JPH019639Y2 - - Google Patents
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- Publication number
- JPH019639Y2 JPH019639Y2 JP12800082U JP12800082U JPH019639Y2 JP H019639 Y2 JPH019639 Y2 JP H019639Y2 JP 12800082 U JP12800082 U JP 12800082U JP 12800082 U JP12800082 U JP 12800082U JP H019639 Y2 JPH019639 Y2 JP H019639Y2
- Authority
- JP
- Japan
- Prior art keywords
- air
- sulfuric acid
- boiler
- hot air
- gas
- 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.)
- Expired
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 72
- 238000002485 combustion reaction Methods 0.000 claims description 18
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 11
- 239000012895 dilution Substances 0.000 claims description 5
- 238000010790 dilution Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 description 46
- 239000012717 electrostatic precipitator Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 17
- 239000000428 dust Substances 0.000 description 16
- 239000003245 coal Substances 0.000 description 9
- 238000000197 pyrolysis Methods 0.000 description 9
- 239000000295 fuel oil Substances 0.000 description 8
- 239000002828 fuel tank Substances 0.000 description 6
- 230000006698 induction Effects 0.000 description 6
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000003750 conditioning effect Effects 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000007865 diluting Methods 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005367 electrostatic precipitation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 238000010793 Steam injection (oil industry) Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010742 number 1 fuel oil Substances 0.000 description 1
- 230000002250 progressing effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Landscapes
- Electrostatic Separation (AREA)
Description
【考案の詳細な説明】
本考案は電気集じん装置の入口ガスを調節する
ための硫酸熱分解装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a sulfuric acid pyrolysis device for regulating the inlet gas of an electrostatic precipitator.
本考案を詳細に説明するために本考案の実施例
の一つとして、石炭または石炭と重油の混合物の
燃料をボイラ設備に供給する場合について詳細に
説明する。 In order to explain the present invention in detail, as one embodiment of the present invention, a case in which coal or a mixture of coal and heavy oil is supplied to boiler equipment will be described in detail.
近年、エネルギ源多様化の一環として石炭焚き
ボイラへの転換が進められている。 In recent years, conversion to coal-fired boilers has been progressing as part of the diversification of energy sources.
一方、環境規制も次第に厳しくなる傾向にある
石炭焚きボイラの排ガス中のダスト（一般にフラ
イアツシユと呼ばれている）の固有電気抵抗値は
炭質の違いや、石炭中の硫黄含有率等によつて異
なつた値を示すが、一般には108〜1013Ω−cmと
いわれている。 On the other hand, the specific electrical resistance of dust (commonly called flyash) in the exhaust gas of coal-fired boilers, whose environmental regulations are becoming increasingly strict, varies depending on the quality of the coal, the sulfur content in the coal, etc. However, it is generally said to be 10 8 to 10 13 Ω-cm.
そして、電気集じん装置に正常な機能を発揮さ
せるためには、ダストの固有電気抵抗値は105〜
1010Ω−cmの範囲以内でなければならないこと
も、よく知られている。 In order for the electrostatic precipitator to function properly, the specific electrical resistance value of dust must be 10 5 ~
It is also well known that it must be within the range of 10 10 Ω-cm.
固有電気抵抗値が1012〜1013Ω−cmと高い値の
ダストは、電気集じん装置において逆電離現象と
呼ばれる現象を示し、集じん率の極端な低下が起
る。 Dust with a high specific electrical resistance value of 10 12 to 10 13 Ω-cm exhibits a phenomenon called reverse ionization in electrostatic precipitators, resulting in an extreme drop in dust collection rate.
この逆電離現象を抑制するために一般的にはガ
ス調質と呼ばれる処置を施し、ダストの固有電気
抵抗値の見掛けの値を下げ、集じん機能を発揮さ
せているのが実情である。 In order to suppress this reverse ionization phenomenon, the actual situation is that a treatment called gas conditioning is generally performed to lower the apparent value of the specific electrical resistance of the dust and to exert its dust collection function.
ガス調質方法にはボイラ排ガス中に異種の気体
を注入する、いわゆる、SO3ガス注入法、蒸気注
入法、アンモニアガス注入法等があり、そのほか
排ガス中に水をスプレイする水スプレイ法をはじ
め多くの方法が実施されている。 Gas conditioning methods include the so-called SO 3 gas injection method, steam injection method, and ammonia gas injection method, in which different types of gases are injected into the boiler exhaust gas.Other methods include the water spray method, in which water is sprayed into the exhaust gas. Many methods have been implemented.
本考案はダストの固有電気抵抗値が約1013Ω−
cm程度の石炭をボイラで燃焼した排ガス中にSO3
を注入する、いわめるSO3注入法を適用し、非常
に良好な結果を得た硫酸熱分解装置を提供するも
のである。 In this invention, the specific electric resistance value of dust is approximately 10 13 Ω−.
SO 3 is present in the exhaust gas from burning about 1.2 cm of coal in a boiler.
The purpose of this project is to provide a sulfuric acid thermal decomposition device that uses the so-called SO 3 injection method, which injects sulfuric acid, and obtains very good results.
なお、本考案におけるSO3ガス注入法は電気集
じんにとつて最も有効な方法といわれている。し
かし、SO3ガスを安定した組成で、さらに安全に
得るためには高度の技術、とくにその制御に優れ
た技術を必要としている。 Note that the SO 3 gas injection method in the present invention is said to be the most effective method for electrostatic precipitation. However, in order to obtain SO 3 gas with a stable composition and even more safely, advanced technology, especially excellent control technology, is required.
従来より本用途に使用されている硫酸熱分解装
置について説明する。第１図はそのプロセスを示
す系統図である。 The sulfuric acid thermal decomposition equipment conventionally used for this purpose will be explained. FIG. 1 is a system diagram showing the process.
本図において、１はボイラの燃料タンクを示
し、２はボイラ用バーナを示す。 In this figure, 1 indicates a boiler fuel tank, and 2 indicates a boiler burner.
３はボイラ本体であるが、本図ではボイラ付属
設備の給水配管や蒸気配管などは省略する。 3 is the boiler body, but the boiler auxiliary equipment such as water supply piping and steam piping are omitted in this figure.
４は空気予熱器、５は電気集じん装置である。
電気集じん装置５ではボイラによつて燃焼された
石炭の燃焼排ガス中のダストを排ガスから分離・
集じんし、排ガスを清浄にする機能をもつてい
る。 4 is an air preheater, and 5 is an electrostatic precipitator.
The electrostatic precipitator 5 separates dust in the flue gas of coal burned by the boiler from the flue gas.
It has the function of collecting dust and purifying exhaust gas.
６は誘引フアンである。誘引フアン６がプロセ
スの最後に設けられているので、ボイラ３、空気
予熱器４、電気集じん装置５およびこれらの装置
部配管、煙道等はすべて大気より低い圧力とな
る。７は煙突、８は押込フアンである。 6 is an attraction fan. Since the induction fan 6 is provided at the end of the process, the boiler 3, air preheater 4, electrostatic precipitator 5, and piping, flue, etc. of these devices are all at a pressure lower than atmospheric pressure. 7 is a chimney, and 8 is a push fan.
以上、第１図において、ボイラの燃料タンク１
から押込フアン８までのすべての機器、装置は完
全なボイラ設備としては必須のものである。 Above, in Fig. 1, boiler fuel tank 1
All equipment and devices from the boiler to the forced fan 8 are essential for complete boiler equipment.
この他に脱硫設備や脱硝設備を設けたシステム
もあるが、本考案には、これらの設備の有無は直
接の関係がないので省略する。 In addition, there are systems equipped with desulfurization equipment and denitrification equipment, but the presence or absence of these equipment is not directly relevant to the present invention and will therefore be omitted.
つぎに硫酸熱分解装置について説明する。 Next, the sulfuric acid thermal decomposition apparatus will be explained.
１０は硫酸貯蔵タンクであり、１１は硫酸を輸
送するポンプを示す。また、１２は燃料タンクを
示し、１３は燃料（主として重油）を輸送するプ
ンプを示す。なお、プロパンガス等を使用する場
合は、燃焼タンク１２およびポンプ１３は不要と
なる。１４は熱風発生炉、１５は連結ダクト、１
６は硫酸熱分解炉、１７は硫酸スプレイノズルで
あり、１８は空気予熱器４より電気集じん装置５
に送られるボイラ排ガス中に硫酸熱分解炉１６か
らSO3を注入するノズルである。 10 is a sulfuric acid storage tank, and 11 is a pump for transporting sulfuric acid. Further, 12 indicates a fuel tank, and 13 indicates a pump for transporting fuel (mainly heavy oil). Note that when propane gas or the like is used, the combustion tank 12 and pump 13 are not necessary. 14 is a hot air generating furnace, 15 is a connecting duct, 1
6 is a sulfuric acid pyrolysis furnace, 17 is a sulfuric acid spray nozzle, and 18 is an electrostatic precipitator 5 from the air preheater 4.
This is a nozzle that injects SO 3 from the sulfuric acid thermal decomposition furnace 16 into the boiler exhaust gas sent to the boiler.
１９は燃焼用空気の流入路を示し、２０は熱ガ
ス希釈空気の流入路を示す。 Reference numeral 19 indicates an inflow path for combustion air, and 20 indicates an inflow path for hot gas dilution air.
２１は燃焼空気フアン、２２は熱風発生炉１４
に設けたノズル、２３は熱風発生炉１６で発生し
たSO3ガスを電気集じん装置５に入る直前の含じ
ん排ガス中に導入する導管である。 21 is a combustion air fan, 22 is a hot air generating furnace 14
The nozzle 23 provided in the hot air generating furnace 16 is a conduit that introduces the SO 3 gas generated in the hot air generating furnace 16 into the dust-containing exhaust gas immediately before entering the electrostatic precipitator 5.
つぎに、第１図に示す工程図によつて従来の硫
酸熱分解装置によるボイラ排ガスの調質操作につ
いて説明する。 Next, a boiler exhaust gas refining operation using a conventional sulfuric acid thermal decomposition apparatus will be explained with reference to the process diagram shown in FIG.
ボイラ本体３内に、微粉炭と、空気予熱器４内
で加熱された空気とを、ボイラ用バーナ２によつ
て噴入し、微粉炭を完全燃焼させる。 Pulverized coal and air heated in an air preheater 4 are injected into the boiler body 3 by the boiler burner 2, and the pulverized coal is completely combusted.
ボイラ本体３内で完全燃焼した微粉炭の灰分
（フライアツシユ）は排ガス中に含まれる。 The ash (fly ash) of the pulverized coal that has been completely burned in the boiler body 3 is contained in the exhaust gas.
このボイラ排ガスは誘引フアン６によつてボイ
ラ本体３内より誘出され、空気予熱器４内に送入
される。 This boiler exhaust gas is extracted from the boiler main body 3 by the induction fan 6 and fed into the air preheater 4.
ボイラ排ガスは空気予熱器４内で、同じく押込
フアン８によつて送入された大気中の空気との間
で熱交換が行なわれる。 In the air preheater 4, the boiler exhaust gas undergoes heat exchange with atmospheric air that is also introduced by a forced fan 8.
空気予熱器４内で適当に冷却されたボイラ排ガ
スは、さらに誘引フアン６によつて誘出されて電
気集じん装置５内に入る。 The boiler exhaust gas appropriately cooled within the air preheater 4 is further induced by an induction fan 6 and enters the electrostatic precipitator 5.
空気予熱器４内でボイラ排ガスと熱交換した空
気は上記したようにボイラ用バーナ２に導かれ、
微粉炭燃焼用の空気としてボイラ本体３内に噴入
される。 The air that has exchanged heat with the boiler exhaust gas in the air preheater 4 is guided to the boiler burner 2 as described above,
It is injected into the boiler main body 3 as air for pulverized coal combustion.
一方、燃料タンク１２より重油をポンプ１３に
よつて輸送してバーナ２２に送る。また、燃焼空
気フアン２１によつて大気中の空気を誘引し、空
気の流路１９を経てバーナ２２に送る。 On the other hand, heavy oil is transported from the fuel tank 12 by the pump 13 and sent to the burner 22. In addition, air from the atmosphere is drawn in by the combustion air fan 21 and sent to the burner 22 through the air flow path 19.
この両者（重油と大気中の空気）をバーナ２２
によつて熱風発生炉１４内に噴射し、重油を燃焼
させて熱風を発生させる。 Both of these (heavy oil and air in the atmosphere) are transferred to the burner 22.
is injected into the hot air generating furnace 14 to burn heavy oil and generate hot air.
この熱風が所定の温度より高いときは、流路２
０によつて大気中の空気の一部を熱風発生炉１４
内に送つて炉内に発生した熱風を希釈して適温の
熱風にし、連結ダクト１５を経て硫酸熱分解炉１
６に導入される。一方、ポンプ１１によつて硫酸
貯蔵タンク１０内より硫酸液を輸送し、硫酸スプ
レイノズル１７によつて硫酸分解炉１６内に噴射
する。 When this hot air is higher than a predetermined temperature, the flow path 2
A part of the air in the atmosphere is transferred to a hot air generating furnace 14 by
The hot air generated in the furnace is diluted into hot air at an appropriate temperature, and then passed through the connecting duct 15 to the sulfuric acid pyrolysis furnace 1.
6 will be introduced. On the other hand, the sulfuric acid solution is transported from the sulfuric acid storage tank 10 by the pump 11, and is injected into the sulfuric acid decomposition furnace 16 by the sulfuric acid spray nozzle 17.
そうすると、硫酸分解炉１６内で噴霧状の硫酸
液が熱風によつて熱分解され、SO3ガスが発生す
る。 Then, the sprayed sulfuric acid liquid is thermally decomposed by the hot air in the sulfuric acid decomposition furnace 16, and SO 3 gas is generated.
このSO3ガスは電気集じん装置５に入る直前の
ボイラ排ガス中に、導管２３および導管２３の先
端のノズル１８によつて噴入される。 This SO 3 gas is injected into the boiler exhaust gas just before entering the electrostatic precipitator 5 through the conduit 23 and the nozzle 18 at the tip of the conduit 23 .
SO3ガスの噴入によつてボイラ排ガスは、適度
に調質されつつ誘引フアン６によつて電気集じん
装置５内に誘引される。 The boiler exhaust gas is moderately refined by the injection of SO 3 gas and is drawn into the electrostatic precipitator 5 by the drawing fan 6 .
ボイラ排ガスは電気集じん装置５内で逆電離現
象と呼ばれるダストの抵抗を受けることなく、円
滑なダストの分離・集じんが行なわれる。 The boiler exhaust gas is smoothly separated and collected in the electrostatic precipitator 5 without being subjected to dust resistance called reverse ionization phenomenon.
ダスト（フライアツシユ）を除かれたボイラ排
ガスは、さらに誘引フアン６によつて電気集じん
装置５外に誘出され、煙突７によつて大気中に放
散される。 The boiler exhaust gas from which dust (fly ash) has been removed is further drawn out of the electrostatic precipitator 5 by an induction fan 6, and is dissipated into the atmosphere by a chimney 7.
一方、ボイラ排ガスより除かれたダストは、電
気集じん装置５下部のホツパより装置外に排出さ
れる。 On the other hand, the dust removed from the boiler exhaust gas is discharged to the outside of the electrostatic precipitator 5 from a hopper at the bottom of the device.
なお、熱風発生炉１４からの熱風の誘引や、硫
酸熱分解炉１６からボイラ排ガス中へのSO3ガス
の噴入はすべて押込フアン２１によつて行なわれ
る。 Note that the induction of hot air from the hot air generating furnace 14 and the injection of SO 3 gas from the sulfuric acid thermal decomposition furnace 16 into the boiler exhaust gas are all performed by the forced fan 21 .
第２図は本考案の硫酸熱分解装置を使用したボ
イラ排ガス調質プロセスを示す系統図である。 FIG. 2 is a system diagram showing a boiler exhaust gas refining process using the sulfuric acid pyrolysis apparatus of the present invention.
図中、第１図と同一部分または相当する部分に
は同一符号を付し、その説明は省略する。 In the figure, parts that are the same as or correspond to those in FIG.
第１図に示す従来の技術と相異する点はつぎの
とおりである。すなわち、
燃焼空気フアン２１を不要とし、大気中の空気
を直接、熱風発生炉１４へ、重油熱焼用または熱
ガス希釈用として噴入することを廃止し、ボイラ
設備に設けた押込フアン８より空気予熱器４を経
て加熱された熱空気の一部を熱風発生炉１４に導
き、重油燃焼用または熱ガス希釈用として使用す
る。 The differences from the conventional technique shown in FIG. 1 are as follows. That is, the combustion air fan 21 is not required, the air in the atmosphere is no longer injected directly into the hot air generation furnace 14 for burning heavy oil or for diluting hot gas, and the air from the atmosphere is no longer injected directly into the hot air generation furnace 14 for burning heavy oil or for diluting hot gas. A part of the hot air heated through the air preheater 4 is guided to the hot air generating furnace 14 and used for burning heavy oil or diluting hot gas.
このため第１図に示す燃焼空気フアン２１およ
び燃焼用空気の流入路１９および熱ガス希釈空気
の流入路をなくし、その代り第２図に示すよう
に、空気予熱器４とボイラ本体３のボイラ用バー
ナ２とを結ぶ熱空気導管２４の途中から熱風発生
炉１４のバーナ２２までの間を燃焼用空気の流入
路１９で連結し、燃焼用空気の流入路１９の途中
から熱風発生炉１４の吸気口までを熱ガス希釈空
気の流入路２０で連結した構成とした。 Therefore, the combustion air fan 21, combustion air inflow path 19, and hot gas dilution air inflow path shown in FIG. 1 are eliminated, and instead, as shown in FIG. A combustion air inflow path 19 connects the hot air conduit 24 from the middle of the hot air conduit 24 to the burner 22 of the hot air generation furnace 14, and The structure is such that the air intake port is connected by an inflow path 20 for hot gas diluted air.
本考案の特徴をさらに詳細に説明すると、つぎ
のとおりである。 The features of the present invention will be explained in more detail as follows.
まず第１点は、従来の装置（第１図参照）では
熱風発生炉１４から硫酸分解炉１６を経てSO3を
注入するノズル１８までの間における圧力損失が
約500mmAqであつたものを、考案者はSO3を注入
するノズル１８をはじめ、熱風発生炉１４、硫酸
熱分解炉１６等の性能、機能を確保するなかで圧
力低減に取組み、理論検討後さまざまな実験を繰
返した結果、200mm以下に低減することに成功し
た。この結果、第１図の燃焼空気フアン２１が不
要となつた。 First, in the conventional device (see Figure 1), the pressure loss between the hot air generator 14, the sulfuric acid decomposition furnace 16, and the nozzle 18 for injecting SO 3 was approximately 500 mmAq. While ensuring the performance and functionality of the nozzle 18 for injecting SO 3 , the hot air generating furnace 14, the sulfuric acid pyrolysis furnace 16, etc., the team worked to reduce the pressure, and as a result of conducting various experiments after conducting theoretical studies, they found that the pressure was reduced to 200 mm or less. succeeded in reducing the As a result, the combustion air fan 21 shown in FIG. 1 is no longer necessary.
第２点は制御性の問題で、硫酸熱分解法は高濃
度のSO3を得るためには、温度制御が重要な要因
である。 The second point is the issue of controllability; temperature control is an important factor in obtaining high-concentration SO 3 in the sulfuric acid thermal decomposition method.
硫酸を熱分解すれば化学反応は
H2SO4→SO3＋H2Oとなるが、硫酸熱分解炉１
６の出口温度が例えば1000℃となるとSO3は完全
にSO2に分解する。 When sulfuric acid is thermally decomposed, the chemical reaction is H 2 SO 4 →SO 3 +H 2 O, but the sulfuric acid thermal decomposition furnace 1
When the outlet temperature of 6 becomes, for example, 1000°C, SO 3 is completely decomposed into SO 2 .
そもそも電気集じん装置の性能向上のためのガ
ス調質は、電気集じん装置の入口ダクト中へSO3
を注入することによつてダスト表面で
SO3＋H2O→H2SO4の反応を起こさせ、ダスト
表面に導通性の硫酸層を形成させることが目的で
ある。それが、SO2に分解してしまうと、この効
果は失なわれる。このために、硫酸熱分解炉１６
の出口温度を450±10℃の範囲内で制御している。 In the first place, gas conditioning to improve the performance of electrostatic precipitators is done by removing SO 3 from the inlet duct of the electrostatic precipitator.
The purpose is to cause a reaction of SO 3 + H 2 O → H 2 SO 4 on the dust surface by injecting it, and to form a conductive sulfuric acid layer on the dust surface. Once it decomposes into SO 2 , this effect is lost. For this purpose, the sulfuric acid pyrolysis furnace 16
The outlet temperature is controlled within the range of 450±10℃.
また、硫酸熱分解炉１６の入口温度も780±20
℃に制御することによつて硫酸熱分解炉１６内で
の温度分布を、できるだけ小さくコントロールす
ることができた。 In addition, the inlet temperature of the sulfuric acid pyrolysis furnace 16 is 780±20
By controlling the temperature to 0.degree. C., the temperature distribution within the sulfuric acid thermal decomposition furnace 16 could be controlled to be as small as possible.
以上述べたように本考案は、空気予熱器４とボ
イラ用バーナ２とを結ぶ熱空気導管２４の途中よ
り分岐して熱風発生炉１４のバーナ２２に至る燃
焼用空気の流入路と、燃焼用空気の流入路より分
岐して熱風発生炉１４の吸気口に至る熱ガス希釈
空気の流入路を設けて、硫酸の熱分解用熱ガス源
に、ボイラ本体３で発生したダストを含む燃焼排
ガスとの熱交換により加熱された空気を利用する
ようにした。 As described above, the present invention provides an inflow path for combustion air that branches from the middle of the hot air conduit 24 connecting the air preheater 4 and the boiler burner 2 and reaches the burner 22 of the hot air generating furnace 14, and An inflow path for hot gas diluted air that branches from the air inflow path and reaches the intake port of the hot air generating furnace 14 is provided, and the combustion exhaust gas containing dust generated in the boiler body 3 and the hot gas source for thermal decomposition of sulfuric acid are provided. The system uses air that has been heated through heat exchange.
したがつて、希釈空気の温度が従来の約20℃に
比べて280℃となつたことで、制御特性上、かえ
つて急激な変動が起り得なくなり精度が向上し
た。 Therefore, the temperature of the dilution air is now 280°C, compared to about 20°C in the past, which prevents sudden fluctuations in control characteristics and improves accuracy.
また、熱風発生炉での燃料の燃焼に加熱空気を
利用したことによつて噴霧が良好となり、燃焼が
非常に安定した。 In addition, by using heated air to burn the fuel in the hot air generating furnace, the spraying was good and the combustion was very stable.
燃料が従来の約50％に低減できるので、熱風発
生炉の大きさを半分以下にすることができるなど
多くの効果をあげることができた。 Since the fuel consumption can be reduced by approximately 50% compared to conventional methods, many benefits have been achieved, including the ability to reduce the size of the hot air generating furnace by more than half.
また、本発明で使用する空気量は押込フアン８
からの空気量の0.5％以下であるので、ボイラ設
備に与える影響は全くない。 In addition, the amount of air used in the present invention is as follows:
Since it is less than 0.5% of the amount of air from the boiler, it has no effect on the boiler equipment.
第１図は石炭焚きボイラの排ガスの電気集じん
において、硫酸熱分解装置を使用して排ガスの調
質を行なう従来のプロセスを示す系統図、第２図
は第１図における本考案のプロセスを示す系統図
である。
１はボイラの燃料タンク、２はボイラ用バー
ナ、３はボイラ本体、４は空気予熱器、５は電気
集じん装置、６は誘引フアン、７は煙突、８は押
込フアン、１０は硫酸貯蔵タンク、１１は硫酸を
輸送するポンプ、１２は燃料タンク、１３は燃料
を輸送するポンプ、１４は熱風発生炉、１５は連
結ダクト、１６は硫酸熱分解炉、１７は硫酸スプ
レイノズル、１８はSO3を注入するノズル、１９
は燃焼用空気の流入路、２０は熱ガス希釈空気の
流入路、２１は燃焼空気フアン、２２はバーナ、
２３は導管、２４は熱空気導管である。
Figure 1 is a system diagram showing the conventional process of refining exhaust gas using a sulfuric acid pyrolysis device in electrostatic precipitation of exhaust gas from coal-fired boilers, and Figure 2 shows the process of the present invention in Figure 1. FIG. 1 is the boiler fuel tank, 2 is the boiler burner, 3 is the boiler body, 4 is the air preheater, 5 is the electrostatic precipitator, 6 is the induction fan, 7 is the chimney, 8 is the forced fan, 10 is the sulfuric acid storage tank , 11 is a pump for transporting sulfuric acid, 12 is a fuel tank, 13 is a pump for transporting fuel, 14 is a hot air generating furnace, 15 is a connecting duct, 16 is a sulfuric acid pyrolysis furnace, 17 is a sulfuric acid spray nozzle, 18 is SO 3 nozzle for injecting, 19
20 is a combustion air inflow path, 20 is a hot gas dilution air inflow path, 21 is a combustion air fan, 22 is a burner,
23 is a conduit, and 24 is a hot air conduit.
Claims (1)
導管の途中より分岐して熱風発生炉のバーナに至
る燃焼用空気の流入路と、燃焼用空気の流入路よ
り分岐して熱風発生炉の吸気口に至る熱ガス希釈
空気の流入路を設けたことを特徴とする硫酸熱分
解装置。 A combustion air inflow path that branches off from the middle of the hot air conduit connecting the air preheater and the boiler burner and reaches the burner of the hot air generation furnace, and a combustion air inflow path that branches off from the combustion air inflow path and leads to the hot air inlet of the hot air generation furnace. A sulfuric acid thermal decomposition device characterized by having an inflow path for hot gas dilution air to reach the temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12800082U JPS5936841U (en) | 1982-08-26 | 1982-08-26 | Sulfuric acid pyrolysis equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12800082U JPS5936841U (en) | 1982-08-26 | 1982-08-26 | Sulfuric acid pyrolysis equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5936841U JPS5936841U (en) | 1984-03-08 |
| JPH019639Y2 true JPH019639Y2 (en) | 1989-03-16 |
Family
ID=30290523
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12800082U Granted JPS5936841U (en) | 1982-08-26 | 1982-08-26 | Sulfuric acid pyrolysis equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5936841U (en) |
-
1982
- 1982-08-26 JP JP12800082U patent/JPS5936841U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5936841U (en) | 1984-03-08 |
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