JPH0325000Y2 - - Google Patents
Info
- Publication number
- JPH0325000Y2 JPH0325000Y2 JP1986111858U JP11185886U JPH0325000Y2 JP H0325000 Y2 JPH0325000 Y2 JP H0325000Y2 JP 1986111858 U JP1986111858 U JP 1986111858U JP 11185886 U JP11185886 U JP 11185886U JP H0325000 Y2 JPH0325000 Y2 JP H0325000Y2
- Authority
- JP
- Japan
- Prior art keywords
- waste
- gas
- combustion
- incinerator
- burner
- 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
Links
- 239000002699 waste material Substances 0.000 claims description 58
- 239000007789 gas Substances 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 22
- 238000007254 oxidation reaction Methods 0.000 claims description 18
- 239000002912 waste gas Substances 0.000 claims description 18
- 239000000446 fuel Substances 0.000 claims description 15
- 230000003647 oxidation Effects 0.000 claims description 15
- 230000003197 catalytic effect Effects 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 239000000567 combustion gas Substances 0.000 claims description 6
- 239000002440 industrial waste Substances 0.000 claims description 5
- 238000000034 method Methods 0.000 claims description 3
- 231100000331 toxic Toxicity 0.000 claims description 3
- 230000002588 toxic effect Effects 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 description 22
- 239000003054 catalyst Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 6
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 230000001737 promoting effect Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 239000003440 toxic substance Substances 0.000 description 2
- -1 and after oxidation Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Incineration Of Waste (AREA)
Description
〔産業上の利用分野〕
本考案は産業廃棄物を処理する廃棄物処理設備
に係り、特に有毒微量成分を含有する廃油、廃
液、廃ガスの同時処理を可能とする廃棄物処理設
備に関する。
〔従来技術〕
一般に顔料、染料、繊維、薬品などを製造する
有機化学工業において排出される廃液、廃ガス、
廃油などの産業廃棄物は、公害排除のために処理
する必要がある。これらの産業廃棄物の一例を示
せば、廃ガスは微量の気相有害物、例えば酢酸、
シアン化水素、軽質の炭化水素などを数ppmから
5vol％程度で含有するLHV50乃至150Kcal／Ｎ
m3の気体である。また廃液は前記有害物を液相で
含有する水溶液であり、LHV30乃至70Kcal／Kg
の液体である。また廃油は重質の炭化水素類を含
有する有機性水溶液で、LHV4000乃至
6000Kcal／Kgの液体であり、補助燃料としての
作用を有する。このような廃棄物を処理するため
には、燃焼温度が800℃乃至1000℃必要であり、
かつ焼却炉内の停留時間が２乃至３秒必要であ
る。このため従来は第２図に示すように、廃油
１、廃液２、廃ガス３を焼却炉４に供給し、焼却
温度を保つために助燃料５をバーナ６によつて燃
焼させて焼却炉４内を加熱している。また炉内に
おける燃焼を促進するために耐火煉瓦で構築され
たマトリツクスウオール７が設置されている。空
気８は押込送風機９によつて焼却炉４内に供給さ
れるが、主処理物である廃油１、廃液２、廃ガス
３の燃焼用の他に、助燃料５の燃焼用としてバー
ナ６にも供給される。例えば下記の第１表に示す
[Industrial Application Field] The present invention relates to waste treatment equipment for treating industrial waste, and particularly to waste treatment equipment that enables simultaneous treatment of waste oil, waste liquid, and waste gas containing toxic trace components. [Prior art] Generally, waste liquids, gases, and
Industrial waste such as waste oil needs to be treated to eliminate pollution. To give an example of these industrial wastes, waste gas contains trace amounts of gas-phase harmful substances such as acetic acid,
Hydrogen cyanide, light hydrocarbons, etc. from a few ppm
LHV50 to 150Kcal/N containing about 5vol%
m 3 of gas. In addition, the waste liquid is an aqueous solution containing the above-mentioned harmful substances in the liquid phase, and is LHV30 to 70Kcal/Kg.
liquid. In addition, waste oil is an organic aqueous solution containing heavy hydrocarbons, with a concentration of LHV4000 to
It is a 6000Kcal/Kg liquid and acts as an auxiliary fuel. In order to treat such waste, a combustion temperature of 800℃ to 1000℃ is required.
Moreover, the residence time in the incinerator is required to be 2 to 3 seconds. For this reason, conventionally, as shown in FIG. 2, waste oil 1, waste liquid 2, and waste gas 3 are supplied to an incinerator 4, and in order to maintain the incineration temperature, auxiliary fuel 5 is burned by a burner 6. It's heating up inside. Additionally, a matrix wall 7 made of refractory bricks is installed to promote combustion within the furnace. Air 8 is supplied into the incinerator 4 by a forced air blower 9, but in addition to the combustion of waste oil 1, waste liquid 2, and waste gas 3, which are the main processing products, it is also supplied to a burner 6 for combustion of auxiliary fuel 5. will also be supplied. For example, as shown in Table 1 below
上述した従来の廃棄物処理設備においては、処
理物の特性に相応した適性のある処理方法につい
ては配慮されておらず、単に燃焼処理をすること
にのみ主眼がおかれていた。このため燃焼効率不
足、助燃料５の増加、燃焼空気８の量の増加など
の問題があり、また、触媒利用率の悪さ、さらに
は焼却炉４、熱回収部１０煙突１１が大型化する
欠点があつた。
本考案は上記事情に鑑みてなされたものであ
り、焼却効率がよく安定した運転が可能な小型の
廃棄物処理設備を提供することを目的とする。
〔問題点を解決するための手段〕
本考案は上記の目的を達成するために、有毒成
分を含有する廃油、廃液、廃ガスの産業廃棄物を
処理する廃棄物処理設備において、前記廃油に点
火するバーナと、この点火された廃油を燃焼する
焼却炉と、前記廃油が焼却されて発生した燃焼ガ
スと前記廃液及び廃ガスとを直接混合する混合部
と、この混合部で混合された混合ガスを完全焼却
する触媒酸化塔と、この完全焼却された混合ガス
を冷却する熱回収部と、この冷却された混合ガス
を外気中に排出する煙突と、前記バーナに空気及
び助燃料を供給する手段とによつて廃棄物処理設
備を構成したものである。
〔作 用〕
上記の構成によると、小形の廃油専用の焼却炉
で廃油を焼却することにより高温の燃焼ガスを発
生する。この燃焼ガスを予熱熱量源として混合部
において廃液、廃ガスと直接混合することによ
り、触媒酸化塔へ供給するに充分な高温の予熱処
理された混合ガスを発生する。また、前記廃液及
び廃ガスとの直接混合により、全体が均一に混合
され。さらにこの予熱処理された混合ガスは、押
込通風機によつて供給された処理物の可燃分を酸
化するに十分かつ最小限の酸素を過剰空気として
含有している。この混合ガスは燃焼触媒が充填さ
れた触媒酸化塔によつて完全酸化され、酸化後に
は有毒物は数ppmまで低減される。この際、触媒
酸化塔に導入される前記廃油の燃焼ガスと、前記
廃液及び廃ガスとの混合ガスは、前記の如く充分
に均一に混合されているため、触媒全面が有効に
利用され、触媒の利用率が高まる。不均一である
とホツトスポツトができて部分的に劣化して触媒
全面が活かされない。このようにして予熱処理さ
れた混合ガスは、燃焼触媒の特性である低温で低
O2酸化反応促進作用により、触媒酸化塔によつ
て焼却炉と同等以上の焼却効率を上げることがで
きる。この結果処理物の完全燃焼、助燃料の低
減、空気量の低減を達成することができる。
〔実施例〕
以下、本考案に係る廃棄物処理設備の一実施例
を図面を参照して説明する。
第１図に本考案の一実施例を示す。この図にお
いて第２図に示す従来例と同一または同等部分に
は同一符号を付して示し、説明を省略する。廃油
専用に燃焼する小形の焼却炉１４に設けられたバ
ーナ６には、廃油１、助燃料５及び空気８をそれ
ぞれ供給する配管１５，１６，１７が接続されて
いる。この焼却炉１４と熱回収部１０とを結ぶダ
クト１８には触媒酸化塔１９が設けられており、
焼却炉１４と触媒酸化塔１９との間のダクト１８
には廃液２及び廃ガス３を導入する導入口２０が
設けられている。触媒酸化塔１９には微量可燃物
の酸化反応促進部材としての公知の燃焼触媒が充
填されている。
次に本実施例の作用を説明する。廃油１は発熱
量が約10000Kcal／Kgと大きいため、バーナ６に
よつて自然し焼却炉１２内にて単独に燃焼する。
このとき燃焼に必要な空気は、他の処理物、すな
わち廃液２及び廃ガス３を燃焼するに必要な十分
な量が押込通風機９により供給される。焼却炉１
２内では廃ガス１の燃焼生成ガスは1200℃乃至
1400℃程度の高温となり、混合部１８において前
記廃液２の蒸発潜熱と廃液ガス及び廃ガス３の加
熱顕熱を供給する。このとき従来は廃液の蒸発・
燃焼のために極めて高温まで加熱しなければなら
なかつたが、本実施例では蒸発に必要な温度まで
加熱すればよい。
混合部１８で混合されたガスは、それぞれに含
有された微量の有毒物を酸化処理するために触媒
酸化塔１９に供給され、燃焼触媒の酸化反応促進
作用によつて完全燃焼される。このため従来800
℃乃至900℃の燃焼温度が必要であつたものが、
400℃乃至600℃の酸化温度で十分となる。触媒酸
化塔を出た排ガスはその顕熱を回収するために熱
回収部１０に入る。この熱回収部１０における排
ガスの温度は、従来は800℃乃至1000℃であつた
ものが、本実施例では400℃乃至600℃と低温とな
る。この結果設備的にも技術的にも熱回収を容易
に達成することができる。そして熱回収部１０を
出た排ガスは煙突１１から完全に無公害化されて
大気中へ放出される。
本実施例によれば、例えば第１表に示す処理物
の完全燃焼に必要な助燃料５及び空気８の量は、
第３図に示すように従来は燃焼温度900℃におい
て、助燃料５は520Kg／ｈ、空気８は8900Nm3／
ｈであつたものが、本実施例では燃焼温度500℃
で同等以上の燃焼効率の達成が可能であり、かつ
助燃料５は110Kg／ｈ、空気は3900Nm3／ｈと、
これらの量を著しく低減することができる。
〔考案の効果〕
上述したように本考案によれば、廃油と、廃液
と、廃ガスとを同時に一括処理することができ
る。また、廃油の燃焼ガスと、廃液及び廃ガスと
を直接混合するため、これら三者が充分に均一に
混合され、触媒の利用効率を高めることができ
る。更に、廃棄物処理設備に廃油燃焼用の焼却炉
と、混合ガスを完全燃焼するための触媒酸化塔を
設けたので、使用する助燃料と空気を低減し、小
型の設備で燃焼効率を向上させることができ、廃
棄物中の微量有害物を完全に除去することができ
る。
In the above-mentioned conventional waste treatment equipment, consideration has not been given to an appropriate treatment method corresponding to the characteristics of the material to be treated, and the main focus has been solely on combustion treatment. For this reason, there are problems such as insufficient combustion efficiency, an increase in the amount of auxiliary fuel 5, and an increase in the amount of combustion air 8, as well as a disadvantage that the catalyst utilization rate is poor and the incinerator 4, heat recovery section 10, and chimney 11 are enlarged. It was hot. The present invention was made in view of the above circumstances, and an object of the present invention is to provide a small-sized waste treatment facility that has high incineration efficiency and is capable of stable operation. [Means for Solving the Problems] In order to achieve the above object, the present invention is designed to ignite the waste oil in a waste treatment facility that processes industrial waste such as waste oil, waste liquid, and waste gas containing toxic components. an incinerator that burns the ignited waste oil; a mixing section that directly mixes the combustion gas generated by incinerating the waste oil with the waste liquid and waste gas; and a mixed gas mixed in the mixing section. a catalytic oxidation tower for completely incinerating the gas, a heat recovery section for cooling the completely incinerated mixed gas, a chimney for discharging the cooled mixed gas into the outside air, and a means for supplying air and auxiliary fuel to the burner. The waste treatment equipment is constructed by: [Function] According to the above configuration, high-temperature combustion gas is generated by incinerating waste oil in a small incinerator dedicated to waste oil. This combustion gas is used as a preheating heat source and is directly mixed with waste liquid and waste gas in the mixing section to generate a preheated mixed gas at a high enough temperature to be supplied to the catalytic oxidation tower. In addition, by directly mixing the waste liquid and waste gas, the entire mixture is uniformly mixed. Furthermore, this preheated gas mixture contains sufficient and minimal oxygen as excess air to oxidize the combustible material supplied by the forced draft fan. This mixed gas is completely oxidized by a catalytic oxidation tower filled with a combustion catalyst, and after oxidation, toxic substances are reduced to several ppm. At this time, since the combustion gas of the waste oil introduced into the catalytic oxidation tower and the mixed gas of the waste liquid and waste gas are sufficiently and uniformly mixed as described above, the entire surface of the catalyst is effectively utilized, and the catalyst usage rate will increase. If the catalyst is non-uniform, hot spots may be formed, resulting in partial deterioration and the entire surface of the catalyst not being utilized. The mixed gas that has been preheated in this way has a low temperature and low
By promoting the O 2 oxidation reaction, the catalytic oxidation tower can increase the incineration efficiency to be equal to or higher than that of an incinerator. As a result, complete combustion of the processed material, reduction of auxiliary fuel, and reduction of air amount can be achieved. [Example] Hereinafter, an example of the waste treatment equipment according to the present invention will be described with reference to the drawings. FIG. 1 shows an embodiment of the present invention. In this figure, the same or equivalent parts as in the conventional example shown in FIG. 2 are designated by the same reference numerals, and the explanation thereof will be omitted. Pipes 15, 16, and 17 for supplying waste oil 1, auxiliary fuel 5, and air 8, respectively, are connected to a burner 6 provided in a small incinerator 14 that burns waste oil exclusively. A catalytic oxidation tower 19 is provided in the duct 18 connecting the incinerator 14 and the heat recovery section 10.
Duct 18 between incinerator 14 and catalytic oxidation tower 19
is provided with an inlet 20 for introducing waste liquid 2 and waste gas 3. The catalytic oxidation tower 19 is filled with a known combustion catalyst as a member for promoting the oxidation reaction of trace amounts of combustible substances. Next, the operation of this embodiment will be explained. Since the waste oil 1 has a large calorific value of about 10,000 Kcal/Kg, it is decomposed by the burner 6 and burned independently in the incinerator 12.
At this time, air necessary for combustion is supplied by the forced draft fan 9 in an amount sufficient to burn the other processed materials, that is, the waste liquid 2 and the waste gas 3. Incinerator 1
In 2, the combustion generated gas of waste gas 1 is 1200℃~
The temperature reaches a high temperature of about 1400° C., and the latent heat of vaporization of the waste liquid 2 and the sensible heat of heating of the waste liquid gas and the waste gas 3 are supplied to the mixing section 18. At this time, conventionally the waste liquid was evaporated and
Although it was necessary to heat the material to an extremely high temperature for combustion, in this example, it is sufficient to heat it to the temperature required for evaporation. The gases mixed in the mixing section 18 are supplied to a catalytic oxidation tower 19 to oxidize trace amounts of toxic substances contained in each gas, and are completely combusted by the oxidation reaction promoting action of the combustion catalyst. Therefore, conventionally 800
Those that required a combustion temperature of ℃ to 900℃,
An oxidation temperature of 400°C to 600°C is sufficient. The exhaust gas leaving the catalytic oxidation tower enters a heat recovery section 10 to recover its sensible heat. The temperature of the exhaust gas in the heat recovery section 10 was conventionally 800°C to 1000°C, but in this embodiment it is as low as 400°C to 600°C. As a result, heat recovery can be easily achieved both in terms of equipment and technology. The exhaust gas leaving the heat recovery section 10 is completely made pollution-free and released into the atmosphere from the chimney 11. According to this embodiment, the amounts of auxiliary fuel 5 and air 8 required for complete combustion of the treated material shown in Table 1 are as follows:
As shown in Figure 3, conventionally, at a combustion temperature of 900°C, auxiliary fuel 5 was 520 kg/h and air 8 was 8900 Nm 3 /h.
In this example, the combustion temperature is 500°C.
It is possible to achieve the same or higher combustion efficiency with auxiliary fuel 5, 110Kg/h for auxiliary fuel 5, and 3900Nm 3 /h for air.
These amounts can be significantly reduced. [Effects of the Invention] As described above, according to the present invention, waste oil, waste liquid, and waste gas can be treated all at once. Further, since the combustion gas of the waste oil, the waste liquid, and the waste gas are directly mixed, these three components are mixed sufficiently and uniformly, and the efficiency of catalyst utilization can be increased. Furthermore, the waste treatment facility is equipped with an incinerator for burning waste oil and a catalytic oxidation tower for complete combustion of mixed gas, reducing the amount of auxiliary fuel and air used and improving combustion efficiency with compact equipment. It is possible to completely remove trace amounts of hazardous substances from waste.
第１図は本考案に係る廃棄物処理設備の一実施
例を示すフロー図、第２図は従来の廃棄物処理設
備のフロー図、第３図は助燃料と空気のそれぞれ
の流量と燃焼温度との関係を示すグラフである。
１……廃油、２……廃液、３……廃ガス、５…
…助燃料、６……バーナ、８……空気、９……押
込送風機、１０……熱回収部、１１……煙突、１
３……制御弁、１４……焼却炉、１８……混合
部、１９……触媒酸化塔。
Figure 1 is a flow diagram showing an embodiment of the waste treatment equipment according to the present invention, Figure 2 is a flow diagram of a conventional waste treatment equipment, and Figure 3 is the flow rate and combustion temperature of each of the auxiliary fuel and air. It is a graph showing the relationship between 1...Waste oil, 2...Waste liquid, 3...Waste gas, 5...
... Auxiliary fuel, 6 ... Burner, 8 ... Air, 9 ... Forced blower, 10 ... Heat recovery section, 11 ... Chimney, 1
3... Control valve, 14... Incinerator, 18... Mixing section, 19... Catalytic oxidation tower.
Claims (1)
業廃棄物を処理する廃棄物処理設備において、
前記廃油に点火するバーナと、この点火された
廃油を燃焼する焼却炉と、前記廃油が焼却され
て発生した燃焼ガスと前記廃液及び廃ガスとを
直接混合する混合部と、この混合部で混合され
た混合ガスを完全燃焼する触媒酸化塔と、この
完全焼却された混合ガスを冷却する熱回収部
と、この冷却された混合ガスを外気中に排出す
る煙突と、前記バーナに空気及び助燃料を供給
する手段とを具備したことを特徴とする廃棄物
処理設備。 ２ バーナに空気を供給する手段は押込通風機で
あり、バーナに助燃料を供給する手段は焼却炉
内の温度に応じて開閉する制御弁であることを
特徴とする実用新案登録請求の範囲第１項記載
の廃棄物処理設備。[Scope of claim for utility model registration] 1. In waste treatment equipment that processes industrial waste such as waste oil, waste liquid, and waste gas containing toxic components,
a burner that ignites the waste oil; an incinerator that burns the ignited waste oil; a mixing section that directly mixes the combustion gas generated by incinerating the waste oil with the waste liquid and waste gas; a catalytic oxidation tower that completely burns the incinerated mixed gas; a heat recovery unit that cools the completely incinerated mixed gas; a chimney that discharges the cooled mixed gas into the outside air; A waste treatment facility characterized by comprising a means for supplying. 2. The scope of the utility model registration claim, characterized in that the means for supplying air to the burner is a forced draft fan, and the means for supplying auxiliary fuel to the burner is a control valve that opens and closes depending on the temperature inside the incinerator. Waste treatment equipment as described in item 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1986111858U JPH0325000Y2 (en) | 1986-07-21 | 1986-07-21 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1986111858U JPH0325000Y2 (en) | 1986-07-21 | 1986-07-21 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6317929U JPS6317929U (en) | 1988-02-05 |
| JPH0325000Y2 true JPH0325000Y2 (en) | 1991-05-30 |
Family
ID=30992175
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1986111858U Expired JPH0325000Y2 (en) | 1986-07-21 | 1986-07-21 |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0325000Y2 (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5222568A (en) * | 1975-08-14 | 1977-02-19 | Kondo Unyu Kiko Kk | Hydrocarbon gas purification apparatus using waste oils |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4840426U (en) * | 1971-09-20 | 1973-05-22 |
-
1986
- 1986-07-21 JP JP1986111858U patent/JPH0325000Y2/ja not_active Expired
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5222568A (en) * | 1975-08-14 | 1977-02-19 | Kondo Unyu Kiko Kk | Hydrocarbon gas purification apparatus using waste oils |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6317929U (en) | 1988-02-05 |
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