JPH0145512B2 - - Google Patents
Info
- Publication number
- JPH0145512B2 JPH0145512B2 JP266682A JP266682A JPH0145512B2 JP H0145512 B2 JPH0145512 B2 JP H0145512B2 JP 266682 A JP266682 A JP 266682A JP 266682 A JP266682 A JP 266682A JP H0145512 B2 JPH0145512 B2 JP H0145512B2
- Authority
- JP
- Japan
- Prior art keywords
- coke oven
- coal
- charged
- drying
- coke
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000000571 coke Substances 0.000 claims description 85
- 239000003245 coal Substances 0.000 claims description 64
- 238000001035 drying Methods 0.000 claims description 38
- 239000000843 powder Substances 0.000 claims description 26
- 238000010438 heat treatment Methods 0.000 claims description 17
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 10
- 238000010298 pulverizing process Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 description 22
- 239000000428 dust Substances 0.000 description 20
- 238000012360 testing method Methods 0.000 description 4
- 239000011280 coal tar Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000004484 Briquette Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001599 direct drying Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Solid Fuels And Fuel-Associated Substances (AREA)
- Coke Industry (AREA)
Description
この発明は、コークスの製造法に係り、特に、
コークス炉装入炭をコークス炉に装入する前に予
めこのコークス炉装入炭を乾燥処理するコークス
の製造法に関する。
コークスの製造に際して、予めコークス炉装入
炭を乾燥処理することはコークス炉で石炭を乾留
するのに要する熱量の節約になり、コークス製造
において極めて有利であることが知られている。
そこで、従来においては、コークス炉装入炭に直
接熱風気流を接触させる気流乾燥法や流動床法、
あるいは熱交換器を用いて熱媒体を間接的にコー
クス炉装入炭と接触させて熱交換させることによ
り乾燥処理する間接加熱乾燥法等、多くの方法が
提案されている。
しかしながら、コークス炉装入炭の乾燥処理法
として、熱風気流を直接接触させる気流乾燥法や
流動床法を採用した場合、例えば特公昭49−
28241号公報に記載されているように、コークス
化のために粒径3mm以下の程度に破砕された石炭
粒子は熱風気流によつて破砕時に発生したミクロ
ンオーダーの微粉末をほとんど完全に飛散排出
し、また直接乾燥の際更に粉砕されて微粉末の量
は原粒石炭の30重量%にも及ぶことが記載されて
いる。そのためこの微粉末を捕集するために集塵
機を多段に設置したり、多種多様の集塵機を使用
することが必要になつて集塵設備が大がかりにな
るほか、捕集した微粉末を再利用するためにこれ
に重質油を添加して造粒する等附帯する多くの手
間と設備を要するという問題があつた。
また、コークス炉装入炭の乾燥処理法として、
間接加熱乾燥法を採用した場合、気流乾燥法や流
動床法のように熱風気流によつて微粉末が大量に
乾燥機から持ち出されるということは防止できて
も、コークス炉装入炭が過度に乾燥処理される
と、このコークス炉装入炭の搬送工程およびコー
クス炉装入工程で大量の粉塵が発生し、作業環境
の汚染が生ずるために搬送工程を密閉系にした
り、集塵を強化しなければならなかつた。
このため、従来においては、コークス炉装入炭
の乾燥処理の程度は水分含有率が約4〜6重量%
までが限度とされていたが、この程度の乾燥処理
であつてもかなりの粉塵の発生は避けられず、ま
たこの過程の乾燥処理ではコークス炉装入炭を予
め乾燥処理することによるメリツトを充分に活用
しているとは言えない。
本発明者等は、かかる観点に鑑み、乾燥処理に
よる微粉末の増加をできるだけ抑制し、しかも、
コークス炉装入炭を予め乾燥処理することによる
メリツトが充分に発揮し得る程度まで乾燥しても
搬送やコークス炉への装入時における粉塵の発生
を効果的に防止することができるコークスの製造
法について鋭意研究を重ねた結果、コークス炉装
入炭の搬送時やコークス炉への装入時に発生する
粉塵のほとんどが約100μ以下の微粉末であり、
また、間接加熱乾燥法により乾燥処理した場合に
は気流乾燥法や流動床法により乾燥処理した場合
に比べてかかる微粉末の生成が著るしく低く、さ
らに、コークス炉装入炭を間接加熱乾燥法で乾燥
処理した後にこれを分級してかかる微粉末を可及
的に分離除去すれば、搬送時やコークス炉への装
入時における粉塵の発生を未然に防止することが
できることを見い出し、本発明を完成したもので
ある。
すなわち、本発明は、コークス炉装入炭の一部
又は全部を間接加熱乾燥し、この乾燥処理したコ
ークス炉装入炭を分級して約100μ以下の微粉末
を可及的に分離除去し、この微粉末を除去したコ
ークス炉装入炭をコークス炉に装入することを特
徴とするコークスの製造法であり、好ましい実施
態様としては、間接加熱乾燥を乾燥途中における
石炭粒子相互間の衝突による微粉末化の少ないド
ラム型乾燥機で行うことであり、また、分級を風
力分級機で行うことである。
本発明において、コークス炉装入炭とは、コー
クス製造の際にコークス炉に装入される通常の装
入炭をいい、コークス製造用の粉炭のほか、この
粉炭に成型炭や造粒炭その他粘結性補填材等が一
部配合されたものも包含される。
また、本発明の方法を遂行する上で、コークス
炉装入炭の乾燥処理は、その全量に対して行つて
もよいほか、その一部に対して行つてもよい。す
なわち、コークスの製造に際して、一部のコーク
ス炉装入炭に対して乾燥処理を施し、この乾燥処
理したコークス炉装入炭を残りのコークス炉装入
炭と混合し、全体として目的とする水分含有量に
調整してからコークス炉に装入するいわゆる装入
炭一部乾燥法が提案されているが、この装入炭一
部乾燥法によるコークスの製造においても本発明
方法を適用することができる。しかしながら、本
発明方法によれば、乾燥処理したコークス炉装入
炭中の約100μ以下の微粉末を分級して可及的に
分離除去することにより粉塵の発生を未然に防止
し得るものであるから、コークス炉装入炭の水分
含有率をできるだけ低下させ、コークス炉装入炭
を予め乾燥処理することによるメリツトを充分に
発揮させるのがよく、好ましくはコークス炉装入
炭の全量を乾燥処理することである。
コークス炉装入炭の間接加熱乾燥に使用される
間接加熱乾燥機としては、従来公知のものを適宜
使用し得るが、石炭粒子に激しい衝撃を与えた
り、また、石炭粒子相互間で激しく衝突して破砕
されることにより微粉末を大量に生成するような
ものは好ましくない。この間接加熱乾燥機として
は、チユーブ側に熱媒体を循環させてシエル側に
コークス炉装入炭を装入するドラム型乾燥機や撹
拌翼型乾燥機があげられる。粉塵発生の原因とな
る約100μ以下の微粉末の生成をできるだけ抑制
する上で好ましいものとしては、例えば、回転す
る横型のドラム内部をコークス炉装入炭がゆつく
りと通過する間にドラム外部を循環する熱媒体と
熱交換させてこのコークス炉装入炭を連続的に乾
燥処理するドラム型乾燥機がある。
本発明方法において、コークス炉装入炭をどの
程度まで乾燥処理するかについては特に制限はな
いが、少くとも予めコークス炉装入炭を乾燥処理
することによるメリツトが充分に発揮される程度
まで行うのがよく、通常水分含有率が4〜5重量
%以下、好ましくは2重量%以下に減少するまで
行うのがよい。
この乾燥処理したコークス炉装入炭を分級して
約100μ以下の微粉末を可及的に分離除去するた
めの分級手段としては、如何なるタイプの分級機
であつてもよいが、約100μ以下の微粉末を効率
良く分級することができ、また、目詰り等のトラ
ブルが少ない風力分級機が好ましい。この分級手
段は、通常、粉塵の飛散を防止するために上記間
接加熱乾燥機の出口に直結されるか、あるいは、
ダクト等の手段で連結される。
なお、この分級手段により分離除去されて回収
された約100μ以下の微粉末については、タール
や重質油の添加等によつて飛散防止処理を施した
り、あるいは成型炭用粉炭中に混合したり、その
他造粒してコークス炉装入炭中に戻すか、あるい
は、別途燃料等として再利用される。
本発明方法によれば、コークス炉装入炭の搬送
時やコークス炉への装入時において粉塵発生の原
因となつている約100μ以下の微粉末の量を著る
しく減少させることができ、また、この約100μ
以下の微粉末を分級により可及的に分離除去する
ので、分級手段のほかには大がかりな集塵設備等
を必要とせず、また、コークス炉装入炭の搬送時
やコークス炉への装入時における粉塵の発生をそ
の根本から防止することができるので乾燥処理後
のコークス炉装入炭の取扱いが極めて容易にな
る。しかも、コークス炉装入炭をコークス炉に装
入する際に発生した粉塵がコークス炉の上昇管部
を上昇してドライメーンに侵入することにより生
じるコールタール中のタールスラツジの量も著し
く減少し、これによつてコールタールの貯蔵や精
製等の処理が著しく容易になる。しかも、本発明
方法によれば、コークス炉装入炭を予め乾燥処理
することによるメリツトが充分に発揮される程度
にまでこのコークス炉装入炭を乾燥処理すること
ができるので、工業的に有利な乾燥コークス炉装
入炭を使用するコークスの製造を円滑に行うこと
ができ、極めてその実用的価値の高いものであ
る。
以下、本発明の方法を試験例及び実施例に基づ
いて説明する。
〔A〕 粉塵の粒度分布測定試験
3mm以下の粒径が88重量%以上となるように
粉砕した粉炭を水分含有率4.2重量%まで乾燥
し、コンベア速度100m分、装入炭量300T/時
でベルト乗継部で自由落下させて発塵させ、飛
散した粉塵を捕集してその粒度分布を測定し
た。結果は表に示す通りであり、発生した粉塵
の99.3重量%が粒径100μ以下の微粉末であつ
た。
The present invention relates to a method for producing coke, and in particular,
The present invention relates to a coke manufacturing method in which coke oven charged coal is subjected to drying treatment before being charged into the coke oven. It is known that drying coal charged in a coke oven in advance saves the amount of heat required for carbonizing the coal in the coke oven, and is extremely advantageous in coke production.
Therefore, in the past, methods such as the flash drying method in which hot air is brought into direct contact with the coal charged in the coke oven, the fluidized bed method,
Alternatively, many methods have been proposed, such as an indirect heating drying method in which a heat exchanger is used to indirectly bring a heat medium into contact with coal charged in a coke oven for heat exchange, thereby drying the coke oven. However, when a flash drying method or a fluidized bed method in which hot air is brought into direct contact with the coal charged in a coke oven is used, for example,
As described in Publication No. 28241, coal particles that have been crushed to a particle size of 3 mm or less for coking are almost completely dispersed and discharged by the hot air flow, and the micron-order fine powder generated during crushing is almost completely dispersed. It is also stated that the amount of fine powder that is further pulverized during direct drying is as much as 30% by weight of the raw coal. Therefore, in order to collect this fine powder, it is necessary to install dust collectors in multiple stages or use a wide variety of dust collectors, making the dust collection equipment large-scale.In addition, it is necessary to reuse the collected fine powder. However, there was a problem in that it required a lot of incidental labor and equipment, such as adding heavy oil to granulation. In addition, as a method of drying coal charged in a coke oven,
When indirect heating drying method is adopted, although it is possible to prevent a large amount of fine powder from being taken out of the dryer by hot air flow as in flash drying method or fluidized bed method, it is possible to prevent excessive amount of coal charged in coke oven. When drying is performed, a large amount of dust is generated during the coke oven charging process and the coke oven charging process, which contaminates the working environment. I had to. For this reason, in the past, the degree of drying treatment of coal charged in a coke oven was such that the moisture content was approximately 4 to 6% by weight.
However, even with this level of drying, it is unavoidable that a considerable amount of dust is generated, and in this drying process, the benefits of pre-drying the coal charged in the coke oven cannot be fully exploited. I cannot say that it is being used effectively. In view of this point of view, the present inventors suppressed the increase in fine powder due to drying treatment as much as possible, and
Production of coke that can effectively prevent the generation of dust during transportation and charging into a coke oven even if the coke oven charging coal is dried to the extent that the benefits of pre-drying can be fully demonstrated. As a result of extensive research into the method, we have found that most of the dust generated during the transportation of coke oven charging coal and charging into a coke oven is fine powder of approximately 100 microns or less.
In addition, when the drying process is performed using the indirect heating drying method, the generation of fine powder is significantly lower than when drying processing is performed using the flash drying method or the fluidized bed method. We have discovered that if we separate and remove as much of the fine powder as possible after drying it using a method, it is possible to prevent the generation of dust during transportation or charging into a coke oven. It is a completed invention. That is, the present invention involves drying part or all of the coal charged in a coke oven by indirect heating, and classifying the dried coal charged in a coke oven to separate and remove fine powder of about 100μ or less as much as possible. This coke production method is characterized by charging the coke oven charged coal from which the fine powder has been removed into a coke oven, and in a preferred embodiment, indirect heating drying is performed by collision between coal particles during drying. The process is carried out using a drum-type dryer that produces less pulverization, and the classification is performed using a wind classifier. In the present invention, coke oven charging coal refers to normal charging coal that is charged into a coke oven during coke production, and includes pulverized coal for coke production, briquette coal, granulated coal, etc. Those containing a part of caking filler material are also included. Further, in carrying out the method of the present invention, the drying treatment of the coal charged in the coke oven may be performed not only on the entire amount thereof, but also on a portion thereof. In other words, when producing coke, some of the coke oven coal is subjected to drying treatment, and this dried coke oven coal is mixed with the remaining coke oven coal to achieve the desired moisture content as a whole. A so-called charging coal partial drying method has been proposed in which the charging coal content is adjusted and then charging into a coke oven, but the method of the present invention can also be applied to the production of coke by this charging coal partial drying method. can. However, according to the method of the present invention, the generation of dust can be prevented by classifying and removing as much fine powder as possible of about 100 μm or less in the dry-treated coal charged in a coke oven. Therefore, it is best to reduce the moisture content of the coal charged in a coke oven as much as possible and fully utilize the benefits of pre-drying the coal charged in a coke oven. Preferably, the entire amount of coal charged in a coke oven is subjected to drying treatment. It is to be. As the indirect heating dryer used for indirect heating drying of coal charged in a coke oven, any conventionally known indirect heating dryer may be used as appropriate. It is not preferable to use a material that produces a large amount of fine powder when crushed. Examples of this indirect heating dryer include a drum type dryer and a stirring vane type dryer, which circulate a heat medium through the tube side and charge coke oven charging coal into the shell side. In order to suppress the generation of fine powder of approximately 100 μm or less, which causes dust, it is preferable to, for example, prevent the outside of the coke oven from passing through the rotating horizontal drum while the charged coal slowly passes through the inside of the rotating horizontal drum. There is a drum type dryer that continuously dries the coal charged in a coke oven by exchanging heat with a circulating heat medium. In the method of the present invention, there is no particular restriction on the extent to which the coke oven charged coal is dried, but it is carried out at least to the extent that the benefits of drying the coke oven charged coal are fully demonstrated. It is recommended that the water content be reduced to 4 to 5% by weight or less, preferably 2% by weight or less. Any type of classifier may be used as the means for classifying this dry coke oven charging coal to separate and remove as much fine powder as possible with a particle size of about 100μ or less. A wind classifier is preferred because it can efficiently classify fine powder and causes fewer problems such as clogging. This classification means is usually directly connected to the outlet of the indirect heating dryer to prevent dust from scattering, or
They are connected by means such as ducts. The fine powder of approximately 100 microns or less separated and removed by this classification method is treated to prevent scattering by adding tar or heavy oil, or mixed into powdered coal for molded coal. , otherwise granulated and returned to the coal charged in a coke oven, or reused separately as fuel, etc. According to the method of the present invention, it is possible to significantly reduce the amount of fine powder of about 100 microns or less, which causes dust generation when transporting coke oven charging coal or charging it into a coke oven, Also, this approximately 100μ
Since the following fine powders are separated and removed as much as possible by classification, there is no need for large-scale dust collection equipment other than the classification means, and it is also possible to remove the fine powder when transporting coal to be charged into a coke oven or charging it into a coke oven. Since the generation of dust during drying can be fundamentally prevented, handling of the coke oven charged coal after drying becomes extremely easy. Moreover, the amount of tar sludge in the coal tar that is generated when the dust generated when charging coke oven coal into the coke oven rises up the riser pipe section of the coke oven and enters the dry main is also significantly reduced. This greatly facilitates processing such as storage and purification of coal tar. Moreover, according to the method of the present invention, it is possible to dry the coke oven charged coal to the extent that the benefits of drying the coke oven charged coal in advance are fully exhibited, which is industrially advantageous. It is possible to smoothly produce coke using dry coal charged in a coke oven, and it has extremely high practical value. The method of the present invention will be explained below based on Test Examples and Examples. [A] Dust particle size distribution measurement test Powdered coal that has been crushed so that the particle size of 3 mm or less is 88% by weight or more is dried to a moisture content of 4.2% by weight, conveyor speed is 100 m, and coal charge is 300 T/hour. The particles were allowed to fall freely at the belt transition area to generate dust, and the scattered dust was collected and its particle size distribution was measured. The results are shown in the table, and 99.3% by weight of the generated dust was fine powder with a particle size of 100μ or less.
【表】
〔B〕 実施例
図に示すように、コークス炉装入炭の供給ラ
イン1にドラム型間接加熱乾燥機2と風力分級
機3とを組み込み、ドラム型間接加熱乾燥機2
にはコークス炉4の上昇管部5に設けたコーク
ス炉ガス顕熱回収装置6を循環する熱媒体(新
日本製鉄化学工業株式会社製商品名サームエ
ス、比熱0.6kcal/Kg℃)により乾燥のための
熱量を供給するようにした。また、上記風力分
級機3の分級点については、上記試験例の結果
を考慮して100μとした。
上記試験例で用いたものと同じコークス炉装
入炭を供給ライン1に流し、その全量をドラム
型間接加熱乾燥機2で水分含有率2重量%に乾
燥処理し、次いで風力分級機3で約100μ以下
の微粉末をを可及的に分離除去し、この微粉末
を除去したコークス炉装入炭をコークス炉4に
装入した。風力分級機3で捕集された約100μ
以下の微粉末はコークス炉装入炭全量の約5重
量%であり、また、風力分級機3からコークス
炉4に至るまでの搬送工程及びコークス炉4内
への装入工程における粉塵の発生はほとんど認
められなかつた。[Table] [B] Example As shown in the figure, a drum-type indirect heating dryer 2 and a wind classifier 3 are installed in a coke oven charging coal supply line 1, and a drum-type indirect heating dryer 2 is installed.
For drying, a heating medium (trade name: THERM-S, manufactured by Nippon Steel Chemical Industry Co., Ltd., specific heat: 0.6 kcal/Kg°C) circulates through a coke oven gas sensible heat recovery device 6 installed in the riser pipe section 5 of the coke oven 4. of heat. Further, the classification point of the wind classifier 3 was set to 100μ in consideration of the results of the test example. The same coke oven charge coal used in the above test example is passed through the supply line 1, and the entire amount is dried in a drum-type indirect heating dryer 2 to a moisture content of 2% by weight, and then in a wind classifier 3 to approximately 2% by weight. Fine powder of 100 μm or less was separated and removed as much as possible, and the coke oven charging coal from which this fine powder had been removed was charged into a coke oven 4. Approximately 100μ collected by wind classifier 3
The following fine powder accounts for approximately 5% by weight of the total amount of coal charged in the coke oven, and dust is generated during the transportation process from the wind classifier 3 to the coke oven 4 and the charging process into the coke oven 4. It was hardly recognized.
図は本発明の実施例に係るコークスの製造法を
説明するための説明図である。
符号説明、1……コークス炉装入炭供給ライ
ン、2……ドラム型間接加熱乾燥機、3……風力
分級機、4……コークス炉、6……コークス炉ガ
ス顕熱回収装置。
The figure is an explanatory diagram for explaining a method for producing coke according to an embodiment of the present invention. Description of symbols: 1... Coke oven charging coal supply line, 2... Drum type indirect heating dryer, 3... Wind classifier, 4... Coke oven, 6... Coke oven gas sensible heat recovery device.
Claims (1)
乾燥し、この乾燥処理したコークス炉装入炭を分
級して約100μ以下の微粉末を可及的に分離除去
し、この微粉末を除去したコークス炉装入炭をコ
ークス炉に装入することを特徴とするコークスの
製造法。 2 コークス炉装入炭の間接加熱乾燥は、その乾
燥過程における石炭粒子の微粉末化が少いドラム
型乾燥機で行う特許請求の範囲第1項記載のコー
クスの製造法。 3 乾燥処理したコークス炉装入炭の分級は、風
力分級機で行う特許請求の範囲第1項又は第2項
記載のコークスの製造法。[Claims] 1. Part or all of the coal charged in a coke oven is dried by indirect heating, and the dried coal charged in a coke oven is classified to separate and remove fine powder of about 100μ or less as much as possible. A method for producing coke, which comprises charging the coke oven charging coal from which the fine powder has been removed into a coke oven. 2. The method for producing coke according to claim 1, wherein the indirect heating drying of the coal charged in the coke oven is carried out in a drum type dryer, which reduces the pulverization of coal particles during the drying process. 3. The method for producing coke according to claim 1 or 2, wherein the dry-treated coal charged in a coke oven is classified using a wind classifier.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP266682A JPS58120690A (en) | 1982-01-13 | 1982-01-13 | Preparation of coke |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP266682A JPS58120690A (en) | 1982-01-13 | 1982-01-13 | Preparation of coke |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS58120690A JPS58120690A (en) | 1983-07-18 |
JPH0145512B2 true JPH0145512B2 (en) | 1989-10-03 |
Family
ID=11535633
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP266682A Granted JPS58120690A (en) | 1982-01-13 | 1982-01-13 | Preparation of coke |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS58120690A (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS63291991A (en) * | 1987-05-26 | 1988-11-29 | Mitsubishi Heavy Ind Ltd | Drying of coal |
JP4787528B2 (en) * | 2005-04-08 | 2011-10-05 | 新日鉄エンジニアリング株式会社 | Wet raw material drying apparatus and drying method |
-
1982
- 1982-01-13 JP JP266682A patent/JPS58120690A/en active Granted
Also Published As
Publication number | Publication date |
---|---|
JPS58120690A (en) | 1983-07-18 |
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