JPH0217676Y2 - - Google Patents
Info
- Publication number
- JPH0217676Y2 JPH0217676Y2 JP8093286U JP8093286U JPH0217676Y2 JP H0217676 Y2 JPH0217676 Y2 JP H0217676Y2 JP 8093286 U JP8093286 U JP 8093286U JP 8093286 U JP8093286 U JP 8093286U JP H0217676 Y2 JPH0217676 Y2 JP H0217676Y2
- Authority
- JP
- Japan
- Prior art keywords
- human waste
- uasb
- scum
- sludge
- methane fermentation
- 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
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 64
- 239000010800 human waste Substances 0.000 claims description 47
- 238000000855 fermentation Methods 0.000 claims description 33
- 230000004151 fermentation Effects 0.000 claims description 33
- 239000010802 sludge Substances 0.000 claims description 30
- 239000002351 wastewater Substances 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 8
- 239000010865 sewage Substances 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 238000004065 wastewater treatment Methods 0.000 claims description 2
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 39
- 238000000034 method Methods 0.000 description 17
- 241000894006 Bacteria Species 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 238000007790 scraping Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 210000002700 urine Anatomy 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000008107 starch Substances 0.000 description 2
- 235000019698 starch Nutrition 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- 241000305071 Enterobacterales Species 0.000 description 1
- 241000588724 Escherichia coli Species 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000000968 intestinal effect Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000989 no adverse effect Toxicity 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002699 waste material 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
Landscapes
- Removal Of Floating Material (AREA)
- Treatment Of Sludge (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【考案の詳細な説明】
〔産業上の利用分野〕
本考案は、上向流式嫌気性汚泥床法（以下、
UASB法と略記する）によりし尿系汚水を嫌気
的に処理するための装置に関するものである。[Detailed description of the invention] [Industrial application field] The present invention is based on the upflow anaerobic sludge bed method (hereinafter referred to as
This relates to equipment for anaerobically treating human waste wastewater using the UASB method (abbreviated as the UASB method).
UASB法は、廃水をメタン発酵するための方
法として近年開発された方法であつて、原廃水を
発酵槽の下部より上向流として流入させ、菌の付
着担体を用いることなく、汚泥をフロツク化若し
くは粒状化せしめることにより汚泥床（スラツジ
ベツド）を形成させ、発酵槽中に高濃度の微生物
を確保することにより高容積負荷を許容しうる嫌
気的微生物処理技術であつて、その装置として
は、低負荷時の短絡防止のため底部に廃水を均一
に流入せしめるための分配流入管を備え、上部に
ガス−汚泥−液（気−固−液）の三相分離装置を
備えたものである（下水道協会誌Vol.22，No.255，
1985／867〜77頁）。
The UASB method is a method developed in recent years for methane fermentation of wastewater. Raw wastewater flows upward from the bottom of the fermenter, and the sludge is flocculated without using carriers for bacteria to adhere to it. It is an anaerobic microbial treatment technology that can tolerate a high volume load by forming a sludge bed by granulating or granulating it and securing a high concentration of microorganisms in the fermenter. It is equipped with a distribution inflow pipe at the bottom to uniformly flow wastewater to prevent short circuits under load, and a three-phase separation device for gas-sludge-liquid (gas-solid-liquid) at the top (sewage system). Association magazine Vol.22, No.255,
1985/pp. 867-77).
この装置は、廃液の質的差異により採用できる
場合と採用できない場合のあることが知られてお
り、この装置がし尿系汚水のメタン発酵に利用で
きるかどうかを検討した報告例はこれまでのとこ
ろ皆無である。 It is known that this device may or may not be adopted depending on the quality of the waste liquid, and so far there have been no reports examining whether this device can be used for methane fermentation of human waste wastewater. There are none.
本考案は、し尿系汚水をUASB法により処理
するための装置を提供することを目的とする。
The purpose of the present invention is to provide a device for treating human waste water using the UASB method.
本考案は、底部にし尿系汚水の分配流入管を、
上部に気−固−液分離部を設けてなる汚泥床式メ
タン発酵槽にし尿を上向流に通水して処理する装
置において、汚泥床式メタン発酵槽の前段に、底
部にし尿系汚水の分配流入管を、上部にスカムの
除去装置を設けた上向流発酵槽を設けたことを特
徴とするし尿系汚水の処理装置である。
This invention has a distribution inflow pipe for night soil wastewater at the bottom.
In a sludge bed type methane fermentation tank with a gas-solid-liquid separation section installed at the top, the system treats human waste by passing water in an upward flow. This is a human waste wastewater treatment device characterized in that the distribution inflow pipe is provided with an upflow fermentation tank equipped with a scum removal device at the top.
従来のし尿系汚水のメタン発酵処理は、メタン
発酵槽内におけるできるだけ長いし尿滞留時間を
確保するために、長時間滞留可能な完全混合式消
化槽、固定床式上向流嫌気性反応槽及び流動床式
嫌気性反応槽が用いられている。これらは何れも
メタン菌等の嫌気性菌のフロツク（径約0.5mm以
下）の形成が、これらの菌の担体に対する付着能
力を利用して構成された処理方法であつて、基質
としてのし尿はこれらの菌のフロツクの形成や担
体への付着に対し悪影響を与えることがないの
で、非効率ながらし尿系汚水を希釈することなく
そのまま処理することが可能であつた。 Conventional methane fermentation treatment of night soil wastewater uses a fully mixed digester that can retain human waste for a long time, a fixed-bed upflow anaerobic reactor, and a fluidized flow reactor in order to ensure as long a time as possible for human waste to remain in the methane fermentation tank. A bed-type anaerobic reactor is used. All of these treatment methods utilize the ability of these bacteria to adhere to carriers to form flocs (approximately 0.5 mm or less in diameter) of anaerobic bacteria such as methane bacteria, and human waste is used as a substrate. Since there is no adverse effect on the formation of flocs of these bacteria or their adhesion to carriers, it has been possible to treat human waste wastewater as it is without diluting it, although inefficiently.
一方、UASB法は、メタン菌等の嫌気性菌の
発酵槽内における保持力ないしは保持量を大とす
るために、担体等の菌の付着媒体を用うることな
く、菌体自身を自己固定化せしめ、即ち菌体が
0.5mm〜５mm程度の顆粒状に凝集したグラニユー
ルを形成せしめ、該グラニユールにより汚泥床
（汚泥のブランケツト層）を形成させ、該汚泥床
中に上向流で廃水を通してメタン発酵を行う方法
であつて、特定の有機性廃水を高効率で処理でき
る方法である。 On the other hand, in the UASB method, in order to increase the retention power or amount of anaerobic bacteria such as methane bacteria in the fermenter, the bacteria self-immobilize without using a carrier or other adhesion medium for the bacteria. Seshime, that is, bacterial cells
A method in which granules aggregated into granules of about 0.5 mm to 5 mm are formed, a sludge bed (sludge blanket layer) is formed by the granules, and wastewater is passed through the sludge bed in an upward flow for methane fermentation. , is a method that can treat specific organic wastewater with high efficiency.
本考案者らは、特定の有機性廃水に対してでは
あるが、高効率でメタン発酵処理を行ないうる
UASB法にし尿を直接適用することを試みたが、
所期の目的を達成することはできなかつた。そこ
で、装置の面からし尿を直接適用できるUASB
装置について種々検討を行なつた。 The present inventors have demonstrated that it is possible to perform methane fermentation treatment with high efficiency for specific organic wastewater.
I tried applying human urine directly to the UASB method, but
It was not possible to achieve the intended purpose. Therefore, UASB, which can apply human waste directly from the device side,
Various studies were conducted regarding the device.
即ち、容量3.5の単段式UASB実験装置を用
い、これに1.0のグラニユール形成の終了した
嫌気性汚泥を装入し、BOD15000mg／、
SS8000mg／の浄化槽汚泥を含むし尿を1.75／
日の割合で通水したところ（し尿の滞留時間は
2.0日である。）、この場合の経過日数とBOD除去
率の関係を示す第１図からわかるように、直ちに
メタン発酵が開始されたが経過日数と共にBOD
除去率が低下し、最終的にはBOD除去率が25％
以下となり、メタン発酵装置として十分に機能し
ないことがわかつた。 That is, a single-stage UASB experimental device with a capacity of 3.5 was used, and 1.0 granule-formed anaerobic sludge was charged to it, with a BOD of 15000 mg/,
SS8000mg/ human waste containing septic tank sludge 1.75/
When water was passed at a rate of 1 day (the residence time of human waste was
It is 2.0 days. ), as can be seen from Figure 1, which shows the relationship between the number of days elapsed and the BOD removal rate, methane fermentation started immediately, but the BOD decreased with the number of days elapsed.
Removal rate decreases, eventually BOD removal rate is 25%
It was found that the system did not function adequately as a methane fermentation device.
そこで、その原因について検討したところ、実
験開始当初、メタン発酵が十分に進行したことに
よつてUASBブランケツト内で活発なガス発生
が生じ、これに伴つて大量のスカムがUASB気
−固−液分離部を充満する形で浮上したことによ
るものと考えられた。即ち、この大量のスカム発
生は、当初種汚泥として充填したグラニユール化
汚泥をもスカムとして同伴浮上させてしまい、
UASBリアクターの特長であるグラニユール化
汚泥によるブランケツト層の形成を不可能とせし
め、本来の処理機能を失わせてしまうためであ
る。 Therefore, we investigated the cause and found that at the beginning of the experiment, methane fermentation had progressed sufficiently, resulting in active gas generation within the UASB blanket, and a large amount of scum was generated in the UASB gas-solid-liquid separation system. This is thought to be due to the fact that it surfaced in such a way that it filled the whole area. In other words, this large amount of scum generated causes the granulated sludge that was initially filled as seed sludge to come to the surface as scum,
This is because it makes it impossible to form a blanket layer using granulated sludge, which is a feature of the UASB reactor, and the original processing function is lost.
一方、通常UASB法に適合でき産業廃水等で
はSS濃度が10000mg／程度含まれていても高効
率メタン発酵処理がこのような単段式のUASB
法で実施可能であることから、このようなスカム
発生によつて従来方式のUASB法によるし尿処
理を不可とするのはし尿中のSSの特質によるも
のと考えられた。 On the other hand, such a single-stage UASB can normally comply with the UASB method and can perform highly efficient methane fermentation treatment even if industrial wastewater contains an SS concentration of about 10,000 mg/day.
It was thought that the characteristics of SS in human waste made it impossible to treat human waste using the conventional UASB method due to the formation of such scum.
そして、発生するガスはし尿を原水とした場合
でも工場廃水を原水とした場合でもその大部分が
メタンガスと炭酸ガスとの混合物であることか
ら、次のような実験を行なつてスカムの発生状況
を観察した。 Since most of the gas generated is a mixture of methane gas and carbon dioxide, whether the raw water is human waste or factory wastewater, the following experiment was conducted to determine the state of scum generation. observed.
まず、メタンガス70容量％、炭酸ガス30容量％
の混合ガスを用意して、し尿とSS濃度2000mg／
のセルロース粉末懸濁液とSS濃度8000mg／
のでん粉懸濁液に夫々容器底部より同一通気条件
で前記混合ガスを散気したところ、し尿中のSS
はその７割がスカムとして浮上分離したのに対
し、セルロース粉末懸濁液及びでん粉懸濁液は共
にスカムの浮上は認められなかつた。 First, methane gas 70% by volume, carbon dioxide gas 30% by volume
Prepare a mixed gas of human waste and SS concentration 2000mg/
cellulose powder suspension and SS concentration 8000mg/
When the above mixed gas was diffused into the starch suspension from the bottom of each container under the same ventilation conditions, SS in human waste was
In contrast, 70% of the scum was floated and separated as scum, whereas no scum was observed to float in both the cellulose powder suspension and the starch suspension.
つぎに、し尿への通気により浮上したスカムを
分析したところ、その乾燥重量の９割が大腸菌等
の腸内細菌により構成れており、し尿中のセルロ
ースのほとんどはスカム側ではなくなお懸濁状態
でし尿液中に残存していた。この実験結果より、
し尿に特有なSS成分としての腸内細菌が特異的
にメタン発酵によつて発生するガスと親和性を有
しており、SSがガス泡を付着させやすいこと、
それによつてスカムが容易に発生することを知り
得た。 Next, when we analyzed the scum that floated to the surface by aerating the human waste, we found that 90% of its dry weight was composed of enteric bacteria such as Escherichia coli, and that most of the cellulose in the human waste was not on the scum side but in a suspended state. It remained in the human urine fluid. From this experimental result,
Intestinal bacteria, which are SS components unique to human waste, have a specific affinity for the gas generated by methane fermentation, and SS tends to attract gas bubbles.
It was found that scum was easily generated as a result.
以上の研究結果から、メタン発酵槽を２基直列
に連結し、第１槽において前記し尿に特有なスカ
ム発生機能を利用してし尿中のスカム発生原因と
なるSSを除去すると共に酸発酵、及びメタン発
酵を部分的に行なせ、第１槽からの溢流水を第２
槽のUASB反応槽でメタン発酵を行わせること
により効率よくし尿を処理しうることを見いだし
た。 From the above research results, two methane fermentation tanks are connected in series, and in the first tank, the scum generation function unique to human waste is used to remove SS, which causes scum formation in human waste, and to perform acid fermentation and Methane fermentation can be carried out partially, and the overflow water from the first tank can be transferred to the second tank.
We discovered that human waste can be efficiently processed by performing methane fermentation in the UASB reaction tank.
即ち、本考案は、第１段の反応槽は本来の
UASB法を行うものではないが、UASB反応槽
を２基直列に連結すると共に、前段の反応槽上部
に浮上したスカムの除去装置を設けたし尿の汚泥
床式メタン発酵槽である。 That is, in the present invention, the first stage reaction tank is
Although it does not use the UASB method, it is a sludge bed type methane fermentation tank for human waste, which has two UASB reaction tanks connected in series and a device for removing scum that has floated to the top of the first reaction tank.
以下第２図に基いて本考案の一実施例を説明す
る。 An embodiment of the present invention will be described below with reference to FIG.
高SS濃度の浄化槽汚泥を含むし尿は、まずし
尿系汚水導入管８からポンプ３により初段目の
UASB反応器１の底部に設けられた分配流入口
４より投入される。 Human waste containing septic tank sludge with a high SS concentration is first transported to the first stage by pump 3 from human waste water introduction pipe 8.
It is introduced through the distribution inlet 4 provided at the bottom of the UASB reactor 1.
この初段UASB反応槽では主として酸発酵が
進行するものであるがメタン発酵も部分的に進行
し消化ガスを発生する。発生したガスが上昇する
際に投入されたし尿中のSSに付着しSSと共に浮
上してスカム層を形成する。形成されたスカム層
は前段の上向流発酵槽上部の水面に設けられたス
カムかき取り装置６によつて連続的もしくは断続
的に除去される。したがつてこの初段の反応槽は
必らずしも従来型にのUASB反応槽である必要
はないが、底部に原水分配流入装置を、上部にス
カムかき取り装置６をそなえていることと、冬期
のように気・水温の低下時でもガス発生がなされ
るように、投入に先だつてし尿を加温（25℃〜40
℃に加温することが望ましい）できる設備（熱交
換器、蒸気吹込み装置等）を具備していることが
必要とされる。 In this first-stage UASB reactor, acid fermentation mainly proceeds, but methane fermentation also partially proceeds, generating digestion gas. As the generated gas rises, it adheres to the SS in the human waste thrown in and floats up with the SS, forming a scum layer. The formed scum layer is continuously or intermittently removed by a scum scraping device 6 provided on the water surface above the upstream fermenter in the previous stage. Therefore, this first-stage reaction tank does not necessarily have to be a conventional UASB reaction tank, but it should be equipped with a raw water distribution and inflow device at the bottom and a scum scraping device 6 at the top, To ensure that gas is generated even when air and water temperatures drop, such as in winter, the human waste is heated (25°C to 40°C) before being added.
It is necessary to have equipment (heat exchanger, steam blowing device, etc.) that can heat the plant (preferably to
なお、初段の反応槽に気・固・液分離部を設け
た場合には、UASB反応槽と同一態様となり
こゝで発生したガスの捕集が可能となり効果的で
ある。 It should be noted that if the first stage reaction tank is provided with a gas/solid/liquid separation section, it will be in the same manner as the UASB reaction tank, and it will be effective because it will be possible to collect the generated gas.
ついで初段のUASB反応器で処理された汚水
を後段のUASB反応槽２に導き反応槽底部の分
配流入設備４′を介して上向流的にメタン発酵さ
せたところ、この後段UASB反応槽内できわめ
て活発なメタン発酵がなされたにもかかわらずス
カムの発生は皆無であつた。したがつてた実験開
始当初種汚泥として後段UASB反応槽２に充填
したグラニユール化汚泥は浮上流亡することな
く、このブランケツト層のグラニユール化汚泥量
が時間の経過に伴つて増加することはなかつた
が、安定な汚泥層が維持された。以上のように、
し尿をUASB法によつて処理するに際して、初
段UASB反応槽上部にスカムかき取り機を設置
して、発生スカムとして極力SSを分離除去し、
後段UASB反応槽へのSS特に腸内細菌由来のSS
の流入を抑制することで、後段UASB反応槽で
のスカム発生をなくせしめて、グラニユール化汚
泥の安定なスラツジブランケツトを保持形成させ
ることによつて初めて、UASB法をし尿のメタ
ン発酵処理に適用することが可能であつた。 Next, the wastewater treated in the first-stage UASB reactor was introduced into the second-stage UASB reactor 2 and subjected to upward flow methane fermentation through the distribution and inflow equipment 4' at the bottom of the reactor. Despite extremely active methane fermentation, no scum was generated. Therefore, the granulated sludge filled into the rear UASB reaction tank 2 as seed sludge at the beginning of the experiment did not float to the surface, and the amount of granulated sludge in this blanket layer did not increase over time. , a stable sludge layer was maintained. As mentioned above,
When treating human waste using the UASB method, a scum scraper is installed above the first stage UASB reaction tank to separate and remove as much SS as possible as generated scum.
SS to the subsequent UASB reaction tank, especially SS derived from enteric bacteria
By suppressing the inflow of sludge, the generation of scum in the subsequent UASB reaction tank is eliminated, and a stable sludge blanket of granulated sludge is retained and formed. This is the first time that the UASB method can be used for methane fermentation treatment of human waste. It was possible to apply it.
本考案の装置を使用してし尿をメタン発酵させ
るに際しては、発酵温度25℃好ましくは30℃以上
の温度で、発酵槽容積１当り0.2／日〜４
／日、の割合特に好ましくは1.0／日〜３
／日の割合で通水するのが好ましい。 When methane fermenting human waste using the device of the present invention, the fermentation temperature is 25°C, preferably 30°C or higher, and 0.2 to 4 times per day per fermenter volume.
/day, particularly preferably 1.0/day to 3
It is preferable to pass water at a rate of /day.
また、前段と後段の発酵槽における滞留時間
（通水割合）は同じでもよいが、酸発酵の難易度
及びメタン発酵の難易度によつて適宜変更するこ
とができる。 Further, the residence time (water flow rate) in the first and second fermenters may be the same, but can be changed as appropriate depending on the difficulty level of acid fermentation and the difficulty level of methane fermentation.
つぎに、実施例を示す。 Next, examples will be shown.
発酵槽容量3.5の初段発酵槽と、発酵槽容量
3.5のUASB発酵槽を直列に連結し、初段の発
酵槽には2.0の消以汚泥を、後段のUASB発酵
槽には1.0のグラニユール形成の終了した嫌気
性汚泥を装入した後、両発酵槽内の液温が33℃〜
37℃に保持されるよう両発酵槽に導入される液を
加温しながら、発酵槽１当り0.8／日のし尿
（SS濃度8000mg／、BOD15000mg／）を初段
発酵槽に導入し（滞留時間1.25日）、初段発酵槽
上部で浮上したスカムを分離し、溢流した汚水を
更に後段のUASB反応槽に導入してメタン発酵
を行なつた。後段のUASB槽に導入される液の
SSは23000mg／で後段のUASB槽ではスカムが
発生することなく、順調にメタン発酵が行なわれ
た。 First stage fermenter with fermenter capacity 3.5 and fermenter capacity
3.5 UASB fermenters are connected in series, and the first stage fermenter is charged with 2.0 sludge, and the second stage UASB fermenter is charged with 1.0 anaerobic sludge that has completed granule formation, and then both fermenters are charged. The liquid temperature inside is 33℃ ~
While heating the liquid introduced into both fermenters to maintain the temperature at 37°C, 0.8/day human waste (SS concentration 8000 mg/, BOD 15000 mg/) per fermenter was introduced into the first fermenter (residence time 1.25 (Japan), the scum that floated to the top of the first stage fermenter was separated, and the overflowing wastewater was further introduced into the second stage UASB reactor for methane fermentation. of the liquid introduced into the subsequent UASB tank.
SS was 23,000 mg/ml, and methane fermentation was carried out smoothly without scum occurring in the latter UASB tank.
第３図に経過日数とBOD除去率の関係を示す。 Figure 3 shows the relationship between the number of days elapsed and the BOD removal rate.
第３図に示す結果と、第１図に示す結果との比
較から判るように、本考案の処理装置全体に対す
るし尿処理時間（滞留時間）は2.5日と極めて短
かかつたにもかかわらず、BOD除去率は安定し
て平均68％が確保され、満足すべきものであつ
た。 As can be seen from the comparison between the results shown in Figure 3 and the results shown in Figure 1, although the human waste processing time (retention time) for the entire processing device of the present invention was extremely short at 2.5 days, The BOD removal rate was stable and maintained at an average of 68%, which was satisfactory.
本考案で達成しうる、がずか2.5日のし尿処理
時間は従来の実用されているし尿嫌気性消化槽の
それが平均30日というし尿処理時間を有している
ことから比較すれば、実に12倍の高負荷処理、高
速処理を達成していることとなり、その実用上の
効果はきわめて大きいものである。 The human waste processing time that can be achieved with this invention is only 2.5 days, compared to the average human waste processing time of 30 days in conventional human waste anaerobic digesters. This means that 12 times higher load processing and faster processing speed have been achieved, and the practical effects are extremely large.
前記実施例においては、発酵温度を33℃〜37℃
となるように加温を行ないながら、し尿を処理し
たが、初段反応槽への投入し尿の温度を一時的に
20℃とし、また初段反応槽の保温温度も一時的に
20℃とした場合には、初段反応槽内でのガス発生
が前記温度条件のそれに比べて半減した。そし
て、し尿中の腸内細菌性SSのほとんどが大粒径
のフロツクを形成してブランケツト化したもの
の、スカムとしての浮上は不十分にしかなされず
約6000mg／のSSが初段反応槽流出水に含まれ
ていた。このSSは次段UASB反応槽に流入した
際、グラニユール化汚泥中における活発なメタン
発酵能によつて大量のスカムを発生させ、グラニ
ユール化汚泥をも同伴浮上させグラニユール化汚
泥によるブランケツト層の汚泥濃度の低下を招い
た。 In the above examples, the fermentation temperature was 33°C to 37°C.
The human waste was processed while being heated so that the temperature of the human waste input into the first stage reaction tank was
20℃, and the temperature of the first stage reaction tank was also temporarily changed.
When the temperature was set at 20°C, gas generation in the first stage reaction tank was halved compared to that under the above temperature conditions. Although most of the enterobacterial SS in the human urine formed large particle-sized flocs and became a blanket, the scum was not sufficiently floated, and approximately 6000 mg/SS of SS entered the first stage reaction tank effluent. It was included. When this SS flows into the next stage UASB reaction tank, it generates a large amount of scum due to the active methane fermentation ability in the granulated sludge, and the granulated sludge is brought to the surface and the sludge concentration in the blanket layer due to the granulated sludge is increased. This led to a decline in
上記現象を防止するために初段反応槽と後段
UASB反応槽の中間に傾斜板沈殿槽を設けたと
ころ、初段反応槽から流出した大径フロツク化し
たSSは容易に沈降分離できた。その結果、一時
的な温度低下があつても中間に固液分離設備を付
設した本考案のし尿処理装置は十分な機能を維持
することができた。 In order to prevent the above phenomenon, the first stage reaction tank and the second stage
When an inclined plate sedimentation tank was installed in the middle of the UASB reaction tank, the large-diameter floc-formed SS flowing out from the first-stage reaction tank could be easily separated by sedimentation. As a result, even if there was a temporary temperature drop, the human waste treatment apparatus of the present invention, which was equipped with an intermediate solid-liquid separation facility, was able to maintain sufficient functionality.
この中間に設ける固液分離設備としては、初段
反応槽流出水に含まれた大径フロツク化したSS
の分離が可能なものであれば機能的に満足できる
ものであつて、単純沈殿槽、や、遠心分離機、メ
ンブランフイルター等の過膜等も利用できる。 The solid-liquid separation equipment installed in the middle is the large-diameter floc-formed SS contained in the first-stage reaction tank effluent.
As long as the separation is possible, it is functionally satisfactory, and a simple sedimentation tank, a centrifugal separator, a membrane filter such as a membrane filter, etc. can also be used.
第１図は、し尿をUASB法に適用した場合の
経過日数とBOD除去率の関係を示す図、第２図
は本考案の一実施例を示すUASB装置を示す図、
第３図はし尿を本考案装置で処理した場合の経過
日数とBOD除去率の関係を示す図である。
１……初段反応槽、２……UASB槽、３……
し尿供給ポンプ、４，４′……分配流入設備、５
……気液分離部、６……スカムかき取り装置、７
……発生ガス排出管、９……処理水排出管。
Fig. 1 is a diagram showing the relationship between the number of days elapsed and the BOD removal rate when human waste is applied to the UASB method, and Fig. 2 is a diagram showing a UASB device showing an embodiment of the present invention.
FIG. 3 is a diagram showing the relationship between the number of days elapsed and the BOD removal rate when human waste is treated with the device of the present invention. 1... Initial reaction tank, 2... UASB tank, 3...
Human waste supply pump, 4, 4'...distribution inflow equipment, 5
... Gas-liquid separation section, 6 ... Scum scraping device, 7
... Generated gas discharge pipe, 9... Treated water discharge pipe.
Claims (1)
−固−液分離部を設けてなる汚泥床式メタン発
酵槽にし尿を上向流に通水して処理する装置に
おいて、汚泥床式メタン発酵槽の前段に、底部
にし尿系汚水の分配流入管を、上部にスカムの
除去装置を設けた上向流発酵槽を設けたことを
特徴とするし尿系汚水の処理装置。 ２ ２つの汚泥床式メタン発酵槽の中間に、更に
固液分離装置を設けた実用新案登録請求の範囲
第１項記載のし尿系汚水の処理装置。[Scope of Claim for Utility Model Registration] 1. A sludge bed type methane fermentation tank comprising a distribution inflow pipe for human waste wastewater at the bottom and a gas-solid-liquid separation section at the top, in which human waste water is passed in an upward flow. The apparatus for treating human waste is characterized in that an upstream fermentation tank having a distribution inflow pipe for human waste wastewater at the bottom and a scum removal device at the top is installed in the front stage of the sludge bed type methane fermentation tank. Sewage treatment equipment. 2. The human waste wastewater treatment device according to claim 1, further comprising a solid-liquid separator between the two sludge bed type methane fermenters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8093286U JPH0217676Y2 (en) | 1986-05-30 | 1986-05-30 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8093286U JPH0217676Y2 (en) | 1986-05-30 | 1986-05-30 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62194499U JPS62194499U (en) | 1987-12-10 |
| JPH0217676Y2 true JPH0217676Y2 (en) | 1990-05-17 |
Family
ID=30932197
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8093286U Expired JPH0217676Y2 (en) | 1986-05-30 | 1986-05-30 |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0217676Y2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7727395B2 (en) * | 2008-07-23 | 2010-06-01 | PurposeEnergy, Inc. | Method and apparatus for processing organic waste |
-
1986
- 1986-05-30 JP JP8093286U patent/JPH0217676Y2/ja not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62194499U (en) | 1987-12-10 |
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