JPS6345880B2 - - Google Patents
Info
- Publication number
- JPS6345880B2 JPS6345880B2 JP13030880A JP13030880A JPS6345880B2 JP S6345880 B2 JPS6345880 B2 JP S6345880B2 JP 13030880 A JP13030880 A JP 13030880A JP 13030880 A JP13030880 A JP 13030880A JP S6345880 B2 JPS6345880 B2 JP S6345880B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- sludge
- dry distillation
- dry
- dehydrated sludge
- 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
- 239000010802 sludge Substances 0.000 claims description 47
- 238000000197 pyrolysis Methods 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 21
- 238000001035 drying Methods 0.000 claims description 13
- 238000002309 gasification Methods 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000004380 ashing Methods 0.000 claims description 7
- 239000010865 sewage Substances 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 239000010801 sewage sludge Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000007664 blowing Methods 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- JOPOVCBBYLSVDA-UHFFFAOYSA-N chromium(6+) Chemical compound [Cr+6] JOPOVCBBYLSVDA-UHFFFAOYSA-N 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Treatment Of Sludge (AREA)
Description
本発明は、下水処理により発生する余剰汚泥を
脱水して得られる脱水汚泥の灰化処理法、更に詳
しくは脱水汚泥を非酸化性雰囲気中で乾溜ガス化
し、発生したガスを汚泥の乾燥及びその他の熱源
として利用し、脱水汚泥を灰化処理する方法に関
するものである。
下水汚泥については、そのほとんど埋立て、海
洋投棄、焼却処分とされている。最近、都市廃棄
物等の焼却処分において、クロムの酸化反応によ
る６価クロムの生成、燃焼ガス中にNOx，SOx
の発生等の二次公害を防止する為に非酸化性雰囲
気中で乾溜することが一部に行なわれている。し
かしながらこれらの方法においては、乾溜の熱源
として重油等の補助燃料を使用しており下水汚
泥、都市廃棄物のエネルギーを充分回収している
とはいえない。
本発明の目的は、下水処理による脱水汚泥を補
助燃料を使用することなく回収される自己の熱源
により乾溜し、得られる乾溜ガスを脱水汚泥の乾
燥その他の熱源として有効に利用し、脱水汚泥を
灰化処理する方法を提供するにある。
本発明による下水汚泥の灰化処理法は、下水処
理により発生する余剰汚泥を脱水して得られる含
水率70〜75％の脱水汚泥を造粒し、後記の乾溜ガ
ス及びガス化ガスを燃焼して得られる熱源により
乾燥した後、後記のガス化ガスの顕熱により乾溜
し、得られた乾溜ガスの一部を前記の燃焼工程
に、残部を後記のガス化工程に使用し、乾溜残渣
を灰として排出すると共に、得られるガス化ガス
を前記乾燥工程に使用し、補助燃料を使用するこ
となく脱水汚泥を灰化処理することを特徴とする
方法である。
以下、本発明の方法を第１図の工程図に基づい
て詳述する。
下水処理により発生する余剰汚泥を脱水して得
られる脱水汚泥は一般に含水率70〜75％である。
本発明の方法においては含水率70〜75％の脱水汚
泥をそのまま使用して、補助燃料を使用すること
なく、脱水汚泥を灰化処理することができる。勿
論、脱水汚泥の含水率が更に低化していても差支
えなく、むしろ好ましい。この場合は、得られる
ガス化ガスを自からの灰化処理に全部使用するこ
となく、排熱ボイラに使用したり、ガスホルダー
に一時貯留し、他に利用することができる。
脱水汚泥は先ず造粒される。造粒には一般に押
出成形型造粒装置が使用される。造粒々径は乾溜
炉内の熱効率をよくする為に10mm以下とすること
が望ましく、また生成乾溜ガスに同伴されること
を防止する為に１mm以上とすることが好ましい。
具体的実施例としては、３mmφの粒又は５mmφ×
10mmＬの筒状体とした。
造粒された脱水汚泥は乾燥装置に送られる。乾
燥装置としては、一般に汚泥乾燥に用いられてい
るどのような乾燥機も使用することができる。熱
風吹込式撹拌、乾燥装置を使用し、乾溜ガス及び
ガス化ガスを燃焼して得られる約400℃の熱風を
熱風吹込口より送入し、撹拌機により撹拌されて
いる脱水汚泥と向流に熱交換させ、含水率約75％
の脱水汚泥を含水率約10％まで乾燥させた。出口
脱水汚泥の温度は約150℃であつた。
乾燥を終えた脱水汚泥は次に乾溜される。乾溜
装置の一例として堅型多段乾溜炉があげられる。
該炉は、次工程のガス化工程で発生する高温のガ
ス化ガスにより周囲より加熱される堅型炉で、中
心に0.5〜3rpmで回転する中心軸を有し、該中心
軸には羽根（仕切板）を有する円板が多段に取付
けられてあり、中心軸の回転により、炉上方から
供給される乾燥汚泥が最上段の円板より、その回
転及び羽根の作用により交互に内側及び外側に送
られることにより、逐次下段の円板に、それらの
内側及び外側に設けた落下口を通り落下し、この
間で乾燥汚泥は約450℃に加熱されて熱分解し、
その約63重量％がガス化され、乾溜ガスとし炉上
部より取出される。約37重量％のものは固定炭
素、未分解有機物、灰分を含む乾溜残渣として炉
底部より取出され、次工程のガス化工程に送られ
る。
ガス化工程においては、乾溜残渣中の固定炭素
のガス化が行なわれる。熱源として乾溜ガスが使
用される。乾溜ガスの燃焼によつて生じた炭酸ガ
ス、水蒸気、空気中の酸素、乾溜残渣中の固定炭
素が次の如き反応によりガス化ガスが発生する。
Ｃ＋１／２O2＝CO＋29400kcal／kmol
Ｃ＋CO2＝2CO−38200kcal／kmol
Ｃ＋H2O＝CO＋H2−28200kcal／kmol
このほか乾溜残渣中の未分解有機物及び乾溜ガ
ス中に含まれる炭化水素が水蒸気、酸素と反応し
て（二次）ガス化ガスが発生する。
CmHn＋mH2O→mCO＋2m＋ｎ／２H2
CmHn＋ｍ／２O2→mCO＋ｎ／２H2
発生したガス化ガスは乾溜工程でその顕熱を与
えた後、乾燥工程における乾燥熱源として燃焼さ
れる。脱水汚泥の灰化工程全体として熱の余剰が
あるときは、ガス化ガスの一部はホルダに貯えら
れ他に使用される。ガス化残渣の灰は炉底より取
出される。
次に、本発明の方法の実施例を述べる。
埼玉県某所の下水処理場の汚泥濃縮槽より濃縮
された汚泥（固形分２〜３％）をロールプレスタ
イプの脱水機により固形分25％まで脱水し、本発
明の方法の実施例に使用する脱水汚泥とした。脱
水汚泥の元素分析結果は第１表の通りであつた。
The present invention relates to a method for ashing dehydrated sludge obtained by dewatering surplus sludge generated in sewage treatment, and more specifically, to drying and gasifying dehydrated sludge in a non-oxidizing atmosphere, and using the generated gas to dry the sludge and other purposes. The present invention relates to a method for ashing dehydrated sludge by using it as a heat source. Most sewage sludge is disposed of by landfill, ocean dumping, or incineration. Recently, in the incineration of municipal waste, etc., hexavalent chromium is produced due to the oxidation reaction of chromium, and NOx and SOx are contained in the combustion gas.
In order to prevent secondary pollution such as the generation of carbon dioxide, dry distillation in a non-oxidizing atmosphere is sometimes carried out. However, these methods use auxiliary fuel such as heavy oil as a heat source for dry distillation, and it cannot be said that the energy from sewage sludge and municipal waste is sufficiently recovered. The purpose of the present invention is to dry distill dehydrated sludge from sewage treatment using its own heat source, which is recovered without using auxiliary fuel, and to effectively use the resulting dry distilled gas as a heat source for drying the dehydrated sludge and other purposes. To provide a method for ashing. The method for ashing sewage sludge according to the present invention involves granulating dehydrated sludge with a moisture content of 70 to 75% obtained by dewatering excess sludge generated during sewage treatment, and burning the dry distilled gas and gasified gas described below. After drying with a heat source obtained from the process, dry distillation is performed using the sensible heat of the gasified gas described below, and a part of the resulting dry distilled gas is used in the combustion process described above, the remainder is used in the gasification process described later, and the dry distillation residue is used. This method is characterized in that the dehydrated sludge is discharged as ash, and the obtained gasified gas is used in the drying step to ash the dehydrated sludge without using auxiliary fuel. Hereinafter, the method of the present invention will be explained in detail based on the process diagram of FIG. Dehydrated sludge obtained by dewatering surplus sludge generated during sewage treatment generally has a water content of 70 to 75%.
In the method of the present invention, dehydrated sludge with a moisture content of 70 to 75% can be used as it is, and the dehydrated sludge can be incinerated without using any auxiliary fuel. Of course, there is no problem even if the water content of the dehydrated sludge is further lowered, and it is even preferable. In this case, the obtained gasified gas does not need to be used entirely for the ashing process itself, but can be used in a waste heat boiler or temporarily stored in a gas holder for other uses. The dewatered sludge is first granulated. For granulation, an extrusion type granulation device is generally used. The diameter of the granules is preferably 10 mm or less in order to improve the thermal efficiency in the dry distillation furnace, and preferably 1 mm or more in order to prevent them from being entrained in the produced dry distillation gas.
As a specific example, 3mmφ grains or 5mmφ×
It was made into a cylindrical body of 10 mmL. The granulated dewatered sludge is sent to a drying device. As the drying device, any dryer commonly used for drying sludge can be used. Using a hot air blowing type stirring and drying device, hot air of approximately 400°C obtained by burning dry distilled gas and gasified gas is sent through the hot air blowing port, and flows countercurrently to the dehydrated sludge being stirred by the stirrer. Heat exchange, moisture content approximately 75%
The dehydrated sludge was dried to a moisture content of approximately 10%. The temperature of the dewatered sludge at the outlet was approximately 150°C. After drying, the dehydrated sludge is then dry distilled. An example of a dry distillation device is a vertical multistage dry distillation furnace.
This furnace is a vertical furnace that is heated from the surroundings by the high-temperature gasification gas generated in the next gasification step, and has a central shaft that rotates at 0.5 to 3 rpm, and a blade ( Discs with partition plates) are installed in multiple stages, and by the rotation of the central axis, the dry sludge supplied from above the furnace is alternately moved inside and outside from the top disc by the rotation of the central shaft and the action of the blades. As the sludge is fed, it sequentially falls to the lower discs through the drop ports provided on the inside and outside of the discs, during which time the dried sludge is heated to about 450°C and thermally decomposed.
Approximately 63% by weight of it is gasified and taken out from the upper part of the furnace as dry distilled gas. Approximately 37% by weight of the residue is removed from the bottom of the furnace as a dry distillation residue containing fixed carbon, undecomposed organic matter, and ash, and sent to the next gasification step. In the gasification step, fixed carbon in the dry distillation residue is gasified. Dry distillation gas is used as a heat source. Gasified gas is generated by the following reaction between carbon dioxide, water vapor, oxygen in the air, and fixed carbon in the dry distillation residue produced by combustion of the dry distillation gas. C+1/2O 2 = CO + 29400kcal/kmol C+CO 2 = 2CO-38200kcal/kmol C+H 2 O=CO+H 2 -28200kcal/kmol In addition, undecomposed organic matter in the dry distillation residue and hydrocarbons contained in the dry distillation gas react with water vapor and oxygen. (secondary) gasification gas is generated. CmHn+mH 2 O→mCO+2m+n/2H 2 CmHn+m/2O 2 →mCO+n/2H 2The generated gasified gas gives its sensible heat in the dry distillation process and is then burned as a drying heat source in the drying process. When there is a surplus of heat throughout the dewatered sludge ashing process, a portion of the gasified gas is stored in a holder and used for other purposes. The ash of gasification residue is taken out from the bottom of the furnace. Next, examples of the method of the present invention will be described. Sludge (solid content 2-3%) concentrated from a sludge thickening tank at a sewage treatment plant in Saitama Prefecture was dehydrated to a solid content of 25% using a roll press type dehydrator, and used in an example of the method of the present invention. It was made into dehydrated sludge. The results of elemental analysis of the dehydrated sludge are shown in Table 1.
【表】
この脱水汚泥を押し出出造粒機により粒径３mm
の粒状に成形し、ガス化ガスと乾溜ガスを燃焼し
て得られた400℃の熱風を使用し、熱風吹込式撹
拌装置で乾燥し、含水率10％の乾燥汚泥を得た。
次にこの乾燥汚泥を乾溜装置に入れ、450℃で
20分乾溜を行い、乾溜ガス、固定炭素及び灰を得
た。脱水汚泥無水物１Kg当りの乾溜ガス量及び各
成分ガス量は第２表の通りであつた。爾後の数値
（分析百分率を除く。）はすべて脱水汚泥１Kgを基
準とした数値で示す。また乾溜ガス出口温度は
200℃であつた。第３表に乾溜実験結果を示す。[Table] This dehydrated sludge is processed using an extrusion granulator with a particle size of 3 mm.
The sludge was molded into granules and dried with a hot air blowing stirring device using 400°C hot air obtained by burning gasified gas and dry distilled gas to obtain dried sludge with a moisture content of 10%. Next, this dried sludge was put into a dry distillation equipment and heated at 450℃.
Dry distillation was performed for 20 minutes to obtain dry distilled gas, fixed carbon, and ash. The amount of dry distillation gas and the amount of each component gas per 1 kg of anhydrous dehydrated sludge were as shown in Table 2. All subsequent values (excluding analytical percentages) are based on 1 kg of dehydrated sludge. In addition, the dry distillation gas outlet temperature is
It was 200℃. Table 3 shows the results of the dry distillation experiment.
【表】【table】
【表】
得られた乾溜ガスの発熱量を次の３式で算出す
ると第４表の如くなる。また乾溜ガス（713）
の燃焼に必要な空気量は2500となる。
CO＋１／２O2＝CO2＋68.2kcal／mol
H2＋１／２O2＝H2O＋57.6kcal／mol
CmHn＋（ｍ＋ｎ／４）O2
＝mCO2＋ｎ／２H2O＋Hg
（Hg：総発熱量）[Table] Table 4 shows the calorific value of the obtained dry distilled gas when calculated using the following three formulas. Also dry distilled gas (713)
The amount of air required for combustion is 2500. CO+1/2O 2 = CO 2 +68.2kcal/mol H 2 +1/2O 2 = H 2 O+57.6kcal/mol CmHn+(m+n/4)O 2
= mCO 2 + n/2H 2 O + Hg (Hg: total calorific value)
【表】
次に乾溜残渣中の固定炭素234ｇに対して水蒸
気180ｇ及び炭酸ガス440ｇの割合で1000℃の下で
30分反応させ固定炭素のガス化を行つた。この時
の反応は水性ガス反応
Ｃ＋H2O＝CO＋H2−28.2kcal／mol
と発生炉ガス反応
Ｃ＋CO2＝2CO−38.2kcal／mol
とが同時に行なわれる。
ガス化ガスは3573／無水汚泥Kg得られ、その
分析結果及び発熱量を第５表及び第６表に示す。
なお、ガス化ガスの発熱量の算出には乾溜ガスに
おけると同じ反応式を用いた。全排出灰分中の六
価クロムの生成量は、0.8mg／無水汚泥Kgであつ
た。[Table] Next, 180g of water vapor and 440g of carbon dioxide were added to 234g of fixed carbon in the dry distillation residue at 1000℃.
The reaction was carried out for 30 minutes to gasify the fixed carbon. In this reaction, a water gas reaction C+H 2 O=CO+H 2 -28.2 kcal/mol and a generator gas reaction C+CO 2 =2CO-38.2 kcal/mol are carried out simultaneously. Gasification gas was obtained in an amount of 3573 kg/kg of anhydrous sludge, and the analysis results and calorific value are shown in Tables 5 and 6.
Note that the same reaction equation as for dry distillation gas was used to calculate the calorific value of gasified gas. The amount of hexavalent chromium produced in the total discharged ash was 0.8 mg/Kg of anhydrous sludge.
【表】【table】
【表】
実施例における各工程及び全体の熱収支は次の
如くなる。基準は無水汚泥１Kg当りのkcalであ
る。[Table] The heat balance for each step and the whole in the example is as follows. The standard is kcal per 1 kg of anhydrous sludge.
【表】【table】
【表】【table】
【表】【table】
【表】【table】
【表】【table】
【表】
全体の熱収支を熱流れ図（単位kcal／無水汚泥
Kg）で示すと第２図の如くなる。
本発明の方法は以上の如く構成されているの
で、汚泥の保有熱を有効に利用し、外部から熱の
供給を受けることなく脱水汚泥を灰化処理するこ
とができる。また、脱水汚泥の含水率が低下した
場合など、回収熱に余剰を生じるので、ガス化ガ
スを貯留して他に転用することもできる。[Table] Heat flow diagram showing the overall heat balance (unit: kcal/anhydrous sludge
When expressed in kg), it is shown in Figure 2. Since the method of the present invention is configured as described above, it is possible to effectively utilize the heat retained in the sludge and to incinerate dehydrated sludge without receiving heat from the outside. In addition, when the water content of dehydrated sludge decreases, a surplus of recovered heat is generated, so the gasified gas can be stored and used for other purposes.
図面は本発明の方法の一実施例を示すもので、
第１図は工程図、第２図は熱流れ図である。
The drawing shows an embodiment of the method of the invention,
Figure 1 is a process diagram, and Figure 2 is a heat flow diagram.
Claims (1)
得られる含水率70〜75％の脱水汚泥を造粒し、後
記の乾溜ガス及びガス化ガスを燃焼して得られる
熱源により乾燥した後、後記のガス化ガスの顕熱
により乾溜し、得られた乾溜ガスの一部を前記の
乾燥工程に、残部を後記のガス化工程に使用し、
乾溜残渣を前記の乾溜ガスの残部及び空気により
ガス化し、残渣を灰として排出すると共に、得ら
れるガス化ガスを前記乾燥工程に使用し、補助燃
料を使用することなく脱水汚泥を灰化処理するこ
とを特徴とする下水汚泥の灰化処理法。1 Dehydrated sludge with a water content of 70 to 75% obtained by dewatering surplus sludge generated by sewage treatment is granulated, dried using a heat source obtained by burning the dry distillation gas and gasification gas described later, and then Dry distillation is performed using sensible heat of the gasified gas, and a part of the obtained dry distilled gas is used in the drying process described above, and the remainder is used in the gasification process described later,
Gasifying the dry distillation residue with the remainder of the dry distillation gas and air, discharging the residue as ash, and using the obtained gasified gas in the drying process to ash the dehydrated sludge without using auxiliary fuel. An ashing method for sewage sludge characterized by the following.
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13030880A JPS5756097A (en) | 1980-09-19 | 1980-09-19 | Method for laying in ashes of sewer sludge |
| GB8127078A GB2087054B (en) | 1980-09-19 | 1981-09-08 | Method and apparatus for incinerating sewage sludge |
| DE19813137227 DE3137227A1 (en) | 1980-09-19 | 1981-09-18 | METHOD AND DEVICE FOR ASHING CLEANING SLUDGE |
| FR8117632A FR2490783A1 (en) | 1980-09-19 | 1981-09-18 | PROCESS AND APPARATUS FOR THE INCINERATION OF RESIDUAL SLUDGE |
| US06/303,988 US4398476A (en) | 1980-09-19 | 1981-09-21 | Method for incinerating sewage sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13030880A JPS5756097A (en) | 1980-09-19 | 1980-09-19 | Method for laying in ashes of sewer sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5756097A JPS5756097A (en) | 1982-04-03 |
| JPS6345880B2 true JPS6345880B2 (en) | 1988-09-12 |
Family
ID=15031207
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13030880A Granted JPS5756097A (en) | 1980-09-19 | 1980-09-19 | Method for laying in ashes of sewer sludge |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5756097A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03108073U (en) * | 1990-02-19 | 1991-11-07 |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59136197A (en) * | 1983-01-25 | 1984-08-04 | Tsuneo Okamoto | Thermal decomposing device for activated sludge |
| JPS6044096A (en) * | 1983-08-19 | 1985-03-08 | Tsuneo Okamoto | Thermal decomposition apparatus of activated sludge |
| JPH059483U (en) * | 1991-07-18 | 1993-02-09 | 富士車輌株式会社 | Distiller for dry cleaning machine |
| JP5846728B2 (en) * | 2010-09-03 | 2016-01-20 | 株式会社御池鐵工所 | Carbonization method and carbonization plant for organic waste |
-
1980
- 1980-09-19 JP JP13030880A patent/JPS5756097A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03108073U (en) * | 1990-02-19 | 1991-11-07 |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5756097A (en) | 1982-04-03 |
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