KR20130065891A - Method for treating organic wastes - Google Patents

Abstract

PURPOSE: A method for treating organic waste is provided to carry out aerobic biological treatment with lower concentrated dehydrated filtrate. CONSTITUTION: A method for treating organic waste comprises a preprocess step, a step to treat the first biological aerobe and a step to treat the second biological aerobe. In the preprocess step, organic waste without contaminants is reacted with a mixture comprising fly ashes and calcium minerals or calcium comprising minerals, neutralized and dehydrated. Dehydrated cake is sent to an anaerobe digesting process, a process to be fertilized or liquefied. The filtrate is sent to the step of treating the first biological aerobe. [Reference numerals] (A1) Organic waste; (A10) Polymer coagulant; (A2) Discharged water anaerobic digestion process fermentation liquid from composting process; (A22) Treated water(discharge); (A3) Mineral containing calcium; (A4) Coal line; (A5) Sulfuric acid; (A6) Discharged water from composting process; (A7) Fermented liquid from anaerobic digestion process; (A8) Brine; (A9) Coagulant; (B1) Dewatered cake; (B10) Dewatered remaining liquid; (B2) Dewatered remaining liquid; (B3) Dewatered cake; (B4) Dewatered remaining liquid; (B5) Remaining waste; (B6) Remaining waste; (B7) Removal; (B8) Dewatered cake; (B9) Deposited sludge; (CC) Dewatering process; (DD) Storage tub; (EE) Crushing and foreign material selecting process; (FF) Mixing process; (GG) First dewatering process; (HH) Composting process or anaerobic digestion process; (II) Mixing and neutralizing process; (JJ) Second dewatering process; (KK) Water collecting tub; (LL) First aerobic living thing processing step; (MM) Second aerobic living thing processing step; (NN) Oxidation sterilizing process; (OO) Coagulation sedimentation process; (PP) Filtering process; (QQ) Third dewatering process

Description

Method for treating organic wastes

The present invention relates to a method for treating organic waste, and more particularly, to wastewater, livestock manure, wastewater having high organic matter concentration discharged from industrial plants, landfill leachate, slaughterhouse waste, food processing plant waste, and agricultural and marine product processing processes. Organic waste containing one kind of high concentration organic matter among the discharged waste, food waste, sewage treatment sludge, industrial waste landfill leachate (collectively referred to as "organic waste" It is about how to handle).

Generally, nutrient, livestock manure, wastewater with high organic concentrations from industrial plants, landfill leachate, slaughterhouse waste, food processing plant waste, waste from agricultural and aquatic product processing, food waste, sewage treatment sludge For the treatment of organic wastes containing high concentrations of organic matter, such as the first anaerobic digestion (anaerobic fermentation) treatment and the second aerobic biological wastewater treatment (active sludge treatment), however, in order to increase the efficiency of the first anaerobic digestion treatment, High rate anaerobic digestion should be performed by heating it to around 55 ℃, in which case there is a problem of high energy cost, and the second anaerobic biological treatment without injecting dilution water due to the high organic load of the first anaerobic digestion solution. When activated sludge treatment) there is a problem that is not treated within the emission standard value.

In the case of organic waste such as slaughterhouse waste, waste from agricultural and aquatic product processing, food waste, and livestock manure, a moisture control agent (swelling agent) is injected to a compost with moisture content in the range of 60wt%. There is a problem that the cost of the regulator is high.

Therefore, the above-mentioned organic wastes do not have any special measures, and most of them are dumped at sea, causing serious coastal pollution. In the future, an international agreement to prohibit dumping at sea should find a reasonable method of treating high-concentration organic waste. Is in.

In Patent Document 1, a method of acid fermentation and methane fermentation using a bio-reactor is proposed, and Patent Document 2 discloses a method for treating solid organic wastes such as citrus by-products and foods. A method consisting of a primary anaerobic fermentation apparatus for fermentation and decomposition, a secondary organic acid fermentation apparatus for decomposing products using acetic acid fermentation, and a solid-liquid separator for separating sludge and liquid from the product which has passed through the secondary organic acid fermentation apparatus are presented. In Patent Document 3, organic waste such as food waste and animal waste is pulverized, organic acid generating, sterilizing, performing methanation, and methane storage. Although a number of patented technologies have been proposed, there is no method for advanced treatment of treated water. It flew there are problems such as facility cost and maintenance cost is high.

Non-Patent Document 1 presents the characteristics of technology for producing biomethane from livestock manure, waste sludge, food waste, etc., domestic and overseas technology development and market trends. In Non-Patent Document 2, anaerobic integrated treatment of sewage sludge and food waste is presented. The characteristics of biogas production according to the food waste content of the city are presented, and the organic sludge fueling technology is presented in Non-Patent Document 3, and other papers and seminar presentation data are presented, but the characteristics and status of organic wastes are simply presented. There is only one technique, but the prior art, and the rational treatment of organic waste has not been proposed.

[Patent Document 1] Korean Patent Registration No. 10-1023684, Organic Waste Treatment Method (March 14, 2011) [Patent Document 2] Korean Patent Registration No. 10-0964031, Solid Organic Waste Treatment System and Its Treatment Method (June 08, 2010) [Patent Document 3] Korean Patent Registration No. 10-0513819, Treatment of Organic Waste (September 03, 2001)

[Non-Patent Document 1] Jung, Young-Young, Biomethane Conversion Technology of Organic Waste Resources, Industrial Chemistry Prospect, Vol. 11, No. 3 (2008) [Non-Patent Document 2] Lee, Byung-Seon, Nam, Sang-Chul, Nam Gung-Wan, Evaluation of Biogas Production Efficiency According to Food Waste Content in Single Phase Anaerobic Integrated Treatment of Sewage Sludge and Food Waste Using Mechanical Pretreatment, Journal of Korean Society for Waste Resources and Circulation, Vol. 28, No. 6 , pp. 648-660 (2011) [Non-Patent Document 3] Song, Han-Chul, Hyun-Tae Jung, Eun-Bak Park, Organic Sludge Fuel Technology, Organic Resources, Vol. 16, No. 1, pp. 20-22 (2008)

The present invention is a wastewater, food waste, sewage treatment sludge (sludge), industrial wastes, wastewater, slaughterhouse wastes, food processing plant wastes, organic wastes with high concentrations of organic matter discharged from industrial plants, livestock manure, industrial plants Organic wastes such as landfill leachate and organic wastes having high water content are reacted with a mixture of coal ash, calcium-containing minerals or calcium-containing minerals to solidify the liquid fatty acid, water-soluble organics and salts, and then dehydrated to obtain organic concentrations (BOD and The dehydrated filtrate, which has low COD), is subjected to two-stage aerobic biological treatment and is highly treated below the discharge standard. The dehydrated cake with reduced capacity is injected with a microbial microbial agent that produces hydrolase. Liquefied at a high temperature of 50-60 ℃ and then subjected to anaerobic fermentation, and the methane gas generated as a fuel And recycling to, or manure (液肥) or composting of solid phase there is provided a method for processing organic waste.

The present invention is a wastewater, food waste, sewage treatment sludge, waste landfill, wastewater, slaughterhouse waste, food processing plant waste, agricultural and aquatic product processing process, high concentration of organic matter discharged from industrial waste, livestock manure In the treatment of organic waste with high concentration of water and one type of organic matter in leachate,

When the organic waste flows into the storage tank, the crushing and foreign substances are sorted, and then dehydrated in the first dehydration process, and the dehydration cake is sent to anaerobic digestion, composting or liquefaction, and the dewatering filtrate of the first dehydration process is coal ash and calcium. After reacting with the mixture containing minerals or minerals containing calcium, neutralization is sent to the secondary dehydration process, and the dehydrated cake is sent to the anaerobic digestion, composting or liquefaction process, and the dehydration filtrate is the first aerobic biological treatment process. Or, if the organic waste is introduced into the storage tank, the first dehydration step is skipped, and the organic waste from which crushed and debris is sorted is mixed with coal ash and calcium-containing minerals or neutralized after the reaction with calcium-containing minerals. Dehydrated cake by sending it to the second dehydration process, anaerobic digestion process, composting process or liquid A pretreatment step sent to the sparking process, and the dehydration filtrate of the second dewatering process is sent to the first aerobic biological treatment process;

Send the dewatered filtrate of the second dehydration process to the first aerobic biological treatment process, or send the first aerobic biological treatment water to the second aerobic biological treatment process after the water reforming treatment to the first aerobic biological treatment process Biological processing steps,

The first aerobic biological treatment water is a second aerobic biological treatment water treated in the second aerobic biological treatment process is discharged or the second aerobic biological treatment step to send to the oxidation and sterilization tank of the final waste water treatment process,

The second aerobic biological treatment water is the final wastewater treatment step of effluent is sequentially treated by oxidation / sterilization treatment, neutralization treatment, flocculation / sedimentation treatment, filtration treatment, and

The anaerobic digestion water treated by the liquefaction, anaerobic digestion, magnesium salt reaction, neutralization, flocculation, sedimentation, and dehydration treatment was sequentially treated in the first and second dehydration processes of the pretreatment step. Anaerobic digestion step sent to the first aerobic biological process,

A liquefaction step of liquefaction and liquefaction of the dehydrated cake dehydrated in the first and second dehydration processes of the pretreatment step to make a liquid ratio;

The dehydration cake dehydrated in the first and second dehydration process, the dehydration cake discharged from the dehydration process of the anaerobic digestion step, the dehydration cake discharged from the dehydration process of the liquefaction step by injecting a moisture control agent (swelling agent), soil improving agent A composting step of fermenting and maturing the mixed treatment to make ripe compost,

It is characterized in that the deodorizing treatment step of deodorizing treatment by sequentially processing biological deodorization treatment, chemical deodorization treatment by collecting the malodorous substance at the point where the odor occurs in each treatment process.

The present invention solidifies liquid fatty acids, water-soluble organics, and salts by reacting organic wastes with high moisture content and organic wastes with coal ash and a mixture of calcium-containing minerals or calcium-containing minerals. Low abundance (BOD and COD) has the effect of being able to perform advanced treatment below the emission standard when aerobic biological treatment is performed, while dehydrated cake has a reduced capacity, so the cost of facility and operation is lower in anaerobic fermentation, liquefaction, or composting. It is expected to be widely used for organic waste treatment.

1 is an organic waste treatment process diagram
2 is a pretreatment step flow chart
Figure 3 is a first aerobic biological process step flow chart
Figure 4 is a second aerobic biological treatment step and final wastewater treatment step process diagram
5 is anaerobic digestion process step chart
6 is a liquefaction step process chart
7 is a composting process chart
8 is a deodorizing treatment step process diagram

The present invention is a wastewater, food waste, sewage treatment sludge, waste landfill, wastewater, slaughterhouse waste, food processing plant waste, agricultural and aquatic product processing process, high concentration of organic matter discharged from industrial waste, livestock manure The present invention relates to a method for treating organic waste having a high concentration of one organic matter and a water content in leachate, which will be described in detail with reference to the accompanying drawings. And in the present invention, "parts" indicating the ratio of mixing means "parts by weight" unless otherwise specified.

Ⅰ. Pretreatment stage

1. Crushing and foreign material selection process

One of the effluent, livestock manure, wastewater with high organic concentration from industrial plants, slaughterhouse waste, food processing plant waste, wastes from agricultural and aquatic product processing, food waste, sludge, landfill leachate When organic wastes with high concentrations of organic matter and high moisture content flow into the organic waste storage tanks, they are shredded and screened with foreign materials, and then sent to calcium minerals, coal ash and reactor 100, or dehydration process. send.

2. Primary dewatering process

In the case of composting the dehydrated cake, the organic waste removed from the shredding and debris sorting process is preferably sent to the first dehydration step and the dehydrated cake is sent to the composting step. Send to). The dehydrated cake can be sent to the liquefaction process or anaerobic digestion process.

In addition, organic waste having a high salt concentration, such as food waste and food factory discharge waste, is preferably sent to an anaerobic fermentation process because dehydrated cakes may cause salt damage when composted.

Although the efficiency of dehydration is somewhat reduced, this primary dehydration process can be omitted for cost reduction, and organic wastes from the crushing treatment of large substances and selected foreign substances can be sent to calcium minerals, coal ash and reaction processes for treatment.

The dehydrator of the primary dehydration process, a centrifugal dehydrator, screw press, vacuum dehydrator, pre-coat vacuum filter, filter press , Belt press, Vibrating screen or rotating trommel screen can be selected and used. The dehydrator of the first dehydration process, using a screw press (Screw press) It is preferable to, but the type of dehydrator in the present invention is not particularly limited.

2. Calcium mineral and coal ash and reaction process

Organic wastes with high salinity and higher fatty acids, such as food waste and food processing plant waste, are difficult to biodegrade and have a salt problem when composted. Therefore, it is necessary to first remove salts and higher fatty acids.

The inventors of the present invention have studied diligently and found that salts, higher fatty acids, and organic substances are simultaneously converted into water-insoluble solid substances when reacted with calcium mineral and coal ash mixtures.

Most organic wastes contain higher fatty acids such as stearic acid, oleic acid, linoleic acid, linolenic acid, and palmitic acid. When a large amount of wastewater or wastewater is supplied to a biological wastewater treatment process, the microbial floc is aggregated and a film is formed to inhibit the metabolic activity. There is a problem with this, so it must be removed.

In addition, organic wastes such as food waste and food waste are not only high in the content of high fatty acids, but also have high salt concentrations (NaCl), making them less efficient during biological treatment of wastewater (wastewater), which is a dehydrated filtrate. In the case of composting also causes harm to the crops (惹起), it is necessary to remove the higher fatty acids and salts together.

end. Organic wastes with high fatty acid and high organic concentration

For organic wastes with high fatty acid and high organic matter concentration, hydrated lime, quicklime, calcined dolomite, calcined dolomite, calcined algae calcium and calcined coral powder with high activated calcium (reactive calcium) content When one kind of calcium-containing mineral and organic waste of calcined right bone powder are supplied to the reaction tank 100 together and reacted with stirring with the reaction agitator 101, the higher fatty acid calcium salt is insoluble in water as shown in the following reaction formula ⑴. Is generated.

Higher fatty acid + calcium → higher fatty acid calcium salt (insoluble in water) ... ... ... ⑴

I. For organic wastes with high salt, high fatty acid and organic concentration

Organic wastes having high salt, high fatty acid and organic concentration, such as food waste and food processing plant wastes, are fed coal ash and a mixture of the calcium-containing minerals together with the organic waste to the reaction tank 100, and stirred with a reaction tank stirrer 101. Upon reaction, the higher fatty acid is in the form of the higher fatty acid calcium salt insoluble in water by the same reaction as in Scheme V above.

Salt (NaCl) is an inorganic material solid insoluble in water such as Friedel's salt when reacted with aluminosilicate mineral volcanic ash, coal ash and calcium-containing minerals. As it turns into salt, the salt is fixed and the salt in the water is removed.

The inventors of the present invention have found that salts are adsorbed into volcanic ash as inorganic material solids when seawater is introduced into the volcanic ash area, which is aluminosilicate soil, and is similar to volcanic ash. When the mixture of minerals and calcium-containing minerals were reacted with brine, it became inorganic solids such as Friedel's salt, and the salts were immobilized to remove salts in the water. It is estimated that the salt in water is removed by the reactions of Schemes VII and VII below.

M-Ca + 2NaCl-> M-2Na + CaCl ₂ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⑵

Where M is the body of the mineral.

_{3CaO + Al 2 O 3 + xCaCl} 2 + yH 2 O → 3CaO · Al 2 O 3 · xCaCl 2 · yH 2 O ... ... ... ... ... ⑶

Friedel salt of Scheme ⑶ (Friedel's salt, 3CaO · Al 2 O 3 · xCaCl 2 · yH 2 O) is less than _{0 ℃ 3CaO · Al 2 O 3} · 3CaCl 2 · 30H 2 O that is not normal (安定相) in _{0~28 ℃ 3CaO · Al 2 O 3} · CaCl 2 · 10H ₂ O is not the top, in the _{28~200 ℃ 3CaO · Al 2 O 3} · CaCl 2 · 10H ₂ O is not a top, 200 to 500 in ℃ is not a _{3CaO · Al 2 O 3 · CaCl} 2 · 6H 2 O top, more than 500 ℃ is known that the stability merchant _{3CaO · Al 2 O 3 · CaCl} 2 · H 2 O.

As described above, a calcium-containing mineral is added to the mixing tank 104 at a ratio of 3 to 4 in the ratio of CaO / Al ₂ O ₃ to volcanic ash or coal ash, and mixed with the mixing tank mixer 105. Is supplied to the reactor 100 by the rotary feeder 107. Here, the bag filter (Bag filter, 106) should be installed on the mixing tank 104 to prevent dust generation.

3. Neutralization process

When organic waste reacts with coal ash and calcium mineral mixture, or calcium-containing minerals, the pH becomes alkaline, so it is sent to the neutralization tank 102 and stirred in a neutralization tank stirrer 103 with 10 to 20wt% sulfuric acid (H ₂ SO ₄ Injecting the aqueous solution to neutralize the pH in the range of 6.5 ~ 7.5 to send to the pretreated organic waste storage tank (108).

4. Second dehydration process

The pretreated organic waste storage tank 108 is sent to the secondary dehydration process supply pump 109 to the secondary dehydration process, and the dehydrated cake is sent to the composting process, liquefaction process or anaerobic digestion process, and the dehydration filtrate is first aerobic. Send to the collection tank 200 of the biological treatment step.

The dehydrator of the secondary dehydration process, centrifugal dehydrator, screw press, vacuum dehydrator, pre-coated vacuum dehydrator, compression filter press, belt press, vibrating screen or rotary trommel screen can be selected and used one, Although the dehydrator of a dehydration process uses a crimping filter press, the kind of dehydrator is not specifically limited.

Dehydration cakes from 120 to 150 tons / day of food waste were composted with screw presses and 6 to 7.5 tons / day of dewatering cakes, and 114 to 142.5 tons / day of dewatering filtrates were analyzed. It was like

Determination of Dehydration Filtrate for Primary Dehydration of Food Waste Item BOD ₅
(Mg / l) COD _Mn
(Mg / l) TN
(Mg / l) TP
(Mg / l) Electrical conductivity
(㎳ / cm) density 162,200 137,870 8,200 1,520 48.4

100 kg x 3 food waste dehydration filtrates of Table 1 were mixed with 5 kg, 8 kg, and 10 kg of CaO / Al ₂ O ₃ molar composition ratios of 3.5 parts of coal ash and slaked lime, respectively. Propeller type) After stirring for 1 hour at a rotation speed of 360rpm with an agitator, neutralizing the solution to pH 7.5 with 20wt% sulfuric acid solution and analyzing the components of the dehydrated filtrate which was dehydrated secondly with a laboratory vacuum filter. It was same as contents of 2.

Component analysis table of dehydrated filtrate secondary dehydrated after reaction of food waste with coal ash and slaked lime mixture Item BOD ₅
(Mg / l) COD _Mn
(Mg / l) TN
(Mg / l) TP
(Mg / l) Electrical conductivity
(㎳ / cm) Injection volume of coal and slaked lime mixture 5 kg 1,520 1,290 64.8 12.8 16.2 8 kg 1,140 968 51.8 9.2 15.8 10 kg 860 688 48.2 7.8 12.6

As shown in Table 2, it can be seen that contaminants caused by organic substances such as BOD, COD, TP, and TP react with a mixture of coal ash and slaked lime at 5 wt% or more to organic waste, and thus the treatment efficiency is very high. It can be seen that the salinity is removed to less than 1wt% that the salinity is also slightly lower than the concentration of the salinity contained in the seawater (the electrical conductivity of seawater, 53 kW / cm).

Ⅱ. First Aerobic Biological Process

The dewatering filtrate dehydrated in the second dehydration step of the pretreatment step, the leachate in the composting step, and the dewatering filtrate discharged in the third dehydration step of the liquefaction step (hereinafter, these dewatering filtrates and leachate are collectively referred to as 'waste water'). When supplied to (200), when the half magnetic width value of the nuclear magnetic resonance (NMR) ¹⁷ O-NMR of the wastewater is 90 kΩ or more, it is also referred to as constant voltage treatment. .) And reforming by magnetization, then sent to the first aerobic biological process for treatment, and the nuclear magnetic resonance of the wastewater ¹⁷ half-width of O-NMR. If the value is less than 90㎐, the aerobic biology is omitted. With processing Processes taking.

1. Water reforming process

In the present invention, when the half width value of the nuclear magnetic resonance ¹⁷ O-NMR of the wastewater is 90 kΩ or more, the wastewater is reformed by constant voltage treatment and magnetization to improve the treatment efficiency in the first and second aerobic biological treatment processes.

In the reforming of water, a steel plate having excellent corrosion resistance is installed under the wastewater collecting tank 200, and the inside of the collecting tank 200 is filled with charcoal or activated carbon having high conductivity. The wire mesh electrode 202 which is excellent in corrosion resistance is provided so that it may not contact with a lower steel plate. Then, the steel sheet is grounded to the ground (204h).

When the dewatered filtrate dehydrated in the second dehydration process of the pretreatment step, the leachate of the composting step, the wastewater which is a dewatered filtrate discharged from the third dehydration process of the liquefaction step is supplied to the wastewater collection tank 200, the constant voltage generator 204 When the high voltage AC constant voltage is applied from the transformer 204a to the wire mesh electrode 202 and the voltage of 3,000 to 5,000 volts is applied, the wire mesh electrode 202 is subjected to the constant voltage treatment. When the electrostatic fields of + and-are alternately applied at the center for 4 to 10 hours, this causes the water molecules themselves to vibrate and rotate, and the first reformed wastewater is transferred to the wastewater transfer pump (203). Magnetizer of a constant voltage conductor tube in which a low voltage of AC or DC in the range of 0.5 to 5 Volts is applied to a coil wound around a conductive tube. To the primary aeration tank (206). The.

When the wastewater is supplied to the wastewater collection tank 200, the wire mesh provided with the output line 204g of the secondary coil 204e of the transformer 204a of the constant voltage generator 204 is provided inside the wastewater collection tank 200. Connected to the electrode 202, an incoming power supply of 100 to 220 volts and an AC power source having a frequency of 50 to 60 Hz is applied, and the voltage regulator 204b is adjusted to adjust the voltage of the constant voltage generator 204 to 1,200 to When electrostatic induction treatment is applied while applying 5,000 volts and a constant voltage of 10 to 150 mA for 4 to 10 hours, the surface tension is reduced and the treatment is reformed with water having excellent penetration.

The transformer 204a of the constant voltage generator 204 includes an iron core 204d, a primary coil 204c, a secondary coil 204e, an output line 204g of a secondary coil 204e, and a secondary coil 204e. And the voltage regulator 204b is connected to the primary coil 204c, and the output line 204g of the secondary coil 204e is a wire mesh electrode of the wastewater collection tank 200. 202).

The wastewater is supplied to the wastewater collection tank 200, the output line 204g of the secondary coil 204e of the constant voltage generator 204 transformer 204a is connected, and the insulation treatment terminal of the secondary coil 204e is connected. 204f is insulated in the insulator in the transformer 204a, and the steel plate 201 provided below the wastewater collection tank 200 is also grounded 204h.

At the same time as forming the capacitor C ₂ insulated from the insulation terminal 204f of the high voltage side secondary coil 204e in the transformer 204a in the insulator in the transformer 204a, the wastewater collection tank 200 Condenser C ₁ is formed by connecting to the steel plate 201 provided at the lower portion thereof. As a result, the voltage between the output line 204g and the ground 204h is 250 to 3,200 volts, and the current is 10 to 150 mA. Since it is a weak current of the ground, there is no danger that a person comes into contact with the wastewater collection tank 200.

In electrostatic induction, when a charged material is charged to an electrically neutral material, a charge having a polarity opposite to that of the charged material appears on the surface of the material close to the charged material, and the same charge as the far charged material appears. In addition, even when an electric field exists outside of the charging body, a charge opposite to the external charge appears. The charges appearing at this time are called induced charges. Neutral materials have induced charges, and charges are induced in the material by external electrical action that is not in contact, resulting in polarization of positive and negative charges. This phenomenon is said to be subjected to electrostatic induction, and applying this phenomenon to applying alternating current voltage to a material, rotation and vibration are applied to the molecule of the material, which promotes the dimerization of molecules and changes the physical properties of the material. It's called treatment.

In other words, according to the present invention, the transformer 204a of the constant voltage generator 204 is of an external iron source coil transformer type using an iron core 204d of a stratified layer, and one of the circuits on the primary side of the transformer 204a. The secondary coil 204c is connected to the AC power supply via the voltage regulator 204b to connect the insulation terminal 204f of the first stage of the secondary coil 204e of the secondary side circuit of the transformer 204a in the transformer 204a. At the same time as the insulator was insulated, the output line 204g of the secondary coil 204e of the secondary circuit was applied to the wire mesh electrode 202 installed in the wastewater collection tank 200 at a voltage of 250 to 3,200 volts. When electrostatic induction treatment is carried out with a current of ˜150 mA, small groups of water molecules in the wastewater injected into the wastewater collection tank 200 become small, resulting in less surface tension and better penetration of microorganisms in the biological treatment process. To be active.

The transformer 204a inserts a cylindrical insulating film into the center of the iron core 204d, winds up the primary coil 204c and the secondary coil 204e on the outer circumferential surface of the insulating film, and then the primary coil 204c. ) Is 220-240 volumes using copper wire coated with polyester of 0.6 mm in diameter, and the secondary coil 204e uses copper wire coated with enamel of diameter 0.09 mm, for example. 40,000 times of the secondary coil 204e, but the first secondary coil 204e may be 22,000, and the second secondary coil 204e may be 18,000. The diameter, type and number of turns of the copper wire coil are determined according to the capacity, treatment time, applied voltage, and the like of the wastewater collection tank 200.

In general, such a copper coil may be used in the range of 0.03 to 3 mm, and the copper wire may be formed using polyester or enamel coated copper wire, and the number of turns of the copper wire coil may be 200 to 200 mm. The second coil 204e is set to 28,000 to 40,000 passes, or the first secondary coil 204e is set to 16,800 to 22,000 turns within the secondary coil 204e, and the second secondary coil ( 204e) may be 11,200 to 18,000 volumes.

The insulated terminal 204f of the secondary coil 204e is in the transformer 204a. After winding the tip of the secondary coil 204e with insulating tape, an insulator such as tar pitch is charged into the transformer 204a to make the secondary. Although the insulation process terminal 204f of the coil 204e is covered and insulated, insulator can also use insulation oil, unsaturated polyester, a polyurethane resin etc. besides tar pitch.

When alternating current flows through the transformer 204a and the primary voltage of the transformer 204a is operated by the voltage regulator 204b to adjust the voltage to 100 to 220 volts, the secondary coil 204e terminal on the secondary side Although a voltage of 12,000 to 18,000 volts is generated, since the insulating terminal 204f of the secondary coil 204e is insulated from the secondary circuit, the wire mesh electrode 202 provided inside the wastewater collection tank 200 and The output line 204g is connected, and a voltage of 3,200 to 5,000 volts and a current of 10 to 150 mA flow between the ground 204h.

The above-described voltage of 12,000 to 18,000 Volts generated on the secondary side becomes a voltage of 3,200 to 5,000 Volts and a current of 10 to 150 mA between the wastewater collection tank 200 and the ground 204h. This is caused by the insulation terminal 204f of the secondary coil 204e, the resistance of the insulator, and the AC resistance circuit of the coil.

That is, the resonance circuit is formed by the ground of the constant voltage generator 204 and the ground of the wastewater collection tank 200, and the ground 204h, which is an area of the insulation terminal 204f, which is one end of the secondary coil 204e, and 2 The output line 204g of the difference coil 204e causes the electrostatic induction to occur by the resonance frequency caused by the discharge from the output voltage by the ground 204h.

According to the size of the wastewater collection tank 200 and the size of the wire mesh electrode 202 filled with the filling material, the voltage between the wastewater collection tank 200 and the ground 204h varies from 3,200 to 5,000 volts, and the current is also 10 The voltage and current are varied in the range of ˜150 mA, and the input power is adjusted from the voltage regulator 204b.

As described above, the voltage of the wastewater collection tank 200 generated by the AC resistance circuit is 3,200 to 5,000 volts at no load, but since the current is a weak current in the range of 10 to 150 mA, It is safe and there is no fear of trouble such as electric shock or fire, and the voltage and current applied to the wastewater collection tank 200 are controlled by the voltage regulator 204b according to the charging capacity and electrostatic induction treatment conditions of the tank. However, in a normal case, when the voltage between the wastewater collection tank 200 and the ground 204h is 550-1,600 volts, and the current is in the range of 30-100 mA, an appropriate alternating electric field is generated. Can be configured.

As for the wastewater collection tank 200, when the wire mesh electrode 202 in the wastewater collection tank 200 becomes positively charged, the negative charge is induced on the ground 204h side, and conversely, the wire mesh electrode in the wastewater collection tank 200 When 202 is -charged, + charge is passed from the ground (204h) side, and then, according to the frequency of the AC power, the wastewater collection tank 200 changes + charge and -charge by the frequency (50 to 60 times) for 1 second. In accordance with this, the charge on the ground 204h side is also inherited, and the + and − charges are changed.

In general, matter is formed by atoms, which are composed of atomic nuclei and electrons, which in turn are composed of neutrons and protons, and have a negative charge around the nucleus. In the normal state in which the electrons are in a circular motion and no external electric field is applied, both positive and negative charges of the electrons are stabilized in the same amount, but when a high voltage is applied from the outside, the electrons move by In addition, since both move on the other hand, the electrical centers of the atoms do not coincide, and the atoms form one electric dipole, and an internal electric field is generated by the balance of charge. While causing polarization.

In this case, since the atom is polarized by an external electric field, this is called electron polarization or atomic polarization, and a high constant voltage is applied to the wastewater charged in the wastewater collection tank 200. In this case, all molecules try to comply with the change of positive and negative charges due to electrostatic induction, but there is a difference between strong and weak binding force between molecules, resulting in less viscous and less permeability due to less surface tension of wastewater. It is reformed with activated water.

Nuclear magnetic resonance of influent wastewater ¹⁷ O-NMR half-width is 90- or less, surface tension is 68dyne / cm or less, and BOD ₅ and COD _Mn concentration is lower than 200mg / ℓ. Since the biological treatment can be treated within the discharge standard value, the water reforming process is omitted, and the wastewater of the low concentration wastewater collection tank 200 is supplied to the primary aeration tank 206 of the first aerobic biological treatment process for treatment.

The magnetizer 205 is a constant voltage conductive tube wound around a coil of a cylindrical conductive tube made of an insulating material such as synthetic resin (PVC, PE, styrene resin, etc.), ebony, FRP, and Bakelite. When a low voltage of AC or DC in the range of 0.5 to 5 Volts is applied to the pipe, a magnetic field is formed inside the coil, and when the fluid passes therethrough, the fluid is magnetized.

Here, instead of the magnetizer 205 wound around a constant voltage conductive tube, a permanent magnet magnetizer magnetized in the range of 10,000 to 15,000 gauss magnetic flux density may be used.

2. First Aerobic Biological Process

The first aerobic biological treatment water while supplying air from the blower 213 and aeration when supplying the waste water reformed or unmodified wastewater in the reforming process of the water is supplied to the primary aeration tank 206 Silver is sent to the primary sedimentation tank 207 to precipitate the solids, and the first biological treatment water, which is a monthly flow of overflow, is sent to the secondary aeration tank 300.

Solids (microbial cells) precipitated in the primary settling tank 207 are collected by the primary settling tank 207 by the primary return pump 209 when collected in the central cone portion of the lower portion of the first settling tank 207. A primary microorganism activator 210 incorporating a primary bioreactor 211 filled with an activated humic substance pellet and a filler 212 of a mineral containing an active mineral component; The surplus sludge discharged while being conveyed to the primary aeration tank 206 is sent to the secondary aeration tank 300 and the biological deodorization tower 701 of the deodorization treatment step.

If the overflowing overflow of the primary settling tank 207 of the primary biological treatment is treated within the discharge standard value, or treated in conjunction with a nearby sewage treatment facility, it is sent to the final treatment tank.

When the first microorganism activation tank 210 is supplied with sludge, which is solid matter (microbial cells) precipitated in the primary precipitation tank 207 by the primary transfer pump 209, the primary microorganism activation tank 210. Blower 213 under the primary bioreactor 211 filled with air from the blower 213, the primary microbial activator 210 and the filler 212 of the mineral containing minerals and the active corrosion material pellets. When air is supplied from the air, the return sludge is air-lifting the layer of the filler 212 of the primary bioreactor 211, and the active bacillus Bacillus mycoides (Bacillus) is active when sufficient mineral components are supplied Polyphenol compounds, such as mycoides, Bacillus luteus, Aspergillus niger, and actinomycetes, are excreted as metabolites to produce water-soluble organics by corrosive reactions. Corrosion insoluble in water Corrosive microorganisms converting into substances or corrosive substances and microorganisms in symbiotic relationship with these microorganisms are activated and sent to the primary aeration tank (206) for the entire aerobic biological wastewater treatment system. Corrosive microorganisms and microorganisms in symbiotic relationship with these microorganisms are induced to treat wastewater by the corrosive reaction.

Microorganisms that produce corrosive substances by corrosive organic substances have high mineral content in the cytoplasm or cell wall, and these microorganisms have active metabolism when ingested enough minerals, so that Bittern ) Is preferably supplied to the primary microorganism activation tank 210. At this time, the water is supplied to 0.001 to 0.01 parts by weight of the first microbial activation tank 210 per 100 parts by weight of wastewater introduced.

Microorganisms that corrode the organic materials to produce corrosive substances are active metabolism when ingested sufficient mineral components.

When the wastewater was treated by the corrosion reaction, odor generating substances such as ammonia (NH ₃ ), hydrogen sulfide (H ₂ S), mercaptans, indole, scartol, and volatile amines It is assimilated with non-volatile and insoluble corrosion precursors or corrosive substances, and it has the effect of suppressing odor.In addition, water-soluble organic substances are treated with highly assimilated corrosion precursors or corrosive substances which are insoluble in water. This is a high feature.

The capacity of the primary aeration tank 206 is determined by the following formula in the F / M ratio (Food / Microorganism ratio) in the range of 0.05 to 0.4, and the depth is in the range of 2 to 6 m.

F / M = (BOD ₅ × Q) / (MLSS × V) [kg BOD / m 3 .day]. ... ... ... ... ... ... ... ... ... ⑷

Where BOD ₅ is the daily biological oxygen demand of the influent wastewater (mg / ℓ), V is the volume of the aeration tank (Volume, m3), MLSS is the concentration of mixed liquor suspended solids (mg / ℓ), Q Is the flow rate of the influent wastewater (m 3 / day).

The surface area of the primary sedimentation tank 207 is a surface area with a margin in consideration of the overflow load of 8 to 25 (m 3 / m 2 · day) and the solid load of 60 to 90 (kg / m 2 · day). The depth is 3-6 m.

The flow rate returned from the primary settling tank 207 to the primary aeration tank 206 and the primary microbial activation tank 210 by the primary transfer pump 209 is mixed liquor suspended solids in the primary aeration tank 206. ) Is determined by the following formula so that the concentration of c) is in the range of 2,000 to 3,500 mg / l.

R = Qr / Q = (MLSS-SS) / (R-MLSS)... ... ... ... ... ... ... ... ... ... ... ... ⑸

Where R is the return rate (%) to return from the primary settling tank 207 to the primary aeration tank 206 and the primary microbial activation tank 210, Qr is the flow rate to return (㎥ / day), Q is the flow rate of the influent wastewater (Mg / l), MLSS is the mixed liquid suspended solids concentration (mg / l) in the primary aeration tank 206, SS is the suspended solids concentration (mg / l) contained in the influent wastewater, R is the suspended solids concentration ( Mg / l).

The flow rate supplied to the primary microorganism activating tank 210 supplies 8-20% of the flow rate of the whole return sludge, the capacity of the primary microorganism activating tank 210 makes the residence time 0.5 to 2 days, and 1 The filling 212 filled in the primary bioreactor 211 contains 5 to 10 kg of active corrosive material pellets per 10 m3 / day and active mineral components supplied to the primary microorganism activation tank 210. Charge 10-20 kg of one mineral.

The amount of air supplied from the blower 213 to the primary aeration tank 206 and the primary microbial activation tank 210 is such that dissolved oxygen concentration is maintained at 2 to 4 mg / l in the primary aeration tank 206. The amount of air supplied to the lower part of the primary bioreactor 211 is 1.5-3.5 Nm 3 -Air / m 2 · hour of aeration intensity. The discharge pressure of the blower 213 is determined in consideration of the static head according to the depth of the tank and the friction head according to the frictional loss of the pipe.

If the discharge standard value of the treated water is not a clean area and the discharge standard value of BOD ₅ , COD _Mn , SS, etc. is high, the case where the primary biological treated water is treated within the discharge standard value or when the sewage combined treatment is performed is as follows. The second biological treatment step of the low concentration wastewater is omitted, and the overflowed monthly water from the primary sedimentation tank 207 is sent to the biological treatment tank 525.

Ⅲ. Second Aerobic Biological Process

1. Second Aerobic Biological Process

When the primary biological treatment water is supplied to the secondary aeration tank 300, the treated water is supplied to the secondary aeration tank 301 by supplying air from the blower 213 to precipitate the solids, and the overflowed secondary water is the overflowed second water. The treated water is discharged or sent to the oxidation sterilization tank 400 of the final wastewater treatment step when advanced treatment is required.

Solids (microbial cells) precipitated in the secondary settling tank 301 are collected by the secondary return pump 303 when the solids (microbial cells) are collected by the secondary settling tank 302 into the central cone portion of the lower portion of the secondary settling tank 301. The secondary bioreactor 305 filled with the active corrosive pellets and the filler 306 of the mineral containing the active mineral component is returned to the secondary microbial activation tank 304 and the secondary aeration tank 300.

In the case of initial or abnormal operation of the secondary biological treatment process, the surplus sludge discharged from the primary biological treatment process is sent to the secondary aeration tank 300 and the secondary microbial activation tank 304 to operate in a normal state. The supply of surplus sludge discharged from the primary biological treatment process to the secondary aeration tank 300 and the secondary microbial activation tank 304 is stopped.

And the surplus sludge discharged from the second biological treatment is sent to the biological deodorization tower 701 of the deodorization treatment step or the storage tank for storing the organic waste together with the surplus sludge discharged from the primary biological treatment.

In the secondary microorganism activation tank 304, the secondary microorganism activation tank (2) is conveyed to the secondary aeration tank 300, the sludge which is solid precipitated in the secondary precipitation tank 301 by the secondary transfer pump 303 ( 304). When sludge as a solid precipitated in the secondary precipitation tank 301 is supplied to the secondary microorganism activation tank 304, air is blown from the blower 213 to the lower portion of the secondary bioreactor 305 and the lower portion of the secondary microorganism activation tank 304. When aeration is supplied, minerals are supplied to aquatic sludge (microbial cells), and as in the first biological treatment process, Bacillus mycoides, Bacillus luteus, Aspergillus niger, Actinomycetes Exclusion of polyphenol compounds as metabolites (代謝 産物), such as (放 線 菌) is sent to the secondary aeration tank (300) by activating the predominantly cultured microorganisms that corrode organic matter. In this way, activating corrosive microorganisms that convert organic matter into insoluble water or corrosive substances insoluble in water and microorganisms in symbiotic relationship with these microorganisms are sent to the secondary aeration tank (300). The whole biological treatment system also leads to the treatment of wastewater by the corrosive reactions by the corrosive microorganisms and microorganisms in symbiosis with these microorganisms.

Microorganisms that produce corrosive substances by corrosive organic substances have high mineral content in the cytoplasm or cell wall, and these microorganisms have active metabolism when they ingest sufficient minerals. It is preferable to supply 0.001 to 0.01 parts by weight per 100 parts by weight of wastewater from which the water is introduced into the secondary microorganism activation tank 304 of the treatment step.

The capacity of the secondary aeration tank 300 is determined by the above formula in the food / microorganism ratio (F / M ratio) in the range of 0.05 to 0.4, the depth is in the range of 2 to 6m, the surface area of the secondary settling tank (301) The surface area of the bath is considered to be sufficient in consideration of the overflow load of 15 to 25 (m 3 / m 2 · day) and the solid load of 60 to 90 (kg / m 2 · day). Is 3 to 6 m.

The flow rate returned from the secondary settling tank 301 to the secondary aeration tank 300 and the secondary microbial activation tank 304 by the secondary conveying pump 303 is MLSS (Mixed liquor suspended) in the secondary aeration tank 300. The concentration of solids) is determined by the above formula so that the concentration is in the range of 2,000 to 3,500 mg / L.

The flow rate supplied to the secondary microorganism activation tank 304 also supplies 8 to 20% of the flow rate of the entire returned sludge, and the capacity of the secondary microorganism activation tank 304 is set at a residence time of 0.5 to 2 days. The filler 306, which is also filled in the primary bioreactor 305, contains 5 to 10 kg of active corrosive material pellets per 10 m 3 / day of flow rate supplied to the secondary microorganism activator 304, and mineral 10 containing an active mineral component. Charge 20 kg.

As the mineral containing the active mineral component, one of Rhyolite or Dacite-like Pumice, Pegmatite or Perlite is used.

The active corrosive pellets are processed into pellets by mixing marine diatoms and marine plants, and mixing them with caking additives such as bentonite and high humic acid, which have a high content of fulvic acid. Buy and use a commercial product.

The amount of air supplied from the blower 213 to the secondary aeration tank 300 and the secondary microbial activation tank 304 is that dissolved oxygen concentration of the secondary aeration tank 300 and the secondary microbial activation tank 304 is increased. It is supplied so that 2-4 mg / L is maintained, and the air supplied to the lower part of the secondary bioreactor 305 shall have an aeration intensity of 1.5-3.5 Nm <3> -Air / m <2> / time. The discharge pressure of the blower 213 is determined in consideration of the static head according to the depth of the tank and the friction head according to the frictional loss of the pipe.

The nuclear magnetic resonance ¹⁷ O-NMR value of the half width of the dehydrated filtrate of 100 kg of food waste of Example 1 reacted with 8 kg of a mixture of coal ash and slaked lime was 128 으나. Omitted only aerobic biological treatment.

 Inject a 20 liter dehydration filtrate reacting 8 kg of coal ash and slaked lime mixture into a container to 100 kg of food waste of Example 1, and injecting sludge in a process of aerobic activated sludge treatment of food waste dewatering filtrate to MLSS (Mixed Liquor). Suspended Solids (3,452 mg / ℓ) to the dissolved oxygen (Dissolved oxygen) concentration of 2 mg / ℓ by injecting aeration while the aerobic treatment results were as shown in Table 3 below.

Anaerobic Biological Treatment Result Analysis Processing time
(time) BOD ₅
(Mg / l) COD _Mn
(Mg / l) TN
(Mg / l) TP
(Mg / l) SS
(Mg / l) 24 252 320 48.2 7.5 45.8 48 113 158 45.2 6.8 54.6 72 76 102 42.3 6.2 58.3 96 57 82 40.5 5.7 61.2

As shown in Table 3, BOD ₅ , COD _Mn, and TP can be treated below the emission standard without using dilution water when treated with aerobic biological treatment for 4 days or more, but TN alone is susceptible to poor treatment efficiency. , SS) concentration is a phenomenon that the sludge (microorganism) is increased as the treatment time passes, the production of pin floc (Pin floc) increases, the SS concentration increases.

IV. Final Wastewater Treatment Stage

When the treated water treated in the second aerobic biological treatment step is to be treated highly, the oxidized and sterilized material is neutralized, aggregated and precipitated, and then discharged after filtration.

1. Oxidation and Sterilization Process

When the treated water treated in the second aerobic biological treatment process is supplied to the oxidation / sterilization tank 400, the oxidizing agent (H ₂ O ₂ , NaClO, O ₃ , ClO ₂ , Cl ₂ ) and the divalent iron salt (FeSO ₄ , FeCl ₂ ) Is injected in the range of Oxidation-reduction potential value of + 700 ~ + 1,100㎷, and stirred with oxidizing / sterilization agitator 401 for 30 ~ 60 minutes to produce highly oxidative hydroxyl group (Hydroxyl radical, OH · ) Is generated and the untreated organic material is decomposed, and microorganisms such as bacteria and viruses are sterilized and sent to the neutralization tank 402. The reaction taking place is as follows.

^{_{Fe 2 + + H 2 O 2}} → Fe 3 + + OH · + OH - ... ... ... ... ... ... ... ... ... ... ... ... ... ⑹

Organic substance + OH->R-COOH->. → CO ₂ + H ₂ O... ... ... ... ... ... ... ... ⑺

In addition to the oxidation and sterilization treatment method using the oxidizing agent, the oxidation and sterilization treatment by ultraviolet irradiation, the oxidation and sterilization treatment by electrolytic oxidation, and the oxidation and sterilization treatment by electron beam irradiation may also be applied.

2. Neutralization process

When the product treated in the oxidation / sterilization process is supplied to the neutralization tank 402, the neutralizing agent (Ca (OH) ₂ , an aqueous solution of NaOH) is supplied in a pH range of 6.5 to 8 while stirring with the neutralization agitator 403. The neutralized treatment is supplied to the coagulation tank 404. The reaction taking place is as follows.

Fe ^{3 ++} 3NaOH → Fe (OH) ₃ + 3Na ⁺ ... ... ... ... ... ... ... ... ... ... ... ... ... ⑻

3. Coagulation and Sedimentation Process

In the genital neutralization process, when the pH of the wastewater neutralized in the range of 6.5 to 8 is supplied to the coagulation tank 404, the solids are aggregated while stirring with the coagulation tank stirrer 405 to facilitate precipitation in the tertiary precipitation tank 406. Aggregate in a floc state and send to the tertiary settling tank 406.

And when supplied to the tertiary sedimentation tank 406, the solids in the floc (Floc) state is settled to the lower portion of the tertiary sedimentation tank 406, the intermediate treated water flowing over the tertiary sedimentation tank 406 to the intermediate treatment tank (409) Sludge precipitated in the lower part of the third settling tank 406 is collected by the settling tank central cone part by the third settling tank 407 to the third dewatering process by the sludge feed pump 408. send.

4. 3rd Dehydration Process

The sludge settled below the third settling tank 406 is supplied to the dehydrator of the third dehydration process by the sludge transfer pump 408, and the dehydrated dehydrated cake is disposed of because of high inorganic concentration, and the dewatered filtrate is an intermediate treatment tank. (409).

5. Filtration Process

The intermediate treated water supplied to the intermediate treated water tank 409 is sent to the filter 411 by the filter feed pump 410, and the filtered filtrate is sent to the final treated water and discharged.

The filter medium 412 filling the filter fills activated carbon when the organic matter concentration (BOD and COD) is higher than expected, and sand when only the solid matter is a problem.

In Example 2, the result of analyzing the filtrate of the treated water treated with aerobic biological treatment for 96 hours by filter paper was as shown in Table 4 below.

Analysis of the Components of Filtrate Filtrated Filtrate Treated Water with Aerobic Biological Treatment BOD ₅
(Mg / l) COD _Mn
(Mg / l) TN
(Mg / l) TP
(Mg / l) SS
(Mg / l) 12 28 8.6 2.1 8.2

As shown in Table 4, wastewater with high concentrations of organic matter discharged from nutrients, livestock manure and industrial plants, landfill leachate, slaughterhouse waste, food processing plant waste, waste discharged from agricultural and aquatic product processing, food waste and sewage treatment Dehydrated filtrate of organic waste with high organic concentration and water content, such as sludge and industrial waste landfill leachate, is reacted with minerals mixed with coal ash and calcium-containing minerals, and then subjected to aerobic biological treatment, followed by oxidation, sterilization, neutralization and aggregation. It can be seen that the sedimentation and filtration treatments can be treated below the emission standard if they are selectively treated according to the water quality of the aerobic biological treatment water.

Ⅴ. Anaerobic Digestion Stage

1. Liquefaction Process

The complex microbial fungus which supplies the dehydration cake discharged from the 1st and 2nd dehydration process of a pretreatment stage to a liquefaction tank 500, and produces a hydrolase while stirring by the liquefaction tank mixer 501. Vi), and while supplying a heat source from the boiler to adjust the temperature to 50-60 ° C., injecting air from the blower 213 to produce dissolved oxygen in a weak aerobic state in the range of 0.2-0.4 mg / l. After 2 days of treatment, the organic solids are liquefied. The liquefied high concentration organic waste is sent to the liquid high concentration organic waste storage tank 504, and the non-liquefied inorganic solid sludge is sent to the third dehydration process by the solids transfer pump 506.

Here, the microbial agent is amylase that hydrolyzes polysaccharides (starch), lysozyme, galactosidase, protease that breaks down protein, lipase that breaks down fat, and fiber A microbial complex of microorganisms producing hydrolase (Hydrolase) such as cellulase, hemicellulase to break down is used.

In other words, Bacillus subtilis, Bacillus licheniformis, Bacillus polyfermenticus, Bacillus mesentericus, Bacillus mycoides Bacillus sp., Such as Bacillus stearothermophilus, Geobacillus stearothermophilus, Anoxybacillus, Lactobacillus acidophilus, Lactobacillus bifidus and Lactobacillus bifidus Lactobacillus sp., Such as Lactobacillus rhamnosus, Lactobacillus thermophilus, Trichoderma viride, Trichoderma reesei, Trichoderma reesei Matrichoderma longgi brachiatum (Trichoderma longibrachiatum) tricot dermaha Trichoderma sp., Such as trichoderma harzianum, Trichoderma penicillatum, Aspergillus oryzae, Aspergillus niger Aspergillus sp., Rhizopus oryzae, such as Aspergillus oryzae, Aspergillus usamii, Aspergillus fumigatus Rhizopus sp., Such as Rhizopus nigricans, Rhizopus oligosporus, Rhizopus japonicum, Humicola insolens, and Saccharo Saccharomyces cerevisiae, Clostridium butyricum, Clostridium thermosaccharolyticum, Streptococcus faecalis facilis, Streptococcus thermophilus, Streptococcus faecium, Streptomyces thermophilus, Thermoerobacter subterraneus Use microbial fungi.

In addition, the microbial fungus used in the present invention is not particularly limited to the microbial species, microorganisms other than the above-mentioned microorganisms amylase, protease, lipase, cellulase, hemicellulase A complex microbial bacterium containing aerobic microorganisms capable of growing at high temperatures of 50 to 70 ° C. that produces hydrolase in metabolites (代謝 産物) can be used.

And heating from the boiler to the liquefaction tank 500 does not need to continuously supply the heat source from the boiler because the temperature rises as the organic matter is aerobic decomposition when heated to 50 ℃ or more only in the initial operation, if the temperature rises over 60 ℃ blower ( The amount of air injected from 213) should be reduced to slow down the decomposition reactions of organics to lower the temperature.

2. Anaerobic Fermentation Process

First, when the mechanism of anaerobic fermentation of liquefied high concentration organic wastes is examined, the liquefied organic wastes occur in three stages: acid fermenter, acid decay, and alkaline fermenter. .

 In the acidic fermenter, the carbohydrates contained in the organic waste liquid are decomposed to become low molecular organic acids. In this stage, the pH drops to around 5 While strong odor (腐敗 臭) occurs. For example, the reaction occurs as shown in the following formula (Glucose).

C ₆ H ₁₂ O ₆ —acid-producing bacteria → 3CH ₃ COOH... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⑼

In the acidic decay group, the decomposition of proteins occurs to form ammonia, amine, and carboxylic acid, and the organic acid generated in the reaction is neutralized and degraded. The resulting pH rises to 6-6.5.

Protein → NH ₄ HCO ₃ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⑽

CH₃COOH + NH₄HCO₃ → CH₃COONH₄ + H₂O + CO₂ ... ... ... ... ... ... ... ... ... ... ... ⑾

The alkaline fermenter is the final stage of anaerobic fermentation, in which the lower organic acid is decomposed to NH ₄ ⁺ by methane forming bacteria. At this stage, the BOD decreases and the pH rises to around 7.5.

CH ₃ COONH ₄ + H ₂ O—methane bacteria → CH ₄ + NH ₄ HCO ₃ . ... ... ... ... ... ... ... ... ... ... ... ⑿

CH ₃ COOH-methane bacteria → CH ₄ + CO ₂ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⒀

The methane bacteria are organized anaerobic bacteria (Methophilic bacteria) active in the temperature range of 30 ~ 36 ℃ and thermophilic bacteria active in the temperature range of 50 ~ 57 ℃ The BOD of the anaerobic fermented leachate by methane fermentation bacteria is high, however, the residual organic matter is high, so post-treatment such as aerobic biological treatment is required.

In the present invention, the first anaerobic fermentation tank 507 in which acidic fermentation and acid decay are generated using the above-described organic waste anaerobic fermentation mechanism, and a secondary anaerobic fermentation tank 509 of an alkaline fermenter in which methane gas and carbon dioxide are generated. The fermentation temperature is maintained in the range of 50 ~ 60 ℃ and it is a process that can cause high rate digestion by two-stage fermentation. Details are as follows.

end. First anaerobic fermentation process

When the liquefied high concentration organic waste is supplied to the liquid high concentration organic waste storage tank 504, it is sent to the first anaerobic fermentation tank supply pump 505 to the first anaerobic fermentation tank 507 while maintaining the temperature in the range of 50 to 60 ℃ primary anaerobic While fermenting with a fermentor stirrer 508, the primary fermentation is carried out to an acidic fermenter and an acidic decay machine, and then to a secondary anaerobic fermenter 509, which is an alkaline fermenter. send.

I. Second anaerobic fermentation process

In the first primary anaerobic fermentation process, the first fermentation broth produced by organic acid fermentation is transferred to the second anaerobic fermentation tank 509, and methane decomposed as lower fatty acids are decomposed into lower fatty acids by CO ₂ and CH ₄ . Gas (CH ₄ ) and carbon dioxide (CO ₂ ) is sent to the methane gas storage tank 512, the sludge deposited in the lower portion of the secondary anaerobic fermentation tank 509 is a magnesium reaction tank to the fermentation sludge transfer pump (513) 514, and the anaerobic fermentation water flowing over the second anaerobic fermentation tank 509 is sent to the collection tank 200 of the first aerobic biological treatment step, or to the magnesium reaction tank 514.

The methane gas stored in the methane gas storage tank 512 is used as a boiler, fuel for heating, and the like.

Looking at the operating conditions and design conditions of the anaerobic fermentation process in the present invention are as follows.

① Forms of the first anaerobic fermenter (507) and the second anaerobic fermenter (509)

The primary anaerobic fermentation tank 507 and the secondary anaerobic fermentation tank 509 are both circular, the inner diameter D is 25 mФ or less, and the side wall depth H is 1/2 ( H = D / 2), and the gradient of the bottom surface is in the range of 20/100 to 30/100.

② Operating temperature and capacity of anaerobic fermenter

The operating temperature of the anaerobic fermenter is in the range of 50 to 60 ° C., and the capacity of the anaerobic fermenter is determined in the range of 5 to 6 kg / m 3 · day of organic matter load. In general, the fermentation time (T) is 20 to 30 days, and the volume of the tank (Volume, V㎥) is {high concentration wastewater input (㎥) + discharged anaerobic fermentation broth (㎥)} x fermentation time (T) / 2. The volume ratio of the first anaerobic fermenter 507 and the second anaerobic fermenter 509 is 1: 1 to 2: 1.

③ Stirring speed of the first anaerobic fermenter

The primary anaerobic fermenter agitator 303 of the primary anaerobic fermenter 507 is a propeller type, and the ratio (Q / V) of the stirring capacity (Q) and the stirring speed (V) is in the range of 0.5 to 2. To become.

④ Rotational speed of secondary anaerobic fermenter scraper 510

The secondary anaerobic fermentation tank 509 of the secondary anaerobic fermentation tank scraper 510 is rotated at 0.01 ~ 0.05rpm while the sludge deposited in the lower portion (Sludge) to the central cone (Cone) part is easy to settle sludge To be discharged.

⑤ The methane gas storage tank 512 has a spherical shape, and stores the methane gas produced by a flow type installed in the water of the spherical methane gas storage tank seal pit 511. Is 10 to 12 hours.

3. Magnesium Reaction and Neutralization Process

Sludge precipitated in the lower portion of the secondary anaerobic fermentation tank 509, anaerobic fermented water flowing over the upper portion of the secondary anaerobic fermentation tank 509 is supplied to the magnesium salt reaction tank 514, and stirred with the magnesium salt reaction tank stirrer 515. while magnesium salt (MgSO _4, MgCl ₂₎ the lower surface of the water ammonium ions (NH ₄ ^+), phosphate ions (PO ₄ ^{3 -)} injection and the magnesium reaction insoluble magnesium phosphate, ammonium phosphate in water (magnesium ammonium phosphate, MAP , MgNH ₄ PO ₄ ) is produced. The reaction taking place is the same as

_{^{Mg 2 2 + + NH 4 +}} + PO 4 3 - → MgNH 4 PO 4 ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⒁

When the reaction of Scheme VII occurs, since the pH is lowered, alkali neutralizers (NaOH, Ca (OH) ₂ ) are injected to neutralize the pH to 7-8, and then sent to the coagulation bath 516.

4. Coagulation and Precipitation Process

When the neutralization after the reaction in the magnesium salt reaction tank 514 is supplied to the coagulation tank 516, the polymer coagulant is injected 2-4 mg / l while stirring with the coagulation tank stirrer 517 to precipitate in the anaerobic digestion process precipitation tank 518. To facilitate this flocs (Floc) are formed and then sent to the anaerobic digestion process settling tank (518).

The reaction stirrer 101, the neutralization stirrer 103, the oxidation / sterilization stirrer 401, the neutralization stirrer 403 and the magnesium salt reaction stirrer 515 are a propeller type stirrer and rotated. The speed | rate is 180-360 rpm, and stirring volume makes ratio of inflow flow volume Q / crude volume V into 1.5-2. And the material uses a corrosion resistant material in consideration of the characteristics of the fluid.

And the flocculation tank stirrer 405 and the flocculation tank stirrer 517 is a pitched paddle type (stirred paddle type) stirrer, the rotation speed is 18 ~ 42rpm, the stirring capacity is the inflow flow rate (Q) / tank capacity The ratio of (V) is in the range of 1.5 to 2. And the material uses a corrosion resistant material in consideration of the characteristics of the fluid.

5. Precipitation Process

 When the solid matter is supplied from the flocculation tank 516 to the anaerobic digestion process settling tank 518 and the solids are precipitated to the lower portion, the 3rd dehydrator supply pump 520 is displayed when the condensation tank 519 is shown as a central cone part. Sent to the car dehydration process, overflowing the overflowing to the water tank 200 of the first aerobic biological treatment step.

The first settling tank 208, the second settling tank 302, the third settling tank 407 and the anaerobic digestion process of the settling tank 519 is set to 0.01 ~ 0.05 rpm.

6. 3rd Dehydration Process

Anaerobic Digestion Process The sludge precipitated in the sedimentation tank 518 and the inorganic solid sludge discharged from the lower part of the liquefaction tank 500 are sent to the third dehydration process so that the dehydrated dehydrated cake is disposed of because the mineral concentration is high, and the dehydration filtrate is anaerobic. The digestion process is sent to the sump tank 200 of the first aerobic biological treatment step together with the monthly water flowing over the top of the settling tank 518.

In this case, when the dehydrated cake is dehydrated and contains magnesium, when the leachate is sent to the composting step, the leachate discharged from the composting step is sent to the storage tank of the pretreatment step, and the magnesium ammonium phosphate phosphate scale is generated in the anaerobic fermentation step. Since there is a problem, it is preferable that the dewatered cake discharged from the third dehydration step of the present step be not sent to the composting step.

If magnesium ions, ammonium ions, or phosphate ions are present in organic wastes such as livestock manure and phosphorus, the magnesium reaction, neutralization process and flocculation and sedimentation process are performed before the anaerobic fermentation process. The anaerobic fermentation process must be performed after removing the magnesium ions so that scale trouble due to magnesium ammonium phosphate is not caused in the anaerobic fermentation process.

VI. Liquefaction stage

1. Liquefaction Process

The complex microbial microbial agent that produces hydrolysis enzyme (Hydrolase) while supplying the dehydration cake discharged from the first and second dehydration process of the pretreatment step to the liquefaction tank (500), and stirred with the liquefaction tank mixer (500). Iv) while injecting a heat source from a boiler to adjust the temperature to 50 to 60 DEG C while injecting air from the blower 213 to produce dissolved oxygen at an aerobic state in the range of 0.4 to 1.0 mg / L. After processing for 1 day, the organic solid material is liquefied. The liquefied high concentration organic waste is sent to the liquid high concentration organic waste storage tank 504, and the non-liquefied inorganic solids are sent to the solids transfer pump 506 in the third dehydration process. The complex microbial bacteria producing hydrolase used here is the same as that used in the liquefaction process of anaerobic digestion.

In the case where the air supply amount from the blower 213 is large, not only the power cost is excessively large, but also the supply from the boiler is increased, and if it is too small, there is a problem in that liquefaction is slow and severe odor is generated. Should be. At this time, the proper supply amount of air should be determined according to the type and concentration of organic waste, but generally in aeration intensity in the range of 3 to 5 [m 3 (air) / (1 ton of organic waste to be introduced) / hour]. If you supply air and aeration, it is OK.

And heating from the boiler to the liquefaction tank 500 does not need to continuously supply a heat source from the boiler because the temperature rises as the aerobic decomposition of organic matter when heated to 50 ℃ or more only at the beginning of operation, if the temperature rises above 70 ℃ blower ( The amount of air injected from 213) should be reduced to slow down the decomposition reactions of organics to lower the temperature.

2. Liquefaction process

The liquefied high-concentration organic waste is supplied to the dilution tank 521, and since the liquefied high-concentration organic waste has a high organic matter concentration, dilution water is supplied to dilute the organic matter concentration to a range of 5 to 20 wt%.

The liquid organic waste diluted by injecting distilled water into the liquid liquefied high concentration organic waste is supplied to the liquefaction tank 523 by the liquefaction tank supply pump 522, and air is blown from the blower 213 to 1.0-2.0 mg / The aerobic fermentation was performed by aerobic fermentation while aeration was carried out for 15 to 30 days, and the liquid was liquefied to be supplied to the liquid storage tank 525 by the liquid storage tank supply pump 524 and stored.

In this liquid liquefaction process, when air is injected into the liquid organic waste and liquefied by aerobic fermentation, the temperature is increased by decomposition of organic matter. When the temperature is over 70 ° C, excessive water vaporization and mesophilic microbes are killed. When the liquefaction is falling, if the air supply is large, excessive power costs are consumed, while the temperature drops, there is also a problem that the liquefaction rate falls. Thus, the amount of air supplied from the blower 213 to the liquefaction tank 523 is 15 to 30 while intermittently aeration so that the temperature is maintained in the range of 50 to 70 ° C. while the dissolved oxygen concentration is injected at 0.5 to 2 mg / l. Daily high temperature aerobic fermentation is sent to the liquid storage tank (525).

The liquid ratio supplied to the liquid storage tank 525 is stored for more than 4 to 6 months and then transferred to the tank lorry with the liquid ratio transfer pump 526 to be shipped as liquid liquid products.

The liquid ratio stored in the liquid storage tank 525 intermittently supplies air from the blower 213 so that the dissolved oxygen concentration is maintained in the range of 0.2 to 1 mg / L.

Liquid spray (하는 肥) is preferably used to inject dilution water so that the organic matter concentration is 5wt% or less when spraying on farmland or crops.

3. 3rd Dehydration Process

Inorganic solid sludge that has not been liquefied in the liquefaction tank 500 is sent to the dehydrator of the third dehydration process, and the dehydrated dehydrated cake is discarded because the inorganic concentration is high. The dehydrated filtrate is transferred to the reactor 100 of the pretreatment stage. send.

In the final dewatering process of the final wastewater treatment step, the third dehydration process of the anaerobic digestion treatment step and the third dehydration process of the liquefaction step, when the treatment capacity is a small amount, it is preferable to use a single joint, and the treatment capacity is In the case of large, it is preferable to install by each process. The dehydrator of the third dehydration process, centrifugal dehydrator, screw press, vacuum dehydrator, precoating vacuum dehydrator, compression filter press, belt press, vibrating screen or rotary trommel screen can be selected and used one, It is preferable to use a compression filter press as in the dehydrator of the dehydration process, but the type of dehydrator is not particularly limited.

VII. Composting Stage

1. Admixture Process

When the dehydration cake discharged from the dehydration process of the first and second dehydration process of the pretreatment stage, the dehydration cake discharged from the dehydration process of the anaerobic digestion treatment stage, the dehydration cake discharged from the dehydration process of the liquefaction stage is supplied to the mixer 600 A water regulator (swelling agent) is introduced while stirring with a mixer 601, mixed with water content of 60 to 65 wt%, and mixed, followed by fermentation and maturation tank 603 of the composting process by fermentation and maturation tank supply conveyor 602. Send to. At this time, if necessary, the water control agent and the soil improving agent are injected and mixed together, and then sent to the fermentation and maturation tank 603 of the composting process by the fermentation and maturation tank supply conveyor 602.

As the moisture control agent (swelling agent), one or a mixture of sawdust, rice hull, rice straw, barley straw, straw, bark, leafy soil, coconut pit or peat is used.

The moisture control agent, sawdust, rice husk, rice straw, barley straw, straw, bark, leafy soil, coconut pit or peat is used to have a C / N (Carbon / Nitrogen) ratio of more than 60 while absorbing.

Soil modifiers contain 100 parts by weight of the moisture control agent and the inflow of dehydrated cakes (organic wastes), including feldspar, phyllite, loess, vermiculite and illite. Mix at least one of Kaolin, Zeolite, Perlite, Bentonite, Smectite, Montmorillonite, Creek Soil, or Mountain Soil with 25% or more Clay. 10 to 40 parts by weight of the mixture is used.

C / N ratios of organic wastes are 8-12 for pigs, 8.4 for poultry meal and 9-20 for food waste, and too low C / N ratios cause NH ₃ gas to cause odor. While nitrogen is lost, on the other hand, when the C / N ratio is over 50 due to low nitrogen content, microbial activity is not smooth and the composting rate is slowed down and the temperature is lowered, so the C / N ratio is adjusted to 30 to 50.

In particular, the CEC (Cation exchange capacity) value is 100 to 150 meq / 100 g for natural zeolite, 50 to 115 meq / 100 g for montmorillonite, 80 to 150 meq / 100 g for vermiculite, 25 to 40 meq / 100 g for illite, and 90 to 120 meq / 100 g for bentonite , Smectite has the ability of adsorbing and preserving cations at 80-150 meq / 100g, and has a high binding force.

2. Fermentation and ripening process

Dehydration cake discharged from the first and second dehydration process of the pretreatment stage, dehydration cake discharged from the dehydration process of the anaerobic digestion process, and dehydration cake discharged from the dehydration process of the liquefaction step, When the mixed material at 600 is supplied to the fermentation and maturation tank 603, firstly, the organic substance that is easily decomposed is decomposed into simple inorganic substances such as CO ₂ , H ₂ O, and NH _3, and the temperature is 60-70 ° C. by the heat of reaction. If you go up, thermophilic bacteria grow, killing germs, pest eggs and weed seeds. When decomposing organic matter disappears and the temperature drops, mesophilic bacteria are grown and fermented and matured to produce compost.

The most important part of the composting process is fermentation and maturation process by mesophilic soil microbes, and the mesophilic soil microorganisms acting here are livers such as Bacillus mycoides and Bacillus luteus. Polyphenolic compounds such as fungi, mucus bacteria such as Sorangium cellulosum, and fungi such as Aspergillus niger. Fusarium, a microorganism that excretes the corrosive microorganisms that excrete as 代謝 産物 and metabolites of physiologically active vitamins (Vitamins) such as Pseudomonas sp. microorganisms that excrete hormones (Hormons), growth promoters such as auxin, and microorganisms that excrete antibiotics, such as Actinomycete, mukor Growth of the plant by microorganisms in a symbiotic relationship with corrosive microorganisms such as fungi such as species, Penicillium sp. And Fusarium sp. Composts that contain a large amount of useful material must be produced to be of good quality.

Soil microorganisms as described above have a high mineral content in the cytoplasm or cell wall, and these microorganisms have active metabolic activity when sufficient mineral components are readily supplied. Bacteria-Mineral-Water system (BMW) has been widely used in the process using soil microorganisms.

Used as the soil conditioner, Phyllite, Loess, Vermiculite, Illite, Kaolin, Zeolite, Pearlite, Bentonite, Bentonite ), Smectite, montmorillonite, stream bed soil or mountain soil have characteristics that make it easy to supply minerals to soil microorganisms.

When the dehydration cake is mixed with the moisture control agent and the soil improving agent in the blender 600 to the fermentation and aging tank 603, the dehydration cake is inverted at 1 to 3 times / day in the fermentation and aging tank mixer 604 for 30 to 50 days. The mature compost fermented by aerobic fermentation is injected into the mature compost hopper 606 by using a shovel (Poclain: 605), and then sent to a foreign matter sorting machine (607) to remove the foreign matter. 608), the dehydration cake discharged from the first and second dehydration processes of the pretreatment stage introduced into the fermentation and maturation tank 603, the dehydration cake discharged from the dehydration process of the anaerobic digestion stage, and the dehydration process of the liquid liquefaction stage. 20 to 50% of the dehydrated cake is discharged based on the mixing amount of the moisture control agent (swelling agent) and the soil improving agent, and the remaining ripe compost is completed by the ripe compost transport conveyor (609). To be sent to market after packaging.

When the dehydration cake discharged from the dehydration process of the first and second dehydration process of the pretreatment stage, the dehydration cake discharged from the dehydration process of the anaerobic digestion process, and the dehydration cake discharged from the dehydration process of the liquefaction stage are returned to the mature compost, The conveyor 608 may be omitted, and the mature compost can be conveyed to the front of the fermentation and maturation tank 603 using the shovel 605.

When the leachate discharged from the fermentation and maturation tank 603 flows into the leachate storage tank 610, the leachate transfer pump 611 is conveyed and sprayed to the high temperature part of the fermentation and maturation tank 603 for temperature control, and the remaining (excess) leachate is Send to reservoir in pretreatment stage.

Dehydration cake discharged from the first and second dehydration process of the pretreatment stage, dehydration cake discharged from the dehydration process of the anaerobic digestion stage, dehydration cake discharged from the dehydration process of the liquefaction stage is a moisture control agent (swelling) in the mixer 600 First, the mixture of the soil modifier and the mixture is mixed into the fermentation and maturation tank (603), and then reversed by the fermentation and maturation tank mixer (604), so that simple proteins and carbohydrates are easily decomposed by aerobic microorganisms. Carbonhydrate) such as simple CO ₂ , H ₂ O, NH ₃ After 3-4 days of fermentation due to heat of reaction and decompose into inorganic materials such as Bacillus stearothermphilus, Bacillus thermoleovorans, Clostridium dermocelum (Clostridium thermocellum), Clostridium thermosaccharolyticum, Clostridium thermoaceticum, Clostridium thermohydrosulfuricum, Lactobacillus thermophilus Thermophilic microorganisms, such as Lactobacillus thermphilus, Streptococcus thermphilus, and Streptomyces thermphilus, grow and grow as eggs and weeds of various bacteria and pests. Seeds, etc. are killed. At this time, if the temperature persists for more than 70 ° C. for a long time, the mesophilic microorganisms are killed and the mesophilic fermentation tank in the fermentation and maturation tank 603 is not completed because the mesophilic fermentation is not proceeded smoothly. The leachate discharged to 610 is sprayed on the high temperature part of the fermentation and maturation tank 603 by the leachate transfer pump 611 so that the temperature is maintained at 60 to 70 ° C, and the remaining leachate is sent to the storage tank of the pretreatment step.

In order for the fermentation and maturation to take place in the fermentation and maturation tank 603, a part of the mature compost is introduced into the seed microorganisms at the front of the fermentation and maturation tank 603 by the maturation compost conveying conveyor 608 or shovel 605. Dehydrated cake from the first and second dehydration process of the pretreatment stage, dehydrated cake from the dehydration process of the anaerobic digestion stage, and dehydrated cake from the dehydration process of the liquefaction stage and the moisture control agent 20 to 50wt% It is necessary to return.

The fermentation and aging tank mixer 604 is a rotary type, a scoop type, a screw type, a crane type, a screw auger type, One can use either a self-propelled mixing type equipped with a Caterpillar or a bucket loader mixing type.

In fermentation and fermentation, the fermentation and aging are mainly open and linear, as shown in Fig. 7, but the open-type fermentation apparatus other than the open and linear fermentation and aging tank 603 is used.裝置), open rotary fermentation device, open stirring fermentation device, open bell type fermentation device, open horizontal fermentation device Endless Scoop Type Fermentation System, Aeration Type Fermentation Fermenter, Rotary Kiln Type Sealed Lateral Fermentation System Fermentation may be carried out by using one type of fermentation equipment, either a closed type fermentation device or a closed type multiple type fermentation device. In the present invention, the form of the fermentation and aging tank 603 is not particularly limited. All. In the case of applying a closed type type fermentation device or an open type type type fermentation device, it is preferable to equip the high temperature fermentation part and the medium temperature fermentation part separately.

In the fermentation and maturation process, the dehydration cake discharged from the first and second dehydration steps of the pretreatment step, the dehydration cake discharged from the dehydration step of the anaerobic digestion step, and the dehydration cake discharged from the dehydration step of the liquefaction step are fermented. Considering the reaction mechanism (Mechanism) is generated as follows.

Organic matter-soil microorganisms (corrosive microorganisms) → polyphenolic compounds (metabolites) + CO ₂ + H ₂ O + Energy. ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ⒂

Polyphenolic compound + air (O ₂ )-oxidase → quinone compound + H ₂ O ₂ . ... (16)

Quinone compounds + hardly decomposable organic substances (lignin, cellulose, tannin, etc.) + volatile substances (NH ₃ , H ₂ S, mercaptans, dimethyl sulfide, etc.)-polycondensation reaction → corrosion precursor material. ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (17)

Corrosive precursors + corrosive microorganisms and symbiotic microbes (Penicillium sp., Pseudomonas sp.… Etc.) → corrosive substances + vitamins as physiologically active substances + hormones as growth promoters + antibiotics (composting compost)… ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (18)

Iii. Deodorization step

1. Biological deodorization process

Livestock manure, phosphorus, food waste, organic waste from agricultural and aquatic products, organic waste from food processing, and organic waste from slaughterhouses are carbohydrates that can be easily decomposed by microorganisms. As simple proteins are broken down into simple minerals such as CO ₂ and H ₂ O, NH ₃ , H ₂ S, Mercaptans, Thiols, Light amines, Indole, Ska Odor is generated while volatile odor generating substances such as skatole are generated.

In the present invention, the biological deodorization tower filled with the filler 702 by inhaling the odorous substances into the odorous material suction blower 700 at the point where the odorous substances of the organic waste pretreatment step, anaerobic fermentation step, liquefaction step and composting step occurs 701 is supplied to the bottom, and the surplus sludge discharged from the aerobic biological wastewater treatment step is sent to the biological deodorization tower 701.

And microbial food, 0.2-0.5% of the wastewater introduced into the wastewater collection tank 200 is sent to the biological deodorization tower 701.

At this time, in order to promote the growth of microorganisms, the salt water produced as a by-product while producing salt is also added to the biological deodorization tower 701 at a ratio of 0.01 to 0.03 parts by weight to 100 parts by weight of wastewater supplied to the biological deodorization tower 701. Supply.

Filling 702 filling the biodeodorization tower 701 is one of rhyolite, Dacite, Pegmatite, Granite or Phyllite, or crushed stone. One type of filler 702 is filled with wood chips such that the contact time of the gas is in the range of 1.2 to 2 seconds.

The biological deodorization tower 701 is a mass velocity ratio (G) of the gas containing the odorous substance in the odorous substance suction blower 700 and the mass velocity ratio of the absorbent liquid and the water (L) supplied from the biological deodorization tower circulation pump 703. L / G) in the range of 0.2 to 0.6, and the area of the tower is determined in consideration of the flying point and the loading point according to the type of the filling 702. In general, when the area of the tower is in the range of 0.15 to 0.3 m / sec of gas flow rate, the contact time is in the range of 1.5 to 2 sec, and the absorption liquid is in the range of 0.2 to 0.6 in mass velocity ratio (L / G). It's OK.

And the storage capacity of the circulating fluid in the lower portion of the biological deodorization tower 701 so that the residence time is 20 to 30 minutes based on the pumping flow rate of the biological deodorization tower circulation pump 703.

The mechanism of removing the malodorous substance in the deodorizing process is as follows.

Since the corrosion screen microorganisms and these microorganisms and microorganisms in symbiosis is contained by the ingestion of excess sludge, the organic matter discharged from the aerobic biological waste water treatment stage arranged a polyphenol compound as a metabolite of generating corrosion material NH _3, Volatile odor generating substances such as H ₂ S, mercaptans (Thiols), volatile amines (Light amines), indole, scarlet (Skatole) can be a non-volatile macromolecular substance, corrosion precursors or corrosion The odor generating substance is first removed by converting it into a substance.

Organic matter + air (O ₂ )-corrosive microorganisms → polyphenol compounds (microbial metabolites) + CO ₂ + H ₂ O. ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (19)

The polyphenol compound generates a quinone compound by catalytic reaction of an oxidase such as polyphenol oxidase in air.

Polyphenol Compound + Air (O ₂ )-Oxidase → Quinone Compound + H ₂ O ₂ . (20)

The quinone compound generates a corrosive precursor material which is a biologically nonvolatile material, and at this time, odorous substances such as volatile NH ₃ , H ₂ S, mercaptans, volatile amines, indole, and scarlet Odor substances are suppressed by converting them into non-volatile corrosion precursors by performing polycondensation reaction with odorous substances. Corrosion precursors are converted to stable corrosive substances by the corrosive microorganisms and soil microorganisms which have a symbiotic relationship with these microorganisms over time.

Quinone compound + volatile organic matter (NH ₃ , H ₂ S, mercaptans, volatile amines, indole, odor generating substances such as scatol)-Polycondensation reaction → Corrosion precursor (non-volatile substance) →→…. → corrosive substances ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (21)

2. Chemical deodorization process

The deodorizing gas subjected to the first deodorization treatment by the biological deodorization treatment is deodorized by chemical deodorization with an acid and an oxidizing agent.

In the biological deodorization process, the first deodorization gas is supplied to the lower portion of the chemical deodorization tower 705 by the chemical deodorization tower supply blower 704, and the chemical deodorization liquid of the chemical deodorization liquid storage tank 708 is subjected to the chemical deodorization tower circulation pump. 709, while partially returning to the middle stage of the filling 706 of the chemical deodorization tower 705 filled with two stages of the filling 706, the remaining chemical deodorant is supplied with water to the top of the filling 706 with chemical deodorization The malodorous substance is removed by causing countercurrent contact with the malodorous substance rising from the column 701 and the filler 706. At this time, the reaction mechanism for removing odorous substances is as follows.

1) Deodorization by Acid

NH ₃ + H ₂ SO ₄ → NH ₄ HSO ₄ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (22)

2NH ₃ + H ₂ SO ₄ → (NH ₄ ) ₂ SO ₄ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (23

(CH ₃ ) ₃ N + H ₂ SO ₄ → (CH ₃ ) ₃ NH ₂ SO ₄ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (24)

2) Deodorization reaction by oxidizing agent

2NaClO + H ₂ SO ₄ ≧ Na ₂ SO ₄ + HClO... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (25)

H ₂ S + 4HClO → H ₂ SO ₄ + 4HCl... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (26)

H ₂ S + HClO → H ₂ O + S + HCl... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (27)

2NH ₃ + 3HClO → N ₂ ↑ + 3HCl + 3H ₂ O... ... ... ... ... ... ... ... ... ... ... ... ... ... (28)

(CH ₃ ) ₃ N + HClO → (CH ₃ ) ₃ NO.HCl... ... ... ... ... ... ... ... ... ... ... ... ... ... (29)

CH ₃ SH + ₃ NaOCl → CH ₃ SO ₃ H + 3NaCl... ... ... ... ... ... ... ... ... ... ... ... ... ... (30)

(CH ₃ ) ₂ S + ₃ HClO → (CH ₃ ) ₂ SO ₃ + 3 HCl... ... ... ... ... ... ... ... ... ... ... ... ... ... (31)

(CH ₃ ) ₂ S ₂ + 2HClO → (CH ₃ ) ₂ S ₂ O ₂ + 2HCl... ... ... ... ... ... ... ... ... ... ... ... ... (32)

The chemical deodorant of the chemical deodorant storage tank 708 is hydrogen peroxide (H ₂ O ₂ ), sodium hypochlorite (NaClO), chlorine dioxide (ClO ₂ ), ozone (O ₃ ), or chlorine (Cl ₂ ). Adjust pH-controlling switch (pHIS) to adjust oxidation-reduction potential indicating control switch (ORPIS) for oxidant supplied with sulfuric acid in the range of pH 1-3. The redox potential is in the range of +800 to +1,100 mA.

The discharged water discharged from the discharge section of the chemical deodorization tower circulation pump 709 is sent to the neutralization tank 102 of the pretreatment step and used as a neutralizing agent.

Material of the filler 706 which is filled in the chemical deodorization tower 705 is stainless steel, porcelain, polyvinylchloride (PVC), polyethylene (PP), polypropylene (PP), ABS resin (Acrylonitrile) with excellent corrosion resistance. Butadiene styrene copolymer, acrylic resin, ebonite or Bakelite, one of the Raschig rings, Pall Rings, Raflux rings, Lessing rings One type of ring, cross partition ring, saddle type or ball type is filled so that the contact time of the gas is in the range of 1.2 to 2 seconds.

The chemical deodorization tower 705 is a mass velocity ratio (L / G) of the absorbent liquid supplied from the chemical deodorization tower circulation pump 709 and the water L from the chemical deodorization tower supply blower 704. ) Is in the range of 0.2 to 0.6, and the top diameter is determined in consideration of the flying point and the loading point according to the type of the filling 706. The area of is good if the gas flow rate is in the range of 0.15 to 0.3 m / sec.

The capacity of the chemical deodorant storage tank 708 is such that the residence time is 20 to 30 minutes based on the pumping flow rate of the chemical deodorization tower circulation pump 709.

In the case where the odor is completely removed by the biological deodorization treatment as in the manure treatment, the chemical deodorization process may be omitted.

Serum, livestock manure, wastewater with high organic concentration from industrial plants, landfill leachate, slaughterhouse waste, food processing plant waste, waste from agricultural and aquatic product processing, food waste, sludge treatment, industrial waste Since there is no rational treatment method due to high organic matter concentration and water content, such as landfill leachate, most of the marine dumping to date, but if the ocean dumping is prohibited by the international convention in the future, the present invention is diluted as shown in Examples 1, 2, 3 Because it can be treated below the emission standard without using water, it is expected to be widely used for treating organic waste having high organic matter concentration and high moisture content.

100: reactor 101: reaction tank stirrer
102: Chinese Tank 103: Chinese Tank Agitator
104: mixing tank 105: mixing tank mixer (Mixer)
106: Bag filter 107: Rotary feeder
108: pretreated organic waste storage tank 109: secondary dewatering process feed pump
200: sump 201: steel sheet
202: wire mesh electrode 203: wastewater transfer pump
204: constant voltage generator 204a: transformer
204b: voltage regulator 204c: primary coil
204d: iron core 204e: secondary coil
204f: insulation terminal 204g: output line
204h: ground 205: magnetizer
206: primary aeration tank 207: primary settling tank
208: primary settling tank Rake 209: primary return pump
210: primary microorganism activation tank 211: primary bioreactor
212: Filling 213: Air Blower
300: secondary aeration tank 301: secondary precipitation tank
507: secondary settling tank 303: secondary conveying pump
304: secondary microbial activator 305: secondary bioreactor
306: Filler 400: Oxidation and Sterilization Tank
401: oxidation and sterilization agitator 402: neutralization tank
403: neutralization agitator 404: agglomeration tank
405: flocculation tank stirrer 406: third settling tank
407: 3rd settling tank 408: sludge transfer pump
409: intermediate treatment tank 410: filter feed pump
411: filter 412: filter medium
500: liquefaction tank 501: liquefaction tank mixer (Mixer)
502: heating jacket 503: insulation
504: liquid organic waste storage tank 505: primary anaerobic fermentation tank feed pump
506: solids transfer pump 507: primary anaerobic fermenter
508: first anaerobic fermenter agitator 509: second anaerobic fermenter
510: secondary anaerobic fermenter scraper
511: methane gas storage tank seal pit
512: methane gas storage tank 513: fermentation sludge transfer pump
514: magnesium salt reaction tank 515: magnesium salt reaction agitator
516: coagulation tank 517: coagulation tank agitator
518: anaerobic digestion process sedimentation tank 519: anaerobic digestion process sedimentation tank
520: third dehydrator feed pump 521: dilution tank
522: liquefaction tank supply pump 523: liquefaction tank supply
524: liquid storage tank supply pump 525: liquid storage tank
526: liquid feeding pump 600: admixture
601: Admixture Mixer 602: Fermentation and Aging Tank Supply Conveyor
603: fermentation and aging tank 604: fermentation and aging tank mixer
605: shovel 606: mature compost hopper
607: Foreign object sorter 608: Finished compost conveyer
609: mature compost transfer conveyor 610: leachate storage tank
611: leachate feed pump 700: odor material suction blower
701: Biodeodorant Tower 702: Fillings
703: biological deodorization tower circulation pump 704: chemical deodorization tower supply blower
705: chemical deodorization tower 706: packing material
707: Demister 708: chemical deodorant reservoir
709: chemical deodorization tower circulation pump
Ⓢ: Solenoid valve FI: Flow indicator
LT: Level transmitter LS: Level switch
LIC: Level indicating controller
pHT: pH transmitter M: Motor
pHIS: pH indicating control switch
TI: Temperature indicator
TT: Temperature transmitter
TIC: Temperature indicating controller
DOI: Dissolved oxygen indicator
ORPT: Oxidation Reduction Potential Transmitter
ORPIS: Oxidation reduction potential indicating control switch

Claims (6)

One of the following: effluent, livestock manure, wastewater with high organic concentrations from industrial plants, slaughterhouse wastes, food processing plant waste, wastes from agricultural and aquatic product processing, food waste, sludge or landfill leachate. In the treatment of kinds of organic waste,
When the organic waste flows into the storage tank, the debris and foreign matters are sorted, and the dehydrated cake dehydrated in the first dehydration process is sent to anaerobic digestion, composting or liquefaction, and the dehydration filtrate of the first dehydration process is coal ash and calcium. After reacting with a mixture containing minerals or minerals containing calcium, neutralization is sent to the secondary dehydration process, and the dehydrated dehydrated cake is sent to anaerobic digestion, composting or liquefaction, and the dehydrated filtrate is subjected to the first aerobic biological treatment process. The dehydrated cake dehydrated in the second dehydration process is sent to the second dehydration process, or sent to the second dehydration process by neutralizing the mixture after mixing coal ash and minerals with minerals or the calcium-containing minerals to the organic waste that has been crushed and foreign matter. Sent to anaerobic digestion process, composting or liquefaction process, the dehydration filtrate of the second dehydration process is 1 And the pre-treatment step are sent to an aerobic biological treatment step,
Send the dewatered filtrate of the second dehydration process to the first aerobic biological treatment process, or send the first aerobic biological treatment water to the second aerobic biological treatment process after the water reforming treatment to the first aerobic biological treatment process Biological processing steps,
The first aerobic biological treatment water is a secondary aerobic biological treatment water treated in the second aerobic biological treatment process is characterized in that the organic aerobic biological treatment step comprising the discharge step of aerobic biological treatment. The method for treating organic waste according to claim 1, wherein the secondary aerobic biological treatment water is discharged by sequentially performing oxidation / sterilization treatment, neutralization treatment, flocculation / precipitation treatment, and filtration treatment. The dehydration cake dehydrated in the first dehydration step and the dehydration cake dehydrated in the second dehydration step are subjected to liquefaction, anaerobic digestion, magnesium salt reaction, neutralization, flocculation, sedimentation, and dehydration. Treatment of organic waste by sending anaerobic digestion water treated by treatment to the first aerobic biological treatment process. The dehydration cake dehydrated in the 1st dehydration process of Claim 1, and the dehydration cake dehydrated in the 2nd dehydration process, The method of making a liquid fertilization by aerobic liquefaction process. The dehydration cake dehydrated in the first dehydration process of claim 1 and the dehydration cake dehydrated in the second dehydration process mixed with a water conditioner (swelling agent) and a soil improving agent and then fermented mature to make a compost. Deodorizing method of claim 1, 2, 3, 4, 5 to collect the malodorous substances by treatment of biological deodorization treatment, chemical deodorization treatment sequentially.

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