JPH0114839B2 - - Google Patents
Info
- Publication number
- JPH0114839B2 JPH0114839B2 JP57173310A JP17331082A JPH0114839B2 JP H0114839 B2 JPH0114839 B2 JP H0114839B2 JP 57173310 A JP57173310 A JP 57173310A JP 17331082 A JP17331082 A JP 17331082A JP H0114839 B2 JPH0114839 B2 JP H0114839B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- sludge
- human waste
- biological treatment
- treated water
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 59
- 238000000034 method Methods 0.000 claims description 33
- 239000010800 human waste Substances 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 18
- 239000010815 organic waste Substances 0.000 claims description 6
- 239000012295 chemical reaction liquid Substances 0.000 claims description 3
- 230000000717 retained effect Effects 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 claims 1
- 239000010802 sludge Substances 0.000 description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 7
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 5
- 230000000813 microbial effect Effects 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 150000007524 organic acids Chemical class 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000009287 sand filtration Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000001954 sterilising effect Effects 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- 229910018626 Al(OH) Inorganic materials 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002361 compost Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- -1 hydrogen ions Chemical class 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
- 230000003313 weakening effect Effects 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
本発明はし尿、各種産業廃液などの有機性廃液
の処理方法に関するものである。
従来のし尿処理において最も進歩したプロセス
として評価され実施例が激増しているプロセス
は、例えば、し尿に希釈水（10倍量程度）を添加
して生物学的硝化脱窒処理したのち、処理水を凝
集沈殿、砂過し、さらにオゾン処理、活性炭吸
着後、滅菌処理するという方法である。
このプロセスは現在秀れたプロセスとして評価
されているが、厳しい視点から技術評価すると、
次のような重大欠点を本質的に内在していること
を本発明者は認識するに至つた。
すなわち、
数多くの単位操作を直列的に並べているた
め、プロセスが複雑で維持管理性も悪い。
凝集沈殿又は凝集浮上工程に多量の無機凝集
剤の添加を必要とし、資源多消費型であるほか
難脱水性の凝集沈殿汚泥が発生し、その処理・
処分が難点となると同時に多大の経費を要す
る。また、凝集汚泥の存在はコンポスト製品の
品質を低下させる。
オゾン発生電力に約25KWH/Kg−O3という
多量の電力を必要とし、また活性炭処理に500
〜600円／Kg−し尿という高額の経費を要する。
生物処理工程の反応槽容積の決定には、年間
の最低水温における微生物反応速度を用いて設
計しなければならないので、どうしても生物処
理槽が大きくならざるを得ない。
本発明者は、このような現状に強い疑問を持ち
検討を進め本発明を完成した。本発明の効果は驚
くべきものと言つてもよく、従来の凝集沈殿、砂
過、オゾン処理、活性炭吸着、滅菌処理の各工
程が全く不要になり、しかも処理水質は著しく向
上する。
すなわち本発明は、し尿などの有機性廃液を生
物処理したのち、該処理水を蒸発濃縮しめ、該蒸
発水蒸気の凝縮水を前記有機性廃液の高度処理水
となすとともに、該凝縮水の保有熱によつて前記
生物処理工程内の反応液を加温することを特徴と
する有機性廃液の処理方法である。
以下に、本発明の一実施態様を図面を参照しな
がら説明する。
除渣したし尿（浄化槽汚泥が混入している場合
が多い）１を、これに希釈水を添加することなく
生物学的硝化脱窒素法による生物処理工程２に流
入せしめ、主としてBOD、NH3−Ｎなどの窒素
成分を充分除去する。生物処理工程２に希釈水を
多量に添加することは水温の低下を招くばかりで
なく蒸発対象水量が増加するので極めて好ましく
ない。
しかして、生物処理工程２から流出する活性汚
泥スラリー３は、遠心濃縮機などを使用する固液
分離工程４において固液分離され、分離汚泥５の
大部分は返送汚泥５′として生物処理工程２にリ
サイクルされる。
一方、余剰活性汚泥６はフイルタプレス、スク
リユープレスなどの汚泥脱水工程７で処理され、
脱水分離水８と、脱水ケーキ９（含水率63〜65
％）に分離される。
生物処理水１０はBOD、窒素成分は良好に除
去されているが非生物分解性COD、リン酸、色
度、有機性窒素が多量に残留している。このため
従来プロセスでは生物処理水１０に対し凝集沈
殿、砂過、オゾン処理、活性炭処理を行ない
COD、色度、リン酸、有機性窒素を除去してい
るのであるが、本発明はこのような問題点の多い
常套手段は採用しない。
即ち、生物処理水１０を蒸発工程１１の蒸発缶
１１′に供給し、蒸発せしめた水蒸気１２を蒸気
圧縮機１３にて圧縮昇温させたのち蒸発缶１１′
の間接加熱部１４に導き、水蒸気の凝縮潜熱を加
熱源として再利用する。
凝縮水１５は100℃弱の高温（蒸発缶１１′内は
ほぼ常圧）であるので、熱交換器１６に流入せし
めて生物処理水１０を予熱したのち、さらに生物
処理工程２内の熱交換器１７に流入させ、生物処
理槽内スラリーを加温し、冬期において微生物の
活性が弱まるのを防止してから、超高度処理水１
８となる。
超高度処理水１８は蒸留水であるので水質は極
めて良好であり、し尿の無希釈処理水として、従
来法では考えられない最高級の水質を示す。
一方、蒸発濃縮液１９は、噴霧燃焼など、任意
の焼却処分工程２０にて処分される。
さらに、この実施態様には重要概念の一つとし
て、次の点が含まれる。すなわち、し尿１を生物
処理する際に発生する微生物酸化熱（本発明者の
実測によれば、30000〜40000Kcal/Kl−し尿の発
熱量がある）によつて、生物処理槽内液温、した
がつて、生物処理水１０の温度が原し尿１の温度
よりも20〜30℃上昇する効果に着目し、微生物酸
化熱によつて温度上昇されたものをさらに予熱し
蒸発濃縮することが重要概念となつている。
以上のようにな実施態様では蒸発工程１１とし
て蒸気圧縮蒸発法によるものを採用した場合を説
明したが、多重効用法又は蒸気圧縮法と多重効用
法の併用によるものも効果的である。また、ゴミ
焼却場などの余熱を利用できる場合は、単効用蒸
発缶を使用しても問題はない。
以上のような本発明によれば、次のような重要
効果を得ることができる。
熱エネルギーを合理的に利用し、冬季など低
水温、低気温時でも生物処理槽内を微生物の活
動に好適な高水温に維持できる。
従来プロセスでは望むべくもない最高級の処
理水質が得られると同時に、プロセスも著く簡
略化される。
凝集剤、オゾン発生電力、活性炭、滅菌剤の
すべてが不要になる。
難脱水性汚泥として周知の無機凝集汚泥
（Al（OH）3、又はFe（OH）3を主成分とする）が
全く発生しないので、処理すべき汚泥は余剰生
物汚泥だけですみ、汚泥処理・処分の経費が著
しく節減できる。
脱水ケーキ中に難脱水性無機凝集汚泥が混入
していないので脱水ケーキの発熱量が約4000K
ｃａｌ／Kg−D.S.と高く、含水率も65％以下にする
ことが容易であるため、燃料的性状に秀れてい
る。従つて、自燃するので重油などの補助燃料
を必要としない。この効果が省エネルギーに大
きく寄与する。
蒸発対象水は、生物処理水でありし尿を直接
蒸発処理するのではないから臭気発生、アンモ
ニア、揮発性有機酸の飛散がなく、しかもし尿
中の高濃度のSS成分による蒸発缶内の目詰ま
り、流動不能現象も起きない。
従来のし尿処理水の塩素イオン濃度は300mg/
程度と高いため、山林・田畑のかんがい用水
にすることは塩類障害のため困難であるが、本
発明の処理水素イオンは０〜１mg/程度であ
るため、容易にかんがい用水に再利用できる。
さらに、し尿を直接蒸発処理すると、し尿中
に存在する硫化物、有機酸のため蒸発缶の腐蝕
の可能性が大きいが、本発明は、生物処理によ
つて硫化物及び有機酸を除去してあるので上記
の問題は解消される。
次に本発明の実施例について記す。
実施例
神奈川県某し尿処理場に搬入されるし尿（浄化
槽汚泥が10％混入）をロータリスクリーンによつ
て除渣したのち、し尿処理量１Kl/日の規模で硝
化液循環型の生物学的硝化脱窒素工程により無希
釈処理した。生物学的硝化脱窒素工程のMLSSは
18000〜20000mg/、滞留日数は７日間とした。
生物処理槽内の水温は微生物酸化熱のため33〜42
℃となつた。
生物処理槽流出スラリーの固液分離には無薬注
型遠心濃縮機（巴工業製品）を使用し、濃縮汚泥
（濃度５〜６％）の大部分を脱窒槽にリサイクル
させ、一部を余剰汚泥として脱水工程に供給し
た。脱水機には全自動フイルタプレスを採用し
た。脱水ケーキの含水率は63〜64％、ケーキ発熱
量は約4000Kcal/Kg−DrySolidであり、流動床焼
却炉で容易に自燃した。
しかして、遠心濃縮分離水を蒸気圧縮蒸発缶に
供給し、濃縮比50倍に濃縮し20／日の濃縮液と
180／日の水蒸気凝縮水（これがし尿の高度処
理水である）を得た。凝縮水（温度100℃）で蒸
発缶供給液（遠心分離水）を予熱したのち、温度
60℃に低下した凝縮水をさらに生物処理槽内に設
置した蛇管式熱交換器に流入させたところ、生物
焼却槽内の液温は冬期（原し尿の温度５〜８℃）
においても39〜42℃に維持できた。一方、凝縮水
によつて生物処理槽を加温しない場合の生物処理
槽内の液温は28〜30℃であつた。
除渣し尿、生物学的硝化脱窒処理水（生物処理
水）および高度処理水（凝縮水）の水質は次表の
とおりであつた。
The present invention relates to a method for treating organic waste liquids such as human waste and various industrial waste liquids. A process that has been evaluated as the most advanced in conventional human waste treatment, and the number of examples of which has been rapidly increasing, is, for example, adding diluted water (approximately 10 times the amount) to human waste, performing biological nitrification and denitrification treatment, and then processing the treated water. This method involves coagulating sedimentation, sand filtration, ozone treatment, activated carbon adsorption, and sterilization. This process is currently being evaluated as an excellent process, but when the technology is evaluated from a strict perspective,
The present inventor has come to realize that the following serious drawbacks are inherently inherent. In other words, because many unit operations are arranged in series, the process is complex and maintenance is poor. The coagulation-sedimentation or coagulation-floating process requires the addition of a large amount of inorganic flocculant, which is resource-intensive and produces coagulation-sedimentation sludge that is difficult to dewater.
Disposal is difficult and requires a great deal of expense. Also, the presence of flocculated sludge reduces the quality of the compost product. A large amount of electricity is required for ozone generation, approximately 25KWH/Kg- O3 , and 500KWH is required for activated carbon treatment.
~600 yen/Kg - requires a high cost of human waste. When determining the reaction tank volume for the biological treatment process, the microbial reaction rate at the annual lowest water temperature must be used in the design, so the biological treatment tank has no choice but to be large. The present inventor had strong doubts about the current situation and proceeded with studies to complete the present invention. The effects of the present invention can be said to be surprising; the conventional steps of coagulation and sedimentation, sand filtration, ozone treatment, activated carbon adsorption, and sterilization are completely unnecessary, and the quality of treated water is significantly improved. That is, the present invention biologically treats organic waste liquid such as human waste, then evaporates and concentrates the treated water, converts the condensed water of the evaporated water vapor into highly treated water of the organic waste liquid, and reduces the heat retained in the condensed water. This is a method for treating an organic waste liquid, characterized in that the reaction liquid in the biological treatment step is heated by a method of heating the reaction liquid in the biological treatment step. An embodiment of the present invention will be described below with reference to the drawings. The removed human waste (often contaminated with septic tank sludge) 1 is passed into the biological treatment process 2 using the biological nitrification and denitrification method without adding dilution water, which mainly produces BOD, NH 3 - Thoroughly remove nitrogen components such as N. Adding a large amount of dilution water to the biological treatment step 2 not only causes a drop in water temperature but also increases the amount of water to be evaporated, which is extremely undesirable. The activated sludge slurry 3 flowing out from the biological treatment process 2 is subjected to solid-liquid separation in a solid-liquid separation process 4 using a centrifugal concentrator, and most of the separated sludge 5 is returned to the biological treatment process 2 as return sludge 5'. will be recycled. On the other hand, the surplus activated sludge 6 is processed in a sludge dewatering process 7 such as a filter press or screw press.
Dehydrated separated water 8 and dehydrated cake 9 (moisture content 63-65
%). In biologically treated water 10, BOD and nitrogen components were successfully removed, but large amounts of non-biodegradable COD, phosphoric acid, chromaticity, and organic nitrogen remained. For this reason, in the conventional process, biologically treated water 10 is subjected to coagulation sedimentation, sand filtration, ozone treatment, and activated carbon treatment.
Although COD, chromaticity, phosphoric acid, and organic nitrogen are removed, the present invention does not employ conventional methods that are fraught with such problems. That is, the biologically treated water 10 is supplied to the evaporator 11' of the evaporation step 11, and the evaporated water vapor 12 is compressed and heated by the vapor compressor 13, and then transferred to the evaporator 11'.
The latent heat of condensation of the water vapor is reused as a heating source. Since the condensed water 15 is at a high temperature of just under 100°C (approximately normal pressure inside the evaporator 11'), it flows into the heat exchanger 16 to preheat the biologically treated water 10, and then undergoes heat exchange in the biological treatment process 2. The slurry in the biological treatment tank is heated to prevent the activity of microorganisms from weakening in the winter, and then the ultra-highly treated water 1
It becomes 8. Since the ultra-highly treated water 18 is distilled water, the water quality is extremely good, and as undiluted treated water of human waste, it exhibits the highest quality water that would be unimaginable with conventional methods. On the other hand, the evaporative concentrate 19 is disposed of in an arbitrary incineration process 20 such as spray combustion. Furthermore, this embodiment includes the following points as one of the important concepts. That is, due to the microbial oxidation heat generated when human waste 1 is biologically treated (according to actual measurements by the inventor, the calorific value of human waste is 30,000 to 40,000 Kcal/Kl), the temperature of the liquid in the biological treatment tank increases. Therefore, we focused on the effect that the temperature of the biologically treated water 10 rises by 20 to 30 degrees Celsius compared to the temperature of the raw human waste 1, and the important concept is to further preheat and evaporate the water whose temperature has been raised by the heat of microbial oxidation. It is becoming. In the embodiments described above, the vapor compression evaporation method is used as the evaporation step 11, but a multiple effect method or a combination of the vapor compression method and the multiple effect method is also effective. Furthermore, if residual heat from a garbage incinerator or the like can be used, there is no problem in using a single-effect evaporator. According to the present invention as described above, the following important effects can be obtained. By using thermal energy rationally, it is possible to maintain the inside of the biological treatment tank at a high water temperature suitable for microbial activity even during low water and air temperatures such as in winter. This method provides the highest quality treated water that could not be achieved using conventional processes, and at the same time, the process is significantly simplified. Flocculants, ozone generating electricity, activated carbon, and sterilizers are all eliminated. Since no inorganic flocculated sludge (mainly composed of Al(OH) 3 or Fe(OH) 3 ), which is well known as sludge that is difficult to dewater, is not generated, the only sludge that needs to be treated is excess biological sludge, and sludge treatment and Disposal costs can be significantly reduced. The calorific value of the dehydrated cake is approximately 4000K because no inorganic flocculated sludge that is difficult to dewater is mixed in the dehydrated cake.
It has excellent fuel properties because it has a high cal/Kg-DS and the water content can be easily reduced to 65% or less. Therefore, since it self-combusts, it does not require auxiliary fuel such as heavy oil. This effect greatly contributes to energy saving. The water to be evaporated is biologically treated water, and human waste is not directly evaporated, so there is no odor, ammonia, or volatile organic acid scattering, and there is no clogging in the evaporator due to the high concentration of SS components in urine. , no flowability phenomenon occurs. The chloride ion concentration of conventional human waste water is 300mg/
However, since the amount of hydrogen ions treated in the present invention is about 0 to 1 mg/1, it is difficult to use water for irrigation in mountains and forests and fields because of the salt damage. Furthermore, if human waste is directly evaporated, there is a high possibility that the evaporator will be corroded due to the sulfides and organic acids present in the human waste, but the present invention removes sulfides and organic acids through biological treatment. Therefore, the above problem is solved. Next, examples of the present invention will be described. Example: Human waste (containing 10% septic tank sludge) delivered to a certain human waste treatment plant in Kanagawa Prefecture is removed using a rotary screen, and then biological nitrification is carried out using nitrifying liquid circulation at a scale of 1 Kl/day of human waste. It was treated without dilution through a denitrification process. MLSS of biological nitrification and denitrification process is
The dose was 18,000 to 20,000 mg/distance and the residence time was 7 days.
The water temperature in the biological treatment tank is 33-42 due to heat of microbial oxidation.
It became ℃. A chemical-free centrifugal concentrator (Tomoe Kogyo products) is used for solid-liquid separation of the slurry flowing out of the biological treatment tank, and most of the thickened sludge (concentration 5-6%) is recycled to the denitrification tank, with some remaining as surplus. It was supplied to the dewatering process as sludge. A fully automatic filter press was used for the dehydrator. The moisture content of the dehydrated cake was 63-64%, the cake calorific value was about 4000 Kcal/Kg-DrySolid, and it easily self-combusted in a fluidized bed incinerator. Then, the centrifugally concentrated separated water is supplied to a vapor compression evaporator and concentrated to a concentration ratio of 50 times, resulting in a concentrated liquid of 20 times a day.
180/day of steam condensed water (this is highly treated human waste water) was obtained. After preheating the evaporator feed liquid (centrifuged water) with condensed water (temperature 100℃), the temperature
When the condensed water, which had dropped to 60℃, was further flowed into a corrugated pipe heat exchanger installed in the biological treatment tank, the liquid temperature in the biological incinerator was found to be the same as in winter (the temperature of raw human waste is 5 to 8℃).
It was also possible to maintain the temperature at 39-42°C. On the other hand, when the biological treatment tank was not heated by condensed water, the liquid temperature in the biological treatment tank was 28 to 30°C. The water quality of the filtered human waste, biologically nitrified and denitrified treated water (biologically treated water), and advancedly treated water (condensed water) was as shown in the table below.
【表】
なお、前記濃縮液は汚泥の流動層焼却炉に噴霧
させ燃焼処分した。[Table] The concentrated liquid was sprayed into a sludge fluidized bed incinerator and burned.
図面は、本発明の一実施態様を示すフローシー
トである。
１…し尿、２…生物処理工程、３…活性汚泥ス
ラリー、４…固液分離工程、５…分離汚泥、５′
…返送汚泥、６…余剰活性汚泥、７…汚泥脱水工
程、８…脱水分離水、９…脱水ケーキ、１０…生
物処理水、１１…蒸発工程、１１′…蒸発缶、１
２…水蒸気、１３…蒸気圧縮機、１４…間接加熱
部、１５…凝縮水、１６，１７…熱交換器、１８
…超高度処理水、１９…蒸発濃縮液、２０…焼却
処分工程。
The drawing is a flow sheet illustrating one embodiment of the invention. 1... Human waste, 2... Biological treatment process, 3... Activated sludge slurry, 4... Solid-liquid separation process, 5... Separated sludge, 5'
...Return sludge, 6... Surplus activated sludge, 7... Sludge dewatering process, 8... Dehydrated separated water, 9... Dehydrated cake, 10... Biological treatment water, 11... Evaporation process, 11'... Evaporator, 1
2... Steam, 13... Vapor compressor, 14... Indirect heating section, 15... Condensed water, 16, 17... Heat exchanger, 18
...Ultra-highly treated water, 19. Evaporation concentrate, 20. Incineration disposal process.
Claims (1)
該処理水を蒸発濃縮せしめ、該蒸発水蒸気の凝縮
水を前記有機性廃液の高度処理水となすととも
に、該凝縮水の保有熱によつて前記生物処理工程
内の反応液を加温することを特徴とする有機性廃
液の処理方法。1 After biologically treating organic wastewater such as human waste,
The treated water is evaporated and concentrated, the condensed water of the evaporated water vapor is used as the highly treated water of the organic waste liquid, and the reaction liquid in the biological treatment process is heated by the heat retained in the condensed water. Features of organic waste liquid treatment method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57173310A JPS5966398A (en) | 1982-10-04 | 1982-10-04 | Treatment of organic waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57173310A JPS5966398A (en) | 1982-10-04 | 1982-10-04 | Treatment of organic waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5966398A JPS5966398A (en) | 1984-04-14 |
| JPH0114839B2 true JPH0114839B2 (en) | 1989-03-14 |
Family
ID=15958071
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57173310A Granted JPS5966398A (en) | 1982-10-04 | 1982-10-04 | Treatment of organic waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5966398A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104418472A (en) * | 2013-09-11 | 2015-03-18 | 三菱丽阳株式会社 | Treatment device and treatment method of wastewater containing organic matters |
| CN117509993B (en) * | 2024-01-04 | 2024-04-09 | 清大国华环境集团股份有限公司 | Physical and chemical high-concentration waste liquid treatment process |
-
1982
- 1982-10-04 JP JP57173310A patent/JPS5966398A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5966398A (en) | 1984-04-14 |
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