JP2015031214A - Co2 recovery type closed cycle gasification power generation system - Google Patents
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本発明はＣＯ２回収型クローズドサイクルガス化発電システムに関し、特にガス化設備で生成するガス化ガスを燃料としてタービンを駆動するクローズドサイクルの複合発電システムに適用して有用なものである。 The present invention relates to a CO 2 recovery type closed cycle gasification power generation system, and is particularly useful when applied to a closed cycle combined power generation system in which a turbine is driven using gasification gas generated in a gasification facility as fuel.
ガスタービンの燃料として化石燃料を用いると、地球温暖化の原因となるＣＯ２を発生する。このため、ＣＯ２を分離回収しながら高効率発電を行うＣＯ２回収型クローズドサイクル石炭ガス化発電システムが提案されている（非特許文献１参照）。図７は提案されている従来技術に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、当該ＣＯ２回収型クローズドサイクル石炭ガス化発電システムVII（以下、システムVIIともいう）は、燃料である石炭と、酸素製造設備２で生成された酸素が供給されて石炭ガスを生成する石炭ガス化設備１と、石炭ガス化設備１で生成され、金属フィルタ３および乾式脱硫器４で浄化された石炭ガスを燃料として燃焼ガスを生成する燃焼器５と、前記燃焼ガスで駆動されて発電機７を駆動するガスタービン６を有する。さらに、当該システムVIIの圧縮機８は、ガスタービン６で仕事をした排ガスの一部を圧縮するとともに圧縮した排ガスを酸素製造設備２で生成された酸素の一部と混合するとともに、排ガスの熱を利用する再生熱交換器９で加熱して燃焼器５に戻すように構成してある。かくして燃焼器５では、酸素製造設備２で生成された酸素の一部と圧縮機８で圧縮された排ガスとの混合ガスにより燃料である石炭ガスが燃焼される。このことにより当該システムVIIの効率を向上させている。 When fossil fuel is used as the fuel for the gas turbine, CO 2 that causes global warming is generated. Therefore, CO 2 recovering closed cycle coal gasification power generation system for a high-efficiency power generation while separating and recovering the CO 2 has been proposed (see Non-Patent Document 1). FIG. 7 is a block diagram showing a proposed CO 2 recovery type closed cycle coal gasification power generation system according to the prior art. As shown in the figure, the CO 2 recovery type closed cycle coal gasification power generation system VII (hereinafter also referred to as the system VII) is supplied with coal as fuel and oxygen generated in the oxygen production facility 2. A coal gasification facility 1 that generates gas, a combustor 5 that generates combustion gas using coal gas generated by the coal gasification facility 1 and purified by the metal filter 3 and the dry desulfurizer 4, and the combustion gas And a gas turbine 6 that drives the generator 7. Further, the compressor 8 of the system VII compresses a part of the exhaust gas worked in the gas turbine 6 and mixes the compressed exhaust gas with a part of the oxygen generated in the oxygen production facility 2 and heats the exhaust gas. The regenerative heat exchanger 9 utilizing the heat is returned to the combustor 5 by heating. Thus, in the combustor 5, coal gas, which is fuel, is combusted by a mixed gas of a part of oxygen generated in the oxygen production facility 2 and the exhaust gas compressed by the compressor 8. This improves the efficiency of the system VII.
また、当該システムVIIでは、ガスタービン６の排ガス中のハロゲンを、汽水分離器１０の水洗塔で除去し、かかる排ガスを、さらに圧縮機１１で圧縮した後、水銀除去部１２で水銀を除去し、汽水分離器１３で水分を分離して圧縮機１４に供給する。圧縮機１４では、圧縮した排ガスの一部を圧縮機１５を介してＣＯ２回収装置１６に供給するとともに、残りの一部を石炭ガス化設備１に戻している。このことにより石炭ガス化設備１内における石炭ガスのガス化効率を向上させ、より多くのＣＯを発生させている。 Further, in the system VII, the halogen in the exhaust gas of the gas turbine 6 is removed by the water washing tower of the brackish water separator 10, and after the exhaust gas is further compressed by the compressor 11, mercury is removed by the mercury removing unit 12. The water is separated by the brackish water separator 13 and supplied to the compressor 14. In the compressor 14, a part of the compressed exhaust gas is supplied to the CO 2 recovery device 16 through the compressor 15, and the remaining part is returned to the coal gasification facility 1. Thereby, the gasification efficiency of coal gas in the coal gasification facility 1 is improved, and more CO is generated.
当該システムVIIは、ガスタービン６で仕事をした排ガスの熱を利用して蒸気タービン１７を駆動し、蒸気タービン１７が発電機１８を駆動する。すなわち、当該システムVIIは、複合発電システムとして構築してあり、このためガスタービン６の下流側には、ガスタービン６の排ガスの熱を回収する排熱回収ボイラ１９および熱交換器２０が配設されている。かくして蒸気タービン１７で仕事をした蒸気が、復水器２１で凝縮されて水となり、その復水ポンプにより熱交換器２０を介して排熱回収ボイラ１９に供給され、蒸気となって蒸気タービン１７に供給される。 In the system VII, the steam turbine 17 is driven using the heat of the exhaust gas worked in the gas turbine 6, and the steam turbine 17 drives the generator 18. That is, the system VII is constructed as a combined power generation system. Therefore, on the downstream side of the gas turbine 6, an exhaust heat recovery boiler 19 and a heat exchanger 20 that recover the heat of the exhaust gas of the gas turbine 6 are arranged. Has been. Thus, the steam that has worked in the steam turbine 17 is condensed in the condenser 21 to become water, and is supplied to the exhaust heat recovery boiler 19 through the heat exchanger 20 by the condensate pump, and becomes steam to become the steam turbine 17. To be supplied.
上述の如きＣＯ２回収型クローズドサイクル石炭ガス化発電システムVIIは、ＣＯ２を回収することに伴う所要エネルギーや動力を低減して発電効率を向上させることを目的とするものであるが、燃焼器５において石炭ガス化ガスと酸素の比が当量付近で燃焼させると、ガスタービン６から排出される排ガス中にＣＯおよびＯ２が残留しやすくなり、それらが残留すると、熱効率の低下やＣＯ２回収率の低下を招くおそれがある。ＣＯが完全にＣＯ２に転化されない場合には、転化されないＣＯに起因する熱量を得ることができず、また残留Ｏ２が増えると、残留しているＯ２を循環させるための無駄な動力が増え、回収したＣＯ２の純度も低下するからである。また、燃焼器５や排熱回収ボイラ１９等のガス流路内で温度、濃度、流速等の分布があると、反応が進む領域とそうでない領域とができてしまいＣＯおよびＯ２の残留の可能性が高まる。さらに、安定燃焼を行うために、希釈ガスを部分的に減らして燃焼器５内に局所的な高温燃焼域を作ると、さらに残存するＣＯ、Ｏ２が増加する可能性を生じる。図８は、表１の条件における化学平衡計算を行った結果を示す特性図であるが、同図を参照すれば明らかな通り、ＣＯやＯ２の平衡組成が１６００℃以上の高温燃焼域では急激に増加するからである。 The CO 2 recovery type closed cycle coal gasification power generation system VII as described above is intended to reduce the required energy and power associated with CO 2 recovery and improve the power generation efficiency. 5, when the ratio of coal gasification gas and oxygen is burned in the vicinity of an equivalent amount, CO and O 2 tend to remain in the exhaust gas discharged from the gas turbine 6, and if these remain, thermal efficiency decreases and CO 2 recovery occurs. There is a risk that the rate will decrease. If the CO is not completely converted to CO 2 can not obtain a heat due to not converted CO, also the residual O 2 is increased, useless power for circulating the O 2 remaining This is because it increases and the purity of the recovered CO 2 also decreases. In addition, if there is a distribution of temperature, concentration, flow velocity, etc. in the gas flow path of the combustor 5 or the exhaust heat recovery boiler 19, etc., there will be a region where the reaction proceeds and a region where the reaction does not occur, and CO and O 2 remaining The possibility increases. Further, if the dilution gas is partially reduced to create a local high-temperature combustion region in the combustor 5 in order to perform stable combustion, there is a possibility that the remaining CO and O 2 further increase. FIG. 8 is a characteristic diagram showing the results of the chemical equilibrium calculation under the conditions in Table 1. As is clear from this figure, in the high-temperature combustion region where the equilibrium composition of CO and O 2 is 1600 ° C. or higher. This is because it increases rapidly.
さらに、上述の如きＣＯ２回収型クローズドサイクル石炭ガス化発電システムにおいて、石炭や石油コークス等、含窒素化合物を含む炭化水素系の燃料をガス化燃料に用いると、ＮＨ３が発生する。ＮＨ３は燃焼器５でＮＯＸに転化し、汽水分離器１０、１３で一部が分離されて硝酸に転化し、排水として排出する場合には中和処理が必要となる。残りのＮＯＸは回収するＣＯ２に含まれるか、燃焼器５に循環供給される。 Furthermore, in the CO 2 recovery type closed cycle coal gasification power generation system as described above, NH 3 is generated when a hydrocarbon-based fuel containing a nitrogen-containing compound such as coal or petroleum coke is used as the gasification fuel. NH 3 is converted to NO X by the combustor 5, partly separated by the brackish water separators 10 and 13, converted to nitric acid, and discharged as waste water, neutralization is required. The remaining NO X is included in the CO 2 to be recovered or is circulated and supplied to the combustor 5.
本発明は、上記従来技術に鑑み、ＣＯの残存および残存Ｏ２の増加を確実に防止し、熱効率およびＣＯ２回収率の向上を図るとともに、さらに環境負荷の原因となるＮＯＸを乾式で除去して排水処理を軽減することができるＣＯ２回収型クローズドサイクルガス化発電システムを提供することを目的とする。 In view of the above prior art, the present invention reliably prevents the increase of residual CO and residual O 2 , improves the thermal efficiency and CO 2 recovery rate, and further removes NO X that causes environmental burdens in a dry manner. An object of the present invention is to provide a CO 2 recovery type closed cycle gasification power generation system capable of reducing wastewater treatment.
上記目的を達成する本発明の第１の態様は、
石炭や重質油を含む炭化水素系の燃料と、酸素製造設備で生成された酸素とが供給されてガス化ガスを生成するガス化設備と、前記ガス化ガスを燃料として燃焼ガスを生成する燃焼器と、前記燃焼ガスで駆動されて発電機を駆動するガスタービンと、該ガスタービンの排ガスの一部を圧縮するとともに圧縮した排ガスを前記酸素製造設備で生成された酸素の一部と混合して前記燃焼器に戻す圧縮機と、前記ガスタービンの排ガスを圧縮して前記排ガスの一部を二酸化炭素回収装置に供給するとともに、残りの前記排ガスを前記ガス化設備に戻す他の圧縮機とを有するＣＯ２回収型クローズドサイクルガス化発電システムにおいて、
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に触媒燃焼装置を配設したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システムにある。
The first aspect of the present invention for achieving the above object is as follows:
Hydrocarbon fuel including coal and heavy oil and oxygen generated in oxygen production facility are supplied to generate gasification gas, and combustion gas is generated using the gasification gas as fuel. A combustor, a gas turbine driven by the combustion gas to drive a generator, and compressing a portion of the exhaust gas of the gas turbine and mixing the compressed exhaust gas with a portion of oxygen produced by the oxygen production facility And a compressor that compresses the exhaust gas from the gas turbine and supplies a part of the exhaust gas to the carbon dioxide recovery device, and returns the remaining exhaust gas to the gasification facility. In a CO 2 recovery type closed cycle gasification power generation system having
In the CO 2 recovery type closed cycle gasification power generation system, a catalytic combustion apparatus is disposed upstream of the compressor and other compressors and downstream of the gas turbine.
本発明の第２の態様は、
第１の態様に記載するＣＯ２回収型クローズドサイクルガス化発電システムにおいて、
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に配設された排熱回収ボイラに触媒燃焼装置を一体的に組み込んだことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システムにある。
The second aspect of the present invention is:
In the CO 2 recovery type closed cycle gasification power generation system described in the first aspect,
A CO 2 recovery type closed cycle gas in which a catalytic combustion apparatus is integrally incorporated in an exhaust heat recovery boiler disposed upstream of the compressor and other compressors and downstream of the gas turbine. In the power generation system.
本発明の第３の態様は、
石炭や重質油を含む炭化水素系の燃料と、酸素製造設備で生成された酸素とが供給されてガス化ガスを生成するガス化設備と、前記ガス化ガスを燃料として燃焼ガスを生成する燃焼器と、前記燃焼ガスで駆動されて発電機を駆動するガスタービンと、該ガスタービンの排ガスの一部を圧縮するとともに圧縮した排ガスを前記酸素製造設備で生成された酸素の一部と混合して前記燃焼器に戻す圧縮機と、前記ガスタービンの排ガスを圧縮して前記排ガスの一部を二酸化炭素回収装置に供給するとともに、残りの前記排ガスを前記ガス化設備に戻す他の圧縮機とを有するＣＯ２回収型クローズドサイクルガス化発電システムにおいて、
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に再熱器を配設するとともに、
前記再熱器は、上流側から順次配設された脱硝触媒および燃焼触媒を有するとともに、前記脱硝触媒には、前記ガスタービンからの排ガスとともに、前記ガス化設備からのガス化ガスを供給するように構成したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システムにある。
The third aspect of the present invention is:
Hydrocarbon fuel including coal and heavy oil and oxygen generated in oxygen production facility are supplied to generate gasification gas, and combustion gas is generated using the gasification gas as fuel. A combustor, a gas turbine driven by the combustion gas to drive a generator, and compressing a portion of the exhaust gas of the gas turbine and mixing the compressed exhaust gas with a portion of oxygen produced by the oxygen production facility And a compressor that compresses the exhaust gas from the gas turbine and supplies a part of the exhaust gas to the carbon dioxide recovery device, and returns the remaining exhaust gas to the gasification facility. In a CO 2 recovery type closed cycle gasification power generation system having
A reheater is disposed upstream of the compressor and other compressors and downstream of the gas turbine;
The reheater has a denitration catalyst and a combustion catalyst sequentially arranged from the upstream side, and supplies the gasification gas from the gasification facility together with the exhaust gas from the gas turbine to the denitration catalyst. The CO 2 recovery type closed cycle gasification power generation system is characterized in that it is configured as described above.
本発明の第４の態様は、
第３の態様に記載するＣＯ２回収型クローズドサイクルガス化発電システムにおいて、
前記圧縮機および他の圧縮機の上流側で前記再熱器の下流側に、さらに前記再熱器の排ガスで駆動される再熱ガスタービンを配設したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システムにある。
The fourth aspect of the present invention is:
In the CO 2 recovery type closed cycle gasification power generation system described in the third aspect,
A CO 2 recovery type closed system characterized in that a reheat gas turbine driven by exhaust gas from the reheater is further arranged upstream of the compressor and other compressors and downstream of the reheater. It is in the cycle gasification power generation system.
本発明の第５の態様は、
第３または第４の態様に記載するＣＯ２回収型クローズドサイクルガス化発電システムにおいて、
前記再熱器は、前記燃焼触媒の下流側に空間部を設けたものであることを特徴とするＣＯ２回収型クローズドサイクルガス化発電システムにある。
According to a fifth aspect of the present invention,
In the CO 2 recovery type closed cycle gasification power generation system described in the third or fourth aspect,
The reheater is a CO 2 recovery type closed cycle gasification power generation system characterized in that a space is provided on the downstream side of the combustion catalyst.
本発明によれば、ＣＯ２回収型クローズドサイクルガス化発電システムにおいて、ガスタービンの下流側に触媒燃焼装置または再熱器を配置したので、ガスタービンから排出される未反応のＣＯとＯ２を反応させてＣＯ２に転換することができる。この結果、ＣＯ２に転換時の熱を適切に利用して熱効率の向上を図るとともに、ＣＯ２回収率の向上も図ることができる。 According to the present invention, in the CO 2 recovery type closed cycle gasification power generation system, since the catalytic combustion device or the reheater is disposed downstream of the gas turbine, unreacted CO and O 2 discharged from the gas turbine are removed. It can be converted to CO 2 by reaction. As a result, the heat at the time of conversion to CO 2 can be appropriately used to improve the thermal efficiency, and the CO 2 recovery rate can be improved.
また、脱硝触媒と燃焼触媒とを有する再熱器を備えた場合には、ガス化燃料の一部を再熱器に供給することにより、燃焼器に供給するガス化燃料を減らし、Ｏ２が十分存在する状態で燃焼することができ、燃焼器から排出される未反応のＣＯを低減することができる。さらに、燃焼器から排出されるＮＯＸと、再熱器に供給される燃料中のＮＨ３とを脱硝触媒で反応させてＮ２に転換し、ＮＯＸとＮＨ３とを除去することができ、燃焼触媒で、燃焼器から排出される未反応のＣＯとＯ２、および再熱器に供給される燃料とを反応させて、ＣＯとＨ２をＣＯ２とＨ２Ｏに転換することができる。この結果、ＣＯ２に転換時の熱を適切に利用した熱効率の向上およびＣＯ２回収率の向上を図ることができるだけでなく、ＮＯＸを乾式で適切に除去することもできる。 In addition, when a reheater having a denitration catalyst and a combustion catalyst is provided, the gasification fuel supplied to the combustor is reduced by supplying a part of the gasification fuel to the reheater, and O 2 is reduced. Combustion can be performed in a sufficiently existing state, and unreacted CO discharged from the combustor can be reduced. Further, NO X discharged from the combustor and NH 3 in the fuel supplied to the reheater can be reacted with a denitration catalyst to be converted to N 2 , thereby removing NO X and NH 3. And reacting unreacted CO and O 2 discharged from the combustor and fuel supplied to the reheater with a combustion catalyst to convert CO and H 2 into CO 2 and H 2 O. it can. As a result, not only can improve the improvement and CO 2 recovery of heat efficiency by appropriately utilizing the conversion time of heat CO 2, it can be properly removed NO X dry.
以下、本発明の実施の形態を図面に基づき詳細に説明する。 Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.
＜第１の実施の形態＞
図１は本発明の第１の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムＩ（以下、システムＩともいう）の、基本的な構成は、図７に示すＣＯ２回収型クローズドサイクル石炭ガス化発電システムVIIと同様であり、これに触媒燃焼装置３１を追加、配設したものである。
<First Embodiment>
FIG. 1 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a first embodiment of the present invention. As shown in the figure, the basic configuration of the CO 2 recovery type closed cycle coal gasification power generation system I (hereinafter also referred to as system I) according to this embodiment is the CO 2 recovery type closed cycle coal shown in FIG. Similar to the gasification power generation system VII, a catalytic combustion device 31 is additionally provided.
すなわち、本形態に係るシステムＩは、燃料である石炭と、酸素製造設備２で生成された酸素が供給されて石炭ガスを生成する石炭ガス化設備１と、石炭ガス化設備１で生成され、金属フィルタ３および乾式脱硫器４で浄化された石炭ガスを燃料として燃焼ガスを生成する燃焼器５と、前記燃焼ガスで駆動されて発電機７を駆動するガスタービン６を有する。 That is, the system I according to the present embodiment is generated by coal as fuel, coal gasification facility 1 that is supplied with oxygen generated in the oxygen production facility 2 and generates coal gas, and the coal gasification facility 1. It has a combustor 5 that generates combustion gas using coal gas purified by the metal filter 3 and the dry desulfurizer 4 as fuel, and a gas turbine 6 that is driven by the combustion gas and drives a generator 7.
ガスタービン６の下流側には、排熱回収ボイラ１９および圧縮機８の上流側に、触媒燃焼装置３１が配設してある。ここで、燃焼触媒としては、既知の触媒（アクチノイドを除く遷移元素のうち少なくとも１種の元素（原子番号２１〜２９、３９〜４７、５７〜７９）を含む触媒）の適用が可能である。また、触媒燃焼装置３１の入口温度は、触媒燃焼が促進され、かつ排熱回収ボイラ１９の効率が向上する５００〜８００℃が好ましい。 A catalytic combustion device 31 is disposed downstream of the gas turbine 6 and upstream of the exhaust heat recovery boiler 19 and the compressor 8. Here, as the combustion catalyst, a known catalyst (a catalyst including at least one element (atomic numbers 21 to 29, 39 to 47, 57 to 79) among transition elements excluding actinides) can be applied. Further, the inlet temperature of the catalytic combustion device 31 is preferably 500 to 800 ° C. in which catalytic combustion is promoted and the efficiency of the exhaust heat recovery boiler 19 is improved.
本形態の圧縮機８は、ガスタービン６で仕事をし、触媒燃焼装置３１で所定の燃焼が行われ、排熱回収ボイラ１９で排熱を回収された後の排ガスの一部を圧縮するとともに圧縮した排ガスを酸素製造設備２で生成された酸素の一部と混合するとともに、排ガスの熱を利用する再生熱交換器９で加熱して燃焼器５に戻す。かくして燃焼器５では、酸素製造設備２で生成された酸素の一部と圧縮機８で圧縮された排ガスとの混合ガスにより燃料である石炭ガスが燃焼される。このことにより当該システムＩの効率を向上させている。 The compressor 8 of the present embodiment works with the gas turbine 6, compresses a part of the exhaust gas after the exhaust heat is recovered by the exhaust heat recovery boiler 19 after predetermined combustion is performed by the catalytic combustion device 31. The compressed exhaust gas is mixed with a part of the oxygen generated in the oxygen production facility 2, and is heated by the regenerative heat exchanger 9 using the heat of the exhaust gas and returned to the combustor 5. Thus, in the combustor 5, coal gas, which is fuel, is combusted by a mixed gas of a part of oxygen generated in the oxygen production facility 2 and the exhaust gas compressed by the compressor 8. This improves the efficiency of the system I.
また、当該システムＩでは、ガスタービン６の排ガス中のハロゲンを、汽水分離器１０の水洗塔で除去し、かかる排ガスを、さらに圧縮機１１で圧縮した後、水銀除去部１２で水銀を除去し、汽水分離器１３で水分を分離して圧縮機１４に供給する。圧縮機１４では、圧縮した排ガスの一部を圧縮機１５を介してＣＯ２回収装置１６に供給するとともに、残りの一部を石炭ガス化設備１に戻している。このことにより石炭ガス化設備１内における石炭ガスのガス化効率を向上させ、より多くのＣＯを発生させている。 In the system I, the halogen in the exhaust gas of the gas turbine 6 is removed by the water washing tower of the brackish water separator 10, and the exhaust gas is further compressed by the compressor 11, and then the mercury is removed by the mercury removing unit 12. The water is separated by the brackish water separator 13 and supplied to the compressor 14. In the compressor 14, a part of the compressed exhaust gas is supplied to the CO 2 recovery device 16 through the compressor 15, and the remaining part is returned to the coal gasification facility 1. Thereby, the gasification efficiency of coal gas in the coal gasification facility 1 is improved, and more CO is generated.
当該システムＩは、ガスタービン６で仕事をした排ガスの熱を利用して蒸気タービン１７を駆動し、蒸気タービン１７が発電機１８を駆動する。すなわち、当該システムＩは、複合発電システムとして構築してあり、このためガスタービン６の下流側には、ガスタービン６の排ガスの熱を回収する排熱回収ボイラ１９および熱交換器２０が配設されている。かくして蒸気タービン１７で仕事をした蒸気が、復水器２１で凝縮されて水となり、その復水ポンプにより熱交換器２０を介して排熱回収ボイラ１９に供給され、蒸気となって蒸気タービン１７に供給される。 In the system I, the steam turbine 17 is driven using the heat of the exhaust gas worked by the gas turbine 6, and the steam turbine 17 drives the generator 18. That is, the system I is constructed as a combined power generation system. Therefore, on the downstream side of the gas turbine 6, an exhaust heat recovery boiler 19 and a heat exchanger 20 that recover the heat of the exhaust gas of the gas turbine 6 are arranged. Has been. Thus, the steam that has worked in the steam turbine 17 is condensed in the condenser 21 to become water, and is supplied to the exhaust heat recovery boiler 19 through the heat exchanger 20 by the condensate pump, and becomes steam to become the steam turbine 17. To be supplied.
かかる本形態においては、触媒燃焼装置３１においては、ガスタービン６から排出される排ガス中の未燃のＣＯとＯ２とが反応し、ＣＯ２に転換される。すなわち、ガスタービン６から排出される排ガス中に未燃のＣＯおよび未反応のＯ２が残留している場合の熱効率の低下やＣＯ２回収率の低下という不都合を可及的に低減することができる。また、ガスタービン６の下流側で、未燃のＣＯとＯ２を反応させることができるので、圧縮機８で圧縮した排ガスと混合されて燃焼器５に供給されるＯ２の量も可及的に低減し得る。このときの触媒燃焼装置３１における反応式は、ＣＯ＋（1/2）Ｏ２→ＣＯ２ である。 In this embodiment, in the catalytic combustion device 31, unburned CO and O 2 in the exhaust gas discharged from the gas turbine 6 react and are converted to CO 2 . That is, it is possible to reduce as much as possible the inconvenience of lowering the thermal efficiency and lowering the CO 2 recovery rate when unburned CO and unreacted O 2 remain in the exhaust gas discharged from the gas turbine 6. it can. Further, since unburned CO and O 2 can be reacted on the downstream side of the gas turbine 6, the amount of O 2 mixed with the exhaust gas compressed by the compressor 8 and supplied to the combustor 5 is also possible. Can be reduced. The reaction formula in the catalytic combustion device 31 at this time is CO + (1/2) O 2 → CO 2 .
なお、本形態に係るシステムＩは、石炭ガス化設備１で生成した石炭ガス化ガスを燃焼器５の燃料にする場合であるが、これに限るものではない。他に重質油やバイオマス等、炭化水素系の燃料をガス化したガス化ガスであれば、同様の燃料として利用することができる。また、本形態に係るシステムＩは、複合発電システムとして構築した場合であるが、これに限るものではない。ガスタービン６の排ガスの熱エネルギーの利用態様は任意である。燃料の限定および発電設備の形態は、以下に述べる第２〜第６の実施の形態でも全く同様である。 In addition, although the system I which concerns on this form is a case where the coal gasification gas produced | generated with the coal gasification equipment 1 is made into the fuel of the combustor 5, it does not restrict to this. In addition, if it is gasification gas which gasified hydrocarbon fuels, such as heavy oil and biomass, it can utilize as a similar fuel. Further, the system I according to the present embodiment is a case where the system is constructed as a combined power generation system, but is not limited thereto. The utilization mode of the heat energy of the exhaust gas of the gas turbine 6 is arbitrary. The limitation of fuel and the form of power generation equipment are exactly the same in the second to sixth embodiments described below.
＜第２の実施の形態＞
図２は本発明の第２の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムII（以下、システムIIともいう）の、基本的な構成は、図１に示すシステムＩと同様である。そこで、図１と同一部分には同一番号を付し、重複する説明は省略する。
<Second Embodiment>
FIG. 2 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a second embodiment of the present invention. As shown in the figure, the basic configuration of the CO 2 recovery type closed cycle coal gasification power generation system II (hereinafter also referred to as system II) according to the present embodiment is the same as the system I shown in FIG. Therefore, the same parts as those in FIG.
本形態に係るシステムIIでは、ガスタービン６の排ガス中の未燃のＣＯを残存Ｏ２で燃焼させる触媒燃焼装置４１を２分割した排熱回収ボイラ１９Ａ，１９Ｂの間に配設してある。 In the system II according to the present embodiment, a catalytic combustion apparatus 41 that combusts unburned CO in the exhaust gas of the gas turbine 6 with residual O 2 is disposed between the exhaust heat recovery boilers 19A and 19B divided into two.
本形態のシステムIIでもシステムＩと同様に、触媒燃焼装置４１で排ガス中の未燃のＣＯおよび未反応のＯ２を反応させてＣＯ２に転換する。本形態における触媒燃焼装置４１の入口温度は、触媒燃焼が促進される３００〜８００℃が好ましい。 In the system II of this embodiment, as in the system I, unburned CO and unreacted O 2 in the exhaust gas are reacted in the catalytic combustion device 41 and converted to CO 2 . The inlet temperature of the catalytic combustion apparatus 41 in this embodiment is preferably 300 to 800 ° C. at which catalytic combustion is promoted.
＜第３の実施の形態＞
図３は本発明の第３の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムIII（以下、システムIIIともいう）の基本的な構成は、図１に示すシステムＩと同様である。そこで、図１と同一部分には同一番号を付し、重複する説明は省略する。
<Third Embodiment>
FIG. 3 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a third embodiment of the present invention. As shown in the figure, the basic configuration of a CO 2 recovery type closed cycle coal gasification power generation system III (hereinafter also referred to as system III) according to the present embodiment is the same as the system I shown in FIG. Therefore, the same parts as those in FIG.
本形態に係るシステムIIIでは、ガスタービン６の下流側に、再熱器５１および再熱器５１で加熱した排ガスで駆動される再熱ガスタービン５２が直列に配設されている。再熱ガスタービン５２は発電機５３を駆動するように構成してあり、この再熱ガスタービン５２でも熱エネルギーを回収してシステムIII全体での発電効率の向上に寄与させている。 In the system III according to this embodiment, a reheater 51 and a reheat gas turbine 52 driven by exhaust gas heated by the reheater 51 are arranged in series on the downstream side of the gas turbine 6. The reheat gas turbine 52 is configured to drive the generator 53, and the reheat gas turbine 52 also collects thermal energy and contributes to improvement of power generation efficiency in the entire system III.
再熱器５１は、上流側から順次配設された脱硝触媒５１Ａおよび燃焼触媒５１Ｂを有する。ここで、脱硝触媒５１Ａには、ガスタービン６の排ガスとともに、燃焼器５に供給される燃料である石炭ガス化ガスの一部が図示していない流量調整弁を介して分割供給される。なお、図示していないが、排ガスと燃料の石炭ガス化ガスを混合して脱硝触媒５１Ａに供給するために、脱硝触媒５１Ａの上流に空間部または混合器などの混合手段が配設される。 The reheater 51 includes a denitration catalyst 51A and a combustion catalyst 51B that are sequentially arranged from the upstream side. Here, along with the exhaust gas of the gas turbine 6, a part of the coal gasification gas that is the fuel supplied to the combustor 5 is dividedly supplied to the denitration catalyst 51 </ b> A via a flow rate adjustment valve (not shown). Although not shown, mixing means such as a space or a mixer is disposed upstream of the denitration catalyst 51A in order to mix the exhaust gas and the coal gasification gas of the fuel and supply them to the denitration catalyst 51A.
以上の構成により、ガス化燃料の一部を再熱器５１に供給することで、燃焼器５に供給するガス化燃料を減らし、Ｏ２が十分存在する状態で燃焼することができ、燃焼器５から排出される未反応のＣＯを低減することができる。 With the above configuration, by supplying a part of the gasified fuel to the reheater 51, the gasified fuel supplied to the combustor 5 can be reduced, and combustion can be performed in a state where O 2 is sufficiently present. Unreacted CO discharged from 5 can be reduced.
燃焼器５では、燃料の石炭ガス化ガスに含まれるＮＨ３からＮＯＸが生成し、その処理が必要となる。本形態では、再熱器５１を脱硝触媒５１Ａと燃焼触媒５１Ｂで構成するとともに、燃焼触媒５１Ｂの上流側に脱硝触媒５１Ａを配設しているので、燃焼器５から排出され、ガスタービン６の排ガスに含まれるＮＯＸと、再熱器５１に供給される燃料中のＮＨ３とを反応させてＮ２に転換することができる。この結果、ＮＯＸとＮＨ３が除去される。 In the combustor 5, NO X is generated from NH 3 contained in the fuel coal gasification gas, and it is necessary to process it. In this embodiment, the reheater 51 is composed of the denitration catalyst 51A and the combustion catalyst 51B, and the denitration catalyst 51A is disposed upstream of the combustion catalyst 51B. NO X contained in the exhaust gas can be reacted with NH 3 in the fuel supplied to the reheater 51 to be converted into N 2 . As a result, NO X and NH 3 are removed.
一方、燃焼触媒５１Ｂでは、燃焼器５から排出され、ガスタービン６の排ガスに含まれる未反応のＣＯおよびＯ２と再熱器５１に供給される燃料とを反応させて、ＣＯとＨ２をＣＯ２とＨ２Ｏに転換する。 On the other hand, in the combustion catalyst 51B, unreacted CO and O 2 discharged from the combustor 5 and contained in the exhaust gas of the gas turbine 6 react with the fuel supplied to the reheater 51, and CO and H 2 are reacted. Convert to CO 2 and H 2 O.
本形態における脱硝触媒５１Ａ、燃焼触媒５１Ｂとしては、既知の触媒（アクチノイドを除く遷移元素のうち少なくとも１種の元素（原子番号２１〜２９、３９〜４７、５７〜７９）を含む触媒）の適用が可能である。また、再熱器５１の入口温度は脱硝反応および触媒燃焼が促進される反面、ＮＯＸ生成反応が抑制され、しかもガスタービン６の効率が向上する５００〜８００℃が好ましい。一方、再熱器５１の出口温度はＮ２とＨ２Ｏの生成反応が促進される反面、ＮＯＸ生成反応が抑制され、しかもガスタービン６の効率が向上する１５００℃以下が好ましい。
本形態における各部での反応式は次の通りである。
燃焼器５での反応式：ＮＨ３＋(5/4)・Ｏ２→ＮＯ＋(3/2)・Ｈ２Ｏ
脱硝触媒５１Ａでの反応式：ＮＯ＋ＮＨ３＋(1/4)・Ｏ２→Ｎ２＋(3/2)・Ｈ２Ｏ
燃焼触媒５１Ｂでの反応式：ＮＨ３＋(3/4)・Ｏ２→(1/2)・Ｎ２＋(3/2)・Ｈ２Ｏ
Application of a known catalyst (a catalyst containing at least one element (atomic numbers 21 to 29, 39 to 47, 57 to 79) among transition elements excluding actinides) as the denitration catalyst 51A and the combustion catalyst 51B in this embodiment Is possible. The inlet temperature of the reheater 51 is preferably 500 to 800 ° C. in which the denitration reaction and catalytic combustion are promoted, but the NO x generation reaction is suppressed and the efficiency of the gas turbine 6 is improved. On the other hand, the outlet temperature of the reheater 51 is preferably 1500 ° C. or less at which the NO x production reaction is suppressed and the efficiency of the gas turbine 6 is improved while the production reaction of N 2 and H 2 O is promoted.
The reaction formula in each part in this embodiment is as follows.
Reaction formula in the combustor 5: NH 3 + (5/4) · O 2 → NO + (3/2) · H 2 O
Reaction formula in the denitration catalyst 51A: NO + NH 3 + (1/4) · O 2 → N 2 + (3/2) · H 2 O
Reaction formula in the combustion catalyst 51B: NH 3 + (3/4) · O 2 → (1/2) · N 2 + (3/2) · H 2 O
＜第４の実施の形態＞
図４は本発明の第４の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムIV（以下、システムIVともいう）は、図３に示すシステムIIIに対し、再熱器６１の構成が異なる。本形態における再熱器６１は、上流側から順に脱硝触媒６１Ａ、燃焼触媒６１Ｂに続き、空間部６１Ｃが形成されている。その他の構成は、図３に示すシステムIIIと同構成である。そこで、図３に示すシステムIIIと同一部分には同一番号を付し、重複する説明は省略する。
<Fourth embodiment>
FIG. 4 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a fourth embodiment of the present invention. As shown in the figure, the CO 2 recovery type closed cycle coal gasification power generation system IV (hereinafter also referred to as system IV) according to this embodiment is different in the configuration of the reheater 61 from the system III shown in FIG. . In the reheater 61 in this embodiment, a space 61C is formed following the denitration catalyst 61A and the combustion catalyst 61B in order from the upstream side. Other configurations are the same as those of the system III shown in FIG. Therefore, the same parts as those in the system III shown in FIG.
本形態でもシステムIIIと同様の作用・効果を得ることができるが、本形態によれば、さらに、燃焼触媒６１Ｂで、ガスタービン６の排ガスに含まれる未反応のＣＯと、再熱器６１に供給される石炭ガス化ガスの一部を燃焼し、燃焼触媒出口のガス温度を気相燃焼が可能な温度に上昇させ、燃焼触媒出口の空間部６１Ｃで残りの未反応ＣＯおよび石炭ガス化ガスを気相燃焼することができる。かかる気相燃焼を行なわせることにより、空間部出口でＣＯおよび石炭ガス化ガスの完全燃焼を達成させながら、触媒の温度を、例えば１５００℃程度の高温にすることなく、より低温で使用できる。したがって、触媒の劣化を抑制することができる。ちなみに、触媒は高温になるほどシンタリング等の劣化が促進される。 In this embodiment, the same operation and effect as in the system III can be obtained. However, according to this embodiment, the unreacted CO contained in the exhaust gas of the gas turbine 6 and the reheater 61 are further added by the combustion catalyst 61B. A part of the supplied coal gasification gas is combusted, the gas temperature at the combustion catalyst outlet is raised to a temperature at which gas phase combustion is possible, and the remaining unreacted CO and coal gasification gas in the space 61C at the combustion catalyst outlet Can be vapor-phase combusted. By performing such gas phase combustion, the catalyst can be used at a lower temperature without increasing the temperature of the catalyst to, for example, about 1500 ° C. while achieving complete combustion of CO and coal gasification gas at the space portion outlet. Therefore, deterioration of the catalyst can be suppressed. Incidentally, deterioration such as sintering is promoted as the temperature of the catalyst increases.
＜第５の実施の形態＞
図５は本発明の第５の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムV（以下、システムVともいう）は、図３に示すシステムIIIの再熱ガスタービン５２を省略して、再熱器５１の排ガスを直接、排熱回収ボイラ１９に供給するように構成したものである。
<Fifth embodiment>
FIG. 5 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a fifth embodiment of the present invention. As shown in the figure, the CO 2 recovery type closed cycle coal gasification power generation system V (hereinafter also referred to as system V) according to the present embodiment omits the reheat gas turbine 52 of the system III shown in FIG. The exhaust gas from the reheater 51 is directly supplied to the exhaust heat recovery boiler 19.
かかる構成のシステムVでも、若干発電効率は劣るが、システムIIIと同等の作用・効果を発揮させることができる。 Even with the system V having such a configuration, the power generation efficiency is slightly inferior, but the same operation and effect as the system III can be exhibited.
なお、図５中、図３と同一部分には同一番号を付し、重複する説明は省略する。 In FIG. 5, the same parts as those in FIG. 3 are denoted by the same reference numerals, and redundant description is omitted.
＜第６の実施の形態＞
図６は本発明の第６の実施の形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムを示すブロック図である。同図に示すように、本形態に係るＣＯ２回収型クローズドサイクル石炭ガス化発電システムVI（以下、システムVIともいう）は、図４に示すシステムIVの再熱ガスタービン５２を省略して、再熱器６１の排ガスを直接、排熱回収ボイラ１９に供給するように構成したものである。
<Sixth Embodiment>
FIG. 6 is a block diagram showing a CO 2 recovery type closed cycle coal gasification power generation system according to a sixth embodiment of the present invention. As shown in the figure, the CO 2 recovery type closed cycle coal gasification power generation system VI (hereinafter also referred to as system VI) according to the present embodiment omits the reheat gas turbine 52 of the system IV shown in FIG. The exhaust gas from the reheater 61 is directly supplied to the exhaust heat recovery boiler 19.
かかる構成のシステムVIでも、若干発電効率は劣るが、システムIVと同等の作用・効果を発揮させることができる。 Even with the system VI having such a configuration, the power generation efficiency is slightly inferior, but the same operation and effect as the system IV can be exhibited.
なお、図６中、図４と同一部分には同一番号を付し、重複する説明は省略する。 In FIG. 6, the same parts as those in FIG. 4 are denoted by the same reference numerals, and redundant description is omitted.
本発明はタービン動力を利用すると同時に、外気へのＣＯ２排出を防止する必要がある、例えば発電等の産業分野に有効に適用し得る。 The present invention can be effectively applied to an industrial field such as power generation in which it is necessary to use the motive power of the turbine and at the same time prevent CO 2 emission to the outside air.
Ｉ、II、III、IV、V、VI ＣＯ２回収型クローズドサイクル石炭ガス化発電システム
１ 石炭ガス化設備
２ 酸素製造設備
５ 燃焼器
６ ガスタービン
８ 圧縮機
１４ （他の）圧縮機
１６ ＣＯ２回収装置
３１、４１ 触媒燃焼装置
５１、６１ 再熱器
５１Ａ，６１Ａ 脱硝触媒
５１Ｂ，６１Ｂ 燃焼触媒
６１Ｃ 空間部
I, II, III, IV, V, VI CO 2 recovery type closed cycle coal gasification power generation system 1 Coal gasification facility 2 Oxygen production facility 5 Combustor 6 Gas turbine 8 Compressor 14 (Other) Compressor 16 CO 2 Recovery device 31, 41 Catalytic combustion device 51, 61 Reheater 51A, 61A Denitration catalyst 51B, 61B Combustion catalyst 61C Space
Claims (5)
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に触媒燃焼装置を配設したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システム。 Hydrocarbon fuel including coal and heavy oil and oxygen generated in oxygen production facility are supplied to generate gasification gas, and combustion gas is generated using the gasification gas as fuel. A combustor, a gas turbine driven by the combustion gas to drive a generator, and compressing a portion of the exhaust gas of the gas turbine and mixing the compressed exhaust gas with a portion of oxygen produced by the oxygen production facility And a compressor that compresses the exhaust gas from the gas turbine and supplies a part of the exhaust gas to the carbon dioxide recovery device, and returns the remaining exhaust gas to the gasification facility. In a CO 2 recovery type closed cycle gasification power generation system having
A CO 2 recovery type closed-cycle gasification power generation system, characterized in that a catalytic combustion device is disposed upstream of the compressor and another compressor and downstream of the gas turbine.
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に配設された排熱回収ボイラに触媒燃焼装置を一体的に組み込んだことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システム。 In the CO 2 recovery type closed cycle gasification power generation system according to claim 1,
A CO 2 recovery type closed cycle gas in which a catalytic combustion apparatus is integrally incorporated in an exhaust heat recovery boiler disposed upstream of the compressor and other compressors and downstream of the gas turbine. Power generation system.
前記圧縮機および他の圧縮機の上流側で、前記ガスタービンの下流側に再熱器を配設するとともに、
前記再熱器は、上流側から順次配設された脱硝触媒および燃焼触媒を有するとともに、前記脱硝触媒には、前記ガスタービンからの排ガスとともに、前記ガス化設備からのガス化ガスを供給するように構成したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システム。 Hydrocarbon fuel including coal and heavy oil and oxygen generated in oxygen production facility are supplied to generate gasification gas, and combustion gas is generated using the gasification gas as fuel. A combustor, a gas turbine driven by the combustion gas to drive a generator, and compressing a portion of the exhaust gas of the gas turbine and mixing the compressed exhaust gas with a portion of oxygen produced by the oxygen production facility And a compressor that compresses the exhaust gas from the gas turbine and supplies a part of the exhaust gas to the carbon dioxide recovery device, and returns the remaining exhaust gas to the gasification facility. In a CO 2 recovery type closed cycle gasification power generation system having
A reheater is disposed upstream of the compressor and other compressors and downstream of the gas turbine;
The reheater has a denitration catalyst and a combustion catalyst sequentially arranged from the upstream side, and supplies the gasification gas from the gasification facility together with the exhaust gas from the gas turbine to the denitration catalyst. A CO 2 recovery type closed-cycle gasification power generation system characterized by comprising:
前記圧縮機および他の圧縮機の上流側で前記再熱器の下流側に、さらに前記再熱器の排ガスで駆動される再熱ガスタービンを配設したことを特徴とするＣＯ２回収型クローズドサイクルガス化発電システム。 In the CO 2 recovery type closed cycle gasification power generation system according to claim 3,
A CO 2 recovery type closed system characterized in that a reheat gas turbine driven by exhaust gas from the reheater is further arranged upstream of the compressor and other compressors and downstream of the reheater. Cycle gasification power generation system.
前記再熱器は、前記燃焼触媒の下流側に空間部を設けたものであることを特徴とするＣＯ２回収型クローズドサイクルガス化発電システム。
In the CO 2 recovery type closed cycle gasification power generation system according to claim 3 or 4,
The reheater is a CO 2 recovery type closed cycle gasification power generation system characterized in that a space is provided on the downstream side of the combustion catalyst.
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| CN111102073A (en) * | 2019-12-16 | 2020-05-05 | 西安交通大学 | Supercritical carbon dioxide circulating system suitable for coal gasification and operation method thereof |
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