JP2003340416A - Method and apparatus for methane fermentation treatment of organic waste - Google Patents
Method and apparatus for methane fermentation treatment of organic wasteInfo
- Publication number
- JP2003340416A JP2003340416A JP2002158549A JP2002158549A JP2003340416A JP 2003340416 A JP2003340416 A JP 2003340416A JP 2002158549 A JP2002158549 A JP 2002158549A JP 2002158549 A JP2002158549 A JP 2002158549A JP 2003340416 A JP2003340416 A JP 2003340416A
- Authority
- JP
- Japan
- Prior art keywords
- organic waste
- fermentation
- fermenter
- pressure
- tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、嫌気性生物を用い
て、生ゴミ、食品加工残滓、活性汚泥処理等の余剰汚泥
等の有機性廃棄物を処理する、有機性廃棄物のメタン発
酵処理方法及び処理装置に関する。TECHNICAL FIELD The present invention relates to a methane fermentation treatment of organic waste, which treats organic waste such as food waste, food processing residue, surplus sludge such as activated sludge treatment using anaerobic organisms. A method and a processing apparatus.
【０００２】[0002]
【従来の技術】生ゴミ等の有機性廃棄物のほとんどは、
焼却や埋立処分されているが、焼却に伴うダイオキシン
の発生や埋立処分地の逼迫、悪臭などの問題から、環境
負荷の少ない処理方法が求められている。これらの問題
を解決するために有機性廃棄物をメタン発酵処理し、発
生したメタンガスを燃料電池やガスエンジンを用いて発
電するシステムが研究、開発されている。2. Description of the Related Art Most of organic waste such as kitchen garbage is
It is incinerated or landfilled, but due to problems such as the generation of dioxin accompanying incineration, tightness of landfill site, and bad odor, a treatment method with a low environmental load is required. In order to solve these problems, a system in which organic waste is subjected to methane fermentation treatment and generated methane gas is generated using a fuel cell or a gas engine has been researched and developed.
【０００３】メタン発酵処理は、有機性廃棄物を粉砕・
スラリー化した後、このスラリーを発酵槽に投入し、嫌
気性下でメタン菌により発酵処理して有機性廃棄物をバ
イオガスと水とに分解する方法であり、有機性廃棄物を
大幅に減量することができると共に、副産物として生成
するメタンガスをエネルギーとして回収できるメリット
がある。また、嫌気性のため曝気動力が不要であるため
省エネルギーな処理法である。The methane fermentation process involves crushing organic waste.
After slurrying, this slurry is put into a fermenter and fermented by methane bacteria under anaerobic conditions to decompose organic waste into biogas and water. In addition to being able to do so, there is an advantage that methane gas produced as a by-product can be recovered as energy. Further, since it is anaerobic and does not require aeration power, it is an energy-saving treatment method.
【０００４】上記の嫌気性生物を用いた発酵槽において
は、細菌と有機性廃棄物の接触をよくし、バイオガスの
発生を促進させるために発酵槽内を攪拌する必要があ
る。また、この攪拌によって、発酵槽内の温度やｐＨが
均一になるので発酵条件が一定となり、安定したバイオ
ガスの発生が可能となる。In the fermenter using the above anaerobic organism, it is necessary to stir the inside of the fermenter in order to improve contact between bacteria and organic waste and promote generation of biogas. Further, by this stirring, the temperature and pH in the fermenter become uniform, so that the fermentation conditions become constant and stable generation of biogas becomes possible.
【０００５】従来、発酵槽を攪拌する方法としては、機
械攪拌法、ポンプ循環法、ガス攪拌法等が用いられてい
る。機械攪拌方法は、羽根式攪拌機やスクリュー式攪拌
機を発酵槽内に設置し、強制的に有機性廃棄物を攪拌す
る方法であり、ポンプ循環法は、発酵槽の外部にあるポ
ンプで有機性廃棄物自身を発酵槽底部から上部へ循環さ
せる方法である。Conventionally, a mechanical stirring method, a pump circulation method, a gas stirring method and the like have been used as a method for stirring a fermenter. The mechanical stirring method is a method in which a blade stirrer or a screw stirrer is installed in the fermentation tank to forcibly stir the organic waste, and the pump circulation method is the organic waste disposal using a pump outside the fermentation tank. This is a method of circulating the product itself from the bottom of the fermentation tank to the top.
【０００６】また、ガス攪拌法は、バイオガスをガス圧
縮機で圧縮し、発酵槽下部より圧入する方法であり、例
えば、特開２００１−４６９９７号公報には、閉鎖空間
を形成するメタン発酵槽と、このメタン発酵槽内に浸漬
されて膜分離装置と散気装置を配置した膜分離槽と、発
酵槽と膜分離槽とを連通する循環系と、一端が発酵槽の
気相部に連通するとともに、他端が散気装置に連通し、
途中にブロアを介装したバイオガス循環系とを有する発
酵槽の攪拌装置が記載されており、発酵槽内で発生する
バイオガスのエアリフト作用を利用して、発酵汚泥を攪
拌することが開示されている。The gas agitation method is a method in which biogas is compressed by a gas compressor and is injected under the fermentation tank. For example, Japanese Patent Laid-Open No. 2001-46997 discloses a methane fermentation tank forming a closed space. And a membrane separation tank in which a membrane separation device and an air diffuser are placed by being immersed in the methane fermentation tank, a circulation system that connects the fermentation tank and the membrane separation tank, and one end of which communicates with the gas phase part of the fermentation tank. And the other end communicates with the air diffuser,
A stirring device for a fermenter having a biogas circulation system with a blower interposed in the middle is described, and it is disclosed that the fermented sludge is stirred by utilizing the air lift action of biogas generated in the fermenter. ing.
【０００７】[0007]
【発明が解決しようとする課題】しかしながら、上記の
従来技術のうち、機械攪拌法においては、発酵槽内に攪
拌機が必要となるので装置構造が複雑となり、また、大
きな攪拌動源が必要となるという問題があった。また、
ポンプ循環法においても、循環ポンプ等の駆動源があ
り、大きな動力を必要とするという問題点があった。However, among the above-mentioned conventional techniques, the mechanical stirring method requires a stirrer in the fermentation tank, which complicates the apparatus structure and requires a large stirring source. There was a problem. Also,
Even in the pump circulation method, there is a problem in that there is a drive source such as a circulation pump and a large amount of power is required.
【０００８】更に、特開２００１−４６９９７号公報の
方法のようなガス攪拌法においても、ガスを発酵槽に送
り込むための、ブロアやガス圧縮機が必要になるとうい
う問題点があった。Further, even in the gas stirring method such as the method disclosed in Japanese Patent Laid-Open No. 2001-46997, there is a problem that a blower or a gas compressor for feeding the gas into the fermentation tank is required.
【０００９】したがって、本発明の目的は、メタン発酵
槽の攪拌動力を低減でき、これによって処理装置のラン
ニングコストを低減できる、有機性廃棄物のメタン発酵
処理方法及び処理装置を提供することにある。Therefore, an object of the present invention is to provide a methane fermentation treatment method and treatment equipment for organic waste, which can reduce the stirring power of the methane fermentation tank and thereby reduce the running cost of the treatment equipment. .
【００１０】[0010]
【課題を解決するための手段】上記目的を達成するた
め、本発明者等は鋭意検討した結果、メタン発酵槽内部
を密閉系にするとバイオガスの発生に伴い発酵槽内の圧
力は上昇するので、この圧力を発酵槽内の原料スラリー
の攪拌に利用すれば、攪拌動力が大幅に低減できること
を見出し、本発明を完成するに至った。[Means for Solving the Problems] In order to achieve the above object, the inventors of the present invention have made diligent studies, and as a result, when the inside of the methane fermentation tank is made a closed system, the pressure in the fermentation tank rises with the generation of biogas. The inventors have found that if this pressure is used for stirring the raw material slurry in the fermenter, the stirring power can be significantly reduced, and the present invention has been completed.
【００１１】すなわち、本発明の有機性廃棄物のメタン
発酵処理方法は、嫌気性微生物によって分解可能な有機
性廃棄物をメタン発酵によって処理する方法において、
前記有機性廃棄物を複数の発酵槽に導入して発酵させ、
前記複数の発酵槽内の圧力を検出して、前記圧力の高い
方の発酵槽から、前記圧力の低い方の発酵槽へと、前記
メタン発酵によって生成したガスを供給することによっ
て、前記圧力の低い方の発酵槽の攪拌を行ない、この攪
拌を前記複数の発酵槽間で交互に行なうことを特徴とす
る。That is, the method for treating methane fermentation of organic waste of the present invention is a method for treating organic waste decomposable by anaerobic microorganisms by methane fermentation.
Introducing the organic waste into a plurality of fermenters to ferment,
Detecting the pressure in the plurality of fermenters, from the higher pressure fermentor to the lower pressure fermentor, by supplying the gas produced by the methane fermentation, The lower fermenter is agitated, and the agitation is alternately performed among the plurality of fermenters.
【００１２】本発明の方法によれば、複数の発酵槽内の
圧力差を利用して、圧力の低い方の発酵槽へ生成ガスを
供給することによって有機性廃棄物の攪拌を行なうこと
ができる。したがって、加圧されたガスを発酵槽内に送
り込むことができるので、ブロアやガス圧縮機が不要で
あり、攪拌に必要な動力を低減してランニングコストを
低減することができる。また、複数の発酵槽間で交互に
攪拌を行うことにより、処理装置の連続運転が可能とな
り、処理効率を向上させることができる。According to the method of the present invention, the organic waste can be agitated by utilizing the pressure difference in a plurality of fermenters to supply the produced gas to the fermenter having a lower pressure. . Therefore, since the pressurized gas can be sent into the fermentation tank, a blower and a gas compressor are not required, and the power required for stirring can be reduced and the running cost can be reduced. Further, by alternately performing stirring between a plurality of fermentation tanks, continuous operation of the processing device becomes possible, and processing efficiency can be improved.
【００１３】本発明の方法においては、前記有機性廃棄
物を、前記複数の発酵槽間で交互に圧力差が生じるよう
に、前記複数の発酵槽に交互に導入することが好まし
い。これによれば、それぞれの発酵槽への有機性廃棄物
の導入のタイミングを順次切替えるだけで、発酵槽間の
圧力差を容易に発生させることができる。In the method of the present invention, it is preferable that the organic waste is introduced into the plurality of fermenters alternately so that a pressure difference is alternately generated between the plurality of fermenters. According to this, the pressure difference between the fermenters can be easily generated by simply switching the timing of introducing the organic waste into the respective fermenters.
【００１４】一方、本発明の有機性廃棄物のメタン発酵
処理装置は、嫌気性微生物によって分解可能な有機性廃
棄物を発酵槽に導入するための有機性廃棄物供給手段
と、前記有機性廃棄物をメタン発酵させるための複数の
発酵槽と、前記発酵槽内の圧力を検出するための圧力検
出手段と、前記メタン発酵によって生成したガスを貯留
するためのガス貯留槽と、前記複数の発酵槽内の前記生
成ガスが占める上部空間と前記ガス貯留槽とを連結する
第１配管と、前記発酵槽内の上部空間と他の発酵槽内の
前記有機性廃棄物が占める下部空間とを連結する第２配
管とを備え、前記圧力検出手段によって前記複数の発酵
槽間の圧力差を検出した場合に、前記圧力の高い方の発
酵槽から前記圧力の低い方の発酵槽へ、前記第２配管を
通じて前記生成ガスを供給する切替え手段が設けられて
いることを特徴とする。On the other hand, the apparatus for treating methane fermentation of organic waste of the present invention comprises an organic waste supply means for introducing an organic waste decomposable by anaerobic microorganisms into a fermenter, and the organic waste. A plurality of fermenters for methane fermenting a product, a pressure detection means for detecting the pressure in the fermentor, a gas storage tank for storing the gas produced by the methane fermentation, and the plurality of fermentations A first pipe connecting an upper space occupied by the generated gas in the tank and the gas storage tank, an upper space in the fermentation tank and a lower space occupied by the organic waste in another fermentation tank And a second pipe for controlling the pressure difference between the plurality of fermenters when the pressure detecting means detects a pressure difference between the plurality of fermenters. The generated gas through piping Wherein the switching means is provided for supplying.
【００１５】本発明の装置によれば、圧力検出手段と第
１配管、第２配管によって、複数の発酵槽内の圧力差を
利用して、圧力の低い方の発酵槽へ生成ガスを供給する
ことによって攪拌ができる。したがって、生成ガスを発
酵槽内に送り込むためのブロアやガス圧縮機が不要とな
り、攪拌に必要な動力が低減できるのでランニングコス
トが低減する。According to the apparatus of the present invention, the pressure detection means and the first pipe and the second pipe make use of the pressure difference in the plurality of fermenters to supply the produced gas to the lower fermenter. This allows stirring. Therefore, a blower and a gas compressor for feeding the produced gas into the fermenter are not required, and the power required for stirring can be reduced, so that the running cost is reduced.
【００１６】また、発酵槽内の攪拌装置が不要であり、
装置の構造を単純にできる。更に、複数の発酵槽間で交
互に攪拌を行うことにより、処理装置の連続運転が可能
となるので、処理効率を向上させることができる。Further, a stirring device in the fermenter is unnecessary,
The structure of the device can be simplified. Further, by alternately performing stirring among a plurality of fermentation tanks, continuous operation of the processing device is possible, and thus processing efficiency can be improved.
【００１７】本発明の装置においては、前記有機性廃棄
物供給手段が、前記有機性廃棄物を前記複数の発酵槽に
交互に供給するための切替え手段を備えることが好まし
い。In the apparatus of the present invention, it is preferable that the organic waste supply means includes a switching means for alternately supplying the organic waste to the plurality of fermentation tanks.
【００１８】これによれば、切替え手段によって、有機
性廃棄物の導入を、複数の発酵槽で交互に行なうことが
できるので、複数の発酵槽における圧力差の発生を容易
に行なうことができる。According to this, since the introduction of the organic waste can be alternately performed in the plurality of fermenters by the switching means, the pressure difference in the plurality of fermenters can be easily generated.
【００１９】[0019]
【発明の実施の形態】以下、本発明について図面を用い
て更に詳細に説明する。BEST MODE FOR CARRYING OUT THE INVENTION The present invention will be described in more detail below with reference to the drawings.
【００２０】図１、２には、本発明の有機性廃棄物のメ
タン発酵処理装置の一実施形態が示されている。図１は
メタン発酵処理装置の概略構成図、図２は発酵槽内の圧
力制御の状態を示すタイムチャートである。1 and 2 show one embodiment of the methane fermentation treatment apparatus for organic waste of the present invention. FIG. 1 is a schematic configuration diagram of a methane fermentation treatment apparatus, and FIG. 2 is a time chart showing a state of pressure control in a fermenter.
【００２１】まず、本発明のメタン発酵装置について説
明すると、図１に示すように、この処理装置は、有機性
廃棄物を粉砕する前処理装置１０と、これをスラリー化
する混合槽２０と、供給ポンプ３０ａ、３０ｂとからな
る有機性廃棄物供給手段と、２つの発酵槽４０ａ、４０
ｂと、圧力センサ５０ａ、５０ｂからなる圧力検出手段
と、生成したガスを貯留するためのガスタンク６０とで
主に構成されている。First, the methane fermentation apparatus of the present invention will be described. As shown in FIG. 1, this processing apparatus comprises a pretreatment apparatus 10 for crushing organic waste, a mixing tank 20 for slurrying the organic waste, Organic waste supply means consisting of supply pumps 30a, 30b and two fermenters 40a, 40
b, a pressure detecting means including pressure sensors 50a and 50b, and a gas tank 60 for storing the generated gas.
【００２２】有機性廃棄物供給手段は、有機性廃棄物を
投入、粉砕するための前処理装置１０が、供給配管８１
によって、次工程の混合槽２０に供給されるように構成
されている。そして、混合槽２０からは、供給配管８２
ａ、８２ｂが、それぞれ発酵槽４０ａ、４０ｂへ連結さ
れるように接続されている。In the organic waste supply means, the pretreatment device 10 for charging and crushing the organic waste is the supply pipe 81.
Is supplied to the mixing tank 20 in the next step. Then, from the mixing tank 20, the supply pipe 82
a and 82b are connected so as to be connected to the fermenters 40a and 40b, respectively.
【００２３】供給配管８２ａ、８２ｂの途中には、供給
ポンプ、３０ａ、３０ｂが設けられており、これによっ
て、発酵槽４０ａ又は４０ｂへの有機性廃棄物の供給が
切替え可能となっている。Supply pumps 30a and 30b are provided in the middle of the supply pipes 82a and 82b, whereby the supply of organic waste to the fermenter 40a or 40b can be switched.
【００２４】本発明においては、複数の発酵槽を用いる
点が特徴となっており、この実施形態においては、２つ
の発酵槽４０ａ、４０ｂを有している。発酵槽としては
特に限定されないが、本発明においては、複数の発酵槽
の圧力差を利用して攪拌を行なうため、それぞれの発酵
槽の体積が等しいことが好ましい。また、発酵槽の数
は、２つに限定されず、３つ以上であってもよい。The present invention is characterized in that a plurality of fermenters are used. In this embodiment, two fermenters 40a and 40b are provided. Although the fermenter is not particularly limited, in the present invention, since the stirring is performed by utilizing the pressure difference between the plurality of fermenters, it is preferable that the volumes of the respective fermenters are equal. Further, the number of fermenters is not limited to two, and may be three or more.
【００２５】メタン発酵を行なうための２つの発酵槽４
０ａ、４０ｂの上部には、それぞれ圧力センサ５０ａ、
５０ｂが設けられており、発酵槽上部のガス圧力をモニ
ターできるようになっている。圧力センサ５０ａ、５０
ｂとしては従来公知の圧力センサが使用可能であり特に
限定されない。Two fermenters 4 for carrying out methane fermentation
0a and 40b have pressure sensors 50a and
50b is provided so that the gas pressure in the upper part of the fermenter can be monitored. Pressure sensor 50a, 50
A conventionally known pressure sensor can be used as b and is not particularly limited.
【００２６】発酵槽４０ａ、４０ｂの上部空間からは、
ガスタンク６０に連結される第１配管８３ａ、８３ｂが
それぞれ接続されており、第１配管８３ａ、８３ｂの途
中には、第１バルブ９０ａ、９０ｂがそれぞれ設けられ
ている。これによって、メタン発酵を行なうための２つ
の発酵槽４０ａ、４０ｂにおいて発生したバイオガス
が、ガスタンク６０に貯蔵されるように構成されてお
り、このガスタンク６０に貯蔵されたバイオガスが、燃
料電池発電装置、ガスエンジン等の発電機やボイラーの
燃料として有効利用されるようになっている。From the upper space of the fermenters 40a and 40b,
First pipes 83a and 83b connected to the gas tank 60 are respectively connected, and first valves 90a and 90b are provided in the middle of the first pipes 83a and 83b, respectively. Thus, the biogas generated in the two fermenters 40a and 40b for performing methane fermentation is configured to be stored in the gas tank 60, and the biogas stored in the gas tank 60 is used for fuel cell power generation. It has come to be effectively used as fuel for power generators and boilers for equipment and gas engines.
【００２７】一方、上記の第１配管とは別に、発酵槽４
０ａ、４０ｂからは、圧力の高い方の発酵槽から圧力の
低い方の発酵槽へ生成ガスを供給して攪拌を行なうため
に、発酵槽４０ａの上部空間と発酵槽４０ｂの下部空間
を連結する第２配管８４、及び、発酵槽４０ａの下部空
間と発酵槽４０ｂの上部空間を連結する第２配管８５が
連結されており、第２配管８４、８５の途中には、それ
ぞれバルブ９１ａ、９１ｂが設けられている。On the other hand, separately from the above-mentioned first pipe, the fermenter 4
From 0a and 40b, the upper space of the fermentor 40a and the lower space of the fermenter 40b are connected to each other in order to supply the produced gas from the fermenter with the higher pressure to the fermenter with the lower pressure to perform stirring. A second pipe 84 and a second pipe 85 connecting the lower space of the fermentation tank 40a and the upper space of the fermentation tank 40b are connected, and valves 91a and 91b are provided in the middle of the second pipes 84 and 85, respectively. It is provided.
【００２８】更に、発酵槽４０ａ、４０ｂの底部から
は、固液分離槽７０に接続される供給配管８６ａ、８６
ｂがそれぞれ設けられており、発酵処理後の残渣が固液
分離槽７０に送られるように構成されている。この固液
分離槽７０からは、分離された液体残渣が再度、混合槽
２０に送られるように供給配管８７が接続されており、
それ以外の残渣は廃液処理装置へ送られるように構成さ
れている。Further, from the bottom of the fermentation tanks 40a, 40b, supply pipes 86a, 86 connected to the solid-liquid separation tank 70 are provided.
b are provided respectively, and the residue after the fermentation treatment is sent to the solid-liquid separation tank 70. A supply pipe 87 is connected from the solid-liquid separation tank 70 so that the separated liquid residue is sent to the mixing tank 20 again.
Other residues are configured to be sent to the waste liquid treatment device.
【００２９】次に、このメタン発酵処理装置を用いた、
有機性廃棄物のメタン発酵処理方法処理方法について説
明する。Next, using this methane fermentation treatment apparatus,
Methane fermentation treatment method of organic waste The treatment method will be described.
【００３０】まず、有機性廃棄物は前処理装置１０に投
入される。処理原料となる有機性廃棄物としては、飲食
店や一般家庭等から排出される生ゴミや、食品工場等か
ら排出される食品加工残渣、屎尿、活性汚泥処理等の余
剰汚泥等が使用できる。First, the organic waste is put into the pretreatment apparatus 10. As the organic waste that is a raw material for processing, raw garbage discharged from restaurants, general households, etc., food processing residues discharged from food factories, etc., excess sludge such as human waste and activated sludge treatment can be used.
【００３１】前処理装置１０では、発酵に適さない異物
を取り除くと同時に、発酵を促進させるために有機性廃
棄物を細かく粉砕する。このように、メタン発酵処理に
供する有機性廃棄物を微粉砕することにより、分解速度
及び消化率を向上することができる。この段階での有機
性廃棄物のＴＳ濃度（固形分濃度）は２０〜２５％であ
ることが好ましい。The pretreatment device 10 removes foreign substances unsuitable for fermentation, and at the same time, finely grinds the organic waste in order to promote fermentation. As described above, by finely pulverizing the organic waste to be subjected to the methane fermentation treatment, the decomposition rate and the digestibility can be improved. The TS concentration (solid content concentration) of the organic waste at this stage is preferably 20 to 25%.
【００３２】そして、上記の粉砕後の有機性廃棄物は混
合槽２０に送られる。混合槽２０において、有機性廃棄
物は、固液分離槽７０から返送される汚泥と混合され
る。これによって、有機性廃棄物はＴＳ濃度等が調整さ
れて原料スラリーとなる。このとき、混合槽２０におけ
る原料スラリーのＴＳ濃度としては１０〜１５％となる
ように調整することが好ましい。Then, the pulverized organic waste is sent to the mixing tank 20. In the mixing tank 20, the organic waste is mixed with the sludge returned from the solid-liquid separation tank 70. As a result, the organic waste is adjusted to have a TS concentration and the like and becomes a raw material slurry. At this time, it is preferable to adjust the TS concentration of the raw material slurry in the mixing tank 20 to be 10 to 15%.
【００３３】次に、原料スラリーは、発酵槽に送られて
メタン発酵が行なわれる。以下、更に、図２のタイムチ
ャートを参照しながら、原料スラリーの供給方法、及び
発酵槽４０ａ、４０ｂ内の圧力制御の方法について説明
する。Next, the raw material slurry is sent to a fermenter for methane fermentation. Hereinafter, the method of supplying the raw material slurry and the method of controlling the pressure in the fermenters 40a and 40b will be further described with reference to the time chart of FIG.
【００３４】この実施形態では、まず、図２ｃに示すよ
うに、一方の供給ポンプ３０ａのみを、所定の時間ｔ0
からｔ1まで作動させ、原料スラリーを発酵槽４０ａに
供給する。このとき、図２ｂに示すように、各バルブ９
０ａ、９０ｂ、９１ａ、９１ｂは閉じられている。In this embodiment, first, as shown in FIG. 2c, only one supply pump 30a is operated for a predetermined time t 0.
To t 1 to supply the raw material slurry to the fermenter 40a. At this time, as shown in FIG.
0a, 90b, 91a and 91b are closed.
【００３５】その結果、メタン発酵が発酵槽４０ａ内で
起こり、メタンガスを主としたバイオガスが発生する。
発酵槽４０ａ内は、汚泥等の有機性廃棄物が含有される
原料スラリー層と、上部に生成したバイオガスが充満す
るガス層から構成され、原料スラリー中の有機物１ｇよ
り約１．９Ｌのバイオガスが発生する。そのため、発酵
槽を密閉系にするとバイオガスの発生に伴い発酵槽内の
圧力は上昇する。As a result, methane fermentation takes place in the fermenter 40a, and biogas consisting mainly of methane gas is generated.
The inside of the fermenter 40a is composed of a raw material slurry layer containing organic waste such as sludge and a gas layer filled with biogas generated at the upper part, and is about 1.9 L of biomaterial from 1 g of organic matter in the raw material slurry. Gas is generated. Therefore, if the fermenter is closed, the pressure in the fermentor rises with the generation of biogas.
【００３６】発酵温度としては、高温メタン菌を用いて
効率的に処理できる５０〜６０℃が好ましく、５５〜５
７℃が特に好ましい。The fermentation temperature is preferably 50 to 60 ° C., which enables efficient treatment with high-temperature methane bacteria, and 55 to 5
7 ° C. is particularly preferred.
【００３７】そして、この実施形態においては、発酵槽
４０ｂに比べて、有機性廃棄物を供給した発酵槽４０ａ
で上記のバイオガスの発生が活発に起こるので、発酵槽
４０ａ内の圧力Ｐａと、発酵槽４０ｂ内の圧力Ｐｂは、
図２ａに示すように上昇し、発酵槽４０ａと発酵槽Ｂに
圧力差Ｐ（Ｐａ−Ｐｂ）が生じる。なお、各発酵槽４０
ａ、４０ｂ内の圧力は圧力センサ５０ａ、５０ｂによっ
て常時モニタされている。In this embodiment, as compared with the fermenter 40b, the fermenter 40a supplied with the organic waste.
Since the biogas is actively generated in the above, the pressure Pa in the fermentation tank 40a and the pressure Pb in the fermentation tank 40b are
As shown in FIG. 2a, the pressure rises and a pressure difference P (Pa-Pb) is generated between the fermenter 40a and the fermenter B. In addition, each fermentor 40
The pressures in a and 40b are constantly monitored by pressure sensors 50a and 50b.
【００３８】次に、この圧力差Ｐが所定の数値に達した
時点で（図２ａのｔ2）、バルブ９１ａとバルブ９０ｂ
を開く。これによって、発酵槽４０ａのバイオガスが、
第２配管８４によって、発酵槽４０ｂの下部空間から導
入されるので、これによって、発酵槽４０ｂの攪拌が行
なわれる。Next, when the pressure difference P reaches a predetermined value (t 2 in FIG. 2a), the valve 91a and the valve 90b.
open. As a result, the biogas in the fermenter 40a
Since it is introduced from the lower space of the fermentation tank 40b through the second pipe 84, the stirring of the fermentation tank 40b is performed by this.
【００３９】このとき、高圧側の発酵槽４０ａ内と圧力
としては１０〜２０ｋＰａなっていることが好ましく、
低圧側の発酵槽４０ｂ内と圧力としては０〜５ｋＰａな
っていることが好ましい。また、発酵槽４０ｂの攪拌に
必要な上記の圧力差Ｐとしては、１０〜２０ｋＰａであ
ることが好ましい。At this time, the pressure in the high-pressure side fermenter 40a is preferably 10 to 20 kPa,
The pressure in the low pressure side fermenter 40b is preferably 0 to 5 kPa. Further, the pressure difference P required for stirring the fermenter 40b is preferably 10 to 20 kPa.
【００４０】そして、攪拌に利用されたバイオガスは、
発酵槽４０ｂの有機性廃棄物を攪拌した後、発酵槽４０
ｂ内の上部空間に達する。ここで、発酵槽４０ｂ内で発
生した圧力Ｐｂのガイオガスと混合された後、第１配管
８３ｂを通じてガスタンク６０へ供給される。The biogas used for stirring is
After stirring the organic waste in the fermenter 40b,
Reach the upper space in b. Here, after being mixed with Gaiogas having a pressure Pb generated in the fermenter 40b, it is supplied to the gas tank 60 through the first pipe 83b.
【００４１】これによって、発酵槽４０ａ内で発生した
ガスを発酵槽４０ｂの攪拌動力として利用でき、攪拌動
力として利用できる。しかも、攪拌に利用されたバイオ
ガスは、発酵槽４０ｂのバイオガスとともに回収するこ
ともできるので、バイオガスの回収効率が低下すること
もない。As a result, the gas generated in the fermentation tank 40a can be used as the stirring power of the fermentation tank 40b and can be used as the stirring power. Moreover, since the biogas used for stirring can be recovered together with the biogas in the fermentation tank 40b, the biogas recovery efficiency does not decrease.
【００４２】そして、発酵槽４０ａ内の発酵後の残渣
は、供給配管８６ａを経て固液分離槽７０へ送られる。
この残渣のＴＳ濃度は、通常２〜３％となっていること
が好ましい。固液分離槽７０では残渣を固液分離し、分
離された廃液の一部は混合槽２０へ返送されて原料スラ
リーのＴＳの濃度の調整に用いられ、残りは廃液処理装
置にて処理される。Then, the residue after fermentation in the fermentation tank 40a is sent to the solid-liquid separation tank 70 through the supply pipe 86a.
It is preferable that the TS concentration of this residue is usually 2 to 3%. In the solid-liquid separation tank 70, the residue is subjected to solid-liquid separation, a part of the separated waste liquid is returned to the mixing tank 20 and used for adjusting the TS concentration of the raw material slurry, and the rest is processed in the waste liquid processing device. .
【００４３】次に、上記の操作によって、発酵槽内の圧
力が低下した時点で（図２ａのｔ3）、図２ｂに示すよ
うにバルブ９１ａとバルブ９０ｂを閉じた後、今度は図
２ｃに示すように供給ポンプ３０ｂのみを、所定の時間
ｔ3からｔ4まで作動させ、原料スラリーを発酵槽４０ｂ
に供給する。Next, when the pressure in the fermenter drops by the above-mentioned operation (t 3 in FIG. 2a), after closing the valves 91a and 90b as shown in FIG. 2b, this time as shown in FIG. 2c. As shown, only the supply pump 30b is operated for a predetermined time t 3 to t 4 to feed the raw material slurry to the fermentation tank 40b.
Supply to.
【００４４】その結果、今度はメタン発酵が発酵槽４０
ｂ内で活発に起こり、発酵槽４０ａ内の圧力Ｐａと、発
酵槽４０ｂ内の圧力Ｐｂは、図２ａのｔ4からｔ5に示す
ように上昇し、発酵槽４０ａと発酵槽４０ｂに圧力差が
Ｐ（Ｐｂ−Ｐａ）が生じる。そして、この圧力差Ｐが所
定の数値に達した時点で（図２ａのｔ5）、今度はバル
ブ９１ｂとバルブ９０ａをｔ5からｔ6まで開く。これに
よって、発酵槽４０ｂのバイオガスが、第２配管８５に
よって、発酵槽４０ａの下部空間から導入されて発酵槽
４０ｂの攪拌が行なわれる。As a result, the methane fermentation is now performed in the fermenter 40.
2b, the pressure Pa in the fermenter 40a and the pressure Pb in the fermenter 40b increase as shown from t 4 to t 5 in FIG. 2a, and the pressure difference between the fermenter 40a and the fermentor 40b increases. Causes P (Pb-Pa). Then, when the pressure difference P reaches a predetermined value (t 5 in FIG. 2a), the valve 91b and the valve 90a are opened from t 5 to t 6 this time. Thereby, the biogas of the fermenter 40b is introduced from the lower space of the fermenter 40a by the second pipe 85 to stir the fermenter 40b.
【００４５】そして、バイオガスは、発酵槽４０ａの原
料スラリーを攪拌した後、発酵槽４０ａ内の上部空間に
達して、発酵槽４０ａ内で発生した圧力Ｐａのガイオガ
スと混合された後、第１配管８３ａを通じてガスタンク
６０へ供給される。The biogas reaches the upper space in the fermenter 40a after stirring the raw material slurry in the fermenter 40a, and is mixed with Gaiogas having a pressure Pa generated in the fermenter 40a. It is supplied to the gas tank 60 through the pipe 83a.
【００４６】上記のように、ｔ0からｔ6までの工程を１
サイクルとして、これを繰り返して運転することで、発
酵槽４０ａ、４０ｂ内の攪拌が交互に行なわれ、しか
も、攪拌を外部からの大きな動力なしに行なうことが可
能となる。また、このように、複数の発酵槽を切替える
ので、処理装置の連続運転を行なうことが可能となり、
処理効率を向上させることができる。As described above, the steps from t 0 to t 6 are
By repeating this operation as a cycle, the stirring in the fermentation tanks 40a and 40b is alternately performed, and the stirring can be performed without a large power from the outside. In addition, since a plurality of fermentation tanks are switched in this way, it becomes possible to continuously operate the processing device,
The processing efficiency can be improved.
【００４７】なお、上記の圧力制御による攪拌操作は、
必ずしも処理装置の運転中常時行なう必要はなく、所定
の間隔で間欠的に行なってもよい。この場合には、バル
ブ９１ａ、９１ｂを共に閉じて第２配管８４、８５を使
用せず、バルブ９０ａ、９０ｂを開いて発酵槽４０ａ、
４０ｂから発生したバイオガスを、それぞれ第１配管の
８３ａ、８３ｂから直接取出すようにすればよい。これ
により、発酵槽４０ａ、４０ｂを同時に使用することも
できる。The stirring operation by the above pressure control is
It is not always necessary to always perform the operation during the operation of the processing apparatus, and it may be performed intermittently at a predetermined interval. In this case, the valves 91a and 91b are both closed and the second pipes 84 and 85 are not used, and the valves 90a and 90b are opened to leave the fermentation tank 40a,
The biogas generated from 40b may be directly taken out from the first pipes 83a and 83b, respectively. Thereby, the fermenters 40a and 40b can be used at the same time.
【００４８】[0048]
【発明の効果】以上説明したように、本発明によれば、
メタン発酵槽の攪拌動力を低減でき、これによって、処
理装置のランニングコストを低減できる、有機性廃棄物
のメタン発酵処理方法及び処理装置を提供することがで
きるので、嫌気性生物を用いた、生ゴミ、食品加工残
滓、活性汚泥処理等の余剰汚泥等の有機性廃棄物の処理
に好適に用いることができる。As described above, according to the present invention,
Since the stirring power of the methane fermentation tank can be reduced, and thus the running cost of the treatment device can be reduced, it is possible to provide a methane fermentation treatment method and treatment device for organic waste. It can be suitably used for the treatment of organic waste such as waste, food processing residue, and excess sludge such as activated sludge treatment.
【図１】 本発明のメタン発酵処理装置の一実施形態を
示す概略構成図である。FIG. 1 is a schematic configuration diagram showing an embodiment of a methane fermentation treatment apparatus of the present invention.
【図２】 発酵槽内の圧力制御の状態を示す図であっ
て、（ａ）各発酵槽内の圧力状態、（ｂ）各バルブの開
閉状態、（ｃ）各供給ポンプの運転状態、を示すタイム
チャートである。FIG. 2 is a diagram showing a state of pressure control in the fermenter, showing (a) pressure state in each fermenter, (b) opening / closing state of each valve, and (c) operating state of each supply pump. It is a time chart shown.
１０ 前処理装置
２０ 混合槽
３０ａ、３０ｂ 供給ポンプ
４０ａ、４０ｂ 発酵槽
５０ａ、５０ｂ 圧力センサ
６０ ガスタンク
７０ 固液分離槽
８１、８２ａ、８２ｂ、８６ａ、８６ｂ、８７ 供給配
管
８３ａ、８３ｂ 第１配管
８４、８５ 第２配管
９０ａ、９０ｂ、９１ａ、９１ｂ バルブ10 Pretreatment device 20 Mixing tank 30a, 30b Supply pump 40a, 40b Fermentation tank 50a, 50b Pressure sensor 60 Gas tank 70 Solid-liquid separation tank 81, 82a, 82b, 86a, 86b, 87 Supply pipe 83a, 83b First pipe 84, 85 Second piping 90a, 90b, 91a, 91b Valve
Claims (4)
廃棄物をメタン発酵によって処理する方法において、前
記有機性廃棄物を複数の発酵槽に導入して発酵させ、前
記複数の発酵槽内の圧力を検出して、前記圧力の高い方
の発酵槽から、前記圧力の低い方の発酵槽へと、前記メ
タン発酵によって生成したガスを供給することによっ
て、前記圧力の低い方の発酵槽の攪拌を行ない、この攪
拌を前記複数の発酵槽間で交互に行なうことを特徴とす
る有機性廃棄物のメタン発酵処理方法。1. A method for treating an organic waste decomposable by anaerobic microorganisms by methane fermentation, wherein the organic waste is introduced into a plurality of fermenters for fermentation, and the pressure in the plurality of fermenters is increased. From the fermenter with the higher pressure to the fermenter with the lower pressure, by supplying the gas generated by the methane fermentation, stirring the fermenter with the lower pressure. A method for methane fermentation treatment of organic waste, characterized in that the stirring is performed alternately between the plurality of fermentation tanks.
間で交互に圧力差が生じるように、前記複数の発酵槽に
交互に導入する請求項１記載の有機性廃棄物のメタン発
酵処理方法。2. The methane fermentation of organic waste according to claim 1, wherein the organic waste is alternately introduced into the plurality of fermenters so that a pressure difference is alternately generated between the plurality of fermenters. Processing method.
廃棄物を発酵槽に導入するための有機性廃棄物供給手段
と、前記有機性廃棄物をメタン発酵させるための複数の
発酵槽と、前記発酵槽内の圧力を検出するための圧力検
出手段と、前記メタン発酵によって生成したガスを貯留
するためのガス貯留槽と、 前記複数の発酵槽内の前記生成ガスが占める上部空間と
前記ガス貯留槽とを連結する第１配管と、前記発酵槽内
の上部空間と他の発酵槽内の前記有機性廃棄物が占める
下部空間とを連結する第２配管とを備え、 前記圧力検出手段によって前記複数の発酵槽間の圧力差
を検出した場合に、前記圧力の高い方の発酵槽から前記
圧力の低い方の発酵槽へ、前記第２配管を通じて前記生
成ガスを供給する切替え手段が設けられていることを特
徴とする有機性廃棄物のメタン発酵処理装置。3. An organic waste supply means for introducing an organic waste decomposable by anaerobic microorganisms into a fermentation tank, a plurality of fermentation tanks for methane-fermenting the organic waste, and Pressure detection means for detecting the pressure in the fermentor, a gas storage tank for storing the gas generated by the methane fermentation, an upper space occupied by the generated gas in the plurality of fermentation tanks and the gas storage A first pipe connecting the tank and a second pipe connecting an upper space in the fermentation tank with a lower space occupied by the organic waste in another fermentation tank; When a pressure difference between a plurality of fermenters is detected, switching means is provided for supplying the produced gas from the fermenter with a higher pressure to the fermenter with a lower pressure through the second pipe. Characterized by Methane fermentation treatment apparatus that organic waste.
性廃棄物を前記複数の発酵槽に交互に供給するための切
替え手段を備える請求項３記載の有機性廃棄物のメタン
発酵処理装置。4. The apparatus for methane fermentation treatment of organic waste according to claim 3, wherein the organic waste supply means includes a switching means for alternately supplying the organic waste to the plurality of fermentation tanks. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002158549A JP3716817B2 (en) | 2002-05-31 | 2002-05-31 | Method and apparatus for methane fermentation treatment of organic waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002158549A JP3716817B2 (en) | 2002-05-31 | 2002-05-31 | Method and apparatus for methane fermentation treatment of organic waste |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2003340416A true JP2003340416A (en) | 2003-12-02 |
| JP3716817B2 JP3716817B2 (en) | 2005-11-16 |
Family
ID=29773760
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002158549A Expired - Fee Related JP3716817B2 (en) | 2002-05-31 | 2002-05-31 | Method and apparatus for methane fermentation treatment of organic waste |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3716817B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005169165A (en) * | 2003-12-08 | 2005-06-30 | Fuji Electric Holdings Co Ltd | Treatment method for organic waste and its system |
| JP2006167608A (en) * | 2004-12-16 | 2006-06-29 | Sumitomo Heavy Ind Ltd | Fermentation method and apparatus by low-power agitation |
| WO2009000554A2 (en) * | 2007-06-27 | 2008-12-31 | Asw Anlagenbau Schlamm- Und Wassertechnik Gmbh | Biogas plant comprising a fermenter |
| JP2010082518A (en) * | 2008-09-30 | 2010-04-15 | Kobelco Eco-Solutions Co Ltd | Method of recovering methane gas and energy conversion system |
| JP2010234319A (en) * | 2009-03-31 | 2010-10-21 | Chugoku Electric Power Co Inc:The | Foreign matter removing apparatus for biomass |
| JP2010269223A (en) * | 2009-05-19 | 2010-12-02 | Hitachi Engineering & Services Co Ltd | Method and apparatus for treating organic waste |
| CN107828649A (en) * | 2017-11-07 | 2018-03-23 | 武汉和信益科技有限公司 | Large-scale full-mixing type anaerobic marsh-gas fermentation tank thermal compensation system and its process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52155177A (en) * | 1976-06-21 | 1977-12-23 | Tomoo Wada | Method of treating organic waste waters |
| JPS56108593A (en) * | 1980-01-31 | 1981-08-28 | Matsushita Electric Works Ltd | Methane fermentation apparatus |
| JPS61114796A (en) * | 1984-11-09 | 1986-06-02 | Japan Organo Co Ltd | Anaerobic filter bed apparatus |
| JPH11162494A (en) * | 1997-12-02 | 1999-06-18 | Ekishii:Kk | Garbage disposal system and method and device for feeding gas to fuel cell by utilizing garbage |
| JP2002066517A (en) * | 2000-08-31 | 2002-03-05 | Toshiba Corp | Garbage biogasification device |
-
2002
- 2002-05-31 JP JP2002158549A patent/JP3716817B2/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52155177A (en) * | 1976-06-21 | 1977-12-23 | Tomoo Wada | Method of treating organic waste waters |
| JPS56108593A (en) * | 1980-01-31 | 1981-08-28 | Matsushita Electric Works Ltd | Methane fermentation apparatus |
| JPS61114796A (en) * | 1984-11-09 | 1986-06-02 | Japan Organo Co Ltd | Anaerobic filter bed apparatus |
| JPH11162494A (en) * | 1997-12-02 | 1999-06-18 | Ekishii:Kk | Garbage disposal system and method and device for feeding gas to fuel cell by utilizing garbage |
| JP2002066517A (en) * | 2000-08-31 | 2002-03-05 | Toshiba Corp | Garbage biogasification device |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005169165A (en) * | 2003-12-08 | 2005-06-30 | Fuji Electric Holdings Co Ltd | Treatment method for organic waste and its system |
| JP2006167608A (en) * | 2004-12-16 | 2006-06-29 | Sumitomo Heavy Ind Ltd | Fermentation method and apparatus by low-power agitation |
| WO2009000554A2 (en) * | 2007-06-27 | 2008-12-31 | Asw Anlagenbau Schlamm- Und Wassertechnik Gmbh | Biogas plant comprising a fermenter |
| WO2009000554A3 (en) * | 2007-06-27 | 2009-02-19 | Asw Anlagenbau Schlamm Und Was | Biogas plant comprising a fermenter |
| JP2010082518A (en) * | 2008-09-30 | 2010-04-15 | Kobelco Eco-Solutions Co Ltd | Method of recovering methane gas and energy conversion system |
| JP2010234319A (en) * | 2009-03-31 | 2010-10-21 | Chugoku Electric Power Co Inc:The | Foreign matter removing apparatus for biomass |
| JP2010269223A (en) * | 2009-05-19 | 2010-12-02 | Hitachi Engineering & Services Co Ltd | Method and apparatus for treating organic waste |
| CN107828649A (en) * | 2017-11-07 | 2018-03-23 | 武汉和信益科技有限公司 | Large-scale full-mixing type anaerobic marsh-gas fermentation tank thermal compensation system and its process |
| CN107828649B (en) * | 2017-11-07 | 2024-04-09 | 武汉和信益科技有限公司 | Large-scale full-mixing type anaerobic biogas fermentation tank thermal compensation system and process method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3716817B2 (en) | 2005-11-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP1767284A1 (en) | Method of biomass processing | |
| US5525229A (en) | Process and apparatus for anaerobic digestion | |
| CN101094735B (en) | Method for decomposing biogenic material | |
| US7556737B2 (en) | Anaerobic phased solids digester for biogas production from organic solid wastes | |
| EP2521768B1 (en) | Apparatus and preculture tank for biomethanation of biomass | |
| CN101921049B (en) | Method and device for producing methane by using dry anaerobic digestion for urban sludge and organic matter | |
| US20040262220A1 (en) | Method and apparatus for anaerobic digestion of biomasses and generation of biogas | |
| CN102921711B (en) | Organic solid waste regeneration resource treatment method and apparatus system thereof | |
| JPS5940518B2 (en) | Anaerobic digestion method for cellulose-containing waste | |
| CN1273373C (en) | Method and device for making hydrogen using sewage plant residual mud to produce anaerobic fermentation | |
| JP2010082518A (en) | Method of recovering methane gas and energy conversion system | |
| JP3716817B2 (en) | Method and apparatus for methane fermentation treatment of organic waste | |
| JP2004082017A (en) | Methane fermentation method of organic waste and system therefor | |
| JP2006314920A (en) | Method for recovering energy from biomass | |
| JP2005125149A (en) | Method and apparatus for anaerobically treating organic waste | |
| JP4572278B2 (en) | Fuel supply method and fuel supply apparatus | |
| CN102056684A (en) | Method and plant for processing waste and producing methane | |
| JP2004194625A (en) | Hydrogen production apparatus and hydrogen production method | |
| KR101756446B1 (en) | Reduction and Biogas Production System Using Anaerobic Digestion of Organic Waste and Livestock manure and Operation Method Using the Same | |
| EP1529850A1 (en) | Process for treating tanned leather wastes and apparatus therefor | |
| JP4025733B2 (en) | Methane fermentation equipment | |
| JP2006255537A (en) | Method and apparatus for treating garbage and paper refuse | |
| JP2005013045A (en) | Method for continuously producing hydrogen from organic waste | |
| KR100196916B1 (en) | Method for organic waste | |
| CN114989966B (en) | Anaerobic fermentation system and anaerobic fermentation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20040713 |
|
| RD02 | Notification of acceptance of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7422 Effective date: 20040726 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20050729 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20050809 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20050822 |
|
| R150 | Certificate of patent or registration of utility model |
Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080909 Year of fee payment: 3 |
|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080909 Year of fee payment: 3 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080909 Year of fee payment: 3 |
|
| S111 | Request for change of ownership or part of ownership |
Free format text: JAPANESE INTERMEDIATE CODE: R313113 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080909 Year of fee payment: 3 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080909 Year of fee payment: 3 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090909 Year of fee payment: 4 |
|
| S111 | Request for change of ownership or part of ownership |
Free format text: JAPANESE INTERMEDIATE CODE: R313111 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090909 Year of fee payment: 4 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090909 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100909 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100909 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110909 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120909 Year of fee payment: 7 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130909 Year of fee payment: 8 |
|
| LAPS | Cancellation because of no payment of annual fees |