JPH10118614A - Process and device for exhausting pyrolysis gas in industrial waste thermal decomposition furnace - Google Patents
Process and device for exhausting pyrolysis gas in industrial waste thermal decomposition furnaceInfo
- Publication number
- JPH10118614A JPH10118614A JP29796496A JP29796496A JPH10118614A JP H10118614 A JPH10118614 A JP H10118614A JP 29796496 A JP29796496 A JP 29796496A JP 29796496 A JP29796496 A JP 29796496A JP H10118614 A JPH10118614 A JP H10118614A
- Authority
- JP
- Japan
- Prior art keywords
- waste
- pyrolysis
- pyrolysis gas
- furnace
- 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.)
- Pending
Links
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 111
- 238000000034 method Methods 0.000 title claims description 10
- 238000005979 thermal decomposition reaction Methods 0.000 title abstract 2
- 239000002440 industrial waste Substances 0.000 title 1
- 239000002699 waste material Substances 0.000 claims abstract description 74
- 238000001816 cooling Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 9
- 239000007789 gas Substances 0.000 description 69
- 238000000926 separation method Methods 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は都市ごみなどの廃棄
物を熱分解炉で熱分解した後の熱分解ガスを処理して取
り出すための熱分解ガス取出方法及び装置に関するもの
である。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for removing a pyrolysis gas for treating and extracting a pyrolysis gas after pyrolysis of waste such as municipal waste in a pyrolysis furnace.
【０００２】[0002]
【従来の技術】現在の廃棄物の処理方式としては、焼却
炉にて廃棄物を燃焼するようにした燃焼方式が採用され
ている。2. Description of the Related Art As a current waste disposal system, a combustion system in which waste is burned in an incinerator is employed.
【０００３】しかしながら、上記燃焼方式の場合には、
燃焼排ガス中に含まれるダイオキシン発生の問題があ
ること、ガス量が多く熱エネルギーの利用効率が悪い
こと、灰が多量に出るのでその処理が大変であるこ
と、埋立地の容量が限界に近付いてきていること、等
の問題が提起されている。[0003] However, in the case of the above-mentioned combustion system,
There is a problem of dioxin generation in the flue gas, the amount of gas is large, the efficiency of using heat energy is inefficient, the ash is generated in large quantities, the treatment is difficult, and the capacity of landfills is approaching its limit. Issues have been raised.
【０００４】そのため、次世代の廃棄物処理方式とし
て、廃棄物を不活性雰囲気下で加熱して熱分解させてガ
ス化後、高温で燃焼させる方式が開発され、一部で実証
運転が行われている。[0004] Therefore, as a next-generation waste treatment method, a method has been developed in which waste is heated under an inert atmosphere, pyrolyzed, gasified, and then burned at a high temperature, and demonstration operation is partially performed. ing.
【０００５】廃棄物を熱分解ガス化するために用いられ
ている熱分解ガス化装置は、図２にその一例の概要を示
す如く、約３度ほど下傾させて横向きに配置したロータ
リーキルン型の熱分解炉１の長手方向一端の入口２に、
廃棄物７の投入ホッパ４を供給用コンベヤ６を介して設
け、上記熱分解炉１の長手方向他端の出口３に、熱分解
ガス７Ａと熱分解残留物７Ｂとを分離する分離室８を設
け、熱分解炉１を低速で回転させた状態において、ホッ
パ４から投入された廃棄物７を供給用コンベヤ６によっ
て熱分解炉１内に徐々に供給しつつ、熱分解炉１を構成
する外側の加熱流路９内に、出口３側から入口２側へ向
けて熱風５を流通させることにより、熱分解炉１内の廃
棄物７を外熱により間接的に加熱、乾燥させて熱分解
し、発生した熱分解ガス７Ａを分離室８上部から取り出
して下流の燃焼炉へと送るようにし、一方、不燃物を含
む熱分解残留物７Ｂを、分離室８下部から一旦取り出し
て不燃物の分別工程を経てから燃焼炉へ送るようにして
ある。The pyrolysis gasifier used for pyrolysis gasification of waste is a rotary kiln-type device which is arranged sideways with a downward inclination of about 3 degrees as shown in FIG. At the inlet 2 at one longitudinal end of the pyrolysis furnace 1,
A hopper 4 for inputting waste 7 is provided via a supply conveyor 6, and a separation chamber 8 for separating a pyrolysis gas 7A and a pyrolysis residue 7B is provided at an outlet 3 at the other end in the longitudinal direction of the pyrolysis furnace 1. In a state where the pyrolysis furnace 1 is rotated at a low speed, the waste 7 supplied from the hopper 4 is gradually supplied into the pyrolysis furnace 1 by the supply conveyor 6 while the pyrolysis furnace 1 is formed. By flowing hot air 5 from the outlet 3 side to the inlet 2 side in the heating flow path 9, the waste 7 in the pyrolysis furnace 1 is indirectly heated and dried by external heat to be thermally decomposed. Then, the generated pyrolysis gas 7A is taken out from the upper part of the separation chamber 8 and sent to the downstream combustion furnace, while the pyrolysis residue 7B containing incombustibles is once taken out from the lower part of the separation chamber 8 to separate incombustibles. After the process, it is sent to the combustion furnace.
【０００６】上記熱分解炉１では、熱分解温度を高くし
て熱分解ガスを低分子量化することが望ましいものであ
るが、残留物中から金属を資源として回収する必要性か
ら、アルミニウムが溶融しない６００℃以下の比較的低
い温度で運転を行うため、発生する熱分解ガス７Ａの温
度は４５０℃程度となる。In the pyrolysis furnace 1 described above, it is desirable to increase the pyrolysis temperature to reduce the molecular weight of the pyrolysis gas. However, since it is necessary to recover metal as a resource from the residue, aluminum is not melted. Since the operation is performed at a relatively low temperature of 600 ° C. or less, the temperature of the generated pyrolysis gas 7A is about 450 ° C.
【０００７】[0007]
【発明が解決しようとする課題】ところが、上記熱分解
ガス７ＡからＣＯやＨ2 、あるいは、Ｃ1 〜Ｃ4 （メタ
ン、エタン、プロパン、ブタン等）の常温可燃ガス成分
を回収する場合には、スクラバーや熱交換器等の装置を
用いて熱分解ガス７Ａを冷却することになるが、上述し
たように比較的低温で熱分解するため、発生した熱分解
ガス７Ａは低分子量化があまり進んでいないことから、
冷却して取り出すとき、冷却過程において、３００℃以
下になると、ガス中のタールや油分が凝縮し、装置に付
着して詰まりや腐食を起す問題が惹起される。このター
ルや油分は処理が難しく、そのため、特殊なタール分離
器や油水分離器が必要となり、又、冷却による熱ロスも
大きい。更に、熱分解ガス７Ａ中に水分が多く含まれて
いるため、見かけ上低カロリーのガスとなってしまう。However, when recovering CO or H 2 or room temperature combustible gas components such as C 1 -C 4 (methane, ethane, propane, butane, etc.) from the pyrolysis gas 7A, The pyrolysis gas 7A is cooled by using a device such as a scrubber or a heat exchanger. However, since the pyrolysis gas is thermally decomposed at a relatively low temperature as described above, the generated pyrolysis gas 7A has a low molecular weight. Not because
When the temperature is lowered to 300 ° C. or less in the cooling process when taking out by cooling, the problem that tar and oil in the gas condense and adhere to the device to cause clogging and corrosion is caused. This tar or oil is difficult to treat, so a special tar separator or oil-water separator is required, and heat loss due to cooling is large. Further, since the pyrolysis gas 7A contains a large amount of water, the gas becomes apparently low in calories.
【０００８】そこで、本発明は、タールや油分を含まず
且つ水分の少ない高カロリーの熱分解ガスを容易に取り
出すことができるようにしようとするものである。Therefore, the present invention is to make it possible to easily extract a high-calorie pyrolysis gas containing no tar or oil and having a low water content.
【０００９】[0009]
【課題を解決するための手段】本発明は、上記課題を解
決するために、廃棄物を圧密状態で熱分解炉の入口へ供
給して該熱分解炉内で廃棄物を熱分解し、該熱分解によ
り生じた４５０℃程度の熱分解ガスを、熱分解炉の出口
より取り出して上記熱分解炉の入口へ供給される圧密状
態の廃棄物中を通過させ、ここで熱交換させて３００℃
以下まで冷却して取り出す廃棄物熱分解炉の熱分解ガス
取出方法とする。According to the present invention, in order to solve the above-mentioned problems, waste is supplied to an inlet of a pyrolysis furnace in a compacted state, and the waste is pyrolyzed in the pyrolysis furnace. The pyrolysis gas of about 450 ° C. generated by the pyrolysis is taken out from the outlet of the pyrolysis furnace and passed through the compacted waste supplied to the inlet of the pyrolysis furnace.
A method for extracting pyrolysis gas from a waste pyrolysis furnace that is cooled down and taken out below.
【００１０】又、熱分解炉の入口へ供給する廃棄物の充
填層部を形成して、該廃棄物充填層部を通して入口へ供
給された廃棄物を熱分解炉で熱分解するようにし、且つ
該熱分解炉の出口に接続した熱分解ガスラインを、上記
廃棄物充填層部に接続し、更に、該廃棄物充填層部に接
続した別の熱分解ガスラインをスクラバーに接続した構
成とする。[0010] Further, a packed bed portion of the waste to be supplied to the inlet of the pyrolysis furnace is formed, and the waste supplied to the inlet through the waste packed bed portion is thermally decomposed by the pyrolysis furnace; A pyrolysis gas line connected to the outlet of the pyrolysis furnace is connected to the waste packed bed, and another pyrolysis gas line connected to the waste packed bed is connected to a scrubber. .
【００１１】熱分解炉で発生した熱分解ガスを熱分解ガ
スラインを通して廃棄物充填層部内に導いて、廃棄物の
中を通過させることにより３００℃以下まで冷却させる
間に、ガス中から出て来たタール、油分が廃棄物に付着
して分離される。更に、廃棄物充填層部から出た熱分解
ガスをスクラバーで洗浄すると共に更に冷却すると、ガ
ス中の水蒸気が凝縮するため、水分の少ないガスとして
取り出すことができる。[0011] The pyrolysis gas generated in the pyrolysis furnace is guided through the pyrolysis gas line into the waste packed bed, and is allowed to pass through the waste while being cooled to 300 ° C. or less. Incoming tar and oil adhere to waste and are separated. Further, when the pyrolysis gas discharged from the waste packed bed is washed with a scrubber and further cooled, water vapor in the gas is condensed, so that the gas can be taken out as a gas having a low moisture content.
【００１２】[0012]
【発明の実施の形態】以下、本発明の実施の形態を図面
を参照して説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１３】図１は本発明の実施の一形態を示すもの
で、熱分解炉１の入口２に設置した給塵機としての供給
用コンベヤ６に廃棄物７を導くようにする図２の投入ホ
ッパ４に代えて、廃棄物７を圧密させてから落下させる
ようにする廃棄物充填層部１０を形成し、上部の投入ホ
ッパ４より落下される廃棄物７を充填層部１０で圧密状
態にしてから供給用コンベヤ６上へ切り出すようにし、
且つ、上記廃棄物充填層部１０の下側部位置にガス入口
１０ａを設けると共に上側部位置にガス出口１０ｂを設
けて、熱分解炉１の出口３側に設置された分離室８の頂
部に一端を接続した熱分解ガスライン１１ａの他端を上
記廃棄物充填層部１０のガス入口１０ａに接続し、又、
上記廃棄物充填層部１０のガス出口１０ｂに一端を接続
した熱分解ガスライン１１ｂの他端をスクラバー１２に
接続し、熱分解炉１で発生した熱分解ガス７Ａを、熱分
解ガスライン１１ａから廃棄物充填層部１０内を通した
後、熱分解ガスライン１１ｂを通しスクラバー１２へ送
って取り出すようにする。FIG. 1 shows an embodiment of the present invention. In FIG. 2, a waste 7 is introduced to a supply conveyor 6 serving as a dust collector installed at an inlet 2 of a pyrolysis furnace 1. Instead of the hopper 4, a waste filling layer portion 10 is formed to consolidate and drop the waste 7, and the waste 7 dropped from the upper input hopper 4 is condensed by the filling layer portion 10. And then cut it out onto the supply conveyor 6,
Further, a gas inlet 10a is provided at a lower portion of the waste packed bed portion 10 and a gas outlet 10b is provided at an upper portion of the waste packed bed portion 10. The gas inlet 10a is provided at the top of the separation chamber 8 provided on the outlet 3 side of the pyrolysis furnace 1. The other end of the pyrolysis gas line 11a having one end connected thereto is connected to the gas inlet 10a of the waste packed bed portion 10, and
The other end of the pyrolysis gas line 11b having one end connected to the gas outlet 10b of the waste packed bed portion 10 is connected to the scrubber 12, and the pyrolysis gas 7A generated in the pyrolysis furnace 1 is sent from the pyrolysis gas line 11a. After passing through the waste packed bed section 10, the waste is sent to the scrubber 12 through the pyrolysis gas line 11b and taken out.
【００１４】なお、１３は熱分解ガスライン１１ｂの途
中に設置した吸引ファン、１４はスクラバー１２の出口
ライン、１５は洗浄水、１６は循環ポンプを示す。Reference numeral 13 denotes a suction fan installed in the middle of the pyrolysis gas line 11b, 14 denotes an outlet line of the scrubber 12, 15 denotes washing water, and 16 denotes a circulation pump.
【００１５】熱分解炉１内で廃棄物７を熱分解すること
により生じた４５０℃程度の温度を有する熱分解ガス７
Ａは、吸引ファン１３の運転により、先ず、分離室８の
頂部から熱分解ガスライン１１ａを通って廃棄物充填層
部１０内に入り、ここに充填されている廃棄物７の中を
通過してから熱分解ガスライン１１ｂに導かれる。上記
廃棄物充填層部１０内では、熱交換が行われて熱分解ガ
ス７Ａが保有する熱を廃棄物７によって熱回収させ、３
００℃以下となるまで冷却させるようにする。この際、
熱分解ガス７Ａは３００℃以下になると、タールや油分
等が凝縮してガスから分離されるので、この冷却過程で
生じたタールや油分は廃棄物７に吸着されることにな
り、更に、このタールや油分は廃棄物７と共に熱分解炉
１内に供給され、循環により繰り返し熱分解ガス化され
るため、熱分解ガス７Ａは徐々に低分子量化されること
になる。なお、上記熱分解ガス７Ａは酸素を含んでいな
いため、廃棄物充填層部１０内を通過するときに、廃棄
物７を着火させてしまう心配はない。Pyrolysis gas 7 having a temperature of about 450 ° C. generated by pyrolyzing waste 7 in pyrolysis furnace 1
A firstly enters the waste packed bed 10 through the pyrolysis gas line 11a from the top of the separation chamber 8 by the operation of the suction fan 13, and passes through the waste 7 filled therein. And then led to the pyrolysis gas line 11b. In the waste packed bed portion 10, heat is exchanged, and the heat held by the pyrolysis gas 7A is recovered by the waste 7, and 3
Cool down to below 00 ° C. On this occasion,
When the pyrolysis gas 7A becomes 300 ° C. or lower, tar and oil are condensed and separated from the gas, so that tar and oil generated in the cooling process are adsorbed by the waste 7, and furthermore, The tar and oil are supplied together with the waste 7 into the pyrolysis furnace 1 and repeatedly pyrolyzed into gas by circulation, so that the pyrolysis gas 7A is gradually reduced in molecular weight. Since the pyrolysis gas 7A does not contain oxygen, there is no fear that the waste 7 is ignited when passing through the waste filling layer portion 10.
【００１６】次に、上記熱分解ガスライン１１ｂに導か
れた熱分解ガス７Ａはスクラバー１２に送られ、ここ
で、洗浄水１５による洗浄が行われると同時に冷却が行
われることになる。この場合、熱分解ガス７Ａ中には、
熱分解炉１での熱分解過程及び廃棄物充填層部１０内を
通過するときの廃棄物乾燥過程で生じた水分を含んでい
るが、スクラバー１２で１００℃以下、たとえば、８０
℃まで冷却することにより上記水分（水蒸気）を凝縮さ
せることができる。又、熱分解炉１内に供給される廃棄
物７には、タールや油分が付着混入していることにより
高カロリー化するため、熱分解ガス７Ａ中の常温可燃ガ
ス成分を多くすることができる。したがって、スクラバ
ー１２の出口ライン１４から水分の少ない高カロリーの
熱分解ガス７Ａを取り出すことができる。Next, the pyrolysis gas 7A guided to the pyrolysis gas line 11b is sent to the scrubber 12, where the cleaning with the cleaning water 15 is performed and the cooling is performed at the same time. In this case, in the pyrolysis gas 7A,
Although it contains moisture generated during the pyrolysis process in the pyrolysis furnace 1 and the waste drying process when passing through the waste packed bed section 10, the scrubber 12 contains water at 100 ° C. or less, for example, 80 ° C.
The above-mentioned water (steam) can be condensed by cooling to a temperature of ° C. In addition, since the waste 7 supplied into the pyrolysis furnace 1 is increased in calorie due to admixture of tar and oil, the room-temperature combustible gas component in the pyrolysis gas 7A can be increased. . Therefore, the high-calorie pyrolysis gas 7A having a low moisture content can be taken out from the outlet line 14 of the scrubber 12.
【００１７】上記において、熱分解ガス７Ａは、廃棄物
充填層部１０内を通過することによって冷却されるが、
その際に、廃棄物７の乾燥が行われるため熱ロスを小さ
くすることができる。又、スクラバー１２に送り込まれ
る熱分解ガス７Ａはタールや油分が分離除去された後の
ものであるため、タールや油分が熱分解ガスライン１１
ｂ、吸引ファン１３、スクラバー１２に付着することは
なく、詰まりや腐食の原因となることはない。In the above, the pyrolysis gas 7A is cooled by passing through the waste packed bed portion 10,
At that time, since the waste 7 is dried, heat loss can be reduced. Further, since the pyrolysis gas 7A sent into the scrubber 12 is obtained after the tar and oil are separated and removed, the tar and oil are removed from the pyrolysis gas line 11.
b, it does not adhere to the suction fan 13 and the scrubber 12, and does not cause clogging or corrosion.
【００１８】[0018]
【発明の効果】以上述べた如く、本発明によれば、廃棄
物充填層部を通して供給された廃棄物を熱分解する熱分
解炉の出口側に、熱分解ガスラインの一端を接続し、熱
分解ガスを、上記廃棄物充填層部を通して熱交換させて
から更にスクラバーに送って洗浄するようにしてあるの
で、次の如き優れた効果を発揮する。 (1) 熱分解炉で発生した熱分解ガスを廃棄物充填層部内
に充填されている廃棄物の中を通すことで冷却すること
により、発生したタールや油分を廃棄物に吸着させるこ
とができ、したがって、後続する熱分解ガスや機器にタ
ールや油分が付着して、詰まりや腐食の問題を起してし
まうようなことをなくすことができる。 (2) 熱分解ガスから熱回収して水分が減少した廃棄物
を、タールや油分と共に熱分解炉に供給できることか
ら、熱分解が容易となり、常温可燃ガス成分を多く含ん
だ高カロリーのガスを取り出すことができる。 (3) タールや油分を繰り返し熱分解させることができる
ようになることから、熱分解ガスを低分子量化すること
ができる。 (4) 熱分解ガスを廃棄物充填層部内で冷却するときに廃
棄物を乾燥させることができることから熱ロスが少な
い。 (5) 廃棄物充填層部で冷却した熱分解ガスを更にスクラ
バーで洗浄冷却することによって、水分の少ない高カロ
リーの常温可燃ガス成分を取り出すことができる。As described above, according to the present invention, one end of the pyrolysis gas line is connected to the outlet side of the pyrolysis furnace for pyrolyzing the waste supplied through the waste packed bed, Since the decomposed gas is subjected to heat exchange through the waste packed bed portion and then sent to a scrubber for cleaning, the following excellent effects are exhibited. (1) By cooling the pyrolysis gas generated in the pyrolysis furnace by passing it through the waste filled in the waste packed bed, the generated tar and oil can be absorbed by the waste. Therefore, it is possible to prevent tar or oil from adhering to the subsequent pyrolysis gas or equipment and causing a problem of clogging or corrosion. (2) Waste, whose moisture has been reduced by heat recovery from the pyrolysis gas, can be supplied to the pyrolysis furnace together with tar and oil, facilitating pyrolysis and producing high-calorie gas containing a large amount of combustible gas components at room temperature. Can be taken out. (3) Since tar and oil can be repeatedly pyrolyzed, the pyrolysis gas can be reduced in molecular weight. (4) Heat loss is small because the waste can be dried when the pyrolysis gas is cooled in the waste packed bed. (5) By further washing and cooling the pyrolysis gas cooled in the waste packed bed with a scrubber, a high-calorie room-temperature combustible gas component having a low moisture content can be taken out.
【図１】本発明の廃棄物熱分解炉の熱分解ガス取出装置
の実施の一形態を示す概要図である。FIG. 1 is a schematic diagram showing one embodiment of a pyrolysis gas extracting device of a waste pyrolysis furnace of the present invention.
【図２】熱分解ガス化装置の一例を示す概要図である。FIG. 2 is a schematic diagram showing an example of a pyrolysis gasifier.
１ 熱分解炉 ２ 入口 ３ 出口 ７ 廃棄物 ７Ａ 熱分解ガス １０ 廃棄物充填層部 １１ａ，１１ｂ 熱分解ガスライン １２ スクラバー DESCRIPTION OF SYMBOLS 1 Pyrolysis furnace 2 Inlet 3 Outlet 7 Waste 7A Pyrolysis gas 10 Waste packing layer part 11a, 11b Pyrolysis gas line 12 Scrubber
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ１０Ｊ 3/00 Ｃ１０Ｊ 3/02 Ｄ 3/02 Ｂ０９Ｂ 3/00 ＺＡＢ (72)発明者 萩谷 宗高 東京都江東区豊洲三丁目１番15号 石川島 播磨重工業株式会社東二テクニカルセンタ ー内──────────────────────────────────────────────────の Continuation of the front page (51) Int.Cl. 6 Identification symbol FI C10J 3/00 C10J 3/02 D 3/02 B09B 3/00 ZAB (72) Inventor Munetaka Hagaya 3-chome Toyosu, Koto-ku, Tokyo No. 1-15 Ishikawajima Harima Heavy Industries, Ltd. Toji Technical Center
Claims (2)
給して該熱分解炉内で廃棄物を熱分解し、該熱分解によ
り生じた４５０℃程度の熱分解ガスを、熱分解炉の出口
より取り出して上記熱分解炉の入口へ供給される圧密状
態の廃棄物中を通過させ、ここで熱交換させて３００℃
以下まで冷却して取り出すことを特徴とする廃棄物熱分
解炉の熱分解ガス取出方法。1. A waste material is supplied to an inlet of a pyrolysis furnace in a compacted state to thermally decompose the waste material in the pyrolysis furnace, and a pyrolysis gas of about 450 ° C. generated by the pyrolysis is pyrolyzed. It is taken out from the outlet of the furnace and passed through the waste in a compacted state supplied to the inlet of the pyrolysis furnace.
A method for removing pyrolysis gas from a waste pyrolysis furnace, wherein the pyrolysis gas is taken out after cooling to below.
層部を形成して、該廃棄物充填層部を通して入口へ供給
された廃棄物を熱分解炉で熱分解するようにし、且つ該
熱分解炉の出口に接続した熱分解ガスラインを、上記廃
棄物充填層部に接続し、更に、該廃棄物充填層部に接続
した別の熱分解ガスラインをスクラバーに接続した構成
を有することを特徴とする廃棄物熱分解炉の熱分解ガス
取出装置。Forming a packed bed of waste to be supplied to an inlet of the pyrolysis furnace, wherein the waste supplied to the inlet through the packed bed is pyrolyzed in the pyrolysis furnace; and A pyrolysis gas line connected to the outlet of the pyrolysis furnace is connected to the waste packed bed, and another pyrolysis gas line connected to the waste packed bed is connected to a scrubber. A pyrolysis gas take-out device for a waste pyrolysis furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29796496A JPH10118614A (en) | 1996-10-22 | 1996-10-22 | Process and device for exhausting pyrolysis gas in industrial waste thermal decomposition furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29796496A JPH10118614A (en) | 1996-10-22 | 1996-10-22 | Process and device for exhausting pyrolysis gas in industrial waste thermal decomposition furnace |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH10118614A true JPH10118614A (en) | 1998-05-12 |
Family
ID=17853377
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP29796496A Pending JPH10118614A (en) | 1996-10-22 | 1996-10-22 | Process and device for exhausting pyrolysis gas in industrial waste thermal decomposition furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH10118614A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010202689A (en) * | 2009-02-27 | 2010-09-16 | Bio Coke Lab Co Ltd | Gasification method, power generation method, gasification device, power generation device, and organic material |
| JP2010222472A (en) * | 2009-03-24 | 2010-10-07 | Jfe Steel Corp | Method for producing biomass charcoal and apparatus for producing biomass charcoal used in the method |
| JP2011089136A (en) * | 2011-01-26 | 2011-05-06 | Bio Coke Lab Co Ltd | Gasification method, power generation method, gasification apparatus, generator, and substance containing organic material and water-soluble organic material as principal components |
| WO2011162185A1 (en) * | 2010-06-22 | 2011-12-29 | Ｊｆｅエンジニアリング株式会社 | Biomass carbonization device and biomass carbonization method |
-
1996
- 1996-10-22 JP JP29796496A patent/JPH10118614A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010202689A (en) * | 2009-02-27 | 2010-09-16 | Bio Coke Lab Co Ltd | Gasification method, power generation method, gasification device, power generation device, and organic material |
| JP2010222472A (en) * | 2009-03-24 | 2010-10-07 | Jfe Steel Corp | Method for producing biomass charcoal and apparatus for producing biomass charcoal used in the method |
| WO2011162185A1 (en) * | 2010-06-22 | 2011-12-29 | Ｊｆｅエンジニアリング株式会社 | Biomass carbonization device and biomass carbonization method |
| JP2011089136A (en) * | 2011-01-26 | 2011-05-06 | Bio Coke Lab Co Ltd | Gasification method, power generation method, gasification apparatus, generator, and substance containing organic material and water-soluble organic material as principal components |
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