JPH0318956B2 - - Google Patents
Info
- Publication number
- JPH0318956B2 JPH0318956B2 JP14572181A JP14572181A JPH0318956B2 JP H0318956 B2 JPH0318956 B2 JP H0318956B2 JP 14572181 A JP14572181 A JP 14572181A JP 14572181 A JP14572181 A JP 14572181A JP H0318956 B2 JPH0318956 B2 JP H0318956B2
- Authority
- JP
- Japan
- Prior art keywords
- digestion
- digestion tank
- liquid
- anaerobic
- tank
- 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 - Lifetime
Links
- 230000029087 digestion Effects 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 23
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 22
- 239000010802 sludge Substances 0.000 claims description 18
- 238000001914 filtration Methods 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 11
- 230000001079 digestive effect Effects 0.000 claims description 9
- 239000004744 fabric Substances 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 239000002351 wastewater Substances 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims 1
- 239000007787 solid Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 239000000758 substrate Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 239000010800 human waste Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000004576 sand 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
Description
【発明の詳細な説明】
この発明は、し尿のような高濃度有機性廃水を
嫌気性消化処理する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for anaerobically digesting highly concentrated organic wastewater such as human waste.
高濃度有機性廃水に対して適用される嫌気性消
化法では、加温、撹拌によつて基質と嫌気性細菌
とを接触させ、基質の分解とメタンガス等の代謝
生産物の生成を促す作用と、嫌気性細菌を多量に
含有する汚泥と脱離液とを分離する作用とによつ
て処理が行われる。この方法にもとづく従来の処
理プロセスを第１図に示す。原水は、まず第１消
化槽ａで嫌気性消化処理を受けたのち、第２消化
槽ｂに送られ、消化汚泥と脱離液との分離が行わ
れる。そして脱離液は次段の処理工程に送られ、
消化汚泥の一部は第１消化槽ａに返送される。こ
の消化汚泥と脱離液との分離は、従来の方法では
静置による沈降分離作用によつているため、その
分離効果は、長い滞留時間をかけても充分でない
場合が多く、脱離液とともに多量の固形物が流出
するという欠点がある。とくに被処理液中の基質
が難分解性で嫌気性細菌の増殖速度が遅くなる場
合には、細菌の脱離液への流出は消化処理の過負
荷状態を招き、消化効率の低下の原因となる。ま
た細菌の流出を防止するために沈降分離時間をい
たずらに長くすると、スカム発生頻度を高めてガ
ス発生を抑制したり、被処理液中に混入している
砂などの固形物が沈積して槽の有効容積を縮少す
る等の別の欠点を生じる。 In the anaerobic digestion method applied to highly concentrated organic wastewater, heating and stirring are used to bring the substrate into contact with anaerobic bacteria, which promotes the decomposition of the substrate and the production of metabolic products such as methane gas. The treatment is carried out by separating sludge containing a large amount of anaerobic bacteria from a desorbed liquid. A conventional treatment process based on this method is shown in FIG. The raw water is first subjected to an anaerobic digestion treatment in the first digestion tank a, and then sent to the second digestion tank b, where the digested sludge and the desorbed liquid are separated. The desorbed liquid is then sent to the next treatment step,
A portion of the digested sludge is returned to the first digestion tank a. In conventional methods, this separation of the digested sludge and the desorbed liquid is based on the sedimentation separation effect caused by standing still, and the separation effect is often not sufficient even after a long residence time, and the separated liquid and the desorbed liquid The disadvantage is that a large amount of solid matter flows out. In particular, if the substrate in the liquid to be treated is difficult to decompose and the growth rate of anaerobic bacteria is slowed down, the flow of bacteria into the desorption liquid may lead to overload of the digestion process and cause a decrease in digestion efficiency. Become. Furthermore, if the sedimentation separation time is unnecessarily prolonged in order to prevent the outflow of bacteria, the frequency of scum generation will increase and gas generation will be suppressed, and solids such as sand mixed in the liquid to be treated will settle and cause This results in other disadvantages such as reducing the effective volume of the device.
この発明は、上記のような欠点を伴なわずに、
嫌気性消化反応の効率を高め、後続の処理の負荷
を低減させることができる嫌気性消化方法を提供
することを目的としている。 This invention does not have the above-mentioned drawbacks, and
The purpose of the present invention is to provide an anaerobic digestion method that can increase the efficiency of the anaerobic digestion reaction and reduce the burden of subsequent processing.
つぎにこの発明方法の工程の一例を図面にした
がつて説明する。第２図において、符号１は第１
消化槽、２は遠心濾過濃縮機、３は第２消化槽を
それぞれ示し、遠心濾過濃縮機２の気密なハウジ
ングの内部は、連通管４を介して第１消化槽１の
上部に連通している。 Next, an example of the steps of the method of this invention will be explained with reference to the drawings. In FIG. 2, numeral 1 indicates the first
2 is a centrifugal filtration and concentration machine, and 3 is a second digestion tank. There is.
し尿のような高濃度有機性廃水は、まず第１消
化槽１内に導入され、嫌気性条件のもとで消化処
理されることによつてメタン発酵を行う。そして
消化液は、遠心濾過濃縮機２に送られ、濃縮液の
一部は第１消化槽１に返送され、残部は余剰汚泥
として排出される。また瀘液は第２消化槽３に送
られ、さらに消化処理されるとともに消化汚泥の
沈澱分離が行われる。ここで生じた脱離液は後続
の処理工程に送られ、消化汚泥は遠心濾過濃縮機
２からの濃縮液とともに余剰汚泥として排出され
る。但し、第２消化槽３は、設けない場合もあ
る。 Highly concentrated organic wastewater such as human waste is first introduced into the first digestion tank 1, and is digested under anaerobic conditions to perform methane fermentation. The digestive fluid is then sent to the centrifugal filtration/concentrator 2, a portion of the concentrated fluid is returned to the first digestion tank 1, and the remainder is discharged as surplus sludge. The filtrate is also sent to the second digestion tank 3, where it is further digested and the digested sludge is separated by sedimentation. The desorbed liquid generated here is sent to the subsequent treatment process, and the digested sludge is discharged as surplus sludge together with the concentrated liquid from the centrifugal filtration thickener 2. However, the second digestion tank 3 may not be provided.
遠心濾過濃縮機２の具体的な構造の一例を第３
図に示す。第３図において気密構造のハウジング
１１内には回転軸１２に指示されたバスケツト１
３が収容され、このバスケツト１３の内面に沿つ
て濾布１４が配置されている。回転軸１２とハウ
ジング１１との間にはメカニカルシール１５が設
けられ、ハウジング１１内の気密性が保持されて
いる。そして処理すべき消化液は、供給パイプ１
６を経て濾布１４の中心部に供給される。回転バ
スケツト１３および濾布１４は上下を逆にした円
錐台形をなし、そして高速回転しているので、消
化液中の液分は濾布１４およびバスケツト１３の
小孔を遠心力の作用で通過して濾液室１７内に放
射方向に放出され、固形分（活性汚泥）は濾布１
４上を回転中心から離れる方向（第３図の上方）
に遠心力の作用で移動したのち、濾液室１７から
隔壁１８で分離されたハウジング上部の濃縮室１
９の上部入口から内に放出される。これによつて
消化液の固液分離が効率よく行われ、消化汚泥を
多量に含む濃縮液はパイプ２０を経て取出され、
瀘液はパイプ２１を経て第２消化槽３に送られ
る。さらにハウジング１１の内部は、連通管４を
介して第１消化槽１の上部と連通しているため、
第１消化槽で発生したメタンガスを主体とするガ
スで充満される。このため遠心濾過濃縮機２を通
過する液体が空気中の酸素と接触することはな
い。 An example of the specific structure of the centrifugal filtration concentrator 2 is shown in the third example.
As shown in the figure. In FIG. 3, a basket 1 is located inside a housing 11 having an airtight structure and is directed to a rotating shaft 12.
3 is housed therein, and a filter cloth 14 is arranged along the inner surface of this basket 13. A mechanical seal 15 is provided between the rotating shaft 12 and the housing 11 to maintain airtightness within the housing 11. The digestive fluid to be treated is supplied to the supply pipe 1.
6 and is supplied to the center of the filter cloth 14. The rotating basket 13 and the filter cloth 14 have an upside-down truncated conical shape and are rotating at high speed, so that the liquid in the digestive fluid passes through the small holes of the filter cloth 14 and the basket 13 due to the action of centrifugal force. The solid content (activated sludge) is released into the filtrate chamber 17 in the radial direction, and the solid content (activated sludge) is
4. Direction away from the center of rotation (above in Figure 3)
The concentration chamber 1 in the upper part of the housing is separated from the filtrate chamber 17 by a partition wall 18.
It is discharged inward from the upper inlet of 9. As a result, solid-liquid separation of the digestive fluid is efficiently performed, and the concentrated fluid containing a large amount of digested sludge is taken out through the pipe 20.
The filtrate is sent to the second digestion tank 3 via a pipe 21. Furthermore, since the inside of the housing 11 communicates with the upper part of the first digestion tank 1 via the communication pipe 4,
It is filled with gas, mainly methane gas, generated in the first digestion tank. Therefore, the liquid passing through the centrifugal filtration concentrator 2 does not come into contact with oxygen in the air.
このように、分離汚泥は、上下を逆にした円錐
台形をなす回転バスケツト１３および濾布１４に
よつてハウジング１１の上方から分離されるの
で、分離汚泥（濃縮液）の返送管高さ（連通管４
からの垂直距離）を節約することが可能となる。
この構造による第１消化槽１の消化作用への寄与
にはたいへん大きなものがある。というのは、第
１消化槽で発生したメタンガスを主成分とするガ
スで遠心濾過濃縮機２内が満たされることになる
が、ガスの主成分であるメタンガスの比重は、空
気１とすると、0.5547であり、このメタンガスは
上方へたまろうとするから、パイプ２０が下方へ
延びれば延びる程、下方（余剰汚泥廃棄部分）か
らの空気（酸素）の侵入を許し、返送汚泥が酸素
に晒されて、活性汚泥の劣化が生じやすくなるか
らである。 In this way, the separated sludge is separated from above the housing 11 by the rotating basket 13 and the filter cloth 14, which have an upside-down truncated cone shape. tube 4
vertical distance) can be saved.
This structure makes a very large contribution to the digestive action of the first digestion tank 1. This is because the centrifugal filtration concentrator 2 is filled with gas whose main component is methane gas generated in the first digestion tank, but the specific gravity of methane gas, which is the main component of the gas, is 0.5547 when air is 1. Since this methane gas tends to accumulate upward, the further the pipe 20 extends downward, the more air (oxygen) is allowed to enter from below (excess sludge disposal area), and the returned sludge is exposed to oxygen. This is because activated sludge tends to deteriorate.
本発明では、上記のように、遠心濾過濃縮機２
では、この装置の上部から分離汚泥を排出できる
構造なので、メタンガスの流入位置から極力近い
垂直方向の位置で第１消化槽１への返送経路を形
成することができる。したがつて、活性汚泥（濃
縮液）は、遠心濾過濃縮機２内におけるばかりで
なく、返送経路中においても嫌気性消化微生物を
劣化させることなく、高活性な濃縮液を第１消化
槽に返送することができる。 In the present invention, as described above, the centrifugal filtration concentrator 2
Since the apparatus is structured so that the separated sludge can be discharged from the upper part, the return path to the first digestion tank 1 can be formed at a vertical position as close as possible to the methane gas inflow position. Therefore, the activated sludge (concentrated liquid) is not only stored in the centrifugal filtration thickener 2, but also during the return route, without deteriorating the anaerobic digestion microorganisms, and the highly active concentrated liquid is returned to the first digestion tank. can do.
なお、符号２２は、多数のノズル２３を設けた
洗浄パイプを示し、濾布１４等が目詰りしたとき
に、作業を中断して洗浄を行う際に使用される。 Note that the reference numeral 22 indicates a cleaning pipe provided with a large number of nozzles 23, which is used to interrupt the operation and perform cleaning when the filter cloth 14 or the like becomes clogged.
第１消化槽内でメタン発酵を効率よく行わせる
ためには、槽内の微生物濃度を高水準に保つこ
と、嫌気性条件を確実に保つこと、およびよく撹
拌することが重要である。この発明によれば、第
１消化槽１から取出された消化液が遠心濾過濃縮
機２に酸素に触れずに濃縮されたのち、前記のよ
うに返送経路においても酸素に触れることなく、
返送されるので、第１消化槽１内の固形物濃度を
高水準（たとえばMLSSが４％以上）に保つこと
ができ、充分な撹拌を行うこともできる。また遠
心濾過濃縮機２の内部は気密に保たれているの
で、空気が混入することはなく、メタン生成菌の
活動は阻害されず、遠心濾過濃縮機２内での濃縮
液（汚泥）分離部分が高い位置にあり、濃縮液の
返送回路を空気の侵入を上方にたまるメタンガス
によつて防ぐことのできる高位置に設定できるた
め、返送濃縮液の微生物の活性を劣化させること
もない。さらに第２消化槽を設ける場合には遠心
濾過濃縮機２で生じた濾液は第２消化槽３内で消
化および沈殿処理を受けるので、瀘液にある程度
の固形物が混入していても支障はない。したがつ
て濾布１４として幾分目の粗いものを使用するこ
とができ、目詰りの機会が減少して安定した連続
運転を行うことが可能である。また運転中にパイ
プ２２を洗浄水を供給して洗浄を行つても、洗浄
排水は濃縮液中には混入せず、瀘液とともに排出
されるので、返送濃縮液への影響はない。 In order to efficiently carry out methane fermentation in the first digestion tank, it is important to maintain the microbial concentration in the tank at a high level, to reliably maintain anaerobic conditions, and to stir well. According to this invention, after the digestive fluid taken out from the first digestion tank 1 is concentrated in the centrifugal filtration concentrator 2 without coming into contact with oxygen, the digestive fluid is concentrated without coming into contact with oxygen in the return route as described above.
Since the solids are returned, the solids concentration in the first digestion tank 1 can be maintained at a high level (for example, MLSS is 4% or more), and sufficient stirring can be performed. In addition, since the inside of the centrifugal filtration concentrator 2 is kept airtight, air does not get mixed in and the activity of methane-producing bacteria is not inhibited. Since the concentrated liquid return circuit can be set at a high position where air can be prevented from entering by the methane gas accumulated above, the activity of microorganisms in the returned concentrated liquid will not be degraded. Furthermore, when a second digestion tank is provided, the filtrate produced in the centrifugal filtration and concentration machine 2 is digested and precipitated in the second digestion tank 3, so there is no problem even if a certain amount of solids are mixed in the filtrate. do not have. Therefore, a somewhat coarse mesh can be used as the filter cloth 14, reducing the chance of clogging and making it possible to perform stable continuous operation. Further, even if the pipe 22 is washed by supplying washing water during operation, the washing waste water is not mixed into the concentrated liquid and is discharged together with the filtrate, so there is no effect on the returned concentrated liquid.
以上のように、この発明によれば、第１消化槽
からの消化液を遠心濾過濃縮機で酸素に触れさせ
ずに濃縮し、その濃縮液は返送経路でも酸素に触
れずに高活性な微生物を維持したまま第１消化槽
に返送するようにしたので、各消化槽における条
件が消化処理に最適なものとなり、消化効率が格
段に向上する。このため、難分解性基質を含む廃
水や高負荷運転にも対応でき、また総容量の縮小
による装置の小形化も可能である。さらに脱離液
のSS、BOD等が低濃度になるので、２次処理系
の負荷が軽減されるという効果も得られる。 As described above, according to the present invention, the digestive fluid from the first digestion tank is concentrated using a centrifugal filtration concentrator without being exposed to oxygen, and the concentrated fluid is highly active microorganisms without being exposed to oxygen even in the return route. Since the water is returned to the first digestion tank while maintaining the same, the conditions in each digestion tank become optimal for the digestion process, and the efficiency of digestion is significantly improved. Therefore, it is possible to handle wastewater containing difficult-to-decompose substrates and high-load operation, and it is also possible to downsize the device by reducing the total capacity. Furthermore, since the concentration of SS, BOD, etc. in the desorbed liquid is reduced, the load on the secondary treatment system is also reduced.
第１図は従来の嫌気性消化方法の工程を示すフ
ローシート、第２図はこの発明方法の工程の一例
を示すフローシート、第３図はこの発明で使用さ
れる遠心濾過濃縮機の概略的縦断面図である。
１……第１消化槽、２……遠心濾過濃縮機、３
……第２消化槽、４……連通管、１１……ハウジ
ング、１２……回転軸、１３……バスケツト、１
４……濾布、１５……メカニカルシール、１６…
…供給パイプ、１７……濾液室、１８……隔壁、
１９……濃縮液室、２３……ノズル。
Fig. 1 is a flow sheet showing the steps of a conventional anaerobic digestion method, Fig. 2 is a flow sheet showing an example of the steps of the method of this invention, and Fig. 3 is a schematic diagram of the centrifugal filtration concentrator used in this invention. FIG. 1...First digestion tank, 2...Centrifugal filtration concentrator, 3
...Second digestion tank, 4...Communication pipe, 11...Housing, 12...Rotating shaft, 13...Basket, 1
4... Filter cloth, 15... Mechanical seal, 16...
... Supply pipe, 17 ... Filtrate chamber, 18 ... Partition wall,
19... Concentrate chamber, 23... Nozzle.
Claims (1)
化させ、この消化液を、前記第１消化槽内におけ
る嫌気性消化によつて発生したメタンを主体とす
るガスで充満するとともに、上下を逆にした円錐
台形をなす回転バスケツトおよび濾布とにより濃
縮液をその上部から分離する遠心濃縮機によつ
て、空気中の酸素に接触させることなく濃縮し、
濃縮液の少なくとも一部を酸素に触れさせること
なく上記第１消化槽に返送することを特徴とする
高濃度有機性廃水の嫌気性消化方法。 ２ 上記遠心濾過濃縮機からの瀘液を第２消化槽
の供給して嫌気性消化させ、消化汚泥を沈殿分離
することを特徴とする特許請求の範囲第１項記載
の高濃度有機性廃水の嫌気性消化方法。[Scope of Claims] 1 Highly concentrated organic wastewater is anaerobically digested in a first digestion tank, and the digestive fluid is converted into a gas mainly composed of methane generated by the anaerobic digestion in the first digestion tank. A centrifugal concentrator separates the concentrated liquid from the upper part using a rotating basket in the shape of an upside-down truncated cone and a filter cloth.
A method for anaerobic digestion of highly concentrated organic wastewater, characterized in that at least a portion of the concentrated liquid is returned to the first digestion tank without being exposed to oxygen. 2. Highly concentrated organic wastewater according to claim 1, characterized in that the filtrate from the centrifugal filtration and concentration machine is supplied to a second digestion tank for anaerobic digestion, and the digested sludge is separated by precipitation. Anaerobic digestion method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56145721A JPS5845797A (en) | 1981-09-16 | 1981-09-16 | Anaerobic digestion of highly-concentrated organic waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56145721A JPS5845797A (en) | 1981-09-16 | 1981-09-16 | Anaerobic digestion of highly-concentrated organic waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5845797A JPS5845797A (en) | 1983-03-17 |
| JPH0318956B2 true JPH0318956B2 (en) | 1991-03-13 |
Family
ID=15391589
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56145721A Granted JPS5845797A (en) | 1981-09-16 | 1981-09-16 | Anaerobic digestion of highly-concentrated organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5845797A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2575625B2 (en) * | 1985-07-25 | 1997-01-29 | 松下電工株式会社 | Discharge lamp lighting device |
| JPH0744077B2 (en) * | 1985-10-25 | 1995-05-15 | 松下電工株式会社 | Discharge lamp lighting device |
| JP2008136984A (en) * | 2006-12-05 | 2008-06-19 | Fuji Electric Holdings Co Ltd | Methane fermentation treatment apparatus |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS528660A (en) * | 1975-07-09 | 1977-01-22 | Hitachi Ltd | Anaerobic digestion of organic waste fluid |
| JPS5541160A (en) * | 1978-09-13 | 1980-03-22 | Meidensha Electric Mfg Co Ltd | Dc feeding system for electric railway |
| JPS5613092A (en) * | 1979-07-14 | 1981-02-07 | Shin Meiwa Ind Co Ltd | Method and apparatus for treating of organic solid |
-
1981
- 1981-09-16 JP JP56145721A patent/JPS5845797A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS528660A (en) * | 1975-07-09 | 1977-01-22 | Hitachi Ltd | Anaerobic digestion of organic waste fluid |
| JPS5541160A (en) * | 1978-09-13 | 1980-03-22 | Meidensha Electric Mfg Co Ltd | Dc feeding system for electric railway |
| JPS5613092A (en) * | 1979-07-14 | 1981-02-07 | Shin Meiwa Ind Co Ltd | Method and apparatus for treating of organic solid |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5845797A (en) | 1983-03-17 |
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