KR20230076562A - Reactor and anaerobic disgedtion device including the same - Google Patents

Abstract

A reactor and an anaerobic digestion apparatus including the same are disclosed. The disclosed reactor comprises: a cover part; a hollow inner wall that is arranged to be spaced apart from the cover part and is configured to allow fluid to flow upward in an inner space; a hollow intermediate wall that is coupled to the cover part to partially surround the hollow inner wall and is configured to allow fluid to flow downward in a space between the hollow inner wall and the hollow intermediate wall; a hollow outer wall that is coupled to the cover part to surround the hollow intermediate wall and is configured to allow solid-liquid separation to occur in a space between the hollow intermediate wall and the hollow outer wall so that liquid flows upward and solids flow downward; and a helical baffle that is disposed in the inner space of the hollow inner wall. The reactor according to one embodiment of the present invention is configured to enable high-efficiency agitation and smooth recirculation without an agitator, thereby significantly reducing operating costs.

Description

Reactor and anaerobic digestion device including the same {Reactor and anaerobic digestion device including the same}

A reactor and an anaerobic digestion device including the same are disclosed. More specifically, a reactor configured to enable high-efficiency agitation and smooth recycling without an agitator and an anaerobic digestion device including the same are disclosed.

Organic wastes such as livestock manure and food waste can seriously damage the environment due to decay and leachate, and must be collected by type and disposed of through a prescribed waste treatment process.

However, the simple disposal of organic waste requires the preparation of treatment facilities and the consumption of manpower, and the wasteful aspect is relatively stronger than the productive aspect.

Accordingly, methods and technologies for recycling organic waste are being developed. Representatively, biogas (or methane gas) is produced using organic waste, and biogas produced through organic waste is converted into energy. can be cited.

Organic waste is composed of carbon, hydrogen, and a small amount of inorganic substances (nitrogen, sulfur, and phosphorus: less than 0.1% of the total amount of inorganic substances), and when anaerobic microorganisms decompose, inorganic substances are discharged and accumulated in the reactor. Accumulated minerals must be removed. Anaerobic microorganisms take only a small amount of minerals and the rest accumulates, and the accumulated minerals act as toxic substances to anaerobic microorganisms and inhibit their activity.

In the circulating biogas production facility disclosed in Korean Patent Publication No. 10-2021-0113104, the reaction solution that has passed through the first reactor and the second reactor is supplied to the stripping column, where inorganic acids are concentrated through a distillation process, and only clean water is the top material. It is a system that is discharged to the primary reactor and supplied back to the primary reactor, eventually preventing the accumulation of minerals in the reactor. However, the circulating biogas production facility has a problem in that a considerable amount of circulation is required to prevent accumulation of inorganic substances. A high circulation amount means that the stripping column discharges a huge amount of clean water as overhead material, which not only causes a huge energy loss, but also makes the additional energy cost for condensing the water too large.

One embodiment of the present invention provides a reactor configured to enable high-efficiency agitation and smooth recirculation without an agitator.

Another embodiment of the present invention provides an anaerobic digestion device capable of improving the production efficiency of biogas.

One aspect of the present invention,

cover part;

a hollow inner wall disposed to be spaced apart from the cover and configured to allow fluid to flow upward in the internal space;

a hollow intermediate wall coupled to the cover part and configured to partially surround the hollow inner wall so that fluid flows downward in a space between the hollow inner wall and the hollow inner wall;

a hollow outer wall coupled to the cover part and configured to surround the hollow intermediate wall so that solid-liquid separation occurs in a space between the hollow intermediate wall and liquid flows upward and solid flows downward; and

A reactor including a helical baffle disposed in an inner space of the hollow inner wall is provided.

The hollow inner wall may have a lower end coupled to the hollow outer wall.

The hollow inner wall may include a plurality of first through holes formed along a circumference of a lower end thereof.

The height of the lower end of the hollow intermediate wall may be higher than that of the lower end of the hollow inner wall.

The hollow middle wall may include a plurality of second through holes formed along a circumference of a lower end thereof and a third through hole formed at an upper end thereof.

The hollow outer wall may be configured such that an upper portion extends to have a constant width along the longitudinal direction and a lower portion gradually narrows toward the center along the longitudinal direction.

The reactor may further include a plurality of first inclined baffles coupled to a narrowing portion of the hollow outer wall and a plurality of second inclined baffles coupled to the hollow inner wall so as to cross each other with the first inclined baffle. .

The reactor may further include an outlet pipe and a plurality of inlet pipes coupled to a lower end of the hollow outer wall in fluid communication.

The reactor may further include a plurality of other outflow pipes coupled to each other in fluid communication with each other at different heights of the middle portion of the hollow outer wall.

The reactor may further include another outlet pipe coupled to the cover part in fluid communication.

The reactor may not include an internal stirrer.

Another aspect of the present invention is

primary reactor;

a secondary reactor disposed after the primary reactor;

a stripping column disposed at the rear end of the secondary reactor; and

It provides an anaerobic digestion apparatus including a heat exchanger configured to heat-exchange the effluent of the secondary reactor and the effluent of the stripping column.

The primary reactor may be the above-described reactor.

The anaerobic digestion apparatus may be configured such that an effluent of the primary reactor is recycled to at least one of the primary reactor and the stripping column.

The anaerobic digestion apparatus may further include a pump for recirculating the effluent of the primary reactor to at least one of the primary reactor and the stripping column.

The secondary reactor may include an activated carbon layer.

The anaerobic digestion device may be configured such that the effluent of the second reactor is recycled to at least one of the first reactor and the second reactor via the heat exchanger.

The anaerobic digestion device may further include another pump for recirculating the effluent of the secondary reactor to at least one of the primary reactor and the secondary reactor via the heat exchanger.

The anaerobic digestion device may be configured such that the effluent of the secondary reactor is recycled to at least one of the primary reactor and the secondary reactor by bypassing the heat exchanger.

The anaerobic digestion device may be configured such that an effluent of the stripping column is recycled to at least one of the primary reactor and the stripping column via the heat exchanger.

The reactor according to one embodiment of the present invention is configured to enable high-efficiency agitation and smooth recirculation without an agitator, thereby significantly reducing operating costs.

In addition, the anaerobic digestion device according to one embodiment of the present invention has excellent removal efficiency of inorganic substances, and thus can achieve high biogas production efficiency with cost reduction.

1 is a longitudinal cross-sectional view of a reactor according to one embodiment of the present invention.
Figure 2 is a view for explaining the operating principle of the reactor of Figure 1.
FIG. 3 is an enlarged view of part “A” of the reactor of FIG. 1 .
4 is a cross-sectional view of the reactor of FIG. 1 taken along line “BB”.
FIG. 5 is an enlarged view of part “C” of the reactor of FIG. 1 .
6 is a schematic view of an anaerobic digestion apparatus according to an embodiment of the present invention.

Hereinafter, a reactor according to an embodiment of the present invention and an anaerobic digestion device including the same will be described in detail with reference to the drawings.

In the present specification, "upward" means the opposite direction of gravity, and "downward" means the direction of gravity.

Also, in this specification, “fluid” means a liquid, a gas, a mixture of a liquid and a solid, or a combination thereof.

In addition, in this specification, "hollow" refers to any hollow shape, for example, a cylindrical shape or a shape similar thereto.

1 is a longitudinal cross-sectional view of a reactor 100 according to an embodiment of the present invention, FIG. 2 is a view for explaining the operating principle of the reactor 100 of FIG. 1, and FIG. 3 is a reactor 100 of FIG. ) is an enlarged view of “A” part, FIG. 4 is a cross-sectional view of the reactor 100 of FIG. 1 by cutting the “BB” line, and FIG. It is a drawing showing an enlarged part.

1 and 2, the reactor 100 according to an embodiment of the present invention includes a cover part 101, a hollow inner wall 102, a hollow middle wall 103, a hollow outer wall 104, and It includes a helical baffle (105).

An outflow pipe EX3 may be coupled to the cover unit 101 in fluid communication.

The outlet pipe EX3 may be a gas outlet pipe.

An upper end of the hollow inner wall 102 may be disposed to be spaced apart from the cover part 101 . The hollow inner wall 102 may be configured to allow fluid to flow upward in its internal space. Specifically, the fluid may flow from a position lower than the lower end of the hollow inner wall 102 to a position higher than the upper end of the hollow inner wall 102 (see arrow in FIG. 2 ).

In addition, the hollow inner wall 102 may have a lower end coupled to the hollow outer wall 104 .

In addition, the hollow inner wall 102 may include a plurality of first through holes h1 formed along the circumference of its lower end. The inner space of the hollow inner wall 102 and the space between the hollow inner wall 102 and the hollow outer wall 104 communicate with each other through the first through hole h1, as shown in FIG. 2, A fluid may flow into the inner space of the hollow inner wall 102 from the space between the hollow inner wall 102 and the hollow outer wall 104 (refer to the arrow in FIG. 2 ).

The hollow middle wall 103 may have an upper end coupled to the cover part 101 . The hollow intermediate wall 103 is configured to partially surround the hollow inner wall 102, and may be configured to allow fluid to flow downward in a space between the hollow inner wall 102 and the hollow inner wall 102. Specifically, the fluid overflowing over the upper end of the hollow inner wall 102 may flow downward in the space between the hollow inner wall 102 and the hollow middle wall 103 (see arrow in FIG. 2 ).

In addition, the hollow middle wall 103 may be configured so that the height of the lower end thereof is higher than that of the lower end of the hollow inner wall 102 .

In addition, the hollow middle wall 103 may include a plurality of second through-holes h2 formed along the circumference of its lower end and a third through-hole h3 formed at its upper end. The space between the hollow inner wall 102 and the hollow middle wall 103 and the space between the hollow middle wall 103 and the hollow outer wall 104 communicate with each other through the second through hole h2, As shown in FIG. 2 , fluid may flow from the space between the hollow inner wall 102 and the hollow middle wall 103 to the space between the hollow middle wall 103 and the hollow outer wall 104. (see arrow in Fig. 2). In addition, after the gas flows from the space between the hollow intermediate wall 103 and the hollow outer wall 104 to the inner space of the hollow intermediate wall 103 through the third through hole h3, the outflow pipe EX3 It can be discharged to the outside of the reactor 100 through. For example, the gas discharged to the outside through the third through hole h3 and the outlet pipe EX3 may include biogas (methane).

The hollow outer wall 104 may have an upper end coupled to the cover part 101 . The hollow outer wall 104 is configured to surround the hollow intermediate wall 103, and solid-liquid separation occurs in the space between the hollow intermediate wall 103 so that the liquid flows upward and the solid flows downward. (see arrow in FIG. 2). Specifically, the fluid flowing downward in the space between the hollow inner wall 102 and the hollow middle wall 103 (ie, a mixture of liquid and solid) flows through the hollow middle wall 103 and the hollow outer wall 104. Solid-liquid separation occurs as it enters the interspace and flows upward. That is, the space between the hollow middle wall 103 and the hollow outer wall 104 may be designed to be wide enough to allow solid-liquid separation to occur in the space by lowering the flow rate of the upwardly flowing fluid. Specifically, in the space between the hollow middle wall 103 and the hollow outer wall 104, large solids such as sludge may be precipitated.

In addition, the hollow outer wall 104 may be configured so that the upper portion extends to have a constant width along the longitudinal direction and the lower portion gradually narrows toward the center along the longitudinal direction.

A helical baffle 105 may be disposed in the inner space of the hollow inner wall 102 . The helical baffle 105 serves to increase the degree of mixing between components contained in the fluid by forming a vortex in the fluid flowing into the reactor 100. Specifically, when a fluid is introduced into the reactor 100 at a predetermined pressure by a pump and rises upward, the fluid forms a vortex by the action of the helical baffle 105 and is well mixed even without an internal agitator. Thus, reactor 100 may not include an internal agitator.

Specifically, the helical baffle 105 may have a screw shape.

In addition, the reactor 100 may further include a screen fixedly installed on the helical baffle 105 and activated carbon filled in the screen. Accordingly, the contact area between the reaction liquid and the activated carbon is increased, and since the flow path of the reaction liquid is not clogged and microorganisms are not accumulated, the biogas production efficiency can be further improved.

In addition, the reactor 100 has a plurality of first inclined baffles 106-1 coupled to the narrowed portion of the hollow outer wall 104 and a hollow inner wall ( 102) may further include a plurality of second slanted baffles 106-2.

The first inclined baffle 106-1 and the second inclined baffle 106-2 form a vortex so that the fluid flows downward (ie, AR1 direction), but upward with a large pressure loss (ie, AR2 direction) The furnace serves to prevent fluid from flowing (see FIG. 5). For example, the inclination angle of the first inclined baffle 106-1 and the second inclined baffle 106-2 may be up to 30° based on the central axis extension line (ie, vertical line) of the hollow inner wall (FIG. 5). reference).

In addition, the reactor 100 may further include an outlet pipe EX4 and a plurality of inlet pipes EN1 and EN2 coupled to the lower end of the hollow outer wall 104 in fluid communication.

The outlet pipe EX4 may be mainly used as a discharge passage for foreign substances (ie, various foreign substances (soil, other impurities, etc.) that microorganisms cannot decompose).

Raw materials and/or condensed water from steam discharged from the stripping column described below may flow into the inflow pipe EN1.

An effluent of the reactor 100 and/or an effluent of a secondary reactor described later may flow into the inlet pipe EN2.

In addition, the reactor 100 may further include a plurality of other outlet pipes EX1 and EX2 coupled to each other in fluid communication with each other at different heights of the middle portion of the hollow outer wall 104 .

A very small amount of suspended solids along with water can be discharged through the outlet pipe EX1, and these substances may not affect the pump even if a pump (not shown) is connected to the outlet pipe EX1. .

A fluid that does not contain macro-solids can be discharged through the outflow pipe (EX2).

6 is a schematic view of an anaerobic digestion apparatus 10 according to an embodiment of the present invention.

Referring to FIG. 6 , an anaerobic digestion apparatus 10 according to an embodiment of the present invention includes a primary reactor 100, a secondary reactor 200, a heat exchanger 300 and a stripping column 400.

The primary reactor 100 performs an anaerobic fermentation of organic waste raw materials with microorganisms to hydrolyze them into lower organic acids and inorganic acids and to generate biogas.

The organic waste raw material introduced into the primary reactor 100 may include, but is not limited to, inorganic materials (nitrogen, sulfur, and phosphorus) of less than 0.1% by weight, for example.

The organic waste raw material may include food waste, animal carcasses, plants, manure, livestock manure, slaughterhouse waste (eg, livestock blood), or a combination thereof.

Specifically, the primary reactor 100 serves to generate biogas containing methane (CH ₄ ) and carbon dioxide (CO ₂ ) by reacting organic matter and microorganisms at a predetermined temperature for a predetermined time.

More specifically, when organic waste raw materials such as food waste or livestock manure are introduced through the inlet pipe provided therein, the primary reactor 100 performs anaerobic fermentation on the organic waste to hydrolyze the organic waste to produce low-grade organic waste. It can be converted into organic and inorganic acids or can produce biogas containing methane.

The lower organic acid may include acetic acid, popionic acid, butyric acid, or a combination thereof, and since these substances have a small molecular weight and are light and easily volatilize, volatile fatty acid (VFA) ) can be referred to as

The microorganism may include methane bacteria, hydrolytic bacteria, denitrifying bacteria, sulfur-reducing bacteria, symbiotic acetic acid producing bacteria, homoacetic acid producing bacteria, or a combination thereof.

Organic waste input as a raw material to the primary reactor 100 includes food waste, human waste and domestic wastewater discharged from residential facilities; manure and waste water from the barn; Or it may include a combination thereof, and any organic matter that does not kill microorganisms by being mixed with microorganisms is applicable.

In addition, a biogas collection unit may be installed at the upper end of the primary reactor 100 to collect biogas generated through the above-described process.

The primary reactor 100 may be the same as or similar to the reactor 100 described above with reference to FIGS. 1 to 5 .

In addition, the anaerobic digestion device 10 may be configured such that the effluent of the primary reactor 100 is recycled to the primary reactor 100. Specifically, the anaerobic digestion device 10 may further include a pump P1 for recirculating the effluent of the primary reactor 100 to the primary reactor 100 . In this way, by recycling the effluent of the primary reactor 100 to the primary reactor 100 by the pump P1, not only can mixing between the inflow materials occur smoothly in the primary reactor 100 without an internal stirrer, but also Inorganic substances can be smoothly accumulated in the primary reactor 100 .

In addition, the primary reactor 100 may be maintained at a temperature of 50 to 65 °C. The temperature of the primary reactor 100 is determined by the flow rate of the raw material supplied thereto through the pipe L1, the primary reactor 100 by the pump P1 through the pipe L2 of the effluent of the primary reactor 100 The flow rate recirculated to, the flow rate supplied to the secondary reactor 200 through the pipe (L3) of the effluent of the primary reactor (100), the flow rate of the effluent of the secondary reactor (200) through the pipes (L4, L41) After passing through the heat exchanger 300, the flow rate recirculated to the primary reactor 100 through the pipe L9 and the effluent of the secondary reactor 200 do not pass through the heat exchanger 300 and the pipes L4, L42, and L9 The flow rate recirculated to the primary reactor 100 through, the heat exchanger 300 through the pipe L6 among the effluents of the stripping column 400, and then to the primary reactor 100 through the pipe L61 It may be determined by the recycled flow rate and the flow rate of the effluent of the stripping column 400 that is recycled to the stripping column 400 through the pipe L62 after passing through the heat exchanger 300 through the pipe L6. Here, each flow rate may be controlled by pumps P1, P2, and P3 and control valves CV1 to CV5.

The secondary reactor 200 serves to generate biogas containing methane by decomposing lower organic acids (volatile fatty acids) that are not completely decomposed in the primary reactor 100 with anaerobic microorganisms, and has a fixed screen (not shown). City) may include an activated carbon layer filled in.

Specifically, in the second reactor 200, the lower organic acid that is not completely decomposed in the first reactor 100 is adsorbed on the activated carbon layer and then decomposed by microorganisms to generate methane gas.

More specifically, in the second reactor 200, since the lower organic acid introduced after being separated from the first reactor 100 becomes a nutrient for methane-producing microorganisms, biogas containing methane is produced, and the first reactor (100 ) Similarly, the biogas generated in the secondary reactor 200 may be separately collected in the biogas collection unit.

In addition, the anaerobic digestion device 10 may further include a gas power plant connected to the biogas collector to utilize the biogas collected in the biogas collector as a resource, and the gas power plant to generate power can

In addition, the flow rate of the effluent of the secondary reactor 200 may be determined by the flow rate of the top of the stripping column 400 (ie, the flow rate of the upper effluent). That is, when the top flow rate of the stripping column 400 increases, the flow rate of the effluent of the secondary reactor 200 also increases.

In addition, the anaerobic digestion device 10 may be configured such that the effluent of the secondary reactor 200 is recycled to the primary reactor 100 and/or the secondary reactor 200 via the heat exchanger 300. Specifically, the anaerobic digestion device 10 is another pump (P2) that recirculates the effluent of the first reactor 100 to the first reactor 100 and / or the second reactor 200 through the heat exchanger 300 may further include. Through such recycling, the concentration of inorganic substances in the first reactor 100 and/or the second reactor 200 may increase. In the first reactor 100 and the second reactor 200, inorganic substances exist as strong inorganic acids (nitric acid, sulfuric acid, phosphoric acid), and the like, and these inorganic acids are chemically very stable when the concentration is low. However, these inorganic acids become chemically unstable as the concentration increases. In particular, anaerobic digestion is a hydrogen-rich environment, and as the concentration of inorganic acids accumulates, the chemically unstable inorganic acids react with hydrogen to change into ammonia and/or hydrogen sulfide, resulting in chemical equilibrium can be achieved. Therefore, there is a maximum permissible concentration at which the inorganic acid does not change into ammonia or hydrogen sulfide, and it is preferable that the secondary reactor 200 is operated under conditions that do not exceed the maximum permissible concentration. It is preferable that the amount is also determined. For example, the maximum permissible concentration may be 1% by weight. That is, when the concentration of inorganic substances (ie, inorganic acid) in the secondary reactor 200 increases, a large amount of inorganic substances can be discharged even if the amount of the upper material of the stripping column 400 is small. For reference, ammonia and hydrogen sulfide can act toxic to microorganisms. However, the present invention is not limited thereto, and the maximum allowable concentration of the secondary reactor 200 may vary depending on circumstances. In addition, the maximum allowable concentration of the secondary reactor 200 may be determined by the size of the primary reactor 100, the size of the secondary reactor 200, and the circulation amount of the stripping column 400.

However, when the concentration of inorganic substances in the secondary reactor 200 is close to the maximum permissible concentration but increases to a level that does not exceed the maximum allowable concentration, the amount of inorganic substances discharged from the secondary reactor 200 to the stripping column 400 increases, Operation of the overhead materials of the stripping column 400 for removing inorganic substances may be reduced.

In addition, the anaerobic digestion device 10 may be configured so that the effluent of the secondary reactor 200 is recycled to the primary reactor 100 and / or the secondary reactor 200 by bypassing the heat exchanger 300 . This configuration may be such that the overhead material of the stripping column 400 is condensed and recycled to the primary reactor 100 and/or the stripping column 400 in a saturated water state.

In addition, the secondary reactor 100 may be maintained at a temperature of 30 to 35 °C. The temperature of the second reactor 200 is determined by the flow rate of the effluent of the first reactor 100 supplied thereto through the pipe L3 and the effluent of the second reactor 200 to the stripping column 400 through the pipe L5. The supplied flow rate, the flow rate of the effluent of the secondary reactor 200 that is recycled to the secondary reactor 200 through the pipe L8 after passing through the heat exchanger 300 through the pipes L4 and L41, and the secondary Among the effluents of the reactor 200, it may be determined by the flow rate recirculated to the secondary reactor 200 through the pipes L4, L42, and L8 without passing through the heat exchanger 300. Here, each flow rate may be adjusted by a pump P1 and control valves CV1 to CV5.

The heat exchanger 300 may be configured to exchange heat between the effluent of the secondary reactor 200 and the effluent of the stripping column 400 . That is, the heat exchanger 300 may be used to heat the first reactor 100 and the second reactor 200 with steam (ie, overhead material) generated by the stripping column 400 . In particular, the heat exchanger 300 absorbs heat from the effluent (ie, steam) of the stripping column 400 to raise the temperature of the material supplied to the first reactor 100 to increase the temperature of the microorganisms present in the first reactor 100. plays a role in enhancing the activity of

The stripping column 400 serves to remove inorganic substances from the effluent of the secondary reactor 200 . That is, the stripping column 400 may separate the effluent of the secondary reactor 200 into concentrated water in which inorganic components are concentrated and fresh water (steam).

As described above, steam generated by the stripping column 400 may be used to heat the primary reactor 100 and/or the secondary reactor 200 through the heat exchanger 300 .

The steam from which inorganic substances are removed from the stripping column 400 is discharged through the upper pipe (L6), passes through the heat exchanger (300), and then part is supplied to the primary reactor (100) through the pipe (L61), and the remaining part may be recycled to the top of the stripping column 400 through the pipe L62.

In addition, concentrated water in which inorganic substances are concentrated in the stripping column 400 may be discharged to the outside through the lower pipe L7.

In addition, the anaerobic digestion device 10 is disposed at the front end of the stripping column 400, and a reboiler configured to heat the effluent of the secondary reactor 200 and supply it to the stripping column 400 (Reboiler (not shown) ) may further include. The reboiler may heat the effluent of the secondary reactor 200 by exchanging heat with steam.

Preferred embodiments according to the present invention have been described with reference to the drawings above, but this is only exemplary, and those skilled in the art can understand that various modifications and equivalent other embodiments are possible therefrom. There will be. Therefore, the scope of protection of the present invention should be defined by the appended claims.

10: anaerobic digestion device 100, 200: reactor
101 inner wall 102 middle wall
103: outer wall 104: helical baffle
105: inclined baffle 300: heat exchanger
400: stripping column

Claims (20)

cover part;
a hollow inner wall disposed to be spaced apart from the cover and configured to allow fluid to flow upward in the internal space;
a hollow intermediate wall coupled to the cover part and configured to partially surround the hollow inner wall so that fluid flows downward in a space between the hollow inner wall and the hollow inner wall;
a hollow outer wall coupled to the cover part and configured to surround the hollow intermediate wall so that solid-liquid separation occurs in a space between the hollow intermediate wall and liquid flows upward and solid flows downward; and
A reactor comprising a helical baffle disposed in an inner space of the hollow inner wall. According to claim 1,
The hollow inner wall is a reactor in which a lower end is coupled to the hollow outer wall. According to claim 2,
The hollow inner wall includes a plurality of first through holes formed along a circumference of a lower end thereof. According to claim 1,
The reactor according to claim 1 , wherein the height of the lower end of the hollow intermediate wall is higher than that of the lower end of the hollow inner wall. According to claim 4,
The hollow middle wall includes a plurality of second through holes formed along a circumference of a lower end thereof and a third through hole formed at an upper end thereof. According to claim 1,
The hollow outer wall is configured such that the upper portion extends to have a constant width along the longitudinal direction and the lower portion gradually narrows toward the center along the longitudinal direction. According to claim 6,
The reactor further comprising a plurality of first inclined baffles coupled to the narrowed portion of the hollow outer wall and a plurality of second inclined baffles coupled to the hollow inner wall so as to cross each other with the first inclined baffle. According to claim 1,
A reactor further comprising an outlet pipe and a plurality of inlet pipes coupled to the lower end of the hollow outer wall in fluid communication. According to claim 1,
The reactor further comprises a plurality of other outflow pipes coupled to each other in fluid communication with each other at different heights of the middle portion of the hollow outer wall. According to claim 1,
A reactor further comprising another outlet pipe coupled to the cover part in fluid communication. According to claim 1,
A reactor that does not contain an internal stirrer. primary reactor;
a secondary reactor disposed after the primary reactor;
a stripping column disposed at the rear end of the secondary reactor; and
Anaerobic digestion apparatus comprising a heat exchanger configured to heat-exchange the effluent of the secondary reactor and the effluent of the stripping column. According to claim 12,
The primary reactor is an anaerobic digestion device according to any one of claims 1 to 12. According to claim 12,
Anaerobic digestion apparatus configured such that the effluent of the primary reactor is recycled to at least one of the primary reactor and the stripping column. According to claim 14,
Anaerobic digestion apparatus further comprising a pump for recycling the effluent of the primary reactor to at least one of the primary reactor and the stripping column. According to claim 12,
The secondary reactor is an anaerobic digestion device comprising an activated carbon layer. According to claim 12,
Anaerobic digestion apparatus configured such that the effluent of the secondary reactor is recycled to at least one of the primary reactor and the secondary reactor via the heat exchanger. According to claim 17,
Anaerobic digestion apparatus further comprising another pump for recycling the effluent of the secondary reactor to at least one of the primary reactor and the secondary reactor via the heat exchanger. According to claim 12,
Anaerobic digestion apparatus configured such that the effluent of the secondary reactor is recycled to at least one of the primary reactor and the secondary reactor by bypassing the heat exchanger. According to claim 12,
The anaerobic digestion apparatus is configured such that the effluent of the stripping column is recycled to at least one of the primary reactor and the stripping column via the heat exchanger.

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