JPH0568849A - Method and device for desulfurizing digestion gas - Google Patents
Method and device for desulfurizing digestion gasInfo
- Publication number
- JPH0568849A JPH0568849A JP23830891A JP23830891A JPH0568849A JP H0568849 A JPH0568849 A JP H0568849A JP 23830891 A JP23830891 A JP 23830891A JP 23830891 A JP23830891 A JP 23830891A JP H0568849 A JPH0568849 A JP H0568849A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- gas
- aerobic
- digestion
- hydrogen sulfide
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
- Treating Waste Gases (AREA)
- Activated Sludge Processes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は下水、し尿、産業排水、
汚泥、ゴミ等の有機性物質の嫌気性微生物消化により発
生する消化ガスから、硫化水素を除去するための消化ガ
スの脱硫方法および装置に関する。The present invention relates to sewage, night soil, industrial wastewater,
The present invention relates to a method and an apparatus for desulfurizing digestive gas for removing hydrogen sulfide from digestive gas generated by anaerobic microbial digestion of organic substances such as sludge and dust.
【０００２】[0002]
【従来の技術】下水、し尿、産業排水等の排水、または
汚泥、ゴミ等の固形廃棄物などの有機性物質の処理法と
して、嫌気性微生物消化（以下、嫌気性消化という場合
がある）および好気性微生物酸化（以下、好気性酸化と
いう場合がある）が行われている。このうち嫌気性消化
では、メタン発酵により、消化ガス（バイオガス）が発
生する。この消化ガス中には、メタンのほかに、二酸化
炭素および硫化水素などのガスが含まれている。このよ
うな消化ガスは、通常エネルギー回収の目的で、ボイラ
ーまたは焼却炉の燃料などとして有効利用される場合が
多いが、焼却装置の腐食防止および大気汚染防止の観点
から、燃焼に利用する前に硫化水素の除去（脱硫）が行
われる。消化ガス中には、通常０．０５〜２ｖ／ｖ％程
度の硫化水素が含まれているが、この濃度はメタン発酵
処理を受ける排水または廃棄物中の硫酸イオン濃度によ
り変わる。BACKGROUND ART Anaerobic microbial digestion (hereinafter sometimes referred to as anaerobic digestion) and a method for treating organic substances such as wastewater such as sewage, night soil, industrial wastewater, and solid waste such as sludge and garbage, and Aerobic microbial oxidation (hereinafter sometimes referred to as aerobic oxidation) is performed. In the anaerobic digestion, digestive gas (biogas) is generated by methane fermentation. In addition to methane, the digestive gas contains gases such as carbon dioxide and hydrogen sulfide. Such digestive gas is usually used effectively as fuel for boilers or incinerators for the purpose of recovering energy, but from the viewpoint of preventing corrosion of incinerators and preventing air pollution, before use for combustion. Hydrogen sulfide is removed (desulfurization). Digestion gas usually contains about 0.05 to 2 v / v% hydrogen sulfide, but this concentration varies depending on the concentration of sulfate ion in wastewater or waste subjected to methane fermentation treatment.
【０００３】従来、消化ガスの脱硫方法としては、水を
用いてガスを洗浄する水洗浄法、薬品を用いてガスを洗
浄する薬品洗浄法、微生物により硫化水素を分解する方
法などがある。Conventionally, as a method for desulfurizing digested gas, there are a water cleaning method of cleaning gas with water, a chemical cleaning method of cleaning gas with chemicals, a method of decomposing hydrogen sulfide by microorganisms, and the like.
【０００４】このうち水洗浄法は、消化ガスを洗浄液と
接触させ、ガス中の硫化水素を洗浄液に吸収させて脱硫
する方法である。しかし、従来の水洗浄法では、吸収効
率が悪く、高い脱硫率を得るためには、大量の洗浄液が
必要であり、また硫化水素を吸収した廃液は鉄塩等の添
加により処理する必要があり、生成する汚泥の処理も困
難であるなどの問題点がある。Of these methods, the water washing method is a method in which a digestion gas is brought into contact with a washing liquid, and hydrogen sulfide in the gas is absorbed by the washing liquid to desulfurize the gas. However, in the conventional water washing method, the absorption efficiency is poor, and in order to obtain a high desulfurization rate, a large amount of washing liquid is required, and the waste liquid that has absorbed hydrogen sulfide needs to be treated by adding an iron salt or the like. However, there is a problem that it is difficult to treat the generated sludge.
【０００５】薬品洗浄法は、洗浄液の代わりにアルカリ
などの吸収剤、例えば水酸化ナトリウムを使用し、この
吸収剤に硫化水素を吸収させて脱硫する方法である。こ
の方法では、薬品と反応させて脱硫するため、大量の消
化ガスを処理する場合、または硫化水素が高濃度の場合
には、処理費が高くなる。また消化ガス中に含まれてい
る二酸化炭素も吸収剤に吸収されるため、硫化水素の吸
収に要求される以上の吸収剤が必要となる。さらに、硫
化水素を吸収した廃液の処理が困難であるなどの問題が
ある。The chemical cleaning method is a method in which an absorbent such as alkali, for example, sodium hydroxide is used in place of the cleaning liquid, and hydrogen sulfide is absorbed in this absorbent to desulfurize. In this method, since it reacts with a chemical to desulfurize, a large amount of digestion gas is treated, or the treatment cost is high when hydrogen sulfide has a high concentration. Further, since carbon dioxide contained in the digestive gas is also absorbed by the absorbent, an absorbent more than that required for absorbing hydrogen sulfide is required. Further, there is a problem that it is difficult to treat the waste liquid that has absorbed hydrogen sulfide.
【０００６】微生物を利用する方法としては、硫化水素
を酸化分解する微生物が付着している充填材層を充填し
た生物脱硫塔に消化ガスを通気して硫化水素を分解する
方法がある（特開平２−２６６１５号）。[0006] As a method of utilizing microorganisms, there is a method of decomposing hydrogen sulfide by aerating digestion gas through a biological desulfurization tower filled with a packing material layer to which microorganisms that oxidize and decompose hydrogen sulfide adhere. 2-26615).
【０００７】この方法は硫化水素を選択的に効率よく分
解除去でき、脱硫に伴って新たに廃液を生じないなどの
点で優れた方法であるが、消化ガス中には酸素が含まれ
ていないため、硫化水素を酸化するのに必要な空気また
は酸素ガスを消化ガスとともに生物脱硫塔に供給する必
要がある。このため、消化ガス中に空気または酸素ガス
が残留するとともに、二酸化炭素も生成し、このため消
化ガスの主成分であるメタンガスの含有率が低下し、利
用価値が低下する。This method is an excellent method in that hydrogen sulfide can be selectively decomposed and removed efficiently, and no new waste liquid is generated with desulfurization, but the digestion gas does not contain oxygen. Therefore, it is necessary to supply the air or oxygen gas required for oxidizing hydrogen sulfide to the biological desulfurization tower together with the digestion gas. For this reason, air or oxygen gas remains in the digestive gas and carbon dioxide is also produced, which lowers the content rate of methane gas, which is the main component of the digestive gas, and reduces the utility value.
【０００８】[0008]
【発明が解決しようとする課題】本発明の目的は、上記
問題点を解決するため、メタンガスの含有率を低下させ
ず、低コストで効率よく、しかも高い脱硫率で脱硫で
き、かつ脱硫に伴って新たな廃液を生じない消化ガスの
脱硫方法および装置を提案することである。SUMMARY OF THE INVENTION An object of the present invention is to solve the above problems, in order to solve the above problems, the methane gas content is not reduced, the cost is low, the efficiency is high, and the desulfurization can be performed at a high desulfurization rate. Therefore, it is an object of the present invention to propose a method and an apparatus for desulfurizing digestion gas that does not generate new waste liquid.
【０００９】[0009]
【課題を解決するための手段】本発明は、次の消化ガス
の脱硫方法および装置である。 （１）有機性物質の嫌気性微生物消化により発生する消
化ガスを、有機性物質の好気性微生物酸化における混合
液または処理液からなる洗浄液と接触させて、前記消化
ガス中の硫化水素を前記洗浄液に吸収させる吸収工程
と、前記吸収工程で得られた吸収液を好気性微生物酸化
して、吸収された硫化水素を酸化する酸化工程とからな
ることを特徴とする消化ガスの脱硫方法。 （２）有機性物質を嫌気性微生物消化し、消化ガスを発
生させる嫌気性消化施設と、有機性物質を好気性微生物
酸化して有機物を分解する好気性酸化装置と、前記嫌気
性消化施設で発生する消化ガスを、前記好気性酸化装置
における混合液または処理液からなる洗浄液と接触させ
て、前記消化ガス中の硫化水素を前記洗浄液に吸収させ
る吸収装置と、前記嫌気性消化施設から前記吸収装置に
消化ガスを供給するガス供給路と、前記好気性酸化装置
から前記吸収装置に混合液または処理液を供給する送液
路と、前記吸収装置から前記好気性酸化装置に吸収液を
返送する返送液路とを有することを特徴とする消化ガス
の脱硫装置。The present invention provides the following digestion gas desulfurization method and apparatus. (1) A digestive gas generated by anaerobic microbial digestion of an organic substance is brought into contact with a cleaning liquid consisting of a mixed liquid or a treatment liquid in aerobic microbial oxidation of an organic substance, and hydrogen sulfide in the digestive gas is replaced with the cleaning liquid. A method for desulfurizing a digestive gas, comprising: an absorption step of absorbing the absorption solution obtained by the above step; and an oxidation step of oxidizing the absorbed liquid obtained in the absorption step by aerobic microorganisms to oxidize the absorbed hydrogen sulfide. (2) In an anaerobic digestion facility that digests organic substances by anaerobic microorganisms to generate digestive gas, an aerobic oxidizer that decomposes organic substances by aerobic microbial oxidation of organic substances, and the anaerobic digestion facility The generated digestive gas is brought into contact with a cleaning liquid composed of a mixed liquid or a treatment liquid in the aerobic oxidation device to absorb hydrogen sulfide in the digestive gas into the cleaning liquid, and the absorption from the anaerobic digestion facility. A gas supply path for supplying a digestive gas to the apparatus, a liquid supply path for supplying a mixed solution or a processing solution from the aerobic oxidation apparatus to the absorption apparatus, and an absorption solution returned from the absorption apparatus to the aerobic oxidation apparatus A desulfurization apparatus for digestive gas, comprising a return liquid passage.
【００１０】本発明の処理の対象となる消化ガスは、例
えば下水、し尿、産業排水等の排水および汚泥、ゴミ等
の固形廃棄物などの有機性物質を嫌気性消化する際、メ
タン発酵により発生する消化ガスである。このような消
化ガス中には、通常メタンガスのほかに、二酸化炭素お
よび硫化水素などのガスが含まれている。上記の消化ガ
スは嫌気性消化装置における嫌気性消化により発生する
のが一般的であるが、ゴミ埋立地など、嫌気性消化装置
以外の嫌気性消化施設における嫌気性消化により発生す
る場合もある。嫌気性消化は、被処理物である有機性物
質を嫌気状態に保つことにより、嫌気性微生物の作用を
利用して行われ、充填層型、流動層型、スラッジブラン
ケット型など、任意の嫌気性消化装置により処理するこ
とができる。The digestive gas to be treated in the present invention is generated by methane fermentation during anaerobic digestion of wastewater such as sewage, night soil, industrial wastewater and organic substances such as sludge and solid waste such as garbage. It is a digestive gas that does. Such digestive gas usually contains gases such as carbon dioxide and hydrogen sulfide in addition to methane gas. The above-mentioned digestive gas is generally generated by anaerobic digestion in an anaerobic digester, but it may also be generated by anaerobic digestion in an anaerobic digester other than the anaerobic digester such as a garbage landfill. Anaerobic digestion is performed by utilizing the action of anaerobic microorganisms by keeping the organic substance that is the object to be treated in an anaerobic state, and can be used for any anaerobic type such as packed bed type, fluidized bed type, sludge blanket type, etc. It can be processed by a digester.
【００１１】本発明では吸収工程において、消化ガスを
洗浄液と接触させて、消化ガス中の硫化水素を洗浄液に
吸収させる。洗浄液としては、有機性物質の好気性酸化
における混合液または処理液が使用される。好気性酸化
を行う有機性物質としては、嫌気性消化の消化液（処理
液）である場合が多いが、嫌気性消化の被処理物と同じ
有機性物質でもよく、あるいは他の有機性物質でもよ
い。In the present invention, in the absorbing step, the digestive gas is brought into contact with the cleaning liquid so that hydrogen sulfide in the digestive gas is absorbed by the cleaning liquid. As the cleaning liquid, a mixed liquid or a treatment liquid for aerobic oxidation of an organic substance is used. The organic substance that performs aerobic oxidation is often the digestive liquid (treatment liquid) of anaerobic digestion, but it may be the same organic substance as the object to be treated of anaerobic digestion, or another organic substance. Good.
【００１２】これらの場合、嫌気性消化施設の消化液を
好気性酸化装置に導入して好気性酸化を行い、その混合
液または処理液を洗浄液として吸収装置に送液し、前記
嫌気性消化施設から供給される消化ガスと接触させるの
が一般的であるが、嫌気性消化の対象と好気性酸化の対
象が異なる場合もある。また嫌気性消化液をそのまま下
水道等に放流する系においては、本発明の脱硫を行うた
めに、嫌気性消化液の一部を好気性酸化することもでき
る。この場合、好気性酸化を行う嫌気性消化液の量は、
脱硫の酸化工程に必要な範囲でよい。In these cases, the digestive liquid of the anaerobic digestion facility is introduced into the aerobic oxidation device to perform aerobic oxidation, and the mixed solution or treatment liquid is sent to the absorption device as a cleaning liquid, and the anaerobic digestion facility is used. Although it is generally contacted with digestive gas supplied from the subject, the target of anaerobic digestion and the target of aerobic oxidation may be different. Further, in a system in which the anaerobic digestive liquid is discharged as it is to a sewer or the like, a part of the anaerobic digestive liquid can be aerobically oxidized in order to carry out the desulfurization of the present invention. In this case, the amount of anaerobic digestive fluid that performs aerobic oxidation is
It may be in the range necessary for the oxidation step of desulfurization.
【００１３】好気性酸化は、被処理物である有機性物質
を好気状態に保って、好気性微生物の作用を利用して有
機物を酸化分解する処理であり、活性汚泥法、散布濾床
法、浸漬型の固定床法、流動床法、回転円板法など、任
意の好気性酸化装置を用いた処理法により処理を行うこ
とができる。The aerobic oxidation is a treatment for keeping an organic substance as an object to be treated in an aerobic state and oxidatively decomposing the organic substance by utilizing the action of aerobic microorganisms. The activated sludge method and the spray filter method are used. The treatment can be carried out by a treatment method using any aerobic oxidizer such as an immersion type fixed bed method, a fluidized bed method or a rotating disk method.
【００１４】洗浄液として用いる好気性酸化における混
合液は、好気性酸化を行っている途中の被処理液が、好
気性微生物を含む汚泥（活性汚泥）と混合した状態の混
合液であり、処理液は好気性酸化を終って汚泥を分離し
た処理液である。The mixed liquid in the aerobic oxidation used as the cleaning liquid is a mixed liquid in which the liquid to be treated during the aerobic oxidation is mixed with sludge containing aerobic microorganisms (activated sludge). Is a treatment liquid obtained by finishing aerobic oxidation and separating sludge.
【００１５】洗浄液としては、混合液を用いる方が硫化
水素の吸収効率は高く、脱硫率が高くなる。これは汚泥
による吸着、または好気性微生物による摂取によるもの
と推測されるが、明らかではない。もっとも気液接触効
率の高い吸収装置を用いれば、処理液による吸収効率も
高くなり、脱硫率も高くなる。As a cleaning liquid, the use of a mixed liquid has a higher hydrogen sulfide absorption efficiency and a higher desulfurization rate. It is speculated that this is due to adsorption by sludge or ingestion by aerobic microorganisms, but it is not clear. If the absorption device with the highest gas-liquid contact efficiency is used, the absorption efficiency of the treatment liquid will be high and the desulfurization rate will be high.
【００１６】吸収工程に用いる吸収装置としては、消化
ガスと洗浄液を効率よく気液接触させるものであればよ
く、ばっ気槽、充填塔、スプレー塔、スクラバーなど、
任意の形式のものが使用可能である。吸収装置への消化
ガスの通ガス条件は、通常空間速度（ＳＶ）が５〜５０
ｈｒ-1、好ましくは１０〜２０ｈｒ-1、洗浄液の通液条
件は、通常滞留時間(ＨＲＴ)が２〜２０分間、好ましく
は５〜１０分間が望ましい。The absorbing device used in the absorbing step may be any one capable of efficiently bringing the digestive gas and the cleaning liquid into gas-liquid contact with each other, such as an aeration tank, a packed tower, a spray tower, and a scrubber.
Any form can be used. The conditions for passing digestion gas to the absorber are usually a space velocity (SV) of 5 to 50.
hr -1, preferably 10～20Hr -1, liquid passing condition of the cleaning liquid is usually residence time (HRT) is 2-20 minutes, preferably desirably 5-10 minutes.
【００１７】吸収装置において気液接触することによ
り、消化ガス中の硫化水素は洗浄液に吸収され、吸収液
が得られる。このとき消化ガス中の二酸化炭素その他の
不純物も洗浄液に吸収され、メタン濃度の高い処理ガス
が得られる。混合液を洗浄液とする場合は、硫化水素が
混合液に吸収されたとき、汚泥による吸着、または微生
物による摂取が生じるものと思われる。洗浄液のｐＨが
高いほど硫化水素の吸収効率が高いが、一般的にはｐＨ
７〜９とするのが好ましい。By making gas-liquid contact in the absorption device, hydrogen sulfide in the digestion gas is absorbed by the cleaning liquid to obtain an absorption liquid. At this time, carbon dioxide and other impurities in the digested gas are also absorbed by the cleaning liquid, and a processed gas having a high methane concentration is obtained. When the mixed solution is used as the cleaning solution, when hydrogen sulfide is absorbed by the mixed solution, it is considered that adsorption by sludge or ingestion by microorganisms occurs. The higher the pH of the cleaning liquid, the higher the absorption efficiency of hydrogen sulfide, but generally the pH
It is preferably 7-9.
【００１８】好気性酸化装置の混合液または処理液はエ
アレーションにより有機物が分解されるとともに、二酸
化炭素がストリッピングされるため、嫌気性消化液に比
べてアルカリ度およびｐＨがともに高くなっており、ｐ
Ｈは通常７〜９である。このため混合液または処理液は
ｐＨ調整することなく、そのまま洗浄液として使用する
ことができるが、ｐＨが低い場合にはアルカリを添加し
てもよい。Since the organic matter is decomposed by aeration and the carbon dioxide is stripped in the mixed solution or treatment solution of the aerobic oxidizer, both alkalinity and pH are higher than those of the anaerobic digestion solution. p
H is usually 7-9. Therefore, the mixed solution or the treatment solution can be used as it is as a cleaning solution without adjusting the pH, but when the pH is low, an alkali may be added.
【００１９】吸収工程において硫化水素を吸収した吸収
液は、酸化工程において好気性酸化装置に返送して好気
性酸化を行い、好気性微生物の作用により硫化水素を酸
化する。このとき吸収工程で吸収された他の不純物も処
理される。例えば二酸化炭素はストリッピングされ、有
機物は分解される。The absorption liquid which has absorbed hydrogen sulfide in the absorption step is returned to the aerobic oxidation device in the oxidation step for aerobic oxidation, and the hydrogen sulfide is oxidized by the action of aerobic microorganisms. At this time, other impurities absorbed in the absorption step are also treated. For example, carbon dioxide is stripped and organic matter is decomposed.
【００２０】好気性酸化装置における好気性微生物は、
有機物を好気的に分解する細菌が主体となっているが、
汚泥中にはチオバチルス属、チオトリックス属およびベ
ギアトア属などのイオウ酸化細菌が含まれているため、
その酸化作用により硫化水素は硫酸イオンまたは単体イ
オウに酸化され無害化する。Aerobic microorganisms in the aerobic oxidizer are:
Mainly bacteria that aerobically decompose organic matter,
Since sludge contains sulfur-oxidizing bacteria such as Thiobacillus, Thiotrix and Begiatoa,
Due to the oxidizing action, hydrogen sulfide is oxidized to sulfate ions or elemental sulfur to render it harmless.
【００２１】硫化水素の酸化により、硫酸イオンが生成
するため、混合液または処理液のｐＨが低下する。通常
はｐＨ調整することなく、混合液または処理液をそのま
ま吸収工程に送って硫化水素の吸収を行うことができる
が、硫化水素の量が多い場合は生成する硫酸イオンの量
も多いので、ｐＨが７より小さくなる場合は、水酸化ナ
トリウム等のアルカリを添加してｐＨを７〜９に維持す
るのが好ましい。この場合でも、アルカリの使用量は、
薬品洗浄法に比べると少ない。Oxidation of hydrogen sulfide produces sulfate ions, which lowers the pH of the mixed solution or treatment solution. Usually, without adjusting the pH, the mixed solution or the treatment solution can be directly sent to the absorption step to absorb hydrogen sulfide, but if the amount of hydrogen sulfide is large, the amount of sulfate ions produced is also large. When is less than 7, it is preferable to maintain the pH at 7-9 by adding an alkali such as sodium hydroxide. Even in this case, the amount of alkali used is
Less than the chemical cleaning method.
【００２２】好気性酸化により有機物を分解するととも
に、硫化水素を酸化した混合液は、固液分離により固形
物を除去し、分離液を処理液として放流する。分離した
汚泥は必要量を好気性酸化装置に返送し、余剰汚泥は系
外に排出する。この間混合液または処理液の一部は洗浄
液として吸収装置に送液される。The mixed liquid obtained by decomposing organic substances by aerobic oxidation and oxidizing hydrogen sulfide is subjected to solid-liquid separation to remove solids, and the separated liquid is discharged as a treatment liquid. The necessary amount of separated sludge is returned to the aerobic oxidizer, and excess sludge is discharged to the outside of the system. During this time, part of the mixed solution or the processing solution is sent to the absorption device as a cleaning solution.
【００２３】[0023]
【実施例】以下、本発明を実施例により説明する。図１
および図２は別の実施例による消化ガスの脱硫装置を示
す系統図である。図において、１は嫌気性消化装置、２
は好気性酸化装置、３は吸収装置である。EXAMPLES The present invention will be described below with reference to examples. Figure 1
FIG. 2 is a system diagram showing a digestion gas desulfurization apparatus according to another embodiment. In the figure, 1 is an anaerobic digester, 2
Is an aerobic oxidizer, and 3 is an absorber.
【００２４】嫌気性消化装置１は密閉型の槽からなり、
スラッジブランケット、流動床等の嫌気性微生物を含む
バイオマス４が形成されている。嫌気性消化装置１の下
部には被処理物導入路５が連絡し、上部から嫌気性消化
液移送路６がポンプＰ1を介して好気性酸化装置２に連
絡し、頂部からガス供給路７が吸収装置３の下部に連絡
している。The anaerobic digester 1 comprises a closed tank,
A biomass 4 containing anaerobic microorganisms such as a sludge blanket and a fluidized bed is formed. An object introduction passage 5 communicates with the lower part of the anaerobic digester 1, an anaerobic digestion liquid transfer passage 6 communicates with the aerobic oxidizer 2 via a pump P 1 from the upper part, and a gas supply passage 7 from the top. Communicates with the bottom of the absorber 3.
【００２５】好気性酸化装置２は、好気性酸化部８と固
液分離部９とからなる。好気性酸化部８の上部には、嫌
気性消化液移送路６および返送液路１０が連絡し、下部
には散気管１１が設けられ、これに給気路１２が連路し
ている。固液分離部９には処理液排出路１３が連絡して
いる。The aerobic oxidizer 2 comprises an aerobic oxidizer 8 and a solid-liquid separator 9. An anaerobic digestion liquid transfer passage 6 and a return liquid passage 10 are connected to the upper part of the aerobic oxidation part 8, and an air diffuser pipe 11 is provided in the lower part thereof, and an air supply passage 12 is connected thereto. The treatment liquid discharge path 13 is connected to the solid-liquid separation section 9.
【００２６】吸収装置３は内部に、図１では洗浄液１４
を貯留し、図２では充填層１５を形成している。吸収装
置３の下部にはガス供給路７および返送液路１０が連絡
し、上部にはガス排出路１６および送液路１７が連絡し
ている。送液路１７は図１では好気性酸化装置２の好気
性酸化部８から、図２では処理液排出路１３から、それ
ぞれポンプＰ2を介して連絡している。The absorption device 3 is internally provided with the cleaning liquid 14 in FIG.
Is stored, and the filling layer 15 is formed in FIG. The gas supply passage 7 and the return liquid passage 10 are connected to the lower portion of the absorber 3, and the gas discharge passage 16 and the liquid passage 17 are connected to the upper portion. The liquid feed passage 17 is connected to the aerobic oxidation section 8 of the aerobic oxidation device 2 in FIG. 1 and the treatment liquid discharge passage 13 in FIG. 2 via a pump P 2 .
【００２７】上記の消化ガスの脱硫装置による脱硫方法
は次の通りである。まず嫌気性消化装置１に被処理物導
入路５から、下水、し尿、排水等の有機性物質からなる
被処理物を導入して、上向流でバイオマス４と嫌気状態
で接触させると、嫌気性微生物の作用によりメタン発酵
および酸発酵が行われ、有機物が分解する。この嫌気性
消化により発生する消化ガスをガス供給路７から吸収装
置３に供給し、嫌気性消化液をポンプＰ1により嫌気性
消化液移送路６から好気性酸化装置２に移送する。The desulfurization method of the above-mentioned digestion gas desulfurization apparatus is as follows. First, an anaerobic digester 1 is introduced with an object to be treated consisting of an organic substance such as sewage, human waste, drainage, etc. from the object introduction path 5 and brought into anaerobic contact with the biomass 4 in an upward flow. Methane fermentation and acid fermentation are performed by the action of the sex microorganisms, and organic substances are decomposed. The digestion gas generated by this anaerobic digestion is supplied to the absorber 3 from the gas supply passage 7, and the anaerobic digestion liquid is transferred from the anaerobic digestion liquid transfer passage 6 to the aerobic oxidation device 2 by the pump P 1 .
【００２８】好気性酸化装置２では、嫌気性消化液移送
路６から流入する被処理液を好気性酸化部８において活
性汚泥と混合し、給気路１２から空気等の酸素含有ガス
を供給して、散気管１１から散気し、好気性酸化を行
う。この好気性酸化において、活性汚泥に含まれる好気
性微生物の作用により有機物が分解される。そして好気
性酸化部８内の混合液の一部は固液分離部９に入って固
液分離され、分離液は処理液として処理液排出路１３か
ら排出される。分離した活性汚泥の一部は好気性酸化部
８に返送され、余剰汚泥は系外へ排出される。In the aerobic oxidizer 2, the liquid to be treated flowing in from the anaerobic digestion liquid transfer passage 6 is mixed with activated sludge in the aerobic oxidizer 8, and an oxygen-containing gas such as air is supplied from the air supply passage 12. Then, air is diffused from the air diffuser 11 to perform aerobic oxidation. In this aerobic oxidation, organic substances are decomposed by the action of aerobic microorganisms contained in activated sludge. Then, a part of the mixed liquid in the aerobic oxidation unit 8 enters the solid-liquid separation unit 9 and is solid-liquid separated, and the separated liquid is discharged from the processing liquid discharge passage 13 as a processing liquid. Part of the separated activated sludge is returned to the aerobic oxidation section 8, and the excess sludge is discharged to the outside of the system.
【００２９】消化ガスの脱硫は、まず吸収工程におい
て、図１では好気性酸化装置２の好気性酸化部８から混
合液の一部を、また図２では処理液排出路１３から処理
液の一部を、それぞれポンプＰ2により送液路１７を通
して、吸収装置３の上部に送液し、図１では吸収装置３
内に注入し、図２では充填層１５上にスプレーする。そ
してガス供給路７から供給される消化ガスを上向流で洗
浄液１４または充填層１５を通過させて気液接触を行
い、消化ガス中の硫化水素、二酸化炭素、その他の水溶
性成分を洗浄液１４に吸収させる。In the absorption step, desulfurization of digestive gas is carried out by first removing a part of the mixed liquid from the aerobic oxidation part 8 of the aerobic oxidation device 2 in FIG. Each of the parts is sent to the upper part of the absorption device 3 by the pump P 2 through the liquid supply path 17, and in FIG.
2 and sprayed on the packed bed 15 in FIG. Then, the digestive gas supplied from the gas supply path 7 is passed upward through the cleaning liquid 14 or the packed bed 15 to make gas-liquid contact, and hydrogen sulfide, carbon dioxide, and other water-soluble components in the digestive gas are removed from the cleaning liquid 14 Absorb it.
【００３０】洗浄液１４は、混合液、処理液のいずれの
場合も二酸化炭素が除去されてｐＨが７〜９となってい
るため、硫化水素、二酸化炭素等の吸収効率はよい。気
液接触により硫化水素、二酸化炭素等を除去した消化ガ
スは、メタン濃度の高い処理ガスとして、ガス排出路１
６から排出される。また硫化水素、二酸化炭素等を吸収
した洗浄液１４は吸収液として返送液路１０から好気性
酸化装置２に返送される。The cleaning liquid 14 has a good absorption efficiency of hydrogen sulfide, carbon dioxide and the like, since carbon dioxide is removed and the pH is 7 to 9 in both cases of the mixed liquid and the treatment liquid. The digested gas from which hydrogen sulfide, carbon dioxide, etc. have been removed by gas-liquid contact is treated as a process gas with a high methane concentration,
Emitted from 6. The cleaning liquid 14 that has absorbed hydrogen sulfide, carbon dioxide, etc. is returned to the aerobic oxidation device 2 through the return liquid passage 10 as an absorbing liquid.
【００３１】好気性酸化装置２に返送された吸収液は、
酸化工程として、好気性酸化部８において活性汚泥を混
合され、好気性酸化を受ける。そして好気性微生物の作
用により、吸収液中の硫化水素その他の被酸化性物質は
微生物酸化され、無害化する。二酸化炭素は散気により
ストリッピングされ、除去される。硫化水素の酸化によ
り硫酸イオンが生成し、ｐＨが下がりすぎるときは、好
気性酸化部８にアルカリを注入し、ｐＨを調整する。The absorption liquid returned to the aerobic oxidizer 2 is
As an oxidation step, activated sludge is mixed in the aerobic oxidation part 8 and undergoes aerobic oxidation. Then, due to the action of aerobic microorganisms, hydrogen sulfide and other oxidizable substances in the absorbing solution are microbially oxidized and rendered harmless. Carbon dioxide is stripped and removed by aeration. When sulfate ions are generated by the oxidation of hydrogen sulfide and the pH is lowered too much, alkali is injected into the aerobic oxidation section 8 to adjust the pH.
【００３２】上記の脱硫のための酸化工程は、有機物除
去のための好気性酸化と同時に行われ、無害化した処理
液は処理液排出路１３からそのまま放流することができ
る。The above-mentioned oxidation step for desulfurization is carried out at the same time as the aerobic oxidation for removing organic matters, and the detoxified processing solution can be discharged as it is from the processing solution discharge passage 13.
【００３３】なお、上記実施例では、嫌気性消化装置１
の嫌気性消化液を、好気性酸化装置２において好気性酸
化しているが、嫌気性消化液をそのまま下水等に放流す
る場合は、他の廃水等の好気性酸化装置の混合液または
処理液を洗浄液１４として使用し、吸収液を返送するこ
とができる。In the above embodiment, the anaerobic digester 1 is used.
Although the anaerobic digestion liquid of 1. is aerobically oxidized in the aerobic oxidation device 2, when the anaerobic digestion liquid is discharged as it is to sewage or the like, a mixed liquid or treatment liquid of another aerobic oxidation device such as wastewater. Can be used as the cleaning liquid 14, and the absorbing liquid can be returned.
【００３４】またゴミ処分地、堆肥化施設等から発生す
る消化ガスを脱硫することもでき、これらの場合は、浸
出水等の好気性酸化の混合液または処理液を洗浄液１４
として利用することができる。It is also possible to desulfurize digestive gas generated from a waste disposal site, a composting facility or the like. In these cases, a mixed liquid or treatment liquid of aerobic oxidation such as leachate is used as the cleaning liquid 14
Can be used as
【００３５】以下、試験例について説明する。 試験例１ 図２に準じた方法で、コーンスターチ廃水の嫌気性消化
により発生した消化ガスの脱硫テストを行った。ただし
吸収装置３の充填層１５は省略されている。すなわち好
気性酸化装置２として５ｌｉｔｅｒの活性汚泥ばっ気
槽、吸収装置３として５００ｍｌの洗気ビンを用い、洗
浄液１４として好気性酸化装置２の処理液を送液し、下
記条件で１０日間にわたって連続脱硫テストを行った。The test examples will be described below. Test Example 1 A desulfurization test of a digestion gas generated by anaerobic digestion of corn starch wastewater was conducted by a method according to FIG. However, the packed bed 15 of the absorber 3 is omitted. That is, a 5-liter activated sludge aeration tank was used as the aerobic oxidizer 2, a 500 ml washing bottle was used as the absorber 3, and the treatment liquid of the aerobic oxidizer 2 was sent as the washing liquid 14, and the treatment liquid was continuously supplied for 10 days under the following conditions. A desulfurization test was conducted.
【００３６】消化ガスの組成：メタン約８０容量％、二
酸化炭素約２０容量％、硫化水素約５０００ｐｐｍ 洗浄液 ：処理液、ｐＨ７．４ 吸収条件 ：洗浄液流量；約５０ｍｌ／ｍｉｎ、消
化ガス流量；１００ｍｌ／ｍｉｎ 好気性酸化条件：被処理液；コーンスターチ廃水の嫌気
性消化液、ＢＯＤ5約１００ｍｇ／ｌ、ｐＨ７．２、滞
留時間；２４時間、アルカリの添加；なしComposition of digestion gas: methane about 80% by volume, carbon dioxide about 20% by volume, hydrogen sulfide about 5000 ppm Cleaning solution: treatment solution, pH 7.4 Absorption condition: cleaning solution flow rate: about 50 ml / min, digestion gas flow rate: 100 ml / min Aerobic oxidation conditions: liquid to be treated; anaerobic digestion liquid of corn starch wastewater, BOD 5 about 100 mg / l, pH 7.2, residence time; 24 hours, addition of alkali; none
【００３７】連続脱硫テストの期間中、朝と夕方の２
回、処理ガス中の硫化水素濃度などを測定した。１０日
間にわたるテスト期間中、安定した脱硫が行われた。結
果は次の通りである。なお数値は各値とも平均値であ
る。 消化ガス中の硫化水素濃度 ：５０３０ｐｐｍ 処理ガス中の硫化水素濃度 ：６７０ｐｐｍ 硫化水素の除去率 ：８６．７％ 活性汚泥ばっ気槽内ＭＬＳＳ ：３４００ｍｇ／ｌ 被処理液中のＳＯ4 2-濃度 ：２．５ｍｇ／ｌ 洗浄液（処理液）中のＳＯ4 2-濃度 ：９２０ｍｇ／ｌDuring the continuous desulfurization test, 2 in the morning and in the evening.
The concentration of hydrogen sulfide in the treated gas was measured. Stable desulfurization occurred during the 10 day test period. The results are as follows. The numerical values are average values. Hydrogen sulfide concentration in digested gas: 5030ppm Hydrogen sulfide concentration in treated gas: 670ppm Hydrogen sulfide removal rate: 86.7% MLSS in activated sludge aeration tank: 3400mg / l SO 4 2- concentration in treated liquid: 2.5 mg / l SO 4 2- concentration in cleaning solution (treatment solution): 920 mg / l
【００３８】試験例２ 図１に準じた方法で消化ガスの脱硫テストを行った。た
だし好気性酸化装置２では、別の合成廃水の好気性酸化
を行った。すなわち好気性酸化装置２として５０００ｍ
ｌの活性汚泥ばっ気槽、吸収装置３として５００ｍｌの
洗気ビンを用い、洗浄液１４として好気性酸化装置２内
の混合液を送液し、下記条件で約１０日間にわたって連
続脱硫テストを行った。Test Example 2 A desulfurization test of a digestion gas was conducted by a method according to FIG. However, in the aerobic oxidation apparatus 2, another synthetic wastewater was aerobically oxidized. That is, 5000m as aerobic oxidizer 2
1 of activated sludge aeration tank, 500 ml of washing bottle as the absorption device 3, the mixed liquid in the aerobic oxidation device 2 was fed as the washing liquid 14, and the continuous desulfurization test was conducted for about 10 days under the following conditions. ..
【００３９】消化ガスの組成：試験例１と同じ 洗浄液 ：混合液、ｐＨ７．５ 吸収条件 ：洗浄液流量；１００ｍｌ／ｍｉｎ、洗
浄液滞留時間（ＭＲＴ）；約５分、消化ガス流量；１５
０ｍｌ／ｍｉｎ、消化ガス空間速度（ＳＶ）；１８ｈｒ
-1 好気性酸化条件：被処理液；ＢＯＤ5約５０ｍｇ／ｌの
合成廃水、ｐＨ７．２、被処理液の流量；２０００ｍｌ
／日、アルカリの添加；水酸化ナトリウムをｐＨが７．
５になるように添加Composition of digestion gas: same as in Test Example 1 Cleaning solution: mixed solution, pH 7.5 Absorption condition: cleaning solution flow rate; 100 ml / min, cleaning solution retention time (MRT); about 5 minutes, digestion gas flow rate; 15
0 ml / min, digestive gas space velocity (SV); 18 hr
-1 Aerobic oxidation conditions: liquid to be treated; BOD 5 about 50 mg / l synthetic wastewater, pH 7.2, flow rate of liquid to be treated; 2000 ml
/ Day, addition of alkali; sodium hydroxide at pH 7.
Add to 5
【００４０】連続脱硫テストの期間中、朝と夕方の２
回、処理ガス中の硫化水素濃度などを測定した。約１０
日間にわたるテスト期間中、安定した脱硫が行われた。
結果は次の通りである。なお数値は各値とも平均値であ
る。 消化ガス中の硫化水素濃度：約５０００ｐｐｍ 処理ガス中の硫化水素濃度：２５０ｐｐｍ 硫化水素の除去率 ：約９５％ ＳＯ4 2-濃度 ：吸収された硫化水素の大部
分がＳＯ4 2-に酸化されたDuring the continuous desulfurization test, 2 in the morning and in the evening.
The concentration of hydrogen sulfide in the treated gas was measured. About 10
Stable desulfurization occurred during the day-long test period.
The results are as follows. The numerical values are average values. Hydrogen sulfide concentration in digested gas: about 5000ppm Hydrogen sulfide concentration in treated gas: 250ppm Hydrogen sulfide removal rate: about 95% SO 4 2- concentration: Most of absorbed hydrogen sulfide is oxidized to SO 4 2- Was
【００４１】比較例１ 吸収装置３として５００ｍｌの洗気ビン、洗浄液として
水道水を用い、下記条件で脱硫テストを行った。Comparative Example 1 A desulfurization test was conducted under the following conditions, using a 500 ml washing bottle as the absorber 3 and tap water as the washing liquid.
【００４２】消化ガスの組成：試験例１と同じ 洗浄液 ：水道水、ｐＨ約７ 吸収条件 ：洗浄液流量；０〜１５０ｍｌ／ｍｉ
ｎ、消化ガス流量；１００ｍｌ／ｍｉｎComposition of digestion gas: same as in Test Example 1 Cleaning solution: Tap water, pH about 7 Absorption condition: Flow rate of cleaning solution: 0 to 150 ml / mi
n, digestion gas flow rate; 100 ml / min
【００４３】吸収装置３に通液する洗浄液の流量を一定
に維持してから３０分後に、処理ガス中の硫化水素濃度
を測定した。その結果、洗浄液の流量をかなり大量にし
て消化ガスの流量と同程度にした場合は、硫化水素の除
去率は約８０％、洗浄液の流量がこれより少ない場合に
は約７５％程度であり、試験例１〜２に比べて硫化水素
の除去率は低かった。Thirty minutes after keeping the flow rate of the cleaning liquid flowing through the absorber 3 constant, the concentration of hydrogen sulfide in the treated gas was measured. As a result, when the flow rate of the cleaning liquid is made to be considerably large and made to be approximately the same as the flow rate of the digestion gas, the removal rate of hydrogen sulfide is about 80%, and when the flow rate of the cleaning liquid is less than this, it is about 75%. The removal rate of hydrogen sulfide was low as compared with Test Examples 1 and 2.
【００４４】[0044]
【発明の効果】本発明によれば、消化ガスを好気性酸化
の混合液または処理液と接触させて硫化水素を吸収さ
せ、これを好気性微生物酸化により酸化するようにした
ので、消化ガスを低コスト、かつ高脱硫率で脱硫でき、
これによりメタン含有率の高い処理ガスを得るととも
に、硫化水素を無害化して処理液とともに放流すること
ができる。According to the present invention, the digestive gas is brought into contact with the mixed solution or treatment solution for aerobic oxidation to absorb hydrogen sulfide, and this is oxidized by aerobic microbial oxidation. Desulfurization at low cost and high desulfurization rate,
This makes it possible to obtain a processing gas having a high methane content, detoxify hydrogen sulfide, and discharge it together with the processing liquid.
【図１】実施例の消化ガスの脱硫装置を示す系統図であ
る。FIG. 1 is a system diagram showing a digestion gas desulfurization apparatus of an example.
【図２】別の実施例の消化ガスの脱硫装置を示す系統図
である。FIG. 2 is a system diagram showing a digestion gas desulfurization device of another embodiment.
１ 嫌気性消化装置 ２ 好気性酸化装置 ３ 吸収装置 ４ バイオマス ５ 被処理物導入路 ６ 嫌気性消化液移送路 ７ ガス供給路 ８ 好気性酸化部 ９ 固液分離部 １０ 返送液路 １１ 散気管 １２ 給気路 １３ 処理液排出路 １４ 洗浄液 １５ 充填層 １６ ガス排出路 １７ 送液路 1 Anaerobic digester 2 Aerobic oxidizer 3 Absorber 4 Biomass 5 Material introduction passage 6 Anaerobic digestion liquid transfer passage 7 Gas supply passage 8 Aerobic oxidation portion 9 Solid-liquid separation portion 10 Return liquid passage 11 Air diffuser 12 Air supply passage 13 Treatment liquid discharge passage 14 Cleaning liquid 15 Packed bed 16 Gas discharge passage 17 Liquid supply passage
Claims (2)
生する消化ガスを、有機性物質の好気性微生物酸化にお
ける混合液または処理液からなる洗浄液と接触させて、
前記消化ガス中の硫化水素を前記洗浄液に吸収させる吸
収工程と、 前記吸収工程で得られた吸収液を好気性微生物酸化し
て、吸収された硫化水素を酸化する酸化工程とからなる
ことを特徴とする消化ガスの脱硫方法。1. A digestive gas generated by anaerobic microbial digestion of an organic substance is brought into contact with a cleaning liquid consisting of a mixed liquid or a treatment liquid for aerobic microbial oxidation of an organic substance,
An absorption step of absorbing hydrogen sulfide in the digestion gas into the cleaning liquid, and an oxidation step of oxidizing the absorbed hydrogen sulfide by oxidizing the absorption liquid obtained in the absorption step by aerobic microorganisms. And the method of desulfurizing digestive gas.
ガスを発生させる嫌気性消化施設と、 有機性物質を好気性微生物酸化して有機物を分解する好
気性酸化装置と、 前記嫌気性消化施設で発生する消化ガスを、前記好気性
酸化装置における混合液または処理液からなる洗浄液と
接触させて、前記消化ガス中の硫化水素を前記洗浄液に
吸収させる吸収装置と、 前記嫌気性消化施設から前記吸収装置に消化ガスを供給
するガス供給路と、 前記好気性酸化装置から前記吸収装置に混合液または処
理液を供給する送液路と、 前記吸収装置から前記好気性酸化装置に吸収液を返送す
る返送液路とを有することを特徴とする消化ガスの脱硫
装置。2. An anaerobic digestion facility that digests organic substances by anaerobic microorganisms to generate digestive gas, an aerobic oxidizer that decomposes organic substances by aerobic microbial oxidation of organic substances, and the anaerobic digestion. A digestion gas generated in the facility is brought into contact with a cleaning liquid composed of a mixed liquid or a treatment liquid in the aerobic oxidation device, and an absorption device for absorbing hydrogen sulfide in the digestive gas into the cleaning liquid, and from the anaerobic digestion facility. A gas supply path for supplying digestive gas to the absorption device, a liquid supply path for supplying a mixed solution or a treatment liquid from the aerobic oxidation device to the absorption device, and an absorption liquid from the absorption device to the aerobic oxidation device. A digestion gas desulfurization apparatus having a return liquid passage for returning the digestion gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23830891A JP3235131B2 (en) | 1991-09-18 | 1991-09-18 | Digestion gas desulfurization method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23830891A JP3235131B2 (en) | 1991-09-18 | 1991-09-18 | Digestion gas desulfurization method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0568849A true JPH0568849A (en) | 1993-03-23 |
| JP3235131B2 JP3235131B2 (en) | 2001-12-04 |
Family
ID=17028278
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP23830891A Expired - Lifetime JP3235131B2 (en) | 1991-09-18 | 1991-09-18 | Digestion gas desulfurization method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3235131B2 (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07996A (en) * | 1993-04-22 | 1995-01-06 | Ngk Insulators Ltd | Method for utilizing sludge digestion gas |
| JPH0824570A (en) * | 1994-07-22 | 1996-01-30 | Kurita Water Ind Ltd | Desulfurizing device for anaerobic biological reaction gas |
| JPH0839090A (en) * | 1994-08-03 | 1996-02-13 | Kurita Water Ind Ltd | Desulfurization equipment of anaerobic biological reaction gas |
| JPH10512801A (en) * | 1995-01-14 | 1998-12-08 | ニールス オレ ヴェステラーゲル | Biomass treatment method for removing heavy metals with hydrogen sulfide |
| JPH11262793A (en) * | 1998-03-18 | 1999-09-28 | National Institute Of Animal Industry | Post-treatment apparatus for anaerobic sewage treatment |
| JP2005255700A (en) * | 2004-03-09 | 2005-09-22 | Mitsui Eng & Shipbuild Co Ltd | Biogas purification method and biogas purification system |
| JP2007038188A (en) * | 2005-08-05 | 2007-02-15 | Kurita Water Ind Ltd | Method and apparatus for desulfurizing hydrogen sulfide-containing gas |
| JP2008208355A (en) * | 2007-01-30 | 2008-09-11 | Toshiba Corp | Apparatus for biodesulfurization of biogas |
| JP2012229382A (en) * | 2011-04-27 | 2012-11-22 | Mitsui Zosen Environment Engineering Corp | Apparatus for purifying biogas |
| US8366932B1 (en) * | 2008-10-08 | 2013-02-05 | Iowa State University Research Foundation, Inc. | Micro-aeration of sulfide removal from biogas |
-
1991
- 1991-09-18 JP JP23830891A patent/JP3235131B2/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07996A (en) * | 1993-04-22 | 1995-01-06 | Ngk Insulators Ltd | Method for utilizing sludge digestion gas |
| JPH0824570A (en) * | 1994-07-22 | 1996-01-30 | Kurita Water Ind Ltd | Desulfurizing device for anaerobic biological reaction gas |
| JPH0839090A (en) * | 1994-08-03 | 1996-02-13 | Kurita Water Ind Ltd | Desulfurization equipment of anaerobic biological reaction gas |
| JPH10512801A (en) * | 1995-01-14 | 1998-12-08 | ニールス オレ ヴェステラーゲル | Biomass treatment method for removing heavy metals with hydrogen sulfide |
| JPH11262793A (en) * | 1998-03-18 | 1999-09-28 | National Institute Of Animal Industry | Post-treatment apparatus for anaerobic sewage treatment |
| JP2005255700A (en) * | 2004-03-09 | 2005-09-22 | Mitsui Eng & Shipbuild Co Ltd | Biogas purification method and biogas purification system |
| JP2007038188A (en) * | 2005-08-05 | 2007-02-15 | Kurita Water Ind Ltd | Method and apparatus for desulfurizing hydrogen sulfide-containing gas |
| JP2008208355A (en) * | 2007-01-30 | 2008-09-11 | Toshiba Corp | Apparatus for biodesulfurization of biogas |
| US8366932B1 (en) * | 2008-10-08 | 2013-02-05 | Iowa State University Research Foundation, Inc. | Micro-aeration of sulfide removal from biogas |
| JP2012229382A (en) * | 2011-04-27 | 2012-11-22 | Mitsui Zosen Environment Engineering Corp | Apparatus for purifying biogas |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3235131B2 (en) | 2001-12-04 |
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