KR101250182B1 - Disposal system for organic waste - Google Patents

Abstract

PURPOSE: An organic waste treatment system is provided to double digestion efficiency for organic waste by implementing digestion of the organic waste with two phases, to increase the digestion efficiency by uniformly stirring the organic waste, and to increase methane collection efficiency by stirring the organic waste and removing scum. CONSTITUTION: An organic waste treatment system includes an acid generating tank(100); a methane generating tank(200) communicating with the acid generating tank; a solid-liquid separating tank(300) communicating with the methane generating tank; and a flash vaporizing apparatus(400). Organic waste flows into the acid generating tank and is hydrolyzed. A gas collecting part is formed at the methane generating tank. The flash vaporizing apparatus treats the leachate generated from the solid-liquid separating tank with concentrated water and condensed water. The acid generating tank and the methane generating tank respectively comprise a main body and multiple stirrers. The main body comprises side walls and a roof so that a storage space can be formed inside the main body. The stirrers are alternately installed on the side walls up and down. Strips are spirally laminated, and are folded with one another so that the side wall can be assembled. A heating pipe is formed on the outer periphery of the side wall, and hot water flows inside the heating pipe.

Description

Organic Waste Disposal System {DISPOSAL SYSTEM FOR ORGANIC WASTE}

The present invention utilizes the desorption liquid after the digestion function usefully, configures the digestion of organic waste in two phases to double the digestion efficiency of organic waste, and to increase the extinguishing efficiency by allowing uniform agitation to the digester, and simultaneously with stirring The present invention relates to an organic waste treatment system that can increase methane collection efficiency by removing scum.

In general, organic waste such as sewage and domestic sewage, including livestock manure, contains a large amount of organic substances, and microorganisms that receive nutrition from such organic substances are multiplying and multiplying. Sludge is agglomeration, which is a mixture of solids and water, which stick together with a substance. These organic wastes are composed of high concentrations of organic matter, which if not discharged, will contaminate rivers and lakes. In particular, large amounts of nitrogen and phosphorus cause eutrophication in the water system, making it impossible to use not only drinking water but also agricultural water.

Anaerobic digestion as a technique for treating such organic waste refers to decomposition of organic matter into relatively stable organic matter or inert inorganic matter by the action of microorganisms when organic matter is put into a closed tank containing anaerobic microorganisms. In addition, the pathogens and their media are killed during this biological process. The sludge digestion process is divided into high temperature digestion (55 ℃) and medium temperature digestion (35 ℃) according to the digestion temperature. In the case of livestock manure, the medium temperature digestion method of 35 ℃ digestion temperature is adopted. When decomposing organic matter, anaerobic bacteria obtain energy by using oxygen in compounds such as carbon dioxide, nitrite, nitrate, and sulfate in water, and generate methane, hydrogen sulfide, and carbon dioxide as by-products.

As an anaerobic digestion technique, Korean Patent Registration No. 8,377,77 consists of a combination of a multistage anaerobic digester and a biogas collection means provided at the top of the multistage anaerobic digester, and the multistage anaerobic digester is disposed next to the first. Anaerobic digestion tank and the second anaerobic digestion tank, partitions provided between the first anaerobic digestion tank and the second anaerobic digestion tank, and biogas supply pipe for supplying biogas in the first anaerobic digestion tank and the second anaerobic digestion tank Although, the first anaerobic digestion tank and the second anaerobic digestion tank, the acid fermentation and methane fermentation of organic waste is sequentially presented, but as mentioned above, the treatment of sludge generated during the treatment of organic waste Is not easy, and the agitation of stored organic waste The problem is not to be made fire extinguishing efficiency with the generation of four areas is inhibited, and it is not digested in the present description of the process of the talriaek generated after action.

Republic of Korea Patent Registration No.

The present invention has been made to solve the above problems, the treatment of the desorption solution after the digestion, as well as to enhance the agitation by improving the agitation, the treatment of sludge is efficient, by removing the scum generated methane collection It is to provide an organic waste treatment system that can increase efficiency.

The organic waste treatment system of the present invention as a means for solving the above problems is an acid generating tank in which organic waste is introduced and hydrolysis is performed; A methane production tank formed with a gas collecting unit for generating methane in communication with the acid generating tank and collecting the generated methane; A solid-liquid separation tank in which solid-liquid separation is performed in communication with the methane production tank; And a reduced pressure evaporation apparatus for treating the desorption liquid generated from the solid-liquid separation tank with concentrated water and condensed water.

In addition, a joint generator is formed in the connection line between the acid production tank and the methane production tank, and the joint generator includes a pressurization unit having a smaller diameter of the tube, a cavity chamber having a larger diameter while communicating with one end of the pressurization unit, and the cavity. It is composed of one or more diaphragm formed in the chamber to be inclined gradient to face the pressurized portion to break the sludge from the organic waste flowing into the methane production tank from the acid production tank, the operation of the methane production tank by sterilizing microorganisms of the acid production tank To make it more efficient.

In addition, the acid production tank and the methane production tank is composed of a main body sealed with side walls and a roof to form a storage space therein, and a plurality of stirrers installed alternately from the side wall, the side wall spirals the strip In order to be assembled by folding, the strips are assembled by folding to form a sealed structure without a welded portion.

In addition, the outer periphery of the side wall it is reasonable that the heating tube is configured to allow the hot water to flow therein so that the anaerobic reaction is efficiently performed.

In addition, the side wall may be composed of a double wall, when the double wall is configured to fill the heat shield mortar between the inner wall and the outer wall, the heat shield mortar 50 to 150 parts by weight of porous minerals, bottom Ash 25 to 50 parts by weight, calcium carbonate 10 to 15 parts by weight, CSA-based expander 1 to 3 parts by weight, thickener 0.1 to 0.5 parts by weight, shrinkage reducing agent 0.01 to 0.05 parts by weight, water reducing agent 0.1 to 0.03 parts by weight, water 30 to It may be included to include 50 parts by weight.

In addition, the acid generating tank and the methane production tank, a floating port in which a motor is built, a body forming a collecting space in the lower part of the floating hole, a plurality of suction pipes formed radially to communicate in the transverse direction from the body, It is reasonable to further configure a floating stirrer which is configured to communicate with the body in the longitudinal direction and is composed of a discharge tube in which an impeller connected to the motor by a rotating shaft is embedded.

In addition, it is preferable that a plurality of cutter blades are formed at the outer circumference of the rotary shaft so that sludge and scum that are sucked are crushed.

In addition, the impeller is composed of an upper, lower impeller, the lower impeller to form a slope gradient in the downward direction, the upper impeller may be to increase the stirring efficiency by forming a slope gradient upward.

In addition, in the vacuum evaporation apparatus, it is preferable to acidify the desorption solution introduced before treating the desorption solution with concentrated water and condensate so that the pH is 5 or less.

As described above, the organic waste treatment system of the present invention can double the digestion efficiency of organic wastes by configuring the digestion of organic wastes in two phases, and after the digestion, the desorption liquid is subjected to solid-liquid separation and reduced pressure evaporation. There is an efficient advantage.

In addition, the organic waste treatment system of the present invention has the advantage that it is possible to prevent the degradation of durability due to corrosion of the welded portion by configuring the acid production tank and the methane production tank as a non-welding structure as the digestion tank.

In addition, the organic waste treatment system of the present invention increases the extinguishing efficiency by making uniform agitation, and has the advantage of increasing the methane collection efficiency by removing scum at the same time of stirring.

1 is a schematic diagram showing an organic waste treatment system of the present invention,
Figure 2 is a side cross-sectional view showing a methane production tank of one configuration in the organic waste treatment system of the present invention,
3 is a side cross-sectional view showing an embodiment of a side wall of the methane production tank shown in FIG.
Figure 4 is a side cross-sectional view showing a joint generating device of one configuration in the organic waste treatment system of the present invention,
Figure 5 is a side cross-sectional view showing a floating stirrer as one component in the organic waste treatment system of the present invention,
FIG. 6 is a schematic view showing an embodiment of an impeller in the floating stirrer shown in FIG. 5.

Hereinafter, the structure and operation of the present invention will be described in more detail with reference to the accompanying drawings. In describing the present invention, the term or word used in the present specification and claims is based on the principle that the inventor can appropriately define the concept of the term in order to best describe the invention of his or her own. It should be interpreted as meanings and concepts corresponding to the technical idea of

The organic waste treatment system of the present invention includes an acid generating tank 100 into which organic waste is introduced and hydrolysis is performed as shown in FIG. 1; A methane production tank 200 in communication with the acid production tank 100 to generate methane and a gas collecting unit for collecting the generated methane; A solid-liquid separation tank 300 in which solid-liquid separation is performed in communication with the methane production tank 200; And a reduced pressure evaporation apparatus 400 for treating the desorption liquid generated from the solid-liquid separation tank 300 with concentrated water and condensed water.

The acid production tank 100 and the methane production tank 200 constitute the two-phase digestion tank, the acid production tank 100 is organic waste is introduced through the inlet line (①) as shown in FIG. It is to be hydrolyzed by microorganisms such as fermentation bacteria that perform hydrolysis. Organic waste consists of proteins, carbohydrates, fats, and the like. Proteins are hydrolyzed by fermentation bacteria to amino acids, carbohydrates to sugars, and fats to fatty acids and alcohols. In this way, the hydrolysis is a protein, carbohydrates, fats are respectively broken down into amino acids, sugars, fatty acids and alcohols, the amino acids are partially broken down into acetic acid, ammonia nitrogen, hydrogen sulfide by fermentation bacteria, and some are hydrogen, carbon dioxide. Sugars and fatty acids are broken down into intermediates, propionic acid, butyric acid, etc., and then, some are decomposed into acetic acid, ammonia nitrogen, and hydrogen sulfide by acetic acid producing bacteria, and some are hydrogen and carbon dioxide. Alcohol is partially decomposed into acetic acid, ammonia nitrogen, and hydrogen sulfide by fermentation bacteria, and some are hydrogen and carbon dioxide. As described above, the process of decomposing amino acids, sugars, fatty acids, and alcohols into acetic acid, ammonia nitrogen, hydrogen sulfide, hydrogen, and carbon dioxide is performed in the acid production tank 100.

The acid production tank 100 is stored for a certain period of time while the digestion by hydrolysis occurs, the organic waste is hydrolyzed is introduced into the methane production tank 200 through the connection line (②).

In this process, the connection line (②) formed between the acid production tank 100 and the methane production tank 200 has a co-generating device 400 as shown in FIG. 4 to hydrolyze in the acid production tank 100. Decomposed sludge contained in the organic waste, and to sterilize the microorganisms involved in the hydrolysis to thereby double the digestion efficiency in the methane production tank (200).

As shown in FIG. 4, the cavity generating device 400 includes a pressurizing part 410 having a smaller diameter of the tube, a cavity chamber 420 having a larger diameter while communicating with one end of the pressurizing part 410, and the cavity. It is formed in the chamber 420 and consists of one or more diaphragm 430 is formed inclined gradient to face the pressing portion 410.

The pressurizing portion 410 is connected to the connection line (②) from the acid production tank 100, as shown in Figure 4 to allow the organic waste that is hydrolyzed from the acid production tank 100 is introduced, as shown in the figure Although it has not been, it is reasonable that the connection line (②) connected to the pressurizing unit 410 is configured to allow the hydrolyzed organic waste to flow into the pressurizing unit 410 at a high pressure. The pressurizing portion 410 is to reduce the speed of the fluid by gradually decreasing the diameter (area) in accordance with the direction of the fluid to increase the pressure of the fluid gradually, the pressurizing flow path 411 is narrowest diameter As it passes, the pressure doubles. When the pressurized fluid passes through the pressurizing part 410 and is discharged to the cavity chamber 420 communicating with the connection line (②) on the side of the methane production tank 200, a large pressure difference is generated. Therefore, cavitation occurs. Such a cavity is a gas-filled microbubble that gradually grows and finally collapses at different speeds according to fluid internal conditions. When the cavity collapses, high temperature and high pressure are generated to decompose sludge contained in the organic waste. In addition, the shock wave generated when the cavity collapses causes the microorganisms contained in the sludge to be killed. That is, by destroying and killing cell walls of microorganisms involved in hydrolysis, the digestion efficiency of the methane production tank 2 is doubled by blocking the introduction of the microorganisms mainly living in the acid production tank 100 into the methane production tank 200. To make it work.

In particular, in the cavity generating device 400, as shown in FIG. 4, an inclined gradient is formed in the cavity chamber 420 opposite to the pressure passage 411 of the pressure part 410 on the opposite side of the pressure part 410. One or more diaphragm 430 to be configured.

Based on the configuration of the diaphragm 430, the fluid passing through the pressure passage 411 forms a turbulent flow and strikes the diaphragm 430, and the vibration energy generated in the diaphragm 430 is generated when the cavity collapses. In addition to the shock wave of high temperature and high pressure, the sludge decomposition and microbial sterilization efficiency are doubled. The reason why the diaphragm 430 forms an inclined gradient is to cause the vibration energy generated from the diaphragm 430 formed at the mutually opposite positions to interfere with each other to cause a greater vibration energy.

The diaphragm 430 is not limited to the material, but it is reasonable to use the elastic material to facilitate the generation of vibration energy by the impact of the fluid discharged through the pressure passage 411.

As shown above, the hydrolysis is performed, and in addition, the organic waste in which the sludge is decomposed is introduced into the methane production tank 200.

In the methane production tank 200, acetic acid, ammonia nitrogen, and hydrogen sulfide are decomposed into methane and carbon dioxide by acetoplastic methane producing bacteria, and hydrogen and carbon dioxide are decomposed into methane and carbon dioxide by reducing methane producing bacteria. In this way, acetic acid, ammonia nitrogen, hydrogen sulfide and hydrogen are decomposed to produce methane.

As shown in FIG. 2, the methane production tank 200 alternates between the main body 210 sealed by the side wall 211 and the roof 212 and the upper and lower alternating sides of the side wall 211 to form a storage space therein. Consists of a plurality of agitator 220 to be installed, the side wall 211 is laminated in a spiral spiral strip 10, as shown in Figure 3, between the strip 10 to be assembled by the folding 20 between the welding portion Without this, a closed structure is formed.

In more detail, the stirrer 220 is configured to be configured in plural on the side wall 211, but it is reasonable to be formed in alternating upper and lower sides as shown in FIG. 2. Here, the up and down alternating is configured such that the stirrer 220 forms a clearance in the circumferential direction on the side wall 211, and when the installation position is the stirrer 220 is configured at the upper end at one point of the side wall 211. In the next point, the stirrer 220 is configured at the lower end to be composed of up and down alternating. Stirring in the transverse direction by the agitator 220 of this installation structure is to prevent the four zones. And the stirring in the longitudinal direction is to be performed based on the configuration of the floating stirrer 240 to be described later in the present invention methane production tank 200 (acid production tank 100) in the transverse direction to prevent the four zones are generated And longitudinal stirring is to increase the extinguishing efficiency.

Since the stirrer 200 may use a known technique, a description of the configuration thereof is omitted.

The side wall 211 is formed by the assembly method by no welding using a strip-shaped strip 10, the welding portion is not generated at the joint portion between the strip 10 and at the same time the strip 10 ) Is made of a material such as stainless to improve the resistance to corrosion against the inner circumference of the side wall 211 in contact with the organic waste.

In more detail, as shown in FIG. 3, the strips 10 are bent up and down between the strips 10 to be folded 20 to be assembled, and overlapped between the strips 10 when the folding 20 is formed. By placing the water-tight pad 30 in the portion to form the folding 20 by bending at the same time to ensure the water-tightness, the spiral folding 20 is formed throughout the side wall 211 is formed side wall Structural stiffness is to be reinforced throughout the whole (211).

Meanwhile, as shown in FIG. 3, in forming the side wall 211, a double wall structure may be formed. In the case of the outer wall 50, the folding 20 may be folded between the strips 10 as described above. It may be configured to be assembled by, but Figure 3 shows a flat structure.

In addition, the outer periphery of the inner wall formed by the assembly of the strip 10 on the side wall 211 can be a heating tube 40 is configured, which is the appropriate extinguishing temperature of the organic waste in the body 210 In order to maintain the, it is reasonable that the heating tube 40 is also configured to surround the inner wall in a spiral. Although not shown in the figure, a hot water heater connected to the heating tube 40 will be further configured, and a reservoir for supplying a medium as hot water should be further configured, and the hot water heater is the methane production tank 200. It is preferable to use the methane generated from as a heat source to enable the regeneration of resources.

In addition, the side wall 211 may be configured as a double wall structure to fill the thermal insulation material between the inner wall and the outer wall, but in Figure 3 to fill the heat shield mortar 60 so as to simultaneously express the functions of the strength reinforcement and heat shield. An example is shown.

The heat shield mortar 60 is 50 to 150 parts by weight of porous minerals, 25 to 50 parts by weight of bottom ash, 10 to 15 parts by weight of calcium carbonate, 1 to 3 parts by weight of CSA-based expander, and 0.1 to 3 parts by weight of cement. 0.5 parts by weight, shrinkage reducing agent 0.01 to 0.05 parts by weight, reducing agent 0.1 to 0.03 parts by weight, characterized in that the formulation including 30 to 50 parts by weight of water.

Portland cement is used as the cement, and the amount of the compound is considered to secure strength and cracks due to hardening shrinkage.

In particular, the porous mineral may be blended as a fine aggregate may be used such as clusters. In this way, by mixing the porous minerals as fine aggregates, the heat shielding function is expressed based on the porosity, thereby preventing heat from leaking to the outside of the side wall 211 during warming. It can be prevented. In addition, the reason why the porous mineral is limited to 50 to 150 parts by weight is that the shrinkage in the curing process is sharply increased in the case of less than 50, and if it exceeds 150, material separation easily occurs, and induction of residual cracks is not easy. It is limited together.

In addition, in the present invention, the bottom ash is blended with cement and the binder, and the bottom ash is made of the material itself so as to be expressed by assisting the thermal minerals and the thermal insulation function based on the porosity. The bottom ash is limited to 25 to 50 parts by weight, the workability is lowered if it is less than 25, the secondary effect of the heat shielding function is insignificant, and the strength is lowered if it exceeds 50 parts by weight, limited as described above It is.

The calcium carbonate functions as a filler to fill the voids in the cement paste, and is limited to 10 to 15 parts by weight, which is less than 10 parts by weight, and the filling effect is less than 15 parts by weight. Rather it is to prevent the strength is reduced.

In addition, as shown in Figure 2, the methane production tank 200 is configured with a floating stirrer 240, the floating stirrer 240 is suspended in the organic waste stored in the organic waste stored in the top of the core centripetally By discharging to the bottom to be agitated in the longitudinal direction, especially in the case of the methane production tank 200 is to remove scum that is likely to form on the water surface by sucking and stirring the upper fluid of the stored organic waste. When scum is deposited on the water surface, the methane collection efficiency is lowered due to blocking or absorption of methane generated by the extinguishing action. In the present invention, the floating stirrer 240 is configured to remove scum at the same time of stirring. You can do it.

As shown in FIG. 5, the floating stirrer 240 includes a floating port 242 in which a motor 241 is embedded, a body 243 forming a collection space in a lower portion of the floating hole 242, and the body ( A plurality of suction pipes 244 radially formed so as to communicate in the transverse direction at 243, and the impeller 248 in the longitudinal communication with the body 243 and connected to the motor 241 by a rotating shaft 246 is embedded therein It consists of a discharge pipe 245.

Based on such a configuration, suction force is generated in the suction pipe 244 as the rotation shaft 246 and the impeller 248 interlocked with the motor 241 generate, and the surface fluid is provided through the plurality of radial suction pipes 244. As the scum is sucked and collected into the body 243, the fluid and scum collected in the body 243 are discharged downward through the discharge pipe 245, whereby stirring in the longitudinal direction is performed. Is decomposed by the impeller 248 to be discharged.

Meanwhile, in the present invention, a plurality of cutter blades 247 are formed on the rotating shaft 246 to decompose scum as well as solids in the sucked fluid by cutting to double the efficiency of stirring and scum removal.

In addition, as shown in FIG. 6, the impeller 448 forms a rotary vortex, and the lower impeller 448-1 forms an inclined gradient in a downward direction, thereby improving the linearity of the rotary vortex to generate the methane generating tank. Rotational vortex is spread to the lower end of the 200, the upper impeller 448-2 has a larger diameter than the lower impeller (448-1), to form a slope gradient in the upward direction wide rotational vortex The impeller 448 is agitated in a longitudinal direction by spreading out to an area, but the agitation efficiency is further increased by agitation in a wide area up to the lower end of the methane production tank 200.

Although the above-mentioned contents are illustrated as an example of the methane production tank 200 based on FIG. 2, the acid production tank 100 has the same configuration, and thus description thereof will be omitted.

After anaerobic digestion based on the digestion of the methane production tank 200 mentioned above, the desorption liquid flows to the solid-liquid separation tank 300 through the connection line ④, and the organic wastewater is fermented in the methane production tank 200. Methane gas generated as it is being raised to the upper body 200 to be collected in the gas collecting unit 230. The collected methane gas is discharged through the discharge line (③) for recycling purposes as shown in FIG. 1, and is recycled as a heat source in the heating of the acid generating tank 100 and the methane producing tank 200 as indicated by the dotted line. It may be, and can be recycled as the energy of the vacuum evaporation apparatus 400 to be described below.

The gas collecting unit 230 is located inside the roof 212 of the main body 200 and the fixing means for the main body 200 of the gas collecting unit 230 may use a known technique, and thus description thereof will be omitted. . When the methane gas generated by the fermentation of organic waste in the methane production tank 200 is collected in the gas collection unit 230, the appropriate amount is discharged to the outside through the discharge line (③), the discharged methane gas is As mentioned, it is to be used for the operation of the system.

More preferably, the gas collecting unit 230 includes a desulfurization apparatus 231 to reduce the concentration of sulfur compounds mixed into the collected methane gas through oxidation. The desulfurization apparatus 231 is to provide an oxidizing agent or oxygen to oxidize a sulfur compound by a known technique.

Digestion filtrate from the methane generating tank 200 mentioned above, that is, the desorption fluid flows to the solid-liquid separation tank 300 through the connection line (④), the solid-liquid separation tank 300 is discharged by separating the solids in the desorption liquid By discharging through the line (⑥) to form a dehydration cake using a separate dehydration device, and the like, the desorption liquid from which the solids are separated is led to the depressurization evaporator 400 through the connection line (⑤). The technology applied to the solid-liquid separation tank 300 may be a variety of techniques such as belt press, filter press, stream press, high-speed stream press, centrifugal force separator as a known technique.

Thus, the desorption liquid from which solid matter is separated from the solid-liquid separation tank 300 is introduced into the depressurization evaporator 400, and condensed water is discharged to the discharge line ⑦ based on the action of the depressurization evaporator 400, and is discharged. The condensed water is introduced into the associated water treatment, that is, sewage pipes, etc., and the concentrated water is discharged to another discharge line (⑧) so that the concentrated water is recycled to a high concentration liquid ratio together with the dehydration cake generated from the solid-liquid separation tank 300.

The depressurization evaporator 400 having such a function is not shown in the drawing to concentrate the desorption liquid by allowing water to evaporate from the desorption liquid under a reduced pressure, but is connected to a plurality of depressurization evaporators and the plurality of decompression evaporators, respectively. A heat exchanger or the like must be configured to perform the evaporation of the reduced pressure evaporator. Condensed water is discharged by condensing the final evaporated water produced while passing through the plurality of vacuum evaporators, and the produced water produced by condensation is discharged to the condensed water so that the associated water is treated. By using such a reduced pressure evaporator 400 it is easy to process a high concentration of nitrogen in the desorption liquid.

In addition, preferably, the depressurization evaporator 400 may be acidified (pH 5 or less) of the desorption liquid before the process of depressurizing and evaporating the desorption liquid to double the nitrogen treatment efficiency.

Applicant has been found that the acidification of the desorption liquid in the reduced pressure evaporator 400 through the following experimental example results in a more reasonable result in the nitrogen treatment efficiency.

The following experimental results are the results of the test using the depressurization evaporator 400 for the desorption solution, the sample amount was 1,000 ml, the pH of the sample was adjusted to pH 4 randomly adjusted to pH 7.5 Samples were carried out. The experimental conditions of this experimental example are as follows.

■ Sample volume (before concentration): 1000 ml

■ Temperature: 80 ℃

■ Pressure: 18.0kPa

■ Concentration Drainage: × 10

Analysis results of the desorption solution (stock solution), the concentrate, and the condensate to the reduced pressure evaporator 400 are shown in Table 1 below.

division Undiluted solution Concentrate (pH 7.5) Condensate pH7.5 pH4 TN (mg / l) 610 790 590 0.957 NH ₃ -N (mg / L) 580 340 570 0.759 TP (mg / l) 73 870 0 0.000

When the water quality was 10-fold concentrated in the desorption liquid, the nitrogen concentration in the condensate was high at pH 7.5, so the nitrogen treatment efficiency could not be obtained. However, the nitrogen concentration in the condensate was very low. there was.

In the case of the above-described experiment of the desorption liquid, the concentration was performed up to 250 times the maximum concentration drainage. In the case of the sample of 1,000 ml, 4 ml of the concentrate was generated, and 960 ml of the condensate was generated. In the case of the experiment example, the concentration was carried out to the maximum drainage, and when applied to the anaerobic digestion process, it is determined that the treatment of the desorption solution may be possible by applying about 50-100 drainage considering the efficiency according to the sample amount.

Those skilled in the art will appreciate that various changes and modifications can be made without departing from the spirit of the present invention. Therefore, the technical scope of the present invention should not be limited to the contents described in the detailed description of the specification, but should be defined by the claims.

100: acid production tank 200: methane production tank
300: solid-liquid separation tank 400: reduced pressure evaporator

Claims (9)

An acid generating tank into which organic waste is introduced and hydrolysis is performed;
A methane production tank formed with a gas collecting unit for generating methane in communication with the acid generating tank and collecting the generated methane;
A solid-liquid separation tank in which solid-liquid separation is performed in communication with the methane production tank;
Including; decompression evaporator for treating the desorption liquid generated from the solid-liquid separation tank with concentrated water and condensed water;
The acid production tank and the methane production tank,
It is composed of a main body sealed by the side wall and the roof so as to form a storage space therein, and a plurality of stirrers which are installed up and down alternately in the side wall, the side wall is stacked in a spiral spiral, assembled by folding between the strips Organic waste treatment system, characterized in that.
The method of claim 1,
A joint generator is formed in the connection line between the acid generator and the methane generator,
The cavity generating device includes a pressurizing portion that reduces the diameter of the tube, a cavity chamber that increases in diameter while communicating with one end of the pressurizing portion, and at least one diaphragm formed in the cavity chamber and having an inclined gradient to face the pressurizing portion. Organic waste treatment system, characterized in that configured.
delete The method of claim 1,
The outer periphery of the side wall is an organic waste treatment system, characterized in that the heating tube is configured to flow the hot water therein.
The method of claim 1,
The side wall is composed of a double wall to fill the heat shielding mortar between the inner wall and the outer wall, 50 to 150 parts by weight of porous minerals, 25 to 50 parts by weight bottom ash, 10 to calcium carbonate with respect to 100 parts by weight of the thermal barrier mortar 15 parts by weight, 1 to 3 parts by weight of CSA-based expander, 0.1 to 0.5 parts by weight of thickener, 0.01 to 0.05 parts by weight of shrinkage reducing agent, 0.1 to 0.03 parts by weight of reducing agent, 30 to 50 parts by weight of organic Waste disposal system.
The method of claim 1,
In the acid production tank and the methane production tank,
A floating ball with a built-in motor, a body forming a collecting space in the lower part of the floating ball, a plurality of suction pipes formed radially so as to communicate in the transverse direction from the body, and in communication with the body in the longitudinal direction and the rotating shaft to the motor Organic waste treatment system, characterized in that the floating stirrer is composed of a discharge pipe in which the impeller connected inwardly.
The method according to claim 6,
And a plurality of cutter blades formed on the outer circumference of the rotary shaft.
The method according to claim 6,
The impeller is composed of an upper, lower impeller, the lower impeller forms a slope gradient in the downward direction, the upper impeller organic waste treatment system, characterized in that the slope is formed upward.
delete

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