 4 preheats the combustion gas with the exhaust gas discharged from the boiler 1. The exhaust gas cooler 5 cools the exhaust gas that has passed through the preheater 4. The dust removing device 6 is a bag filter or an electric dust collector, and is configured to collect the soot dust in the exhaust gas cooled by the exhaust gas cooler 5. The exhaust gas recirculation line 8R serves as a combustion gas for the boiler 1 and a carrier gas for pulverized coal by operating the attracting fan 7 and the forced draft fan 9 so that the exhaust gas in which the dust is collected by the dust removing device 6 is operated. It is designed to be recycled. As shown in FIG. 1, the oxygen production apparatus 10 is adapted to supply oxygen to exhaust gas recirculated as combustion gas for the boiler 1.

本参考例の場合、前記排ガス再循環ライン８Ｒにおける押込通風機９の入側に、再循環される排ガスから水分を除去する脱水装置１１を設けると共に、該脱水装置１１の入側の排ガスによって前記脱水装置１１の出側の排ガスを加熱する加熱器としてのガスガスヒータ１２を設けてある。尚、前記脱水装置１１は、空気燃焼運転時における空気取入口１４（図２参照）より上流位置に設けられている。 In the case of the present reference example , a dehydrator 11 for removing water from the recirculated exhaust gas is provided on the inlet side of the forced draft fan 9 in the exhaust gas recirculation line 8R, and the exhaust gas on the inlet side of the dehydrator 11 causes A gas gas heater 12 is provided as a heater for heating exhaust gas on the outlet side of the dehydrator 11. The dehydrator 11 is provided at a position upstream of the air intake 14 (see FIG. 2) during the air combustion operation.

尚、前記誘引通風機７の出側の排ガスライン８からは抜出ライン８Ｄを分岐させ、該抜出ライン８Ｄから排ガスの一部をＣＯ２濃縮ユニットへ送出するようになっている。 An extraction line 8D is branched from the exhaust gas line 8 on the outlet side of the induction fan 7, and a part of the exhaust gas is sent to the CO 2 concentration unit from the extraction line 8D.

又、図１には酸素燃焼運転時の状態を示しているが、図２には空気燃焼運転時の状態を示している。図２に示す空気燃焼運転時の場合、仮想線で示す如く、前記酸素製造装置１０、脱水装置１１、及びガスガスヒータ１２は使用されず、空気取入口１４から空気が取り入れられると共に、前記ボイラ１から排出される排ガスは、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットではなく、煙突へ送出されるようになっている。因みに、前記脱水装置１１及びガスガスヒータ１２は、前記抜出ライン８Ｄの分岐点より下流側における排ガス再循環ライン８Ｒに設けられている。 Further, FIG. 1 shows the state during the oxyfuel combustion operation, while FIG. 2 shows the state during the air combustion operation. In the air combustion operation shown in FIG. 2, as indicated by the phantom line, the oxygen production device 10, the dehydration device 11 and the gas gas heater 12 are not used, and air is taken in from the air inlet 14 and the boiler 1 is used. The exhaust gas discharged from the exhaust fan 7 is sent from the exhaust gas line 8 on the outlet side of the induction fan 7 to the chimney, not to the CO 2 concentration unit, through the extraction line 8D. Incidentally, the dehydrator 11 and the gas gas heater 12 are provided in the exhaust gas recirculation line 8R on the downstream side of the branch point of the extraction line 8D.

次に、上記参考例の作用を説明する。 Next, the operation of the above reference example will be described.

ミル２で石炭を微粉砕した燃料としての微粉炭は、予熱器３で予熱された搬送用ガスにより乾燥されつつボイラ１へ供給され、該ボイラ１において予熱器４で予熱された燃焼用ガスにより燃焼し、その燃焼熱によって蒸気が発生される。 Pulverized coal as a fuel obtained by finely pulverizing coal in the mill 2 is supplied to the boiler 1 while being dried by the carrier gas preheated in the preheater 3 and by the combustion gas preheated in the preheater 4 in the boiler 1. It burns and the heat of combustion produces steam.

前記ボイラ１から排ガスライン８へ排出される排ガスは、予熱器３を通過する際に前記搬送用ガスに熱を与え、更に予熱器４を通過する際に前記燃焼用ガスに熱を与える。 The exhaust gas discharged from the boiler 1 to the exhaust gas line 8 gives heat to the carrier gas when passing through the preheater 3, and gives heat to the combustion gas when passing through the preheater 4.

酸素燃焼ボイラ設備の酸素燃焼運転時には、前記予熱器４を通過した排ガスは、排ガスクーラ５で冷却され、脱塵装置６で煤塵が捕集され、誘引通風機７で昇圧された後、図１に示す如く、脱水装置１１で水分が除去される。該脱水装置１１で水分が除去された排ガスは、ガスガスヒータ１２を通過する際に前記脱水装置１１の入側の排ガスによって加熱された後、押込通風機９へ導かれ、該押込通風機９の作動により排ガス再循環ライン８Ｒから前記ボイラ１の燃焼用ガス及び微粉炭の搬送用ガスとして再循環される。前記燃焼用ガスは、前記予熱器４で予熱された後、酸素製造装置１０から酸素が供給され、ボイラ１へ導入される。前記ボイラ１から排出される排ガスの一部は、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットへ送出され、排ガスからのＣＯ2の分離回収作業が行われる。 During the oxyfuel combustion operation of the oxyfuel boiler equipment, the exhaust gas that has passed through the preheater 4 is cooled by the exhaust gas cooler 5, soot dust is collected by the dust removing device 6, and the pressure is increased by the induction fan 7, and then, as shown in FIG. As shown in, the dehydrator 11 removes water. The exhaust gas from which water has been removed by the dehydrator 11 is heated by the exhaust gas on the inlet side of the dehydrator 11 when passing through the gas gas heater 12, and is then guided to the forced draft fan 9 of the forced draft fan 9. Upon operation, it is recirculated from the exhaust gas recirculation line 8R as a combustion gas for the boiler 1 and a pulverized coal carrying gas. The combustion gas is preheated by the preheater 4, and then oxygen is supplied from the oxygen production device 10 to be introduced into the boiler 1. A part of the exhaust gas discharged from the boiler 1 is sent from the exhaust gas line 8 on the outlet side of the induced draft fan 7 to the CO 2 concentrating unit via the extraction line 8D, and the separation and recovery work of CO 2 from the exhaust gas is performed. Done.

一方、前記酸素燃焼ボイラ設備の空気燃焼運転時には、図２に示す如く、前記脱水装置１１及びガスガスヒータ１２は使用されず、前記押込通風機９の入側から空気が導入され、該空気が前記ボイラ１の燃焼用ガス及び微粉炭の搬送用ガスとして使用される。前記燃焼用ガスとして使用される空気は、前記予熱器４で予熱された後、酸素製造装置１０から酸素が供給されずに、そのままボイラ１へ導入される。前記ボイラ１から排出される排ガスは、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットではなく、煙突へ送出され、大気放出される。 On the other hand, during the air combustion operation of the oxyfuel boiler equipment, as shown in FIG. 2, the dehydrator 11 and the gas gas heater 12 are not used, and air is introduced from the inlet side of the forced draft fan 9 and the air It is used as a combustion gas for the boiler 1 and a carrier gas for pulverized coal. The air used as the combustion gas is preheated by the preheater 4 and then introduced into the boiler 1 without being supplied with oxygen from the oxygen production device 10. The exhaust gas discharged from the boiler 1 is sent from the exhaust gas line 8 on the outlet side of the induced draft fan 7 to the chimney, not to the CO 2 concentrating unit, through the extraction line 8D, and is discharged to the atmosphere.

因みに、一般的な酸素燃焼ボイラ設備の場合、図７に示す如く、脱水装置１１は、押込通風機９の出側における排ガス再循環ライン８Ｒから分岐して予熱器３へ通じる排ガス再循環ライン８Ｒ−１に設置されていた。つまり、非常に圧力損失の高い機器である脱水装置１１が押込通風機９の出側に存在していたため、押込通風機９を容量の大きいものにしなければならなくなると共に、酸素燃焼運転時に再循環させる排ガスが燃焼用ガスの流通系統にばかり流れることを防止すべく、前記脱水装置１１と同等の流通抵抗を付与するためのダンパ１５（図７の仮想線参照）等の追加機器を燃焼用ガスの流通系統に設けることが必要となっていたわけである。更に、酸素燃焼運転時の押込通風機９の入口ガス温度は、１３０〜１５０℃程度であるのに対し、空気燃焼運転時（図８参照）の押込通風機９の入口ガス（空気）温度は、大気温度と略等しく、３０℃程度である。このため、押込通風機９の入口ガス温度に関し、空気燃焼運転時と酸素燃焼運転時の温度差が大きくなり、空気燃焼運転と酸素燃焼運転の切替時間も長くなっていたのである。 Incidentally, in the case of a general oxyfuel boiler facility, as shown in FIG. 7, the dehydrator 11 branches off from the exhaust gas recirculation line 8R on the outlet side of the forced draft fan 9 and leads to the preheater 3 by the exhaust gas recirculation line 8R. It was installed at -1. That is, since the dehydrator 11 which is a device with a very high pressure loss was present on the outlet side of the forced draft fan 9, the forced draft fan 9 had to have a large capacity, and the recirculation was performed during the oxyfuel combustion operation. In order to prevent the exhaust gas to flow only into the distribution system of the combustion gas, an additional device such as a damper 15 (see the phantom line in FIG. 7) for imparting a distribution resistance equivalent to that of the dehydrator 11 is used as the combustion gas. It was necessary to install it in the distribution system of. Further, while the inlet gas temperature of the forced draft fan 9 during the oxyfuel combustion operation is about 130 to 150° C., the inlet gas (air) temperature of the forced draft fan 9 during the air combustion operation (see FIG. 8) is Is approximately equal to the atmospheric temperature and is about 30°C. Therefore, with respect to the inlet gas temperature of the forced draft fan 9, the temperature difference between the air combustion operation and the oxyfuel operation becomes large, and the switching time between the air combustion operation and the oxyfuel operation also becomes long.

しかし、本参考例のように、前記脱水装置１１を押込通風機９の入側に設置すると、押込通風機９の下流側の搬送用ガスと燃焼用ガスの圧力損失バランスが、空気燃焼運転時と酸素燃焼運転時で変わらなくなる。これにより、押込通風機９を容量の大きいものにしなくて済むと共に、酸素燃焼運転時に再循環させる排ガスが燃焼用ガスの流通系統にばかり流れることを防止すべく、前記脱水装置１１と同等の流通抵抗を付与するためのダンパ１５（図７の仮想線参照）等の追加機器を燃焼用ガスの流通系統に設けることが不要となる。この結果、酸素燃焼ボイラ設備の運用が制限されることもなくなる。 However, if the dewatering device 11 is installed on the inlet side of the forced draft fan 9 as in the present reference example , the pressure loss balance between the carrier gas and the combustion gas at the downstream side of the forced draft fan 9 is the same during air combustion operation. And it does not change during oxyfuel combustion operation. As a result, the forced draft fan 9 does not have to have a large capacity, and the exhaust gas to be recirculated during the oxyfuel combustion operation is prevented from flowing only to the distribution system of the combustion gas. It is not necessary to provide an additional device such as a damper 15 (see the phantom line in FIG. 7) for giving resistance to the combustion gas distribution system. As a result, the operation of the oxyfuel boiler equipment is not restricted.

更に、前記押込通風機９の入側の排ガス再循環ライン８Ｒに、前記脱水装置１１の入側の排ガスによって前記脱水装置１１の出側の排ガスを加熱する加熱器としてのガスガスヒータ１２を設置することで、熱損失が最小限に抑えられると同時に、脱水装置１１をコンパクトにし、押込通風機９に流入するガスの乾き度を確保することが可能となる。しかも、前記押込通風機９の入側に脱水装置１１及びガスガスヒータ１２を設置していない場合、酸素燃焼運転時の押込通風機９の入口ガス温度は、１３０〜１５０℃程度となるが、脱水装置１１及びガスガスヒータ１２の設置により７０〜９０℃程度に低下するため、空気燃焼運転時の押込通風機９の入口ガス（空気）温度（即ち、大気温度＝約３０℃）に近づくことになる。これによって、押込通風機９の入口ガス温度に関し、空気燃焼運転時と酸素燃焼運転時の温度差が小さくなり、空気燃焼運転と酸素燃焼運転の切替時間も短縮できる。 Further, a gas gas heater 12 is installed in the exhaust gas recirculation line 8R on the inlet side of the forced draft fan 9 as a heater for heating the exhaust gas on the outlet side of the dehydrator 11 by the exhaust gas on the inlet side of the dehydrator 11. As a result, the heat loss can be minimized, and at the same time, the dehydrator 11 can be made compact and the dryness of the gas flowing into the forced draft fan 9 can be secured. Moreover, when the dehydration device 11 and the gas gas heater 12 are not installed on the inlet side of the forced draft fan 9, the inlet gas temperature of the forced draft fan 9 during oxyfuel combustion operation is about 130 to 150° C. Since the temperature is lowered to about 70 to 90° C. by installing the device 11 and the gas gas heater 12, the temperature approaches the inlet gas (air) temperature of the forced draft fan 9 during air combustion operation (that is, atmospheric temperature=about 30° C.). . As a result, regarding the inlet gas temperature of the forced draft fan 9, the temperature difference between the air combustion operation and the oxyfuel operation becomes small, and the switching time between the air combustion operation and the oxyfuel operation can be shortened.

こうして、押込通風機９の大容量化を阻止して、流通抵抗を付与するための追加機器を不要とし得る。 In this way, it is possible to prevent an increase in capacity of the forced draft fan 9 and eliminate the need for an additional device for imparting flow resistance.

図３は本発明の酸素燃焼ボイラ設備の参考例の変形例であって、図中、図１及び図２と同一の符号を付した部分は同一物を表わしており、基本的な構成は図１及び図２に示す参考例と同様である。本変形例の特徴とするところは、図３に示す如く、前記脱水装置１１及び加熱器としてのガスガスヒータ１２による排ガスの圧力損失を補うよう前記押込通風機９の入側で且つ前記ガスガスヒータ１２の出側に補助通風機９´を設けた点にある。 FIG. 3 is a modification of the reference example of the oxyfuel boiler equipment of the present invention. In the figure, the parts denoted by the same reference numerals as those in FIGS. 1 and 2 represent the same things, and the basic configuration is as shown in FIG. 1 and the reference example shown in FIG. As shown in FIG. 3, the feature of this modification is that the dehydration device 11 and the gas gas heater 12 serving as a heater are provided on the inlet side of the forced draft fan 9 and the gas gas heater 12 so as to compensate the pressure loss of the exhaust gas. The auxiliary ventilator 9'is provided on the outlet side of the.

図３に示す変形例のように補助通風機９´を設けると、前記脱水装置１１及び加熱器としてのガスガスヒータ１２による排ガスの圧力損失を補うことが可能となり、押込通風機９や誘引通風機７に対して容量的に更に余裕を持たせることができ、好ましい。 When the auxiliary ventilator 9'is provided as in the modification shown in FIG. 3, it becomes possible to compensate for the pressure loss of the exhaust gas due to the dehydration device 11 and the gas gas heater 12 as the heater, and the forced draft fan 9 and the induced draft fan. It is preferable because it is possible to further allow the capacity of 7 in terms of capacity.

図４及び図５は本発明の酸素燃焼ボイラ設備の実施例であって、図中、図１及び図２と同一の符号を付した部分は同一物を表わしており、基本的な構成は図１及び図２に示す参考例と同様である。 4 and 5 is an embodiment of the oxyfuel combustion boiler facility of the present invention, in the figure, portions denoted by the same reference numerals as in FIGS. 1 and 2 represents the same parts, basic configuration diagram 1 and the reference example shown in FIG.

本実施例では、図４及び図５に示す如く、前記排ガス再循環ライン８Ｒにおける押込通風機９の入側（前記抜出ライン８Ｄの分岐点より下流側）から分岐して排ガスの一部を予熱器３へ導く分岐排ガス再循環ライン８Ｒ´を設け、該分岐排ガス再循環ライン８Ｒ´には、前記押込通風機９と並列に配置される一次通風機１３を設けてある。前記分岐排ガス再循環ライン８Ｒ´における一次通風機１３の入側、即ち押込通風機９より少なくとも上流位置で且つ空気燃焼運転時における空気取入口１４（図５参照）より上流位置には、再循環される排ガスから水分を除去する脱水装置１１を設けると共に、該脱水装置１１の入側の排ガスによって前記脱水装置１１の出側の排ガスを加熱する加熱器としてのガスガスヒータ１２を設けてある。 In this embodiment , as shown in FIGS. 4 and 5, part of the exhaust gas is branched from the inlet side of the forced draft fan 9 in the exhaust gas recirculation line 8R (downstream from the branch point of the extraction line 8D). A branch exhaust gas recirculation line 8R′ leading to the preheater 3 is provided, and the branch exhaust gas recirculation line 8R′ is provided with a primary fan 13 arranged in parallel with the forced draft fan 9. Recirculation is performed on the branch exhaust gas recirculation line 8R' at the inlet side of the primary fan 13, that is, at a position at least upstream from the forced draft fan 9 and upstream from the air intake 14 (see FIG. 5) during air combustion operation. A dehydrator 11 for removing water from the exhaust gas is provided, and a gas gas heater 12 as a heater for heating the exhaust gas on the outlet side of the dehydrator 11 by the exhaust gas on the inlet side of the dehydrator 11.

尚、図４には酸素燃焼運転時の状態を示しているが、図５には空気燃焼運転時の状態を示している。図５に示す空気燃焼運転時の場合、仮想線で示す如く、前記酸素製造装置１０、脱水装置１１、及びガスガスヒータ１２は使用されず、空気取入口１４から空気が取り入れられて押込通風機９及び一次通風機１３により圧送されると共に、前記ボイラ１から排出される排ガスは、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットではなく、煙突へ送出されるようになっている。 4 shows the state during the oxyfuel combustion operation, while FIG. 5 shows the state during the air combustion operation. In the air combustion operation shown in FIG. 5, the oxygen producing device 10, the dehydrating device 11 and the gas gas heater 12 are not used as indicated by the phantom line, and air is taken in from the air intake port 14 and the forced draft fan 9 is used. The exhaust gas discharged from the boiler 1 while being pressure-fed by the primary fan 13 is sent from the exhaust gas line 8 on the outlet side of the induction fan 7 to the chimney instead of the CO 2 concentration unit via the extraction line 8D. It is supposed to be done.

次に、上記実施例の作用を説明する。 Next, the operation of the above embodiment will be described.

酸素燃焼ボイラ設備の酸素燃焼運転時には、予熱器４を通過した排ガスは、排ガスクーラ５で冷却され、脱塵装置６で煤塵が捕集され、誘引通風機７で昇圧された後、図４に示す如く、押込通風機９の作動により排ガス再循環ライン８Ｒから前記ボイラ１の燃焼用ガスとして再循環される。前記燃焼用ガスは、前記予熱器４で予熱された後、酸素製造装置１０から酸素が供給され、ボイラ１へ導入される。前記誘引通風機７で昇圧された排ガスの一部は分岐排ガス再循環ライン８Ｒ´へ導かれ、脱水装置１１で水分が除去される。該脱水装置１１で水分が除去された排ガスは、ガスガスヒータ１２を通過する際に前記脱水装置１１の入側の排ガスによって加熱された後、一次通風機１３へ導かれ、該一次通風機１３の作動により分岐排ガス再循環ライン８Ｒ´から予熱器３を経由し前記ミル２の微粉炭の搬送用ガスとして再循環される。前記ボイラ１から排出される排ガスの一部は、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットへ送出され、排ガスからのＣＯ2の分離回収作業が行われる。 During the oxyfuel combustion operation of the oxyfuel boiler equipment, the exhaust gas that has passed through the preheater 4 is cooled by the exhaust gas cooler 5, soot dust is collected by the dust remover 6, and the pressure is increased by the induced draft fan 7, and then in FIG. As shown, the forced draft fan 9 is operated to recirculate the exhaust gas recirculation line 8R as combustion gas for the boiler 1. The combustion gas is preheated by the preheater 4, and then oxygen is supplied from the oxygen production apparatus 10 to be introduced into the boiler 1. A part of the exhaust gas whose pressure has been raised by the induced draft fan 7 is guided to the branched exhaust gas recirculation line 8R', and the dehydrator 11 removes water. The exhaust gas from which moisture has been removed by the dehydrator 11 is heated by the exhaust gas on the inlet side of the dehydrator 11 when passing through the gas gas heater 12, and is then guided to the primary fan 13 to pass through the primary fan 13. By operation, it is recirculated from the branch exhaust gas recirculation line 8R' via the preheater 3 as a carrier gas for the pulverized coal of the mill 2. A part of the exhaust gas discharged from the boiler 1 is sent from the exhaust gas line 8 on the outlet side of the induced draft fan 7 to the CO 2 concentrating unit via the extraction line 8D, and the CO 2 separation and recovery work from the exhaust gas is performed. Done.

一方、前記酸素燃焼ボイラ設備の空気燃焼運転時には、図５に示す如く、前記脱水装置１１及びガスガスヒータ１２は使用されず、前記押込通風機９及び一次通風機１３の入側から空気が導入され、該空気が前記ボイラ１の燃焼用ガス及び微粉炭の搬送用ガスとして使用される。前記燃焼用ガスとして使用される空気は、前記予熱器４で予熱された後、酸素製造装置１０から酸素が供給されずに、そのままボイラ１へ導入される。前記ボイラ１から排出される排ガスは、前記誘引通風機７の出側の排ガスライン８から抜出ライン８Ｄを経てＣＯ２濃縮ユニットではなく、煙突へ送出され、大気放出される。 On the other hand, during the air combustion operation of the oxyfuel boiler equipment, as shown in FIG. 5, the dehydrator 11 and the gas gas heater 12 are not used, and air is introduced from the inlet side of the forced draft fan 9 and the primary draft fan 13. The air is used as a combustion gas for the boiler 1 and a carrier gas for pulverized coal. The air used as the combustion gas is preheated by the preheater 4 and then introduced into the boiler 1 without being supplied with oxygen from the oxygen production device 10. The exhaust gas discharged from the boiler 1 is sent from the exhaust gas line 8 on the outlet side of the induced draft fan 7 to the chimney, not to the CO 2 concentrating unit, through the extraction line 8D, and is discharged to the atmosphere.

本実施例のように、前記排ガスを前記押込通風機９と並列に設けられる一次通風機１３の作動により前記搬送用ガスとして再循環させる分岐排ガス再循環ライン８Ｒ´を備え、前記脱水装置１１を、前記一次通風機１３の入側の分岐排ガス再循環ライン８Ｒ´に設けると、一次通風機１３が単独で搬送用ガスの圧送を担い、押込通風機９が単独で燃焼用ガスの圧送を担う形となる。このことから、押込通風機９の下流側において、搬送用ガスと燃焼用ガスの圧力損失バランスが、空気燃焼運転時と酸素燃焼運転時で変わってしまうようなことがなくなる。これにより、押込通風機９を容量の大きいものにしなくて済むと共に、酸素燃焼運転時に再循環させる排ガスが燃焼用ガスの流通系統にばかり流れることを防止すべく、前記脱水装置１１と同等の流通抵抗を付与するためのダンパ１５（図７の仮想線参照）等の追加機器を燃焼用ガスの流通系統に設けることが不要となる。この結果、酸素燃焼ボイラ設備の運用が制限されることもなくなる。 As in the present embodiment, a branched exhaust gas recirculation line 8R' for recirculating the exhaust gas as the carrier gas by the operation of the primary fan 13 provided in parallel with the forced draft fan 9 is provided, and the dehydrator 11 is provided. When provided in the branch exhaust gas recirculation line 8R' on the inlet side of the primary air blower 13, the primary air blower 13 is solely responsible for pumping the conveying gas, and the forced draft fan 9 is solely responsible for pumping the combustion gas. Be in shape. Therefore, the pressure loss balance between the carrier gas and the combustion gas does not change between the air combustion operation and the oxyfuel operation on the downstream side of the forced draft fan 9. As a result, the forced draft fan 9 does not have to have a large capacity, and the exhaust gas to be recirculated during the oxyfuel combustion operation is prevented from flowing only to the distribution system of the combustion gas. It is not necessary to provide an additional device such as a damper 15 (see the phantom line in FIG. 7) for giving resistance to the combustion gas distribution system. As a result, the operation of the oxyfuel boiler equipment is not restricted.

更に、前記一次通風機１３の入側の分岐排ガス再循環ライン８Ｒ´に、前記脱水装置１１の入側の排ガスによって前記脱水装置１１の出側の排ガスを加熱する加熱器としてのガスガスヒータ１２を設置することで、熱損失が最小限に抑えられると同時に、脱水装置１１をコンパクトにし、一次通風機１３に流入するガスの乾き度を確保することが可能となる。 Further, a gas gas heater 12 as a heater for heating the exhaust gas on the outlet side of the dehydrator 11 by the exhaust gas on the inlet side of the dehydrator 11 is provided in the branch exhaust gas recirculation line 8R' on the inlet side of the primary fan 13. With the installation, heat loss can be minimized, and at the same time, the dehydrator 11 can be made compact and the dryness of the gas flowing into the primary fan 13 can be secured.

こうして、前記押込通風機９と並列に設けられる一次通風機１３を備えた酸素燃焼ボイラ設備の実施例においても、参考例と同様、押込通風機９の大容量化を阻止して、流通抵抗を付与するための追加機器を不要とし得る。 Thus, also in the embodiment of the oxyfuel boiler equipment provided with the primary fan 13 provided in parallel with the forced draft fan 9, as in the reference example , the large capacity of the forced draft fan 9 is prevented and the flow resistance is reduced. No additional equipment to apply may be needed.

図６は本発明の酸素燃焼ボイラ設備の実施例の変形例であって、図中、図４及び図５と同一の符号を付した部分は同一物を表わしており、基本的な構成は図４及び図５に示す実施例と同様である。本変形例の特徴とするところは、図６に示す如く、前記酸素製造装置１０からの酸素を、再循環される排ガスに対し前記押込通風機９の入側（前記抜出ライン８Ｄの分岐点より下流側）で混合するよう構成した点にある。 FIG. 6 is a modified example of the embodiment of the oxyfuel boiler equipment of the present invention, in which the parts denoted by the same reference numerals as those in FIGS. 4 and 5 represent the same things, and the basic configuration is as shown in FIG. 4 and the embodiment shown in FIG. The feature of this modification is that, as shown in FIG. 6, the oxygen from the oxygen production device 10 is fed to the inlet side of the forced draft fan 9 (the branch point of the outlet line 8D with respect to the exhaust gas to be recirculated. It is configured to mix at the downstream side).

図６に示す変形例のように、前記酸素製造装置１０からの酸素を、再循環される排ガスに対し前記押込通風機９の入側で混合するよう構成すると、前記酸素と排ガスが押込通風機９で撹拌されるため、特別な混合器等を設置しなくても前記酸素と排ガスの混合が促進され、均一なガス分布となる。 When the oxygen from the oxygen producing apparatus 10 is mixed with the exhaust gas to be recirculated at the inlet side of the forced draft fan 9 as in the modified example shown in FIG. 6, the oxygen and the exhaust gas are forced draft fan. Since it is agitated at 9, mixing of the oxygen and the exhaust gas is promoted without installing a special mixer or the like, and a uniform gas distribution is achieved.

前記押込通風機９で混合された酸素と排ガスは、予熱器４にて予熱され昇温される。これは、予熱器４で予熱された排ガスに対して常温の酸素を注入するのに比べ、再循環される排ガスの温度がボイラ１に至るまでに低下しないことを意味する。即ち、前記予熱器４で予熱された酸素と排ガスの混合ガスは、そのままの温度でボイラ１に供給されるため、燃焼性の向上も期待できる。 The oxygen and the exhaust gas mixed by the forced draft fan 9 are preheated by the preheater 4 to be heated. This means that the temperature of the recirculated exhaust gas does not drop by the time it reaches the boiler 1, as compared with injecting room temperature oxygen into the exhaust gas preheated by the preheater 4. That is, since the mixed gas of oxygen and exhaust gas that has been preheated by the preheater 4 is supplied to the boiler 1 at the same temperature, improvement of combustibility can be expected.

又、前記押込通風機９の入側への酸素の混合により、前記予熱器４の高温側（排ガス側）と低温側（再循環される排ガス側）の流量バランスが改善され、予熱器４のガス側温度効率が上がり、予熱器４の出口ガス温度が下げられ、ひいてはその下流側に設置される排ガスクーラ５を小さくできる。 Further, by mixing oxygen into the inlet side of the forced draft fan 9, the flow rate balance between the high temperature side (exhaust gas side) and the low temperature side (recirculated exhaust gas side) of the preheater 4 is improved, and the preheater 4 The gas side temperature efficiency is increased, the outlet gas temperature of the preheater 4 is lowered, and the exhaust gas cooler 5 installed on the downstream side can be reduced in size.

更に又、前記押込通風機９の入側への酸素の混合により、前記押込通風機９の入口ガス温度に関し、空気燃焼運転時と酸素燃焼運転時の温度差が小さくなるため、空気燃焼運転と酸素燃焼運転の切替時間も短縮できる。 Furthermore, the mixing of oxygen into the inlet side of the forced draft fan 9 reduces the temperature difference between the air combustion operation and the oxyfuel combustion operation with respect to the inlet gas temperature of the forced draft fan 9. The switching time of oxyfuel combustion operation can also be shortened.

尚、本発明の酸素燃焼ボイラ設備は、上述の実施例にのみ限定されるものではなく、本発明の要旨を逸脱しない範囲内において種々変更を加え得ることは勿論である。 The oxyfuel boiler equipment of the present invention is not limited to the above-mentioned embodiments, and it goes without saying that various modifications can be made without departing from the scope of the present invention.

１ ボイラ
２ ミル
３ 予熱器
４ 予熱器
８Ｒ 排ガス再循環ライン
８Ｒ´ 分岐排ガス再循環ライン
９ 押込通風機
９´ 補助通風機
１０ 酸素製造装置
１１ 脱水装置
１２ ガスガスヒータ（加熱器）
１３ 一次通風機
１４ 空気取入口 1 Boiler 2 Mill 3 Preheater 4 Preheater 8R Exhaust gas recirculation line 8R' Branch exhaust gas recirculation line 9 Pushing fan 9'Auxiliary fan 10 Oxygen production device 11 Dehydrator 12 Gas gas heater (heater)
13 primary fan 14 air intake

Claims (2)

ボイラから排出される排ガスを燃料の燃焼用ガスとして再循環させる排ガス再循環ラインに押込通風機が設けられた酸素燃焼ボイラ設備であって、
前記排ガスを前記押込通風機と並列に設けられる一次通風機の作動により燃料の搬送用ガスとして再循環させる分岐排ガス再循環ラインを備え、
脱水装置は、前記一次通風機の入側の分岐排ガス再循環ラインに設けられ、
前記一次通風機の入側の分岐排ガス再循環ラインに、前記脱水装置の入側の排ガスによって前記脱水装置の出側の排ガスを加熱する加熱器が設けられる酸素燃焼ボイラ設備。 An oxyfuel boiler facility in which a forced draft fan is provided in an exhaust gas recirculation line for recirculating exhaust gas discharged from a boiler as a combustion gas for fuel,
A branch exhaust gas recirculation line for recirculating the exhaust gas as a gas for carrying fuel by the operation of a primary fan provided in parallel with the forced draft fan;
The dehydrator is provided in the branch exhaust gas recirculation line on the inlet side of the primary fan,
An oxyfuel boiler facility in which a heater for heating the exhaust gas on the outlet side of the dehydrator by the exhaust gas on the inlet side of the dehydrator is provided in the branched exhaust gas recirculation line on the inlet side of the primary fan. 前記排ガス再循環ラインにより再循環される燃焼用ガスに酸素を供給する酸素製造装置を備え、該酸素製造装置からの酸素を、再循環される排ガスに対し前記押込通風機の入側で混合するよう構成した請求項１記載の酸素燃焼ボイラ設備。 An exhaust gas recirculation line is provided with an oxygen production device for supplying oxygen to the combustion gas, and oxygen from the oxygen production device is mixed with the recirculated exhaust gas at the inlet side of the forced draft fan. The oxyfuel boiler equipment according to claim 1, configured as described above.
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