JPH0561996B2 - - Google Patents
Info
- Publication number
- JPH0561996B2 JPH0561996B2 JP58245279A JP24527983A JPH0561996B2 JP H0561996 B2 JPH0561996 B2 JP H0561996B2 JP 58245279 A JP58245279 A JP 58245279A JP 24527983 A JP24527983 A JP 24527983A JP H0561996 B2 JPH0561996 B2 JP H0561996B2
- Authority
- JP
- Japan
- Prior art keywords
- wastewater
- biological treatment
- evaporator
- treatment device
- 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 - Lifetime
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 238000000034 method Methods 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 21
- 239000010802 sludge Substances 0.000 claims description 21
- 239000002351 wastewater Substances 0.000 claims description 17
- 238000001704 evaporation Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 7
- 239000010800 human waste Substances 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 238000004065 wastewater treatment Methods 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000002361 compost Substances 0.000 claims description 3
- 238000009264 composting Methods 0.000 claims description 3
- 210000003608 fece Anatomy 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 239000005416 organic matter Substances 0.000 claims description 2
- 230000002159 abnormal effect Effects 0.000 claims 1
- 244000144972 livestock Species 0.000 claims 1
- 230000000630 rising effect Effects 0.000 claims 1
- 230000002085 persistent effect Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- 238000010977 unit operation Methods 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000009419 refurbishment Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Description
この発明は、し尿、畜ふん等の高濃度廃水を処
理する方法に関するものである。
し尿や畜ふんなどの高濃度廃水を処理する目的
で、第１図に示すようなシステムが従来から適用
されている。このシステムにおいて、処理すべき
廃水は、前処理装置１を経て生物処理装置２に導
入され、ここで生物処理を受けたのち、固液分離
装置３で活性汚泥の分離が行われ、その一部が返
送汚泥として生物処理装置１に返送される。また
生物処理では除去されなかつた難分解性成分を除
去するために、固液分離装置３からの液体を凝集
沈殿装置４およびろ過装置５を順次に通過させ、
さらに活性炭吸着装置６を通過させるなどの手段
が採られている。
しかしながら従来の方法では、難分解性成分の
除去のために必要とされる単位操作が多く複雑で
あるほか、薬剤の大量注入や処理材の頻繁な更
新、更生を行わなければならないため、処理コス
トが高くなる欠点がある。
このため、従来、生物処理した液体中の難分解
性成分を除去する手段として、蒸発処理を施す方
法が提案されている。
しかし従来の蒸発式処理法では、固体分を含ま
ない純粋な液体分のみを蒸発工程に送ることを目
的としているので、蒸発工程の前に、固液分離工
程、あるいは凝集沈殿・濾過等の工程を必要と
し、経済的・効率的な処理法とは言い難いもので
ある。
この発明は上記した従来の問題に鑑みてなされ
たもので、生物処理を施した後の活性汚泥混合液
体を蒸発工程へ送ることにより、蒸発工程の前の
固液分離工程、および凝集沈殿・濾過工程を不要
にし、単位操作数すなわち工程数を大幅に削減し
て、経済的かつ効率的な処理の遂行を可能にする
とともに、処理済みの水質を良好に向上させるこ
とができる高濃度廃水処理方法を提供することを
目的とする。
以下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、１は廃水中の
夾雑物を除去するための前処理装置で、後段の各
機器を円滑に運転できるようにするとともに、負
荷を低減させるために装置することが望ましい
が、廃水中の夾雑物が少ない場合には省略しても
よい。除渣した廃水はつぎの生物処理装置２へ移
送され、脱水し渣は最終処理工程であるコンポス
トまたは乾燥・焼却施設９で処理される。
生物処理装置２は、活性汚泥方式のものでもよ
いが、アンモニアを除去することで後段の蒸発装
置１５における処理水の水質の向上をはかるため
に、有機物除去だけなく窒素除去も可能な循環脱
窒方式または好気性脱窒式によるものが好適であ
る。アンモニアは揮発性であるので、蒸発装置１
５での蒸発処理では蒸発処理水中に移行してしま
うので、生物処理の段階で除去しておくことが望
ましい。また施設簡略化のため、反応槽は貯留機
能をも備えた水位変動可能な構造のものが適す
る。この生物処理装置２内における処理では、
BOD、COD等の有機物と、Ｔ−Ｎの大部分が分
解されるが、難分解性のCOD、色度成分、Ｔ−
Ｐ等は残存する。なお脱窒処理は、効果的な運転
が行えるものであれば、どのような方法で行われ
てもよい。
一般に、し尿処理において無希釈処理を行う生
物分解にともない水温が異常上昇する。生物反応
における水温の上限は38℃であるので、冷却する
必要が生じるが、この冷却は、後段の蒸発装置１
５に熱を供給することで効率よく行うことがで
き、蒸発装置１５でもこの熱を蒸発のために利用
することができる。また廃水の性状などにより発
熱量が大きく、上記の冷却では間に合わない場合
には、処理槽内に熱交換器２１を設け、この熱交
換器２１に、蒸発装置１５で得られた温度の低い
処理水を通してもよい。
蒸発装置１５で行われる処理は、生成物処理で
は、分解されなかつた難分解性のCOD、色度成
分、Ｔ−Ｐ、溶解性物質等を一括処理するための
ものである。この例では、蒸発装置１５として、
熱効率のよいヒートポンプ型のものが使用されて
いる。生物反応を終えた液体は、ポンプによりま
ず蒸発器１０に導かれる。この蒸発器１０には、
フアン１３により乾燥空気が送られ、この空気は
蒸発器１０内の液体からの蒸発水を同伴すること
で加湿されたのち除湿器１１に系路１４を通して
送られる。除湿器１１は、コンプレツサ１２を運
転することにより圧縮、膨張をくり返す熱媒の作
用で得られる冷却および加熱効果で、系路１４か
ら流入した湿潤空気を冷却してその中の水分を除
去し、ついでこの乾燥空気を加熱する動作を行
い、この加熱された乾燥空気が再び蒸発器１０に
供給される。蒸発器１０で水分を蒸発させた濃縮
液は生物処理装置２に戻され、一方、除湿器１１
で凝縮した凝縮水は処理水としてそのまま、ある
いは熱交換器２１を通して外部に取出される。こ
の処理水は、蒸発器１０における蒸発が38℃以下
の低温で行われているために、難分解性の物質の
ほとんどが除去され、水道水と同等以上の良好な
水質を有し、したがつて種々の用水として有効利
用することが可能である。
一方、生物処理装置２内で生じた余剰汚泥は、
脱水機８に送られ、分離液は生物処理装置２に戻
され、脱水汚泥はコンポストまたは乾燥・焼却施
設９に移送される。脱水機８としては、通常の加
熱圧脱水機、ベルトプレス、遠心分離機等から任
意のものを選択できるが、プロセスの処理水量を
少なくし得る点から、洗浄水量が少なくてすむ遠
心分離機が適している。また生物処理装置２から
余剰汚泥を引抜くよりも、蒸発器１０からの返送
汚泥を引抜く方が、濃縮されている分だけ有利で
ある。
最終処理工程であるコンポストまたは乾燥・焼
却施設９は、前段の各処理工程で発生したし渣お
よび脱水汚泥を一括処理するためのもので、一般
的な施設をそのまま適用できる。また乾燥・冷却
に必要な熱の一部として、コンプレツサ１２の廃
熱を利用すればエネルギの利用効率がさらに向上
する。
実施例
第２図に示した工程にしたがつて、通常の生し
尿を処理した。生し尿、除渣し尿、生物処理水お
よび蒸発処理水の各々の組成は第１表のとおりで
あつた。なお生物処理水はろ液の水質である。
The present invention relates to a method for treating highly concentrated wastewater such as human waste and animal dung. BACKGROUND ART A system as shown in Figure 1 has been conventionally used to treat highly concentrated wastewater such as human waste and animal dung. In this system, wastewater to be treated is introduced into a biological treatment device 2 via a pretreatment device 1, where it is subjected to biological treatment, and then activated sludge is separated in a solid-liquid separation device 3. is returned to the biological treatment device 1 as return sludge. In addition, in order to remove persistent components that were not removed by biological treatment, the liquid from the solid-liquid separator 3 is sequentially passed through a coagulation sedimentation device 4 and a filtration device 5.
Furthermore, measures such as passing through an activated carbon adsorption device 6 are taken. However, conventional methods require many complicated unit operations to remove persistent components, and require injection of large amounts of chemicals and frequent renewal and refurbishment of processing materials, resulting in high processing costs. It has the disadvantage of being high. For this reason, a method of performing evaporation treatment has conventionally been proposed as a means for removing persistent components in a biologically treated liquid. However, in the conventional evaporative treatment method, the purpose is to send only pure liquid containing no solids to the evaporation process. It is difficult to call this an economical or efficient treatment method. This invention was made in view of the above-mentioned conventional problems, and by sending the activated sludge mixed liquid after biological treatment to the evaporation process, the solid-liquid separation process, coagulation sedimentation, and filtration process before the evaporation process can be performed. A high-concentration wastewater treatment method that eliminates the need for processes, significantly reduces the number of unit operations, that is, the number of processes, enables economical and efficient treatment, and can improve the quality of treated water. The purpose is to provide An example of the steps of the method of this invention will be explained below with reference to the drawings. In Figure 2, 1 is a pre-treatment device for removing impurities from wastewater.It is desirable to install this device in order to enable the smooth operation of each subsequent stage equipment and to reduce the load. It may be omitted if there are few impurities inside. The removed wastewater is transferred to the next biological treatment device 2, and the dehydrated residue is processed in a composting or drying/incineration facility 9, which is the final treatment step. The biological treatment device 2 may be of an activated sludge type, but in order to improve the water quality of the treated water in the subsequent evaporation device 15 by removing ammonia, it is a cyclic denitrification device that can remove not only organic matter but also nitrogen. or aerobic denitrification is preferred. Since ammonia is volatile, evaporator 1
In the evaporation treatment in step 5, it migrates into the evaporation treated water, so it is desirable to remove it at the biological treatment stage. Furthermore, in order to simplify the facility, it is suitable for the reaction tank to have a structure that also has a storage function and allows the water level to fluctuate. In the treatment within this biological treatment device 2,
Most organic substances such as BOD and COD and T-N are decomposed, but persistent COD, chromaticity components, and T-N are decomposed.
P etc. remain. Note that the denitrification treatment may be performed by any method as long as it can be operated effectively. Generally, in human waste treatment, water temperature increases abnormally due to biodegradation that is performed without dilution. The upper limit of water temperature in biological reactions is 38°C, so cooling is required, but this cooling is done by the evaporator 1 in the subsequent stage.
This can be done efficiently by supplying heat to the evaporator 5, and the evaporator 15 can also use this heat for evaporation. In addition, if the heat generation value is large due to the nature of the wastewater and the above cooling is not sufficient, a heat exchanger 21 is provided in the treatment tank, and the heat exchanger 21 is used to process the low-temperature treatment obtained by the evaporator 15. You can also pass water through it. The processing carried out in the evaporator 15 is for the purpose of collectively processing the persistent COD, chromaticity components, T-P, soluble substances, etc. that were not decomposed in the product processing. In this example, as the evaporator 15,
A heat pump type with high thermal efficiency is used. The liquid that has undergone the biological reaction is first guided to the evaporator 10 by a pump. This evaporator 10 has
Dry air is delivered by a fan 13 which is humidified by entraining evaporated water from the liquid in the evaporator 10 and then sent to the dehumidifier 11 through line 14. The dehumidifier 11 cools the humid air flowing in from the system path 14 and removes moisture therein, using cooling and heating effects obtained by the action of a heating medium that repeatedly compresses and expands when the compressor 12 is operated. Then, an operation is performed to heat this dry air, and this heated dry air is supplied to the evaporator 10 again. The concentrated liquid from which water has been evaporated in the evaporator 10 is returned to the biological treatment device 2, while the dehumidifier 11
The condensed water is taken out as treated water as it is or through the heat exchanger 21 to the outside. Since the evaporation in the evaporator 10 is carried out at a low temperature of 38°C or lower, most of the non-decomposable substances are removed from this treated water, and the water quality is as good as or better than that of tap water. Therefore, it can be effectively used as water for various purposes. On the other hand, the excess sludge generated in the biological treatment equipment 2 is
The separated liquid is sent to the dehydrator 8, and the separated liquid is returned to the biological treatment device 2, and the dehydrated sludge is transferred to a compost or drying/incineration facility 9. As the dehydrator 8, any one can be selected from ordinary heat-pressure dehydrators, belt presses, centrifugal separators, etc., but a centrifugal separator that requires less water for washing is preferable because it can reduce the amount of water processed in the process. Are suitable. Moreover, it is more advantageous to extract return sludge from the evaporator 10 than to extract excess sludge from the biological treatment device 2 because it is concentrated. The composting or drying/incineration facility 9, which is the final treatment step, is for collectively processing the residue and dewatered sludge generated in the previous treatment steps, and a general facility can be applied as is. Furthermore, if waste heat from the compressor 12 is used as part of the heat required for drying and cooling, energy use efficiency can be further improved. Example Normal raw human waste was treated according to the steps shown in FIG. The compositions of raw human waste, filtered human waste, biologically treated water, and evaporatively treated water were as shown in Table 1. The quality of biologically treated water is that of filtrate.
【表】
本発明の効果を説明すると、本発明において
は、蒸発装置１５で蒸発させる対象が、活性汚泥
混合液体であるので、蒸発工程の前に固液分離工
程、および凝集沈殿・濾過等の高度処理工程を必
要とせず、したがつて工程数および設備機器が大
幅に削減され、きわめて経済的となる。また、本
発明の場合、蒸発工程で生じた余剰汚泥を脱水機
８へ返送し、コンポストまたは乾燥・焼却施設９
へ送るので、活性汚泥混合液体を蒸発工程へ送り
込んでも、全く問題が生じない。
また、本発明では、蒸発工程で生じた濃縮液を
生物処理工程へ戻すので、この濃縮液を処理する
ための専用施設を設ける必要がなく、この面から
も、経済的で効率的な処理が行われる。
さらに、本発明において、蒸発工程から最終的
に取り出された処理済みの水は、水道水と同等以
上の良好な水質を有し、したがつて種々な用水と
して有効利用できることが確認された。[Table] To explain the effects of the present invention, in the present invention, since the target to be evaporated in the evaporator 15 is an activated sludge mixed liquid, a solid-liquid separation process, coagulation sedimentation, filtration, etc. are performed before the evaporation process. It does not require advanced processing steps, and therefore the number of steps and equipment are significantly reduced, making it extremely economical. In addition, in the case of the present invention, surplus sludge generated in the evaporation process is returned to the dewatering machine 8 and composted or dried/incinerated at the drying/incineration facility 9.
Therefore, no problem occurs even if the activated sludge mixed liquid is sent to the evaporation process. Furthermore, in the present invention, since the concentrated liquid produced in the evaporation process is returned to the biological treatment process, there is no need to provide a dedicated facility for processing this concentrated liquid, and from this point of view as well, economical and efficient treatment is possible. It will be done. Furthermore, in the present invention, it has been confirmed that the treated water finally taken out from the evaporation process has good water quality equivalent to or better than tap water, and can therefore be effectively used as water for various purposes.
第１図は従来の高濃度廃水処理方法の工程を示
す系統図、第２図はこの発明の一実施例による高
濃度廃水処理方法の工程を示す系統図である。
１……前処理装置、２……生物処理装置、８…
…脱水機、９……コンポストまたは乾燥・焼却施
設、１０……蒸発器、１１……除湿器、１２……
コンプレツサ、１３……フアン、１４……系路、
１５……蒸発装置、２１……熱交換器。
FIG. 1 is a system diagram showing the steps of a conventional high concentration wastewater treatment method, and FIG. 2 is a system diagram showing the steps of a high concentration wastewater treatment method according to an embodiment of the present invention. 1... Pretreatment device, 2... Biological treatment device, 8...
... Dehydrator, 9 ... Compost or drying/incineration facility, 10 ... Evaporator, 11 ... Dehumidifier, 12 ...
Compressa, 13... Juan, 14... Lineage,
15... Evaporator, 21... Heat exchanger.
Claims (1)
方法であつて、し渣の少ない処理すべき廃水を生
物処理装置２の反応漕内へ送る工程と、この反応
漕内で、活性汚泥処理および脱窒処理により、前
記廃水から有機物および窒素を除去する工程と、
前記反応漕内で生物処理を終えた活性汚泥混合液
体を、難分解生成分の一括処理を行なう蒸発装置
１５内の、乾燥空気に接触させる蒸発器１０へ移
送するとともに、前記生物処理装置２内で生じた
余剰汚泥を脱水機８へ移送する工程と、この脱水
機８で分離された液体を前記生物処理装置２へ戻
すとともに、脱水済み汚泥をコンポストまたは乾
燥・焼却施設９へ移送する工程と、一方、前記蒸
発器１０へ送られた活性汚泥混合液体からの蒸発
水を前記乾燥空気に随伴させ、この蒸発水随伴空
気を除湿器１１へ送る工程と、この除湿器１１内
で、前記蒸発水随伴空気を冷却して、この中の水
分を除去し、ついで、この水分を除去して残つた
乾燥空気を加熱する工程と、この加熱済みの乾燥
空気を再度前記蒸発器１０へ供給するとともに、
前記除湿器１１内で凝縮した凝縮水を処理済水と
してそのまま外部へ、あるいは前記生物処理装置
２内の廃水温度の異常上昇を防止するため、生物
処理装置２内の熱交換器２１へ通して、生物処理
装置２内の廃水の冷却を行つた後、外部へ取り出
す工程と、前記蒸発器１０内で水分を蒸発された
濃縮液を、前記生物処理装置２へ戻すとともに、
蒸発器１０からの返送汚泥を余剰汚泥として、前
記脱水機８を介して前記コンポストまたは乾燥・
焼却施設９へ送る工程とを具備する高濃度廃水処
理方法。 ２ 前記処理すべき廃水中のし渣を減少させるた
めに、廃水中の夾雑物を除去する前処理を行な
い、この後、廃水を前記生物処理装置２へ送るこ
とを特徴とする特許請求の範囲第１項記載の高濃
度処理方法。 ３ 前記生物処理装置内の廃水温度の異常上昇を
防止するため、この廃水の熱を前記蒸発装置１５
の乾燥空気の加熱部へ供給することを特徴とする
特許請求の範囲第１項または第２項記載の高濃度
廃水処理方法。[Scope of Claims] 1. A method for treating highly concentrated wastewater such as human waste and livestock dung, which includes a step of sending wastewater to be treated with a small amount of human sludge into a reaction tank of a biological treatment device 2, and a step in this reaction tank. a step of removing organic matter and nitrogen from the wastewater by activated sludge treatment and denitrification treatment;
The activated sludge mixed liquid that has been subjected to biological treatment in the reaction tank is transferred to the evaporator 10 in which it is brought into contact with dry air in the evaporator 15 that collectively processes the difficult-to-decompose products. a step of transferring the surplus sludge generated in the step to the dehydrator 8, a step of returning the liquid separated by the dehydrator 8 to the biological treatment device 2, and a step of transferring the dehydrated sludge to the composting or drying/incineration facility 9. , on the other hand, a step of causing evaporated water from the activated sludge mixed liquid sent to the evaporator 10 to accompany the dry air, and sending the air accompanied by this evaporated water to the dehumidifier 11; A step of cooling the water-entrained air to remove moisture therein, then heating the remaining dry air after removing the moisture, and supplying the heated dry air to the evaporator 10 again. ,
The condensed water condensed in the dehumidifier 11 can be directly sent to the outside as treated water, or can be passed through the heat exchanger 21 in the biological treatment device 2 in order to prevent the wastewater temperature in the biological treatment device 2 from rising abnormally. , a step of cooling the wastewater in the biological treatment device 2 and then taking it out to the outside, and returning the concentrated liquid from which water has been evaporated in the evaporator 10 to the biological treatment device 2;
The returned sludge from the evaporator 10 is used as surplus sludge and is passed through the dehydrator 8 to the compost or dried sludge.
A highly concentrated wastewater treatment method comprising a step of sending the wastewater to an incineration facility 9. 2. Claims characterized in that in order to reduce the residue in the wastewater to be treated, a pretreatment is performed to remove impurities in the wastewater, and then the wastewater is sent to the biological treatment device 2. The high concentration treatment method according to item 1. 3. In order to prevent an abnormal rise in the temperature of wastewater in the biological treatment device, the heat of this wastewater is transferred to the evaporation device 15.
3. The high concentration wastewater treatment method according to claim 1 or 2, wherein the dry air is supplied to the heating section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58245279A JPS60139398A (en) | 1983-12-28 | 1983-12-28 | Treatment of high concentration waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58245279A JPS60139398A (en) | 1983-12-28 | 1983-12-28 | Treatment of high concentration waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60139398A JPS60139398A (en) | 1985-07-24 |
| JPH0561996B2 true JPH0561996B2 (en) | 1993-09-07 |
Family
ID=17131306
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58245279A Granted JPS60139398A (en) | 1983-12-28 | 1983-12-28 | Treatment of high concentration waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60139398A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3477526B2 (en) | 1997-05-27 | 2003-12-10 | 日立造船株式会社 | Wastewater recovery equipment |
| CN104310714B (en) * | 2014-11-03 | 2016-05-04 | 广西龙道环保工程有限责任公司 | A kind of cultivation and system and technique thereof of butchering sewage processed |
| JP7226731B2 (en) * | 2018-10-19 | 2023-02-21 | Ｄｏｗａテクノロジー株式会社 | Processing method of the object to be processed |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS586280A (en) * | 1981-07-02 | 1983-01-13 | Nishihara Environ Sanit Res Corp | Drying treatment of night soil |
| JPS58112092A (en) * | 1981-12-25 | 1983-07-04 | Kubota Ltd | Treatment of excretion |
| JPS58223498A (en) * | 1982-06-23 | 1983-12-26 | Ebara Infilco Co Ltd | Treatment of organic waste water |
-
1983
- 1983-12-28 JP JP58245279A patent/JPS60139398A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS586280A (en) * | 1981-07-02 | 1983-01-13 | Nishihara Environ Sanit Res Corp | Drying treatment of night soil |
| JPS58112092A (en) * | 1981-12-25 | 1983-07-04 | Kubota Ltd | Treatment of excretion |
| JPS58223498A (en) * | 1982-06-23 | 1983-12-26 | Ebara Infilco Co Ltd | Treatment of organic waste water |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60139398A (en) | 1985-07-24 |
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