JPH10185170A - Combustion apparatus - Google Patents
Combustion apparatusInfo
- Publication number
- JPH10185170A JPH10185170A JP8356837A JP35683796A JPH10185170A JP H10185170 A JPH10185170 A JP H10185170A JP 8356837 A JP8356837 A JP 8356837A JP 35683796 A JP35683796 A JP 35683796A JP H10185170 A JPH10185170 A JP H10185170A
- Authority
- JP
- Japan
- Prior art keywords
- combustion
- heat exchange
- exhaust gas
- tower
- exchange integrated
- 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.)
- Pending
Links
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 31
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000003054 catalyst Substances 0.000 claims abstract description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000001257 hydrogen Substances 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 11
- 238000004064 recycling Methods 0.000 claims abstract description 3
- 230000003197 catalytic effect Effects 0.000 claims description 7
- 238000000034 method Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910001882 dioxygen Inorganic materials 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 101150076749 C10L gene Proteins 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000006114 decarboxylation reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Landscapes
- Chimneys And Flues (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は燃焼装置に関し、特
に、炭酸ガスの分離塔がないにもかかわらず炭酸ガスの
排出量が少ない、安価で熱効率に優れた燃焼装置に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a combustion apparatus, and more particularly to a combustion apparatus which is low in cost and excellent in thermal efficiency, emits a small amount of carbon dioxide gas even without a carbon dioxide separation tower.
【０００２】[0002]
【従来技術】近年、種々の内燃機関から排出される排ガ
ス中に含まれるＣＯ2 が地球の温暖化をもたらすという
ことが明確になり、その削減の重要性が認識されるに至
った。そこで、例えば大規模なＣＯ2 の発生源となって
いる火力発電所においては、排ガス中のＮＯX やＳＯX
を除去した後ＣＯ2 をアミン液に吸収させ、次いで、液
化して固定化し、海に隔離する方法が検討されている。
また、ＣＯ2 を吸収するアミン液の代わりにゼオライト
を使用する方法も検討されているが、何れにしても、そ
の脱炭酸部分の建設費は、石炭火力発電所の全建設費の
３０％を占めると試算されているように、高額となると
いう欠点がある。2. Description of the Related Art In recent years, it has been clarified that CO 2 contained in exhaust gas discharged from various internal combustion engines causes global warming, and the importance of the reduction has been recognized. Therefore, for example, in a thermal power plant that is a large-scale source of CO 2 , NO X and SO X in exhaust gas
A method has been studied in which CO 2 is absorbed into an amine solution after removal of CO 2 , then liquefied and immobilized, and sequestered in the sea.
In addition, a method of using zeolite instead of an amine solution that absorbs CO 2 has been studied, but in any case, the construction cost of the decarboxylation portion accounts for 30% of the total construction cost of a coal-fired power plant. There is a drawback that it is expensive, as estimated to occupy.
【０００３】また、排ガス中のＣＯ2 を分離する方法と
して、高分子分離膜や無機膜を使用したり、ＣａＯと反
応させる方法も検討されているが、高分子分離膜は２０
０℃以上の排ガスに適用できず、無機膜は分離特性や耐
久性等が十分でなく、ＣａＯ＋ＣＯ2 の反応の場合に
は、反応速度が遅いため装置が大型とならざるを得ず、
コスト高となる等、夫々難点がある。As a method for separating CO 2 from exhaust gas, a method using a polymer separation membrane or an inorganic membrane or a method of reacting with CaO has been studied.
It cannot be applied to exhaust gas of 0 ° C. or higher, and the inorganic membrane has insufficient separation characteristics and durability. In the case of CaO + CO 2 reaction, the reaction speed is slow, so the apparatus must be large,
Each has its own drawbacks, such as high costs.
【０００４】これらのプロセスの検討は、例えば、“Ｏ
2 ／ＣＯ2 燃焼”野口等、火力原子力発電、Ｖｏｌ．４
４，Ｐ４１２，（１９９３）、“ＣＯ2 回収型石炭部分
燃焼”藤井等、火力原子力発電、Ｖｏｌ．４５，Ｐ２６
（１９９４）、“気体反応による火力発電所排気ガスか
らのＣＯ2 分離プロセス”、清水等、ケミカルエンジニ
アリング．Ｐ６４７（１９９６）においてなされてい
る。The examination of these processes is described, for example, in "O
2 / CO 2 combustion “Noguchi et al., Thermal and Nuclear Power, Vol.
4, P412, (1993), "CO 2 capture type coal partial combustion", Fujii et al., Thermal Nuclear Power, Vol. 45, P26
(1994), "CO 2 separation process from thermal power plants the exhaust gas by the gaseous reaction", Hitoshi Shimizu, Chemical Engineering. P647 (1996).
【０００５】一方、ＣＯ2 を藻類に吸収させたり、尿
素、メタン、アルコール等の原材料として有効活用しよ
うとする研究もなされている。特にメタンについては、
次の（１）及び（２）式の触媒反応がよく知られてお
り、何れの場合も大きな生成熱が得られることも知られ
ている。 （１）ＣＯ2 ＋４Ｈ2 ＝ＣＨ4 ＋２Ｈ2 Ｏ △Ｈ298 ＝−１６５KJ／モル （２）ＣＯ2 ＋３Ｈ2 ＝ＣＨ4 ＋Ｈ2 Ｏ △Ｈ298 ＝−２０６KJ／モル[0005] On the other hand, studies have been made to absorb CO 2 into algae and to make effective use as a raw material such as urea, methane and alcohol. Especially for methane,
The following catalytic reactions (1) and (2) are well known, and it is also known that in each case, a large heat of formation is obtained. (1) CO 2 + 4H 2 = CH 4 + 2H 2 O ΔH 298 = −165 KJ / mol (2) CO 2 + 3H 2 = CH 4 + H 2 O ΔH 298 = −206 KJ / mol
【０００６】この場合、通常、下記（３）又は（４）式
も考慮される。 （３）ＣＯ2 ＋Ｈ2 →ＣＯ＋Ｈ2 Ｏ △Ｈ298 ＝−４２KJ／モル （４）ＣＯ2 ＋３Ｈ2 →ＣＨ3 ＯＨ＋Ｈ2 Ｏ △Ｈ298 ＝−４９KJ／モル しかしながら、これらの１００〜５００℃における平衡
定数は、（１）及び（２）式の場合よりはるかに小さい
ため、ＣＨ3 ＯＨは殆ど生成せず、メタンが優先的に生
産される。また、（４）式によってメタノールを優先的
に生産するためには、２００〜３００℃で１００気圧程
度の圧力を必要とするのでコスト高となる。In this case, usually, the following equation (3) or (4) is also considered. (3) CO 2 + H 2 → CO + H 2 O ΔH 298 = −42 KJ / mol (4) CO 2 + 3H 2 → CH 3 OH + H 2 O ΔH 298 = −49 KJ / mol However, their equilibrium at 100 to 500 ° C. Since the constant is much smaller than in the case of the equations (1) and (2), almost no CH 3 OH is produced, and methane is preferentially produced. Further, in order to preferentially produce methanol according to the formula (4), a pressure of about 100 atm is required at 200 to 300 ° C., which increases the cost.
【０００７】そこで、本発明者等は、ＣＯ2 をメタンに
転換する系について更に検討したところ、前記（１）及
び（２）式に基づいて発生する生成熱の除去機能をも有
する熱交換一体型の触媒反応器を組み込むと共に、生成
したメタンを燃焼塔に戻すことにより、従来のような大
型の脱炭酸装置を設置する必要のない燃焼装置を実現す
ることができることを見い出し、本発明に到達した。The inventors of the present invention have further studied a system for converting CO 2 to methane, and found that the heat exchange system also has a function of removing generated heat generated based on the above formulas (1) and (2). By incorporating a body-shaped catalytic reactor and returning the generated methane to the combustion tower, it has been found that a combustion device that does not require the installation of a large-sized decarbonation device as in the past can be realized, and the present invention has been achieved. did.
【０００８】[0008]
【発明が解決しようとする課題】従って本発明の目的
は、大型の脱炭酸装置を不要とし、安価な設備コスト
で、効率的に、排出する排ガス中のＣＯ2 の含有量を低
減することのできる燃焼装置を提供することにある。SUMMARY OF THE INVENTION Accordingly, an object of the present invention is to eliminate the need for a large-sized decarboxylation device, to reduce the CO 2 content in exhaust gas to be discharged efficiently at low equipment cost. It is to provide a combustion device which can be used.
【０００９】[0009]
【課題を解決するための手段】本発明の上記の目的は、
ＣＯ2 を排出する燃焼塔と排ガス用ダクトを、水素とＣ
Ｏ2 を反応させてメタンを生成する熱交換一体型触媒反
応器を介して接続してなる燃焼装置であって、前記燃焼
塔と熱交換一体型触媒反応器の間に水素供給口を有する
と共に、該熱交換一体型触媒反応器から排出されるガス
の一部を前記燃焼室に再供給する如く、前記排ガス用ダ
クトに、少なくともブロア及びリサイクル用管路を配し
てなることを特徴とする燃焼装置によって達成された。SUMMARY OF THE INVENTION The above objects of the present invention are as follows.
The combustion tower that emits CO 2 and the exhaust gas duct
A combustion device connected via a heat exchange integrated catalyst reactor for reacting O 2 to produce methane, comprising a hydrogen supply port between the combustion tower and the heat exchange integrated catalyst reactor. The exhaust gas duct is provided with at least a blower and a recycling pipe so that a part of the gas discharged from the heat exchange integrated catalytic reactor is resupplied to the combustion chamber. Achieved by the combustion device.
【００１０】[0010]
【発明の実施の形態】以下に、本発明を図面に基づいて
詳述する。図１は、本発明の燃焼装置の構成概念図であ
る。図において、符合１は燃焼塔、２は脱ＮＯX 装置及
び／又は脱ＳＯX 装置、３は熱交換器、４は熱交換一体
型触媒反応塔、５はブロワー、６は、装置外に排出する
排気ガスを浄化するための熱交換一体型反応塔である。
燃焼塔１は、酸素を用いてＬＮＧ等の燃料を燃焼させる
公知の燃焼塔の中から適宜選択して使用することができ
る。また、脱ＮＯX 及び脱ＳＯX 装置は、燃料の種類に
応じて、公知のものの中から最も適当なものを選択して
使用する。熱交換器３は、ＣＯ2 と反応させる水素を予
熱するためのものであり、通常使用されるものを使用す
ることができる。予熱された水素は、水素供給口から燃
焼装置内に供給される。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below in detail with reference to the drawings. FIG. 1 is a conceptual diagram of the configuration of the combustion device of the present invention. In the figure, reference numeral 1 is a combustion tower, 2 de NO X device and / or de-SO X device, 3 a heat exchanger, 4 the heat exchanger-integrated catalyst reaction tower, five blowers 6, discharged out of the apparatus This is a heat exchange integrated reaction tower for purifying exhaust gas.
The combustion tower 1 can be appropriately selected from known combustion towers for burning fuel such as LNG using oxygen. Also, de-NO X and de SO X device, depending on the type of fuel is used to select the most appropriate from known materials. The heat exchanger 3 is for preheating hydrogen to be reacted with CO 2 , and a commonly used one can be used. The preheated hydrogen is supplied into the combustion device from a hydrogen supply port.
【００１１】本発明で使用する熱交換一体型触媒反応塔
としては、例えば、実公平８−４１０４号や特願平７−
３４９１９２号に記載されたような、少なくとも反応室
の内壁が触媒を担持したアルマイト表面となっている、
熱伝導性に優れた、金属性で熱交換器を兼ねた触媒反応
器を複数組み立てて使用する。触媒は、ＣＯ2 とＨ2 か
らメタンを生成するための公知の触媒の中から適宜選択
して用いることができる。The heat exchange integrated catalytic reaction tower used in the present invention includes, for example, Japanese Utility Model Publication No. Hei 8-4104 and Japanese Patent Application No.
At least the inner wall of the reaction chamber has an alumite surface supporting a catalyst, as described in JP-A-349192.
Assemble and use multiple catalytic reactors with excellent thermal conductivity that also function as heat exchangers. The catalyst can be appropriately selected from known catalysts for producing methane from CO 2 and H 2 and used.
【００１２】本発明においては、ＣＯ2 とＨ2 からメタ
ンを生成する前記（１）及び（２）の反応が暴走するこ
とを防ぐために、反応燃を直ちに除去することのできる
上記熱交換一体型触媒反応塔が必須である。上記の反応
熱は、熱交換一体型反応器の非反応室内に通す冷媒によ
って除去する。本発明においては、上記の冷媒として、
燃焼塔に供給する酸素、及び／又はＣＯ2 と反応させる
水素を用いることが、装置全体の熱効率を高める上から
好ましく、特に、除去する熱量の大きさその他の熱効率
の観点から、酸素ガスを使用し、これによって該酸素ガ
スを予熱することが好ましい。In the present invention, in order to prevent runaway of the above-mentioned reactions (1) and (2) for producing methane from CO 2 and H 2, the above-mentioned heat exchange integrated type which can immediately remove the reaction fuel can be used. A catalytic reaction tower is essential. The above-mentioned reaction heat is removed by the refrigerant passing through the non-reaction chamber of the integrated heat exchange reactor. In the present invention, as the above refrigerant,
It is preferable to use oxygen supplied to the combustion tower and / or hydrogen reacted with CO 2 from the viewpoint of increasing the thermal efficiency of the entire apparatus. In particular, from the viewpoint of the amount of heat to be removed and other thermal efficiencies, oxygen gas is used. However, it is preferable to preheat the oxygen gas.
【００１３】熱交換一体型反応塔４内では、前記（１）
又は（２）式の反応が進行し、燃焼塔から排出される排
ガスは、該排ガス中に含まれるＣＯ2 の殆どはメタンに
還元された後放出される。本発明においては、上記の如
く改質された排ガスの一部をブロワー５によって燃焼塔
に還流し、該排ガスの中のメタンを燃料の一部として使
用する。In the heat exchange integrated reaction tower 4, (1)
Alternatively, the reaction of formula (2) proceeds, and the exhaust gas discharged from the combustion tower is released after most of the CO 2 contained in the exhaust gas is reduced to methane. In the present invention, a part of the exhaust gas reformed as described above is returned to the combustion tower by the blower 5, and methane in the exhaust gas is used as a part of the fuel.
【００１４】このような構成上、及び、ＮＯX の発生を
防止する観点から、本発明においては、燃焼塔で使用す
る酸素中には窒素の存在が少ない方が好ましいので、純
酸素ガスを用いることが好ましい。純酸素の代わりに空
気を用いる場合はＮ2 ／メタンの分離が必要である。但
し、何れにしても、（１）又は（２）の反応を進行させ
るために、及び爆発の危険をなくすために、燃焼塔１の
燃焼後の排ガス中に酸素が残存しないように、脱酸素塔
を設けるか燃料と酸素の混合比を調節することが必要で
ある。[0014] on this structure, and, from the viewpoint of preventing the occurrence of NO X, in the present invention, since it is preferred presence of nitrogen is small in oxygen used in the combustion tower, using pure oxygen gas Is preferred. When air is used instead of pure oxygen it is necessary to separate the N 2 / methane. However, in any case, in order to allow the reaction of (1) or (2) to proceed and to eliminate the danger of explosion, deoxygenation is performed so that no oxygen remains in the exhaust gas after combustion of the combustion tower 1. It is necessary to provide a tower or adjust the mixing ratio of fuel and oxygen.
【００１５】本発明で使用する水素については、本装置
と供にメタンの部分酸化等による水素製造装置を併設し
ても、タンクローリー等で搬入して使用しても良い。
尚、排煙脱硫装置を乾式とする場合には、本装置内にお
けるＨ2 Ｏの分圧が高くなるので、水蒸気を除去する必
要がある。また、ＣＯ2 の分圧が１０容量％を超えると
下記の如く、排ガスの温度は、約５７０℃と極めて高温
になる。With respect to the hydrogen used in the present invention, a hydrogen producing apparatus for performing partial oxidation of methane or the like may be provided together with the present apparatus, or may be carried in using a tank truck or the like.
If the flue gas desulfurization device is of a dry type, the partial pressure of H 2 O in the device increases, so that it is necessary to remove water vapor. When the partial pressure of CO 2 exceeds 10% by volume, the temperature of the exhaust gas becomes extremely high at about 570 ° C. as described below.
【００１６】前記（１）式によって炭酸ガスをメタン化
する場合の排気ガスの温度上昇△ｔ（℃）は、排気ガス
中のＣＯ2 の分圧を１０容量％と仮定すると、１ｍ3 中
のＣＯ2 の量は、（１００，０００×１０-6／２２．
４）×１０3 ＝４．４６（モル／ｎｍ3 ）である。ま
た、ＣＯ2 の生成熱は、１６５×０．２４（ｋｃａｌ／
モル）であるから、その発熱量は、１６５×０．２４×
４．４６＝１７６．６（ｋｃａｌ／ｎｍ3 ）となる。更
に、空気の比熱は０．３１（ｋｃａｌ／ｎｍ3 ・℃）で
あるので、△ｔ（℃）＝１７６．６／０．３１＝５６
９．７（℃）となる。[0016] (1) temperature rise △ t (° C.) of the exhaust gas when the methanation of carbon dioxide by the formula, assuming the partial pressure of CO 2 in the exhaust gas and 10 volume%, in 1 m 3 The amount of CO 2 is (100,000 × 10 −6 / 22.
4) × 10 3 = 4.46 (mol / nm 3 ). The heat of formation of CO 2 is 165 × 0.24 (kcal /
Mol), the calorific value is 165 × 0.24 ×
4.46 = 176.6 (kcal / nm 3 ). Further, since the specific heat of air is 0.31 (kcal / nm 3 · ° C.), Δt (° C.) = 176.6 / 0.31 = 56
9.7 (° C.).
【００１７】この熱は、前記熱交換一体型反応器におい
て冷媒に供給され、これによって反応を安定に維持する
ことができる。更に、窒素を加えてＣＯ2 の分圧を抑制
することもできる。尚、水蒸気の除去には、適宜公知の
脱水蒸気塔を設ければ良いが、これは、脱ＮＯX 及び／
又は脱ＳＯX 装置と熱交換一体型触媒反応器との間に設
けることが特に好ましい。This heat is supplied to the refrigerant in the heat exchange integrated reactor, whereby the reaction can be maintained stably. Further, the partial pressure of CO 2 can be suppressed by adding nitrogen. Note that the removal of water vapor, may be provided as appropriate known de steam tower, which is de-NO X and /
Or it is particularly preferably provided between the de-SO X device and the heat exchanger-integrated catalyst reactor.
【００１８】熱交換一体型反応塔４から排出される排気
ガスのうち、燃焼塔１に還流されない部分については、
空気を供給して他の熱交換一体型反応塔６で燃焼させ、
浄化した後、排気すれば良い。この場合に発生する燃焼
熱も、前記熱交換一体型反応塔の場合と同様に、水素ガ
ス等の予熱に使用することができる。更に、前記熱交換
器３の代わりに使用できるように設計することもでき
る。The part of the exhaust gas discharged from the heat exchange integrated reaction tower 4 that is not recirculated to the combustion tower 1 is
Air is supplied and burned in another heat exchange integrated reaction tower 6,
After purifying, it may be exhausted. The combustion heat generated in this case can also be used for preheating hydrogen gas or the like, similarly to the case of the heat exchange integrated reaction tower. Furthermore, it can be designed so that it can be used instead of the heat exchanger 3.
【００１９】[0019]
【発明の効果】本発明の燃焼装置は、熱交換一体型触媒
反応塔を使用しているので、従来設けられていた脱炭酸
塔を必要としない。従って、装置全体が小型となって設
備費が安価となるのみならず、炭酸ガスをメタン化する
際の反応熱を有効利用する上、排気ガスの一部を燃焼塔
に還流させるので、エネルギー効率が良好である。The combustion apparatus of the present invention does not require the conventionally provided decarbonation tower because it uses a heat exchange integrated catalytic reaction tower. Therefore, not only is the entire apparatus compact and the equipment cost is low, but also the heat of reaction when carbon dioxide gas is methanated is effectively used, and a part of the exhaust gas is returned to the combustion tower. Is good.
【図１】本発明の燃焼装置の構成を示す概念図である。FIG. 1 is a conceptual diagram showing a configuration of a combustion device of the present invention.
１ 燃焼塔 ２ 脱ＮＯX 及び／又はＳＯX 装置 ３ 熱交換器 ４ 熱交換一体型反応塔 ５ ブロワー ６ 熱交換一体型反応塔1 combustion tower 2 de NO X and / or SO X 3 heat exchanger 4 heat exchanger-integrated reaction column 5 Blower 6 heat exchanger-integrated reaction column
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ１０Ｌ 3/06 Ｃ１０Ｌ 3/00 Ａ Ｆ２３Ｊ 15/00 Ａ Ｈ Ｂ ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 6 Identification symbol FI C10L 3/06 C10L 3/00 A F23J 15/00 A H B
Claims (4)
トを、水素とＣＯ2を反応させてメタンを生成する熱交
換一体型触媒反応器を介して接続してなる燃焼装置であ
って、前記燃焼塔と熱交換一体型触媒反応器の間に水素
供給口を有すると共に、該熱交換一体型触媒反応器から
排出されるガスの一部を前記燃焼室に再供給する如く、
前記排ガス用ダクトに、少なくともブロア及びリサイク
ル用管路を配してなることを特徴とする燃焼装置。1. A combustion device comprising a combustion tower for discharging CO 2 and an exhaust gas duct connected via a heat exchange integrated catalytic reactor for producing methane by reacting hydrogen and CO 2 , A hydrogen supply port is provided between the combustion tower and the heat exchange integrated catalyst reactor, and a part of gas discharged from the heat exchange integrated catalyst reactor is resupplied to the combustion chamber,
A combustion apparatus characterized in that at least a blower and a recycling pipe are arranged in the exhaust gas duct.
に、脱ＮＯX 及び／又は脱ＳＯX 装置を有している、請
求項１に記載された燃焼装置。2. Between the combustion tower and the heat exchanger-integrated catalyst reactor, and a de-NO X and / or de-SO X device, combustion apparatus according to claim 1.
一体型触媒反応器との間に、脱水蒸気塔を配してなる、
請求項２に記載された燃焼装置。3. A de-steam column is disposed between a NO x removal and / or SO x removal device and a heat exchange integrated catalytic reactor.
The combustion device according to claim 2.
気ガスのうち、燃焼塔に再供給しない部分の排気ガスを
浄化して燃焼装置の外に排出する如く、更に、他の熱交
換一体型触媒反応器を設けてなる、請求項１〜３の何れ
かに記載された燃焼装置。4. A method for purifying a portion of the exhaust gas discharged from the heat exchange integrated catalytic reactor which is not re-supplied to the combustion tower and purifying the exhaust gas to the outside of the combustion apparatus. The combustion device according to any one of claims 1 to 3, comprising an integrated catalytic reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8356837A JPH10185170A (en) | 1996-12-25 | 1996-12-25 | Combustion apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8356837A JPH10185170A (en) | 1996-12-25 | 1996-12-25 | Combustion apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH10185170A true JPH10185170A (en) | 1998-07-14 |
Family
ID=18451022
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8356837A Pending JPH10185170A (en) | 1996-12-25 | 1996-12-25 | Combustion apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH10185170A (en) |
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