KR20150037788A - Method for treatment of food waste - Google Patents

Abstract

The present invention relates to a method for treating food waste. More specifically, the method comprises: crushing collected food waste, dehydrating the food waste in which foreign substances are separated and processed, processing dehydrated cake for composting, methane fermentation, alcoholic fermentation or feed, reacting wastewater which is dewatering filtrate with lime and fly ash, injecting pre-dry distilled fiber powder into an insoluble material converted by adding a water-soluble organic matter, a liquid organic matter, and salt in water, mixing the pre-dry distilled fiber powder and the insoluble material, removing a solid matter by coagulating and precipitating the mixture, and treating the food waste by aerobic biological treatment.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating food waste,

More particularly, the present invention relates to a method of treating food waste, and more particularly, to a method of treating food waste, which comprises subjecting collected food waste to crushing and separating foreign matters, and subjecting the dehydrated cake to composting, methane fermentation, alcohol fermentation, , Wastewater which is a dehydrated filtrate is reacted with lime and fly ash to convert water soluble organic matter, liquid organic matter and salt into insoluble matter, and it is mixed with pre-dry cellulosic powder (dry pre-distillation fibrinogen powder) ≪ RTI ID = 0.0 > a < / RTI > method of treating food waste by aerobic biologic treatment.

Food waste has a high water content with a high concentration of organic matter, and the dehydration filtrate after the dehydration treatment has a high concentration of contaminants. Therefore, there is a problem that the dehydration cake is composted by the end of 2012, There is a problem that it causes salting of the crop and there is a problem that the compost of good quality can not be produced. Therefore, it has been attempted to perform the fermentation of anaerobic methane fermentation and sewage in the food waste dehydration filtrate, but the food waste has a high fatty acid content, which causes coagulation of microorganisms and coating of the surface, And the food waste was tried to be incinerated together with the industrial waste in the incinerator of the garbage incinerator. However, when the incinerator is incinerated, the chlorine component contained in the food garbage reacts with the organic substance and the second contaminant such as dioxin There has been a problem of being discharged.

Since 2013, international dumping of pollutants such as organic wastes has been banned by the International Convention, there is a need to find ways to rationalize treatment of high concentration organic wastes such as food wastes.

In the case of Patent Document 1 and Korean Patent Registration No. 10-0356966, there is proposed a method of treating food waste and livestock manure by pretreatment and methane fermentation method, but the efficiency of methane fermentation treatment The concentration of ammonia nitrogen and water-soluble phosphorus is high in the fermentation treatment liquid. Therefore, it is not possible to efficiently perform denitrification and denitrification without using dilute water, and in order to perform denitrification and denitrification, And the driving ratio is high.

In Patent Document 2 and Korean Patent Registration No. 10-0587235, organic waste such as livestock manure or food waste is fermented at a temperature of 75 to 85 ° C for 4 hours in a drier, and then dried and mixed with quicklime and zeolite There is a problem in that when the organic waste is fermented in the dryer at a temperature of 75 to 85 캜 for 4 hours, the compost can not be produced in good quality and the drying cost is high .

In Patent Document 3, a method and apparatus for composting organic wastes (organic wastes composting method and apparatus), organic wastes such as animal feces and food wastes are evaporated and dried by hot air to be fermented and composted However, there is a problem that the disposal cost is high due to the drying cost, and the food waste has a high salt concentration, so that there is a problem that good quality compost can not be produced.

Patent Document 4 and Korean Patent Registration No. 10-1106129 disclose a desalination method using an electrical extraction method for organic wastes containing salt such as food waste, livestock manure or food waste, , And the desalination process of the present invention can utilize the technique of Patent Document 4 in the present invention.

Non-Patent Document 1, "Domestic and Foreign Trends of Food Processing Using Earthworms", suggests a method of breeding and treating earthworms with earthworms, but there is a problem in that a lot of land and operating expenses are involved in the processing of food wastes by earthworm rearing , There are other problems as well, and it is not widely available.

Non-Patent Document 2, "Overview of Food Waste Disposal Method in Korea", is a technology that present the present state and characteristics of domestic food waste disposal to date, and it is merely data that explains the prior art.

In addition, a variety of data from patent documents and non-patent documents are presented, but no technology for reasonably processing food waste has been proposed.

Korean Patent Registration No. 10-0356966, Integrated Digestion Treatment Device and Method of Food Waste and Livestock Manure, October 04, 2002 Korean Patent Registration No. 10-0587235, Method of Manufacturing Compost Using Organic Waste, and Manure Compost, May 30, 2006 Japanese Patent Application Laid-Open No. 2009-167063, a method and apparatus for composting organic wastes (composting method and apparatus for organic wastes), July 30, 2009 Korea Patent Registration No. 10-1106129, desalination apparatus for saline-containing organic waste, January 09, 2012

   Choi, Hoon Keun, Trends in Food Processing Using Earthworms, National Institute for Environmental Studies, Joint Conference on Reduction of Food Waste, June 1998    Park, Jin - Seo, Cha Dong - Won, Se - Seung Jik, An Overview of Food Waste Treatment Methods in Korea, Korea Society of Applied Environment,. 427-432

The present invention relates to a method for solving the problems of the prior art, wherein the dehydrated cake is subjected to composting, methane fermentation, alcohol fermentation or feed conversion, the wastewater being a dehydrated filtrate is lime, coal ash, And pre-dry cellulosic powder (dry pre-distillation fibrinogen powder) to convert the water-soluble organic matter, liquid organic matter and salt into a solid material insoluble in water, then aggregate and precipitate to remove solid matter, and then reduce pollution load and salt concentration And to provide a food waste disposal method capable of highly wastewater treatment.

In order to achieve the above object, the present invention provides a method of treating food waste, wherein when the food waste is put into a feed tank, the cake is crushed and debris is removed, and the dehydrated cake is subjected to a composting process, a methane fermentation process, Or feedstuff process. The dehydrated filtrate is converted into a solid material in which water-soluble organic substances, liquid organic substances and salts are insoluble in water by reacting lime, fly ash and pre-dry distilled fiber powder A pretreatment step in which the neutralized wastewater after coagulation and sedimentation is removed and then neutralized is sent to an aerobic biological treatment process, a wastewater treatment step in which the neutralized wastewater is subjected to aerobic biological treatment, sterilization and filtration treatment, After liquefaction treatment, lime and fly ash were injected into aerobic fermentation broth and water soluble salt was added to water A methane fermentation step of liquefying the dehydrated cake, followed by acid fermentation and methane fermentation to produce methane gas, and a step of subjecting the dehydrated cake to a saccharification treatment A fermentation step of fermenting alcohol to produce ethanol, a step of feeding the fermented broth to fermented liquor by fermenting the dewatered cake at a high temperature to produce feeds, and a step of using excess sludge discharged from the aerobic biological treatment process And a deodorizing process step of collecting the odor generating substances generated in the respective process steps and deodorizing the deodorizing process by biological treatment.

Food waste with a high concentration of organic matter and salt is not disposed of reasonably because there is no rational treatment method, but the marine dumping was done until the end of 2012. However, since marine dumping was prohibited by international agreements by 2013, . Thus, in the present invention, water-soluble organic matter and liquid organic matter are converted into insoluble organic matter by using lime to lower the pollution load of the wastewater, so that the wastewater can be highly treated and the dehydrated cake can be effectively composted, It is expected to be widely used for food waste disposal in the future because it has the effect of producing by-products of oil prices by plowing, alcohol fermentation or feed conversion.

Fig. 1 is a view showing a food waste disposal process
Fig. 2 is a view showing a pre-
FIG. 3 is a graph showing the aerobic biological treatment process
Figure 4 shows the composting process
Figure 5 shows the methane fermentation process
Fig. 6 is a view showing an alcohol fermentation process
Fig. 7 is a diagram
Fig. 8 is a flowchart
9 is a graph showing the dissolution diagram of oxygen in water under atmospheric pressure
Figure 10 shows the dissolution diagram of oxygen in water with changes in temperature and pressure
Fig. 11 is a photograph showing the growth of strawberries by injecting the produced compost into the strawberry cultivation pot

First, the background of the present invention will be described. The food waste is easily corroded to cause bad odor, and the wastewater as the dehydrated dehydrated filtrate has high pollution load and salt concentration, and the concentration of unsaturated fat in the liquid is high, In addition, there are various problems such as difficulty in composting the dehydrated cake because of high salt concentration.

Therefore, in order to solve the problem of high contamination load and salt concentration of wastewater, which is a dehydration filtrate, lime, fly ash and pre-dry distilled fiber powder are injected to obtain water- The present invention relates to a method for treating waste water, comprising the steps of treating a liquid organic material with lime and converting it into a calcium salt insoluble in water to reduce pollution load of wastewater, treating salinity with an insoluble salt, The water was removed and the treated capacity was decreased. As a result, the dehydrated cake was dehydrated and the treated capacity was decreased, so that the composting, Methane fermentation, alcohol fermentation, or feed conversion. Also, in the case of composting, it is possible to produce good quality compost by removing the salinity which is a problem.

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

Ⅰ. Preprocessing step

When the food waste flows into the feed tank, the separation and removal of foreign substances and the crushing process of the large material are sent to the dehydration process, and the dehydrated dehydrated cake is sent to the alcohol fermentation process, composting process, methane fermentation process, alcohol fermentation process or feed conversion process , Lime, fly ash, and pre-dried fibrin powder are injected into the dehydrated filtrate to convert the water-soluble organic matter and the liquid organic matter into calcium-reacting substance to be insoluble in water, and the water-soluble pollutant is adsorbed on the pre- After the conversion, the solid matter is removed by coagulation and precipitation, and the wastewater is sent to the aerobic biological treatment process.

1. Removal and crushing process

When garbage is put into the input tank, the surplus sludge from the aerobic biological treatment process and the biological deodorizing solution from the deodorization process are sprayed to suppress the generation of odor, and then the glass debris, stone, vinyl, Removal of foreign matter such as sculptures, shells, and animal bones, and bulk materials are broken in a crusher and then sent to the primary dehydration process.

2. Primary dehydration process

The dehydrated cake is sent to the composting process, the methane fermentation process, the alcohol fermentation process or the feed process, and the dehydrated filtrate is sent to the dehydrated cake, (1).

The dehydrator of the primary dehydration process may be a centrifugal dehydrator, a screw press, a vacuum dehydrator, a belt press, a vibrating screen, or a rotary Trommel screen screen. Of these, it is preferable to use a centrifugal dehydrator or a screw press. However, in the present invention, the dehydrator type of the primary dehydration process is not particularly limited.

3. Reaction Process

When the dehydrated filtrate of the primary dehydration process is supplied to the reaction tank 1, lime and fly ash are poured into the reaction tank stirrer 2 at 180 to 360 rpm while the reaction product is reacted for 30 to 60 minutes, (3). The reactor agitator (2) uses a propeller type.

Lime and coal fly ash is added to the dehydrated food waste and the reaction is carried out. Oleic acid, linoleic acid, linolic acid, arachidonic acid, palmitic acid, stearic acid It reacts with a part of a water-soluble contaminant such as a fatty acid ester such as a higher fatty acid such as stearic acid, a fatty acid ester such as a glyceride, an amino acid or a phosphate ion, Calcium salt.

2R-COOH (higher fatty acid) + Ca (OH) ₂ → (R-COO) ₂ Ca ↓ + 2H ₂ O ... ... (One)

Wherein R is a base of a higher fatty acid or amino acid.

The phosphoric acid component reacts with calcium hydroxide and is treated with phosphate insoluble in water.

_{Ca (OH) 2 + H 3} PO 4 → CaHPO4 + 2H 2 O ... ... ... ... ... ... ... ... ... ... ... ... ... (2)

Fly ash has the ability to adsorb odor generating substances such as ammonia (NH ₃ ), hydrogen sulfide (H ₂ S), methyl mercaptan, trimethylamine, and volatile organic acid And thus has a characteristic of reducing odor generation. In addition, the calcium hydroxide (Ca (OH) ₂ ) also converts odor generating substances such as hydrogen sulfide (H ₂ S) into water-insoluble and nonvolatile calcium sulfate (CaS) .

Ca (OH) ₂ + H ₂ S? CaS + 2H ₂ O ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (3)

Fly ash contains a large amount of pozzolanic material such as activated SiO ₂ and Al ₂ O _3. This pozzolanic substance is converted to calcium hydroxide (Ca (OH) ₂ ) and pozzolanic reaction (Calcium aluminate hydrates, 3CaO · Al ₂ O ₃ · 6H ₂ O) and calcium silicate hydrates (3CaO · 2SiO ₂ · 3H ₂ O).

_{3Ca (OH) 2 + Al 2} O 3 + 3H 2 O → 3CaO · Al 2 O 3 · 6H 2 O ... ... ... ... ... ... ... ... ... ... (4)

_{3Ca (OH) 2 + 2SiO 2} + 6H 2 O → 3CaO · 2SiO 2 · 3H 2 O ... ... ... ... ... ... ... ... ... (5)

The calcium aluminate hydrate (3CaO.Al ₂ O ₃ .6H ₂ O) produced in the above reaction formula (4) can be obtained by reacting chlorine ion (Cl ^- ) in water with friedel's salt (Cl ^- ) in water while reacting in the form of Friedel's salt.

3CaO · Al ₂ O ₃ · 6H ₂ O + 2Cl ^- + Ca (OH) ₂ + 4H ₂ O → 3CaO · Al ₂ O ₃ · CaCl ₂ · 10H ₂ O (Friedel's salt) ↓ + 2OH ^- ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (6)

Sodium ion (Na ⁺⁾ is the above reaction scheme 5, the reaction of calcium silicate hydrate (Calcium silicate hydrates, 3CaO · 2SiO 2 · 3H 2 O) and Scheme reaction of soda lime silicate insoluble in water, as shown in (7) of the (Na ₂ O · 3CaO · 2SiO ₂ · XH ₂ O) is generated and the salt is removed from the water.

_{^{2Na + + 3CaO · 2SiO 2 ·}} 3H 2 O + 2OH - + (X-4) H 2 O → Na 2 O · 3CaO · 2SiO 2 · XH ₂ O ↓ ... (7)

And AL pane (Allophane) quality clay mineral _{(Al 2 O 3 · SiO 2} · nH 2 O), volcanic ash soil (火山灰土), incineration time (燒却灰), cement (Cement) of the incinerator to pozzolanic material (Pozzolanic material ), It can be used instead of the fly ash.

When an acidic substance such as sulfuric acid, hydrochloric acid or carbonic acid (H ₂ CO ₃ ) is injected into water and becomes acidic, the reaction of the above reaction formulas (6) and (7) Sediments containing post-saline should be removed immediately in water.

If the dehydrated food waste solution is fed to the reaction tank 3, lime and fly ash are fed, and the reaction is carried out, then neutralization is carried out using sulfuric acid (H ₂ SO ₄ ) as a neutralizing agent. Since chlorine ion (Cl ^- ) is re-released into water by the same reaction and salt is not removed, it is necessary to remove precipitate immediately at pH 8.4 or higher.

_{3CaO · Al 2 O 3 · CaCl} 2 · 10H 2 O + SO 4 2 - → 3CaO · Al 2 O 3 · CaSO 4 · 12H 2 O + 2Cl - ... (8)

The reaction to remove the salt by the reaction formulas (6) and (7) is carried out by the equivalent amount of salinity, fly ash and lime, but the composition of coal fly ash varies depending on the type of coal used in the thermal power plant In order to improve the salt removal efficiency, it is preferable to supply the fly ash in an amount of 1.2 to 2 times as much as the amount of salt, and the lime is supplied in accordance with the organic substance concentration. However, Supplying parts by weight is safe.

4. Mixing Process

When the reactant in the reaction step is supplied to the mixing tank 3, 2 to 5 parts by weight of the pre-dry cellulosic powder is poured into 100 parts by weight of the reactant to be supplied, stirred at 180 to 360 rpm for 30 to 60 minutes with the mixing bath mixer 4 When it is mixed, it is sent to the coagulation tank (5). Propeller type stirrer (4) is used.

The pre-dry distilled fiber powder used in the present invention may be selected from the group consisting of wood, sawdust, bark, straw, barley straw, straw, chaff, grass, peat moss, The present invention relates to a method for producing a cellulose fiber which is capable of decomposing one or more kinds of fibrous materials among fiber materials such as carbon fiber, coir, paper or fibrous sludge from pyrolysis of a cellulose component at 180 to 200 ° C, Treated powder is pulverized to a mesh of 40 to 200 mesh.

The pre-dry fibrinogen powder is excellent in the ability to adsorb water-soluble contaminants, and when it is dewatered after flocculation, the water content is in the range of 60 to 70 wt%, and the dehydration efficiency is excellent. In addition, when the dehydrated cake is composted, it has a good swelling property (swelling property) and excellent air permeability.

5. Coagulation and Precipitation Process

When the pre-dried fibrinogen powder is injected and mixed in the mixing tank 3, the polymer flocculating agent is dissolved in 0.01 to 0.1% solution in water to obtain a solution of 2 to 4 mg / l And the solid material is floc easily precipitated in the primary settling tank 7 while stirring in the range of 18 to 48 rpm for 20 to 40 minutes with the flocculating tank agitator 6 to form the primary settling tank 7, Lt; / RTI >

In the flocculation tank 5, when the solid material floc is easily deposited and sent to the primary settling tank 7, when the solid floe is settled to the lower part of the primary settling tank 7, Is collected at the lower cone portion of the primary settling tank 7 while rotating at 0.01 to 0.02 rpm and sent to the secondary dewatering process by the settling sludge transfer pump 9 and the overflow ) Is sent to the neutralization tank (10).

The polymer coagulant is preferably a polyacrylamide polymer coagulant, but the type of the polymer coagulant used in the present invention is not particularly limited.

The settler rake 8 has the same structure as the rake of the thickener in the wastewater treatment plant, and the rotation speed is 0.01 to 0.02 rpm.

The primary sedimentation tank 7 has a solid loading rate in the range of 60 to 90 kg / m 2 · hr, a depth of 3 to 5 m and a slope of 1/10 to 1/20 .

6. 2nd dehydration process

The solid material on the sludge settled in the lower part of the primary settling tank 7 is sent to the secondary dewatering process by the settling sludge transfer pump 9, and the dewatered dewatered cake is sent to the composting process and the dehydrated filtrate is supplied to the primary settling tank 7) to the neutralization tank 10 together with the overflowing overflow.

The dehydrator of the second dehydration process may be a centrifugal dehydrator, a screw press, a vacuum dehydrator, a pre-coat vacuum dehydrator, a filter press, Or a belt press, and it is preferable to use a filter press dehydrator.

7. Neutralization process

When the overflowing overflowing water and the dehydrating filtrate of the second dehydration process are supplied to the neutralization tank 11 above the primary settling tank 7, the neutralization tank stirrer 11 stirs the mixture at a stirring speed of 180 to 360 rpm, The pH of the solution is neutralized to a range of 5.6 to 8.2 and then sent to the water collecting tank 12 of the aerobic biological treatment process.

The reactor tank 3 and the neutralization tank tank 11 are of a propeller type and the flocculation tank 11 is of a pitched paddle type.

Table 1 shows the result of analyzing the dehydrated filtrate from a food waste disposal plant for dehydrating and treating food waste by separating and removing impurities and crushing it with a screw press filter.

Analysis value of component of dehydrated filtrate of food waste Item Analytical value Item Analytical value pH 4.2 T-N (mg / l) 3,240 BOD ₅ (mg / l) 152,860 NH ₄ ⁺ -N (mg / l) 255 COD _Mn (mg / l) 201,150 T-P (mg / l) 352 SS (mg / l) 134,500 Electrical Conductivity (ms / cm) 22.4

1,000 kg of the food waste dewatering filtrate of Table 1 was poured into a 1.5 m3 round iron tank and 30 kg of lime and 40 kg of fly ash as shown in Table 2 were poured into the tank, The mixture was stirred at 360 rpm for 40 minutes and then 20 kg of pre-dry fibrillated powder pulverized with 120 mesh was pyrolyzed at 200 ° C. The mixture was stirred with a propeller type stirrer at a rotational speed of 360 rpm for 40 minutes, 0.02% solution of polyacrylamide polymer flocculant was injected at 4 mg / L while stirring with a pitched paddle type stirrer at a rotating speed of 18 rpm and stirred for 30 minutes to form a floc easily, The operation was stopped and the solids were settled.

Analysis of composition of coal fly ash SiO ₂ Al ₂ O ₃ Fe ₂ O ₃ CaO MgO Others (including ignition loss) 57.8 23.2 5.2 8.2 2.7 2.9

After the floc was formed, the operation was stopped, and the water quality of the supernatant liquid in which the solid matter was precipitated was analyzed as shown in Table 3 below.

Analyze the quality of the supernatant that precipitated the solids Item Analytical value Item Analytical value pH 13.6 T-N (mg / l) 112 BOD ₅ (mg / l) 860 NH ₄ ⁺ -N (mg / l) 12 COD _Mn (mg / l) 1,020 T-P (mg / l) 0.3 SS (mg / l) 82 Electrical Conductivity (ms / cm) 2.4

As shown in the results of the water quality analysis of the supernatant obtained by precipitating the solids in Table 3, lime, fly ash, and pre-dry cellulosic powder were injected into the dehydrated filtrate of food waste and the primary treated water was reacted with aerobic biological treatment method (activated sludge method) It can be confirmed that the water quality which can be easily treated by the above method is processed.

Ⅱ. Wastewater treatment stage

1. Aerobic biologic treatment process

The overflowing overflowing water and the dehydration filtrate of the second dehydration process are sent to the neutralization tank 10 over the first settling tank 7 and the neutralized product is then neutralized to a pH of 5.6 to 8.2 Is supplied to the aeration tank 12 of the aerobic biological treatment process, it is supplied to the primary aeration tank 18a by the aeration tank supply pump 16.

When the wastewater from the water collecting tank 12 is supplied to the primary aeration tank 18a, the air is injected from the blower 26 and aerated by the aerobic biological treatment to the secondary settling tank 19a to precipitate the solids , And the first aerobic biologically treated water, which is the overflowing overflow, is sent to the final treatment tank 25, the sterilization / filtration process, or the secondary aeration tank 18b of the second aerobic biological treatment process.

When the solid material (microbial cells) precipitated in the secondary settling tank 19a is collected by the secondary settler tank 20a into the central cone portion under the secondary settling tank 19a, the solidified material is collected by the primary returning pump 21a A primary microorganism activating tank 22a and a primary microorganism activating tank 22b in which a primary bioreactor 23a charged with an activated humic substance pellet and a mineral filler 24 containing an active mineral ingredient are contained, The excess sludge that is discharged while being conveyed to the car aeration tank 18a is sent to the input tank and the deodorization process.

When the overflowing overflowing water in the second settling tank 19a of the aerobic biological treatment process is treated within the discharge standard value or when it is treated in connection with the nearby sewage treatment facility, it is sent to the final treatment tank 25 Or sent to a nearby sewage treatment facility.

When the sludge which is the solid matter (microbial cells) precipitated in the secondary settling tank 19a by the primary transfer pump 21a is supplied to the primary microorganism activating tank 22a, air is blown from the blower 26 to the primary Air is supplied from the blower 26 to the lower portion of the primary bioreactor 23a filled with the microorganism activating tank 22a and the filler 24 containing the minerals containing active minerals and the active corrosive material pellets, Together with the filler (24) layer of the primary bioreactor (23a) are air lifted to receive the mineral component.

Bacillus mycoides, Bacillus luteus, actinomycetes, which actively metabolize when the minerals are fully supplied, are supplied with sufficient mineral components from the primary microorganism activation tank 22a, (Polyphenol compounds) as metabolic products to convert liquid water-soluble organic substances into water-insoluble corrosion precursors (humic substances precursors) or corrosive substances (humic substances) by corrosion reaction Corrosive microorganisms and microorganisms that are in symbiotic relationship with these microorganisms are activated and sent to the first aeration tank 18a so that the entire first aerobic biological wastewater treatment system is able to remove corrosive microorganisms and microorganisms The aerobic biologic treatment is caused by the corrosion reaction.

The microorganisms that corrode the organic substances and generate corrosive substances have a high content of minerals in the cytoplasm or the cell wall and these microorganisms actively metabolize when the minerals are sufficiently taken, A primary bioreactor 23a filled with a mineral containing a large amount of an active corrosion ingredient and an active mineral ingredient capable of easily eluting the microorganisms can be installed in the primary microorganism activating tank 22a so that sufficient minerals can be supplied to the microorganisms .

The amount of the active corrosion material pellets and the minerals containing minerals is charged into the primary bioreactor 23a installed in the primary microorganism activating tank 22a at a flow rate of 10m3 / day of the wastewater supplied to the primary aeration tank 18a 5 to 10 kg of active corrosion material pellets and 10 to 20 kg of minerals containing active minerals.

Minerals containing large amounts of active minerals that can easily supply minerals to microorganisms can be obtained from one of Rhyolite or Dacite quality Pumice, Pegmatite or Perlite. do.

The active corrosion material pellets are formed by mixing marine diatoms and marine plants with pellets such as humus soil with high fulvic acid content and a binder such as bentonite Purchase and use commercially available products.

The amount of air to be supplied to the primary aeration tank 18a and the primary microorganism activation tank 22a in the blower 26 is such that the dissolved oxygen concentration of the primary aeration tank 18a and the primary microorganism activated tank 22a is 2 to 4 mg / L, and the air supplied to the lower portion of the primary bioreactor 23a has an aeration intensity of 1.5 to 3.5 Nm-Air / m 2 · hour. The discharge pressure of the blower 26 is determined in consideration of the frictional loss due to the static head and the friction loss of the pipe depending on the water depth of the tank.

In the present invention, the wastewater treatment is carried out by aerobic biologic treatment by a corrosion reaction, and thereby, volatile organic acids such as propionic acid, butyric acid, valeric acid, ammonia (NH ₃ ), trimethylamine Volatile nitrogen compounds such as dimethylamine, indole and skatol, hydrogen sulfide (H ₂ S), dimethyl sulfide, methyl disulfide, mercaptan, Volatile sulfur compounds such as sulfuric acid and volatile sulfur compounds such as acetaldehyde are assimilated into corrosive precursors or corrosive substances that are nonvolatile and insoluble in water to inhibit the generation of odor, Is highly insoluble in corrosion precursors or corrosive substances, and is highly efficient in wastewater treatment.

The capacity of the primary aeration tank 18a is determined by the following equation (9) in the range of 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 x Q) / (MLSS x V) [kg BOD / m 3. ... ... ... ... ... ... ... ... ... (9)

In this case, BOD ₅ is the biological oxygen demand (㎎ / ℓ) of the influent wastewater at 5 days, V is the volume of the aeration tank (Volume, ㎥), MLSS is the concentration of mixed liquor suspended solids in the aeration tank (mg / (M3 / day) of the inflow wastewater.

The surface area of the secondary settling tank 19a is set to have a surface area with a margin considering an overflow load of 8 to 25 (m 3 / ㎡ · day) and a solid load of 60 to 90 (kg / ㎡ · day) The depth is 3 ~ 6m.

The flow rate of the first settling tank 18a and the first microorganism activating tank 22a carried by the first settling tank 19a in the second settling tank 19a is set to MLSS (Mixed Liquor Suspended Solids ) Is determined in accordance with the following equation (10) so that the concentration is in the range of 2,000 to 3,500 mg / l.

R = Qr / Q = (MLSS-SS) / (R-MLSS) ... ... ... ... ... ... ... ... ... ... ... ... (10)

Where Q is the flow rate (m3 / day) to be conveyed, Q is the flow rate of the incoming wastewater (Mg / L), ML is the mixed liquid suspended solids concentration (mg / L) in the primary aeration tank 18a, 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 22a is 8 to 20% of the flow rate of the entire sludge sludge, and the capacity of the primary microorganism activating tank 22a is 0.5 to 2 days.

The amount of air to be supplied to the primary aeration tank 18a and the primary microorganism activation tank 22a in the blower 26 is such that the dissolved oxygen concentration in the primary aeration tank 18a is maintained at 2 to 4 mg / And the amount of air supplied to the lower portion of the primary bioreactor 23a is an aeration intensity of 1.5 to 3.5 Nm-Air / m 2 · hour. The discharge pressure of the blower 26 is determined in consideration of the frictional loss due to the static head and the friction loss of the pipe depending on the water depth of the tank.

When the aerobic biological treatment water is treated within the discharge reference value or when the sewage merging treatment is carried out, the aerobic biological treatment water is sent to the final treatment tank 25 and then discharged or sent to the sewage treatment plant.

In order to improve the aerobic biologic treatment efficiency, a stainless steel plate (15, conductor) connected to the ground 13h at the bottom of the water collecting tank 12 is installed. On the stainless steel plate 15, polyethylene, polyvinyl chloride A stainless steel such as PVC or Styrofoam is installed on the top of the insulator and a charcoal or activated carbon filled with charcoal or activated carbon having a high conductivity. And a high voltage of 3,000 to 5,000 volts is applied to the wire mesh electrode 14 from a static voltage generating device 13 for 4 to 10 hours to form a constant voltage When electrostatic pressure treatment is performed, electrostatic fields of + and - are generated around the wire mesh electrode 14 so that the water molecule itself vibrates and rotates repeatedly, and surface tension (surface tension) Less activated water with high permeability Quality treated wastewater has a characteristic microbial active to improve wastewater treatment efficiency. If necessary, the efficiency of the biological wastewater treatment can be further improved by additionally providing the magnetizing device 17 in the constant-voltage process and the discharge unit of the aeration tank feed pump 16 and reforming the water together.

The magnetizing device 17 is made of a cylindrical conductive tube made of an insulating material such as synthetic resin (PVC, PE, styrene resin, etc.), ebonite, FRP, bakelite, When a low voltage of AC or DC is applied in a range of 0.5 to 5 volts to a conductive pipe, a magnetic field is formed inside the coil. When the fluid passes through the coil, the fluid is magnetized, do.

Here, a permanent magnet magnetizer in which magnetic flux density (magnetic flux density) in the range of 10,000 to 15,000 Gauss is magnetized instead of the magnetizer 17 in which a coil is wound around the constant voltage power may be used.

The wastewater is supplied from a static voltage generating device 13 to a water collecting tank 12 in which a wire net electrode 14 charged with charcoal or activated carbon charged with a constant voltage is incorporated and the transformer 13a of the constant voltage generating device 13 The output line 13f of the secondary coil 13e of the secondary winding 13a is connected to the wire mesh electrode 14 provided in the water collecting tank 12 to supply the AC power of 100 to 220 volts and a frequency of 50 to 60 Hz When the voltage is adjusted by the voltage regulator 13b and the voltage is applied from the constant voltage generator 13 to the electrostatic induction treatment while applying a constant voltage of 1,500 to 5,000 volts for 4 to 10 hours, It is reformed with excellent water. At this time, a weak current in the range of 10 to 150 μA flows.

The transformer 13a of the constant voltage generator 13 includes an iron core 13d, a primary coil 13c, a secondary coil 13e, an output line 13f of the secondary coil 13e, a secondary coil 13e, And the voltage regulator 13b is connected to the primary coil 13c and the output line 13f of the secondary coil 13e is connected to an insulation processing terminal (14) of the wire mesh electrode (12).

The wastewater is supplied to the water collecting tank 12 and the output line 13f of the secondary coil 13e of the constant voltage generator 13 is transformed to the insulation processing terminal of the secondary coil 13e 13g are placed in an insulated state in the transformer 13a and the wire mesh electrode 14 is placed on an insulator which is insulated from the ground 13h by an insulator and the stainless steel plate 15 And ground 13h.

The condenser C _{2 in} which the insulating processing terminal 13g which is one end of the high-voltage secondary coil 13e in the transformer 13a is isolated from the insulating material in the transformer 13a is formed, It connects to the coil remaining earth (13h) and a water tank (12) insulating the one output line of (13f) by an insulator of (13e) form a capacitor (C _1), as a result, the output lines (13f) and ground ( 13h are in a range of 250 to 3,500 volts, a weak current in the range of 10 to 150 [micro] A flows, so that there is no risk of human contact with the water collecting tank 12 in a grounded state.

Electrostatic induction induces an electric charge of opposite polarity on the surface of a substance close to the entire mass when an electrically neutral substance is approached all over the charged mass. In addition, even when there is an electric field outside, it is opposite to the external charge. In this case, the induced charge is called induction charge, and the neutral substance has induction charge, which causes the charge to be induced in the material due to the external electrical action that is not in contact, so that the + charge and - charge are polarized This phenomenon is called induction of electrostatic induction. Applying AC voltage to the material by applying this phenomenon, rotation and vibration are applied to the molecules of the material to accelerate the assimilation of molecules and change the physical characteristics of the material. Treatment (electrostatic induction treatment).

In other words, in the present invention, the transformer 13a of the constant voltage generator 13 is of the outer coil type coil transformer type using the iron core 13d of the layered structure, and the transformer 13a of the primary side circuit of the transformer 13a The secondary coil 13e of the secondary circuit of the transformer 13a is connected to the insulation processing terminal 13g of the first stage through the voltage regulator 13b via the voltage regulator 13b, The output wire 13f of the secondary coil 13e of the secondary circuit is connected to the ground wire 13h and the insulator in the water collecting tank 12 is connected to the ground 13h, A voltage of 250 to 3,500 volts and a current of 10 to 150 microamperes are caused to flow in the electrostatic induction treatment, the water molecule group of the wastewater injected into the water collecting tank 12 is subdivided and the surface tension is reduced, Microorganisms become active in biological processing process.

The transformer 13a is formed by inserting a tubular insulating film in the center of the iron core 13d and winding the primary coil 13c and the secondary coil 13e on the outer circumferential surface of the insulating film and winding the primary coil 13c For example, 220-240 turns by using a copper wire coated with polyester having a diameter of 0.6 mm, and the secondary coil 13e is wound around a copper wire coated with enamel, for example, 0.09 mm in diameter However, the number of the first secondary coil 13e may be set at 22,000 times and the number of the second secondary coils 13e may be set at 18,000 times among 40,000 times of the secondary coil 13e The diameter and kind of the copper wire, and the number of turns of the copper wire are determined according to conditions such as the capacity of the water collecting tank 12, the processing time, and the applied voltage.

Usually, copper wire having a coil diameter of 0.03 to 3 mm can be used. Copper wire coated with polyester or enamel is used as the copper wire. 250 times, the secondary coil 13e is 28,000 to 40,000 times, or the first secondary coil 13e is 16,800 to 22,000 in the secondary coil 13e, and the second secondary coil 13e may be 11,200 to 18,000 volumes.

The insulating processing terminal 13g of the secondary coil 13e is located in the transformer 13a and its distal end portion is wound with an insulating tape and then an insulating material such as a tar pitch is charged into the transformer 13a, The insulation treatment terminal 13g of the coil 13e is enclosed and insulated so as to be insulated. In addition to the tar pitch, insulating oil, unsaturated polyester, polyurethane resin, or the like may also be used.

When the primary voltage of the transformer 13a is adjusted to be 100 to 220 volts by operating the voltage regulator 13b by flowing alternating current to the transformer 13a and between the terminals of the secondary coil 13e of the secondary side, The output line 13f is connected to the water collecting tank 12 on the insulated insulator because the insulating processing terminal 13g of the secondary coil 13e is insulated from the secondary side circuit by 12,000 to 18,000 volts. And a voltage of 3,500 to 5,000 volts and a current of 10 to 150 mu A flows between the ground and the ground 13h.

The above-described voltage of 12,000 to 18,000 Volts generated on the secondary side causes a voltage of 3,500 to 5,000 Volts and a current of 10 to 150 μA between the water collecting tank 12 and the ground 13h, The resistance of the insulation processing terminal 13g of the car coil 13e, the resistance of the insulator, and the AC resistance circuit of the coil.

That is, a resonance circuit is formed by the ground 13h of the constant voltage generator 13 and the ground 13h of the water collecting tank 12. The resonance circuit of the ground 13h, which is a region of the insulating processing terminal 13g, The output line 13f of the secondary coil 13h and the output line 13f of the secondary coil 13e are caused to undergo electrostatic induction by the resonance frequency due to the discharge from the output voltage by the ground 13h insulated by the insulator.

The voltage between the water collecting tank 12 and the ground 13h varies from 3,500 to 5,000 volts depending on the size of the water collecting tank 12 and the size and insulator of the wire mesh electrode 14 charged with the filling material, To 150 mu A. Further, the voltage and the current can be changed by adjusting the voltage from the voltage regulator 13b as the input power source.

As described above, the voltage of the water collecting tank 12 generated by the AC resistance circuit is 3,500 to 5,000 Volts when no load is applied. However, since the current is a weak current in the range of 10 to 150 占 안전, The voltage and the current to be applied to the water collecting tank 12 are adjusted by the voltage regulator 13b in accordance with the charge capacity of the bath and the electrostatic induction treatment condition, and there is no possibility of causing troubles such as electric shock or fire, However, in the normal case, the voltage between the water collecting tank 12 and the ground 13h is in the range of 550 to 1,600 volts, and the electric current is in the range of 30 to 100 占 폚, so that a proper AC electric field can be formed have.

In the water collecting tank 12, when the wire mesh electrode 14 in the water collecting tank 12 becomes a positive electric charge, - the electric charge is induced on the ground 13h side and conversely, the wire mesh electrode 14 in the water collecting tank 12 - When the electric charge is generated, the positive electric charge is transferred from the ground 13h side. Then, the electric charge and the negative charge are changed by the frequency (50 to 60 times) in one second in accordance with the frequency of the AC power source, (13h) side are also inherited and the + and - charges are changed.

In general, matter is formed by atoms, which are composed of nuclei and electrons, and the nuclei are made up of neutrons and protons, and around the nucleus, In the steady state in which the electrons are moving in a circular motion and the external electric field is not applied, the positive charge and the electron charge of both are stabilized in the same amount. However, when a high voltage is applied from the outside, And the electrons move in the opposite directions. As a result, the electric centers of the atoms do not coincide with each other. As a result, the atoms form an electric dipole, and an internal electric field is generated by the balance of the electric charges (Polarization) is generated.

In this case, since the atom (molecule) is polarized by an external electric field (an external electric field), it is referred to as an electron polarization (atomic polarization) or an atomic polarization (atomic polarization). When a high constant voltage is applied to the wastewater filled in the water collecting tank 12 All molecules try to adapt according to the change of + charge and - charge by induction of electrostatic induction, but there is a difference between strong and weak binding force between molecules. As the surface tension of surface of wastewater decreases, viscosity decreases and it dissolves in water Mineral components such as calcium, magnesium, iron and the like are also converted into ultrafine particles by promoting ionization of molecules, and then converted into activated water having high permeability.

Nuclear Magnetic Resonance of Influent Wastewater ¹⁷ O-NMR When the half-width value is 90 Hz or less and the surface tension is 68 dyne / cm or less and when the concentration of BOD ₅ and COD _Mn is as low as 500 mg / It is possible to omit the water reforming process such as the constant voltage induction process or the magnetization process because the biological treatment can be performed within the discharge reference value.

When the aerobic biological treatment water is not treated within the discharge reference level, the same aerobic biotic treatment as the above-mentioned first aerobic biological treatment is performed, as shown in the lower part of FIG. 3 'Aerobic biological treatment process diagram'.

In the first aerobic biologic treatment, overflowing overflow water is supplied to the secondary aeration tank 18b above the secondary settling tank 19a to supply air from the blower 26 to the secondary aeration tank 18b, A second aerobic biotreatment is carried out while the aeration is maintained so that the oxygen concentration is maintained in the range of 2 to 4 mg / l, the sediment is settled by the third settling tank 19b, and the overflowed second The aerobic biological treatment water is sent to the final treatment water tank 25 or the sterilization / filtration process.

When the solids, which are microbial cells precipitated in the third settling tank 19b, are collected by the third settling tank rake 20b into a central cone portion under the third settling tank 19b, they are activated by the second returning pump 21b A secondary microorganism activating tank 22b in which a secondary bioreactor 23b filled with a filler 24 containing minerals containing an activated humic substance pellet and an active mineral ingredient is incorporated and a secondary While being conveyed to the aeration tank 18b, the excess sludge discharged is sent to the input tank and the deodorization process. The design conditions and operating conditions are the same as those of the first aerobic biologic treatment.

2. Sterilization and filtration process

The aerobic biological treatment water is subjected to sterilization treatment by a combination of one or more kinds of treatment methods such as injection of an oxidizing agent, ultraviolet ray irradiation, electrooxidation or electron beam irradiation, and then subjected to sand filtration to remove suspended solids Next, discharge it.

end. Sterilization by injection of oxidizing agent

Sterilization by the injection of an oxidizing agent can be achieved by adding NaClO, ClO ₂ , Cl ₂ , H ₂ O ₂ Or O ₃ is injected in the range of oxidation-reduction potential in the range of + 700 to + 1,100 ° C., and the mixture is stirred for 30 to 60 minutes to sterilize microorganisms such as bacteria and viruses in the water .

I. Sterilization by ultraviolet irradiation (ultraviolet irradiation)

The sterilization by ultraviolet irradiation is performed by irradiating water at a dose of 100 to 300 kPa / cm 2 · min from ultraviolet sterilization with a wavelength of 250 to 260 nm to denature DNA base portions of microorganisms such as bacteria and viruses, And sterilization treatment is performed.

All. Sterilization by electrooxidation

In the sterilization treatment by the electrooxidation, the oxidation-reduction potential is set in the range of + 700 to + 1,100 ° C to sterilize microorganisms such as bacteria and viruses in the water.

la. Sterilization by electron beam irradiation

In the sterilization by electron beam irradiation, the microorganisms such as bacteria and viruses present in water are irradiated in water to destroy the base arrangement itself, and the sterilization treatment is performed.

Disinfection by electron beam irradiation is performed by sterilizing microorganisms in water by irradiating the electron beam from 0.1 to 10 MeV in the range of 0.1 KGy / h to 100 MGy / h in terms of the rate of electron beam irradiation .

Since the efficiency of the sterilization treatment is improved when the oxygen concentration in the water is high or when oxidizing agents (NaClO, H ₂ O ₂ , O ₃ , ClO ₂ , HClO, Cl _2, etc.) are present, The sterilization treatment efficiency can be further improved by injecting an oxidizing agent, and the sterilization treatment efficiency can be improved even when electron beams are irradiated while air (oxygen) is supplied to increase the concentration of dissolved oxygen in the water.

5. Filtration process

The sterilized water is subjected to sand filtration to remove suspended solids in water and then discharged.

The filtration speed of the sand filtration is 6 to 10 m / hour, the effective diameter of the filtration sand is 0.3 to 0.45 mm, the uniformity coefficient is 2.0 or less, The thickness is 0.5 to 1.0 m. In this case, the filtration pressure is determined by considering the pressure loss of the filter and the pressure loss of the pipe depending on the operating conditions.

The sterilization and filtration process may be omitted if the concentration of suspended solids in the water is less than 50 mg / L and sterilization is not required.

The pH of the solution was adjusted to 7.6 by injecting a 20% aqueous solution of sulfuric acid into the supernatant obtained by precipitating the solids shown in Table 3 in Example 1. 400 kg of the supernatant was injected into a 0.5 m 3 plastic pail to confirm the aerobic biological treatment efficiency of the present invention 1 kg of corrosion pellets, which were mined from the Taraki wetland in Nagasaki Prefecture, Japan, and then treated with the corrosion-resistant soil with the composition shown in Table 4, and mined from the volcanic area of Aso Mountain in Kumamoto Prefecture, Japan 2 kg of pumice with the composition shown in Table 5 was placed in a mesh bag and installed in plastic basin. The excess sludge discharged from the aerobic biologic treatment was injected at a MLSS concentration of 3,200 mg / L, dissolved oxygen concentration (BOD ₅₎ and COD _Mn (BOD ₅₎ and COD _Mn (BOD ₅ ) were measured in batch aerobic biochemical treatment, As shown in Fig.

Analysis of composition of building constituents ingredient Organic matter SiO ₂ Al ₂ O ₃ Fe ₂ O ₃ Na ₂ O K ₂ O CaO MgO Etc content(%) 32.7 52.5 7.8 4.0 0.5 0.3 0.5 0.5 1.2

Component composition analysis of Pumice ingredient SiO ₂ Al ₂ O ₃ Fe ₂ O ₃ Na ₂ O K ₂ O CaO MgO TiO ₂ Etc content(%) 68.50 15.07 1.92 4.33 4.38 1.41 0.48 0.45 3.46

BOD ₅ and COD _Mn were measured by treatment time in batch aerobic biologic treatment. Processing time (hr) BOD ₅ (mg / l) COD _Mn (mg / l) Processing time (hr) BOD ₅ (mg / l) COD _Mn (mg / l) 6 142 203 12 98 127 8 125 179 14 89 104 10 110 157 16 82 93

As shown in the analytical values of BOD ₅ and COD _Mn measured in the treatment time in the above Table 6 batch aerobic biologic treatment, when the aerobic biological treatment is carried out with the capacity of the aeration tank being 12 hours or more, .

In order to confirm the aerobic biological wastewater treatment efficiency by the water reforming treatment, a stainless steel plate as a conductor was installed under the same 0.5 m 3 plastic container as in Example 2, A plastic plate as an insulator was provided on the upper part, and a metal wire electrode filled with charcoal was provided on a plastic plate.

Aqueous solution of 20% sulfuric acid was injected into the supernatant obtained by precipitating the solid matter of Table 3 treated in Example 1 in the plastic tube equipped with the wire mesh electrode, and 400 kg of the pH adjusted to 7.6 was injected into a 0.5 m3 plastic pail. Nuclear magnetic resonance (NMR) spectrum of water The half width (half width) of ¹⁷ O-NMR was measured and found to be 127 Hz. Then, a high voltage of 3,500 volts was applied from a static voltage generating device to a wire mesh electrode installed in a plastic bag for 4 hours to perform a static pressure treatment, and then a nuclear magnetic resonance spectrum of water ^As a result of measuring the half width of ¹⁷ O-NMR, it was confirmed that the water was modified at 58 Hz.

1 kg of corrosion pellets and 2 kg of pumice stone, which had been treated with the same corrosion-resistant as in Example 2, were placed in a mesh bag, and the water was subjected to a reforming treatment. The excess sludge was injected with MLSS concentration of 3,200 mg / L, aerated by injecting air to maintain the dissolved oxygen concentration of 2 to 3 mg / L, and BOD ₅ and COD _Mn The results were processed as shown in Table 7 below.

BOD ₅ and COD _Mn were measured at the treatment time in the batch aerobic biologic treatment after the water was reformed. Processing time (hr) BOD ₅ (mg / l) COD _Mn (mg / l) Processing time (hr) BOD ₅ (mg / l) COD _Mn (mg / l) 6 127 182 12 89 116 8 112 160 14 81 95 10 99 126 16 75 84

As shown in the analysis results of the BOD ₅ and COD _Mn of the treatment time in the batch aerobic biologic treatment after the water was reformed as shown in Table 7, the treatment efficiency was improved by about 10% as compared with the batch aerobic biological treatment of Example 2 If aerobic biologic treatment is performed after the water is reformed, aerobic biologic treatment of the aeration tank with a capacity of 10 hours or more can be performed to a level lower than the allowable level of pollutant emission in the area.

Ⅲ. Composting step

Food waste is high in water content and high in salinity, so it can not be composted reasonably. Therefore, in the present invention, only the dehydrated dehydrated cake is composted in order to reduce the water content of the water content adjusting agent (moisture control agent) by reducing the moisture content, and since the desalted dehydrated cake is difficult to desalt in the solid state, After desalting, we suggest how to compost.

In the composting step, the dewatered cake of the primary dehydration process is injected into the aerobic liquefier 100, and organic substances such as protein, sugar, starch and fat, which are easily decomposed by high temperature aerobic fermentation, When the temperature rises to 60 ~ 80 ℃ due to decomposition heat as a simple inorganic substance, seeds of harmful pathogens, seeds of weeds and eggs of insect pests are liquefied and liquefied. At this time, the water is evaporated and the salt is concentrated, When the value is in the range of 50 to 60 ms / cm, the activity of the microorganism is lowered and the fermentation efficiency is lowered. Therefore, the high temperature aerobic fermentation is carried out to remove the salt by desalting process, The present invention relates to a method of liquefying or composting a liquefied petroleum gas or a solid-phase composting process, the details of which are as follows .

1. Liquefaction Process

When the dewatering cake of the primary dehydration process is supplied to the aerobic liquefier 100, the aerobic liquefier mixer 101 mixes the high-temperature aerobic fermentation liquid at 60 to 80 DEG C at a rotating speed of 2 to 4 rpm, Stream through the nozzle on the upstream side of the oxygen dissolving apparatus 103 of the aspirator type and is injected to the gas inlet side through the nozzle on the upstream side of the oxygen dissolving apparatus 103 which is concentrated in the pressure swing adsorption (PSA) When one type of oxygen is supplied together with oxygen or oxygen from an oxygen storage tank or oxygen in the oxygen storage bomb, oxygen gas is sucked by Bernoulli's theorem and the downstream of the oxygen dissolving apparatus 103 When the high-temperature aerobic fermentation broth in which oxygen is dissolved is supplied to the upper portion of the liquefier 100, oxygen and high-temperature aerobic microorganisms are added to the solid food waste in the aerobic liquefier 100, ball It is.

When the high-temperature aerobic fermentation broth in which oxygen is dissolved is supplied to the upper portion of the liquefier 100, the solid food waste is decomposed into low-molecular substances by the high-temperature aerobic microorganisms, and the solid food waste is liquefied. The liquefied liquid food waste escapes into the lower hole of the aerobic liquefier 100 and is transported to the liquid food waste storage tank 104.

In the aerobic liquefier 100, when non-degradable substances such as vinyl, plastic, gravel, pebbles, sand, bone, shell, animal bone, etc. are accumulated, Liquid separation process, the liquid material is sent to the liquid food waste storage tank 104, and the solid material is disposed of (incinerated or buried).

When the alcohol fermentation treatment is performed, the fermentation liquid of the methane fermentation step is also sent to the liquid food waste storage tank 104 when the fermentation waste liquid and the methane fermentation treatment are performed in the alcohol fermentation process.

In the case where the liquid-phase food waste storage tank 104 is not required to be laid out, the liquid food waste storage tank 104 and the liquid food waste transfer pump 105 are omitted, and the liquid- Liquid food garbage may be sent to the high-temperature aerobic fermentation tank 106.

The solid-liquid separation step uses one of a Trommel separator or a vibrating screen.

The aerobic liquefier 100 is a steel structure provided with a heat insulating material 102 on the outside and may be a horizontal structure as shown in Fig. 4, but it may be a vertical structure, or alternatively, Concrete structures may also be used.

The aerobic liquefier mixer 101 may be a paddle type, a horse anchor type, a ribbon type, a helical ribbon type, a screw type, One of which is equipped with a bladed blade in a stirring arm, and a mixing speed is 2 to 4 rpm.

Bacillus stearothermophilus, Bacillus coagulans, Bacillus flavothermus, Bacillus flavothermus, and Bacillus cereus are the most commonly used strains for Bacillus species such as Bacillus stearothermophilus, Bacillus coagulans, Bacillus species such as Bacillus kaustophilus, Bacillus schlegelii, Bacillus smithii, Bacillus thermocatenulatus, Bacillus thermocloacae, Bacillus thermocloacae, thermodenitrificans Bacillus thermoglucosidasius Bacillus thermoleovorans Bacillus tusciae Bacillus thermoruber Bacillus brevis Bacillus palpharseus Bacillus pallidus) · High temperature bacillus such as Bacillus lentus ), Clostridium thermosaccharolyticum, Lactobacillus thermophilus, Lactobacillus delbrueckii, Synechococcus lividus, and the like. , Streptococcus thermophilus, Streptomyces thermophilus, Desulfotomaculum nigrificans, Geobacillus thermodenitrificans, Geoacillus thermophilus, Such as Geobacillus toebii, Geobacillus stearothermophilus, Geobacillus sp., Geobacillus stearothermophilus, Geobacillus thermoleovorans such as Geobacillus stearothermophilus, ), Geobacillus sp., Thermoshell fume Such as Thermocrispum sp., Thermus thermophilus, Anoxybacillus beppuensis, Anoxybacillus rupiensis, Anoxybacillus flavithermus, and the like, such as Thermocrispum sp., Thermus thermophilus, Anoxybacillus rupiensis, Such as Thermoactinomyces vulgaris, Thermoactinomyces sacchari, Thermomonospora curvara, and the like, as well as other thermophilic bacteria such as Thermophilic bacteria such as Thermoactinomyces vulgaris, Thermoactinomyces saccharia, Thermomonospora curvara, Actinomycetes, Sulfolobus acidocaldarius, Alicyclobacillus sendaiensis sp., Humicola insolens, Mastigocladus laminosus, Tararomai, Talaromyces dupontii or Geotrichum candidum may be one or more thermophilic 0.04 to 0.1 part by weight of foodstuffs which are cultured in a medium containing L or L of a thermophilic bacteria or a WSG medium and added with a certain amount of ingredient into the liquefier 100 is added to the liquefier 100 as aerobic The compost which is being fermented in the process of being fed to the liquefier 100 or the high-temperature aerobic fermentation tank 106 or fermenting the organic waste at a high temperature of 60 to 80 ° C in the fermentation process is fed to the liquefier 100 It is necessary to supply aerobic microbial bacteria to the aerobic liquefier 100 or the high-temperature aerobic fermentation tank 106 for 0.1 to 0.5 parts by weight per 100 parts by weight of the incoming food waste. And it is not necessary to continuously supply the strain when normal operation is performed.

2. High-temperature aerobic fermentation process

In order to perform fermentation by aerobic microorganisms in a liquid state, the concentration of dissolved oxygen should be maintained at 2 to 4 mg / L, and as shown in FIG. 9 'dissolution diagram of oxygen in water according to temperature change under atmospheric pressure In the case of organic wastes where the dissolved oxygen saturation concentration is 3 mg / l when the oxygen is simply injected at 80 ° C and the impurities such as organic matter and salinity are present, the dissolved oxygen saturation concentration further decreases to 60-80 ° C. There is a problem that it can not be maintained at 2 to 4 mg / L, so that the high temperature aerobic fermentation has not been carried out in the liquid state until now.

 As can be seen from FIG. 10, 'Oxygen dissolution diagram in water with changes in temperature and pressure', it can be seen that the concentration of dissolved oxygen saturation increases at low temperature and high pressure.

The inventor of the present invention has conducted an intensive investigation and found that when oxygen is dissolved in a state where partial pressure of oxygen and total pressure are high and supplied to a high temperature aerobic fermentation process at 70 to 80 ° C, , We have found that high temperature aerobic fermentation can occur.

When the liquid food waste liquefied in the liquefaction process is supplied to the high temperature aerobic fermentation tank 106, a heating jacket 108 installed outside the high temperature aerobic fermentation tank 106 is mixed with the high temperature aerobic fermentation tank stirrer 107, ) Is supplied with heat from the boiler to adjust the temperature in the range of 60 to 80 ° C and the oxygen or oxygen in the oxygen storage tank or the oxygen storage bomb and the aerobic fermentation liquid at high temperature in the PSA (Pressure Swing Adsorption) Temperature fermentation broth in which oxygen is dissolved at 2 to 4 atmospheres (atm) is fed to the pressurized oxygen dissolving tank 110. The high-temperature aerobic fermentation broth containing the carbohydrate, starch, protein, fat (Fat), decomposing easily decomposable organic matter into simple inorganic substances such as CO ₂ and H ₂ O, and destroying harmful pathogens, seeds of weeds and insect pests.

The reaction mechanism at this time is as follows.

① For carbohydrates

Carbohydrates can be represented by C _m (H ₂ O) _n . Carbohydrates such as starch and sugar are oxidatively decomposed and eventually become carbon dioxide (CO ₂ ) and water (H ₂ O).

C _m (H ₂ O) _n + mO ₂ → mCO ₂ ↑ + nH ₂ O ↑ + reaction heat ... ... ... ... ... ... ... ... ... ... (11)

② fat, protein and fat

Proteins and fats are oxidized and decomposed as shown in the following reaction formula (12) to gradually release carbon dioxide, water, and ammonia, resulting in a substance having a small molecular weight.

C _x H _y N _z O _p + aO ₂ → C _u H _v N _w O _q + bCO ₂ + dH ₂ O + eNH ₃ + reaction heat ... ... ... ... (12)

Ammonia produced by decomposition of protein and fat reacts with primary water to produce ammonium hydroxide. Further, ammonium ions are oxidized to nitrate by nitrifying bacteria and nitrifying bacteria of aerobic microorganisms. Nitrate is the nitrogen source that plants are most likely to use.

NH ₃ + H ₂ O → NH 4 ⁺ + OH ^- ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (13)

Ammonium ions are first oxidized to nitrite by nitrite bacteria (Nitrocystis, etc.).

NH ₄ ⁺ + 3 / 2O ₂ → NO ₂ ^- + H ₂ O + 2H ⁺ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (14)

Next, nitrite is oxidized to nitrate by nitrifying bacteria (Nitrosomonas, Nitrosococcus, Nitrosospira, etc.).

NO ₂ ^- + 1 / 2O ₂ → NO ₃ ^- ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (15)

When the high-temperature aerobic fermentation temperature rises to around 70 ° C, most of the pathogenic bacteria, pests, eggs, viruses, and weed seeds are inactivated and hygienically safe compost can be produced.

In the reaction of Equations (11) and (12), organic matter is decomposed into carbon dioxide and water, and a considerable amount of water contained in the food waste is evaporated by the heat of reaction. At this time, as the water is evaporated and the salinity is concentrated and the electrical conductivity value is in the range of 50 to 60 ms / cm, the activity of the microorganism is lowered and the fermentation efficiency is lowered. Thus, the high temperature aerobic fermentation solution, To the reaction tank (111).

The heat source may be supplied from the high temperature aerobic fermentation tank 106 to the boiler by supplying heat to the heating jacket 108 provided outside the high temperature aerobic fermentation tank 106 or by installing an electric heater in the high temperature aerobic fermentation tank 106 And the heat can be supplied also by electric heating. When the high-temperature aerobic fermentation occurs normally as in the above reaction formulas (11) to (12), when the temperature is in the range of 60 to 80 ° C due to the self-reaction heat, the heat source supply is stopped from the outside.

The high-temperature aerobic fermentation tank 106 may be a circular iron structure for supplying a heat source from the boiler to the warming jacket 108 that has been thermally treated with a warming material 102 on the outside as shown in FIG. 4, A heating coil may be provided inside or an electric heater may be installed to supply heat. It can also be a concrete structure instead of a steel structure.

The high temperature aerobic fermenter stirrer 107 is a pitched paddle type stirrer and the stirring speed is 4 to 8 rpm.

3. Desalination Process

Since garbage (NaCl) concentration is high in food waste, composting can not be performed without desalination treatment. Therefore, in the present invention, lime and fly ash are injected into high-temperature aerobic fermentation treated at high temperature and aerobic fermentation so that water- Temperature aerobic fermentation broth to which the salt removed by precipitation has been removed is sent to a mesophilic aerobic fermentation tank 118 to be fermented at middle temperature to produce a slurry or a high temperature aerobic fermentation broth in which salt has been removed is supplied to the mixer 120, , A water absorbent, and a soil conditioner are mixed and fed to a fermentation / aging tank (123) for fermentation, aging, and composting.

Since the dehydrated food waste discharged from the primary dehydration process, the fermentation waste discharged from the alcohol fermentation process, and the fermentation liquid discharged from the methane fermentation process exist in the water-soluble salt, they must be desalted to be composted. The separation and removal of dehydrated dewatered cake or foreign matter discharged from the tea dewatering process and the reaction of the large-sized material with the lime and coal fly ash in the solid state reactor of the food waste which has been crushed in the crusher were dehydrated in the primary dehydration process (3CaO · Al ₂ O ₃ · CaCl ₂ · 10H ₂ O) in the form of insoluble Friedel's salt (3CaO · Al ₂ O ₃ · CaCl ₂ · 10H ₂ O), but the carbon dioxide generated in the high temperature aerobic fermentation process CO ₂₎ and then equation (16) and the back of chloride ion (Cl as shown in Scheme 17 by ^- so) the re-dissolution in the desalination process Once again it injected with lime and coal ash, and converted into salts insoluble in water, and then, is necessary to remove precipitate.

CO ₂ + H ₂ O → 2H ⁺ + CO ₃ ^{2 -} ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (16)

_{3CaO · Al 2 O 3 · CaCl} 2 · 10H 2 O + CO 3 2 - → 3CaO · Al 2 O 3 · CaCO 3 · 10H 2 O + 2Cl - ... (17)

When the high-temperature aerobic fermentation broth is supplied to the saline reaction tank 111, lime and coal fly ash are poured into the salt tank agitator 112 while stirring, and stirred for 30 to 40 minutes. The water-soluble salt is converted into a salt-insoluble salt, and then sent to the salt-reactant sedimentation tank 113.

When the salt reactant converted into a salt insoluble in water is supplied to the salt reactant settling tank 113 and precipitates to the lower portion of the salt reactant settling tank 113, the salt reactant settler trough 114 is rotated at 0.01-0.02 rpm, Cone), and then sent to the tertiary dehydration process by the salt reactant settler sludge transfer pump 115 to discard the dehydrated cake containing insoluble salt in the water, and the dehydrated filtrate is transferred to the upper part of the salt reactant settling tank 113 Is sent to the high temperature aerobic fermentation broth (116) in which salinity is removed together with the overflowing overflow.

The high-temperature aerobic fermentation broth in which the salt has been removed is supplied to the mesophilic aerobic fermentation tank 118 in the slurry production process by the high-temperature aerobic fermentation broth transfer pump 117 from which the salt has been removed , Or to the mixer 120 of the solid compost production process.

The reaction in which the salt is removed by the reaction formula (6) and the reaction formula (7), the salt and the fly ash and the lime react in an equivalent amount of the equivalent amount, but the composition of the fly ash varies depending on the type of coal used in the thermal power plant And the amount of the fly ash is preferably 2 to 3 times as much as the amount of the salt, and the lime is supplied within a range where the pH does not exceed 10. If the pH is more than 10, it will interfere with the growth of fermenting microorganisms. Preferably, the lime is supplied at a pH ranging from 8.4 to 9.5.

When the CaO component is contained in the fly ash in an amount of 10 wt% or more, lime may not be supplied separately.

It is not necessary to neutralize the lime even if the lime is supplied and the pH is about 10. Ca (OH) ₂ , which is a component of lime, reacts with carbon dioxide (CO ₂ ) produced by fermentation and is neutralized with calcium carbonate (CaCO ₃ ).

The saline reaction tank 111, the salt reactant settling tank 112, and the high temperature aerobic fermentation broth 116 from which the salt is removed are made of iron structure or concrete structure.

The saline reactor stirrer 112 is a propeller type, and the capacity of the saline reaction tank 111 is set so that the stirring speed is 180 to 360 rpm and the stirring reaction time is 30 to 40 minutes.

The salt reactant settler rake 114 has the same structure as the rake of the thickener of the lower wastewater treatment plant, and the rotation speed is 0.01 to 0.02 rpm.

The salt reactant settling tank 113 has a sectional loading of 60 to 90 kg / m 2 · hr, a depth of 3 to 5 m, and a slope of 1/10 to 1/20 .

The capacity of the high temperature aerobic fermentation broth 116 from which the salt is removed has a residence time of 30 minutes or more, and an upper limit of 30 minutes or more is not limited.

In place of the desalting method in which the water soluble salt is converted into a water-insoluble salt by injecting lime and fly ash into the high-temperature aerobic fermentation, the method described in Patent Document 4 'Electrophoresis of a food waste dewatering filtrate desalination apparatus' The desalination process may be performed by a desalting process for removing the salt.

The high temperature aerobic fermentation broth containing the salt is injected into the interior separated by the cation exchange membrane and the anion exchange membrane while a direct current is applied from the rectifier to the desalination unit composed of the desalting chamber provided with the anode and the cathode outside, When Na ⁺ ions contained in the organic waste migrate to the cathode of the desalting chamber through the cation exchange membrane by electrophoresis, the Cl ^- ion passes through the anion exchange membrane and the anode of the desalting chamber , The high temperature aerobic fermentation broth which the salt contained in the high temperature aerobic fermentation broth is extracted and removed by the desalting bath is sent to the liquid production process or the solid compost production process.

3. Liquid production process

When the high-temperature aerobic fermentation broth in which the salt is removed is supplied to the mesophilic aerobic fermentation tank 118, air is blown from the blower 127 so that the dissolved oxygen concentration is maintained in a range of 1 to 4 mg / Aerobic fermentation makes liquid fertilizer. The liquid fermentation liquid, which is a medium temperature aerobic fermentation liquid, is sent to the tank lorry by the liquid transfer pump 119 and is shipped to the liquid product.

The mesophilic aerobic fermentation is a process in which the degradable polymer organic substances such as lignin and cellulose, which were not degraded by high temperature aerobic fermentation, are decomposed by mesophilic aerobic microorganisms and nitrification of the unoxidized ammonia by nitric acid, It progresses gently compared to fermentation.

In the mesophilic aerobic fermentation tank (118), when a new operation is started after commissioning or idle (suspended), bacillus such as Bacillus subtilis, Bacillus mycoides, Bacillus natto Streptomyces griseolus, Streptomyces olivaceus, Streptomyces griseus, Micromonospora purprea, Micromonosporaekinosu, Streptomyces griseolus, Streptomyces griseus, Actinomycetes such as Micromonospora echinospora, Micromonospora fusca, Micromonospora olivasterospora, Lactobacillus sp., Streptococcus sp. Lactic acid bacteria such as Streptococcus sp., Pediococcus sp., Leuconostoc, Saccharomyces sp. Yeasts such as Sporobolomyces sp. And Cryptococcus sp., Aspergillus sp., Penicillium sp., Fusae sp. Microorganisms such as Fusarium sp., Mucor sp., Rhizopus sp., Micrococcus sp., Spirochaeta sp. ), A middle-temperature aerobic microbial strain prepared by mixing at least one kind of bacteria among Bacterium such as Clostridium sp. And Pseudomonas sp., Is used to remove the salt introduced into the mesophilic aerobic fermentation tank (118) 0.02 to 0.1 part by weight of the aerobic microorganism strain is fed to 100 parts by weight of the aerated aerobic fermentation broth at a temperature of 20 to 40 占 폚 for composting the organic waste, When the salt introduced into the mesophilic aerobic fermentation tank 118 is removed From 0.04 to 0.1 in aerobic fermentation broth on 100 parts by weight of parts by weight for the microorganisms it is necessary to supply the aerobic microorganisms in the medium temperature gyunje aerobic fermentors (118). And, in normal operation, it is not necessary to continuously supply aerobic microbial strains.

As described above, high-temperature aerobic fermentation and mesophilic aerobic fermentation can be performed at high temperature and atmospheric aerobic fermentation microorganisms and mid-temperature aerobic fermenting microorganisms, such as biologically active substances such as vitamins useful for plant growth, growth promoting substances such as hormone, In addition, at high temperature aerobic fermentation, harmful pathogenic microorganisms, seeds of weeds and larvae of larvae are killed and thus hygienically safe liquid or solid compost can be produced. In other words, since conventional aerobic fermentation can not be carried out in the production of liquid fertilizer, it can be said that harmful pathogenic microorganisms, seeds of weeds and larvae of larvae are not completely killed.

4. Process of compost production

The high temperature aerobic fermentation liquid from which the salt has been removed and the dehydration cake of the second dehydration process are injected into the mixer 120, the water content adjusting agent is added, and the mixture is mixed while mixing with the mixer mixer 121, To the fermentation / fermentation tank 123 by the fermentation / fermentation tank 123. In order to reduce the consumption of the water content modifier, a water content modifier may be mixed with a water content modifier, and a soil conditioner may be added to supplement the function of the compost.

In the composting step, as in the mesophilic aerobic fermentation tank 118, when the microbial aerobic fermentation tank 118 is newly operated after the trial operation or the suspension, the mesophilic aerobic microbial strains are introduced into the mixer 120 0.04 to 0.1 part by weight per 100 parts by weight of the sum of the high-temperature aerobic solids from which salt is removed and the dehydration cake of the secondary dehydration process is supplied to the seed or the aging process for composting the organic waste is carried out at 20 to 40 캜 0.04 to 0.1 part by weight of the aerobic microorganism homogenate is added to 100 parts by weight of the high-temperature aerobic fermentation broth which has been removed from the salt introduced into the mesophilic aerobic fermentation tank 118 for the microbial fermentation, It is necessary to supply. And, in normal operation, it is not necessary to continuously supply aerobic microbial strains.

The water content modifier may be selected from the group consisting of pulp, coconut peat, peat moss, peat, peat, humus, and the like, which are excellent fibrous materials (absorbent) Mulberry), cotton crumbs, bark, sawdust, wood powder, chaff, straw, barley straw. A mixture of one or more kinds selected from straw, cornflakes, bagasse, soybean cake, bran, oilseed rape, coffee bean, tea cake, The removed high-temperature aerobic fermentation broth is fed with a water content ranging from 55 to 65 wt%.

The purpose of using the water content adjusting agent in the present invention is to increase the ratio of carbon to nitrogen (C / N ratio) while improving the air permeability by improving the porosity while absorbing the liquid fermentation liquid and bulging it, So as to suppress volatilization of the nitrogen component.

In the present invention, when the organic substance which is easily decomposed in the high-temperature aerobic fermentation is decomposed, when it is used as a water content adjusting agent containing a substance which is easy to decompose, aging becomes long during the aging process, It is preferable to use one or two or more kinds selected from the group consisting of degraded coconut peat, humus soil, peat moss or peat as a water content adjusting agent.

Pectin, Carrageenan, Guar gum, Xanthan gum, Gum arabic (gum arabic), gum arabic (gum arabic), and gum arabic are excellent in water absorption properties to reduce the required amount ), Locust bean gum, dimethyl amino ethyl methacrylate, diethyl amino ethyl methacrylate, diethylamino-2-hydroxypropyl methacrylate ( Diethyl amino-2-hydroxypropyl methacrylate, dimethyl amino propyl methacrylate, dimethyl amino ethyl methacrylamide, sodium alginate, sodium polyacrylate crosslinked ( Poly-N-vinylacetamide, hydroxyethylcellulose, and the like, such as cross-linked sodium polyacrylate, cellulose, carboxymethyl cellulose, alginic acid, hyaluronic acid, polyglutamic acid, chitosan, polylysine, silk, fibroin, , Cellulose glycolic acid, oxidized cellulose, cross-linked products, polyvinyl alcohol, polyacrylamide, polyvinylpyrrolidone, polyhydroxy alcohols, Polyvinyl methyl ether, polyisobutylene-maleic acid, poly 2-acrylamido-methyl-1-propanesulfonic acid (Poly 2 2-methylpropanesulfonic acid, 2-acrylamido-2-methylpropanesulfonic acid, polyvinyl phosphonic acid, polymethacryloyl- 1-oxyethyl Poly 4-vinylpyridine, NN-dimethyl-N- (3-acrylamidopropyl) -N- (carboxymethyl) ammonium [NN-Dimethyl (Superabsorbent) materials such as poly (ethylene glycol), poly (ethylene glycol), poly (dioxolane), and polyethyleneimine. Or a mixture of two or more kinds thereof is used as a water absorbing agent. The amount of the water absorbing agent to be used is 1 to 10 parts by weight of a water absorbent mixed with 100 parts by weight of the water content adjusting agent.

Instead of the moisture content adjusting agent, a pre-dry fibrinogen powder may be used. It is also possible to use a mixture of 100 parts by weight of the fibrous powder before drying and 1 to 10 parts by weight of the water absorbent.

The soil conditioner is selected from the group consisting of Loess, Bentonite, Kaolinite, Phyllite, Vermiculite, Illite, Kaolin, Zeolite, Perlite, Paper sludge carbide of paper mills, smectite, montmorillonite, calcined feldspar, activated silica minerals, charcoal, bamboo charcoal, activated charcoal, , Activated carbon (activated carbon) activated by coal, carbon black produced by unstable combustion of fuel or carbon black (charcoal), or a mixture of two or more of them. In the aged compost, To 15 wt%.

The mixer 120 may be a horizontal type as shown in FIG. 4, but may be a vertical type. The mixer mixer 121 is of a paddle type or a screw ribbon type and has a rotation speed of 2 to 4 rpm and a mixing time of 30 to 40 minutes.

When the mixed mixture mixed in the mixer 120 is supplied to the fermentation and aging tank 123 by the mixed conveying conveyor 122, oxygen is supplied while being turned over to the rotary mixer 121, Carbohydrates such as sugars and starches which are easy to be decomposed are fermented and decomposed. Finally, the organic substances which can be decomposed by mesophilic microorganisms such as molds, aquatic bacteria and general bacteria are finally decomposed and then released into compost products when they are aged. In the case where the composting capacity is small, the rotary mixer 124 may be used to flip the cabin with the sprocket 125 instead of flipping it.

As shown in FIG. 4, when the composting treatment capacity is small, the open-type circular fermenting device (open-type fermenting device) is used instead of the open / Open - type fermentation device (open type fermentation device), open type fermentation device (open type fermentation device), open type fermentation device (open type fermentation device), Endless Scoop type fermentation device, Upper type aeration type fermentation device, Rotary kiln type closed type horizontal type fermentation device, Open type horizontal type fermentation device, Open end type fermentation device, (Sealed type fermenter) or enclosed type fermenter (sealed type fermenter), sealed type multistage type fermenter (sealed type multistage fermentation type fermenter). In the present invention, the type of the fermentation-aging tank is specifically limited It does. The number of times of flipping by the rotary mixer 124 is about 2 to 4 times a day.

Table 8 shows the results of analyzing the dehydrated cake dewatered from the food waste disposal plant for dehydrating and treating food waste separated and disintegrated in the above Example 1 by using a screw press filter.

Analysis table of food waste dewatering cake pH Flammability (wt%) Ash (wt%) Moisture (wt%) Electrical Conductivity (ms / cm) 4.7 20.3 5.1 74.6 22.4 (corresponding to 1.3 wt% of NaCl)

1,000 kg of the dewatered dehydrated cake was poured into a round tank of a steel structure having a capacity of 1.2 m 3 and mixed with a paddle type mixer at a rotating speed of 2 rpm while the compost 1 was fermented at a high temperature of 60 to 70 캜 Kg was supplied for the aerobic fermentation microorganisms at high temperature and oxygen was supplied from the oxygen storage bomb to the lower part of the tank while being maintained at 70 to 75 ° C by the electric heat provided inside the tank. As a result, Was liquefied and discontinued and 35 kg of non-liquefied solids such as un-liquefied shells, glass fragments, small stones, sand, and vinyl pieces were removed.

After removing the non-liquefied solids from the tank, the mixer was replaced with a pitched paddle type stirrer and the liquefied liquid food waste in the tank was pumped into the tank with a pump The oxygen is supplied from the oxygen storage bomb while the pressure is maintained at a pressure of 2 to 3 atmospheric pressure to return the liquid food garbage dissolved with oxygen while the dissolved oxygen concentration is maintained in the range of 2 to 3 mg / When the aerobic fermentation was carried out for 14 hours at a temperature of 70 to 75 ° C, the electric conductivity value was 60 ms / cm and the operation was stopped. At this time, the amount of aerobic fermentation broth decreased to 368 kg. In other words, 597 kg (= 1,000-368-35) of the high-temperature aerobic fermentation was evaporated by carbon dioxide and moisture, indicating that it was reduced.

16 kg of lime and 20 kg of fly ash as shown in Table 2 were poured into 368 kg of the aerobic fermentation broth and stirred at a rotating speed of 360 rpm for 40 minutes by a propeller type stirrer. Thereafter, stirring was stopped, The precipitated precipitate was dehydrated by a vacuum dehydrator, and the dehydrated cake was discarded, and 310 kg of a dehydrated filtrate and a desalted aerobic fermentation broth as a supernatant were obtained.

As a result of measuring the electrical conductivity of the desalted aerobic fermentation broth, it was confirmed that the salt concentration dropped to 0.1 wt% or less at 1.8 ms / cm.

To 310 kg of the desalted aerobic fermentation broth, 150 kg of a mixture of 10 parts by weight of poly-gamma-glutamic acid and 100 parts by weight of coconut peat having a water content of 7.5 wt% 15 kg of Vermiculite (138 meq / 100 g of Cation exchange capacity, CEC) and 15 kg of charcoal were mixed, and compost was prepared by twisting the blend with a slave for 20 days twice a day.

100 kg of the compost made in Example 4, 100 kg of clay containing 30% of clay in the pH range of 4.5 to 5.5, 1 kg of borax, 13 kg of slow-release fertilizer for strawberry of N-company, 1.5 kg of metalaxyl and 3 kg of carbofuran (Furadan) as an insecticide were mixed to make a strawberry cultivation soil.

The above soil was poured into a strawberry cultivation pot (pot), and strawberry was cultivated. As shown in FIG. 11, it was confirmed that strawberry was normally lost without causing salting.

IV. Methane fermentation step

Conventionally, in the methane fermentation of food waste, the entire food waste that has been pre-treated such as the removal of foreign materials and the crushing treatment is subjected to the methane fermentation treatment, thereby consuming a large amount of the facility investment, In the present invention, the methane fermentation method of the present invention is characterized in that the pre-treated food wastes are dehydrated to a water content of about 75% and the capacity for methane fermentation is reduced to 1/10 to 1 / 20, the concentration of the organic substance is concentrated in the range of 20 to 25%, and the methane fermentation is carried out. As a result, the methane fermentation method of the food waste with improved methane fermentation yield with the reduced facility cost is presented. FIG. 5 'Methane fermentation process diagram' will be described in detail as follows.

1. Anaerobic liquefaction process

When the dehydrated cake of the primary dehydration process is supplied to the anaerobic liquefaction tank 200, the methane fermentation liquid of the methane fermentation tank 209 is fed into the anaerobic liquefying tank mixer 201 at a mixing rate of 2 to 4 rpm, The sludge is supplied to the sludge conveying pump 211 and a heat source is supplied from the boiler to the heating jacket 202 provided outside the anaerobic liquefier 200. The solid food waste is treated with liquid food waste while being maintained at 50 to 60 캜 , The liquid food waste is sent to the liquid food waste storage tank 204 and sent to the acid fermentation tank 207 by the liquid food waste transfer pump 205.

In the anaerobic liquefaction tank 200, non-liquefied materials such as sand, soil, and glass fragments such as liquefied inorganic materials and plastic pieces are sent to the solid-liquid separation process by the anaerobic liquefier slurry transfer pump 206, And the liquid material is sent to the liquid food garbage storage tank 204.

Here, one kind of the solid-liquid separation process is selected from a Trommel separator or a vibrating screen.

The anaerobic liquefying tank 200 is a steel structure provided with a heating jacket 202 on the outside and a thermal insulation material on the outside of the heating jacket 202 with a thermal insulating material 203, Or a horizontal structure may be used, or alternatively, a concrete structure may be used instead of a steel structure.

The anaerobic liquefying tank mixer 201 is provided with a rake at the bottom and a paddle type, a horse anchor type, a ribbon type, a helical type a ribbon type, a screw type or a stirring shaft and a rectangular plate blade in a stirring arm may be used. The rotation speed may be adjusted to 2 to 4 rpm by mixing ) do.

2. Acid Fermentation Process

When the food waste liquefied in the anaerobic liquefaction process is supplied to the acidic fermentation tank 207 by the liquid food waste transfer pump 205, the mixture is stirred in the acidic fermentor stirrer 208 and the acidic fermenter The acidic fermentation liquid which has undergone the acidic fermentation until the acid decay period (acidic decay phase) is sent to the methane fermentation tank 209, which is an alkaline fermentation stage.

Anaerobic fermentation of high concentration organic wastes such as food waste occurs in three stages: acidic fermentation (acidic fermentation), acid fermentation (acidification) and alkaline fermentation.

In the acidic fermentation stage, the carbohydrate contained in the organic waste solution is decomposed to become a low molecular organic acid. In this process, the pH drops to around 5 There is a strong corruption (rotten smell). For example, a reaction such as the following reaction formula (18) takes place in the case of glucose.

C ₆ H ₁₂ O ₆ - acid producing bacteria → 3CH ₃ COOH ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (18)

Ammonia, amine, and carboxylic acid are formed as the protein is decomposed in the acidic decay phase (acidic decay phase), and the neutralization and decomposition of the organic acid generated in the reaction occur, The pH increases to 6-6.5.

Protein → NH ₄ HCO ₃ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (19)

CH ₃ COOH + NH ₄ HCO ₃ → CH ₃ COONH ₄ + H ₂ O + CO ₂ ... ... ... ... ... ... ... ... ... ... ... (20)

3. Methane fermentation process

In the acid fermentation process, when the acidic fermentation broth is supplied to the methane fermentation tank 209, the methane gas (CH ₄ ) and the carbon dioxide gas (CO ₂ ) are decomposed by decomposing organic matters into CO ₂ and CH ₄ The sludge settled in the lower part of the methane fermentation tank 209 is sent to the methane fermentation sludge transfer pump 211 and part of the sludge is transferred to the anaerobic liquefying tank 200 for sterilization Is sent to the aerobic fermentation tank (104) of the composting process together with the methane fermentation liquid that overflows at the top of the methane fermentation tank (209).

The methane gas stored in the methane gas storage tank 212 is used as boiler fuel and the remaining gas is used as heating fuel.

Methane fermentation, an alkaline fermentation, is the final stage of anaerobic fermentation in which the lower organic acids are degraded to methane, carbon dioxide and NH ₄ ⁺ ions by methane-forming bacteria. At this stage, the BOD decreases and the pH rises to around 7.5.

CH ₃ COONH ₄ + HO - Methane bacteria → CH ₄ + NH ₄ HCO ₃ ... ... ... ... ... ... ... ... ... ... ... ... (21)

CH ₃ COOH - Methane bacteria → CH ₄ + CO ₂ ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (22)

Methane bacteria are classified into anaerobic bacteria (anaerobic bacteria), thermophilic bacteria which act actively in temperature range of 30 ~ 36 ℃ and methophilic bacteria which act actively in temperature range of 50 ~ 60 ℃. , And the BOD of the anaerobic fermentation effluent from the methane fermentation bacteria is significantly reduced even though the BOD of the fermented anaerobic fermentation effluent is considerably low. Therefore, it is sent to the aerobic fermentation tank 104 of the composting process because the concentration of the residual organic matter is high. (May be sent to the aerobic biologic treatment process.)

The operation conditions and the design conditions of the anaerobic fermentation process in the present invention are as follows.

(1) The form of the acidic fermentation tank 207 and the methane fermentation tank 209

The acidic fermentation tank 207 and the methane fermentation tank 209 are both circular and have an inside diameter D of 25 m or less. The side wall depth (H) is 1/2 of the inner diameter (H = D / 2) and the slope of the bottom surface is in the range of 20/100 to 30/100.

(2) Operation temperature and capacity of the acid fermenter (207) and the methane fermenter (209)

The anaerobic fermenter is supplied with energy from the boiler in the liquefying tank 200 of the anaerobic fermentation tank and is operated in the range of 50 to 60 ° C. while the organic matter load (organic matter load) is in the range of 5 to 6 kg / 209). Generally, the fermentation time (T) is 20 to 30 days, and the volume of the tank (Volume, Vm3) is [(amount of high concentration wastewater (m3) + amount of anaerobic fermentation liquid (m3) / 2]. The volume ratio of the acidic fermentation tank 207 to the methane fermentation tank 209 is 1: 1 to 2: 1.

(3) The stirring speed of the acid fermenter stirrer 208

The acid fermenter stirrer 208 of the acidic fermentation tank 207 is a propeller type and the ratio Q / V of the stirring capacity Q to the stirring speed V is in the range of 0.5 to 2.

(4) The rotational speed of the methane fermentation lake 210

The rotating speed of the methane fermentation tank rake 210 of the methane fermentation tank 209 is 0.01 to 0.05 rpm while the sludge precipitated at the bottom is collected at the central cone portion so that the precipitated sludge is easily discharged .

(5) The methane gas storage tank 212 has a spherical shape and stores the methane gas produced as a water-retaining type in the water of the spherical methane gas storage tank seal pit 213, Is 10 to 12 hours.

Ⅴ. Alcohol fermentation step

Conventionally, alcohol fermentation of carbohydrates can be carried out by a method in which a carbohydrate is hydrolyzed with koji fungus or malted sprouts of koji, oxalic acid, hydrochloric acid or sulfuric acid, amylase enzyme , And the fermentation was carried out by Saccharomyces sp. Yeast or Zymomonas mobilis anaerobic bacteria. However, the above conventional saccharification method is costly, and therefore, There is a lot of problems.

In the present invention, the inventors of the present invention have carefully examined food garbage. As a result, it has been found that a substantial portion of carbohydrates are glycosylated or glycosylation is proceeding in the food garbage, while microorganisms that secrete amylase are released from the food garbage. Therefore, in the present invention, microorganism strains that produce amylase are added to the food garbage where saccharification is proceeding, if necessary, and ethanol is added in accordance with environmental conditions such as pH and temperature with good fermentation efficiency in the fermentation process of alcohol. Provides a method of production.

1. Saccharification process

The dehydrated food waste, which is a dehydrated cake in the primary dehydration process, is introduced into the saccharification tank 300 through the dehydrated cake of the primary dehydration process, wherein the dehydrated cake contains a large amount of starch hydrolysates such as noodles, bread, potatoes, sweet potatoes, , A heat source is supplied from the boiler to the heating jacket 302 provided outside the saccharification tank 300 while stirring the sugar mixer 301 at a stirring speed in the range of 2 to 4 rpm, The saccharified liquid is sent to the saccharified liquid storage tank 304 and then sent to the alcohol fermentation tank 307 by the saccharified liquid transfer pump 305. [

In the saccharification tank 300, the temperature is adjusted to a temperature at which the optimum temperature of alcohol fermentation is maintained at 25 to 30 DEG C in the alcohol fermentation tank 307, and the saccharified liquid is sent to the alcohol fermentation tank 307. [

It is not necessary to supply the heat source to the heating jacket 302 from the boiler in the case where the temperature of the food garbage is higher than 20 ° C in the summer and it is not necessary to supply the heat source from the boiler to the electric heater ) May be installed and heated with electric energy.

In the case of reactivation after commissioning or idle (suspended), 100 parts by weight of dehydrated food waste flowing into the sugar tank 300 is added to 100 parts by weight of Bacillus subtilis, Bacillus natto (Bacillus subtilis), which produces amylase enzyme natto, Bacillus licheniformis, Bacillus macerans, Bacillus megaterium, Bacillus amyloliquefaciens, Bacillus cereus, Bacillus amyloliquefaciens, Such as Bacillus circulans, Bacillus acidocaldarius, Bacillus stearothermophilus, Geobacillus stearothermophilus, Geobacillus thermodinitricipacin, Geobacillus sp., Such as Geobacillus thermodenitrificans, Lacto bacillus amyloborus, bacillus amylovorus, Lactobacillus cellobiosus, Lactobacillus manihotivorans, bacteria such as Pseudomonas stutzeri, Klebsiella aerogenes, and the like. Actinomycetes such as Streptomyces griseus, Aspergillus oryzae, Aspergillus niger, Aspergillus awamori, Aspergillus oryzae, Aspergillus oryzae, Aspergillus niger, Aspergillus awamori, 0.08 to 0.1 wt. ≪ RTI ID = 0.0 > g / ml < / RTI > of a strain cultivated with at least one filamentous fungus such as Aspergillus flavus, Aspergillus kawachii, Aspergillus sclerotiorum It is preferable that the part is fed to the saccharification tank 300 for seeding.

When the temperature of the food waste flowing in the winter is low and the microbial activity is not smooth and the glycation is not good, 0.01 to 0.06 part by weight of amylase enzymatic agent sold on the market per 100 parts by weight of the food waste flowing into the saccharification tank 300 May be supplied. (If the temperature of the incoming food waste exceeds 20 ℃, it is not necessary to supply the amylase enzyme.)

In the saccharification tank 300, the non-liquefied material such as sand, soil, and glass fragments, which is not liquefied and the liquefied material such as plastic pieces, is sent to the solid-liquid separation process by the anaerobic glycation slurry transfer pump 306 to discard the solid material, The substance is sent to the glycation solution reservoir 304.

Here, one kind of the solid-liquid separation process is selected from a Trommel separator or a vibrating screen.

The sugar tank 300 is a steel structure provided with a heating jacket 302 on the outside and a heating structure 303 on the outside of the heating jacket 302. The sugar tank 300 may be vertical as shown in FIG. It may be a horizontal structure or a concrete structure instead of a steel structure.

The saccharification mixer 301 is provided with a rake at the bottom and a paddle type, a horse anchor type, a ribbon type, a helical ribbon type a screw type or a stirring shaft and a rectangular plate blade is provided on a stirring arm and the rotation speed is 2 to 4 rpm.

2. Alcohol fermentation process

When the saccharified liquid is fed to the alcohol fermentation tank 307, saccharomyces cerevisiae, an alcohol fermenting yeast, is injected into the alcohol fermentation tank stirrer 308, and alcohol fermentation is carried out in an anaerobic state When the alcohol fermentation liquid containing ethanol is produced, it is sent to the distillation tower 310 by the alcohol fermentation liquid transfer pump 309.

In the alcohol fermentation process, the temperature is in the range of 25 to 30 ° C and the pH is in the range of 4.5 to 5.5. Since the alcohol production efficiency is excellent, it is preferable to supply the saccharified liquid in consideration of this.

In alcohol fermentation, alcohol is produced by the microorganism (Saccharomyces spp., Zymomonas mobilis) decomposing the saccharide into alcohol and carbon dioxide as in the reaction formula (23) in an oxygen-free anaerobic state.

C ₆ H ₁₂ O ₆ ? 2CH ₃ CH ₂ OH + 2CO ₂ + Reaction heat ... ... ... ... ... ... ... ... ... ... ... (23)

The alcohol fermentation tank 307 is a ferrous structure tank which is thermally treated with a heat insulating material 303 on the outside and the alcohol fermentation tank stirrer 308 is a pitched paddle type stirrer and the stirring speed is 2 to 4 rpm do.

3. Distillation Process

In the alcohol fermentation process, the alcohol fermentation liquid is supplied to the middle stage of the distillation tower 310 having the packing or tray 311 at the upper and lower ends thereof. The alcohol fermentation waste liquid at the lower part of the distillation tower 310 is supplied to the alcohol fermentation waste liquid transfer pump 312 The ethanol component contained in the alcohol fermentation broth is evaporated and passed through the packing or the tray 311 to the distillation tower 313, 310), the ethanol vapor and some water vapor of 62-63 deg. C escape.

The vapor of the ethanol component that has escaped to the upper part of the distillation tower 310 is sent to the condenser 314 and the cooling water is supplied to cool the solution to 20 to 40 ° C. The ethanol and a part of the water are liquefied and sent to the distillation accumulator 315 .

The ethanol-containing distillate sent to the distillate accumulator 315 is refluxed to the upper part of the distillation column 310 by the distillate feed pump 316 while the distillate containing the remaining ethanol is removed Process.

The alcohol fermentation waste liquid discharged from the lower part of the distillation tower 310 is sent to the acid fermentation tank 207 of the methane fermentation process or to the aerobic fermentation tank 104 of the composting process.

When the capacity of the alcoholic fermentation broth is small, a known simple distillation method may be used instead of the continuous distillation method described above.

The packing 311 to be filled in the distillation tower 310 may be a Raschig ring, a Pall ring, a Raflux ring, a Lessing ring, a Cross partition ring, , A saddle type, or a ball type, is used as the filling material 311.

4. Moisture removal process

At a normal pressure, the boiling point of ethanol (CH ₃ CH ₂ OH) is 78.37 ° C. and the boiling point of water is 100 ° C., but it exists as an azeotropic mixture in the composition of 95.63% ethanol-water 4.37% -Ethanol azeotropic mixture has a boiling point of 78.15 DEG C, and it is impossible to separate the water-ethanol at an atmospheric pressure to an ethanol concentration of 96% or more by the above distillation method only.

Therefore, the distillate of the distillation accumulator 315 is subjected to an azeotropic distillation method in which an azeotropic agent such as benzene, cyclohexane, or diethyl ether is introduced (Solvent extraction distillation method), membrane separation method (membrane separation method), synthesis method by hydration reaction of ethylene (synthesis method), vapor phase adsorption method (azeotropic distillation method), solvent extraction distillation method One way is to remove water to produce ethanol with 99% or higher purity.

VI. Feeding stage

Conventionally, for the purpose of feedstuffs for food waste, pre-treated food waste, such as foreign matter removal and crushing treatment, was fermented in a liquid state and then fed to livestock such as pigs, chickens and ducks as liquid feeds. However, In order to compensate for these problems, dry food production methods have been tried. However, since the food waste is high in water content due to high water content, I can not.

In order to solve the problems of the prior art, in order to reduce the water content, the food waste which has been pretreated such as the foreign matter removal and crushing treatment is dehydrated, and the dehydrated cake is subjected to high temperature fermentation using the fermentation microorganism, A method for producing feedstuffs such as pigs, chickens, ducks, and fishes by mixing the feedstuffs with the pathogenic microorganisms is described below with reference to FIG.

1. Fermentation Process

When the dehydrated cake having been dehydrated in the primary dehydration process is supplied to the feed process high temperature fermenter 400, the useful microorganism strains are injected and mixed with the high temperature fermenter mixer 401, The heat source is supplied from the boiler to the heating jacket 402 provided outside the boiler 400, and the fermentation is performed while the temperature is maintained in the range of 35 to 45 ° C., whereby pathogenic microorganisms, decaying bacteria and harmful microorganisms harmful to the livestock are killed and liquefied.

The fermentation liquid that has been liquefied in the high-temperature fermentor 400 is sent to the fermentation broth storage tank 404 and the solid material that is not liquefied in the slurry state such as sand, glass fragments, The liquid substance separated by the pump 406 is sent to the fermentation liquid reservoir 404, and the solid substance is discarded.

The solid-liquid separation step uses one of a Trommel separator or a vibrating screen.

The high-temperature fermenter 300 may have a jacketed outer jacket 402 and the outer surface of the warm jacket 402 is insulated by a thermal insulating material 403, as shown in FIG. 7, It may be a horizontal structure or a concrete structure instead of a steel structure.

The high temperature fermenter mixer 401 has a rake at the bottom and a paddle type, a horse anchor type, a ribbon type, a helical ribbon type a screw type or a stirring shaft and a rectangular plate blade is provided on a stirring arm and the rotation speed is 2 to 4 rpm.

Bacillus subtilis, Bacillus mycoides, Bacillus natto, and Bacillus natto are added to 100 parts by weight of the food waste to be introduced when the microbial bacteria are restarted after commissioning or idle Bacillus mycoides, Bacillus such as Bacillus stearothermophilus, Lactobacillus acidophilus, Lactobacillus bifidus, Lactobacillus bulgaricus, Bacillus strains such as Bacillus mycoides, Bacillus stearothermophilus, Lactobacillus acidophilus, Lactobacillus bifidus, Lactobacillus delbrueckii, Lactococcus lactis, Lactobacillus amylovorus, Lactobacillus casei, Lactobacillus plantarum and Lactobacillus spp.), Lactobacillus spp., Lactobacillus spp. The same Lactobacillus sp., Clostridium butyricum, Such as Pediococcus sp., Enterococcus sp., Leuconostoc sp., Pediococcus sp. Or Saccharomyces cerevisiae, and the like. 0.05 to 0.1 parts by weight of a microbial strain obtained by co-culturing one or more kinds of yeast strains is supplied. In normal operation, it is not necessary to continue infusing useful microbial strains.

2. Mixing Process

When the fermentation broth of the fermentation broth 404 is supplied to the mixer 407 by the fermentation broth 405, the broth 408 mixes the broth with the nutritionally balanced nutrients according to the type of livestock, A feed mix is delivered to the feed process by the feed mix conveying conveyor 409.

The mixer 407 may be a horizontal type as shown in FIG. 7, but may be a vertical type. The mixer mixer 407 has a paddle type and a screw ribbon type. The mixing speed is 2 to 4 rpm, and the mixing time is 30 to 40 minutes.

The feedstuffs used are those mixed appropriately in nutritional balance according to the type of livestock. When making feeds of ball type or pellet type, the water content is in the range of 40 to 43% And mix them.

3. Feeding process

When the feed mixture is fed in the mixing process, the feed mixture is sent to a dryer to dry the feed at a moisture content of less than 12% to prepare a dry feed, or it may be fed to a molding process to supply a binder to form a ball type or pellet type Pellet type) is sent to the dryer to dry the water content to 12% or less to make ball or pellet type feed.

The dryer may be one of a dryer such as a hearth dryer, a drum dryer, a tower drier, a band dryer or a cabinet type dryer, The kind of the dryer in the present invention is not particularly limited.

In the case of forming a molded feed, a binder is prepared by mixing 100 parts by weight of feed mixture with pre-gelatinized starch such as corn, wheat, potatoes, methyl cellulose (MC), carboxy Natural gums such as carboxymethylcellulose (CMC), alginate, guar gum and tragacanth gum, carbopol, agar, pectin, Chitosan, Sodium polyacrylate, Poly methyl carbamide, Gelatin, Lignin sulfonate, Agar pragmatics or Carrageenan, among others. And 1 to 3 parts by weight of at least one kind is added.

VII. Deodorization step

Food waste is decomposed and deteriorated by anaerobic microorganisms (anaerobic microorganisms) and liquid anaerobic (common anaerobic), and ammonia (NH ₃ ), trimethylamine, dimethylamine ), Volatile nitrogen compounds such as indole and skatol, volatile organic acids such as acetic acid, propionic acid, butyric acid and valeric acid, hydrogen sulfide (H ₂ S), volatile sulfur compounds such as mercaptans, dimethyl sulfide, and methyl disulfide, and volatile odor substances such as acetaldehyde.

However, in the soil in the forests of the mountains, organic matter such as fallen leaves, animal feces and carcasses are deposited, but odor is hardly generated, and the mountain valley water discharged from here is clean water.

The inventors of the present invention have studied the fact that odor is not generated even when organic matter such as leaves, animal feces and carcasses are deposited in the soil in the above-mentioned forests. As a result, it has been found that the use of polyphenolic compounds as metabolites As microorganisms such as Bacillus mycoides, Bacillus luteus and actinomycetes are dominant species, these microorganisms excrete polyphenol compounds as metabolites .

Organic matter + air (O ₂ ) - polyphenol-producing microbe → polyphenol compound (microbial metabolite) + CO ₂ + H ₂ O ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (24)

The polyphenol compound is oxidized to quinone compounds by catalytic reaction of oxidizing enzymes such as polyphenol oxidase in the air.

Polyphenol compound + air (O ₂ ) - oxidizing enzyme (Oxidase) → quinone compound + H ₂ O ₂ ... (25)

The quinone compound is subjected to a polycondensation reaction with the volatile odorous substance to become a corrosive precursor substance (humic substance precursor substance), which is a non-volatile high molecular substance, and further a corrosive substance (humic substance) .

Quinone compounds + volatile odor substances (NH ₃ , H ₂ S, mercaptans, volatile amines, indoles, scatol) - condensation reaction → corrosion precursors (nonvolatile substances) → ... → Corrosive substances ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... ... (26)

The microorganisms that excrete the polyphenol compound as a metabolite are characterized by having many mineral components in the cells. They live on ingesting sufficient mineral components from the surface layer of the soil, the tombstone, and the surface of the rock, and are resistant to ultraviolet rays, Microorganisms, perishable and degrading microorganisms. In other words, the microorganisms that excrete polyphenol compounds as metabolic products inhibit the growth of pathogenic microorganisms, perishable and degrading microorganisms by exerting antibiotics against mutually antagonistic microorganisms while performing active metabolism when sufficient mineral components are supplied .

Therefore, in the present invention, a bioreactor 506 in which a packing 507 for easily eluting a mineral component is embedded is provided in a microorganism culture tank 504 for discharging a polyphenol compound, and aerobic biologic treatment A method for collecting and deodorizing odorous substances generated in each of the above processes by supplying a microbial culture liquid for discharging polyphenol compounds by receiving wastewater and excess sludge from the process will be described in detail with reference to FIG.

1. Biological deodorization process

The biological deodorization process of the present invention is characterized in that a rhyolite or Dacite pumice and rhyolite or a large-site volcanic ash soil and a marine plant which are easy to dissolve mineral components in water, A bioreactor 506 in which a packing 507 formed by pelletizing a coarse sediment formed together with sediment is placed in a microorganism culture tank 504 for discharging a polyphenol compound.

Raschig ring, Pall ring, Raflux ring, Lessing ring, Cross partition ring, Saddle type ring, and Saddle type ring are provided on the culture tank 504, ) Or a ball type is installed in a deodorizing tower 501 filled with two kinds of packing 502 of one type.

The wastewater from the aerobic biological treatment process water collecting tank 12 is poured into the culture tank 504 and the excess sludge discharged from the aerobic biological treatment process in the wastewater treatment stage is treated with a mixed liquor suspended solid (MLSS) concentration of 3,000 to 4,000 mg / And air is supplied from the blower 508 to the lower portion of the bioreactor 506 and the lower portion of the microorganism culture tank 504 to aeration so that the dissolved oxygen concentration is maintained in the range of 2 to 4 mg / Bacillus mycoides, Bacillus luteus, and the like, which receive minerals from pumice minerals and pellets filled in bioreactor 506 and excrete polyphenol compounds as metabolites, , Actinomycetes (Acinetobacter sp.) And Acinetobacter sp. Are the dominant microorganism cultures.

The microorganism culture liquid in the culture tank 504 is supplied to the lower end and upper end packing 502 built in the deodorization tower 501 by the deodorization tower circulation pump 505 and circulated, The volatile odor material and the microbial culture liquid are supplied to the bottom of the deodorization tower 501 through the odor absorbing pen 500. In this case, The volatile odor substance is converted into a corrosive substance (humic substance) through a non-volatile macromolecule substance (humic substance precursor) through a reaction similar to the reaction formula (26) with the quinone compound contained in the microorganism culture liquid, The gas from which the substance is removed and the odorous substance is removed is discharged to the atmosphere through the upper part of the deodorization tower 501 after the small droplet is removed from the large mist 503.

The capacity of the culture tank 504 for culturing a microorganism that excretes the polyphenol compound as a metabolite is 20-30 m 3 per 100 ton / day of food waste introduced into the feed tank, The reactor 506 is filled with 40 to 60 kg of rhyolite or large-site pumice, and 20 to 30 kg of pumice pellet.

The deodorization tower 501 is connected to the microbial culture liquid supplied from the deodorizing tower circulation pump 505 and the mass velocity G of the gas containing the odorous substance supplied from the odor substance intake fan 500 to the lower portion of the odor column 501 The mass flow rate L of the solution containing the surplus sludge and the wastewater in the aerobic biological treatment process is in the range of 0.2 to 0.6 and the area of the deodorization tower 501 is the same as the area of the packing 502, The flow rate of the gas is generally in the range of 0.15 to 0.3 m / sec, and the filling capacity of the filling material 502 is preferably in the range of 0.15 to 0.3 m / sec. It is safe to set the contact time between the upper and lower ends in the range of 2 to 3 seconds.

The amount of surplus sludge and wastewater supplied from the aerobic biological treatment process is supplied to the microorganism culture tank 504 so that the concentration of MLSS is maintained in the range of 3,000-4,000 mg / L, and the culture liquid accumulated in the culture tank 504 And sends it to the food waste collection tank by the controller (LIC).

When a high degree of deodorization treatment is desired, an adsorption method in which the gas discharged to the upper part of the deodorization tower 501 is adsorbed by an adsorbent such as activated carbon, diatomaceous earth or zeolite, an oxidation method using an oxidizing agent such as hydrogen peroxide, ozone, chloric acid, One or more deodorization methods may be added among the oxidation method or the combustion method.

The method of treating food wastes by the method of the present invention is characterized in that the method of treating food wastes by the method of the present invention is a method of treating food wastes by the use of lime, The wastewater, which is a dehydrated filtrate after conversion of liquid organic matter into insoluble organic matter in solid water, is low in pollution load and low in facility cost and operation ratio, and can be treated at high altitude. In the dehydrated cake, The dehydrated cake is concentrated by dehydration, and the concentration of the organic matter is high. Since the water content is low and the water content is small, the size of the facility is small in the case of methane fermentation or alcohol fermentation, Is inexpensive and widely used in the treatment of food waste. The.

1: Reactor 2: Reactor stirrer
3: mixing tank 4: mixing tank mixing tank
5: Coagulation tank 6: Coagulation tank stirrer
7: Primary settling tank 8: Primary settling tank Rake
9: Settling sludge transfer pump 10: Neutralization tank
11: neutralization tank stirrer 12: water collecting tank
13: Constant voltage generating device 13a: Transformer
13b: Voltage regulator 13c: Primary coil (Coil)
13d: iron core 13e: secondary coil
13f: output line 13g: insulation processing terminal
20h: Earth 14: Wire mesh electrode
15: stainless steel plate (conductor) 16: aeration tank feed pump
17: magnetic charger 18a primary aeration tank
18b: Secondary aeration tank 19a: Second settling tank
19b: Third settling tank 20a: Second settling tank Lake
20b: tertiary settling tank lake 21a: primary return pump
21b: Secondary return pump 22a: Primary microorganism activating tank
22b: secondary microorganism activating tank 23a: primary bioreactor
23b: secondary bioreactor 24: packing
25: Final treatment tank 26: Blower
100: aerobic liquefier 101: aerobic liquefier mixer
102: Heat retainer 103: Oxygen dissolution apparatus
104: Liquid food garbage storage tank 105: Liquid food waste transfer pump
106: high temperature aerobic fermentation tank 107: high temperature aerobic fermenter stirrer
108: Heating jacket 109: High temperature aerobic fermentation liquid transfer pump
110: pressurized oxygen dissolving tank 111: saline reaction tank
112: saline reaction tank stirrer 113: saline reactant precipitation tank
114: Saline Reactor Sedimentation tank Rake
115: Saline Reactor Settler Settling Sludge Transfer Pump
116: High temperature aerobic fermentation broth without salt removed
117: Saline-free high-temperature aerobic fermentation liquid transfer pump
118: Medium temperature aerobic fermentation tank 119: Liquid transportation pump
120: mixer 121: mixer mixer
122: Conveyor conveying mixed cargo 123: Fermentation, aging treatment
124: Rotary mixer 125:
126: Compressor 127: Blower
200: Anaerobic liquefaction tank 201: Anaerobic liquefying tank mixer
202: Gaion jacket 203: Insulation material
204: Liquid food waste storage tank 205: Liquid food waste transfer pump
206: Anaerobic liquefier slurry transfer pump 207: Acid fermenter
208: Acid fermenter stirrer 209: Methane fermenter
210: Methane fermentation tank Lake 211: Methane fermentation sludge transfer pump
212: Methane gas storage tank 213: Methane gas storage tank seal pit
300: sugar tank 301: sugar tank stirrer
302: Heating jacket 303: Insulation material
304: Saccharification solution reservoir 305: Saccharification solution transfer pump
306: Saccharification slurry transfer pump 307: Alcohol fermentation tank
308: Alcohol fermenter stirrer 309: Alcohol fermenter feed pump
310: Distillation tower 311: Packing
312: Alcohol fermentation waste liquid transfer pump 313: Reboiler
314: Condenser 315: Distillation Accumulator
316: distillate transfer pump
400: high temperature fermenter 401: high temperature fermenter mixer
402: Heating jacket 403: Insulation material
404: fermentation broth storage tank 405: fermentation broth transfer pump
406: Fermentation liquid slurry transfer pump 407: Mixer
408: mixer mixer 409: feed conveyor conveyor
500: Odorant intake fan 501: Deodorization tower
502: Filler 503: Demister
504: Microorganism culture tank 505: Deodorization tower circulation pump
506: Bioreactor 507: packing
508: blower C ₁ , C ₂ : condenser
Ⓢ: Solenoid valve M: Motor (Motor)
LT: Level transmitter LS: Level control switch (Level switch)
LIC: Level indicating controller
FI: Flow indicator pHI: pH indicator (pH indicator)
pHT: pH Transmitter (pH transmitter)
pHIS: pH indicating control switch
DOI: Dissolved oxygen indicator
TI: Temperature indicator
TT: Temperature transmitter
TIC: Temperature indicating controller

Claims (3)

In food garbage disposal,
The dehydrated cake is sent to a composting process, a methane fermentation process, an alcohol fermentation process or a feed process, and the wastewater, which is a dehydrated filtrate, contains lime And the coal fly ash were supplied to the reacted reactant, and the pre-dry cellulosic powder was supplied to the mixed reactant, and the coagulant was supplied to the mixed reactant. The flocculated sludge was sent to the first settling tank and the dehydrated cake was sent to the composting process A pretreatment step of sending the neutralized wastewater to the aerobic biological treatment process in a pH range of 5.6 to 8.2,
The wastewater which has been neutralized in the pH range of 5.6 to 8.2 is supplied to the primary aeration tank by the aeration tank feed pump and the air supplied from the blower to the aeration tank, The treated solids were sent to a secondary settler and the precipitated solids were treated with a primary microorganism with a primary bioreactor packed with activated humic substance pellets and a mineral filler containing active minerals The surplus sludge that is discharged to the activated tank and the primary aeration tank is sent to the input tank and the deodorization process. The overflow water that flows over the secondary tank is treated as the first treated aerobic biological treatment tank, the sterilization / And a wastewater treatment step to be sent to the bio-aerobic biological treatment process. The method according to claim 1, wherein the wastewater neutralized in the pH range of 5.6 to 8.2 is installed in a collection tank of an aerobic biological treatment process and a high voltage of 3,000 to 5,000 volts is applied to a wire mesh electrode from a constant voltage generator A process of modifying the water by the constant voltage process or a process of modifying one kind or two kinds of water among the process of modifying the water by the magnetization process by providing the magnetizing device in the aeration tank feed pump discharge portion is an additional process Thereby treating the food waste. The method according to claim 1, wherein the food waste is treated using pre-dry fibrin powder instead of the moisture content adjusting agent in the composting step.

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