JP3537305B2 - Gas generation method in refuse gasification and melting furnace with pyrolysis zone and refuse pellets used in the method - Google Patents
Gas generation method in refuse gasification and melting furnace with pyrolysis zone and refuse pellets used in the methodInfo
- Publication number
- JP3537305B2 JP3537305B2 JP36427097A JP36427097A JP3537305B2 JP 3537305 B2 JP3537305 B2 JP 3537305B2 JP 36427097 A JP36427097 A JP 36427097A JP 36427097 A JP36427097 A JP 36427097A JP 3537305 B2 JP3537305 B2 JP 3537305B2
- Authority
- JP
- Japan
- Prior art keywords
- refuse
- gasification
- zone
- dust
- pellets
- 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 - Fee Related
Links
- 238000000034 method Methods 0.000 title claims description 36
- 239000008188 pellet Substances 0.000 title claims description 31
- 238000002309 gasification Methods 0.000 title claims description 21
- 238000000197 pyrolysis Methods 0.000 title claims description 21
- 238000002844 melting Methods 0.000 title claims description 15
- 230000008018 melting Effects 0.000 title claims description 15
- 239000007789 gas Substances 0.000 claims description 35
- 238000006243 chemical reaction Methods 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000000428 dust Substances 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 8
- 238000000354 decomposition reaction Methods 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 2
- 229910001882 dioxygen Inorganic materials 0.000 claims description 2
- 238000006722 reduction reaction Methods 0.000 description 6
- 238000005979 thermal decomposition reaction Methods 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010943 off-gassing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000010882 bottom ash Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000007787 solid Substances 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
- 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
-
- 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
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
- Coke Industry (AREA)
Description
【０００１】[0001]
【発明の属する分野】本発明は、都市ゴミ等を焼却処理
するのに際し、ゴミの可燃物からＣＯ、Ｈ２及びＣＨ４
を生成して取り出すところの熱分解域を備えたゴミのガ
ス化溶融炉に於けるガス生成方法と該方法に用いるゴミ
のペレットに関する。The present invention relates to a method for incinerating municipal garbage and the like, in which CO, H 2 and CH 4 are removed from combustible garbage.
The present invention relates to a gas generation method in a gasification and melting furnace for refuse provided with a pyrolysis zone for producing and taking out refuse, and refuse pellets used in the method.
【０００２】[0002]
【従来の技術】都市ゴミ等（可燃性産業廃棄物等も意味
する）を処理するのに、これを単に焼却処理した場合
に、大別すると二つの問題がある。 一つは、焼却に伴
う熱エネルギーをどのように有効に回収乃至再利用する
か、もう一つは、焼却によって発生する焼却灰をどのよ
うに二次処理するかという点である。2. Description of the Related Art In treating municipal garbage and the like (which also means flammable industrial waste and the like), there are two main problems if they are simply incinerated. One is how to effectively recover or reuse the heat energy associated with incineration, and the other is how to secondarily treat incineration ash generated by incineration.
【０００３】前者、即ち、熱エネルギーの有効利用の方
法としては、特公昭５１−４２４３４号公報或いは特公
昭５２−２４７９０号公報等において提案されている如
く、焼却炉に熱分解域を形成し、ゴミの可燃分（可燃分
は一般にゴミの約５０％で、水分は約４１％）をガス化
して取り出して（ガス化で残った可燃分中の炭素は約５
４％）、この可燃性ガス（ＣＯ、Ｈ２及びＣＨ４）を再
利用する方法が知られており、その再利用方法として
は、例えば、この熱分解型の焼却炉に連設したガス燃焼
炉において前記ガスを燃焼させ、その熱エネルギーによ
りボイラーを稼働させて発電を行ったり、熱交換器を介
して種々の目的に利用する方法が提案されている。As the former method, that is, a method for effectively utilizing thermal energy, a thermal decomposition zone is formed in an incinerator as proposed in JP-B-51-42434 or JP-B-52-24790. The combustibles of the garbage (the combustibles are generally about 50% of the garbage and the water is about 41%) are gasified and taken out (the carbon in the combustibles remaining after gasification is about 5%).
4%), and a method for reusing the combustible gas (CO, H 2 and CH 4 ) is known. Examples of the method for reusing the combustible gas include gas combustion connected to the pyrolysis type incinerator. A method has been proposed in which the gas is burned in a furnace and the boiler is operated by the thermal energy to generate power, or used for various purposes via a heat exchanger.
【０００４】また、後者、即ち、焼却によって発生する
焼却灰（ボトム灰）の処理方法として、前述した特公昭
５２−２４７９０号公報においても提案されているよう
に、その同じ焼却炉の炉底部に溶融域を形成し、下方か
ら酸素を供給して焼却灰を溶融せしめ、溶融スラグを下
方から取り出すという方法が提案されている。こうした
乾燥、分解、溶融は、竪炉において上方から、設計上必
要とされる所定の時間プロセスを経て行われることは言
うまでもない。As a method of treating the latter, ie, incineration ash (bottom ash) generated by incineration, as proposed in the above-mentioned Japanese Patent Publication No. 52-24790, the same method is applied to the bottom of the same incinerator. A method has been proposed in which a melting zone is formed, oxygen is supplied from below to melt the incinerated ash, and molten slag is removed from below. Needless to say, such drying, decomposition, and melting are performed from above in a vertical furnace through a predetermined time process required for design.
【０００５】このように、都市ゴミ等の焼却処理におけ
る二つの大きな問題については、それぞれの解決方向が
既に定まっており、概ね目的を達しているのであるが、
竪炉の上方から投入されたゴミが乾燥域を経て熱分解域
に至り、ここでガス生成の反応が生じる際、このガス生
成効率が非常に悪く、ＣＯ２或いはＨ２Ｏが形成され、
ＣＯ或いはＨ２の総量、特に回収されたガス中の、特に
Ｈ２の占める割合が低く、Ｈ２に比較して熱量の小さい
ＣＯが主体となる結果、回収熱エネルギー総量が小さな
ものであった。 為に、生成ガスからのエネルギー回収
方法として、上述したように、その生成ガスを単にガス
燃焼炉において燃焼させて熱エネルギーとして回収する
という方法が採られていたのである。[0005] As described above, with regard to the two major problems in the incineration treatment of municipal garbage and the like, the directions for solving the respective problems have already been determined, and the objectives have largely been achieved.
When refuse introduced from the upper part of the vertical furnace passes through the drying zone and reaches the pyrolysis zone, where a gas generation reaction occurs, the gas generation efficiency is very poor, and CO 2 or H 2 O is formed.
The total amount of CO or H 2 , particularly the proportion of H 2 in the recovered gas, especially H 2 , was low, and as a result, mainly CO having a smaller amount of heat than H 2 , the total amount of recovered thermal energy was small. . Therefore, as a method of recovering energy from product gas, as described above, a method of simply burning the product gas in a gas combustion furnace and recovering it as thermal energy has been adopted.
【０００６】[0006]
【発明が解決しようとする課題】本発明者は、こうした
現状に鑑み、乾燥域から熱分解域におけるゴミの可燃分
のガス化に関し、炉内温度帯とガスの生成反応との関係
について研究を重ねた。データの多いコークスの熱分解
から見ると、４４０°Ｃ〜５１２゜Ｃにおいてガス放出
が開始され、その固体からのガス放出は７５０°Ｃまで
続くことが分かっている。In view of these circumstances, the present inventor has conducted research on the gasification of combustible garbage from the dry zone to the pyrolysis zone with respect to the relationship between the furnace temperature zone and the gas generation reaction. Stacked. From the pyrolysis of coke with more data, it has been found that outgassing begins at 440 ° C. to 512 ° C., with outgassing from the solid continuing up to 750 ° C.
【０００７】そこで、生成ガスの反応について見ると、
熱分解の行われる６００゜Ｃ乃至１０００°Ｃの温度域
において、その６００゜Ｃ前後〜７００°Ｃ近辺ではＣ
＋２Ｈ２Ｏ→ＣＯ２＋２Ｈ２及びＨ２＋１／２Ｏ２→Ｈ
２Ｏの反応が起きる共に僅かにＣ＋Ｈ２Ｏ→ＣＯ＋Ｈ２
の反応が起こり得る。 また、６００゜Ｃ〜１０００゜
Ｃにおいて、主にＣ＋Ｈ２Ｏ→ＣＯ＋Ｈ２の反応が起き
て、Ｈ２の発生が多く（７０％程度）なり、１００゜Ｃ
においてコークスが形成される。Therefore, looking at the reaction of the produced gas,
In the temperature range of 600 ° C. to 1000 ° C. where the thermal decomposition is performed, C is approximately 600 ° C. to 700 ° C.
+ 2H 2 O → CO 2 + 2H 2 and H 2 + ／ O 2 → H
The reaction of 2 O occurs and both C + H 2 O → CO + H 2
Can occur. Further, at 600 ° C. to 1000 ° C., a reaction of mainly C + H 2 O → CO + H 2 occurs, and the generation of H 2 increases (about 70%), and
Coke is formed.
【０００８】このことから、ゴミ等（通常、水分が５０
％〜７０％、可燃分が５０〜５５％、他灰分等で、その
可燃分中、Ｃが５４％、Ｏが３６％を占める）について
も、前記コークスに準じたプロセスを経るものと推測で
きる。そこで、ＣＯ及びＨ２が生成される温度域に着目
すると、６００゜Ｃ〜１０００゜Ｃであるところから、
これらＣＯ及びＨ２、特にＨ２が多量に生成されるため
には充分なＨ２Ｏが必要であるところから、この温度域
における水性ガス化反応の効率を高めることが必要であ
ることが分かった。[0008] From this, garbage and the like (usually 50% water
% To 70%, flammable content is 50 to 55%, and other ash content, of which flammable content accounts for 54% of C and 36% of O). . Therefore, focusing on the temperature range in which CO and H 2 are generated, from 600 ° C. to 1000 ° C.,
Since a sufficient amount of H 2 O is required to generate a large amount of CO and H 2 , particularly H 2 , it is understood that it is necessary to increase the efficiency of the water gasification reaction in this temperature range. Was.
【０００９】本発明は、熱分解域を備えたゴミのガス化
溶融炉に於けるガスの生成において還元反応の効率を高
めてＣＯ及びＨ２、特にＨ２の多いガスを生成できるよ
うにし、ゴミ等焼却におけるエネルギー回収効率を向上
させることを目的とする。[0009] The present invention is to increase the efficiency of the reduction reaction in the gas generation in a gasification and melting furnace for refuse provided with a pyrolysis zone so that CO and H 2 , particularly H 2 rich gas, can be generated. The purpose is to improve the energy recovery efficiency in incineration of garbage and the like.
【００１０】[0010]
【課題を解決するための手段】本発明は、上記目的を達
成するために、竪炉の上部からゴミを投入し、炉底部か
ら酸素ガスを供給し、投入されたゴミが乾燥域、熱分解
域を経てガス化溶融されて取り出される熱分解域を備え
たゴミのガス化溶融炉に於けるガス生成方法であって、
投入に先立ってゴミを非乾燥状態において６０〜８０ｋ
ｇ／ｃｍ ２ で圧縮して水分を含有したペレットに形成
し、前記ペレットの中心が未乾燥状態で乾燥域を通過し
て熱分解域に至り、該未乾燥状態のペレットの微量残留
水分が蒸発する温度域が６００℃〜１０００℃であり、
前記ゴミのペレットの水分が水性ガス化反応を促進して
ゴミの可燃分のＨ２のガス化効率を向上させるようにし
た、という手段を講じたのである。According to the present invention, in order to achieve the above object, dust is introduced from the top of a vertical furnace, oxygen gas is supplied from the furnace bottom, and the introduced dust is dried, pyrolyzed. A gas generation method in a gasification and melting furnace for garbage provided with a pyrolysis zone that is taken out by being gasified and melted through a zone,
60-80k in non-dry state prior to loading
g / cm 2 to form a pellet containing water, and the center of the pellet passes through a dry zone in an undried state.
To the pyrolysis zone, leaving a small amount of the undried pellets.
The temperature range in which water evaporates is 600 ° C to 1000 ° C,
Moisture of the pellets of the dust is as to promote the water-gas reaction to improve the combustibles gasification efficiency of H 2 in the waste, it was taken means of.
【００１１】また、本発明において、上記生成ガスの成
分のうち、ＣＯ及びＨ２がモル比で次式
ＣＯ／（ＣＯ＋Ｈ ２）＝０．３３〜０．６７
を充足することが好ましい。本発明に於いて、上記生成
されるガスがＣＯ，Ｈ２及びＣＨ４である。In the present invention, among the components of the product gas, it is preferable that CO and H 2 satisfy the following formula: CO / (CO + H 2 ) = 0.33 to 0.67. In the present invention, the generated gas is CO, H 2 and CH 4 .
【００１２】本発明の方法に用いられるゴミのペレット
は、非乾燥状態のゴミが、直径１５０ｍｍ〜２５０ｍｍ
の球状又は円柱状に形成されているか、一辺が３００ｍ
ｍ〜５００ｍｍの立方体又は一辺が３００ｍｍ〜５００
ｍｍの断面を有する直方体で形成されているのが好まし
い。[0012] Pellets of waste used in the method of the present invention, dust undried state, diameter 150mm~250mm
Spherical or cylindrical shape are formed, one side is 300m
Cube of m to 500 mm or 300 mm to 500 on one side
It is preferably formed of a rectangular parallelepiped with a mm cross section
No.
【００１３】[0013]
【発明の実施の態様】本発明の方法によれば、非乾燥状
態で強く（６０〜８０ｋｇ／ｃｍ２程度）圧縮されて嵩
のある形状（例えば、直径１５０ｍｍ〜２５０ｍｍの球
状又は円柱状）に成形されたペレット状のゴミは、竪炉
の乾燥域を通過するも未だ完全乾燥に至らず、その中心
に微量水分を残留した状態で分解域（ゾーン）に到達す
る。勿論、この種の竪炉は、乾燥、分解、溶融が設計上
必要とされる所定の時間プロセスを経て行われるもので
あり、その乾燥域についても、格別に長く停留するとい
うものではなく、所定の時間経過で通過することは従来
技術と変わらない。According to the method of the present invention, it is strongly compressed (about 60 to 80 kg / cm 2 ) in a non-dried state to a bulky shape (for example, a spherical or cylindrical shape having a diameter of 150 mm to 250 mm). Although the formed pellet-like dust passes through the drying zone of the vertical furnace, it has not yet been completely dried, and reaches the decomposition zone (zone) with a trace amount of water remaining at its center. Of course, in this type of vertical furnace, drying, decomposition, and melting are performed through a predetermined time process required for design, and the drying region does not stop for a particularly long time. Passing with the passage of time is the same as in the prior art.
【００１４】分解域に到達したペレットは、ここで残留
する微量水分を完全蒸発させることになるが、この分解
域においてはゴミの可燃分のガス化が進行しており、酸
化、還元反応が生じている。特に、６００℃〜１０００
℃の温度域において放出される水分は、水性ガス化反応
の効率を高めることになる。その結果として、モル比
で、
ＣＯ／（ＣＯ＋Ｈ ２）＝０．３３〜０．６７
というＨ２の含有比率の高いガスを生成できるのであ
る。[0014] The pellets that have reached the decomposition zone completely evaporate the remaining traces of moisture. In this decomposition zone, gasification of combustible garbage proceeds, and oxidation and reduction reactions occur. ing. In particular, 600 ° C. to 1000
Water released in the temperature range of ° C. will increase the efficiency of the water gasification reaction. As a result, a gas having a high H 2 content ratio of CO / (CO + H 2 ) = 0.33 to 0.67 can be generated in a molar ratio.
【００１５】本発明の方法に用いられるゴミのペレット
としては、上述の形状の他に、非乾燥状態のゴミが６０
〜８０ｋｇ／ｃｍ２で圧縮され、一辺が３００ｍｍ〜５
００ｍｍの立方体又は一辺が３００ｍｍ〜５００ｍｍの
断面を有する直方体で形成されている物、或いはこれに
実質的に同じ物を使用することが出来る。As the dust pellets used in the method of the present invention, in addition to the above-mentioned shapes, non-dried dust can be used.
Compressed in ~80kg / cm 2, one side 300mm~5
An object made of a cube of 00 mm, a rectangular parallelepiped having a cross section of 300 mm to 500 mm on one side, or substantially the same can be used.
【００１６】[0016]
【実施例】以下、本発明の熱分解域を備えたゴミのガス
化溶融炉に於けるガス生成方法と該方法に用いるゴミの
ペレットの好適実施例について、図面を参照して詳述す
る。図１は、本発明の熱分解域を備えたゴミのガス化溶
融炉の概念図を示し、竪炉１の上方からゴミのペレット
２が投入される。 竪炉１は、投入されたペレット２は
炉内に堆積されるが、この炉内は、上部が乾燥域３、そ
の下層が熱分解域４、その下層が燃焼及び溶融域５とな
っている。炉床６の近傍には酸素供給口７が備えられ、
純度の高い酸素が供給されて、熱分解域４でチャー（炭
素）となった可燃分を燃焼、溶融させ、炉底６から溶融
スラグが取り出される。また、竪炉１の上方からは熱分
解によって生成されたガスが取り出され、二次処理、例
えば、ガス分離器、ガス燃焼炉等へ導かれる。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of a gas generating method in a gasification and melting furnace for refuse provided with a pyrolysis zone of the present invention and refuse pellets used in the method will be described below in detail with reference to the drawings. FIG. 1 is a conceptual diagram of a refuse gasification and melting furnace provided with a pyrolysis zone according to the present invention, and refuse pellets 2 are charged from above a vertical furnace 1. In the vertical furnace 1, the charged pellets 2 are deposited in the furnace. In the furnace, the upper part is a drying zone 3, the lower layer is a pyrolysis zone 4, and the lower layer is a combustion and melting zone 5. . An oxygen supply port 7 is provided near the hearth 6,
Oxygen of high purity is supplied, and combustibles that have become char (carbon) in the pyrolysis zone 4 are burned and melted, and molten slag is taken out from the furnace bottom 6. Further, gas generated by thermal decomposition is taken out from above the vertical furnace 1 and guided to a secondary treatment, for example, a gas separator, a gas combustion furnace or the like.
【００１７】上記ペレット２は、この実施例では、６０
〜８０ｋｇ／ｃｍ２で圧縮され、図２に示すように、直
径１５０ｍｍ程度の円柱状に形成されている。 このペ
レット２（水分含有率４５％）の昇温傾向を、外面部分
と中心部分とについて、夫々Ｘ線を用いて図３に示す。
比較例として、単にプッシャーの圧力で塊状として投
入されたゴミ塊の外面部分と中心の昇温をＹ線で示す。
図３のグラフから、従来のゴミ塊と比較してこのペレッ
ト２の中心の昇温が極めて緩やかであることが分かる。
図中、時間経過の６０分は、概ね乾燥域３を通過する時
間に相当する。残留水分を分析したところ、ペレット２
の中心において水分が、換算値としてみた場合に０．２
〜１．５％程度残留するという結果が出た。In the present embodiment, the pellet 2 is made of 60
It is compressed at ~ 80 kg / cm 2 and, as shown in FIG. 2, is formed in a columnar shape with a diameter of about 150 mm. FIG. 3 shows the tendency of the pellet 2 (having a water content of 45%) to rise in temperature with respect to the outer surface portion and the central portion using X-rays.
As a comparative example, the temperature rise at the outer surface portion and the center of the lump of garbage which is simply input as a lump by the pressure of the pusher is indicated by a Y line.
It can be seen from the graph of FIG. 3 that the temperature rise at the center of the pellet 2 is much slower than that of the conventional lump.
In the figure, the elapsed time of 60 minutes generally corresponds to the time of passing through the dry area 3. Analysis of residual moisture showed that pellet 2
The water content at the center of
Approximately 1.5% remained.
【００１８】図４は、熱分解域４において、生起されて
いる反応を想定したもので、これを竪炉１の生成ガス出
口温度と分解域近辺の炉内温度との関係において示す。
想定した反応式は、次の通りである。
３Ｃ＋１１／２Ｏ２＋Ｈ２→２ＣＯ＋ＣＯ２＋Ｈ２
・・・○線で示す。
３Ｃ＋１１／２Ｏ２＋２Ｈ２→ＣＯ＋２ＣＯ２＋２
Ｈ２・・・●線で示す。
５Ｃ＋３１／３Ｏ２＋１１／３Ｈ２Ｏ＋Ｈ２→２Ｃ
Ｏ＋３ＣＯ２＋Ｈ２Ｏ＋１１／３Ｈ２・・・△線で示
す。 但し、炉出口ガスを、ＣＯ／ＣＯ＋Ｈ２がモル比
で０．６に近似させたもの。
５Ｃ＋３１／３Ｏ２＋２１／２Ｈ２Ｏ＋１／３Ｈ２
→２ＣＯ＋３ＣＯ２＋１１／２ＨＯ＋１１／３Ｈ２・・
・□線で示す。 但し、熱分解ガス中の水分比を生成水
分に近似させ、炉出口ガス成分をＣＯ／ＣＯ＋Ｈ２が、
モル比で０．６に近似させたもの。FIG. 4 assumes a reaction occurring in the thermal decomposition zone 4 and shows the relationship between the temperature of the product gas outlet of the vertical furnace 1 and the temperature in the furnace near the decomposition zone.
The reaction formula assumed is as follows. 3C + 1 / 2O 2 + H 2 → 2CO + CO 2 + H 2
... indicated by a circle. 3C + 1 / 2O 2 + 2H 2 → CO + 2CO 2 +2
It is shown by H 2 ··· ● line. 5C + 31 / 3O 2 + 11 / 3H 2 O + H 2 → 2C
O + 3CO 2 + H 2 O + 11 / 3H 2 ... However, the furnace exit gas, which CO / CO + H 2 was allowed to approximate to 0.6 molar ratio. 5C + 31 / 3O 2 + 21 / 2H 2 O + ／ H 2
→ 2CO + 3CO 2 + 1 / 2HO + 11 / 3H 2 ...
・ Indicated by □ line. However, the moisture ratio in the pyrolysis gas is approximated to the generated moisture, and the gas component at the furnace outlet is CO / CO + H 2 ,
The molar ratio approximated to 0.6.
【００１８】次の酸化、還元反応式をモル比で見る。
２Ｃ＋１１／２Ｏ２＝ＣＯ＋ＣＯ２・・・（１）酸化反応
２Ｃ＋３Ｈ２Ｏ＝ＣＯ＋ＣＯ２＋３Ｈ２・・・（２）還元反応
これら（１）、（２）式より、４Ｃ＋１１／２Ｏ２＋３
Ｈ２＝２ＣＯ＋２ＣＯ＋２ＣＯ２＋３Ｈ２となり、従っ
て、
ＣＯ／ＣＯ＋Ｈ２＝２／２＋３＝２／５＝０．４
となる。The following oxidation and reduction equations are shown in terms of molar ratio. 2C + 1 / 2O 2 = CO + CO 2 (1) Oxidation reaction 2C + 3H 2 O = CO + CO 2 + 3H 2 (2) Reduction reaction From these formulas (1) and (2), 4C + 1 / 2O 2 +3
H 2 = 2CO + 2CO + 2CO 2 + 3H 2 , and the thus, the CO / CO + H 2 = 2 /2 + 3 = 2/5 = 0.4.
【００１９】また、次の酸化、還元反応式をモル比で見
ると、
２Ｃ＋１１／２Ｏ２＝ＣＯ＋ＣＯ２・・・（３）酸化反応
Ｃ＋２Ｈ２Ｏ＝ＣＯ２＋２Ｈ２・・・（４）還元反応
これら（３）、（４）式より、３Ｃ＋１１／２Ｏ２＋２
Ｈ２Ｏ＝２ＣＯ２＋ＣＯ＋２Ｈ２となり、従って、
ＣＯ／ＣＯ＋Ｈ２＝２／２＋２＝２／４＝０．５
となる。When the following oxidation and reduction reaction formulas are viewed in molar ratio, 2C + 1 / 2O 2 = CO + CO 2 (3) oxidation reaction C + 2H 2 O = CO 2 + 2H 2 (4) reduction reaction From these equations (3) and (4), 3C + 1 / 2O 2 +2
H 2 O = 2CO 2 + CO + 2H 2 , and therefore CO / CO + H 2 = 2/2 + 2 = 2/4 = 0.5.
【００２０】また、図４の温度軸に平行に、所定の温度
域に対応した反応を略示している。同図において、６０
０゜Ｃ以上において、Ｃ＋Ｈ２Ｏ→ＣＯ＋Ｈ２の反応が
主に生起し、ここに於いてペレット２の水分揮散により
水性ガス化反応の効率が高まるものである。Further, a reaction corresponding to a predetermined temperature range is schematically shown in parallel with the temperature axis in FIG. In FIG.
At 0 ° C. or higher, a reaction of C + H 2 O → CO + H 2 occurs mainly, and the efficiency of the water gasification reaction is enhanced by the evaporation of water from the pellets 2.
【００２１】尚、本発明において得られたＨ２がリッチ
である生成ガスからのエネルギー回収方法については、
直接燃焼による発電のほか、ＣＯと分離抽出して貯蔵
し、別途目的に使用できるものであるが、この使用目的
については本発明の対象としない。The method of recovering energy from the H 2 -rich product gas obtained in the present invention is described below.
In addition to power generation by direct combustion, CO can be separated and extracted from CO and stored, and can be used for another purpose. However, this purpose is not the object of the present invention.
【００２２】[0022]
【発明の効果】本発明の方法及び該方法に用いるペレッ
トによれば、ゴミ等の熱分解域を備えたガス化溶融炉に
おける熱分解のガス生成において、ゴミを非乾燥状態に
おいて６０〜８０ｋｇ／ｃｍ ２ で圧縮して水分を含有し
たペレットに形成し、前記ペレットの中心が未乾燥状態
で乾燥域を通過して熱分解域に至り、該未乾燥状態のペ
レットの微量残留水分が蒸発する温度域が６００℃〜１
０００℃であることによって、水性ガス化反応を助長
し、特に、Ｈ２ のリッチなガスを生成することがで
き、従来の熱分解方式に比べて、格段の高エネルギー回
収を図ることが出来る利点がある。本発明のその他の利
点は、発明の詳細な説明に記載の通りである。According to the method of the present invention and the pellets used in the method, in the gas generation for pyrolysis in a gasification and melting furnace having a pyrolysis zone for debris , the debris is kept in a non-dry state.
And compress at 60-80 kg / cm 2 to contain water
Pellets, and the center of the pellets is in an undried state
In dry region passing over to reach the pyrolysis zone, a yet-dry Bae
The temperature range where the trace residual moisture of the let evaporates is from 600 ° C to 1
By being at 000 ° C., the water gasification reaction can be promoted, and in particular, an H 2 rich gas can be generated, and an extremely high energy recovery can be achieved as compared with the conventional thermal decomposition method. There is. Other advantages of the present invention are as described in the detailed description of the invention.
【図１】本発明の方法を実施例する竪炉の概念図であ
る。FIG. 1 is a conceptual diagram of a vertical furnace embodying a method of the present invention.
【図２】本発明の方法に用いるペレットの斜視図であ
る。FIG. 2 is a perspective view of a pellet used in the method of the present invention.
【図３】本発明の方法におけるペレットの昇温を示すグ
ラフである。FIG. 3 is a graph showing the temperature rise of pellets in the method of the present invention.
【図４】本発明の方法におけるガス化反応域を示すグラ
フである。FIG. 4 is a graph showing a gasification reaction zone in the method of the present invention.
１ 竪炉 ２ ペレット ３ 乾燥域 ４ 熱分解域 ５ 溶融域 ６ 炉床 ７ 酸素供給口 1 vertical furnace 2 pellets 3 Dry area 4 Thermal decomposition zone 5 melting zone 6 Hearth 7 Oxygen supply port
フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｆ２３Ｇ 5/04 ＺＡＢ Ｆ２３Ｇ 5/04 ＺＡＢＺ (58)調査した分野(Int.Cl.7，ＤＢ名) F23G 5/027 F23G 5/24 F23G 5/04 B09B 3/00 C10B 53/00 C10J 3/00 F23G 5/00 Continuation of the front page (51) Int.Cl. 7 identification code FI F23G 5/04 ZAB F23G 5/04 ZABZ (58) Investigated field (Int.Cl. 7 , DB name) F23G 5/027 F23G 5/24 F23G 5/04 B09B 3/00 C10B 53/00 C10J 3/00 F23G 5/00
Claims (4)
酸素ガスを供給し、投入されたゴミが乾燥域、熱分解域
を経てガス化溶融されて取り出される熱分解域を備えた
ゴミのガス化溶融炉に於けるガス生成方法であって、 投入に先立ってゴミを非乾燥状態において６０〜８０ｋ
ｇ／ｃｍ ２ で圧縮して水分を含有したペレットに形成
し、 前記ペレットの中心が未乾燥状態で乾燥域を通過して熱
分解域に至り、該未乾燥状態のペレットの微量残留水分
が蒸発する温度域が６００℃〜１０００℃であり、前記
ゴミのペレットの水分が水性ガス化反応を促進してゴミ
の可燃分のＨ２のガス化効率を向上させるようにした、
熱分解域を備えたゴミのガス化溶融炉に於けるガス生成
方法。1. A pyrolysis zone is provided in which dust is introduced from the top of a vertical furnace, oxygen gas is supplied from the bottom of the furnace, and the introduced dust is gasified and melted through a drying zone and a pyrolysis zone to be taken out. This is a gas generation method in a gasification and melting furnace for garbage, wherein the garbage is dried in a non-dried state at a temperature of 60 to 80k prior to charging.
g / cm 2 to form pellets containing water, and the center of the pellets passes through a drying zone in an undried state and is heated.
Decomposition zone, trace residual moisture of the undried pellet
The temperature range in which is vaporized is 600 ° C. to 1000 ° C., and the moisture of the refuse pellets promotes the water gasification reaction to improve the gasification efficiency of flammable H 2 in the refuse.
Gas generation method in refuse gasification and melting furnace with pyrolysis zone.
がモル比で次式ＣＯ／（ＣＯ＋Ｈ２）＝０．３３〜０．
６７を充足するものである、請求項１の熱分解域を備え
たゴミのガス化溶融炉に於けるガス生成方法。 2. Among the components of the product gas, CO and H 2
Is a molar ratio of the following formula: CO / (CO + H 2 ) = 0.33-0.
67. A gas generation method in a refuse gasification and melting furnace provided with a pyrolysis zone according to claim 1 , which satisfies 67.
ペレットであって、未乾燥状態のゴミが、直径１５０ｍ
ｍ〜２５０ｍｍの球状又は円柱状に形成されている、ゴ
ミのペレット。3. A pellet of waste used in the method of claim 1 or 2, dust undried state, diameter 150m
A garbage pellet formed in a spherical or cylindrical shape of m to 250 mm.
ペレットであって、未乾燥状態のゴミが、一辺が３００
ｍｍ〜５００ｍｍの立方体又は一辺が３００ｍｍ〜５０
０ｍｍの断面を有する直方体で形成されている、ゴミの
ペレット。 4. A pellet of waste used in the method of claim 1 or 2, dust undried state, a side 300
mm to 500 mm cube or 300 mm to 50 mm on one side
Dust pellets formed of a rectangular parallelepiped having a cross section of 0 mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP36427097A JP3537305B2 (en) | 1997-11-28 | 1997-11-28 | Gas generation method in refuse gasification and melting furnace with pyrolysis zone and refuse pellets used in the method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP36427097A JP3537305B2 (en) | 1997-11-28 | 1997-11-28 | Gas generation method in refuse gasification and melting furnace with pyrolysis zone and refuse pellets used in the method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH11159721A JPH11159721A (en) | 1999-06-15 |
| JP3537305B2 true JP3537305B2 (en) | 2004-06-14 |
Family
ID=18481409
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP36427097A Expired - Fee Related JP3537305B2 (en) | 1997-11-28 | 1997-11-28 | Gas generation method in refuse gasification and melting furnace with pyrolysis zone and refuse pellets used in the method |
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| Country | Link |
|---|---|
| JP (1) | JP3537305B2 (en) |
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|---|---|---|---|---|
| CN112358155A (en) * | 2020-11-05 | 2021-02-12 | 北京一亚高科能源科技有限公司 | Sludge drying, gasifying and incinerating system and method thereof |
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1997
- 1997-11-28 JP JP36427097A patent/JP3537305B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH11159721A (en) | 1999-06-15 |
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