JPH02157021A - Ammonia gas producing apparatus from ammonia water - Google Patents
Ammonia gas producing apparatus from ammonia waterInfo
- Publication number
- JPH02157021A JPH02157021A JP63311019A JP31101988A JPH02157021A JP H02157021 A JPH02157021 A JP H02157021A JP 63311019 A JP63311019 A JP 63311019A JP 31101988 A JP31101988 A JP 31101988A JP H02157021 A JPH02157021 A JP H02157021A
- Authority
- JP
- Japan
- Prior art keywords
- ammonia
- gas
- ammonia water
- water
- evaporation chamber
- 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
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 182
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 31
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 30
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 54
- 238000001704 evaporation Methods 0.000 claims description 23
- 230000008020 evaporation Effects 0.000 claims description 22
- 229910021529 ammonia Inorganic materials 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims description 3
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 19
- 238000000034 method Methods 0.000 abstract description 9
- 238000005260 corrosion Methods 0.000 abstract description 6
- 230000007797 corrosion Effects 0.000 abstract description 6
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000428 dust Substances 0.000 abstract description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical class N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、排煙脱硝装置に係り、粕に都市型の自家発電
設備で必要となるアンモニア（以下Ｎ Ｉ−１。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a flue gas denitrification device, in which ammonia (hereinafter referred to as NI-1) necessary for urban private power generation equipment is added to lees.
と称す）ガス発生装置に関する。(referred to as ) gas generator.
アンモニア接触還元性排煙脱硝装置に採用されるＮＨ３
ガス発生装置は、通常、液体アンモニア（以下液安と称
す）をガス化させて使用するため、その殆どが、容量５
仕様的な面から、高圧ガス取締法の適用対象となり、そ
の取り扱いが大幅に制約を受ける。このため、そのよう
な法的制約が少ないアンモニア水（以下安水と称す）を
利用し、これを煙道内に吹き込んで、ＮＨ３をガス化さ
せる方法が採用されるようになったきた。この方式を第
２図で説明する。即ち、安水ａはタンク１に貯えられ、
（Ｊｔ給ポンプ２にて加圧され、戻し制御弁３で一部安
水を戻しながら、煙道５内への安水量をコントロールし
、安水噴霧ノズル４より霧状にスプレーし、煙１ｆｆｉ
ｓ内の排ガスによ−ってＮｌｌ。NH3 used in ammonia catalytic reduction flue gas denitrification equipment
Gas generators usually gasify liquid ammonia (hereinafter referred to as liquid ammonia), so most of them have a capacity of 5.
Due to its specifications, it is subject to the High Pressure Gas Control Law, and its handling is subject to significant restrictions. For this reason, a method has been adopted in which ammonia water (hereinafter referred to as ammonium water), which has fewer such legal restrictions, is used and blown into the flue to gasify NH3. This method will be explained with reference to FIG. That is, ammonium water a is stored in tank 1,
(The ammonium water is pressurized by the Jt supply pump 2, and while some of the ammonium water is returned by the return control valve 3, the amount of ammonium water into the flue 5 is controlled, and the ammonium water is sprayed in a mist form from the ammonium water spray nozzle 4, resulting in 1ffi of smoke.
Nll by exhaust gas in s.
も水分も一緒に蒸発さセる仕組めになっている。It is designed to evaporate water and water together.
４０は脱硝装置である。40 is a denitrification device.
この場合、問題は排ガス中での安水の完全蒸発であるが
、これが非常に難しく、ドレンが煙道５内に溜まったり
、後流脱硝触媒層まで水滴が飛散し、触媒性能劣化を引
き起こしたりする。また、ＳＯＸを含む排ガスを処理す
る場合には、脱色後流の排熱ボイラ低温チューブバンク
の腐食や、煙道内腐食を促進させたりする。さらに、安
水噴霧ノズル後流の機器や煙道でのメンテナンスも大変
である。In this case, the problem is the complete evaporation of ammonium water in the exhaust gas, but this is extremely difficult, and condensate may accumulate in the flue 5, or water droplets may scatter to the downstream denitration catalyst layer, causing catalyst performance deterioration. do. Furthermore, when exhaust gas containing SOX is treated, corrosion of the low-temperature tube bank of the waste heat boiler downstream of decolorization and corrosion within the flue are promoted. Furthermore, maintenance of the equipment downstream of the ammonium water spray nozzle and the flue is also difficult.
このため、より効果的な安水の噴霧を行うため、安水を
、オイルバーナ等のように、高圧蒸気でアトマイズする
方式も提案されているが、改善されたとは言い難い。こ
のようなことから、安水方式は実用化に至っておらず、
実績も非常に少ない。For this reason, in order to more effectively spray ammonium water, a method of atomizing ammonium water using high-pressure steam, such as with an oil burner, has been proposed, but it cannot be said that this has been improved. For these reasons, the cheap water method has not been put into practical use.
There are also very few achievements.
しかしながら、最近、ディーゼルやガスターヒンを使っ
たコジェネレーションプラントの設置か急増し、特に、
都市型として、ビルの地下に設置するケースも増加して
きている。この場合は、やはり、高圧ガス取締法の適用
から外れる安水法で計画を要求される場合が多い。この
ため、安水を使って、従来の安水煙道内噴霧方式より信
頼性の高いＮＨ３ガス発生方式の提案の要求か必須であ
る。However, recently, the installation of cogeneration plants using diesel and gas turbines has increased rapidly, and in particular,
As an urban type, the number of cases where they are installed underground in buildings is increasing. In this case, plans are often required under the Safe Water Law, which is exempt from the High Pressure Gas Control Law. Therefore, it is essential to propose a method for generating NH3 gas using ammonium water, which is more reliable than the conventional ammonium water flue spraying method.
上記従来技術は、排ガス中へ安水を噴霧スプレーさせる
ことが出来ない。あるいは排カス流中で完全蒸発をさせ
ることが出来ないという問題かあった。The above-mentioned conventional technology cannot spray ammonium water into exhaust gas. Alternatively, there was a problem that complete evaporation could not be achieved in the waste stream.
例えば、排ガス中の煤塵や、排ガス中のＳＯ３と安水中
のＮ Ｔ（３とから生成する硫安化合物が、噴霧ノズル
先端に付着堆積し、安水のツｔＸを阻害した場合に起こ
る。また、排ガス中に安水の水分が蒸発し、排ガス中の
水分濃度を上昇させる結果、酸性硫安生成域が拡大し、
排熱回収ボイラの低温、チューブバンクの腐食域が広が
ると同時に、煤塵の付着堆積も促進される。For example, this occurs when soot in the exhaust gas or ammonium sulfate compounds generated from SO3 in the exhaust gas and NT (3) in the aqueous solution adhere and accumulate at the tip of the spray nozzle, inhibiting the TStX of the aqueous solution. The moisture in the ammonium sulfate evaporates in the exhaust gas, increasing the moisture concentration in the exhaust gas, and as a result, the area where acidic ammonium sulfate is generated expands.
The low temperature of the waste heat recovery boiler expands the corrosion area of the tube bank, and at the same time promotes the adhesion and accumulation of soot and dust.
本発明の目的は、排煙脱硝装置の安水を作ったＮ Ｈ３
ガス発生装置において、安水からＮＨ３ガス（一部水蒸
気含）を分離し、これをエア希釈して、煙道内に希釈Ｎ
Ｈ３ガスを注入する方式を採用し、上記の従来技術の
欠点を完全になくすことにある。The purpose of the present invention is to use NH3 produced as ammonium water for flue gas denitration equipment
In the gas generator, NH3 gas (containing some water vapor) is separated from the ammonium water, diluted with air, and diluted N gas is added into the flue.
The purpose is to completely eliminate the drawbacks of the prior art by adopting a method of injecting H3 gas.
安水からＮＨ：＋ガスを蒸発分離することが出来れば、
脱硝反応器上流煙道内に、安水を注入する必要はなく、
安水から分離したＮＨ３（水蒸気台）をガス状で排ガス
中へ注入することができる。If NH:+ gas can be evaporated and separated from ammonium water,
There is no need to inject ammonium water into the flue upstream of the denitrification reactor.
NH3 (steam table) separated from ammonium water can be injected into the exhaust gas in gaseous form.
このような安水からＮＨ，ガスを造る手段として、蒸気
や電気を熱源とした安水の加熱器を内蔵したＮＨ３発生
装置に、安水を入れ、安水温度を上昇してゆけば、過飽
和のＮ Ｈ３が蒸発する。この蒸発したガス状ＮＨ３を
空気を媒体として、ＮＨ３ガス発生装置外へ気流搬送し
、これを脱硝反応器上流煙道に注入する。こうすること
によって、前項で説明した従来技術の問題点は完全に解
決できる。As a means of producing NH and gas from such ammonium water, ammonium water is poured into an NH3 generator equipped with an ammonium water heater that uses steam or electricity as a heat source, and if the ammonium water temperature is increased, supersaturation occurs. of NH3 evaporates. This evaporated gaseous NH3 is transported by air to the outside of the NH3 gas generator using air as a medium, and is injected into the flue upstream of the denitrification reactor. By doing so, the problems of the prior art explained in the previous section can be completely solved.
尚、上述の安水からのＮ Ｈｚの蒸発分離は、安水中の
ＮＨ，溶解度が液温か高くなるにつれて下がり、１００
℃ではゼロ（０）となるこ々を利用したものである。In addition, the evaporative separation of N Hz from ammonium water mentioned above decreases as the solubility of NH in ammonium water increases as the liquid temperature increases.
This takes advantage of the fact that it is zero (0) at °C.
基本的には、安水を加熱することによって、ＮＨ３が容
易に蒸発する現象を利用する。第３図にＮＨ３の水への
溶解度を示す（出典；化学便覧法礎編、改訂２版、丸首
、昭和５０年６月発行）。Basically, it utilizes the phenomenon that NH3 easily evaporates by heating ammonium water. Figure 3 shows the solubility of NH3 in water (Source: Chemistry Handbook Law Foundation Edition, revised 2nd edition, Marukubi, published June 1975).
これにより、安水（Ｎ Ｈ３水）温度が」二昇する程、
ＮＨ，の水への溶解度が下がり、］ ００ ’Ｃでその
溶解度はゼロ（０）になる。As a result, the temperature of ammonium water (NH3 water) rises by 2',
The solubility of NH, in water decreases, and its solubility becomes zero (0) at ]00'C.
即ち、安水を蒸気や電気等を熱源にし、直接的あるいは
間接的に加熱し、安水からＮＨｌを蒸発分離し、空気を
媒体として気流搬送し、この希釈ＮＨ，ガスを直接、あ
るいは、さらに空気により希釈して、排ガス中に注入す
る。That is, ammonium water is directly or indirectly heated using steam or electricity as a heat source, NH1 is evaporated and separated from the ammonium water, air is used as a medium to transport the diluted NH and gas directly or further. Dilute with air and inject into the exhaust gas.
方、安水から完全にＮ１１３を蒸発分離した水は、１０
０℃近辺の高温水であるため、このエネルギーを常温で
供給する安水の昇温エネルギーとして使うと省エネの観
点からも有効である。On the other hand, water from which N113 has been completely evaporated and separated from ammonium water has a concentration of 10
Since the water is at a high temperature of around 0°C, it is effective from the viewpoint of energy saving if this energy is used to raise the temperature of the ammonium water supplied at room temperature.
第１図に本発明の実施例を示す。 FIG. 1 shows an embodiment of the present invention.
全体構成は、安水貯蔵装置１０．ＮＨ３ガス発生装置２
０．ＮＨ３ガス注入装置３０とからなる。The overall configuration is an ammonium water storage device 10. NH3 gas generator 2
0. It consists of an NH3 gas injection device 30.
安水貯蔵装置１０においては、安水タンク１１に安水ａ
が一旦貯蔵され、安水ａは安水送水ポンプ１２より送水
される。Ｎ ＋−１３ガス発生装置２０への送水量は、
脱硝装置４０に必要なＮＨ，量に見合った安水量が調節
弁１３により制御されて送られる。従って、余分な安水
ａは抵抗弁１４を経由して安水タンク１１へ戻される。In the ammonium water storage device 10, ammonium water a is placed in the ammonium water tank 11.
is temporarily stored, and the ammonium water a is sent by the ammonium water water pump 12. The amount of water fed to the N+-13 gas generator 20 is:
An amount of ammonium water commensurate with the amount of NH required for the denitrification device 40 is controlled by the control valve 13 and sent. Therefore, excess ammonium water a is returned to the ammonium water tank 11 via the resistance valve 14.
ＮＨ，ガス発生装置２０へ送水された安水ａは、ここで
加熱昇温されて飽和含有Ｎ Ｈ，を蒸発分離される。安
水ａは完全にＮＨ３分が蒸発分離除去されると無害な排
水となってＮＨ３ガス発生装置２０外へ放流される。The ammonium water a sent to the NH gas generator 20 is heated and heated to evaporate and separate the saturated NH. When the NH3 component of the ammonium water a is completely removed by evaporation and separation, it becomes harmless waste water and is discharged to the outside of the NH3 gas generator 20.
この安水ａから含有Ｎ Ｉ−１、を蒸発分離する過程を
以下説明する。ＮＨ，ガス発生装置２０の内部は、ＮＨ
，ガス蒸発室２１と排水路２２とからなっている。ＮＨ
，ガス蒸発室２１は、安水流入口側からせき２３と防液
板２４とが交互に配置されており、最終室には電気ヒー
タや蒸気加熱器等の熱源２５を設け、ここで安水ａは約
１００℃まで昇温制御されている。この段階で安水中の
Ｎ１１゜は総で蒸発し、安水は約１００℃の高温排水と
なって、排水路２２を通って流れて行くが、この際、高
温排水の上部はＮＨ，ガス蒸発室２１の底部−Ｃ１その
底板を伝熱板として、高温水と安水ａとが交流で熱交換
し、高温水は熱回収されて温度を下げ、一方、安水は熱
回収して昇温しで行く。このようにして、安水は最終的
には約１００℃となって含有Ｎ Ｈ３分を完全に蒸発除
去されて無害な温水となり、この温水は供給されてくる
安水に熱回収されて、放流される程度まで温度を下げる
ことができる。The process of evaporating and separating the contained N I-1 from this ammonium water a will be described below. NH, the inside of the gas generator 20 is NH
, a gas evaporation chamber 21 and a drainage channel 22. N.H.
In the gas evaporation chamber 21, weirs 23 and liquid-proof plates 24 are arranged alternately from the ammonium water inlet side, and a heat source 25 such as an electric heater or a steam heater is provided in the final chamber, where the ammonium water a The temperature is controlled to rise to approximately 100°C. At this stage, all of the N11° in the ammonium chloride evaporates, and the ammonium water turns into high-temperature wastewater of approximately 100°C and flows through the drainage channel 22. At this time, the upper part of the high-temperature wastewater contains NH and gas evaporation. Bottom of chamber 21 - C1 Using the bottom plate as a heat transfer plate, high-temperature water and ammonium water a exchange heat through alternating current, the high-temperature water recovers heat and lowers its temperature, while the ammonium water recovers heat and raises its temperature. I'll go. In this way, the ammonium water eventually reaches a temperature of approximately 100°C, and the NH3 content is completely removed by evaporation, resulting in harmless hot water.The heat of this hot water is recovered by the supplied ammonium water, and the water is discharged. The temperature can be lowered to the extent that
次に、ＮＨ３注大装置３０であるが、ＮＨｉ希釈空気フ
ァン３１からの空気すの一部、又は、全部をＮＨ３ガス
発生装置２０に送風し、ＮＨ３ガス発生装置２０内で発
生したＮＨ３ガスを気流搬送し、希釈ＮＨ，ｌガスＣと
して、脱硝装置４０の上流に設置されたＮＨ３注入ノズ
ルグリッド３２により煙道３３内に注入する。Next, the NH3 pouring device 30 blows some or all of the air from the NHi dilution air fan 31 to the NH3 gas generator 20 to collect the NH3 gas generated in the NH3 gas generator 20. The gas is conveyed by air current and injected as diluted NH,1 gas C into the flue 33 through the NH3 injection nozzle grid 32 installed upstream of the denitrification device 40.
尚、ダンパ３４はＮＨ３希釈空気ファン３１からの空気
すの一部をＮＨ３ガス発生装置２０に流し、残りをバイ
パスさせる場合の調整用として設けたものである。The damper 34 is provided for adjustment when a part of the air from the NH3 diluted air fan 31 is flowed to the NH3 gas generator 20 and the rest is bypassed.
以上、一実施例を示したが、この実施例では熱源２５は
ＮＨ３ガス蒸発室２１の最終室にのみある例を示したが
、各室に設けてもよく、また、ＮＨ，ガス蒸発室２１の
下部に排水路２２を設け、高温排水を流し、高温排水か
ら熱回収するようにしたが、排水路２２をなくし、高温
排水で放出することもできる。さらに、ＮＨ３ガス蒸発
室２１の室内に設けるせき２３と防液板２４とは安水ａ
の効率的な熱回収による効果的なＮＨ３ガス蒸発を考慮
し取付けたものであるが、安水、ｊが十分均一に昇温さ
れ、含有Ｎ Ｈ３を完全に蒸発できれは何段階に分けて
もよく、ゼロ（０）でもよい。One embodiment has been described above. In this embodiment, the heat source 25 is provided only in the last chamber of the NH3 gas evaporation chamber 21, but it may be provided in each chamber. A drainage channel 22 is provided at the bottom of the tank to allow high-temperature wastewater to flow through and recover heat from the high-temperature wastewater, but it is also possible to eliminate the drainage channel 22 and discharge heat as high-temperature wastewater. Furthermore, the weir 23 and the liquid-proof plate 24 provided inside the NH3 gas evaporation chamber 21 are
This was installed in consideration of effective NH3 gas evaporation through efficient heat recovery. It may be zero (0).
第４図、第５図はＮＨ３発生装Ｔ１．２０の他の実施例
を示す概略構成図である。FIGS. 4 and 5 are schematic configuration diagrams showing other embodiments of the NH3 generator T1.20.
第４図に示す実施例では、ＮＩＬ、ガス蒸発″＋２１を
複数の室には仕切らず、−室として構成し、傾斜したＮ
Ｈ３ガス蒸発室２１の上方から安水ａが、安水噴霧ノ
ズル２６により噴霧状態で送り込まれ、熱源２５によっ
て加熱され、含有ＮＩ１．を蒸発させる。そして、ＮＨ
３ガス蒸発室２１の下方から送り込まれる空気すにより
Ｎ Ｈｚ希釈ガスＣとして上方のパイプから送り出す。In the embodiment shown in FIG.
Ammonium water a is fed in a sprayed state from above the H3 gas evaporation chamber 21 by the ammonium water spray nozzle 26, heated by the heat source 25, and containing NI1. evaporate. And N.H.
3. Air is sent from below into the gas evaporation chamber 21 and sent out from the upper pipe as NHz dilution gas C.
２７は排水オーバフロー管である。27 is a drainage overflow pipe.
第５図に示す実施例では、上端の開「］部をガスパイプ
２８に臨ませて、蒸発したＮ１■、をこのカスパイプ２
８の左側から送られて来る空気すと混合させ、Ｎ Ｈ３
希釈ガスＣとしてガスパイプ２８の右側に送り出すうよ
うになっている。In the embodiment shown in FIG.
Mix it with the air sent from the left side of No. 8, and make N H3
The diluent gas C is sent out to the right side of the gas pipe 28.
本発明を採用することによる効果を以下に列挙する。 The effects of adopting the present invention are listed below.
＋１．１従来の安水噴霧方式と同様、高圧ガス取締法の
適用を受りることなく、特に、都市型としてのコージェ
ネレーションプラントに好適な脱硝用Ｎ Ｈ３ガス発生
装置である。+1.1 Similar to the conventional ammonium spray method, this is a denitrification NH3 gas generator that is not subject to the High Pressure Gas Control Law and is particularly suitable for urban cogeneration plants.
（２）従来の安水の煙道内直接噴霧方式と異なり、安水
から蒸発分離したＮＨｆｆガスを煙道内に注入するため
、従来法で問題となる安水の不完全蒸発による煙道内へ
のドレン凝縮や、その結果生じる煙道内腐食、さらには
、致命的事故となる脱硝触媒層への安水水滴飛散による
触媒性能劣化等の問題は全く起こりようがない。このた
め、装置としては長期安定運転かできる高信頼性のもの
となる。(2) Unlike the conventional method of directly spraying ammonium water into the flue, the NHff gas separated by evaporation from the ammonium water is injected into the flue, so there is no drainage into the flue due to incomplete evaporation of the ammonium water, which is a problem with conventional methods. Problems such as condensation, resulting corrosion in the flue, and deterioration of catalyst performance due to the scattering of ammonium water droplets onto the denitrification catalyst layer, which can lead to fatal accidents, are completely unlikely to occur. Therefore, the device is highly reliable and can operate stably for a long period of time.
（３）煙道内へはＮＨＪガス（若干水分台）を注入する
ため、排ガス中にＳＯＸ （イオウ酸化物）が含まれ
ているときは、従来法で生しる排ガス中への安水水分蒸
発による排ガス中の水分濃度上昇による脱硝後流排熱回
収ボイラ低温デユープバンクでの酸性硫安の生成領域が
縮小されることにより、チューブ腐食が軽減されるとと
もに、ダスト付着堆積による排熱回収効率の低下やチュ
ーブ間ダスト閉塞などの伝熱管障害が大幅に改善される
。(3) Because NHJ gas (slightly high moisture content) is injected into the flue, if the flue gas contains SOX (sulfur oxide), ammonium water will evaporate into the flue gas instead of using conventional methods. By reducing the generation area of acidic ammonium sulfate in the low-temperature duplex bank of the exhaust heat recovery boiler downstream of denitrification due to the increase in moisture concentration in the exhaust gas, tube corrosion is reduced, and the reduction in exhaust heat recovery efficiency due to dust adhesion and accumulation is reduced. Heat transfer tube failures such as inter-tube dust blockage are significantly improved.
第１図は本発明の一実施例に係るアンモニアガス発生装
置を含むシステム全体の概念図、第２図は従来例に係る
アンモニアガス供給ソステトの概念図、第３図は水に対
するアンモニアの溶解度のデータを示す図、第４図、第
５し１は本発明の他の実施例に係るアンモニアガス発生
装置の概略図である。
２１・・・アンモニアガス蒸発室、２５・・・熱源、３
１・・・ファン、３３・・・煙道、ａ・・・アンモニア
水、ｂ・・・空気、Ｃ・・・希釈アンモニアガス。
第
図
第
図
第
図
第
図Fig. 1 is a conceptual diagram of the entire system including an ammonia gas generator according to an embodiment of the present invention, Fig. 2 is a conceptual diagram of a conventional ammonia gas supply system, and Fig. 3 is a diagram of the solubility of ammonia in water. Figures 4 and 5 showing the data are schematic diagrams of an ammonia gas generator according to another embodiment of the present invention. 21... Ammonia gas evaporation chamber, 25... Heat source, 3
1... Fan, 33... Flue, a... Ammonia water, b... Air, C... Diluted ammonia gas. Figure Figure Figure Figure Figure
Claims (4)
モニアガス発生装置において、アンモニア水を加熱する
手段と、加熱により蒸発する過飽和のアンモニアをガス
状で取り出し、排煙脱硝装置まで気流搬送する手段とを
備えたことを特徴とするアンモニア水からのアンモニア
ガス発生装置。(1) In the ammonia gas generation device in the ammonia catalytic reduction flue gas denitrification device, a means for heating ammonia water and a means for extracting supersaturated ammonia that evaporates by heating in gaseous form and transporting it in airflow to the flue gas denitrification device are provided. An ammonia gas generator from ammonia water, characterized by comprising:
ニアガス発生装置において、供給されるアンモニア水が
オーバーフローしながら流れるように、せきと防液板と
で交互に仕切るとともに、最終室には熱源を有するアン
モニアガス蒸発室と、 このアンモニアガス蒸発室の下方に設けた排水路とを備
えたことを特徴とするアンモニア水からのアンモニアガ
ス発生装置。(2) In the ammonia gas generating device from ammonia water according to claim (1), the final chamber is partitioned alternately with weirs and liquid-proof plates so that the supplied ammonia water flows while overflowing. An ammonia gas generating device from ammonia water, comprising: an ammonia gas evaporation chamber having a heat source; and a drainage channel provided below the ammonia gas evaporation chamber.
ニアガス発生装置において、アンモニア水が底面を流下
するように傾けたアンモニアガス蒸発室の底面に、電熱
ヒーターや蒸気加熱器等の熱源を配し、アンモニアガス
蒸発室の上部にアンモニア水噴霧ノズルからアンモニア
水をスプレーし、そのアンモニア水がアンモニアガス蒸
発室の底面を流下する間にアンモニア水を昇温、その液
中のアンモニアの大部分を蒸発させ、さらに、室内底部
に約１００℃の液温となる液溜まりを作り、ここでアン
モニア水中の残りの含有アンモニアを完全に蒸発させて
、このガス化したアンモニアを空気により気流搬送しア
ンモニアガス蒸発室外へ取り出す構成にしたことを特徴
とするアンモニア水からのアンモニアガス発生装置。(3) In the ammonia gas generation device from ammonia water according to claim (1), a heat source such as an electric heater or a steam heater is installed on the bottom of the ammonia gas evaporation chamber which is tilted so that the ammonia water flows down the bottom. Ammonia water is sprayed from an ammonia water spray nozzle onto the top of the ammonia gas evaporation chamber, and while the ammonia water flows down the bottom of the ammonia gas evaporation chamber, the temperature of the ammonia water is increased, and most of the ammonia in the liquid is heated. Furthermore, a liquid pool with a liquid temperature of approximately 100°C is created at the bottom of the room, where the remaining ammonia contained in the ammonia water is completely evaporated, and this gasified ammonia is transported by air with air to convert it into ammonia. An apparatus for generating ammonia gas from aqueous ammonia, characterized in that the ammonia gas is extracted to the outside of the gas evaporation chamber.
ニアガス発生装置において、竪型のアンモニアガス蒸発
室の周囲に電熱ヒーターや蒸気加熱器等の熱源を配し、
室内天井部に取り付けたアンモニア水噴霧ノズルよりア
ンモニア水をスプレーし、アンモニア水噴霧水滴の昇温
により大部分の過飽和アンモニアを蒸発させ、さらに底
部に約１００℃の液温となる液溜まりを作り、ここでア
ンモニア水中の残りの含有アンモニアを完全に蒸発させ
、蒸発したアンモニアガスを蒸気加熱器の天井部より蒸
気加熱器外へ抜き出し、空気により、アンモニア希釈ガ
スとして気流搬送する構成にしたことを特徴とするアン
モニアからのアンモニアガス発生装置。(4) In the ammonia gas generation device from ammonia water according to claim (1), a heat source such as an electric heater or a steam heater is arranged around the vertical ammonia gas evaporation chamber,
Spray ammonia water from an ammonia water spray nozzle attached to the ceiling of the room, evaporate most of the supersaturated ammonia by raising the temperature of the ammonia water spray droplets, and create a liquid pool at the bottom with a liquid temperature of about 100°C. Here, the remaining ammonia contained in the ammonia water is completely evaporated, and the evaporated ammonia gas is extracted from the ceiling of the steam heater to the outside of the steam heater, and is transported by air as ammonia dilution gas. Ammonia gas generator from ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63311019A JPH02157021A (en) | 1988-12-10 | 1988-12-10 | Ammonia gas producing apparatus from ammonia water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63311019A JPH02157021A (en) | 1988-12-10 | 1988-12-10 | Ammonia gas producing apparatus from ammonia water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02157021A true JPH02157021A (en) | 1990-06-15 |
Family
ID=18012140
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63311019A Pending JPH02157021A (en) | 1988-12-10 | 1988-12-10 | Ammonia gas producing apparatus from ammonia water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02157021A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0617698A1 (en) * | 1990-10-15 | 1994-10-05 | Exxon Research And Engineering Company | Aqueous ammonia injection scheme |
| WO2002062704A3 (en) * | 2001-02-08 | 2003-02-13 | Chemithon Corp | Method for quantitative production of gaseous ammonia |
| JP2011226434A (en) * | 2010-04-22 | 2011-11-10 | Isuzu Motors Ltd | System for supplying ammonia to scr device |
-
1988
- 1988-12-10 JP JP63311019A patent/JPH02157021A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0617698A1 (en) * | 1990-10-15 | 1994-10-05 | Exxon Research And Engineering Company | Aqueous ammonia injection scheme |
| EP0617698A4 (en) * | 1990-10-15 | 1995-02-01 | Exxon Research Engineering Co | Aqueous ammonia injection scheme. |
| WO2002062704A3 (en) * | 2001-02-08 | 2003-02-13 | Chemithon Corp | Method for quantitative production of gaseous ammonia |
| JP2011226434A (en) * | 2010-04-22 | 2011-11-10 | Isuzu Motors Ltd | System for supplying ammonia to scr device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4999167A (en) | Low temperature Nox /Sox removal apparatus | |
| CN107032428A (en) | A kind of undersaturation flue gas condensing crystallizing desulfurization wastewater zero-discharge treatment system and method | |
| CN109045976A (en) | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system and application | |
| CN105668669B (en) | A kind of power plant desulfurization wastewater treatment system and technique | |
| WO1995007751A1 (en) | Exhaust gas boiler | |
| CN107986365A (en) | A kind of fluoroplastics falling film evaporator that desulfurization wastewater concentration is carried out using fume afterheat | |
| CN208025546U (en) | It is a kind of to remove white thermal siphon heat exchanger for wet flue gas | |
| CN206799197U (en) | A kind of undersaturation flue gas condensing crystallizing desulfurization wastewater zero-discharge treatment system | |
| CN107973475A (en) | Desulfurization wastewater Zero discharging system and method based on waste heat reuse under running on the lower load | |
| CN109945277A (en) | A kind of energy conserving system being used for central heating using electric heat pump depth recycling remaining heat of flue gas from steam power plant | |
| CN105536484A (en) | Pollutant pretreating tower condensing based on flue gas | |
| CN108786404A (en) | A kind of system of the high efficiente callback gas fired-boiler fume afterheat based on bubble techniques | |
| CN108469033A (en) | A kind of dehumidifying decontamination heating of flue gas condensing disappears white heat exchanger | |
| CN109939557A (en) | The system and method for coloured plume are eliminated in collaboration | |
| CN211650417U (en) | Desulfurization slurry cooling flue gas waste heat supply integrated system | |
| CN107120673A (en) | Low temperature SCR denitration and flue gas take off white device | |
| CN102512910A (en) | Smoke heat exchange process for recycling evaporated water of gas desulfurization system | |
| JPH02157021A (en) | Ammonia gas producing apparatus from ammonia water | |
| CN208620331U (en) | A kind of boiler energy recovery system | |
| CN209411826U (en) | Waste water concentrating decrement treatment system | |
| CN204042943U (en) | Desulfurization system for thermal power plant | |
| CN209034090U (en) | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system | |
| CN107344052A (en) | Gas cleaning and plume control method and device | |
| JPS5990617A (en) | Treatment of waste gas | |
| CN206755219U (en) | A kind of low temperature SCR denitration and flue gas take off white device |