KR20150114154A - Treatment System of Food Waste Leachate Capable of Deodoring, Denitration and Highly Concentration with High Solubility - Google Patents

Abstract

The present invention provides a food waste desorption leachate treating system comprising: a heat solubilizing device for solubilizing sludge by applying heat to a food waste desorption leachate; a boiler for supplying heat needed for the heat solubilizing device; a heat exchanger for cooling treated water discharged from the heat solubilizing device; a pressure floating tank for floating and removing a coagulated material including oil of the treated water heat-solubilized in the heat solubilizing device; an anaerobic digestion tank for methane-fermenting the treated water discharged from the pressure floating tank; and a denitrifying tank for removing nitrogen from the treated water discharged from the anaerobic digestion tank.

Description

Description: TECHNICAL FIELD [0001] The present invention relates to a food waste disposal filtrate treatment system capable of deodorizing, denitrifying,

The present invention relates to a food waste rejection filtrate processing system capable of deodorization, denitrification and high concentration treatment with high availability efficiency, and more particularly, to a system and method for efficiently removing oil and solids in a food waste desorption filtrate, It minimizes the amount of sludge generation, significantly reduces operating cost and energy consumption, contributes to solving the energy problem in the winter season by recycling and energizing the waste, has high availability efficiency to reduce the secondary environmental pollution problem, The present invention relates to a system for removing waste matter from a garbage which can be denitrified and highly concentrated.

The desorption filtrate discharged from the food waste dehydration process is composed of water, suspended solid and oil. Since the oil is stably present in the water phase in an emulsion state and the suspended solid is dispersed as fine particles, it is difficult to separate the oil and the suspended solid from the desolvation solution by a conventional method.

To date, various methods for treating food waste have been known as follows.

First, it can be landfilled directly in the ground, but it is prohibited as a problem of odor and groundwater pollution.

Secondly, it can be sterilized by high temperature to be used as feed for animals. However, this method has bad odor, low nutritional value as feed, low demand, low fuel cost and high condensation water treatment efficiency in the metropolitan area.

Third, food waste is composted by mixing it with a sub-homogenizer. This method is not only notable in that the odor is not only bad but also it is difficult to compost due to salinity and oil content. Also, due to problems such as salinity scale of farmland, .

Fourth, solid-liquid separation is performed and the dehydrated sludge is incinerated and the desorption filtrate is introduced into the sewage treatment plant. This treatment method should also solve the odor problem, it should have an extension of the incinerator and the sewage treatment plant, re-examine the total phosphorus (TP) and total nitrogen (TN) treatment method of the sewage treatment plant, do.

Next, solid-liquid separation is performed, and the dehydrated sludge is composted, and the desalination filtrate is treated separately. In the composting of dehydrated sludge, salinity and oil are mostly discharged into desalination filtrate, which can solve the problem of salinization and processing compaction and the amount of dehydrated sludge is reduced to 20 ~ 40%. Therefore, It can reduce security and bad complaints. It is also very economical because it recycles waste. However, in the treatment of tale filtrate, it was possible to dispose of it by ocean dumping, but the prohibition of marine dumping was confirmed and it is an urgent task to dispose of it.

The total amount of solid (TS) concentration of 80,000 to 150,000 mg / ℓ, the CODcr concentration of 100,000 to 250,000 mg / ℓ, the BOD concentration of 50,000 to 100,000 mg / ℓ, the total nitrogen TN concentration of 2,000 ~ 4,000 mg / ℓ, salinity concentration of 8,000 ~ 10,000 mg / ℓ, total phosphorus concentration of 600 ~ 800 mg / ℓ and oil concentration of 0.5 ~ 15,000 mg / ℓ . In addition, acid fermentation takes place during the collection process and the pH is very low as 3.0 ~ 4.0. This is because the concentration is 500 to 2000 times higher than that of sewage, and if the concentration is lowered in the pretreatment process and neutralization is not performed, the treatment cost and site area become larger and the treatment efficiency becomes lower.

In addition, since the food waste disposal filtrate contains a high concentration of solid matter, it must be separated and dehydrated, but it does not react well with chemicals, and there are many sludges that are generated by coagulation.

The sludge generated in such a large quantity can not be landfilled because of the contamination of groundwater, and it is composted or transferred to the incinerator for incineration. However, this sludge has high salinity and water content, high concentrations of flora and fauna, many problems in composting and incineration, and chronic odors in the vicinity.

Therefore, it is urgently required to reduce the amount of generated sludge and the offensive odor in the processing of the food waste sludge filtrate in terms of economy and environmental protection.

SUMMARY OF THE INVENTION The present invention has been conceived to solve the problems of the prior art as described above. It is an object of the present invention to effectively remove oil and solids in a food waste rinse filtrate, minimize the amount of sludge generated while reducing the amount of chemical feed, And energy consumption, as well as to recycle and energy the wastes to help solve energy problems during the summer months, and also to provide a food and beverage which can be used for deodorization, denitrification and high concentration, And a waste disposal filtrate treatment system.

The technical problem of the present invention as described above is achieved by the following means.

(1) a trough filtrate reservoir for collecting the filtrate of the food garbage tallies; A solid-liquid separator for solid-liquid separation of the desorption filtrate supplied from the desulfurization solution storage tank; A neutralizer for neutralizing the treated water separated in the solid-liquid separator; A heat dissolving device for solubilizing the sludge by applying heat to the food waste desorption filtrate; A boiler for supplying heat required for the heat dissolving apparatus; A heat exchanger for cooling the treated water discharged from the thermal solubilizer; A pressurized floating tank for floating and removing flocculated matter including oil in the treated water subjected to heat-solubilization treatment in the thermal solubilizer; An anaerobic digester for methane fermentation of the treated water discharged from the pressurized floating tank; An denitrification tank for removing nitrogen from the treated water discharged from the anaerobic digestion tank; A dehumidifier for removing moisture from the gas discharged from the anaerobic digester; And a deodorizer having activated carbon for deodorizing the dehumidified gas from the dehumidifier,

The solid-liquid separator includes a first dewatering means for firstly dewatering sludge by introducing sludge containing raw water therein; Second dehydrating means for dehydrating the first dehydrated sludge in the first dehydrating means; And a sludge feeding part for feeding sludge that has been first dewatered by the first dewatering device to the second dewatering device,

Wherein the first dehydrating means comprises:

A body housing having a raw water space part in which raw water is moved, a sludge space part in which sludge contained in the raw water is moved, and a treatment water space part in which the sludge separated treatment water is moved,

A raw water inflow portion for supplying raw water to the raw water space portion of the body housing;

A rotary drum screen provided so as to close the open part of the process water hole and rotatably provided with a plurality of filter holes to allow the process water separated from the raw water to pass to the process space part;

A first dewatering unit rotatably provided at a predetermined distance from the outer surface of the rotary drum screen, for squeezing and rolling the sludge moved along the raw water in the direction of the rotary drum screen to firstly dehydrate the sludge;

A sludge discharge unit for discharging sludge separated from the sludge space of the body housing by moisture separated by the first dehydrating unit and the rotary drum screen; And

And a process water discharging portion for discharging process water separated from the raw water or sludge by the first dehydrating portion and the rotary drum screen and transferred to the process water space portion,

Wherein the second dehydrating means comprises:

And a second discharge port for discharging the sludge that has been secondly dewatered while being transported along the second dewatering space, and a second discharge port for discharging the second dewatered sludge A second dewatering body formed;

A transfer screw unit having a transfer screw and rotatably installed in the second dewatering body to transfer the first dewatered sludge introduced into the second inlet to the second outlet while second dewatering;

A second driving unit for rotating the conveying screw unit;

A second sludge discharge unit provided to open and close the second discharge port and opened by the transferred sludge when the second sludge is dewatered by the transfer screw unit to discharge the sludge; And

And a second process water discharge unit provided in the second dewatering body for discharging the second dewatered process water by the transfer screw unit,

Wherein the heat dissolving apparatus includes an inner tube, an outer tube, and a swirl flow guide portion,

The inner pipe has a treatment water inlet formed at one end thereof and a treatment water outlet formed at the other end thereof. The outer pipe has an inlet through which a heating medium supplied from the boiler is inserted into one end of the outer pipe, The heating medium introduced through the heating medium outlet formed at one side of the other end is discharged to the outside and circulated through the boiler,

The swirling flow guiding portion is formed by twisting the inner pipe. The swirling flow guiding portion is protruded spirally toward the inner pipe so that the contact area with the heat medium moving along the outer pipe increases, And the heat exchange rate is improved.

(2) In the above (1)

Further comprising a coagulation reaction tank for introducing an inorganic coagulant, caustic soda, and a polymer between the thermal solubilizer and the pressurized floating tank to coagulate the food waste.

According to the present invention as described above, denitrification and high concentration treatment can be performed in the treatment of the food garbage tear filtrate, thereby effectively removing oil and solids in the food garbage tear filtrate, minimizing the amount of sludge generated while reducing the amount of drug input, Not only does it significantly reduce energy consumption, it also recycles waste and reduces secondary environmental pollution problems.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a block diagram of a system for treating a food garbage tearing filtrate capable of high deodorization, denitrification, and high concentration treatment according to the present invention. FIG.
FIGS. 2A to 2C are schematic views of a solid-liquid separator according to the present invention,
3 is a configuration diagram of a heat dissolving apparatus according to an embodiment of the present invention.
4 is a configuration diagram of a flocculation tank according to an embodiment of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will now be described in detail with reference to the accompanying drawings.

FIG. 1 is a block diagram of a system for removing a garbage from a food waste, which has a high availability efficiency according to the present invention and is capable of deodorization, denitrification, and high-concentration treatment.

1, the desorption filtrate processing system according to the present invention includes a desulfurization filtrate storage tank 1, a solid-liquid separator 2, a crusher 3, a neutralization unit 4, a mixing unit 5, a heat exchanger A boiler 8, a flocculation reaction tank 9, a pressurized floating tank 10, a storage tank 11, an anaerobic digestion tank 12, and a denitrification tank 17.

The collected food waste is first separated into a solid fraction and a desorption filtrate, and then the desorption filtrate is transferred to the storage tank 1 and stored.

The desorption filtrate stored in the storage tank 1 is transferred to the solid-liquid separator 2 to separate solid components (fine contaminants) having a predetermined size, for example, φ = 1 mm or more.

The solid-liquid separator 2 comprises a first dewatering unit 100 for introducing a desorption filtrate (raw water) and performing primary dewatering as shown in FIGS. 2A to 2C, a secondary dewatering unit A second dewatering means 200 for dewatering the sludge, and a sludge transferring unit 300 for supplying the first dewatered sludge from the first dewatering means to the second dewatering means.

Preferably, the first dehydration means 100 includes a raw water space 112 in which raw water is moved, a sludge space 114 in which the sludge contained in the raw water is moved, A raw water inflow part 120 for supplying raw water to the raw water space of the body housing, and a water inlet part 120 for closing the open part of the treated water hole part, A rotary drum screen 130 for allowing a plurality of filter holes 130a to be formed and passed through the process water separated from the raw water to be transferred to the process water space, A first dewatering unit (140) rotatably provided to sludge moved along the raw water by squeezing and rolling the sludge in the direction of the rotating drum screen to first dewater sludge, a first dewatering unit A sludge discharge unit 150 for discharging sludge separated from the sludge space of the body housing by moisture separated from raw water or sludge by the first dewatering unit and the rotary drum screen, And a process water discharging portion 160 for discharging the treated water.

As shown in FIG. 2B, the rotary drum screen 130 includes a drum screen 131 having a plurality of filter holes formed along an outer circumferential surface thereof, a coupling block 132 provided on the rotational center axes at both ends of the drum screen, And the other end of which is rotatably installed in the body housing 110 in a state of being hermetically sealed. The rotation shaft 133 is rotatably supported by the rotation shaft 133, A coupling piece 134 for closing the coupling hole, and a fixing member 135 for fixing the coupling piece to one end of the rotary shaft.

The second dewatering unit 200 includes a second dewatering space 212 and a second inlet 214 for introducing the first dewatered sludge into the second dewatering space, A second dewatering body 210 having a second outlet 216 for discharging the second dewatered sludge while being conveyed along the dewatering space and a conveying screw 224 for rotating the second dewatering body 210, A transfer screw unit 220 for transferring the first dewatered sludge introduced into the second inlet to the second outlet while being second dewatered, a second drive unit 230 for rotating the transfer screw unit, A second sludge discharging part 240 provided to open and close the second sludge discharging port and opened by the sludge conveyed when the second sludge is dewatered by the conveying screw part to discharge the sludge, For discharging the second dehydrated treated water by the screw portion And a second treated water discharging part 250.

The transfer screw unit 220 includes a plurality of second dewatering holes 223 and a transfer screen 222 positioned at the second dewatering body. The transfer screw unit 220 is provided at both ends of the transfer screen, A transfer shaft (226) rotatably provided on the dewatering body, and a transfer screw (224) formed in a spiral shape along an inner circumference of the transfer screen located in the second dewatering space, wherein the transfer screw The gap between the one end of the second drainage space 212 in which the second inlet 214 is formed is gradually narrowed toward the other end of the second drainage space in which the second outlet 216 is formed, The dewatered sludge is secondarily dewatered as it is adhered to the other direction, and the dewatered solid is discharged through the second outlet (216).

The solid component separated in the solid-liquid separator 2 is sent to the pulverizer 3, pulverized to less than 1 mm, and then conveyed to the storage tank 1.

The crusher (3) is equipped with a propeller-shaped blade in the body which prevents scattering of the crushed contaminants, and the number of revolutions of the blade is adjusted to 1,200 to 3,600 rpm according to the kind of impurities.

The treated water separated from the solid-liquid separator 2 (hereinafter, the wastewater discharged through each of the constitution steps will be referred to as treated water) is conventionally treated with an acidic solution having a pH within the range of 3 to 5, To be neutralized.

The neutralizer 4 is equipped with a stirrer of 90 to 120 rpm in a reactor having a rectangular tube shape, and an inlet pump and a neutralizer reservoir for introducing the neutralizer are installed. Preferably, the pH of the treated water discharged from the neutralization unit 4 is adjusted to a range of 6 to 7, and the treatment efficiency of the desorbing effluent initially supplied within the above range is increased to 50%. To this end, a pH meter (not shown) for detecting and adjusting the amount of neutralizing agent may be mounted on the neutralization device 4.

The treated water discharged from the neutralizing device 4 flows into the mixing device 5 to induce complete mixing to increase the solubilization efficiency of the subsequent stage of the thermal solubilizer 7.

The mixing apparatus 5 is equipped with a stirrer of 90 to 120 rpm in a reactor in the form of a rectangular tube. In the present invention, the mixing device 5 may be omitted and the neutralization device 4 may be directly connected to the heat exchanger 6 as occasion demands.

The treated water discharged from the mixing device (5) flows into the heat exchanger (6). The heat exchanger (6) performs heat exchange in a noncontact manner between the high temperature treated water discharged from the heat dissolving apparatus (7) and the low temperature treated water flowing into the heat exchanger.

In the heat exchanger 6, a flow meter and a pressure gauge are provided in the inflow portion of the treated water to control the flow rate and pressure, and a pressure control pressure gauge and an automatic valve are installed in the discharge portion of the heat-exchanged cooled treated water .

The treated water preliminarily heated in the heat exchanger 6 can be effectively subjected to the thermal hydrolysis reaction even when a relatively small heat source is supplied from the boiler 8 to the heat dissolving apparatus 7.

 For this purpose, the boiler (8) is composed of a body, a burner, a circulating pump, a heating medium expansion tank, an oil shutoff automatic valve, a communication pipe, a reservoir for supplying heat and a control system. Preferably, the burner of the boiler 8 uses a combined burner capable of using biogas and propane gas produced by the system of the present invention. The heating medium supply temperature is 200 to 250 DEG C, and the automatic valve is operated according to the temperature of the heat dissolving apparatus, and the supply pressure is preferably 1 to 3 kg / cm < 2 >.

The heat dissolving apparatus 7 comprises an inner tube 71, an outer tube 72, and a swirling flow guide portion 73, as illustrated in Fig.

The inner pipe 71 has a treated water inlet 71a at one end and a treated water outlet 71b at the other end. In the inner pipe 71, the treated water is introduced through the treated water inlet 71a, the treated water is thermally hydrolyzed and discharged to the outside through the treated water outlet 71b, and the treated water And serves as a reaction space.

The outer tube 72 is formed with an inlet 72a through which the heating medium supplied from the boiler 8 is inserted at one end of the outer tube 72 and the heating medium is introduced into the inner tube 72 through the heating medium outlet 72b formed at the other end of the outer tube 72, Is discharged to the outside and circulated by the boiler (8).

Herein, the outer tube 72 serves to heat the inner tube 71 by the heating medium introduced into the inner tube 71 to heat the treated water flowing into the inner tube 71, thereby promoting the flow of the treated water and promoting thermal hydrolysis of the treated water do.

The swirling flow guiding portion 73 functions to swirl the process water while partitioning the internal space of the inner pipe 71 into a plurality of spaces, and guides the moving direction of the process water.

The swirling flow guiding portion 73 is formed by twisting the inner tube 71 and is spirally protruded toward the inner side of the inner tube 71.

As a result, the outer surface of the inner pipe 71 increases the contact area with the heating medium moved along the outer pipe 72, thereby improving the heat exchange rate with the treated water that is swirled along the inner pipe 71.

Due to the above structure, the efficiency of heat exchange between the treated water and the heating medium, that is, the heat transfer efficiency from the heating medium to the treated water, becomes very large, so that the stirring of the treated water can be smoothly performed without a separate stirring facility, It is possible to prevent precipitation or deposition of the catalyst and increase the reaction efficiency.

Preferably, the heat dissolving apparatus 7 performs the heat solubilization at a pressure of 18 to 22 kg / cm 2 and a temperature of 180 to 200 ° C. For this purpose, the temperature of the heating medium supplied from the boiler 8 is 200 to 250 ° C. It is good. Under the above-described conditions, the solubilization of the solids can be completely performed even with a relatively small heat source, without additionally adding a reaction catalyst, an oxidizing agent, or the like into the thermal solubilizer 7.

To this end, the thermal solubilizer 7 may further include a sensor for sensing flow rate, temperature and pressure, an automatic valve for controlling the pressure, and a control means for controlling them.

The treated water discharged from the thermal solubilizer 7 is supplied to the flocculation tank 9 through the heat exchanger 6. The flocculation tank 9 is preferably equipped with a stirring means (not shown) and a pH meter (not shown) for sensing and adjusting the amount of flocculant to assist the flocculation reaction.

The flocculation tank (9) is used for flocculating various particles including oil, fine solid particles and the like contained in the treated water. In this case, inorganic flocculant, caustic soda, and polymer are supplied through the flocculant inlet as needed. At this time, the amount of the flocculant can be detected and adjusted using a pH meter (not shown).

In the present invention, the flocculation reaction tank 9 is preferably a pipe reactor type as shown in FIG. 4, in which a pipe 90a such as a discharge port of a feed pump (not shown) at the front end is stacked in multiple stages, Space utilization can be increased.

At this time, the multi-stage pipes 90a are stacked and the upper and lower pipes are connected by an elbow 90b made up of both ends 90b ₁ and 90b ₂ of the upper and lower pipes. Then, the front end 91 is an inflow pump, And connects it to the floating tank (10). In this case, preferably, an inlet (not shown) is provided at the front part of the reactor so that the organic coagulant can be introduced. The length of the pipe reactor is preferably set so that the residence time is 25 to 60 seconds.

When a multi-stage pipe is used to implement the flocculation tank 9, a separate stirrer is not required, and facilities and operation costs are reduced. In general, the flocculant addition apparatus and the inorganic flocculant input device are required for the flocculation reaction. (9), due to the nature of the process, it is possible to exhibit a high solid-liquid separation efficiency in the pressurized floating tank (10) at the downstream stage without these devices.

In the present invention, in the flocculation reaction tank 9, the pressurized floating tank 10 (10) is provided at the rear end of the flocculation tank 9, ).

The pressurized floating tank 10 removes the remaining suspended solids, thereby eliminating the disturbing elements of the anaerobic digester 12 at the downstream stage and increasing the digestion efficiency. The pressurized floating tank 10 is provided with a rectangular square barrel and a scraper for scumming off the upper portion thereof to discharge the suspended solids to the rear end of the pressurized floating tank. A pressurizing pump of a high pressure is installed in the lower part of the rear end of the pressurized floating tank 10 to continuously circulate the treated water to the front end through a pipe reactor type distributing device and a high pressure air 3 kg / ㎠ or more) is injected using a compressor or the like to increase the floatation efficiency. In the embodiment of the present invention, the linear speed of the scraper is 1 to 3 m / min, the pressure of the pressurizing pump is 3 to 5 kg / cm 2, the circulating rate of the pressurizing pump is 50 to 100% The area load is preferably 4 to 5 m 3 / m 2 · hr.

The treated water discharged from the pressurized floating tank 10 is once stored in the storage tank 11 and is transferred to the anaerobic digestion tank 12 at the following stage.

In the anaerobic digestion tank (12), organic substances present in the treated water are removed using methane fermentation. In the anaerobic digestion tank 12, methane fermentation bacteria are cultivated, and organic matter in the treated water is decomposed by these bacteria, and the generated methane gas is discharged to the outside.

The anaerobic digestion tank 12 is equipped with a square column-shaped barrel, an inflow and distribution unit at the bottom, and a GSS unit for gas-liquid separation. At this time, the inflow water can be introduced using the lower distribution device, and the return pump can be installed to increase the activity of the anaerobic microorganism. The upper GSS unit installs square type gas-holder to prevent scattering of methane gas, and WAIR is installed to discharge treated water.

Preferably, the gas discharged from the anaerobic digestion tank 12 is completely removed through the dehumidifier 13, and the dehumidified gas is deodorized in the deodorizer 14 mounted on the column, Adsorbs and removes sulfur compounds and various volatile substances.

As described above, the moisture and odor-causing substances are removed and the remaining methane gas is stored in the gas reservoir 15 to self-procure the energy required in the process. The residual methane gas (about 50 to 60% The electricity is produced through the device 16 or utilized as a fuel gas.

The gas storage tank 15 stores the methane gas generated in the form of a dome, and makes it possible to use it according to the application purpose. The methane gas is temporarily stored in the gas storage tank 15, and is transported to the compression storage furnace by using the gas compressor to be used according to the purpose of utilization. At this time, a part of the gas may be used as fuel for the heat boiler (8) of the heat dissolving apparatus, and the surplus gas remaining may be supplied to the gas company by installing a generator to produce electricity or installing a purifier. Preferably, the dome-shaped and compressed-storage tank is installed in a size of HRT = 6 to 8 hours, and the generator and the methane gas purifier are installed inside and outside with a capacity of 1 to 2 hr.

The treated water discharged from the anaerobic digestion tank (12) is then transferred to the denitrification tank (17). In the denitrification tank 17, nitric acid or nitrous acid is reduced by known denitrifying bacteria to nitrogen gas and released to the atmosphere.

In describing the apparatus of the present invention as described above, a pump can be installed as many times as necessary in a necessary portion for transferring treated water between respective apparatuses, and such a configuration is obvious to those skilled in the art, and a detailed description thereof will be omitted.

As described above, when the system according to the present invention is used, the heat exchange efficiency is maximized, and the fine solids (impurities) and sludge contained in the desorbing filtrate of the food waste are not immersed in the heat dissolving apparatus constituting the system, Not only efficiently removes oil and solids in the finally discharged treatment water but also allows the organic substances in the treated water to be completely removed by anaerobic fermentation.

Hereinafter, the present invention will be described in more detail with reference to the following examples and comparative examples. It is to be understood, however, that the same is by way of illustration and example only and is not to be taken by way of limitation.

[Example 1]

As a result of treating the food waste using the system shown in FIG. 1 (see the operating conditions in Tables 1 to 2 below), oil and solid matter in the final 20 ton of treated water discharged from the initial desolvation filtrate Filtrate), as well as organic matter in the treated water was completely removed by methane gas by anaerobic fermentation up to 80% (Table 3).

Heat exchanger operating conditions Inlet temperature
(° C) Discharge temperature
(° C) Inlet pressure
(kg / cm2) Outlet pressure
(kg / cm2) Residence time
(min) Tally filtrate 3 to 20 120 ~ 132 22 21 30 to 40 Heat-solubilized water 180 ~ 200 45 to 55 20 19 40 to 60

The pressure change is caused by the pressure loss due to the passage length.

Heat-Solubilization Apparatus Operating Conditions Inlet temperature
(° C) Discharge temperature
(° C) Inlet pressure
(kg / cm2) Outlet pressure
(kg / cm2) Residence time
(min) Heat-solubilizing device 120 ~ 132 180 ~ 200 21 20 90-120

Processing result Oil Solids Organic matter Initial desorption filtrate 100 100 100 Final processed number 0 10 3

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. It can be understood that

1: Tally filtrate reservoir
2: Solid-liquid separator
3: crusher
4: Neutralizer
5: Mixing device
6: Heat exchanger
7: Thermolysis apparatus
8: Boiler
9: Flocculation tank
10: Pressurized floating tank
11: Storage tank
12: anaerobic digester
13: Dehumidifier
14: Deodorizer
15: Gas storage
16: Surplus gas utilization appliances
17: Denitrification tank
100: First dehydrating means
200: second dehydrating means
300: Send sludge

Claims (2)

A trough filtrate reservoir for collecting the filtrate of the food garbage tear; A solid-liquid separator for solid-liquid separation of the desorption filtrate supplied from the desulfurization solution storage tank; A neutralizer for neutralizing the treated water separated in the solid-liquid separator; A heat dissolving device for solubilizing the sludge by applying heat to the food waste desorption filtrate; A boiler for supplying heat required for the heat dissolving apparatus; A heat exchanger for cooling the treated water discharged from the thermal solubilizer; A pressurized floating tank for floating and removing flocculated matter including oil in the treated water subjected to heat-solubilization treatment in the thermal solubilizer; An anaerobic digester for methane fermentation of the treated water discharged from the pressurized floating tank; An denitrification tank for removing nitrogen from the treated water discharged from the anaerobic digestion tank; A dehumidifier for removing moisture from the gas discharged from the anaerobic digester; And a deodorizer having activated carbon for deodorizing the dehumidified gas from the dehumidifier,
The solid-liquid separator includes a first dewatering means for firstly dewatering sludge by introducing sludge containing raw water therein; Second dehydrating means for dehydrating the first dehydrated sludge in the first dehydrating means; And a sludge feeding part for feeding sludge that has been first dewatered by the first dewatering device to the second dewatering device,
Wherein the first dehydrating means comprises:
A body housing having a raw water space part in which raw water is moved, a sludge space part in which sludge contained in the raw water is moved, and a treatment water space part in which the sludge separated treatment water is moved,
A raw water inflow portion for supplying raw water to the raw water space portion of the body housing;
A rotary drum screen provided so as to close the open part of the process water hole and rotatably provided with a plurality of filter holes to allow the process water separated from the raw water to pass to the process space part;
A first dewatering unit rotatably provided at a predetermined distance from the outer surface of the rotary drum screen, for squeezing and rolling the sludge moved along the raw water in the direction of the rotary drum screen to firstly dehydrate the sludge;
A sludge discharge unit for discharging sludge separated from the sludge space of the body housing by moisture separated by the first dehydrating unit and the rotary drum screen; And
And a process water discharging portion for discharging process water separated from the raw water or sludge by the first dehydrating portion and the rotary drum screen and transferred to the process water space portion,
Wherein the second dehydrating means comprises:
And a second discharge port for discharging the sludge that has been secondly dewatered while being transported along the second dewatering space, and a second discharge port for discharging the second dewatered sludge A second dewatering body formed;
A transfer screw unit having a transfer screw and rotatably installed in the second dewatering body to transfer the first dewatered sludge introduced into the second inlet to the second outlet while second dewatering;
A second driving unit for rotating the conveying screw unit;
A second sludge discharge unit provided to open and close the second discharge port and opened by the transferred sludge when the second sludge is dewatered by the transfer screw unit to discharge the sludge; And
And a second process water discharge unit provided in the second dewatering body for discharging the second dewatered process water by the transfer screw unit,
Wherein the heat dissolving apparatus includes an inner tube, an outer tube, and a swirl flow guide portion,
The inner pipe has a treatment water inlet formed at one end thereof and a treatment water outlet formed at the other end thereof. The outer pipe has an inlet through which a heating medium supplied from the boiler is inserted into one end of the outer pipe, The heating medium introduced through the heating medium outlet formed at one side of the other end is discharged to the outside and circulated through the boiler,
The swirling flow guiding portion is formed by twisting the inner pipe. The swirling flow guiding portion is protruded spirally toward the inner pipe so that the contact area with the heat medium moving along the outer pipe increases, And the heat exchange rate is improved. The method according to claim 1,
Further comprising a coagulation reaction tank for introducing an inorganic coagulant, caustic soda, and a polymer between the thermal solubilizer and the pressurized floating tank to coagulate the food waste.

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