WO2012070493A1 - 嫌気性処理方法 - Google Patents
嫌気性処理方法 Download PDFInfo
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- WO2012070493A1 WO2012070493A1 PCT/JP2011/076675 JP2011076675W WO2012070493A1 WO 2012070493 A1 WO2012070493 A1 WO 2012070493A1 JP 2011076675 W JP2011076675 W JP 2011076675W WO 2012070493 A1 WO2012070493 A1 WO 2012070493A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2833—Anaerobic digestion processes using fluidized bed reactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- 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
Definitions
- the present invention introduces water to be treated into an acid generation tank, decomposes a polymer component in the water to be treated into an organic acid, and then discharges the effluent from the acid generation tank to methane filled with a fluid non-biological carrier.
- the present invention relates to an anaerobic treatment method for introducing methane fermentation into a production tank.
- a sludge blanket is formed by forming granular sludge with high density and high sedimentation in the reaction tank, and upwardly circulating organic wastewater containing soluble BOD.
- the UASB (Upflow Anaerobic Sludge Blanket) method is used, which performs high-load and high-speed processing by contacting with a high-pressure anaerobic sludge blanket.
- a solid organic substance having a low digestion rate is separated and separately treated, and only a soluble organic substance having a high digestion rate is processed at high speed with high load by anaerobic treatment using granular sludge having a high anaerobic microorganism density.
- EGSB Extra Granule
- Sludge Blanket method is also being carried out.
- anaerobic treatment using granular sludge such as UASB method and EGSB method
- sludge containing anaerobic microorganisms is maintained and grown in a granular state for treatment.
- This anaerobic treatment method can achieve a high sludge retention concentration compared to treatment with a fixed bed or fluidized bed that holds sludge on a carrier, and therefore can be operated at a high load, and a treatment system that is already in operation. It is possible to start up in a short period by procuring surplus sludge from, which is efficient.
- the initially charged granule may be gradually disassembled, and operation may become impossible.
- the method using a fluid non-biological carrier can prevent the carrier from flowing out of the reaction vessel by a mechanical method such as a screen, and can always secure the surface of the carrier as a microbial growth place. Further, it has an advantage that it can be applied to low-concentration COD wastewater and wastewater in which granules are dismantled.
- Organic wastewater containing polymer components such as sugar and protein may be treated with a two-phase anaerobic treatment device using an acid generation tank and an anaerobic reaction tank.
- the organic wastewater is introduced into an acid generation tank, and after the polymer in the wastewater is decomposed to a low molecular organic acid such as acetic acid or propionic acid, it is treated in a reaction tank filled with granules or a carrier.
- Wastewater containing only compounds that can be directly used by methanogenic bacteria such as methanol and acetic acid is a one-phase process in which water to be treated is directly passed through a reaction tank filled with granules or a carrier without providing an acid generation tank. Efficient processing can be performed by the apparatus.
- the water to be treated containing a large amount of the polymer component is treated with high treatment efficiency in the subsequent reaction tank by decomposing the polymer component in the acid generation tank and reducing the molecular weight in advance.
- Patent Document 1 describes an anaerobic treatment method in which an organic wastewater is treated in an acid production tank and then treated by flowing upwardly into a UASB method methane production tank.
- the anaerobic treatment described in Patent Document 1 controls granular sludge with high activity and good sedimentation in the UASB method methane production tank by controlling the sugar / COD Cr ratio in the liquid introduced into the methane production tank. Proliferate.
- Patent Document 2 a beer effluent of high concentration is treated in an acid generation tank (raw water adjustment tank) and then diluted to a COD Cr concentration of 3000 mg / L or less and introduced into a fluidized bed methane fermentation tank filled with a carrier.
- the anaerobic treatment method using a fluid non-biological carrier can stably treat low-concentration wastewater that is difficult to treat by the granule method or wastewater with a biased composition.
- the biofilm attached to the carrier is enlarged and the carriers are fixed to each other, or the fixed carrier is floated.
- the carrier floats up, scum is generated in the upper part of the reaction tank (methane generation tank filled with the carrier), resulting in a decrease in processing capacity, or operation troubles such as the carrier collecting in the flow path and blocking the piping. is there.
- the present invention provides an anaerobic treatment method that solves such problems.
- the present inventors introduced water to be treated into an acid generation tank, decomposes a polymer component in the water to be treated into organic acids,
- anaerobic treatment in which effluent is introduced into a methane production tank filled with a fluid non-biological carrier and subjected to methane fermentation, the content of polymer components other than organic acids in the inflow water of the methane production tank is a predetermined value. It has been found that a stable treatment can be continued by preventing the carrier from rising in the methane production tank by the following.
- the present invention has been achieved on the basis of such knowledge, and the gist thereof is as follows.
- concentration of high molecular components other than the organic acid in the inflow water of this methane production tank shall be 300 mg / L or less, It is characterized by the above-mentioned .
- the COD Cr concentration of the water to be treated is 300 mg / L or more, and is derived from a polymer component other than an organic acid in the total COD Cr of the water to be treated. COD Cr is 30% or more, The anaerobic processing method characterized by the above-mentioned.
- the effluent from the acid generation tank is converted into methane filled with a fluid non-biological carrier. It is introduced into the production tank and treated with methane fermentation.
- the COD Cr concentration of the polymer component other than the organic acid in the inflowing water of the methane generation tank is 300 mg / L or less, the following mechanism of action allows the carriers to adhere to each other due to the enlargement of the biofilm, or to adhere to the carriers. Therefore, it is possible to prevent the operation troubles such as the rising of the air flow and the blockage of the flow path, and to carry out the efficient anaerobic treatment stably for a long time.
- the polymer component In the acid generation tank, the polymer component is converted to an organic acid, and dispersed cells are generated. Dispersed bacterial cells flow out into treated water without accumulating even if they flow into a methane production tank filled with a carrier. When anaerobic protozoa grow in the methane production tank, the dispersed cells are preyed on by the protozoa. Since this protozoan is a higher-order organism in the food chain, and its growth amount, that is, the amount of surplus sludge produced, is very small, there is no possibility of carrier sticking and floating due to the growth of the protozoa.
- an acid generation reaction occurs inside the methane generation tank.
- Microorganisms responsible for acid production are known to have a fast growth rate, and the amount of sludge generated is significantly higher than that of methanogens. For this reason, if the acid generation reaction proceeds in the methane generation tank, the amount of microbial growth increases, and the carriers tend to adhere to each other with a biofilm, which causes levitation and clogging problems.
- the granule method In the granule method, a small amount of polymer component is required in the inflow water of the methane production tank in order to maintain the granule.
- the polymer method since the methanogen is grown on the surface of the non-biological carrier, the polymer method is not necessarily used. There is no need to contain any components, and operation is possible even at 300 mg / L or less. Operation that treats organic acids and low-molecular-weight organic wastewater that do not contain polymer components that are difficult to form granules is also possible.
- water to be treated is introduced into an acid generation tank, the polymer component in the water to be treated is decomposed into an organic acid, and then the effluent from the acid generation tank is converted into a fluid non-living organism. It is introduced into a methane production tank filled with a carrier and subjected to methane fermentation treatment.
- the COD Cr concentration of the polymer component other than the organic acid in the inflow water of the methane generation tank is set to 300 mg / L or less.
- the COD Cr concentration of the polymer component other than the organic acid-treated water acid formation tank flowing into the methanogenesis tank to less 300 mg / L can employ the following means. i) Depending on the specifications of the acid generation tank, the processing conditions, for example, the residence time of the acid generation tank, so that the COD Cr concentration of the polymer component other than the organic acid in the acid generation tank is 300 mg / L or less. For 2.5 hours or more. ii) Diluting the treated water flowing into the acid generation tank or the treated water of the acid generation tank with water that does not contain these polymer components, for example, city water, industrial water, treated water of the methane generation tank, etc. Thus, the concentration of the polymer component other than the organic acid of water flowing into the methane generation tank is set to 300 mg / L or less.
- the methane generation tank inflow water in which the COD Cr concentration of the polymer component other than the organic acid is 300 mg / L or less does not contain any polymer component other than the organic acid and contains only the low-molecular organic component. Good.
- High molecular components other than organic acids are organic substances having 7 or more carbon atoms such as sugars, proteins, fats and oils, and low molecular organic components are organic substances having 6 or less carbon atoms such as ethanol and methanol.
- the COD Cr concentration of the polymer component other than the organic acid in water can be obtained from the difference between the COD Cr concentration in the water to be treated and the COD Cr concentration of the organic acid.
- the COD Cr concentration of the organic acid can be obtained by measuring the organic acid concentration and converting the measured organic acid concentration into the COD Cr concentration.
- the organic acid concentration can be analyzed by a known method such as liquid or gas chromatography by ion exchange, ion exclusion or reverse phase. There is a correlation between the COD Cr concentration of the organic acid and the alkali consumption.
- the organic acid concentration and the concentration of the polymer component other than the organic acid are obtained from the amount of alkali added to the acid generation tank and the methane generation tank by the correlation equation, and based on this value.
- the COD Cr concentration of the polymer component other than the organic acid of the inflow water of the methane generation tank can be adjusted to be 300 mg / L or less. .
- the water to be treated that is treated in the acid generation tank has a COD Cr concentration of 300 mg / L or more and is derived from a polymer component other than the organic acid in the total COD Cr of the water to be treated.
- Organic wastewater with COD Cr of 30% or more is suitable.
- organic wastewater having a COD Cr concentration of 300 mg / L or less to-be-treated water or wastewater with a low proportion of COD Cr derived from polymer components other than organic acids in the total COD Cr the present invention is used. Processing can be performed without application.
- the COD Cr concentration of the water to be treated in the present invention is 300 mg / L or more, particularly 300 It is preferably about 5,000 mg / L, particularly about 500 to 3,000 mg / L, but is not limited thereto.
- the ratio of COD Cr derived from polymer components other than organic acids in the total COD Cr contained in the water to be treated is 30% or more, particularly about 40 to 80%, and COD derived from polymer components other than organic acids.
- the present invention is particularly effectively applied to organic wastewater having a relatively high content of polymer components other than organic acids, such as a Cr content of 300 to 4000 mg / L, particularly 500 to 2500 mg / L.
- Such organic wastewater includes, but is not limited to, manufacturing wastewater from food factories, organic wastewater from chemical factories, general sewage, and the like.
- such organic waste water is first introduced into an acid generation tank, and the polymer component is decomposed into low molecular organic acids such as acetic acid and propionic acid.
- the treatment conditions of this acid generation tank vary depending on the conditions such as the biodegradability of the waste water, but the pH is 5 to 8, preferably 5.5 to 7.0, the temperature 20 to 40 ° C., preferably 25 to 35 ° C., HRT 2 -24 hr, preferably 2-8 hr is appropriate.
- a methane generation tank filled with a fluid non-biological carrier into which treated water of this acid generation tank is introduced a fully mixed reaction tank using a stirrer or the like, an upward flow type in which the inside of the tank is mixed with water flow and generated gas
- a reaction vessel or the like it is particularly preferable to use an upward flow type reaction vessel since the height and shape of the reaction vessel can be freely set and a large amount of carrier can be charged.
- the processing conditions in the complete mixing type reaction tank and the upward flow type reaction tank are not particularly limited as long as desired processing efficiency can be obtained.
- the following conditions can be set.
- the load per microorganism adhering to the carrier is preferably 1 to 10 kg-COD Cr / kg-VSS / day, particularly 2 to 8 kg-COD Cr / kg-VSS / day.
- the amount of microorganisms (VSS amount) adhering to the carrier can be determined by alkali-extracting the carrier protein and measuring the protein by a known Bradford method. At this time, the VSS amount is calculated by setting the protein content in the microbial cells to 50%.
- the fluid wastewater biological carrier filled in the methane production tank has a size of 1.0 to 5.0 mm and a sedimentation speed of 200 to 500 m / hr.
- the preferred size of the carrier used in the present invention is 2.5 to 4.0 mm.
- the size of the carrier is usually referred to as “particle size”.
- particle size For example, in the case of a rectangular parallelepiped carrier, the length of its long side is referred to, and in the case of a cubic carrier, the length of one side thereof is defined. In the case of a cylindrical carrier, it represents the larger one of the diameter and the height of the cylinder.
- the particle diameter of the irregularly shaped carrier other than these shapes is the interval between the plates where the interval between the plates becomes the largest when the carrier is sandwiched between two parallel plates.
- the average size of the carrier may be 1.0 to 5.0 mm, preferably 2.5 to 4.0 mm, and all the carrier sizes are not in this range. Also good.
- the sedimentation rate of the carrier is too small, it is likely to float due to water flow and generated gas, and accumulates in a scum shape near the water surface. That is, in the case of a method using a non-biological carrier, a biofilm is formed on the surface and a reaction in which gas is generated proceeds inside the biofilm, so that the apparent specific gravity of the carrier becomes lighter as the biofilm is formed. In consideration of the influence of this biofilm, it is necessary to determine the specific gravity and sedimentation rate of the carrier itself. Conversely, if the sedimentation rate of the carrier is too high, the contact efficiency with the water to be treated will be poor, and sufficient treatment efficiency will not be obtained, or solid matter will accumulate in the deposited layer of the carrier and the channel will be blocked. coming out.
- a more preferable sedimentation rate of the carrier used in the present invention is 200 to 500 m / hr.
- the sedimentation rate of the carrier is the amount of sedimentation that takes place when the carrier is immersed in water (fresh water such as tap water) and is taken into a graduated cylinder in water (fresh water such as tap water). This is a value obtained by measuring the distance. In the present invention, measurement is carried out on 10 or more, preferably 10 to 20 carriers, and the average value is taken as the sedimentation rate.
- foam (I) A foam containing 30 to 95% by weight of a resin component mainly composed of a polyolefin resin and 5 to 70% by weight of a hydrophilizing agent for cellulose powder, the surface of which has a melt fracture state ( Hereinafter, it may be referred to as “foam (I)”.
- a foam comprising 30 to 95% by weight of a resin component mainly composed of a polyolefin resin, 4 to 69% by weight of a hydrophilizing agent for cellulose powder, and 1 to 30% by weight of an inorganic powder, Has a melt fractured state (hereinafter sometimes referred to as “foam (II)”)
- Melt fracture is generally known as a phenomenon in which irregularities occur on the surface of a molded product during plastic molding (a state in which there is no smooth surface).
- a phenomenon in which irregularities occur on the surface of a molded product during plastic molding a state in which there is no smooth surface.
- the internal pressure of the extruder becomes extremely high, the extrusion speed becomes extremely large, or the temperature of the plastic material becomes too low, irregular irregularities on the surface of the molded product or occur, it refers to a phenomenon in which to lose the gloss of the surface.
- a preferable melt fracture state of the carrier according to the present invention satisfies the specific surface area ratio represented by the following formula (1).
- B / A 1.5 to 4.0 (1)
- A represents the apparent specific surface area of the foam
- B represents the actual specific surface area of the foam.
- the apparent specific surface area A of the foam indicates a specific surface area in a state where the surface of the foam is smooth, that is, a state where no melt fracture occurs
- the actual specific surface area B indicates a state where the melt fracture occurs.
- the actual specific surface area at is shown. That is, the value of B / A represented by the above formula (1) indicates the rate of increase in specific surface area due to the occurrence of melt fracture, and those having a B / A of 1 depend on the melt fracture on the surface. It means that there is no unevenness.
- the contact area between the water to be treated and the carrier becomes small, which is not preferable because the treatment capacity becomes small.
- the value of B / A is larger than 4.0, the melt fracture on the surface is easily scraped by contact between the carriers at the time of use, which is not preferable.
- the apparent specific surface area A and the actual specific surface area B values measured with an automatic specific surface area / pore distribution measuring device [Tristar 3000, manufactured by Shimadzu Corporation] can be used.
- the resin component constituting the foam preferably has a melt flow index of 5 to 25 g / 10 min. If the melt flow index is less than 5 g / 10 min, the fluidity of the resin component is insufficient, so that it is unsuitable for foam molding, and if it exceeds 25 g / 10 min, a phenomenon of crushing during foam molding may occur.
- Melt flow index (hereinafter sometimes simply abbreviated as “MFI”) is one of the measures for the fluidity of a resin in a molten state.
- the amount of resin flowing out from a nozzle (orifice) is measured, and is generally known as an index expressed by weight per 10 minutes (unit: g / 10 min).
- the value at 230 ° C. and 21.6 N load (DIN 53735) is adopted.
- Preferred resin components constituting the foams (I) and (II) are polyethylene (hereinafter sometimes simply abbreviated as “PE”), polypropylene (hereinafter simply abbreviated as “PP”). And ethylene-vinyl acetate copolymer (hereinafter sometimes simply referred to as “EVA”). These resins may be used alone or as a mixture appropriately combined.
- the resin component constituting the foams (I) and (II) may be a resin obtained by adding another thermoplastic resin component to a polyolefin resin.
- thermoplastic resin components include polystyrene (hereinafter sometimes abbreviated as “PS”), polyethylene terephthalate, polyvinyl chloride, polyvinylidene chloride, polycarbonate, polyurethane, polyamide, polyacetal, polylactic acid, polymethyl methacrylate. , ABS resin and the like.
- Polyethylene is particularly preferred as the resin component constituting the foams (I) and (II), but within the above MFI range, a mixture of PE and other polyolefin resins, for example, PE and PP It may be a mixture, a mixture of PE and EVA, a mixture of PE, PP and EVA, a mixture of PE, PP and PS, a mixture of PE, PP, EVA and PS, or a mixture obtained by further mixing other thermoplastic resins.
- These resin components may be recycled resins.
- cellulose-based powder examples include wood powder, cellulose powder, hemp cellulose powder and the like, and sawdust, avicel, arbocel, paper powder, cellulose beads, microcrystalline cellulose, microfibrillated cellulose and the like.
- wood flour any of these may be used alone, or two or more of them may be mixed and used in an arbitrary ratio.
- the shape of the hydrophilizing agent is spherical, elliptical, wedge-shaped, whisker-shaped, fibrous or the like, but other shapes may be used.
- the hydrophilizing agent preferably has a particle size of 200 mesh pass, preferably 100 mesh pass, more preferably 40 mesh pass.
- the hydrophilizing agent has a role of imparting a water permeation function to the foam having closed cells.
- the hydrophilizing agent is desirably exposed or protruded from the surface of the foam.
- exposure means that part of the surface of the hydrophilizing agent appears on the foam surface
- protrusion means that part of the hydrophilizing agent protrudes from the foam surface.
- being exposed or protruding means that the whole or part of the hydrophilizing agent is buried in the foam and a part of the surface of the hydrophilizing agent appears on the foam surface, or It means a state in which a part of the hydrophilizing agent protrudes from the foam surface.
- Examples of the inorganic powder used for the foam (II) include barium sulfate, calcium carbonate, zeolite, talc, titanium oxide, potassium titanate, and aluminum hydroxide, and barium sulfate is particularly preferable. Any of these inorganic powders may be used alone, or two or more kinds of inorganic powders may be used.
- the ratio of the resin component is larger than the above range and the ratio of the hydrophilizing agent is small, the effect of imparting the water penetration function by using the hydrophilizing agent is not sufficient, It takes a long time to set the state of sedimentation, and conversely, if the proportion of the resin component is less than the upper range and the proportion of the hydrophilizing agent is large, the strength of the carrier is lowered.
- the inorganic powder is blended for the purpose of adjusting the core material and the specific gravity during foaming, but the amount of resin components and hydrophilizing agents is further reduced to reduce production costs. is there. If the proportion of the inorganic powder is less than the above range, the blending effect of such inorganic powder cannot be sufficiently obtained, and if it is large, the specific gravity becomes too large.
- the foams (I) and (II) are foamed using a foaming agent.
- the foaming ratio is 2 to 10 times, and the specific gravity determined from the apparent volume is 0.10 to 0.00. It is preferably 80 g / ml.
- the specific gravity becomes too large, and thus a large force is required when flowing in water, which is not preferable. If the expansion ratio is larger than the above upper limit, the specific gravity is small, and therefore, it tends to float on the water surface, which is not preferable.
- the specific gravity obtained from the apparent volume of the foam is a value (unit: g / ml) obtained by measuring 30 ml of the foam in an apparent volume in a 50 ml graduated cylinder and calculating from the weight.
- the specific gravity shall be shown. This is because the foams (I) and (II) have a melt-lacquered state on the surface, and it is very difficult to measure the true volume.
- the specific gravity obtained from the apparent volume of the foam is simply referred to as “specific gravity”.
- Foams (I) and (II) are prepared by melting and kneading the above-mentioned polyolefin resin, hydrophilizing agent, and further inorganic powder, and further foaming a mixture obtained by melting and kneading the foaming agent. It can be manufactured by cutting into a size.
- foaming agent examples include sodium bicarbonate (bicarbonate) and azodicarbonamide.
- a foaming agent is not restricted to these, A chemical foaming agent, a physical foaming agent, etc. are mentioned.
- the chemical foaming agent include azo compounds such as barium azodicarboxylate, nitroso compounds such as N, N-dinitrosopentamethylenetetramine, hydrazine derivatives such as 4,4′-oxybis (benzenesulfonylhydrazide), and semicarbazide.
- the physical foaming agent include aliphatic hydrocarbons (eg, butane, pentane, hexane, etc.), chlorinated hydrocarbons (eg, dichloroethane, dichloromethane, etc.), fluorinated chlorohydrocarbons (eg, trichloromonofluoromethane).
- sodium bicarbonate sodium bicarbonate
- a so-called self-supporting foaming agent also referred to as an independent foaming agent, microsphere, or thermally expandable microcapsule
- this self-supporting foaming agent becomes hollow spherical particles having an outer wall surface by foaming
- the resin composition may be extruded in the gas phase (for example, in the air) instead of being extruded and foamed in water.
- the hollow portion of the foam is maintained without being crushed, and a foam having a desired expansion ratio is obtained.
- the self-supporting foaming agent for example, vinylidene chloride-acrylonitrile copolymer or acrylonitrile-methacrylonitrile copolymer is used as a polymer for the outer wall, and isobutane, isopentane or the like is used as a volatile liquid contained therein. Is mentioned. Specific examples include EXPANSEL (Nippon Philite Co., Ltd.) and EPD-03 (Eiwa Chemical Industry Co., Ltd.).
- EXPANSEL Natural Philite Co., Ltd.
- EPD-03 Eiwa Chemical Industry Co., Ltd.
- foaming agents may be used alone or in combination of two or more.
- the foaming agent is 100 parts by weight of the polyolefin resin and the hydrophilizing agent in the foam (I), and the polyolefin resin and the hydrophilic in the foam (II). It is preferable to use 0.5 to 8 parts by weight with respect to 100 parts by weight of the total of the agent and the inorganic powder.
- the processing conditions of the acid generation tank 1 and the methane generation tank 3 were as follows. ⁇ Acid production tank> Capacity: 18L HRT: 1.5 hr pH: 6.5 Temperature: 30 ° C
- ⁇ Methane production tank> Capacity: About 10L (Diameter 15cm, Height 60cm) HRT: 0.9 hr Ascending flow velocity (LV): 2 m / hr pH: 7.0 Carrier filling rate: 40% Carrier: A cylindrical polyolefin resin carrier having a diameter of 2 mm, a height of 3 mm, and a sedimentation speed of 300 m / hr.
- the amount of treated water was about 305 L / day, and 2 L of dispersed anaerobic sludge (10 g-VSS / L) was added to the methane generation tank 3 as seed sludge at the start of treatment.
- Example 1 treatment was performed in the same manner except that the COD Cr concentration of the raw water was changed as shown in Table 1, except for the total COD Cr concentration of the treated water in the acid generation tank and the organic acid.
- the COD Cr concentration derived from the polymer component of referred to as “residual sugar COD Cr concentration” in Table 1), the COD Cr concentration of the treated water in the methane generation tank, and the presence or absence of floating of the carrier in the methane generation tank, The results are shown in Table 1.
- Table 1 also shows the load per microorganism adhering to the support in the methane production tank (referred to as “support load” in Table 1).
- This carrier load was determined by measuring the amount of microorganisms adhering to the support in the methane production tank by the above-mentioned method (this value was 8000 to 16000 mg-VSS / L-support), and this value and the load in the methane production tank. And calculated by the value of.
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Abstract
Description
担体が浮上すると、反応槽(担体を充填したメタン生成槽)上部でスカムが発生して処理能力が低下したり、流路に担体が集積して配管を閉塞させる等の運転障害を引き起こすことがある。
i) 酸生成槽の仕様に応じて、酸生成槽の処理水の有機酸以外の高分子成分のCODCr濃度が300mg/L以下となるように、処理条件、例えば、酸生成槽の滞留時間を2.5時間以上とする。
ii) 酸生成槽に流入する被処理水又は酸生成槽の処理水を、適宜これらの高分子成分を含まない水、例えば、市水、工水、メタン生成槽の処理水などで希釈することにより、メタン生成槽に流入する水の有機酸以外の高分子成分の濃度が300mg/L以下となるようにする。
従って、被処理水の性状が変動する場合には、酸生成槽及びメタン生成槽へのアルカリ添加量から相関式により有機酸濃度及び有機酸以外の高分子成分の濃度を求め、この値に基いて酸生成槽の処理条件や希釈の程度等を制御することにより、メタン生成槽の流入水の有機酸以外の高分子成分のCODCr濃度が300mg/L以下となるように調整することもできる。
被処理水のCODCr濃度が300mg/L以下であるような低濃度有機性排水や、全CODCr中の有機酸以外の高分子成分に由来するCODCrの割合の低い排水では、本発明を適用することなく処理を行うことができる。
被処理水に含まれる全CODCr中の有機酸以外の高分子成分に由来するCODCrの割合が30%以上、特に40~80%程度であり、有機酸以外の高分子成分に由来するCODCr含有量が300~4000mg/L、特に500~2500mg/Lであるような、比較的有機酸以外の高分子成分の含有量の多い有機性排水に対して、本発明は特に有効に適用される。
担体充填率:10~30%
HRT:1.0~24hr
槽負荷:4.0~12.0kg-CODCr/m3/day
汚泥負荷:0.8~3.0kg-CODCr/kg-VSS/day
pH:6.5~7.5
温度:25~38℃
<上向流型反応槽>
担体充填率:10~80%
HRT:1.0~24hr
上昇流速(LV):1.0~20m/hr
槽負荷:4.0~32kg-CODCr/m3/day
汚泥負荷:0.8~3.0kg-CODCr/kg-VSS/day
pH:6.5~7.5
温度:25~38℃
本発明において、担体の大きさは、その平均値が1.0~5.0mm、好ましくは2.5~4.0mmの範囲であればよく、すべての担体の大きさがこの範囲でなくてもよい。
(I) ポリオレフィン系樹脂を主体とする樹脂成分30~95重量%と、セルロース系粉末の親水化剤5~70重量%とを含む発泡体であって、表面がメルトフラクチャー状態を有する発泡体(以下「発泡体(I)」と記載する場合がある。)
(II) ポリオレフィン系樹脂を主体とする樹脂成分30~95重量%と、セルロース系粉末の親水化剤4~69重量%と、無機粉末1~30重量%とを含む発泡体であって、表面がメルトフラクチャー状態を有する発泡体(以下「発泡体(II)」と記載する場合がある。)
B/A=1.5~4.0 ・・・(1)
発泡体の見かけの比表面積Aとは、発泡体の表面が平滑な状態、つまり、メルトフラクチャーを生じていない状態での比表面積を示し、実比表面積Bとは、メルトフラクチャーが生じている状態での実際の比表面積を示す。即ち、上記式(1)で示されるB/Aの値は、メルトフラクチャーを生じることによる比表面積の増加の割合を示すものであり、B/Aが1であるものは、表面にメルトフラクチャーによる凹凸が全くないことを意味する。
化学的発泡剤としては、例えば、バリウムアゾジカルボキシレート等のアゾ化合物、N,N-ジニトロソペンタメチレンテトラミン等のニトロソ化合物、4,4’-オキシビス(ベンゼンスルホニルヒドラジド)等のヒドラジン誘導体、セミカルバジド化合物、アジド化合物、トリアゾール化合物、イソシアネート化合物、重炭酸ナトリウム等の重炭酸塩、炭酸塩、亜硝酸塩、水素化物、重炭酸ナトリウムと酸の混合物(例えば、重炭酸ナトリウムとクエン酸等)、過酸化水素と酵素との混合物、亜鉛粉末と酸との混合物などが挙げられる。物理発泡剤としては、例えば、脂肪族炭化水素類(例えば、ブタン、ペンタン、ヘキサンなど)、塩化炭化水素類(例えば、ジクロロエタン、ジクロロメタンなど)、フッ化塩化炭化水素類(例えば、トリクロロモノフロロメタン、ジクロロジフロロメタン、ジクロロモノフロロメタン、ジクロロテトラフロロエタンなど)、代替フロン類、空気、炭酸ガス、窒素ガス、水などが挙げられる。中でも、分解温度が低く、安価であるという点から、重炭酸ナトリウム(重曹)を用いることが特に好ましい。
図1に示す嫌気性処理装置により、糖とタンパクを主体とする合成排水(CODCr濃度:500~1500mg/L、全CODCr中の有機酸以外の高分子成分に由来するCODCrの割合:約60%、pH7.0)を原水として通水試験を行った。
この嫌気性処理装置は、原水を酸生成槽1で処理した後、ポンプP1でpH調整槽2に送給してpH調整し、pH調整水をポンプP2により流動性非生物担体4を充填したメタン生成槽3に上向流で通水して処理する。メタン生成槽3の流出水は一部が循環水としてpH調整槽2に循環され、残部が処理水として系外へ排出される。酸生成槽1内の水はポンプP0により循環されている。酸生成槽1及びpH調整槽2には、pH調整のためにアルカリ剤として水酸化ナトリウムが添加される。1A,2AはpH計であり、3A,3Bはスクリーンである。
<酸生成槽>
容量:18L
HRT:1.5hr
pH:6.5
温度:30℃
容量:約10L(直径15cm、高さ60cm)
HRT:0.9hr
上昇流速(LV):2m/hr
pH:7.0
担体充填率:40%
担体:直径2mm、高さ3mm、沈降速度=300m/hrの円柱形状のポリオレフィン樹脂製担体
この担体負荷は、前述の方法でメタン生成槽の担体に付着した微生物量を測定し(この値は、8000~16000mg-VSS/L-担体であった。)、この値とメタン生成槽の負荷の値とで算出して求めた。
原水CODCr濃度500~1200mg/Lの実施例1~3では、酸生成槽の酸生成の残糖CODCr濃度が300mg/L以下となり、メタン生成槽における担体の浮上は起こらなかった。一方、原水CODCr濃度1200~1500mg/Lの比較例1の場合は、酸生成槽の処理水のCODCr濃度にばらつきがあり、メタン生成槽において担体の浮上が起こる場合と、起こらない場合が確認された。担体浮上が起こる場合には酸生成槽の処理水の残糖CODCr濃度が300mg/Lを超え400mg/L以上であり、担体浮上が起こらない場合には、酸生成槽の残糖CODCr濃度が300mg/L以下であることが確認された。
なお、本出願は、2010年11月26日付で出願された日本特許出願(特願2010-263584)に基づいており、その全体が引用により援用される。
Claims (5)
- 被処理水を酸生成槽に導入して該被処理水中の高分子成分を有機酸に分解した後、該酸生成槽の流出水を、流動性の非生物担体を充填したメタン生成槽に導入してメタン発酵処理する嫌気性処理方法において、該メタン生成槽の流入水中の有機酸以外の高分子成分のCODCr濃度を300mg/L以下とすることを特徴とする嫌気性処理方法。
- 請求項1において、該メタン生成槽における、担体に付着している微生物当たりの負荷を1~10kg-CODCr/kg-VSS/dayとすることを特徴とする嫌気性処理方法。
- 請求項1において、前記有機酸以外の高分子成分が炭素数7以上の有機物であることを特徴とする嫌気性処理方法。
- 請求項1において、前記被処理水のCODCr濃度が300mg/L以上であり、該被処理水の全CODCr中有機酸以外の高分子成分に由来するCODCrが30%以上であることを特徴とする嫌気性処理方法。
- 請求項1ないし4のいずれか1項において、前記担体の大きさが1.0~5.0mmであり、沈降速度が200~500m/hrであることを特徴とする嫌気性処理方法。
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WO2014156216A1 (ja) * | 2013-03-27 | 2014-10-02 | 栗田工業株式会社 | 嫌気性処理方法 |
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