JP4051329B2 - Waste gasification and melting treatment method - Google Patents
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- 238000002844 melting Methods 0.000 title claims description 82
- 230000008018 melting Effects 0.000 title claims description 82
- 239000002699 waste material Substances 0.000 title claims description 65
- 238000002309 gasification Methods 0.000 title claims description 48
- 238000000034 method Methods 0.000 title claims description 29
- 238000002485 combustion reaction Methods 0.000 claims description 79
- 239000007789 gas Substances 0.000 claims description 43
- 239000000428 dust Substances 0.000 claims description 37
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 32
- 239000000463 material Substances 0.000 claims description 32
- 239000001301 oxygen Substances 0.000 claims description 32
- 229910052760 oxygen Inorganic materials 0.000 claims description 32
- 238000000197 pyrolysis Methods 0.000 claims description 29
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 22
- 238000002407 reforming Methods 0.000 claims description 13
- 229910052742 iron Inorganic materials 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 8
- 229910052782 aluminium Inorganic materials 0.000 claims description 7
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 7
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- 238000009835 boiling Methods 0.000 claims description 5
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- 239000007788 liquid Substances 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 239000010849 combustible waste Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 150000002739 metals Chemical class 0.000 claims description 3
- 238000010309 melting process Methods 0.000 claims description 2
- 238000003672 processing method Methods 0.000 claims 2
- 230000003197 catalytic effect Effects 0.000 claims 1
- 239000000571 coke Substances 0.000 description 26
- 239000000155 melt Substances 0.000 description 9
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- 238000004140 cleaning Methods 0.000 description 2
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
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- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Description
本発明は、一般廃棄物、産業廃棄物、又はそれらとそれらを乾燥、焼却、破砕処理等によって得られた処理物（焼却灰やそれを一度埋め立て処理後、再度掘り起こした土砂分を含む埋め立てごみ）や汚泥等の廃棄物の処理方法に関し、特にシャフト炉式ガス化炉で燃焼・熔融処理するに際し、そのガス化効率を向上させ、操業コストの低減を図った廃棄物ガス化溶融方法に関する。 The present invention relates to general waste, industrial waste, or processed materials obtained by drying, incineration, crushing, etc. (incinerated ash and landfill waste containing earth and sand that has been dug up again after it has been landfilled once) In particular, the present invention relates to a waste gasification and melting method for improving the gasification efficiency and reducing the operation cost when burning and melting in a shaft furnace type gasification furnace.
廃棄物の処理方式として、焼却炉方式があるが、焼却方式では焼却灰の処分場を必要とする等の欠点がある。特に、大都市圏では焼却灰の処分場の確保が困難である。そのため、廃棄物を焼却炉で焼却した後の焼却灰を溶融して減容化する方法、又は、廃棄物を直接溶融し、スラグとして再資源化する方法の必要性が高まってきた。 There is an incinerator method as a waste treatment method, but the incineration method has drawbacks such as requiring an incineration ash disposal site. In particular, it is difficult to secure an incineration ash disposal site in metropolitan areas. Therefore, the necessity of a method for melting and reducing the volume of incineration ash after incineration of waste in an incinerator, or a method for directly melting waste and recycling it as slag has increased.
廃棄物を直接溶融する方法としては、例えば、シャフト炉式廃棄物溶融炉がある（特許文献１参照）。これは図２に示すように、炉本体１ｃは、シャフト部１ａと下部の朝顔部５とからなり、朝顔部５の下端には燃焼溶融帯用の下段羽口２を設けると共に、その上方には熱分解帯用の複数段の上段羽口３を有している。 As a method for directly melting the waste, for example, there is a shaft furnace type waste melting furnace (see Patent Document 1). As shown in FIG. 2, the furnace body 1c is composed of a shaft portion 1a and a lower morning glory portion 5. A lower tuyere 2 for a combustion melting zone is provided at the lower end of the morning glory portion 5 and above it. Has a plurality of upper tuyere 3 for the pyrolysis zone.
下段羽口２からは酸素または酸素を富化した空気を供給し、上段羽口３からは燃焼支持ガスとして空気を供給している。 The lower tuyere 2 supplies oxygen or oxygen-enriched air, and the upper tuyere 3 supplies air as a combustion support gas.
炉本体の上部には処理対象となる廃棄物や助燃剤としてのコークス、塩基度調整剤としての石灰石等を炉内に装入する装入口１１が設けられ、炉本体下端部には廃棄物を溶融処理した後のスラグ１８の出滓口１９が設けられている。
The upper part of the furnace body is provided with an
上記構成にあって、装入された廃棄物１ｂは、溶融炉本体１ｃの上層から乾燥帯６、熱分解帯７、燃焼溶融帯８を経過して溶融処理される。
In the above configuration, the
下段羽口２から供給した酸素又は酸素富化空気によってコークス４や熱分解残渣１４を高温で燃焼し、溶融熱源とし、一方、上段羽口３からは空気を供給して主に廃棄物の熱分解残渣１４を燃焼し、発生したガスで廃棄物の乾燥及び熱分解を行う。溶融した廃棄物はスラグ１８として出滓口１９より排出される。
The
高温の燃焼排ガスは、溶融炉内の廃棄物の充填層を対向流として上昇させ、溶融炉本体上部の排ガス管１２から可燃ガスとしてガス洗浄工程を経て回収するか、又は、燃焼室へ供給される。燃焼室には空気供給管を介して燃焼用空気が供給され、室内で燃焼される。燃焼排ガスは、排ガス管を通ってボイラーへ導入され、排熱を回収された後、減温塔で温度を調整して集塵機に通し、更には、触媒反応塔で公害物質を除去した後、煙突から排出される。
The high-temperature combustion exhaust gas is raised as a counterflow through the waste packed bed in the melting furnace, and is recovered as a combustible gas from the
その際、燃料源となるコークスを出来るだけ少なくして被処理物を効率よく燃焼熔融せしめるための手段として、炉頂から排出した可燃性ダスト（チャー）を除じん装置により捕集し、再度熔融炉本体へ羽口を介して装入する方法（特許文献２、３参照）、また、廃プラスチックを破砕し、同じく羽口から又は大きなものは炉頃から装入する方法（特許文献４参照）等がある。吹込むものは、捕集ダストや廃プラスチックだけでなく、一般廃棄物のＲＤＦ燃料等の破砕可燃物でもよい。
前記特許文献に記載されている捕集したチャーや廃プラスチック等の微細な可燃性廃棄物又はその中間処理物を、羽口を介して炉本体内へ吹き込んだ場合に次の問題点があった。 There was the following problem when fine combustible waste such as collected char and waste plastic described in the patent document or an intermediate treatment product thereof was blown into the furnace body through the tuyere. .
ダストを吹き込む時、吹込ダスト量が比較的少ない場合には、炉内温度は高く、ダストの粒子径はコークスに比べて十分小さく比表面積が大きいため燃焼速度は速く、コークス消耗を抑えることに寄与する。 When blowing dust, if the amount of dust blown is relatively small, the furnace temperature is high, the particle size of the dust is sufficiently small compared to coke, and the specific surface area is large, so the combustion speed is fast and contributes to reducing coke consumption. To do.
しかしながら、吹込ダストの量をさらに増加し、さらにコークスの消耗を抑えようとすると、常温で吹き込まれるダストは固体の初期昇温のためにコークスベッドから顕熱を奪うため、温度が低下してコークスベッドは十分な温度を維持できなくなるので、これを運転継続するためには、酸素富化量をアップし酸素濃度をあげる必要があり、コークスは吹込むダスト熱量相当の削減ができないだけでなく、コークスと酸素富化量の総合的なエネルギ一削減が達成できず十分な効果が得られない。また、酸素富化量をアップし酸素濃度を上げない場合は、溶融物の温度も低下し、融点の高いメタル分の溶融が不完全となり運転継続も困難となるので、ダスト吹込によるコークスの削減は限界が生じる。 However, when the amount of blown dust is further increased and the consumption of coke is further suppressed, the dust blown at room temperature takes sensible heat from the coke bed for the initial temperature rise of the solid, so the temperature decreases and the coke is reduced. Since the bed cannot maintain a sufficient temperature, in order to continue this operation, it is necessary to increase the oxygen enrichment amount and raise the oxygen concentration, and not only can the coke not reduce the amount of dust heat blown in, The total energy reduction of coke and oxygen enrichment cannot be achieved and sufficient effects cannot be obtained. In addition, if the oxygen enrichment is increased and the oxygen concentration is not increased, the temperature of the melt will also decrease, and the melting of the high melting point metal will be incomplete, making it difficult to continue operation. There is a limit.
そこで、本発明は、廃棄物の処理において、廃棄物の保有する熱量で廃棄物のガス化と溶融を行うことができ、且つ金属を溶融することなく有価物として回収できる廃棄物ガス化溶融処理方法を提供するものである。 Accordingly, the present invention provides a waste gasification and melting process that can perform waste gasification and melting with the amount of heat retained by the waste and that can be recovered as a valuable material without melting the metal. A method is provided.
本発明は、廃棄物をシャフト炉式ガス化炉でガス化処理し、炉底部より熱分解残渣を排出する廃棄物ガス化溶融処理方法において、
前記シャフト炉式ガス化炉に紛状可燃物の燃焼滞留時間を０．５秒以上確保した空間を有する燃焼溶融炉を連設し、該燃焼溶融炉の炉底部と前記シャフト炉式ガス化炉の炉底部とを連通せしめ、前記シャフト炉式ガス化炉の炉底部より熱分解残渣冷却排出装置で１５０℃以下に冷却し排出された熱分解残渣から溶融していない金属類を除去後、破砕した粉状物を前記燃焼溶融炉に配置した粉状可燃物吹き込み用バーナから前記燃焼溶融炉に旋回させながら吹き込んで、空気比０．７〜１で燃焼・溶融し、生成された高温可燃性ガスを燃焼溶融炉の炉底部からシャフト炉式ガス化炉の炉底部に排気し、熱分解帯へ導入して乾燥・熱分解用の熱源とすることを特徴とする。
The present invention is a waste gasification and melting treatment method in which waste is gasified in a shaft furnace type gasification furnace, and pyrolysis residues are discharged from the bottom of the furnace.
A combustion melting furnace having a space in which the combustion residence time of the powdered combustible material is secured for 0.5 seconds or more is connected to the shaft furnace type gasification furnace, and the bottom of the combustion melting furnace and the shaft furnace type gasification furnace The bottom of the shaft furnace type gasification furnace is communicated with the bottom of the shaft furnace type gasification furnace and cooled to 150 ° C. or lower with a pyrolysis residue cooling / discharging device to remove unmelted metals from the pyrolysis residue and then crushed. The powdered combustible material is blown into the combustion melting furnace while swirling from the burner for injecting powdered combustible material disposed in the combustion melting furnace, and combusted and melted at an air ratio of 0.7 to 1 to produce a high temperature combustible material. The gas is exhausted from the bottom of the combustion melting furnace to the bottom of the shaft furnace type gasifier, and introduced into the thermal decomposition zone to serve as a heat source for drying and pyrolysis.
本発明は、廃棄物をガス化するシャフト炉式ガス化炉に連設した燃焼溶融炉で粉状可燃物を燃焼させることにより、コークスを用いることなく廃棄物中の灰分の溶融を行うことができる。また、廃棄物中の鉄分、アルミ等の有価金属を酸化燃焼しないので有価物として回収可能となる。 The present invention is capable of melting ash in waste without using coke by burning powder combustibles in a combustion melting furnace connected to a shaft furnace type gasification furnace for gasifying waste. it can. In addition, valuable metals such as iron and aluminum in the waste are not oxidized and burned, and can be recovered as valuable materials.
また、本発明では、微細な可燃廃棄物及びその中間処理物を併せて処理することができる。 Moreover, in this invention, a fine combustible waste and its intermediate process thing can be processed collectively.
また、燃焼溶融炉で還元燃焼する場合、溶融物中の重金属が、還元ガスとの接触時間が長く取れるので十分還元揮発され、溶融物を再資源化する際に問題となる重金属の含有割合を低減することができる。 Also, when reducing combustion in a combustion melting furnace, the heavy metal in the melt is sufficiently reduced and volatilized because the contact time with the reducing gas can be long, and the content ratio of heavy metal that becomes a problem when recycling the melt is increased. Can be reduced.
本発明の廃棄物ガス化溶融処理方法で使用する燃焼溶融炉では、従来の廃棄物溶融炉のコークスベッドへの吹込と異なり、必要な燃焼空間を確保することで、ダストの燃焼が維持される。ダストの理論燃焼空気に対し空気比１以上で燃焼する場合、酸素がほぼ消失する空間を確保し、燃焼ガス温度が最高に達したところで、シャフト炉式ガス化炉の炉底部へ燃焼ガスを導入する。ダスト中の灰分はダストの燃焼により溶融し、旋回による遠心力で壁面に捕捉され燃焼溶融炉の炉底部より排出される。 In the combustion melting furnace used in the waste gasification melting treatment method of the present invention, the dust combustion is maintained by ensuring the necessary combustion space, unlike the conventional waste melting furnace blowing into the coke bed. . When combustion is performed at an air ratio of 1 or more with respect to the theoretical combustion air of dust, a space where oxygen is almost lost is secured, and when the combustion gas temperature reaches the maximum, the combustion gas is introduced into the bottom of the shaft furnace type gasifier. To do. The ash content in the dust is melted by the combustion of the dust, captured on the wall surface by centrifugal force due to swirling, and discharged from the bottom of the combustion melting furnace.
空気比１以上で運転すると、シャフト炉式ガス化炉の炉底部に導入する排ガスは酸素が残存し、高温の酸素含有ガスで炉底部廃棄物を燃焼し、熱分解・乾燥用の熱源となるが、燃焼による局部高温と熱分解残渣の灰化により、半溶融固着が懸念されるので極力酸素は残存させないのが望ましい。 When operating at an air ratio of 1 or more, oxygen remains in the exhaust gas introduced to the bottom of the shaft furnace type gasifier, and the waste at the bottom of the furnace is burned with a high-temperature oxygen-containing gas, which becomes a heat source for pyrolysis and drying. However, it is desirable not to leave oxygen as much as possible because there is a concern of semi-molten fixation due to local high temperature due to combustion and ashing of the pyrolysis residue.
また、本発明における燃焼溶融炉には、従来のコークスベッドへの吹込と異なり、ダスト以外のコークスや廃棄物が存在しないため、ダストと共に燃焼溶融炉に供給する酸素はダストの燃焼のみに利用される。また、供給酸素は流量計により、ダストは重量計や切出容積により計量すれば、空気比の厳密な制御が容易に可能となる。さらに、燃焼部に温度計やガス分析計を設置すれば、燃焼状態も監視可能となり、より厳密な制御も可能となる。 Also, in the combustion melting furnace in the present invention, unlike conventional coke bed blowing, since coke and waste other than dust do not exist, oxygen supplied to the combustion melting furnace together with dust is used only for dust combustion. The Further, if the supplied oxygen is measured by a flow meter and the dust is measured by a weight meter or a cut-out volume, the air ratio can be easily controlled precisely. Further, if a thermometer or a gas analyzer is installed in the combustion section, the combustion state can be monitored, and more precise control is possible.
ダストの理論燃焼空気に対し空気比１未満で還元燃焼する場合、ダストが燃焼し、さらに、ＣＯ２＋Ｃ→２ＣＯに代表されるガス化反応がほぼ完了する空間を確保し、ダストがほぼガス化したところで、溶融物の保熱部に燃焼ガスを導入し保熱、及び溶融物中の重金属の還元揮発を行う。還元燃焼の場合、滞留時間の確保、燃焼温度の確保のため、高濃度酸素を富化することが有効である。 When reducing combustion is performed at an air ratio of less than 1 against the theoretical combustion air of dust, the dust is combusted, and furthermore, a space for completing the gasification reaction represented by CO 2 + C → 2CO is secured, and the dust is almost gasified. Then, combustion gas is introduce | transduced into the heat retention part of a melt, heat retention, and the reduction volatilization of the heavy metal in a melt are performed. In the case of reductive combustion, it is effective to enrich high-concentration oxygen in order to ensure residence time and combustion temperature.
また、燃焼溶融炉へ供給する粉状可燃物は、シャフト炉式ガス化炉の炉底部より排出される熱分解残渣のほかに、捕集ダスト、廃プラスチック、一般廃棄物のＲＤＦ燃料等の破砕可燃物を添加しても良い。 In addition to the pyrolysis residue discharged from the bottom of the shaft furnace type gasifier, the powdered combustible material supplied to the combustion melting furnace is crushed, such as collected dust, waste plastic, and general waste RDF fuel. Combustible materials may be added.
鉄分を磁選除去、アルミ分を金属選別回収しマテリアルリサイクルするだけでなく鉄分を溶融対象としないので、燃焼溶融炉の運転温度を１３００℃程度の低温にすることが可能となる。 Since not only the iron content is removed by magnetic separation, the aluminum content is separated and recovered by metal and the material is recycled, but the iron content is not targeted for melting, the operating temperature of the combustion melting furnace can be lowered to about 1300 ° C.
その後、鉄分、アルミ分を回収後の熱分解残渣を破砕し、燃焼溶融部に供給する。また、破砕前に篩いを設け、ガラ分を除去し有価物として再利用することも可能である。 Thereafter, the pyrolysis residue after recovering the iron and aluminum components is crushed and supplied to the combustion melting section. It is also possible to provide a sieve before crushing, remove the glass, and reuse it as a valuable resource.
シャフト炉式ガス化炉の排ガスを燃料ガスとして回収する場合には、シャフト炉式ガス化炉の後段に常温常圧で液化する高沸点液状ガスを改質する改質工程を設ける。あるいはシャフト炉式ガス化炉の上部に直結しても良い。 When the exhaust gas from the shaft furnace type gasification furnace is recovered as a fuel gas, a reforming step for reforming the high boiling point liquid gas that is liquefied at normal temperature and normal pressure is provided after the shaft furnace type gasification furnace. Or you may connect directly to the upper part of a shaft furnace type gasification furnace.
排ガス中には、常温常圧で液化する高沸点液状ガスを多量に含むので、燃料ガスとして利用するには常温常圧で液化しないガスに改質することが望ましい。この改質反応は主にＣｍＨｎ＋ｍＨ２Ｏ→ｍＣＯ＋（ｍ＋ｎ／２）Ｈ２で表わされるが、吸熱反応であるので必要熱量を確保するため、適量の酸素を供給し、可燃ガスの一部を部分燃焼する。 Since the exhaust gas contains a large amount of high-boiling liquid gas that is liquefied at normal temperature and pressure, it is desirable to reform the gas to a gas that does not liquefy at normal temperature and pressure in order to use it as a fuel gas. This reforming reaction is mainly represented by CmHn + mH 2 O → mCO + (m + n / 2) H 2. However, since this is an endothermic reaction, an appropriate amount of oxygen is supplied in order to secure the necessary heat, and a part of the combustible gas is partially Burn.
水蒸気は、廃棄物中の付着水分で通常はまかなえるが、付着水分が少ない廃棄物をガス化する場合は、必要量の水蒸気を改質炉に添加する。 The water vapor is usually covered by the adhering moisture in the waste, but when gasifying the waste having a small adhering moisture, a necessary amount of water vapor is added to the reforming furnace.
また、反応温度は９００℃以上望ましくは１１００℃以上とすることが必要である。 The reaction temperature should be 900 ° C. or higher, preferably 1100 ° C. or higher.
また、改質反応を促進するために触媒を用いると５００〜９００℃望ましくは、６００〜８００℃への低温域でも改質を行うことが可能となる。 Further, when a catalyst is used to promote the reforming reaction, it is possible to perform reforming even in a low temperature range of 500 to 900 ° C., preferably 600 to 800 ° C.
触媒には、ドロマイト、ニッケル系（ニッケル−アルミナ系、ニッケル−マグネシア系）等を用いることができる。 As the catalyst, dolomite, nickel-based (nickel-alumina-based, nickel-magnesia-based), or the like can be used.
改質反応炉は、流動層式、ハニカム状やペレット状の触媒を用いた固定層式のいずれでも良い。 The reforming reactor may be either a fluidized bed type or a fixed bed type using a honeycomb or pellet type catalyst.
改質工程の後段には、ガス洗浄、冷却、圧縮を経てガスホルダーに貯留し、ガスエンジン、ガスタービンやボイラー用のガス燃料、また、燃料電池用の原料ガスとして利用する。 In the subsequent stage of the reforming process, gas cleaning, cooling and compression are performed and the gas is stored in the gas holder and used as gas fuel for gas engines, gas turbines and boilers, and as raw material gas for fuel cells.
熱分解残渣の破砕後、粉状物の一部を抜き出し、他のボイラー、製鉄用熱源として、石炭、石油、コークス、ＬＮＧ等の化石燃料の部分的な代替燃料として利用する。 After crushing the pyrolysis residue, a part of the powder is extracted and used as a partial substitute fuel for fossil fuels such as coal, petroleum, coke, and LNG as a heat source for other boilers and iron making.
実施例１
図１は本実施例のシャフト炉式ガス化炉の断面図である。
Example 1
FIG. 1 is a cross-sectional view of a shaft furnace type gasification furnace of the present embodiment.
図２に示す廃棄物溶融炉においては、炉頂より装入された廃棄物が、シャフト部１ａの乾燥帯６にて乾燥され、熱分解帯７、燃焼溶融帯８にコークスと共に降下する。熱分解帯用の上段羽口３より空気を吹込み、乾燥され一部熱分解した廃棄物を主に燃焼する。燃焼溶融帯用の下段羽口２より酸素富化した空気を吹込み、主にコークスベット４を形成するコークスと一部廃棄物の熱分解残渣１４を１５００℃以上で高温燃焼し、廃棄物中の灰分を溶融し、１４００℃以上の溶融物１８として炉底部１０に設置した出滓口１９より排出される。
In the waste melting furnace shown in FIG. 2, the waste charged from the top of the furnace is dried in the
一方、図１に示す本発明のシャフト炉式ガス化炉１においては、シャフト炉への上段羽口、下段羽口からの空気吹込み、酸素富化空気吹込みまた、コークスの供給は行なわない。
On the other hand, in the shaft furnace
シャフト炉式ガス化炉１の炉底部１０に連通する燃焼溶融炉１６に設けられた粉状可燃物吹込用バーナ１７からは、除じん装置２５で捕集した可燃ダスト２０とシャフト炉式ガス化炉から排出された熱分解残渣１４を破砕、鉄分金属分除去した炭化物と空気又は酸素富化した空気を吹込み、燃焼溶融炉１６内で燃焼溶融炉出口温度で１４００℃以上の高温燃焼を行い、その排ガスをシャフト炉式ガス化炉の炉底部１０に排気し、廃棄物の熱分解、乾燥を行いシャフト炉式ガス化炉の上部より可燃性ガスを排気し、除じん装置２５でダスト分を分離除去し、改質工程で常温常圧で液化する高沸点液状ガスを分解し、水素と一酸化炭素主体の合成ガスに変換する。
The
改質工程の温度は、酸素を供給し可燃ガスの部分燃焼を行うことで改質工程出口温度で１０００℃以上とし、水蒸気は、廃棄物中の付着水分と熱分解による生成水でまかなうので通常は添加不要であるが、改質工程出口でメタン濃度が高い場合は追添加する。
更に、従来例３で可燃ダストをｌ００Ｋｇ／ｈに増量し、その可燃ダスト中の可燃分はコークスで４０Ｋｇ／ｈ相当のため、コークス添加量１０Ｋｇ／ｈに低減しようとしたところ、炉底部のコークスベッドはコークス添加量を低減したために小さくなり、可燃ダストの固体温度を昇温する熱源が不足し、可燃ダストの燃焼遅れを助長するため、前記酸素濃度を５０％に増加しても、溶融物の温度は１４００℃以下に低下し安定溶融の継続は困難であった。これは、可燃ダスト量の増大につれ、燃焼溶融帯の最高温度は上方に移動且つ最高温度は低下するので、溶融物は滴下過程において燃焼ガスにより冷却されてしまうことが主因である。 Furthermore, the amount of combustible dust was increased to 100 kg / h in Conventional Example 3 and the combustible content in the combustible dust was equivalent to 40 kg / h of coke. The bed becomes smaller because the amount of coke added is reduced, the heat source for raising the solid temperature of the combustible dust is insufficient, and the combustion delay of the combustible dust is promoted. Therefore, even if the oxygen concentration is increased to 50%, The temperature dropped to 1400 ° C. or lower, and it was difficult to continue stable melting. This is mainly due to the fact that the maximum temperature of the combustion melting zone moves upward and the maximum temperature decreases as the amount of combustible dust increases, so that the melt is cooled by the combustion gas during the dropping process.
一方、本実施例では、粉状可燃物吹込用バーナ１７に供給する可燃ダスト及びシャフト炉式ガス化炉の排出残渣を、鉄分、金属除去後破砕した炭化物（以降粉状可燃物という）は、シャフト炉式ガス化炉の炉底部近傍に設置した燃焼溶融炉１６に空気とともに吹き込まれ、廃棄物の粉状可燃物は可燃分２５〜４５％、灰分７５〜５５％程度で揮発分も多く含まれるため、燃焼溶融炉内の耐火壁から熱輻射を受け、安定燃焼が可能となる。
On the other hand, in this embodiment, the combustible dust supplied to the
表１に示す実施例１は、粉状可燃物量に対し、ほぼ空気比１．０となるように粉状可燃物吹込用バーナから粉状可燃物吹込量と空気、酸素富化量を調節した例である。実施例１では、空気比１、酸素濃度３０％の条件のため、粉状可燃物の燃焼排ガス温度は１５００℃を超える温度で燃焼し、粉状可燃物中の灰分が溶融し、シャフト炉熱分解帯にその排ガスが導かれることで、シャフト炉上部から装入された廃棄物中の熱分解・乾燥用熱源として利用される。 In Example 1 shown in Table 1, the amount of powdered combustible material blowing, air, and oxygen enrichment were adjusted from the powdered combustible material blowing burner so that the air ratio was approximately 1.0 with respect to the amount of powdered combustible material. It is an example. In Example 1, because of the conditions of an air ratio of 1 and an oxygen concentration of 30%, the combustion exhaust gas temperature of the powdered combustible material burns at a temperature exceeding 1500 ° C., the ash content in the powdered combustible material melts, and the shaft furnace heat When the exhaust gas is guided to the decomposition zone, it is used as a heat source for thermal decomposition and drying in the waste charged from the upper part of the shaft furnace.
なお、酸素濃度２１％の空気でも空気比０．９〜１．１程度で１４００℃以上の高温燃焼が可能であり、酸素濃度３０％にすれば、空気比０．７〜１．４程度でも１４００℃以上の高温燃焼排ガスを生成することが可能である。 In addition, even with air with an oxygen concentration of 21%, high-temperature combustion at 1400 ° C. or higher is possible at an air ratio of about 0.9 to 1.1. It is possible to generate high-temperature combustion exhaust gas at 1400 ° C. or higher.
廃棄物は乾燥、熱分解され６００〜８００℃で降下し、炉底部の熱分解残渣冷却排出装置２４で大気中で発火しない１５０℃以下の温度に冷却し排出する。この熱分解残渣は熱分解前に比べ容易に破砕することができる。また、残渣中の鉄分、アルミ分は酸化されていないので有価物として分離回収可能である。鉄分、アルミ分を除去した後の炭化物は、破砕後図示しない異物篩により、１０ｍｍ以上のものを分離し１０ｍｍ以下の粉状炭化物を空気輸送により粉状可燃物吹込用バーナ１７に供給する。また、燃焼溶融炉１５の粉状可燃物吹込用バーナ１７の粉状可燃物に対する空気比が１以下の還元燃焼を行えば、高温可燃性ガスが生成されるので、粉状可燃物中の固定炭素分が容易にガス化される。
The waste is dried and pyrolyzed, falls at 600 to 800 ° C., and is cooled and discharged to a temperature of 150 ° C. or less that does not ignite in the atmosphere by the pyrolysis residue cooling and discharging
燃焼溶融炉１６での粉状可燃物の燃焼滞留時間は、０．５秒以上望ましくは１秒以上確保すれば、燃焼はほぼ完了する。また、燃焼溶融炉は旋回流燃焼が望ましく、フレームの保炎性向上、滞留時間の増大、粉状可燃物中灰分の溶融物の壁面での捕捉が可能であり、燃焼溶融炉の小型化が可能である。
If the combustion residence time of the powder combustible material in the
本発明のシャフト炉式ガス化炉では、廃棄物を溶融することなく乾燥・熱分解のみ行うので、溶融するための熱分が不要となり、燃焼溶融炉での灰分の溶融は粉状可燃物のもつ熱量で十分であり、従来の廃棄物溶融炉と比較すると、コークス添加は不要となる。 In the shaft furnace type gasification furnace of the present invention, only the drying and thermal decomposition is performed without melting the waste, so the heat for melting is unnecessary, and the melting of the ash in the combustion melting furnace is the powdery combustible material. The amount of heat it has is sufficient and no coke addition is required compared to conventional waste melting furnaces.
廃棄物の処理において、廃棄物の保有する熱量で廃棄物のガス化と溶融を行うことができ、且つ金属を溶融することなく有価物として回収できる廃棄物ガス化溶融処理に利用できる。 In the treatment of waste, the waste can be gasified and melted by the amount of heat held by the waste, and can be used for waste gasification and melting that can be recovered as a valuable material without melting the metal.
１：シャフト炉式ガス化炉
１ｃ：溶融炉本体
１ａ：シャフト部
１ｂ：廃棄物
１ｃ：溶融炉本体
２：下段羽口
３：上段羽口
４：コークス
５：朝顔部
６：乾燥帯
７：熱分解帯
８：燃焼溶融帯
１０：炉底部
１１：装入口
１２：排ガス管
１４：熱分解残渣
１５：鉄、アルミ
１６：燃焼溶融炉
１７：粉状可燃物吹込用バーナ
１８：溶融物（スラグ）
１９：出滓口
２０：可燃ダスト
２１：合成ガス
２２：酸素＋水蒸気
２３：空気＋酸素
２４：熱分解残渣冷却・排出装置
２５：除じん装置
1: Shaft furnace type gasification furnace 1c: Melting furnace body 1a:
19: Outlet 20: Combustible dust 21: Syngas 22: Oxygen + water vapor 23: Air + oxygen 24: Pyrolysis residue cooling / exhaust device 25: Dust removal device
Claims (9)
前記シャフト炉式ガス化炉に紛状可燃物の燃焼滞留時間を０．５秒以上確保した空間を有する燃焼溶融炉を連設し、該燃焼溶融炉の炉底部と前記シャフト炉式ガス化炉の炉底部とを連通せしめ、前記シャフト炉式ガス化炉の炉底部より熱分解残渣冷却排出装置で１５０℃以下に冷却し排出された熱分解残渣から溶融していない金属類を除去後、破砕した粉状物を前記燃焼溶融炉に配置した粉状可燃物吹き込み用バーナから前記燃焼溶融炉に旋回させながら吹き込んで、空気比０．７〜１で燃焼・溶融し、生成された高温可燃性ガスを燃焼溶融炉の炉底部からシャフト炉式ガス化炉の炉底部に排気し、熱分解帯へ導入して乾燥・熱分解用の熱源とすることを特徴とする廃棄物ガス化溶融処理方法。 In the waste gasification melting treatment method in which waste is gasified in a shaft furnace type gasification furnace and pyrolysis residue is discharged from the bottom of the furnace,
A combustion melting furnace having a space in which the combustion residence time of the powdered combustible material is secured for 0.5 seconds or more is connected to the shaft furnace type gasification furnace, and the bottom of the combustion melting furnace and the shaft furnace type gasification furnace The bottom of the shaft furnace type gasification furnace is communicated with the bottom of the shaft furnace type gasification furnace, cooled to 150 ° C. or lower with a pyrolysis residue cooling / discharging device, and after removal of unmelted metals from the pyrolysis residue discharged, crushing The powdered combustible material is blown into the combustion melting furnace while being swirled from the burner for injecting powdered combustible material disposed in the combustion melting furnace, burned and melted at an air ratio of 0.7 to 1, and generated high temperature combustibility A waste gasification and melting treatment method characterized in that gas is exhausted from the furnace bottom of a combustion melting furnace to the furnace bottom of a shaft furnace type gasification furnace and introduced into a thermal decomposition zone as a heat source for drying and pyrolysis .
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