JPH07232155A - Fly ash treating device - Google Patents
Fly ash treating deviceInfo
- Publication number
- JPH07232155A JPH07232155A JP6027715A JP2771594A JPH07232155A JP H07232155 A JPH07232155 A JP H07232155A JP 6027715 A JP6027715 A JP 6027715A JP 2771594 A JP2771594 A JP 2771594A JP H07232155 A JPH07232155 A JP H07232155A
- Authority
- JP
- Japan
- Prior art keywords
- fly ash
- exhaust gas
- washing
- high temperature
- secondary combustion
- 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.)
- Granted
Links
- 239000010881 fly ash Substances 0.000 title claims abstract description 46
- 238000005406 washing Methods 0.000 claims abstract description 24
- 238000002485 combustion reaction Methods 0.000 claims abstract description 22
- 238000005245 sintering Methods 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000001035 drying Methods 0.000 claims abstract description 9
- 239000000428 dust Substances 0.000 claims description 23
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 238000012545 processing Methods 0.000 claims description 5
- 239000008187 granular material Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 abstract description 12
- 230000003179 granulation Effects 0.000 abstract 2
- 238000005469 granulation Methods 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 44
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 19
- 238000000034 method Methods 0.000 description 13
- 239000002956 ash Substances 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 8
- RELMFMZEBKVZJC-UHFFFAOYSA-N 1,2,3-trichlorobenzene Chemical compound ClC1=CC=CC(Cl)=C1Cl RELMFMZEBKVZJC-UHFFFAOYSA-N 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 238000005979 thermal decomposition reaction Methods 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 239000002243 precursor Substances 0.000 description 5
- 238000007711 solidification Methods 0.000 description 5
- 230000008023 solidification Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 3
- 150000002013 dioxins Chemical class 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000002738 chelating agent Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000007908 dry granulation Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
【0001】[0001]
【産業上の利用分野】本発明は、主として都市ごみ焼却
炉から排出される飛灰の処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention mainly relates to a device for treating fly ash discharged from an incinerator for municipal solid waste.
【0002】都市ごみ焼却炉から出る飛灰中にはN
a+ 、K+ 、Ca++、Cl- 、SO4 --等の高温で揮散
しやすい物質や、ダイオキシン、重金属等の有害物質が
多量含まれている。例えば、飛灰を1300℃以上の高
温で溶融固化処理すると、上記の諸物質が排ガス中に揮
散するので、これらの物質を再度捕捉しなければなら
ず、その為の洗煙装置の設置と2次公害防止の配慮が必
要である。そのため飛灰の処理方法の技術確立が社会的
ニーズとなっている。N is present in the fly ash discharged from the municipal refuse incinerator.
It contains a large amount of substances that easily volatilize at high temperatures, such as a + , K + , Ca ++ , Cl − , SO 4 − , and harmful substances such as dioxins and heavy metals. For example, when fly ash is melted and solidified at a high temperature of 1300 ° C. or higher, the above substances volatilize into the exhaust gas, and therefore these substances must be captured again. It is necessary to consider the next pollution prevention. Therefore, the establishment of technology for fly ash treatment methods has become a social need.
【0003】[0003]
【従来の技術】飛灰中のダイオキシンを無害化処理する
方法として、図6に示すように、N2等の還元ガスの高
温雰囲気における、間接加熱による熱分解方式(ハーゲ
ンマイヤー方式)がある。2. Description of the Related Art As a method for detoxifying dioxin in fly ash, there is a thermal decomposition method (Hagenmeier method) by indirect heating in a high temperature atmosphere of a reducing gas such as N 2 as shown in FIG.
【0004】このプロセスでは、飛灰をコンベヤ(51)に
よってホッパー(52)に搬入し、ここから多数の回転羽根
(54)を内装した加熱装置(53)の始端部へ送られ、加熱さ
れる。ついで加熱飛灰は加熱装置(53)の終端部から通路
(55)を経て、スクリュー(57)を内装した冷却装置(56)の
始端部へ送られ、冷却される。ついで冷却飛灰は冷却装
置(56)の終端部から搬出車(58)へ排出される。In this process, fly ash is carried into a hopper (52) by a conveyor (51), from which a large number of rotary blades are fed.
It is sent to the start end of a heating device (53) containing (54) and heated. The heated fly ash then passes from the end of the heating device (53) to the passage.
After passing through (55), it is sent to the start end of a cooling device (56) having a screw (57) installed therein and cooled. Then, the cooling fly ash is discharged from the end portion of the cooling device (56) to the carry-out vehicle (58).
【0005】加熱装置(53)の始端部には窒素ガスボンベ
(59)から不活性ガスとして窒素ガスが導入され、ここを
通過した後、加熱装置(53)の終端部から集塵装置(60)に
送られ、ここで除塵処理される。除塵された400℃の
窒素ガスは冷却器(61)(62)で冷却された後、ブロア(63)
で加熱装置(53)の始端部へ循環され、一部は系外へ放出
される。窒素ガスの放出分の補充は加熱装置(53)の終端
部で行われる。(60)に送られ、ここで除塵処理される。A nitrogen gas cylinder is provided at the beginning of the heating device (53).
Nitrogen gas is introduced as an inert gas from (59), and after passing through it, it is sent to the dust collector (60) from the end portion of the heating device (53), where it is subjected to dust removal processing. The 400 ° C nitrogen gas from which dust has been removed is cooled by coolers (61) (62), and then blower (63)
Is circulated to the start end of the heating device (53), and part of the heat is discharged to the outside of the system. Replenishment of the released nitrogen gas is performed at the end of the heating device (53). It is sent to (60), where the dust is removed.
【0006】[0006]
【発明が解決しようとする課題】上記構成の間接加熱に
よる熱分解方式では、次のような問題がある。The above-described thermal decomposition method using indirect heating has the following problems.
【0007】伝熱面積が限定されるので、スケールア
ップが難しい。例えば、大径のキルンでは加熱面積が小
さくなり、長いキルンではスケール掻き取り用の支持棒
が垂れる。It is difficult to scale up because the heat transfer area is limited. For example, a large-diameter kiln has a small heating area, and a long kiln has a support rod for scale scraping.
【0008】加熱伝熱面でハードなスケールが発生し
易く、スケール掻き取り装置の破損が頻発する。Hard scales are easily generated on the heat transfer surface, and the scale scraping device is frequently damaged.
【0009】排出排ガス中のダイオキシン再処理が必
要である。Reprocessing of dioxins in exhaust gas is necessary.
【0010】不活性ガスの注入がコストアップを招
く。Injecting an inert gas causes an increase in cost.
【0011】200kw/(500kg飛灰)の大容
量電力を必要とする。A large capacity electric power of 200 kw / (500 kg fly ash) is required.
【0012】本発明は、上記の諸問題を解決することが
できる飛灰の処理装置を提供することを目的とする。An object of the present invention is to provide a fly ash processing apparatus which can solve the above problems.
【0013】[0013]
【課題を解決するための手段】本発明による飛灰の処理
装置は、上記目的を達成すべく工夫されたものであっ
て、飛灰を水洗する洗浄槽と、水洗後の飛灰を乾燥造粒
する乾燥造粒機と、造粒物を焼結するキルン炉とを具備
してなるものである。The apparatus for treating fly ash according to the present invention has been devised to achieve the above-mentioned object, and includes a washing tank for washing fly ash with water, and a drying process for drying fly ash after washing with water. It comprises a dry granulator for granulating and a kiln furnace for sintering the granulated material.
【0014】水洗後の排液は重金属の捕捉後、系外へ放
流される。The effluent after washing with water is discharged to the outside of the system after capturing heavy metals.
【0015】キルン炉は例えば800℃以上の酸化雰囲
気で運転される。The kiln furnace is operated, for example, in an oxidizing atmosphere at 800 ° C. or higher.
【0016】本発明による飛灰の処理装置は、好ましく
は、上記洗浄槽と乾燥造粒機とキルン炉とに加えてさら
に、排ガス中の未燃物を完全に燃焼する2次燃焼炉を具
備している。The apparatus for treating fly ash according to the present invention preferably further comprises a secondary combustion furnace for completely burning unburned materials in exhaust gas, in addition to the cleaning tank, the drying granulator and the kiln. is doing.
【0017】本発明による飛灰の処理装置は、好ましく
は、上記洗浄槽と乾燥造粒機とキルン炉と2次燃焼炉と
に加えてさらに、乾燥造粒機から出た低温排ガスと、キ
ルン炉または2次燃焼炉から出た高温排ガスとの混合ガ
スを除塵処理する集塵機を具備している。低温排ガスと
高温排ガスとの混合により、混合ガスの温度は例えば4
00〜700℃に調整される。集塵機としては例えばセ
ラミックフィルターからなるものが好ましい。The apparatus for treating fly ash according to the present invention preferably comprises, in addition to the washing tank, the dry granulator, the kiln furnace and the secondary combustion furnace, a low temperature exhaust gas discharged from the dry granulator and a kiln. It is equipped with a dust collector that removes dust from the mixed gas with the high-temperature exhaust gas discharged from the furnace or the secondary combustion furnace. By mixing the low temperature exhaust gas and the high temperature exhaust gas, the temperature of the mixed gas is, for example, 4
The temperature is adjusted to 00 to 700 ° C. The dust collector is preferably a ceramic filter, for example.
【0018】本発明による飛灰の処理装置は、好ましく
は、上記洗浄槽と乾燥造粒機とキルン炉と2次燃焼炉と
集塵機とに加えてさらに、集塵機から出た排ガスを冷却
する脱硝触媒付きガスクーラーを具備している。このガ
スクーラーにより排ガスは例えば400〜500℃に冷
却され、この冷却後、触媒層における添加NH3 による
還元脱硝によりNOxやダイオキシンが除去された後、
排ガスはさらに250〜350℃まで冷却・熱回収され
る。The apparatus for treating fly ash according to the present invention is preferably a denitrification catalyst for cooling exhaust gas from the dust collector in addition to the cleaning tank, the dry granulator, the kiln furnace, the secondary combustion furnace and the dust collector. Equipped with a gas cooler. The exhaust gas is cooled to, for example, 400 to 500 ° C. by this gas cooler, and after this cooling, NOx and dioxin are removed by reduction denitration with added NH 3 in the catalyst layer,
The exhaust gas is further cooled to 250 to 350 ° C. and heat is recovered.
【0019】本発明による飛灰の処理装置は、好ましく
は、上記洗浄槽と乾燥造粒機とキルン炉と2次燃焼炉と
集塵機と脱硝触媒付きガスクーラーとに加えてさらに、
ガスクーラーにおける熱交換により生じた高温空気を、
乾燥造粒機、キルン炉および/または2次燃焼炉の各バ
ーナへ送る熱風管路を具備している。The apparatus for treating fly ash according to the present invention preferably further comprises, in addition to the above-mentioned washing tank, drying granulator, kiln furnace, secondary combustion furnace, dust collector, and gas cooler with a denitration catalyst,
The hot air generated by heat exchange in the gas cooler,
It is equipped with a hot air duct for feeding to each burner of a dry granulator, a kiln furnace and / or a secondary combustion furnace.
【0020】[0020]
(1) 洗浄槽で飛灰を水洗し、乾燥造粒機で乾燥造粒し、
キルン炉で造粒物を焼結し、場合によっては2次燃焼炉
でさらに加熱することにより、飛灰中に含まれるNa、
K、Ca、Cl、SO3 等を除去することができる。上
記水洗による除去率はNa、K、Cl、SO4 について
は70〜90%である。その分析値一例を表1に示す。(1) Fly ash is washed with water in a washing tank, dried and granulated with a dry granulator,
By sintering the granulated product in a kiln furnace and optionally further heating it in a secondary combustion furnace, Na contained in fly ash,
It is possible to remove K, Ca, Cl, SO 3, etc. The removal rate by washing with water is 70 to 90% for Na, K, Cl and SO 4 . Table 1 shows an example of the analysis value.
【0021】(2) 上記水洗により飛灰の焼結温度が高温
側に移行し、高温処理時の固結および上記Na+ 、
K+ 、Ca++、Cl- 、SO4 --等の揮散が防止でき
る。水洗を行わない場合には、焼結は400℃から始ま
り、600℃で最高強度を持つ焼結物が得られる。水洗
による焼結点の移行の結果、焼結は600℃から始ま
り、最大強度もかなり小さいものとなる。飛灰の焼結強
度の一例を図2に示す。(2) The above-mentioned washing with water shifts the sintering temperature of fly ash to the high temperature side, and solidification during the high temperature treatment and the above Na + ,
It is possible to prevent volatilization of K + , Ca ++ , Cl − , SO 4 − and the like. Without washing with water, sintering begins at 400 ° C and at 600 ° C a sintered product with maximum strength is obtained. As a result of the transition of the sintering point by washing with water, the sintering starts from 600 ° C. and the maximum strength becomes considerably small. FIG. 2 shows an example of the sintering strength of fly ash.
【0022】(3) 伝熱面の限られる間接加熱方式から高
温熱風によるキルン型直接焼結方式とすることにより、
焼結による固結閉塞の問題が解決され、さらに800℃
以上の高温域での操作も可能となり、ダイオキシンの熱
分解および酸化が容易に行われる。(3) By changing from the indirect heating method with limited heat transfer surface to the kiln type direct sintering method with high temperature hot air,
The problem of solidification blockage due to sintering was solved, and 800 ° C
Operation in the above high temperature range is also possible, and thermal decomposition and oxidation of dioxin can be easily performed.
【0023】(4) 飛灰の焼結処理前に乾燥造粒装置が設
けられているので、焼結後の灰分は粒状となり、焼結時
の粉塵飛散を抑制しかつ排出灰のハンドリングを容易に
することができる。(4) Since the dry granulation device is provided before the sintering process of fly ash, the ash content after sintering becomes granular, which suppresses dust scattering during sintering and facilitates handling of discharged ash. Can be
【0024】(5) 集塵機でキルン炉または2次燃焼炉か
ら出た高温排ガスを除塵するとともに、高温雰囲気にお
けるフィルター表面上で、CO、灰中の未燃カーボン、
ダイオキシンの前駆物質(例えばトリクロロベンゼン)
等が酸化分解され、排出ガスを極めてクリーンな排ガス
とすることができる。(5) The dust collector removes high-temperature exhaust gas from the kiln furnace or the secondary combustion furnace, and CO, unburned carbon in ash, on the filter surface in a high-temperature atmosphere,
Dioxin precursors (eg trichlorobenzene)
The exhaust gas can be made into an extremely clean exhaust gas.
【0025】図3は、フィルターの使用による、排ガス
中のCOの高温雰囲気における低減性能を示すものであ
る。図4は、フィルターの使用による、灰中の未燃カー
ボンの酸化および燃焼によるCO発生とカーボンの減少
をそれぞれ示すものである。図5は、フィルターの使用
による、ダイオキシン前駆物質であるトリクロロベンゼ
ン(TCB)の高温雰囲気における低減性能を示すもの
である。これらの物質はいずれも600℃の温度域でほ
ぼ完全に酸化されることが判る。なお、フィルターのな
い場合はさらに50〜100℃高温度域においてのみ上
記酸化が進むこと、および、高温反応の面でフィルター
が有効であることが判る。FIG. 3 shows the reduction performance of CO in exhaust gas in a high temperature atmosphere by using a filter. FIG. 4 shows CO generation and carbon reduction due to oxidation and combustion of unburned carbon in ash by using a filter, respectively. FIG. 5 shows the reduction performance of trichlorobenzene (TCB), which is a dioxin precursor, in a high temperature atmosphere by using a filter. It can be seen that all of these substances are almost completely oxidized in the temperature range of 600 ° C. It should be noted that, in the case where the filter is not provided, the oxidation proceeds only in the high temperature range of 50 to 100 ° C. and that the filter is effective in terms of high temperature reaction.
【0026】(6) 脱硝触媒においてアンモニアの添加に
よりNOxの還元除去とダイオキシンの分解が行われ
れ、ダイオキシンおよびNOxがいずれも除去できた。(6) NOx was reduced and removed and dioxin was decomposed by adding ammonia in the denitration catalyst, and both dioxin and NOx could be removed.
【0027】(7) この処理後の高温ガスは完全除塵され
ているので、以後250〜400℃におけるダイオキシ
ンの再発生はなく、また熱回収装置としてはクリーンガ
ス処理用のコンパクトな装置で充分な熱回収が可能であ
り、この熱分解に要するエネルギーも低消費である。(7) Since the high temperature gas after this treatment is completely removed of dust, no dioxin is regenerated at 250 to 400 ° C. thereafter, and a compact device for clean gas treatment is sufficient as a heat recovery device. It is possible to recover heat, and the energy required for this thermal decomposition is also low consumption.
【0028】[0028]
【実施例】本発明を図示の実施例により具体的に説明す
る。The present invention will be described in detail with reference to the embodiments shown in the drawings.
【0029】図1は飛灰処理プロセスの一例である。FIG. 1 is an example of a fly ash treatment process.
【0030】処理すべき飛灰は、まず、攪拌機(2) を備
えた洗浄槽(1) に投入され、ここで洗浄水にて水洗され
る。洗浄された飛灰はスラリー状態にて脱水機(3) へ送
られ、ここで脱水される。この脱水によって生じた濾液
は、攪拌機(5) を備えた混合槽(4) へ送られ、ここでキ
レート剤と混合される。キレート剤の添加により、この
液中の重金属類が沈降させられ、この沈澱物はフィルタ
ー(6) にて濾過される。該沈殿物からなるスラッジ状の
固形物の分離後、固形物はセメント固化等により処理す
る。フィルター(6) の放流水はNa+ 、K+ 、Ca++等
と、Cl- 、SO4 --等との反応塩類を含む希薄水溶液
であって、透明である。なお、この液はややpH≧8の
傾向があるので、この場合は水和処理後放流する。勿論
この中にはダイオキシンは含まれず、ダイオキシンは全
て灰分に付着している。The fly ash to be treated is first put into a washing tank (1) equipped with a stirrer (2), where it is washed with washing water. The washed fly ash is sent to the dehydrator (3) in a slurry state, where it is dehydrated. The filtrate produced by this dehydration is sent to a mixing tank (4) equipped with a stirrer (5), where it is mixed with a chelating agent. By adding the chelating agent, the heavy metals in this liquid are precipitated, and this precipitate is filtered by the filter (6). After separation of the sludge-like solid consisting of the precipitate, the solid is treated by cement solidification or the like. The water discharged from the filter (6) is a dilute aqueous solution containing reaction salts of Na + , K + , Ca ++, etc., with Cl − , SO 4 −, etc., and is transparent. Since this solution tends to have a pH of ≧ 8, in this case, it is discharged after hydration treatment. Of course, this does not include dioxin, and all dioxin is attached to the ash.
【0031】スラリー状の飛灰の脱水によって生じた脱
水汚泥は、次に乾燥造粒機(7) へ送られ、ここで乾燥、
造粒される。この熱源は、灯油タンク(8) から供給され
た灯油等のラインバーナ(8) における燃焼ガスである。
得られた造粒物はキルン炉(9) へ送られ、ここで約80
0℃の酸化雰囲気にて高温焼結され、ダイオキシン等が
分解される。キルン炉(9) の熱源はバーナ(10)にて発生
する燃焼ガスである。The dehydrated sludge produced by dehydration of the fly ash in the form of slurry is then sent to the drying granulator (7), where it is dried and
Granulated. This heat source is combustion gas in the line burner (8) such as kerosene supplied from the kerosene tank (8).
The obtained granules are sent to the kiln furnace (9), where about 80
High-temperature sintering is performed in an oxidizing atmosphere at 0 ° C. to decompose dioxins and the like. The heat source of the kiln furnace (9) is the combustion gas generated in the burner (10).
【0032】排ガス中に揮散したダイオキシンの分解に
は充分な滞留時間が必要であるので、得られた焼結物は
2次燃焼炉(10)へ送られ、ここでさらに高温下で加熱さ
れる。2次燃焼炉(11)の熱源はバーナ(12)にて発生する
燃焼排ガスである。こうして処理された飛灰は2次燃焼
炉(10)の底部から取り出される。Since sufficient residence time is required for the decomposition of dioxin volatilized in the exhaust gas, the obtained sintered product is sent to the secondary combustion furnace (10) where it is further heated at a high temperature. . The heat source of the secondary combustion furnace (11) is the combustion exhaust gas generated in the burner (12). The fly ash thus treated is taken out from the bottom of the secondary combustion furnace (10).
【0033】2次燃焼炉(11)から出た約1200℃の高
温排ガスは、乾燥造粒機(7) から出た約150℃の低温
ガスと混合させ、約600℃となる。この排ガスはセラ
ミックフィルターからなる高温集塵機(13)へ送られ、除
塵処理される。ここで得られた捕集灰は乾燥造粒機(7)
へ戻される。高温集塵機(13)のセラミックフィルター上
ではCO、灰中の未燃カーボン、ダイオキシンの前駆物
質(例:トリクロロベンゼン)等が酸化分解され、排出
ガスは極めてクリーンなガスになる。The high temperature exhaust gas of about 1200 ° C. discharged from the secondary combustion furnace (11) is mixed with the low temperature gas of about 150 ° C. discharged from the dry granulator (7) to be about 600 ° C. This exhaust gas is sent to a high temperature dust collector (13) composed of a ceramic filter and subjected to dust removal processing. The collected ash obtained here is a dry granulator (7)
Returned to. On the ceramic filter of the high temperature dust collector (13), CO, unburned carbon in ash, dioxin precursor (eg trichlorobenzene), etc. are oxidatively decomposed and the exhaust gas becomes an extremely clean gas.
【0034】高温集塵機(13)から出た熱排ガスは、さら
にガスクーラー(14)へ送られ、ここで400〜500℃
に冷却され、触媒層(15)におけるNH3 還元脱硝により
NOx低減とダイオキシンの除去が行われた後、完全な
クリーンガスとなって、煙突(16)より系外へ放出され
る。ガスクーラー(14)における排ガス冷却は空気にて行
われ、ガスクーラー(14)で生じた約300℃の熱風は熱
風管路(17)を経てバーナ(8) (10)(12)へ供給される。The hot exhaust gas discharged from the high temperature dust collector (13) is further sent to the gas cooler (14) where it is heated to 400 to 500 ° C.
After being cooled down to NOx reduction and dioxin removal by NH 3 reduction denitration in the catalyst layer (15), it becomes a completely clean gas and is discharged from the chimney (16) to the outside of the system. Exhaust gas cooling in the gas cooler (14) is performed by air, and the hot air of about 300 ° C generated in the gas cooler (14) is supplied to the burners (8) (10) (12) via the hot air duct (17). It
【0035】このようにして、処理灰、放流排水、排出
ガスは規制値を十分クリアできる迄浄化される。In this way, the treated ash, the discharged waste water, and the exhaust gas are purified until the regulated value is sufficiently cleared.
【0036】上記プロセスで得られた処理飛灰の有害物
質除去成績を表2に示す。Table 2 shows the harmful substance removal results of the treated fly ash obtained by the above process.
【0037】[0037]
【発明の効果】本発明による飛灰の処理装置は以上の如
く構成されているので、下記の効果を奏することができ
る。Since the fly ash processing apparatus according to the present invention is constructed as described above, the following effects can be obtained.
【0038】(1) 洗浄槽で飛灰を水洗し、乾燥造粒機で
乾燥造粒し、キルン炉で造粒物を焼結し、場合によって
は2次燃焼炉でさらに加熱することにより、飛灰中に含
まれるNa、K、Ca、Cl、SO3 等を除去すること
ができる。(1) Fly ash is washed with water in a washing tank, dried and granulated by a dry granulator, the granulated product is sintered in a kiln furnace, and further heated in a secondary combustion furnace in some cases. Na, K, Ca, Cl, SO 3 and the like contained in fly ash can be removed.
【0039】(2) 上記水洗により飛灰の焼結温度が高温
側に移行し、高温処理時の固結および上記Na+ 、
K+ 、Ca++、Cl- 、SO4 --等の揮散が防止でき
る。(2) The above-mentioned washing with water shifts the sintering temperature of fly ash to the high temperature side, and solidification during the high temperature treatment and the above Na + ,
It is possible to prevent volatilization of K + , Ca ++ , Cl − , SO 4 − and the like.
【0040】(3) 高温熱風によるキルン型直接焼結方式
により、焼結による固結閉塞の問題が解決され、さらに
800℃以上の高温域での操作も可能となり、ダイオキ
シンの熱分解および酸化が容易に行われる。(3) The kiln-type direct sintering method using high-temperature hot air solves the problem of solidification blockage due to sintering, and enables operation in a high temperature range of 800 ° C. or higher, resulting in thermal decomposition and oxidation of dioxin. Easily done.
【0041】(4) 飛灰の焼結処理前に乾燥造粒装置が設
けられているので、焼結後の灰分は粒状となり、焼結時
の粉塵飛散を抑制しかつ排出灰のハンドリングを容易に
することができる。(4) Since the dry granulation device is provided before the sintering process of fly ash, the ash content after sintering becomes granular, the dust scattering at the time of sintering is suppressed, and the discharged ash is easily handled. Can be
【0042】(5) 集塵機でキルン炉または2次燃焼炉か
ら出た高温排ガスを除塵するとともに、高温雰囲気にお
けるフィルター表面上で、CO、灰中の未燃カーボン、
ダイオキシンの前駆物質(例えばトリクロロベンゼン)
等が酸化分解され、排出ガスを極めてクリーンな排ガス
とすることができる。(5) The dust collector removes high temperature exhaust gas from the kiln furnace or the secondary combustion furnace, and CO, unburned carbon in ash, on the filter surface in a high temperature atmosphere.
Dioxin precursors (eg trichlorobenzene)
The exhaust gas can be made into an extremely clean exhaust gas.
【0043】(6) 脱硝触媒においてアンモニアの添加に
よりNOxの還元除去とダイオキシンの分解が行われ
れ、ダイオキシンおよびNOxがいずれも除去できた。(6) NOx was reduced and removed and dioxin was decomposed by adding ammonia in the denitration catalyst, and both dioxin and NOx could be removed.
【0044】(7) この処理後の高温ガスは完全除塵され
ているので、以後300〜400℃におけるダイオキシ
ンの発生はなく、また熱回収装置としてはクリーンガス
処理用のコンパクトな装置で充分な熱回収が可能であ
り、この熱分解に要するエネルギーも低消費である。(7) Since the high-temperature gas after this treatment is completely removed of dust, no dioxin is generated at 300 to 400 ° C. thereafter, and the heat recovery device is a compact device for treating clean gas and has sufficient heat. It can be recovered and the energy required for this thermal decomposition is also low consumption.
【0045】[0045]
【表1】 [Table 1]
【表2】 [Table 2]
【図1】本発明の実施例を示すフローシートである。FIG. 1 is a flow sheet showing an example of the present invention.
【図2】焼結飛灰の圧壊加重と温度の関係を示すグラフ
である。FIG. 2 is a graph showing the relationship between the crushing load of sintered fly ash and the temperature.
【図3】フィルターの使用による、排ガス中のCOの高
温雰囲気における低減性能を示すグラフである。FIG. 3 is a graph showing the reduction performance of CO in exhaust gas in a high temperature atmosphere by using a filter.
【図4】フィルターの使用による、灰中の未燃カーボン
の酸化および燃焼によるCO発生とカーボンの減少をそ
れぞれ示すグラフである。FIG. 4 is a graph showing CO generation and carbon reduction due to oxidation and combustion of unburned carbon in ash by using a filter, respectively.
【図5】フィルターの使用による、ダイオキシン前駆物
質であるトリクロロベンゼン(TCB)の高温雰囲気に
おける低減性能を示すグラフである。FIG. 5 is a graph showing reduction performance of trichlorobenzene (TCB), which is a dioxin precursor, in a high temperature atmosphere by using a filter.
【図6】従来技術を示すフローシートである。FIG. 6 is a flow sheet showing a conventional technique.
1:洗浄槽 7:乾燥造粒機 9:キルン炉 10:2次燃焼炉 13:集塵機 14:ガスクーラー 15:触媒層 17:熱風管路 1: Washing tank 7: Dry granulator 9: Kiln furnace 10: Secondary combustion furnace 13: Dust collector 14: Gas cooler 15: Catalyst layer 17: Hot air duct
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 FI 技術表示箇所 B09B 3/00 F23J 1/00 A B09B 3/00 ZAB 303 L (72)発明者 伊藤 道雄 大阪市此花区西九条5丁目3番28号 日立 造船株式会社内─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Reference number within the agency FI Technical display location B09B 3/00 F23J 1/00 A B09B 3/00 ZAB 303 L (72) Inventor Michio Ito Osaka City Hitachi Shipbuilding Co., Ltd.
Claims (5)
を乾燥造粒する乾燥造粒機と、造粒物を焼結するキルン
炉とを具備してなる飛灰の処理装置。1. An apparatus for treating fly ash, comprising a washing tank for washing fly ash with water, a dry granulator for drying and granulating the fly ash after washing with water, and a kiln furnace for sintering the granulated material. .
に、排ガス中の未燃物を完全に燃焼する2次燃焼炉を具
備してなる飛灰の処理装置。2. The processing apparatus according to claim 1, further comprising a secondary combustion furnace that completely burns unburned substances in the exhaust gas.
て、さらに、乾燥造粒機から出た低温排ガスと、キルン
炉または2次燃焼炉から出た高温排ガスとの混合ガスを
除塵処理する集塵機を具備してなる飛灰の処理装置。3. The dust collector according to claim 1, further comprising: a mixed gas of a low temperature exhaust gas discharged from a dry granulator and a high temperature exhaust gas discharged from a kiln furnace or a secondary combustion furnace. An apparatus for treating fly ash, which comprises:
に、集塵機から出た排ガスを冷却する脱硝触媒付きガス
クーラーを具備してなる飛灰の処理装置。4. The fly ash treatment apparatus according to claim 3, further comprising a gas cooler with a denitration catalyst for cooling the exhaust gas discharged from the dust collector.
に、ガスクーラーにおける熱交換により生じた高温空気
を、乾燥造粒機、キルン炉および/または2次燃焼炉の
各バーナへ送る熱風管路を具備してなる飛灰の処理装
置。5. The treatment apparatus according to claim 4, further comprising hot air ducts for sending high temperature air generated by heat exchange in a gas cooler to burners of a drying granulator, a kiln furnace and / or a secondary combustion furnace. An apparatus for treating fly ash, which comprises:
Priority Applications (1)
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JP06027715A JP3104112B2 (en) | 1994-02-25 | 1994-02-25 | Fly ash processing equipment |
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Application Number | Priority Date | Filing Date | Title |
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JP06027715A JP3104112B2 (en) | 1994-02-25 | 1994-02-25 | Fly ash processing equipment |
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JPH07232155A true JPH07232155A (en) | 1995-09-05 |
JP3104112B2 JP3104112B2 (en) | 2000-10-30 |
Family
ID=12228706
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Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002326077A (en) * | 2001-05-08 | 2002-11-12 | Mitsubishi Heavy Ind Ltd | Method for treating waste and equipment therefor |
JP2003103232A (en) * | 2001-07-26 | 2003-04-08 | Tokuyama Corp | Method for treating incineration ash |
JP2009131792A (en) * | 2007-11-30 | 2009-06-18 | Chugoku Electric Power Co Inc:The | Fly ash balloon recovering method and system |
JP2009240933A (en) * | 2008-03-31 | 2009-10-22 | Taiheiyo Cement Corp | Pretreatment device and pretreatment method in wet decarbonization of fly ash |
JP2019051494A (en) * | 2017-09-19 | 2019-04-04 | 太平洋セメント株式会社 | Processing equipment and processing method for mercury-containing substance |
CN117276551A (en) * | 2023-11-23 | 2023-12-22 | 兰钧新能源科技有限公司 | Sodium-electricity layered oxide positive electrode material, preparation method thereof and sodium-ion battery |
CN117358732A (en) * | 2023-10-26 | 2024-01-09 | 北京科技大学 | Fly ash resource product and treatment method and application thereof |
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1994
- 1994-02-25 JP JP06027715A patent/JP3104112B2/en not_active Expired - Fee Related
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002326077A (en) * | 2001-05-08 | 2002-11-12 | Mitsubishi Heavy Ind Ltd | Method for treating waste and equipment therefor |
JP2003103232A (en) * | 2001-07-26 | 2003-04-08 | Tokuyama Corp | Method for treating incineration ash |
JP2009131792A (en) * | 2007-11-30 | 2009-06-18 | Chugoku Electric Power Co Inc:The | Fly ash balloon recovering method and system |
JP2009240933A (en) * | 2008-03-31 | 2009-10-22 | Taiheiyo Cement Corp | Pretreatment device and pretreatment method in wet decarbonization of fly ash |
JP2019051494A (en) * | 2017-09-19 | 2019-04-04 | 太平洋セメント株式会社 | Processing equipment and processing method for mercury-containing substance |
CN117358732A (en) * | 2023-10-26 | 2024-01-09 | 北京科技大学 | Fly ash resource product and treatment method and application thereof |
CN117276551A (en) * | 2023-11-23 | 2023-12-22 | 兰钧新能源科技有限公司 | Sodium-electricity layered oxide positive electrode material, preparation method thereof and sodium-ion battery |
CN117276551B (en) * | 2023-11-23 | 2024-03-19 | 兰钧新能源科技有限公司 | Sodium-electricity layered oxide positive electrode material, preparation method thereof and sodium-ion battery |
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JP3104112B2 (en) | 2000-10-30 |
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