WO2004080903A1 - Non-sludge high-speed waste water treatment system - Google Patents

Abstract

It is intended to provide a non-sludge high-speed wastewater treatment system equipped with a means of culturing a strong oxidative digestion bacterium, a means of supplying oxygen at a high concentration and a means of solid/liquid separation. The above-described means of supplying oxygen at a high concentration may have a means of supplying oxygen and a means of generating fine bubbles. By the above-described means of generating fine bubbles, bubbles having a diameter not more than about 3 μm may be generated. The above-described means of solid/liquid separation may comprise a porous membrane. In a preferred case, the above-described strong oxidative digestion bacterium may comprise a bacillus which shows a growth speed expressed in generation time in a complete medium at 30°C or 30 minutes or below and belongs to the genus Bacillus. Alternatively, above-described strong oxidative digestion bacterium may be a PVA-digesting bacterium belonging to the genus Pseudomonas or Acinetobacter. It is also intended to provide a non-sludge high-speed wastewater treatment system which is further equipped with a means of removing oil, a means of removing nitrogen, a means of removing heavy metals and a means of sterilization and deodorization.

Description

 TECHNICAL FIELD The present invention relates to the field of wastewater treatment. More specifically, the present invention relates to a non-sludge high-speed wastewater treatment system using a strong oxidative degradation bacteria culture means, a high-concentration oxygen supply means, and a solid-liquid separation means. BACKGROUND ART Biological treatment is the most widely used technique for treating organic wastewater. Biological treatment methods include aerobic treatment such as activated sludge method, biofilm method and stabilization pond method, and anaerobic treatment. Its history dates back to the end of the 19th century (Eiichi Mikami, biological treatment in water treatment technology, water and wastewater, 27 (10) 11 (19985)).

Activated sludge is a continuous process in which floc-like biological growth (activated sludge) is mixed with wastewater, aerated, and then separated from the wastewater by sedimentation. Fig. 1 (a) shows a typical process flow of the conventional activated sludge method. This is a process called the standard activated sludge method. Wastewater (raw water) 1 is first introduced into the adjustment tank 3. Activated sludge is sensitive to fluctuations in pH, load fluctuations, and sudden influxes and leaks of toxic substances.Therefore, it is necessary to adjust activated sludge according to the properties of raw water so as not to adversely affect activated sludge. is there. Next, if necessary, the raw water introduced into the neutralization tank 5 is introduced into the aeration tank (activated sludge tank) 7 and mixed with the returned sludge 11 at the inflow end of the aeration tank. Then, the mixture of wastewater and activated sludge passes through the aeration tank. Organic substances are gradually removed through this process. The activated sludge that has passed through the aeration tank It is introduced into the bath tank 9, separated from the treated water 21 by settling, and returned to the aeration tank. Activated sludge decomposes organic matter in the influent wastewater in the presence of oxygen, releases carbon dioxide and proliferates the activated sludge.

 In the conventional activated sludge method, i) a large amount of sludge is generated, and high sludge treatment cost is required for the treatment; ii) high running cost; iii) long treatment time; i V) technology for operation management V) Sludge treatment facilities require high investment, etc. The present invention solves the above-mentioned problems of the conventional activated sludge method, i) no sludge is generated (no sludge treatment cost is required); ii) drastically reduced running cost (conventional 110); iii) high-speed treatment (Conventional 1Z10); iv) Easy operation (semi-unmanned); V) Objective to provide a system that can use existing equipment as it is. DISCLOSURE OF THE INVENTION The present invention relates to a non-sludge high-speed wastewater treatment system, which can include a means for culturing strong oxidatively decomposing bacteria, a means for providing high-concentration oxygen, and a solid-liquid separation means. The system may further comprise a strong oxidatively degrading bacterium. The non-sludge high-speed wastewater treatment system may further include an oil removal means for pretreatment of wastewater, if necessary. Further, the non-sludge high-speed wastewater treatment system may further include a nitrogen removing means as needed. Further, the non-sludge high-speed drainage treatment system may further include a heavy metal removing means as required. Further, the non-sludge high-speed wastewater treatment system may further include a sterilizing means as required. The non-sludge high-speed wastewater treatment system may further include a deodorizing and removing means as needed.

Preferably, the high-concentration oxygen providing means includes: an oxygen providing means; and fine bubble generation. Means may be provided.

 Preferably, the microbubble generating means removes bubbles having a diameter of about 5 / cm2, about 3 mm, about lm, about 0.5 m, about 0.2, about 0.1 xm, more preferably no more than about 3. Can occur.

 Preferably, the solid-liquid separation means may be a porous membrane.

 Preferably, the porous membrane can be a metal membrane or a ultrafiltration membrane.

 Preferably, the metal film can be manufactured by spraying stainless metal particles onto a stainless steel wire net and then sintering.

 Preferably, the ultrafiltration membrane may be tubular. Preferably, the ultrafiltration membrane is a hollow fiber membrane. Also, preferably, the hollow fiber membrane has a pore size of 0.01 m to 0.5 m in diameter. The ultrafiltration membrane is capable of permeating solvents, metal ions, etc. without applying pressure to the wastewater to be treated and bringing the wastewater into contact with the membrane, without allowing microorganisms and the like in the wastewater to permeate through the membrane. The material of the ultrafiltration membrane is, for example, but not limited to, polysulfone and polyvinyl alcohol. When a hollow fiber membrane is used, by applying pressure to the wastewater and letting it pass through the inside of the hollow fiber, it is possible to permeate a solvent, metal ions, and the like through the membrane without allowing microorganisms and the like in the wastewater to pass through the membrane. The treated wastewater can be circulated inside the hollow fiber and concentrated.

 Preferably, the porous membrane may have a pore size of about 0.2 im in diameter. Preferably, the strongly oxidatively degrading bacterium is a bacillus that shows a growth rate of 30 minutes or less at 30 ° C. in a complete medium and that degrades oils and fats under aerobic conditions. obtain.

 Preferably, the bacillus is capable of producing a fat / oil decomposition promoting substance selected from the group consisting of protease, cellulase, amylase, lipase, and biological surfactant.

 Preferably, the bacilli can produce a biological surfactant.

Preferably, the bacilli are capable of producing amylase and lipase. Preferably, the bacilli are capable of producing cellulase.

 Preferably, the bacilli are capable of producing protease and amylase.

 Preferably, the bacillus may be Bacillus subtilis FERM BP-7270.

 Preferably, the bacillus is Bacillus. Subtilis FERM BP-7271.

 Preferably, the strongly oxidatively degrading bacterium may include a polypinyl alcohol degrading bacterium. Preferably, the polyvinyl alcohol-degrading bacterium may be Pseudomonas strain FERM P-19204.

 Preferably, the polyvinyl alcohol-degrading bacterium is an Acinetobacter IAM

—May be 3 strains.

 Preferably, the polyvinyl alcohol-degrading bacterium may be Acinetopaque yuichi IAM-4 strain.

 The present invention also relates to a non-sludge high-speed wastewater treatment system comprising a decomposition reaction tank, high-concentration oxygen providing means, and solid-liquid separation means.

 The high-concentration oxygen providing means and the solid-liquid separation means may be combined to increase the concentration of microorganisms in the decomposition reaction vessel to at least 10, OO Opm. The high-concentration oxygen providing means can convect the liquid in the decomposition reaction tank.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a diagram showing an example of the system of the present invention in comparison with a conventional technology. (a) shows the prior art, and (b) shows the system of the present invention.

 FIG. 2 is a diagram showing an example of the system of the present invention.

FIG. 3 is a diagram showing an example of the high-concentration oxygen providing means used in the system of the present invention. FIG. 4 is a diagram showing an example of the system of the present invention.

 FIG. 5 is a diagram showing operation results of the system of the present invention.

 FIG. 6 is an electron micrograph of an example of bacteria used in the system of the present invention. FIG. 7 is a diagram showing an operation result of the system of the present invention.

 FIG. 8 is a diagram showing an example of the system of the present invention.

 FIG. 9 is a diagram showing the results of comparing the bactericidal activity of Cu-type zeolite and Ag-type zeolite.

 FIG. 10 is a diagram showing the results of comparing the bactericidal activity of Cu-type zeolite and Ag-type zeolite.

 Figure 11 shows the results of comparing the bactericidal activity of Cu-type zeolites and Ag-type zeolites against bacteria in seawater.

 The reference numbers in the drawings are as follows:

 1 drainage

 1 'Inflow tank

 3, 3 'adjustment tank

 5 Neutralization tank

 7 Aeration tank

 9 Settling tank

 11 Return sludge

 17, 17 ', 18 Decomposition reaction tank

 19 Microbial separation tank

 21 Treated water

 22 'Outflow tank-

23 Metal film

 23 'solid-liquid separation means

25 Air conditioning system 25 Air diffuser

 27 Intake device

 33 Aerator

 35 Ultra-fine bubble generator

 36 Oxygen generator

 37 of intake system

 43 Enricher Tank

 51 Treated water

 61 Primary treated water

 71 Treated water

 81 Pretreatment water light

 11 5 Exterior

 1 1 6 Air diffuser

 11 7, 118 projection

 12 1 Gas-liquid mixing cylinder

 13 1 Oil removal means

 13 2 Nitrogen removal means

 13 3 Means for removing heavy metals

 13 4 Sterilization and deodorization removal means

Hereinafter, the present invention will be described. Throughout this specification, singular forms of the article (e.g., "a", "an", "the" for English, "ein", "der", "das", "die" for German "Un" in Spanish, "un" in Spanish, "une", "1e", "1a", etc. It should be understood that corresponding articles and adjectives in other languages, such as "una", "e1", and "1a", also include the concept of the plural unless otherwise stated. . It is to be understood that the terms used in the present specification are used in a meaning commonly used in the art unless otherwise specified.

 (Definition of terms)

 As used herein, the term “strongly oxidatively degrading bacteria” refers to a group of useful microorganisms, such as hard-to-degrade COD-utilizing bacteria, and is generally a genus Bacillus (Ba ci 11 us), Pseudomonas (Pseudomonas). Includes bacteria belonging to the genera, genus Acinetha, genus Acinet ob acter, and genus Arthr ob acter. Strongly oxidatively degrading bacteria generally have the ability to strongly oxidize organic matter, thereby achieving zero excess sludge generation. Examples of strong oxidatively degrading bacteria include Bacillus subtilis FERM P-17512 and Bacillus subtilis FERM P-17513, which are lipolytic bacilli described in JP-A-2001-61468 by the present inventors. (Each deposited on August 11, 1999 at the National Institute of Bioscience and Human-Technology, National Institute of Advanced Industrial Science and Technology (currently, the Institute of Advanced Industrial Science and Technology, Patent Organism Depositary, Yuichi), and on August 10, 2000, Bacillus subtilis FERM P-17512 is a Gram-stained, rod-shaped bacterium with unstable Gram-stainability, and the stained cells are transferred to a deposit under the Budapest Treaty. Easily bleached. This bacterium was positive for catalase and oxidase.

Further, as another example of the “strong oxidatively degrading bacterium”, a polyoxylated bacterium described in the co-pending application entitled “New polypinyl alcohol-degrading bacterium” filed on the same date as the present inventors Biel alcohol (hereinafter PVA) degrading bacteria. For reference, these patent documents are incorporated herein in their entirety. Representative examples of this PVA-degrading bacterium include Pseudomonas FERM P-19204 strain, Acinetobacter IAM-3 strain, and IAM-4 strain. Pseudomonas FERM P— The 19204 strain was deposited with the National Institute of Advanced Industrial Science and Technology Patent Organism Depositary on February 7, 2003. The Acipetopactor I AM-3 and IAM-4 strains are stored at the Graduate School of Engineering, Kyoto University (Yoshida-Honmachi, Sakyo-ku, Kyoto-shi) and sold on request.

In addition, any bacteria isolated according to the methods described in these patent documents can be used as strong oxidative decomposers. The above bacterium can be modified using a mutation treatment, acclimatization, genetic engineering technique and the like well known to those skilled in the art, and used as a strongly oxidatively degrading bacterium. For example, in the case of using the PVA decomposing bacteria, the hardly decomposable substance typified by PVA, the capacitive load ^{0. 1~0. 8 k gZm 3} · day, capable of decomposing under C OD removal rate 90% or more .

 As used herein, unless otherwise specified, the term “oil / fat” refers to an n-hexane extractable substance measured according to the gravimetric method described in Table 4 of the Notification of the Environment Agency No. 64. As used herein, the term “generation time” refers to the average time required from one cell division to the next, ie, the average time required for doubling the number of cells (doubling time). A growth rate that is less than or equal to 30 minutes is a term well known to those skilled in the art, and can be rephrased as having a specific growth rate of at least 1.38 Z hours. The “specific growth rate”, which indicates the growth rate of microorganisms, is obtained by measuring the absorbance at 660 nm (OD660) of the culture over time and plotting it on a semilogarithmic graph. Calculated as β [1Z time]. Generation time 1: (doubling time) is calculated from the obtained specific growth rate according to the formula: = 1 η 2 Ζ = 0.693 n.

 As used herein, the terms "protease", "cellulase", "amylase", and "lipase" are generally used in the meanings used in the art, and they are used for proteolytic enzyme, fibrinolytic enzyme, Starch hydrolase and lipolytic enzyme are collectively referred to, and their activities can be measured by methods known in the art.

The term "biological surfactant (biosurfactant)" as used herein refers to a surfactant produced by a living organism, and particularly a surfactant produced by a microorganism outside a cell. Refers to quality. In general, biological surfactants have a hydrophilic site and a hydrophobic site in the molecule, and a typical example is a glycolipid in which a hydrophilic sugar and a hydrophobic fatty acid are bonded. Not limited.

 The “high-concentration oxygen providing means” used in the present invention may typically include an oxygen providing means and a microbubble generating means.

 The high oxygen supply means provides a strong air (oxygen) supply to cultivate strong oxidatively degrading bacteria at a high concentration and maintain the complete oxidative decomposition activity of organic matter. This high-concentration oxygen supply means prevents the decomposition activity of the strongly degrading bacteria present in the aeration tank at a high concentration from being limited by oxygen supply. Typically, the microbubble generating means can generate microbubbles (ultrafine bubbles) having a diameter () of less than about 3 m. Examples of the fine bubble generating means include, for example, an ultra-fine bubble generating device (Suzuki Sangyo Co., Ltd., 5-6, Yamadanakayoshimi-cho, Nishikyo-ku, Kyoto-shi), and JP-A No. 2001-3114888 A diffuser can be used. For example, the air diffusion device described in Japanese Patent Application Laid-Open No. 2001-3140888 has a bell-shaped gas-liquid mixing cylinder, in which a plurality of protrusions are arranged. I have. The effect of the projections is that, when the liquid containing the bubbles hits the projections, the bubbles are broken into small pieces and the gas and the liquid are mixed. As the bubbles become smaller, the contact area between the gas and the liquid surface increases. This makes it easier for oxygen in the air to dissolve in the water. An air discharge nozzle is provided below the gas-liquid mixing cylinder, and the air discharge nozzle is connected to an air supply pipe. The air discharge nozzle is disposed obliquely upward and slightly inward from the tangential direction of the gas-liquid mixing cylinder. When the air is discharged from the air discharge nozzle, the air rises obliquely upward along the inner wall of the gas-liquid mixing cylinder. Along with this, a water flow is generated in the gas-liquid mixing cylinder. The water flow generated in the gas-liquid mixing cylinder rises spirally along the inner wall of the gas-liquid mixing cylinder.

When a spiral water flow is generated in this gas-liquid mixing cylinder, the flow velocity in the upper part is higher than that in the lower part. This generates a vortex water flow in the air diffuser Then, the water near the lower opening of the gas-liquid mixing cylinder is sucked up, discharged from the upper part of the gas-liquid mixing cylinder, and can generate a swirling flow. Since the external shape of the air diffuser is bell-shaped, the vortex is enhanced by the tornado effect, and a large angular momentum can be obtained. Then, the super-high-speed spiral flow collides strongly with the hemispherical projection, generating fine bubbles and improving the air diffusion efficiency. As a result, an ultra-high-speed spiral flow is generated, which collides with the projections arranged in the upper part (upper hemisphere) and emits fine bubbles. Thus, a vortex containing a large amount of dissolved oxygen and having high aeration efficiency can be convected in the aerobic reaction tank.

 An ultra-fine bubble is a bubble having a diameter of 0.1 / m to 3 and smaller than a fine bubble (diameter of 10 to 100 m). The ultrafine bubbles have small buoyancy due to their small diameter, so they are likely to get on the swirling water stream and get caught in the downward flow in the processing tank, and thus stay in the processing tank and stay in the processing tank. Is uniformly diffused. As a result, the microbubbles are not dissolved in the water, but rather are dispersed and float in the water, and can exist in the water at a concentration equivalent to 180 to 200 ppm.

The means for generating microbubbles may be connected to the means for providing oxygen, thereby providing a more enriched oxygen environment. High-concentration oxygen supply means equipped with microbubble generation means and oxygen supply means can dissolve oxygen of about 93% purity at a concentration of 180 ppm, and inject oxygen into bubbles of about 3 m in diameter As a result, a BOD treatment capacity about 10 times that of the conventional activated sludge method is possible. For example, a standard activated sludge BOD volume load of 0.5-1.5 kg / m ² · day can be increased to about 5 kg / m ² · day.

The solid-liquid separation means enables wastewater treatment by microorganisms with a high concentration exceeding about 13, OOO ppm by solid-liquid separation. As the solid-liquid separation means, a microfiltration membrane, an ultrafiltration membrane, a reverse osmosis membrane, or the like can be used. Typically, a metal membrane is used as a solid-liquid separation means, and is produced by, for example, spraying stainless metal particles on a stainless steel wire mesh and sintering. This solid-liquid separation metal membrane has physical strength not found in resin membrane, It can be used even under severe conditions. In summary, ① heat resistance is high, steam sterilization at 121 ° C is possible; ② chemical resistance is high, washing with strong alkaline and strong acid is possible; ③ handling of organic solvents is possible;大 き く High mechanical strength and can handle highly viscous fluids; ⑤The membrane itself is not assimilated by microorganisms and does not need to be immersed in a bacteriostatic agent during storage. . If film fouling occurs, the decomposition of organic components by alkali and the dissolution of inorganic scale by acid may be performed. Functional degradation due to deterioration is almost negligible. Cleaning such as a sponge pole or backwashing, such as a resin film whose function is reduced by such cleaning, is unnecessary. The metal film is a porous film and typically has a pore size of about 0.2 im in diameter.

 Preferably, the ultrafiltration membrane may be tubular. Preferably, the ultrafiltration membrane is a hollow fiber membrane. Also, preferably, the hollow fiber membrane has a pore size of 0.01 / im to 0.5111 in diameter. The ultrafiltration membrane is capable of permeating solvents, metal ions, etc. without applying pressure to the wastewater to be treated and bringing the wastewater into contact with the membrane, without allowing microorganisms and the like in the wastewater to permeate through the membrane. The material of the ultrafiltration membrane is, for example, but not limited to, polysulfone and polyvinyl alcohol. When a hollow fiber membrane is used, by applying pressure to the wastewater and letting it pass through the inside of the hollow fiber, it is possible to permeate a solvent, metal ions, and the like through the membrane without allowing microorganisms and the like in the wastewater to pass through the membrane. The treated wastewater can be circulated inside the hollow fiber and concentrated. When a flammable hollow fiber membrane is used, the hollow fiber membrane itself containing the concentrated wastewater can be incinerated, which facilitates the treatment.

 The non-sludge high-speed wastewater treatment system of the present invention comprises the above-mentioned strong oxidative degrading bacteria, high-concentration oxygen providing means, and solid-liquid separation means, whereby organic matter in the wastewater is finally converted into carbon dioxide gas and water. Decomposition can eliminate the generation of excess sludge.

The non-sludge high-speed wastewater treatment system of the present invention further Oil removal means for pretreatment may be provided. Examples of the oil removing means include, but are not limited to, SIMS (EMS; JPS Inc., Kagawa-cho, Kagawa-gun, Kagawa). Immus: Volatile particulate matter is produced by adding silicone oil and an alkaline solution to incinerated ash, mixing, stirring, and solidifying. When these particles are added to a mixture of oil and water, the particles repel the water and float in water as the oil is taken into the pores of the particles. The safe organic oil recovered in this way can be used as a substitute for oil cake, and in the case of mineral oil, can be reused as fuel. The amount of addition of ims can be appropriately selected according to the ratio of fats and oils in the wastewater. Typically, a concentration of 0.1 to 10% (wXv) is used. Use any substance that can selectively adsorb fats and oils from a mixture of oil and aqueous solution, other than volatile particulate matter obtained by adding silicone oil and alkali solution to the above incinerated ash, mixing, stirring and hardening. It is possible to do.

As used herein, the term “zeolite” refers to a porous substance having many cavities in a crystal and has at least one of the following basic units. The first fundamental unit of the Si_〇 ₄ tetrahedrons and Si are A10 ₄ tetrahedra substituted with A1, two additional T0 ₄ tetrahedra also all Ο shared between the first basic structure include. The second basic unit is a four-, six-, eight-, or twelve-membered ring formed by connecting tetrahedrons, and a double ring in which each of these is overlapped by two. A special case is the five-membered mordenite ring. The third unit is a large symmetric polyhedron, octahedron (TO—sodalite unit), decahedron (TO—cantharinite-cancrinite unit), and tetradecahedron (gmelinite-gmelin-fluorite unit). ). The structure and cavities of zeolite formed by the connection form of the second basic unit are diverse, and various polyhedrons are formed, from the octahedron found in zeolite A to the 26-hedron found in faujasite. Zeolites contain water molecules and exchangeable cations in the large cavities of a comprehensive anion with a three-dimensional framework structure of aluminosilicate.There are various types of cations depending on the skeleton (Si / Al) ratio and cation type. A structure is formed.

The shape of zeolite is indefinite in natural zeolite, and spherical or circular in synthetic zeolite. It has pillars and is circular in artificial zeolite. Particle size is expressed in units of micronanometers. The cations contained in the zeolite crystal cavities can be exchanged depending on the type of cations, the size of the cage, and the strength of the electrostatic field. Zeolite has the function of absorbing and converting cation crystals. The ability to exchange cations is called “cation exchange capacity (CEC)” or “base substitution capacity”. The higher the value, the higher the ability to exchange cation crystals. Is done. A1 has +3 valence and Si has +4 valence, and one positive charge per Al molecule is insufficient. Therefore, the CEC is generally larger as the alum ratio is smaller. Artificial zeolite, for example, according to the method described in JP-A-2003-002638, the raw material concentration at the time of the heat treatment of the raw material containing coal ash is 0.2 kg / Pt or more, and the heating temperature is 100 ° C or more It can be synthesized by heat treatment in an alkaline aqueous solution. Examples of the alkaline solution used here include an aqueous alkali solution such as sodium hydroxide, calcium hydroxide and magnesium hydroxide. The alkali aqueous solution is added so that the concentration of the raw material (solid content) is 0.2 kgZ liter or more, preferably 0.3 kgZ liter or more, more preferably 0.5 kgL or more. If the concentration of the alkaline aqueous solution is less than 0.2 kgZ liter, the minerals (quartz and mullite) contained in the coal ash will undergo a physicochemical reaction and the zeolite will be unstable. The concentration of the raw material is preferably 1 kg, liter or less, particularly preferably 0.7 kgZ liter or less. If the raw material concentration is higher than 1 kg liter, the basic structure of zeolite tends to be difficult to form. The concentration of the alkaline aqueous solution is preferably 2 to 4N, particularly preferably 2 to 3.5N. If the concentration of the alkaline aqueous solution is less than 2 N, the reactivity of the gel product having a zeolite composition tends to decrease, and if it exceeds 4 N, the crystalline product of the porous product of zeolite tends to be broken.

 As an example of the synthesis method, fly ash from coal incineration ash (produced by Ishikawa Coal Power Plant) 8 kg, a 25% aqueous sodium hydroxide solution 33 kg (3.5 N), 33 liters of water , 6 kg of waste diatomaceous earth is added to add diatom 6.

And stirred in a stainless steel container at 60 Hz for 20 minutes in a slurry state. The mixed solution thus obtained was put into an autoclave, and the state in which the internal temperature was heated to 150 ° C by saturated steam was maintained for 2.0 hours.After that, the internal reaction product was transferred to another stainless steel container. After cooling for 12 to 24 hours, using a high-speed centrifugal separator, dehydration is performed at 800 to 1500 rpm and a rotation time of 20 minutes to obtain a reaction method for removing a reaction product. Is disclosed.

 The non-sludge high-speed wastewater treatment system of the present invention may further include nitrogen removing means as needed. Examples of the nitrogen removing means include, but are not limited to, zeolite supporting calcium. When activated sludge is treated aerobically, it is usually detected as nitrate nitrogen as nitrogen remaining in the treated water. If this water is treated with, for example, zeolite carrying calcium, nitric acid can be removed. Examples of the zeolite supporting calcium include, but are not limited to, Ryukyu Light No. 10 (Environmental Purification Center Co., Ltd.). The amount of zeolite to be added can be appropriately selected according to the nitrogen content in the wastewater. Typically, a concentration of 0.1-10% (w / v) is used.

Further, the non-sludge high-speed wastewater treatment system of the present invention may further include a heavy metal removing means as needed. The heavy metal removing means includes, but is not limited to, Fe-type, Na-type, and Ca-type zeolites. Preferably, about 1 to 10% of zeolite is added. Examples of zeolite for removing heavy metals include, but are not limited to, Ryukyu Light No. 20 (Environmental Cleansing Center Co., Ltd.). The amount of zeolite to be added can be appropriately selected according to the ratio of heavy metals in the wastewater. Typically, a concentration of 0.1-10% (w / v) is used. Further, the non-sludge high-speed wastewater treatment system of the present invention may further include a sterilizing / deodorizing means as required. Examples of sterilization and deodorization means include, but are not limited to, Ag-type zeolite. Examples of zeolite for disinfection and deodorization include, but are not limited to, Ryukyu Light RA (Environmental Purification Senyuichi). Ag + ionized in water has no effect on the human body. Also carried Cu Zeolite did not show any bactericidal effect. Further, with Ag-loaded zeolite, deodorization can also be performed. This sterilization method can be used not only for wastewater treatment but also for sterilization of pools. The amount of zeolite to be added can be appropriately selected according to the amount of microorganisms in the wastewater. Typically, concentrations of 0.001 to 10% (w / v) are used.

 In a system including at least one of the above-described nitrogen removing means, heavy metal removing means, and sterilizing and / or deodorizing means, these three means can be used in series in any order. Therefore, the order of the nitrogen removing means, the heavy metal removing means, and the sterilizing / deodorizing means is not limited to the order of the nitrogen removing means, the sterilizing / deodorizing means, and the heavy metal removing means. Means, and the order of sterilization and deodorization means, even the order of heavy metal removal means, sterilization, deodorization means, and nitrogen removal means, sterilization-deodorization means, nitrogen removal means, and heavy metal removal The order of the means may be the order of the sterilizing / deodorizing means, the heavy metal removing means, and the nitrogen removing means. Further, a system provided with only one of these three means or only two of these means is also within the scope of the present invention. DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention combines conventional activated sludge with large-scale aeration by combining useful microorganisms such as strong oxidatively degrading bacteria and recalcitrant COD assimilating bacteria, high acidity equipment, and solid-liquid separation membrane. Provide a wastewater treatment system that does not depend on tanks.

The non-sludge high-speed wastewater treatment system of the present invention includes a means for culturing strong oxidatively degrading bacteria, a means for providing high-concentration oxygen, and a solid-liquid separation means. The non-sludge high-speed wastewater treatment system of the present invention may further include an oil removing means for pretreatment of wastewater, if necessary. Further, the non-sludge high-speed wastewater treatment system of the present invention may further include nitrogen removing means as needed. Also, the non-sludge high-speed drainage of the present invention The processing system may further include a heavy metal removing means as needed. Further, the non-sludge high-speed wastewater treatment system of the present invention may further include a sterilizing means as needed. Further, the non-sludge high-speed wastewater treatment system of the present invention may further include a deodorizing and removing means as needed.

(Embodiment 1)

 One example of an embodiment of the present invention is shown in FIG. The provision of the conditioning tank 3 and the neutralization tank 5 is the same as the conventional activated sludge method described above. The sludge containing the strong oxidatively degrading bacteria is retained in the decomposition reaction tank. The raw water that has passed through the decomposition reaction tank 17 is sent to a denitrification tank as needed, and then flows into the microorganism separation tank 19. The metal membrane 23 arranged in the microorganism separation tank 19 also captures sludge and free bacteria. The reference numeral 25 in the figure schematically shows a means for providing high-concentration oxygen as a powerful air conditioning system. The high-concentration oxygen providing means 25 may be connected to a decomposition reaction tank 17 and, if necessary, a denitrification tank or a microorganism separation tank 19. Reference numeral 43 in Fig. 1 (b) indicates a tank for an additive (enricher) supplied to the strong oxidative degrading bacteria as needed.

 (Embodiment 2)

Another example of the embodiment of the present invention is shown in FIG. In this embodiment, the high-concentration oxygen providing means includes an oxygen generator 36, an ultrafine bubble generator 35, and an aerator 33. As the oxygen generator and the ultra-fine bubble generator, a commercially available device (for example, commercially available from Suzuki Sangyo Co., Ltd. (5-6 Yamadanakayoshimi-cho, Nishikyo-ku, Kyoto-shi)), and as an air conditioner An air diffuser having the structure shown in FIG. 3 can be used. This ultra-fine bubble generator generates ultra-fine bubbles to increase the concentration of dissolved air, and by adding an oxygen generator to the air inlet of this ultra-fine bubble generator, a concentration of about 93% Pure oxygen is introduced, and a high concentration oxygen environment (dissolved oxygen concentration of 200 ppm or more) is achieved in the decomposition reaction tank 17. Shown in Figure 3 The diffuser having the structure includes a bell-shaped gas-liquid mixing cylinder 12 1 as shown in the figure, and generates an ultra-high-speed spiral flow of ultrafine bubbles in the gas-liquid mixing cylinder. Bubbles collide with the projections 1 17 and 1 18 at the top, and ultra-fine bubbles are released from the upper opening 1 15. This makes it possible to convect a vortex containing a large amount of dissolved oxygen and having high aeration efficiency to the decomposition reaction tank 17. The combination of an oxygen generator, an ultra-fine bubble generator, an air heater, and a solid-liquid separator will provide a cost-effective system that does not depend on a large aeration tank.

 (Embodiment 3)

 Another example of the embodiment of the present invention is shown in FIG. The non-sludge high-speed drainage system according to this embodiment includes an inflow tank 1 ′, a decomposition reaction tank 17 ′, an outflow tank 22 ′, a solid-liquid separation unit 23 ′, and an air diffuser 25 ′. In Fig. 4, wastewater is supplied from the inflow tank to the decomposition reaction tank by the pump indicated by P. The diffuser generates an upward flow of the generated fine bubbles in the decomposition reaction tank, thereby stirring the liquid in the decomposition reaction tank and causing a flow in the decomposition reaction tank indicated by an arrow in FIG. The wastewater treated in the decomposition reaction tank is separated into solid and liquid by a metal membrane via a pump P. The treated water that has passed through the metal membrane is introduced into the outflow tank.

 (Embodiment 4)

 FIG. 8 shows another example of the embodiment of the present invention. In this embodiment, oil removing means 13 1, nitrogen removing means 13 2, heavy metal removing means 13 3, sterilizing / deodorizing removing means 1 34 are added to Embodiment 2. .

 The treated waste water from the neutralization tank 5 passes through oil removing means 13 1 including EMS (EMS; JPS Co., Ltd., Kagawa-cho, Kagawa-gun) to remove oil. By this means, the first oil removal, which causes subsequent processes to rupture and cause wastewater treatment to fail, is made.

The treated wastewater that has passed through the non-sludge high-speed wastewater treatment system according to the second embodiment is then subjected to nitrogen removal means including Ryukyu Lite No. 10 (Environmental Purification Center Co., Ltd.). Is filtered. Next, the treated wastewater is filtered by heavy metal removal means, including Ryukyu Light No. 20 (Environmental Purification Senyuichi). Next, the treated wastewater is filtered by sterilizing and deodorizing means including Ryukyu Lite RA (Environmental Purification Center Co., Ltd.).

 As a result of the post-treatment of the non-sludge high-speed wastewater treatment system, nitrogen and heavy metals, which were difficult to remove by the conventional activated sludge method, were removed, and bacteria contaminating the activated sludge were sterilized. , Advanced treatment wastewater will be provided. Example

 (Example 1)

The wastewater was treated using the system according to the third embodiment shown in FIG. The drainage, synthetic wastewater (PVA50mgZL, peptone 75MgZL, meat extract 50 mg L, urea _{25mgZL, Na 2 HP0 4 25mgZL,} KC 13. 5mg / L, C a C 1 2 3. 5mgZL, MgS_〇 ₄ 2. 5 mg / L , NaC 17.5mg / L). The capacity of the decomposition reaction tank 17 'was 15L. As the metal film, a stainless steel wire mesh (pore size 0.1 ljm, 30 × 50 cm) was used. Surplus sludge obtained from the sewage treatment plant was used as seed sludge, and this system was operated for 60 days, and the microbial concentration (MLSS) in the decomposition reactor was measured over time. Figure 5 shows the results of the MLSS in the decomposition reaction tank over time. As shown in the figure, 60 days after the start of operation of the system, the MLSS in the decomposition reaction tank exceeded 1000 OmgZL, and a significant increase in the concentration of microorganisms was observed due to solid-liquid separation using a metal membrane.

Note that a and b in FIG. 6 indicate the distance between the baffle plate and the metal film, and the distance between the metal film and the wall of the decomposition reaction tank. By appropriately selecting a and b, the efficient convection of the liquid in the decomposition reaction tank and the efficiency of oxygen transfer are improved. In the operated 15 L decomposition reactor, a and b were each set to 2.5 cm. Figure 6 is an electron micrograph of the bacteria present in the decomposition reaction tank. Fig. 6 The bacterium was identified as a bacterium belonging to the genus Bacillus, and the bacterium on the right in FIG. 6 was identified as a bacterium belonging to the genus Arthrobacter. (Example 2)

The wastewater was treated using the system according to the second embodiment shown in FIG. Wastewater from a dyeing factory containing PVA was used as wastewater. Degradation reaction tank 17 is the first tank containing strong oxidative degradation bacteria (Pseudomonas FERM P-19204 strain, Acinetovak Yuichi IAM-3 strain, IAM-4 strain), and reaction tank 18 contains acclimated PVA sludge The second tank was used and the microorganism separation tank 19 was used as the ^third tank. The capacity of each tank was about 4 m3. Fig. 7 shows the operation results. The horizontal axis in FIG. 7 indicates the operation period. The upper two graphs in Fig. 7 show the PVA concentration (left) and the COD concentration (right) in each reactor measured according to the conventional method, and the lower two graphs show the PV during operation. A load (left) and COD load (right) are shown.

As shown in the upper part of Fig. 2, the PVA concentration and COD concentration in each tank are lower in the order of conditioning tank, tank I, tank II, and discharged water, and the lower the downstream of the system, the better the system is. It worked. Operating on day 8, but increased the amount of waste water flowing into the system from 85 m ³ Z Date 0. to 1. 42m ³ Z date, P VA concentration and CO D concentration of the released water hardly changes. As shown in Figure 2 below, the PVA treatment efficiency and CDD treatment efficiency (I + II + III) of the system on the 9th day of operation were about 0.1 kgZm ³ Z It was about 0.30.1 kg / m ³ / day.

(Example 3)

Various zeolites were tested for their ability to remove nitrate nitrogen. In the experiment, tap water was filtered using Ca-type zeolite, Mg-type zeolite, and Fe-type zeolite at 1% (w / v) each. As a countermeasure, "Rokko no Mizu" was used. About the water after treatment The amount of nitrate nitrogen was detected using the nitrate ion detection reagent “GR nitrate reagent”. If the color turns pink, it indicates that it contains nitrate nitrogen. As a result, when Fe-type and Ca-type zeolites were used, nitrate nitrogen could be removed. In contrast, Mg-type zeolite was unable to remove nitrate nitrogen efficiently.

(Example 4).

 An experiment was conducted on the cadmium removal ability using various zeolites (Environmental Purification Center Inc.). As a material, a solution was used.

 In a 1.5 ml tube, 0.1 g of zeolite and lm 1 of buffer solution were mixed (10% (wXv)), and the mixture was vigorously stirred at 4 ° C overnight. Thereafter, the mixture was centrifuged twice at about 20,000 Xg for 20 minutes, and the supernatant was collected and analyzed using ICP (inductively coupled plasma). The results are shown below.

 (table 1)

 -Zeolite cadmium concentration used Percentage remaining Stock solution only 0.0594 p pm 00%

 Phillipsite Na type 0.0034 p pm 6%

 Philippite C type a Below detection limit

 Tenjin 0.0036 p pm 6%

 C a 0.0009 ρ pm 1%

 Phillipsite Fe type Below detection limit

 Philippite Na type Below detection limit ―

 The above results indicate that not only Fe-type and Ca-type zeolites but also Na-type zeolites are effective in removing heavy metals.

(Example 5) The bactericidal effect of zeolite was tested. Cu-type zeolite and Ag-type zeolite (zeolite RA-1) were added to a suspension of E. coli of about 300,000 cells Zml, and changes in the number of viable cells were observed. As a result, Cu-type zeolite showed almost no bactericidal effect. In contrast, Ag-type zeolites showed high bactericidal activity (Fig. 9). Next, after sterilizing 100 Oml containing 0.04 g of zeolite by autoclaving, adding about 12,000 cells / ml of E. coli, shaking at 28 ° C, and for a certain time (initial, 1 hour, After 6 hours), the number of viable cells was checked for E. coli. As a result, Ryukyu Light (RA_1 to RA-4) showed a bactericidal effect immediately after contact (0 hour).

(Viable count = 0). In contrast, Zeomighty showed a bactericidal effect, but the viable cell count did not reach 0 even after 1 hour (Fig. 10).

 Next, various Ag-type zeolites (Ryukyu Light RA_1, RA-2. RA-3, and RA_4) and zeolites carrying both silver and copper ions

(Zeomighty) was compared. Approximately 120,000 cells A variety of zeolites (0.04%) were added to a Zml suspension of Escherichia coli, and after a certain period of time (initial, 1 hour, 3 hours, 6 hours), the number of viable cells was observed. . As a result, zeolites that carry only silver ions (RA-1, RA-2, RA-3, and RA-4) have better sterilization than zeolites (zeomite) that carry both silver and copper ions. The effect was shown (Table 2).

Performance comparison when 0.04% zeolite is added)

 Oh lh 3h 6h

Control (Wed) 120000 147000 120000 134000

 RA- 1 0 0 0 0

 RA-2 0 0 0 0

 RA-3 0 0 0 0

RA— 4 0 0 0 0 Zeomighty 20 600 2000 0 0

 Next, RA-1 and Zeomighty were compared at different concentrations. Add 0.01% or 0.04% zeolite RA_1 and zeomighty to an E. coli suspension of about 1 million cells ml, and after a certain period of time (initial, 3 hours, 6 hours), Changes in the number of bacteria were observed. As a result, at all concentrations, zeolite carrying only silver ions (RA-1) exhibited a better bactericidal effect than zeolite carrying both silver ions and copper ions (zeomite) (Table 1). 3) (Comparison of performance when adding zeolite)

 Oh 3h 6h Control (Wed) 1080000 970000 880000

RA-1 0.04% 0 0 0

RA-10.0 1% 33 0 0 Zeomighty 0.04% 32000 0 0 Zermighty 0.01% 248000 50000 15300

(Numerical value is the number of cells Zml) Next, the minimum growth inhibitory concentration for various bacteria was determined by using zeolite (Ryukyu Wright), which carries only silver ions, and zeolite (Zeomighty), which carries both silver and copper ions. And compared. At various concentrations, zeolite was added to the bacterial suspension and after culturing at 37 ° C, the zeolite concentration that did not result in bacterial growth was determined. As is evident from the results in Table 4, zeolites carrying only silver ions exhibited a better bactericidal effect on zeolites carrying both silver and copper ions for all the bacteria tested. Was. Comparison of fungicide properties)

 Ryukyu Light Zeomighty

 MlC (ppm) MlC (ppm) Gram-positive bacteria

Bacillus subtilis 20 250 Bacillus cereus 15 125 Staphylococcus aureus 20 250 Lactobacillus casei 15 125 Gram-negative bacteria

Escherichia coli 15 125 Pseudomonas aeruginosa 20 125 Salmonella typhi murium 15 125 Thiobacillus thioocidans 10 50 (Tiobacillus)

 MIC (minimal inhibitory concentration): minimum inhibitory concentration

(Example 6)

 The bactericidal effect of zeolite was observed not only in treated wastewater but also in seawater with high salt concentration, as shown in the following results.

 (Medium composition)

In order to detect as many microorganisms as possible in seawater, LB medium (nutrient medium), artificial seawater medium (MA medium), MA + YT medium (MA medium + yeast extract 0.05%), agar A medium was prepared. When seawater samples of Osaka Bay Seawater and Kobe Port Seawater were tested, the bacterial count and bacterial species (yellow, orange, white, etc.) (Judgment based on the color of the colony). However, since the maximum number of bacteria was detected in the MA + YT medium for all samples, the MA + YT medium was used hereafter.

 Using MA + YT medium, a sample containing bacteria of about 100,000 cells Zml was added to zeolite (Ryukyu light RA-1) carrying only silver ion and silver ion copper ion Zeolite carrying both (zeomighty) was added. As a result, as shown in Table 5 and FIG. 11, RA-1 exhibited a superior bactericidal effect.

(Table 5)

産業上の利用可能性 活性汚泥に替わるものとして、 強力酸化分解菌を用いた排水処理システムが提 供される。 これらの菌群の多くは比較的大型のバチルス属、 ァルスロパクター属 に属する常温好気性菌で、 増殖が速く、 活性の高い酵素群を菌体外へ分泌するの で、 排水中の有機物を炭酸ガスと水に完全分解することが可能である。 本発明の 排水処理システムは、 菌体フロックは形成されず管理が容易、 余剰汚泥が発生し ないなど、 排水処理システムとしての優位性を提供する。

Industrial applicability As an alternative to activated sludge, a wastewater treatment system using strong oxidative degradation bacteria will be provided. Many of these bacterial groups are relatively large-sized aerobic bacteria belonging to the genera Bacillus and Arsulopactor, which grow rapidly and secrete highly active enzymes out of the cells. And can be completely decomposed into water. The wastewater treatment system of the present invention provides advantages as a wastewater treatment system, such as easy formation of bacterial cell flocs and easy management and generation of excess sludge.

Strong oxidative degradation bacteria degrade hard-to-degrade COD and strongly oxidize organic matter It has the capacity to achieve zero excess sludge generation. The high-concentration oxygen supply means provides a strong air (oxygen) supply to cultivate strong oxidative degradation bacteria at a high concentration and maintain the complete oxidative decomposition activity of organic matter. This high-concentration oxygen providing means prevents the decomposition activity of the strongly degrading bacteria present at a high concentration in the aeration tank from being limited by oxygen supply. The solid-liquid separation means enables wastewater treatment with a high concentration of microorganisms exceeding about 13,000,000 ppm by solid-liquid separation. By combining useful microorganisms such as strong oxidatively degrading bacteria and hard-to-degrade COD assimilating bacteria, high acidity equipment and solid-liquid separation membrane, a wastewater treatment system that does not depend on conventional activated sludge and large aeration tanks Provided.

 Furthermore, according to the present invention, even if the wastewater contains a large amount of fats and oils, it does not cause any problems in the treatment system, and it has been difficult to remove the nitrogen and heavy metals, and the altitude has been sterilized. It has become possible to provide treated wastewater.

Claims

The scope of the claims 1. A non-sludge high-speed wastewater treatment system,  A system comprising means for culturing strong oxidatively degrading bacteria, means for providing high-concentration oxygen, and means for solid-liquid separation.  2. The system according to claim 1, wherein said means for providing high-concentration oxygen comprises means for providing oxygen, and means for generating microbubbles.  3. The system of claim 2, wherein said microbubble generating means generates bubbles having a diameter not exceeding about 3 im.  4. The system according to claim 1, wherein said solid-liquid separation means is a porous membrane.  5. The system according to claim 4, wherein said porous membrane is a metal membrane.  6. The system according to claim 5, wherein the metal film is formed by spraying stainless metal particles onto a stainless steel wire net and then sintering.  7. The system according to claim 4, wherein said porous membrane is an ultrafiltration membrane. ,  8. The system according to claim 4, wherein the porous membrane is a hollow fiber membrane.  9. The system of claim 4, wherein the porous membrane has a pore size of about 0.2 in diameter.  10. The system of claim 1, further comprising a strong oxidatively degrading bacterium.  1 1. The strong oxidative degrading bacterium is a bacterium having a growth rate of 30 minutes or less at 30 ° C. in a complete medium, and comprises a bacterium that decomposes oils and fats under aerobic conditions. The system according to item 1.  12. The system according to claim 11, wherein the bacilli produce an oil and fat decomposition promoting substance selected from the group consisting of proteases, cellulases, amylases, lipases, and biological surfactants. . 13. The system according to claim 12, wherein said bacilli produce a biological surfactant. 14. The system of claim 12, wherein said bacilli produce amylase and lipase.  15. The system of claim 12, wherein said bacilli produce cellulase. 16. The system of claim 12, wherein said bacilli produce protease and amylase.  17. The system according to claim 11, wherein the bacillus is Bacillus subtilis FERM BP-7270.  18. The system according to claim 11, wherein the bacillus is Bacillus subtilis FERM BP-7271.  19. The system of claim 1, wherein the strongly oxidatively degrading bacteria include polyvinyl alcohol degrading bacteria.  20. The system according to claim 19, wherein the polyvinyl alcohol-degrading bacterium is Pseudomonas FERM P-19204 strain. ' 21. The system according to claim 19, wherein the polyvinyl alcohol-degrading bacterium is an Acinetobacter IAM-3 strain.  22. The bacterium according to claim 19, wherein the polyvinyl alcohol-degrading bacterium is an Acinetobacter IAM-4 strain.  23. The system according to claim 1, wherein the high-concentration oxygen providing means convects the liquid in the decomposition reaction tank.  24. The system of claim 1, further comprising oil removal means.  25. The system according to claim 24, wherein the oil removing means is a volatile particulate material obtained by adding a silicone oil and an alkaline solution to the incinerated ash, mixing, stirring and solidifying the mixture.  26. The system of claim 1, further comprising nitrogen removal means.  27. The system of claim 26, wherein the means for removing nitrogen is zeolite carrying calcium. 28. The system of claim 1, further comprising a heavy metal removal means. 29. The system according to claim 28, wherein said heavy metal removing means is a zeolite selected from the group consisting of a zeolite carrying Fe, a zeolite carrying Na, and a zeolite carrying Ca.  30. Further sterilization. The system according to claim 1, further comprising a deodorizing and removing unit. 31. The sterilization and deodorization removing means is zeolite carrying silver. System according to 0.  32. A wastewater treatment method using the system according to claim 1.  33. Sterilization Method using sterilization and deodorization removal means.  34. A non-sludge high-speed wastewater treatment system,  Equipped with a decomposition reaction tank, high-concentration oxygen providing means, and solid-liquid separation means,  A system wherein the high oxygen concentration providing means and the solid-liquid separation means are combined to increase the concentration of microorganisms in the decomposition reactor to at least 10,000 ppm.