JPS6019490A - Aeration of fermentation tank - Google Patents
Aeration of fermentation tankInfo
- Publication number
- JPS6019490A JPS6019490A JP58127817A JP12781783A JPS6019490A JP S6019490 A JPS6019490 A JP S6019490A JP 58127817 A JP58127817 A JP 58127817A JP 12781783 A JP12781783 A JP 12781783A JP S6019490 A JPS6019490 A JP S6019490A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- heat
- fermenter
- fermentation
- heat exchanger
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/24—Recirculation of gas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/26—Conditioning fluids entering or exiting the reaction vessel
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/59—Biological synthesis; Biological purification
Abstract
Description
【発明の詳細な説明】
本発明は、有機汚泥をコンポスト化するだめの発酵槽の
送気方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for supplying air to a fermenter for composting organic sludge.
一般に下水等の有機汚泥は、発酵槽に貯留して空気を送
入し、有機物を発酵させてコンポスト化しているが、発
酵槽の送気方法としては、−過式か或いは循環式が採用
されている。Generally, organic sludge such as sewage is stored in a fermenter and air is pumped in to ferment the organic matter and compost it. However, the air supply method for the fermenter is either a through type or a circulation type. ing.
ところが、−過式は、発酵槽に供給した空気が有機物を
発酵させて発酵槽から排ガスとして排出されると、その
排ガスは再循環されることなく全量放出されるため、排
ガスの温度があまり高くならず、排ガス中の熱を回収す
る場合、その廃熱を回収する熱交換器によって発酵槽に
供給される空気を加温しても、その空気を十分な温度゛
まで加温することができず、別途加温設備を設けて空気
を加温しなければならなかった。However, in the double-pass type, when the air supplied to the fermenter ferments the organic matter and is discharged from the fermenter as exhaust gas, the exhaust gas is not recirculated and is released in its entirety, so the temperature of the exhaust gas is too high. However, if heat is recovered from the exhaust gas, even if the air supplied to the fermenter is heated by a heat exchanger that recovers the waste heat, the air cannot be heated to a sufficient temperature. First, separate heating equipment had to be installed to heat the air.
また、−過式においては、排ガスの全量が放出されるた
め、放出される排ガスの脱臭処理量が多くなり、脱臭設
備が大型となる欠点があった。In addition, in the overpass type, since the entire amount of exhaust gas is released, the amount of the released exhaust gas to be deodorized increases, and the deodorizing equipment becomes large-sized.
これに対し、循環式は、排ガスの一部を発酵槽内に再循
環させているため、排ガスの温度が高くなり、排ガスの
廃熱を利用して発酵槽へ供給する空気ン十分に加温する
ことができると共に、排ガスの脱臭処理量が少く、脱臭
処理設置を小型にすることができる利点はあるが、排ガ
ス中には発酵槽内で、蒸発した水分が多量に含まれてい
るため、その排ガスが発酵槽内に再循環されると、発酵
槽内で発酵中の有機汚泥の含水率が増加して発酵効率が
低下し、良質のコンポストを得ることができなかった。On the other hand, with the circulation type, a portion of the exhaust gas is recirculated into the fermenter, so the temperature of the exhaust gas becomes high, and the waste heat of the exhaust gas is used to sufficiently heat the air supplied to the fermenter. It has the advantage that the amount of deodorizing treatment of exhaust gas is small and the deodorizing treatment installation can be made compact, but since the exhaust gas contains a large amount of water that evaporated in the fermenter, When the exhaust gas was recirculated into the fermenter, the moisture content of the organic sludge undergoing fermentation in the fermenter increased, reducing fermentation efficiency and making it impossible to obtain high-quality compost.
また、循環式においては、排ガス中に多量の水分が含ま
れているだめ、排ガスを脱臭処理する脱臭材等が劣化し
て脱臭能力が低下する欠点があり、更には、排ガス中に
多量の粉塵が含まれるだめ、排ガスを水洗して除塵する
こともあるが、排ガスを水洗すると発酵槽へ再循環する
排ガスの温度が低下し、発酵効率が低下するという欠点
があった。In addition, the circulation type has the disadvantage that the exhaust gas contains a large amount of moisture, and the deodorizing material used to deodorize the exhaust gas deteriorates, reducing its deodorizing ability. In some cases, the exhaust gas is washed with water to remove dust, but washing the exhaust gas with water lowers the temperature of the exhaust gas that is recirculated to the fermenter, reducing fermentation efficiency.
本発明は、上記従来の欠点に鑑み提案されたもので、発
酵槽に供給される空気を、発酵槽から排出される排ガス
の廃熱を回収する熱交換器によって加温すると共に、熱
交換器によって熱回収された排ガスを、ヒートポンプ式
の除湿兼加熱器によって除湿・加温させた後、その一部
を発酵槽内に再循環させ、残部の排ガスを脱臭しブヒ後
放出するようにして、循環排ガスの除湿・加温を能率よ
く行なって、発酵効率がよく、ランニングコストが低摩
でしかも脱臭処理が簡易に行い得る発酵槽の送８気方法
を提供しようとするものである。The present invention has been proposed in view of the above-mentioned drawbacks of the conventional technology. The heat recovered exhaust gas is dehumidified and heated by a heat pump type dehumidifier/heater, and then part of it is recirculated into the fermenter, and the remaining exhaust gas is deodorized and released after fermentation. To provide an air supply method for a fermenter that efficiently dehumidifies and warms circulating exhaust gas, has good fermentation efficiency, has low running cost, and can easily perform deodorizing treatment.
以下、本発明を図面に示す実施例に基づいて具体的に説
明する。Hereinafter, the present invention will be specifically described based on embodiments shown in the drawings.
図面は本発明に係る発酵槽の送気方法の１実施例を示す
フローシート図である。The drawing is a flow sheet diagram showing one embodiment of the method for supplying air to a fermenter according to the present invention.
図中Ａは有機汚泥をコンポスト化するための発酵室が上
下２段ある立型の発酵槽で、上段の発酵室Ａ＋と下段の
発酵室Ａ２とを有している。In the figure, A is a vertical fermenter with two fermentation chambers, upper and lower, for composting organic sludge, and has an upper fermentation chamber A+ and a lower fermentation chamber A2.
ＢはファンＦ、（よって上段の発酵室Ａ、に供給される
新鮮な空気（１）を加温する熱交換器で、加温された空
気（２）は上段の゛発酵室Ａ、の底部に供給されるよう
になっている。上段の発酵室Ａ１の排ガス（３）と下段
の発酵室Ａ、の排ガス（４）を合せた排ガス（５）は、
熱交換器Ｂに送られて廃熱が回収され、熱交換器Ｂを通
過する新鮮な空気（１）を加温する。B is a heat exchanger that heats the fresh air (1) supplied to the fan F (and thus the upper fermentation chamber A), and the heated air (2) is sent to the bottom of the upper fermentation chamber A. The exhaust gas (5) is a combination of the exhaust gas (3) from the upper fermentation chamber A1 and the exhaust gas (4) from the lower fermentation chamber A.
The waste heat is sent to heat exchanger B where it is recovered and warms the fresh air (1) passing through heat exchanger B.
熱交換器Ｂによって熱回収された排ガス（６）は、水洗
塔Ｃに送られ、ことで散水されて排ガス（６）中の、粉
塵が除却されるが、同時に臭気の一成分であるアンモニ
ア等も一部水に溶けて除去されることになる。The exhaust gas (6) whose heat has been recovered by the heat exchanger B is sent to the water washing tower C, where it is sprinkled with water to remove dust in the exhaust gas (6), but at the same time remove ammonia, etc., which is a component of odor. Some of it will also dissolve in water and be removed.
なお、水洗塔Ｃから出た排水は、図示しない排水処理施
設に導かれて処理されるようになっている。Note that the wastewater discharged from the washing tower C is led to a wastewater treatment facility (not shown) for treatment.
また、Ｄはヒートポンプ式の除湿兼加熱器で、との調湿
ユニットはエバポレータとコンデンサーとコンプレッサ
及び送Ｘ機からなっている。In addition, D is a heat pump type dehumidifying/heating device, and D is a humidity control unit consisting of an evaporator, a condenser, a compressor, and an X sender.
そして、水洗塔Ｃによって水洗された排ガス（７）は、
ヒートポンプ式の除湿兼加熱器りに送られる。The exhaust gas (7) washed with water by the water washing tower C is
The water is sent to a heat pump type dehumidifier/heater.
水洗塔Ｃによって水洗された排ガスけ）は、水分がほぼ
飽和状態となっているが、調湿ユニットのエバポレータ
によって蒸発される冷媒ガスの蒸発熱によって冷却され
、排ガス（７）の水分は凝縮して除去され除湿されるこ
とになる。エバポレータによって除湿された排ガスは、
次にコンデンサーによって凝縮される冷媒ガスの凝縮熱
によって加等されることになる。The exhaust gas drain (7) washed with water by the water washing tower C is almost saturated with moisture, but it is cooled by the heat of evaporation of the refrigerant gas evaporated by the evaporator of the humidity control unit, and the moisture in the exhaust gas (7) is condensed. It will be removed and dehumidified. The exhaust gas dehumidified by the evaporator is
Next, it will be added by the heat of condensation of the refrigerant gas condensed by the condenser.
このように、排ガス（ηの通路にヒートポンプ式の除湿
兼加熱器りを設けておけば６ｖ冷媒ガスを圧縮するコン
プレッサと送風機を駆動するだけの少ない動力で、排ガ
ス（７）の除湿と加温を一つの調湿ユニットで行なうこ
とができる。In this way, if a heat pump type dehumidifying/heating device is installed in the passage of the exhaust gas (η), the exhaust gas (7) can be dehumidified and heated with the small amount of power required to drive the compressor and blower that compresses the 6V refrigerant gas. can be done with one humidity control unit.
ヒートポンプ式の除湿兼加熱器りによって除湿・加温さ
れた排ガス（８１は、その一部を分岐させてファンＦ、
により循環用の排ガス（９）として下段の発酵室Ａ２の
底部に供給され、再循環される。Exhaust gas (81) is dehumidified and heated by a heat pump type dehumidifier/heater (81 is a part of the exhaust gas that is branched off to the fan F,
The exhaust gas (9) is supplied to the bottom of the lower fermentation chamber A2 as a circulating exhaust gas (9), and is recirculated.
また、残部の排ガス（１０Ｉ）は、ファンＦ、によって
脱臭床５に送られ５、ここで脱臭された後、ファントに
て大気中に放出されるようになっている。The remaining exhaust gas (10I) is sent to a deodorizing bed 5 by a fan F, where it is deodorized and then released into the atmosphere by a fan.
上記構成よりなる本発明の発酵槽の送気方法の有効性を
確認するため、図示のフ四−シートに基づいて、含水率
６５チ程度の有機汚泥の加圧脱水ケーキを、１５ ｔｏ
ｎ／日の処理能力を有する発酵槽Ａでコンポスト化させ
たところ、図中（１）〜ａ〔に示す部分の乾ガス流量Ｑ
Ｄと温度Ｔ、相対湿度Ｈ水分量Ｗは次表に示すような値
となった。In order to confirm the effectiveness of the air supply method for the fermenter of the present invention having the above configuration, 15 to
When composting was performed in fermenter A with a processing capacity of n/day, the dry gas flow rate Q in the parts (1) to a [in the figure]
D, temperature T, relative humidity H, moisture content W had values as shown in the following table.
この表からも解るように、ヒートポンプ式の除湿兼加熱
器りを設けると、温度Ｔ＝３０℃、相対湿度Ｈ＝１００
％の排ガス（７）は、温度Ｔ＝５５℃、相対湿度Ｈ＝１
３％まで加温除湿することができ、下段の発酵室Ａ２の
底部に再循環される排ガス（９）の温度Ｔは５５℃まで
高められ、相対湿度Ｈも１３チまで低下した。また、上
段の発酵室Ａ、の底部に供給される空気（２）の温度Ｔ
も、排ガス（５）の廃熱を回収する熱交換器Ｂにょつて
３５℃まで高めることができた。従って、発酵槽Ａの各
発酵室Ａ１．Ａ、内は高温に保たれ、循環される排ガス
（９）によって有機汚泥の含水率が増加することもない
ので、発酵が促進され、効率良く良質のコンポストを得
ることができた。As can be seen from this table, if a heat pump type dehumidifying/heating device is installed, the temperature T = 30°C and the relative humidity H = 100°C.
% exhaust gas (7) has a temperature T = 55°C and a relative humidity H = 1
It was possible to heat and dehumidify up to 3%, and the temperature T of the exhaust gas (9) recirculated to the bottom of the lower fermentation chamber A2 was increased to 55° C., and the relative humidity H was also reduced to 13° C. Also, the temperature T of the air (2) supplied to the bottom of the upper fermentation chamber A.
It was also possible to raise the temperature to 35°C using heat exchanger B, which recovers waste heat from exhaust gas (5). Therefore, each fermentation chamber A1 of the fermenter A. A. Since the inside was kept at a high temperature and the water content of the organic sludge did not increase due to the circulated exhaust gas (9), fermentation was promoted and high quality compost could be obtained efficiently.
なお、このとき使用したヒートポンプ式の除湿兼加熱器
りの必要動力は、コンプレッサが１１ＫＩＴ、送風機が
１．５ Ｋ１１１の合せて１２．５．にＷであり、２４
時間連続運転で負荷率を０．９５ 、Ｉ ＫＷ＝ ２０
円としてランニングコストを計算すると、
（１１ＫＷ＋１．５ＫＷ）、Ｘ２４ ｈｒ Ｘｏ、 ９
５Ｘ ２０７２／ＫＷｈ＝５７００円／日
となる。The required power for the heat pump type dehumidifying/heating device used at this time was 11KIT for the compressor and 1.5KIT for the blower, totaling 12.5KIT. is W and 24
Continuous operation for hours, load factor 0.95, I KW = 20
Calculating the running cost in yen: (11KW + 1.5KW), X24 hr Xo, 9
5X 2072/KWh=5700 yen/day.
これに対し、ヒートポンプ式の除湿兼加熱器りを用いず
に、２０℃の空気を重油だきの熱風発生炉で５５℃まで
加温して下段の発酵室んの底部に５０ｄ／分の流量で供
給するには、重油が１０〜１５Ｋ＜！／ｈｒ必要であっ
た。含重油の率的消費量を１２に９／ｍｒ、重油のコス
トを７５円／Ｋｇトしてランニングコストを計算すると
、１２ＫＱ／ｍｒ Ｘ ２４ ｈｒＸ ７５円／に９＝
２１，６００円／日となり、本発明の方がランニングコ
ストが大幅に少なくなり、実用上きわめて有効であるこ
とがわかる。On the other hand, without using a heat pump type dehumidifying/heating device, air at 20°C is heated to 55°C in a heavy oil-fired hot air generator, and the air is heated to 55°C at a flow rate of 50 d/min at the bottom of the lower fermentation chamber. To supply, heavy oil is 10-15K<! /hr was necessary. Calculating the running cost by adding the rate of consumption of heavy oil to 12 to 9/mr and the cost of heavy oil to 75 yen/Kg, 12KQ/mr x 24 hrX 75 yen/to 9 =
The cost is 21,600 yen/day, which shows that the running cost of the present invention is significantly lower and is extremely effective in practice.
なお、本実施例においては、熱交換器Ｂとヒートポンプ
式の除湿兼加熱器りとの間に水洗塔Ｃを設けているが、
水洗塔Ｃに送られてくる排ガス（６）は熱交換器Ｂによ
って廃熱回収され、温度が低下しているので、水洗塔Ｃ
で散水される冷却水量は比較的少なくてよく、場合によ
っては水洗塔Ｃを省略してもよい。In this embodiment, a water washing tower C is provided between the heat exchanger B and the heat pump type dehumidifying/heating device.
The exhaust gas (6) sent to the water washing tower C has waste heat recovered by the heat exchanger B, and the temperature has decreased, so the waste gas (6) is sent to the water washing tower C.
The amount of cooling water sprinkled in the step C may be relatively small, and the water washing tower C may be omitted in some cases.
また、本発明においては、脱臭床Ｅで脱臭される排ガス
（１０）はヒートポンプ式の除湿兼加熱器りによって十
分に除湿、加温されているので、脱臭材としてコンポス
トを使用しても、排ガス（１０）中の水分が脱臭用のコ
ンポストに移行して、コンポストの性状を劣化させるこ
とはない。更に、本実゛雄側は文型の上下２段の発酵槽
に適用した場合について示しているが、本発明は各種型
式の発酵槽にも応用し得ることはいうまでも ・ない。In addition, in the present invention, the exhaust gas (10) deodorized on the deodorizing floor E is sufficiently dehumidified and heated by the heat pump type dehumidifying/heating device, so even if compost is used as a deodorizing material, the exhaust gas (10) (10) The moisture inside will not transfer to the deodorizing compost and deteriorate the properties of the compost. Furthermore, although the present invention is applied to two fermenters, upper and lower, it goes without saying that the present invention can be applied to various types of fermenters.
本発明は上記のように構成されているので、ヒートポン
プ式Ｃ除湿兼加ｊ熱器によって排ガスを少ない動力で除
湿、加温することができ、ランニングコストが安くなる
と共に、排ガスはヒートポンプ式の除湿兼加熱器によっ
て十分に除湿、加温された後、発酵槽内に再循環される
ので、発酵槽内を高温に保つことができ、しかも発酵中
の有機汚泥の含水率を高めることはないので、高い発酵
効率を維持することができる。Since the present invention is configured as described above, exhaust gas can be dehumidified and heated using a heat pump type C dehumidifier/heater with a small amount of power, and running costs are reduced. After being sufficiently dehumidified and heated by the combined heater, it is recirculated into the fermenter, allowing the inside of the fermenter to be kept at a high temperature without increasing the moisture content of the organic sludge during fermentation. , high fermentation efficiency can be maintained.
また、発酵槽に供給される空気は、発酵槽から排出され
る高温の排ガスの廃熱を回収する熱交換器によって十分
に加温することができるので、別途加臨股備を設ける必
要がなく、しかも、排ガスは十分に除湿された後脱臭さ
れて放出されるので、排ガス中の水分によって脱臭材等
が劣化して脱臭能率が低下することはなく、脱臭処理量
も少なくてすむ等多くの利点を有するものである。In addition, the air supplied to the fermenter can be sufficiently heated by a heat exchanger that recovers waste heat from the high-temperature exhaust gas discharged from the fermenter, eliminating the need for separate heating equipment. Moreover, since the exhaust gas is sufficiently dehumidified and then deodorized and released, the deodorizing material etc. will not deteriorate due to moisture in the exhaust gas and the deodorizing efficiency will not decrease, and the amount of deodorizing treatment can be reduced. It has advantages.
図面は本発明に係る発酵槽の送気方法の一実゛雄側を示
すフローシート図である。
Ａ・・・・・・発酵槽 Ｂ・・・・・・熱交換器Ｃ・・
・−・・水洗塔 Ｄ・・・・・・ヒートポンプ式のＥ−
−１−０脱臭床 除湿兼加熱器
Ｆ、〜Ｆ４・・・ファン （１） 、 （２）・・・空
気（３）〜（１０）・・・排ガスThe drawing is a flow sheet diagram showing an example of the method for supplying air to a fermenter according to the present invention. A... Fermenter B... Heat exchanger C...
・・・・Water washing tower D・・・・・・Heat pump type E-
-1-0 Deodorizing floor Dehumidifier/heater F, ~F4...Fan (1), (2)...Air (3)-(10)...Exhaust gas
Claims (1)
スの廃熱を回収する熱交換器によって加温すると共に、
熱交換器によって熱回収された排ガスを、ヒートポンプ
式の除湿兼加熱器によって除湿、加温させた後、その一
部を発酵槽内に再循環させ、残部の排ガスを脱臭した後
放出するようにしたことを特徴とする発酵槽の送気方法
。The air supplied to the fermenter is heated by a heat exchanger that recovers waste heat from the exhaust gas discharged from the fermenter, and
The exhaust gas whose heat is recovered by the heat exchanger is dehumidified and warmed by a heat pump-type dehumidifier/heater, and then part of it is recirculated into the fermenter, and the remaining exhaust gas is deodorized and then released. A method for supplying air to a fermenter, which is characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58127817A JPS6019490A (en) | 1983-07-15 | 1983-07-15 | Aeration of fermentation tank |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58127817A JPS6019490A (en) | 1983-07-15 | 1983-07-15 | Aeration of fermentation tank |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6019490A true JPS6019490A (en) | 1985-01-31 |
| JPH0335911B2 JPH0335911B2 (en) | 1991-05-29 |
Family
ID=14969392
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58127817A Granted JPS6019490A (en) | 1983-07-15 | 1983-07-15 | Aeration of fermentation tank |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6019490A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62252815A (en) * | 1986-04-23 | 1987-11-04 | Itoo Yookadou:Kk | Garbage incineration and fermentation device |
| US6569673B1 (en) * | 1998-01-30 | 2003-05-27 | Matsushita Electric Works, Ltd. | Garbage disposing device |
| JP2013505815A (en) * | 2009-09-28 | 2013-02-21 | グアンチョウ、ピュデ、エンバイロンメンタル、プロテクション、エキップメント、リミテッド | Method and apparatus for aerobically air drying sludge filter cake |
| CN105733931A (en) * | 2016-04-12 | 2016-07-06 | 广州市集木蓄能技术开发有限公司 | Fermentation heat energy recycling equipment and heat energy recycling method |
-
1983
- 1983-07-15 JP JP58127817A patent/JPS6019490A/en active Granted
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62252815A (en) * | 1986-04-23 | 1987-11-04 | Itoo Yookadou:Kk | Garbage incineration and fermentation device |
| JPH0262775B2 (en) * | 1986-04-23 | 1990-12-26 | Itoo Yookado Kk | |
| US6569673B1 (en) * | 1998-01-30 | 2003-05-27 | Matsushita Electric Works, Ltd. | Garbage disposing device |
| JP2013505815A (en) * | 2009-09-28 | 2013-02-21 | グアンチョウ、ピュデ、エンバイロンメンタル、プロテクション、エキップメント、リミテッド | Method and apparatus for aerobically air drying sludge filter cake |
| CN105733931A (en) * | 2016-04-12 | 2016-07-06 | 广州市集木蓄能技术开发有限公司 | Fermentation heat energy recycling equipment and heat energy recycling method |
| CN105733931B (en) * | 2016-04-12 | 2018-08-10 | 广州市集木蓄能技术开发有限公司 | A kind of heat of fermentation reclaimer and heat energy recovering method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0335911B2 (en) | 1991-05-29 |
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