JPS62279895A - Control of redox potential in anaerobic treatment - Google Patents
Control of redox potential in anaerobic treatmentInfo
- Publication number
- JPS62279895A JPS62279895A JP61123433A JP12343386A JPS62279895A JP S62279895 A JPS62279895 A JP S62279895A JP 61123433 A JP61123433 A JP 61123433A JP 12343386 A JP12343386 A JP 12343386A JP S62279895 A JPS62279895 A JP S62279895A
- Authority
- JP
- Japan
- Prior art keywords
- reactor
- raw water
- liquid
- gas
- orp
- 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.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 239000002253 acid Substances 0.000 claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims description 19
- 239000002699 waste material Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 10
- 239000001301 oxygen Substances 0.000 abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 abstract description 10
- 239000002351 wastewater Substances 0.000 abstract description 8
- 238000004090 dissolution Methods 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 238000007664 blowing Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000000855 fermentation Methods 0.000 description 4
- 230000004151 fermentation Effects 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 150000007524 organic acids Chemical class 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 229920002261 Corn starch Polymers 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000008120 corn starch Substances 0.000 description 1
- 229940099112 cornstarch Drugs 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- -1 lower fatty acids Chemical class 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【発明の詳細な説明】
３、発明の詳細な説明
〔産業上の利用分野〕
本発明は、酸化還元電位の制御方法に関するものであり
、更に詳細には、酸生成リアクター処理といった嫌気性
生物処理において、酸化還元電位をコントロールするた
めの新規にして極めて有効な方法に関するものである。Detailed Description of the Invention 3. Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a method for controlling redox potential, and more specifically, to an anaerobic biological treatment such as acid production reactor treatment. relates to a novel and extremely effective method for controlling redox potential.
本発明によれば、極めて迅速且つ正確にバイオリアクタ
ー内部液の酸化還元電位を調整することができるので、
従来より処理することが困難であった食品工業廃水その
他の特に高濃度の有機性廃水のメタン生成を伴う嫌気性
処理が可能となるものである。According to the present invention, the redox potential of the bioreactor internal solution can be adjusted extremely quickly and accurately.
This makes it possible to perform anaerobic treatment involving methane production of food industry wastewater and other particularly high-concentration organic wastewater, which has been difficult to treat in the past.
したがって本発明は、農産製造、水畜産製造、発酵工業
、製糖工業等各種食品工業において排出される廃水はも
とより、濃尿処理下水、都市下水その他の各種有機性廃
水を処理する技術分野において重用されるものであって
、公害防止技術としても非常に有用なものである。また
更に１本発明によれば、効率よくメタンを得ることがで
きるので、メタン発酵といった嫌気性生物処理技術分野
においても重要なものである。Therefore, the present invention is of great use in the technical field of treating not only wastewater discharged from various food industries such as agricultural production, water and livestock production, fermentation industry, and sugar manufacturing industry, but also concentrated urine treated sewage, urban sewage, and other various organic wastewaters. This technology is extremely useful as a pollution prevention technology. Furthermore, according to the present invention, methane can be obtained efficiently, so it is also important in the field of anaerobic biological treatment technology such as methane fermentation.
嫌気性生物処理、例えばメタン発酵は、各種有機性廃液
といった複雑な化合物混合体を低級脂肪酸といった有機
酸のような簡単な化合物に分解する工程、及び、これら
有機酸をメタンと炭酸ガスに分解する工程から成るもの
である。Anaerobic biological treatment, such as methane fermentation, is a process that decomposes complex compound mixtures such as various organic waste liquids into simple compounds such as organic acids such as lower fatty acids, and decomposes these organic acids into methane and carbon dioxide gas. It consists of processes.
このような嫌気性生物処理技術における前者の工程、つ
まり処理対象となる有機物が低分子に分解される液化工
程（または、有機酸生成工程）においては、バイオリア
クター内部液の酸化還元電位のレベルによってこの工程
で作用する微生物の種類や、その産生ずる酵素活性が異
なってくる。In the former process of such anaerobic biological treatment technology, that is, the liquefaction process (or organic acid production process) in which the organic matter to be treated is decomposed into low molecules, the level of redox potential of the internal liquid of the bioreactor changes. The types of microorganisms that act in this process and the enzyme activities they produce vary.
従って、酸生成リアクターにおける酸化還元電位（以下
ｒＯＲＰＪ と略記することもある）を制御することが
処理効果に著しく影響する。Therefore, controlling the redox potential (hereinafter sometimes abbreviated as rORPJ) in the acid production reactor significantly affects the treatment effect.
しかしながら、現状では嫌気性処理工程においては、Ｏ
ＲＰについて留意されておらず、ましてや、工場レベル
でＯＲＰについて注意を払うだけでなくこれをコントロ
ールすることは、実用化はおろか考えられたこともない
。However, at present, in the anaerobic treatment process, O
No attention has been paid to RP, and it has never been thought of to not only pay attention to ORP but also control it at the factory level, let alone put it into practical use.
ただ、わずかに、研究所における実験レベルで。However, only at the experimental level in a laboratory.
第２図に示したシステムが極く小規模で試験のために用
いられているにすぎない。つまり、原水貯槽３１から原
水ポンプ３３を介して、原水を原水供給管３６から酸生
成リアクター３２に注入し、この中にブロワ−３４を用
いて空気及び／又は酸素を送気管３９を通して送気し、
ＯＲＰを単にプラス側に変える試みがなされているにす
ぎない。The system shown in Figure 2 has only been used for testing on a very small scale. That is, raw water is injected from the raw water storage tank 31 via the raw water pump 33 and into the acid production reactor 32 from the raw water supply pipe 36, and air and/or oxygen is supplied into the reactor 32 through the air supply pipe 39 using the blower 34. ,
Attempts are being made to simply change the ORP to the positive side.
なお、３５はＯＲＰメーターであって、リアクター３２
で処理された処理水ないし流出水は、リアクター３２の
処理水流出管３７から流出し、発生したガスはリアクタ
ーの排気管３８から外部へ排出ないしは集気タンクに集
めて適宜な用途に利用される。In addition, 35 is an ORP meter, and the reactor 32
The treated water or effluent water flows out from the treated water outflow pipe 37 of the reactor 32, and the generated gas is discharged to the outside from the exhaust pipe 38 of the reactor or collected in a collection tank and used for appropriate purposes. .
しかじかから、このような既知のシステムでは、酸生成
リアクターにおけるＯＲＰのデリケートなコントロール
は全く不可能であるし、もともと−上記したシステム自
体が工場用のシステムではなく、工場処理に適合した大
規模なＯＲＰコントロールは全く行われておらず、した
がって１本発明のように独特なシステムによってＯＲＰ
を自由自在にコントロールするという技術思想は、従来
未知の全く新規なものであるどころか、工場レベルで大
規模にしかもデリケートにＯＲＰをコントロールすると
いう技術課題自体が既に新規なものである。Indeed, with such known systems, delicate control of the ORP in acid-producing reactors is simply not possible, and originally - the above-mentioned system itself was not a factory system, but a large-scale system adapted for factory processing. Therefore, ORP control is not carried out at all, and therefore ORP control is not carried out at all by a unique system like the present invention.
The technical concept of freely controlling ORP is not only completely new and previously unknown, but the technical problem of controlling ORP on a large scale and delicately at the factory level itself is already new.
本発明は、上記したように従来技術が有する、特に次の
ような欠点を解決するためになされたものである。The present invention has been made in order to specifically solve the following drawbacks of the prior art as described above.
■従来の嫌気性リアクターは滞留時間が１０以Ｈもかか
り、応答速度がおそい。■Conventional anaerobic reactors require residence time of 10 hours or more and have slow response times.
■酸生成リアクターに直接空気（または酸素）を吹込む
と、槽内液のｍ気状態を部分的に不調にする。■Blowing air (or oxygen) directly into the acid production reactor will partially upset the atmospheric condition of the liquid in the tank.
■○ＲＰレベルを目的とする所定値に制御することがで
きない。■○The RP level cannot be controlled to a desired predetermined value.
■従来システムではＯＲＰレベルを晒にプラス側へもっ
ていくといった程度のいわば定性的ともいうべき○ＲＰ
コントロール（しかも実験室規模でのコントロール）し
かできず、工場レベルでの大規模且つ微妙な省エネルギ
ー的コントロールは全く不可能である。■In the conventional system, ○RP can be called qualitative, such as bringing the ORP level to the positive side.
Control (moreover, control on a laboratory scale) is possible only, and large-scale and delicate energy-saving control on a factory level is completely impossible.
本発明は、上記欠点を一挙に解決して、大規模リアクタ
ーにおいて極めて迅速且つ正確に酸化還元電位を調整す
る新規な省エネルギー的低コスト化方法を完成するため
になされたものであって、活性汚泥を中心とする微生物
学、流体の行動、固液分離、気液分離、汚水処理槽、バ
イオリアクター等、生物、物理、化学といった各方面か
ら広く且つ鋭意研究した結果、遂に完成されたものであ
る。The present invention has been made in order to solve the above-mentioned drawbacks at once and complete a new energy-saving and cost-reducing method for adjusting the redox potential extremely quickly and accurately in a large-scale reactor. It was finally completed as a result of extensive and intensive research from various fields such as biology, physics, and chemistry, including microbiology, fluid behavior, solid-liquid separation, gas-liquid separation, sewage treatment tanks, and bioreactors. .
以下、本発明を図面を参照しながら詳細に説明する。Hereinafter, the present invention will be explained in detail with reference to the drawings.
原水貯槽１に貯えた原廃水は、原水ポンプ５により原水
注入配管工０を介して酸生成リアクター３へ送入するの
であるが、この原液をそのままリアクター３へ搬送し、
リアクター３内へ空気を直接送入したのでは所期の目的
は達成されない。The raw wastewater stored in the raw water storage tank 1 is sent to the acid production reactor 3 by the raw water pump 5 via the raw water injection plumber 0, and this raw solution is transported to the reactor 3 as it is,
Directly introducing air into the reactor 3 would not achieve the intended purpose.
その前に、次のようにしてＯＲＰのコントロールを実施
しなければならない。つまり、先ず、酸生成リアクター
３から流出水（処理水）ないしリアクター内部液を取り
出し、原水ポンプ５の吸込側管に返送ないし循環せしめ
る。流出水（処理水）ないし内部液の返送ないし循環量
は、リアクター３に供給する廃水の約１／２量〜５０倍
量程度とするのが良く、特に、処理水や原液の種類、濃
度、○ＲＰレベル等にしたがって適量を選択するのが好
ましく、一般的には、処理水（内部液）を原液と等量な
いしその３０倍量程度使用するのが好適である。Before that, the ORP control must be performed as follows. That is, first, the effluent water (treated water) or the reactor internal liquid is taken out from the acid production reactor 3 and returned or circulated to the suction side pipe of the raw water pump 5. The amount of return or circulation of the effluent water (treated water) or internal liquid is preferably about 1/2 to 50 times the amount of wastewater supplied to the reactor 3, and in particular, the type, concentration, It is preferable to select an appropriate amount according to the RP level, etc. Generally, it is preferable to use the treated water (internal liquid) in an amount equal to or 30 times the amount of the original solution.
このようにして流出水（処理水）ないし内部液を、上記
した特定量だけ、原水ポンプの吸込側配管に返送ないし
循環せしめつつ、供給原水と混合せしめしかもその間に
空気及び／又は酸素を強制的に吸込み、これを更に加圧
して、ＯＲＰコントロールを行う。例えばこの操作は次
のようにして行う。つまり、原水ポンプ５の吐出側から
吸込側配管に原水循環用配管９を設けるとともに、この
リサイクル配管９に空気（又は酸素）を吹込ませるため
のインジェクタ装置７を設け、更にポンプ５の下流に加
圧槽２を設けて、ＯＲＰコントロールを行う。先ず、リ
アクター３から引抜いてきた流出水ないし内部液は、原
水ポンプの吸込側配管に上記した特定量を返送ないし循
環させ、これを原水貯槽１からの原水と混合し、その一
部ないし全部をリサイクル管９に流入せしめる。そこで
、インジェクター７から強制吹込みされた酸素（又は空
気）によって原水中に酸素を混入溶解せしめる。吹込む
気体は、酸素及び／又は空気であるが、窒素やアルゴン
、キセノンガスといった各種不活性ガスと酸素の混合気
体も適宜使用できる。このようにして得られた気液混合
液は、原水ポンプ５の吐出側配管の先端部分に設けた加
圧タンク２に送入し、加圧することによって気体の溶解
度を向上させ、これを原水圧入配管１０によってリアク
ター３に圧入し、この酸生成リアクター３に設けたＯＲ
Ｐメータ８のレベルに合わせて吸込気体量を調整し、も
って、酸生成リアクター３のＯＲＰを正確且つ迅速にコ
ントロールするのである。なお１１は、加圧タンク２か
らの圧力を除去したりそのコントロールを行ったりする
ための加圧槽排気管である。In this way, the specified amount of the effluent water (treated water) or internal liquid is returned or circulated to the suction side piping of the raw water pump, while being mixed with the supplied raw water. This is then further pressurized and ORP control is performed. For example, this operation is performed as follows. In other words, a raw water circulation pipe 9 is provided from the discharge side of the raw water pump 5 to the suction side pipe, and an injector device 7 is provided for blowing air (or oxygen) into the recycling pipe 9. A pressure tank 2 is provided to perform ORP control. First, the effluent water or internal liquid drawn from the reactor 3 is returned or circulated in the above-mentioned specific amount to the suction side piping of the raw water pump, mixed with the raw water from the raw water storage tank 1, and part or all of it is It is made to flow into the recycling pipe 9. Therefore, oxygen (or air) forcedly blown in from the injector 7 is used to mix and dissolve oxygen into the raw water. The gas to be blown in is oxygen and/or air, but a mixed gas of oxygen and various inert gases such as nitrogen, argon, and xenon gas can also be used as appropriate. The gas-liquid mixture obtained in this way is sent to the pressurized tank 2 installed at the tip of the discharge side piping of the raw water pump 5, and pressurized to improve the solubility of the gas. It is press-fitted into the reactor 3 through the piping 10, and the OR provided in this acid generation reactor 3 is
The amount of suction gas is adjusted according to the level of the P meter 8, thereby accurately and quickly controlling the ORP of the acid production reactor 3. Note that 11 is a pressurized tank exhaust pipe for removing and controlling the pressure from the pressurized tank 2.
このようにして混合液は、一定のＯＲＰ条件下で、リア
クター３内で迅速且つ効率よく処理されてリアクター流
入管１２から流出し、レシーバ−タンク４を介して処理
水流出管１３から流出する。In this way, the mixed liquid is quickly and efficiently treated in the reactor 3 under constant ORP conditions, flows out from the reactor inlet pipe 12, and flows out from the treated water outflow pipe 13 via the receiver tank 4.
この流出液は、更にメタン発酵に使用したり、直ちに河
川に放流したり、工業用水として各種用途に利用できる
ほか、循環水ポンプ６を介して循環水配管１６を通り原
水ポンプ５の上流側に送って、前記した返送ないし循環
液として使用することができる。また、この返送ないし
＃Ｉ環液としては。This effluent can be further used for methane fermentation, immediately discharged into a river, or used for various purposes as industrial water, or can be passed through the circulating water pipe 16 via the circulating water pump 6 to the upstream side of the raw water pump 5. It can be sent and used as the above-mentioned return or circulation fluid. Also, as this return or #I reflux liquid.
処理水、流出液のほかにリアクター内部液も適宜使用で
きるし、これらの混合液も自由に使用できる。なお、１
５はレシーバ−排気管を示し、これらは１図示したよう
にリアクター排気管１４と連結してもよいし、連結する
ことなく独立させておいてもよい。In addition to treated water and effluent, reactor internal liquid can also be used as appropriate, and mixtures thereof can also be used freely. In addition, 1
Reference numeral 5 indicates a receiver exhaust pipe, and these may be connected to the reactor exhaust pipe 14 as shown in Figure 1, or may be left independent without being connected.
次に本発明の実施例について述べる。Next, examples of the present invention will be described.
実施例
第１図に示した酸生成リアクターのＯＲＰコントロール
システムを用い、上水１ａ当りコーンステイープリカー
３０ｇを溶解した原液を次のようにして処理した。EXAMPLE Using the ORP control system of the acid production reactor shown in FIG. 1, a stock solution in which 30 g of cornstarch liquor was dissolved per 1 a of tap water was treated as follows.
実容積５Ｑの酸生成リアクターを使用し、リアクターの
運転水温は３０℃に維持した。処理水返送率を原液の１
５倍量に設定し、加圧タンクにおいて、水柱５０嗣の圧
力下で、空気をインジェクタ装置によって吸込ませて原
液の処理を行った。An acid production reactor with an actual volume of 5Q was used, and the operating water temperature of the reactor was maintained at 30°C. The treated water return rate is 1
The undiluted solution was treated in a pressurized tank under a pressure of 50 water columns by inhaling air with an injector device.
空気の吹込量を１０＋ｗｆｌ／ｗｉｎと２ Ｑ ｍｆｆ
／ｗｉｎとにセットして原液を処理し、それぞれ次表の
ようなＯＲＰコントロール結果を得た。Air blowing amount is 10+wfl/win and 2 Q mff
/win and processed the stock solutions, and obtained ORP control results as shown in the following table.
表
ＴＯＣ負荷量１０ｋｇ／ｍコ／日 ＴＯＣ負荷量２０ｋ
ｇ／ｍコ／日空気吹込１０ｍＡ／ｌ１ｌｉｎ Ｏ
ＩＩＰ−３２０ｍＶ ＯＲＰ−４３０ｍＶ空
気吹込２０ｍＱ／ｗｉｎ
ＯＲＰ−３３０ｍＶ以上の結果から明らかなように、有
機物負荷量、空気吹込量に対してＯＲＰのレベルに比例
関係が認められ、有機物負荷量が一定の場合、供給する
気体量を調節することによってリアクター内部液のＯＲ
Ｐレベルを正確且つデリケートに制御することが可能で
あることがわかる。Table TOC load amount 10kg/m/day TOC load amount 20k
g/m/day Air blowing 10mA/l1lin O
IIP-320mV ORP-430mV air blowing 20mQ/win
As is clear from the results of ORP -330mV or higher, there is a proportional relationship between the ORP level and the amount of organic matter loading and the amount of air blown.When the amount of organic matter loading is constant, the reactor can be adjusted by adjusting the amount of gas supplied. OR of internal liquid
It can be seen that it is possible to accurately and delicately control the P level.
（効 果）
本発明は、前記したように、酸生成リアクター流出水（
処木理）またはリアクター内部液をリアクターに供給す
る廃水と等量ないし３０倍量程度を原水ポンプの吸込側
配管に返送循環させ、原水ポンプ吐出側から吸込側配管
にリサイクル配管を設け、このリサイクル配管に空気（
または酸素）を吸込ませるためのインジェクター装置を
設け、原水ポンプの吐出側配管の先端に加圧タンクを設
け、気液混合液を加圧することによって気体の溶解度を
向上させ、酸生成リアクターに設けたＯＲＰメーターの
レベルに連動させて、吸込気体量を調整し、もってＯＲ
Ｐをコントロールするものである。(Effects) As described above, the present invention provides acid production reactor effluent water (
The same amount to 30 times the amount of waste water supplied to the reactor is returned and circulated to the suction side piping of the raw water pump, and a recycling piping is installed from the raw water pump discharge side to the suction side piping, and this recycling is carried out. Air in the piping (
An injector device was installed to inhale oxygen (or oxygen), and a pressurized tank was installed at the tip of the discharge side piping of the raw water pump to improve the solubility of the gas by pressurizing the gas-liquid mixture. The amount of suction gas is adjusted in conjunction with the level of the ORP meter, resulting in OR
It controls P.
したがって、本発明によれば、このような新規にして独
特な構成を採ることにより、工場レベルでの大規模なリ
アクター内のＯＲＰコントロールがはじめて可能となっ
たのである。Therefore, according to the present invention, by adopting such a new and unique configuration, ORP control within a large-scale reactor at the factory level has become possible for the first time.
そのうえ１本発明はによれば１次のように、囃に大規模
ＯＲＰコントロールができるだけでなく。Moreover, according to the present invention, large-scale ORP control is not only possible in the first order.
極めて迅速にしかも極めて正確にデリケートなＯＲＰコ
ントロールがきわめて省エネルギー的にできるという著
効も併せ得られるのである。It also has the remarkable effect of being able to perform delicate ORP control extremely quickly, extremely accurately, and in an extremely energy-saving manner.
■ 酸生成リアクターに流入させる水量を増大させるこ
とによってリアクターにおける滞留時間を短縮して応答
速度を早くシ。■ By increasing the amount of water flowing into the acid production reactor, the residence time in the reactor is shortened and the response speed is increased.
■ インジェクター装置によって気体を吸込ませ、加圧
タンクで加圧することによりブローワ等の動力設備を附
加することなく省エネルギー的に気体の溶解効果を向上
させ。■ By inhaling gas with an injector device and pressurizing it with a pressurized tank, the gas dissolution effect is improved in an energy-saving manner without adding power equipment such as a blower.
■ リアクターに設置したＯＲＰメーターと吸込気体量
を連動させることによってＯＲＰレベルを正確に制御す
ることができる。（これはリアクターに供給する有機物
量と混合液に溶解する気体量とリアクターの○ＲＰレベ
ルがある範囲に比例関係にあるからである。）■ The ORP level can be accurately controlled by linking the intake gas amount with the ORP meter installed in the reactor. (This is because there is a proportional relationship between the amount of organic matter supplied to the reactor, the amount of gas dissolved in the mixed liquid, and the RP level of the reactor within a certain range.)
第１図は本発明に係る酸生成リアクターのＯＲＰコント
ロールシステムの１実施例を図示したものであり、第２
図は従来システムを図示したものである。
１．３１・・・原水貯槽、 ２・・・加圧槽、３
．３２・・・酸生成リアクター１５・・・原水ポンプ。
７・・・インジェクタ装置、 ９・・・原水循環用配
管、１６・・・循環水配管、３４・・・ブロワ−０代理
人 弁理士 戸 １）親 男
第 １ 図
七FIG. 1 illustrates one embodiment of the ORP control system for an acid production reactor according to the present invention, and FIG.
The figure illustrates a conventional system. 1.31... Raw water storage tank, 2... Pressurized tank, 3
．． 32...Acid production reactor 15...Raw water pump. 7... Injector device, 9... Piping for raw water circulation, 16... Circulating water piping, 34... Blower-0 agent Patent attorney door 1) Parent Male No. 1 Figure 7
Claims (1)
ら処理されて流出してくる処理水を、該リアクターに供
給する廃液量の１／２量ないし５０倍量だけ原水ポンプ
の吸込側配管に返送ないし循環させつつ、供給原液と合
して、混合せしめ、しかもその間に空気及び／又は酸素
を強制的に吹込み、次いでこのようにして得られた気液
混合液を加圧して気体の溶解度を向上させること、を特
徴とする嫌気処理における酸化還元電位の制御方法。The internal liquid of the acid production reactor and/or the treated water that flows out from the acid production reactor is returned or circulated to the suction side piping of the raw water pump in an amount of 1/2 to 50 times the amount of waste liquid supplied to the reactor. The gas-liquid mixture thus obtained is then pressurized to improve the solubility of the gas. A method for controlling redox potential in anaerobic treatment, characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61123433A JPS62279895A (en) | 1986-05-30 | 1986-05-30 | Control of redox potential in anaerobic treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61123433A JPS62279895A (en) | 1986-05-30 | 1986-05-30 | Control of redox potential in anaerobic treatment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62279895A true JPS62279895A (en) | 1987-12-04 |
Family
ID=14860450
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61123433A Pending JPS62279895A (en) | 1986-05-30 | 1986-05-30 | Control of redox potential in anaerobic treatment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62279895A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1015595A (en) * | 1996-07-08 | 1998-01-20 | Mitsubishi Heavy Ind Ltd | Treatment of waste water |
| JP2014000550A (en) * | 2012-06-20 | 2014-01-09 | Sumitomo Heavy Industries Environment Co Ltd | Methane fermentation system and methane fermentation method |
-
1986
- 1986-05-30 JP JP61123433A patent/JPS62279895A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1015595A (en) * | 1996-07-08 | 1998-01-20 | Mitsubishi Heavy Ind Ltd | Treatment of waste water |
| JP2014000550A (en) * | 2012-06-20 | 2014-01-09 | Sumitomo Heavy Industries Environment Co Ltd | Methane fermentation system and methane fermentation method |
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