WO2023096139A2 - Reactor and anaerobic digestion apparatus including same - Google Patents
Reactor and anaerobic digestion apparatus including same Download PDFInfo
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- WO2023096139A2 WO2023096139A2 PCT/KR2022/014909 KR2022014909W WO2023096139A2 WO 2023096139 A2 WO2023096139 A2 WO 2023096139A2 KR 2022014909 W KR2022014909 W KR 2022014909W WO 2023096139 A2 WO2023096139 A2 WO 2023096139A2
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/18—Flow directing inserts
- C12M27/20—Baffles; Ribs; Ribbons; Auger vanes
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M1/00—Apparatus for enzymology or microbiology
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M1/00—Apparatus for enzymology or microbiology
- C12M1/02—Apparatus for enzymology or microbiology with agitation means; with heat exchange means
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M1/00—Apparatus for enzymology or microbiology
- C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/26—Conditioning fluids entering or exiting the reaction vessel
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- 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.
- biogas or methane gas
- organic waste is converted into energy.
- 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.
- inorganic substances nitrogen, sulfur, and phosphorus: less than 0.1% of the total amount of inorganic substances
- 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.
- 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.
- 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;
- 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
- 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.
- the anaerobic digestion device has excellent removal efficiency of inorganic substances, and thus can achieve high biogas production efficiency with cost reduction.
- FIG. 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 .
- FIG. 4 is a cross-sectional view of the reactor of FIG. 1 taken along line “B-B”.
- FIG. 5 is an enlarged view of part “C” of the reactor of FIG. 1 .
- FIG. 6 is a diagram schematically showing an anaerobic digestion apparatus according to an embodiment of the present invention.
- fluid means a liquid, a gas, a mixture of a liquid and a solid, or a combination thereof.
- hollow refers to any hollow shape, for example, a cylindrical shape or a shape similar thereto.
- FIG. 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
- 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
- FIG. It is a drawing showing an enlarged part.
- the reactor 100 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 ).
- hollow inner wall 102 may have a lower end coupled to the hollow outer wall 104 .
- 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 ).
- 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 .
- 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).
- the outflow pipe EX3 It can be discharged to the outside of the reactor 100 through.
- 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).
- 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
- the hollow middle wall 103 and the hollow outer wall 104 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.
- large solids such as sludge may be precipitated.
- 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.
- the helical baffle 105 may have a screw shape.
- 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.
- 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).
- 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).
- 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.
- 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).
- FIG. 6 is a schematic view of an anaerobic digestion apparatus 10 according to an embodiment of the present invention.
- an anaerobic digestion apparatus 10 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.
- 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.
- CH 4 methane
- CO 2 carbon dioxide
- 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.
- 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 .
- the anaerobic digestion device 10 may be configured such that the effluent of the primary reactor 100 is recycled to the primary reactor 100.
- 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 .
- 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 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 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.
- 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.
- 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.
- 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
- 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.
- 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.
- 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.
- P2 another pump
- the concentration of inorganic substances in the first reactor 100 and/or the second reactor 200 may increase.
- 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.
- these inorganic acids become chemically unstable as the concentration increases.
- 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.
- 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.
- ammonia and hydrogen sulfide can act toxic to microorganisms.
- 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.
- 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.
- 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.
- 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 Of the effluent of the reactor 200 it may be determined by the flow rate that is recycled to the secondary reactor 200 through the pipes L4, L42, and L8 without passing through the heat exchanger 300.
- 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).
- 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.
- concentrated water in which inorganic substances are concentrated in the stripping column 400 may be discharged to the outside through the lower pipe L7.
- the anaerobic digestion device 10 is disposed in front 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.
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Abstract
A reactor and an anaerobic digestion apparatus including same are disclosed. The disclosed reactor comprises: a cover part; a hollow inner wall which 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 which 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 which 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 which is disposed in the inner space of the hollow inner wall.
Description
반응기 및 이를 포함하는 혐기성 소화 장치가 개시된다. 보다 상세하게는, 교반기 없이 고효율의 교반 및 원활한 재순환이 가능하도록 구성된 반응기 및 이를 포함하는 혐기성 소화 장치가 개시된다.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.
축산 분뇨 및 음식물 쓰레기 등과 같은 유기성 폐기물은 부패 및 침출수 등에 의해 환경을 심각하게 훼손시킬 수 있는 것으로서, 폐기시 반드시 종류별로 취합하여 정해진 폐기물 처리과정을 거쳐서 폐기되어야 한다.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.
그러나, 유기성 폐기물의 단순 폐기 처리는 처리시설 마련과 인력의 소모가 요구되는 것으로서, 생산적인 측면보다는 낭비적인 측면이 상대적으로 강하다.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.
이에 따라, 유기성 폐기물을 재활용하기 위한 방법과 기술들이 개발되고 있는데, 대표적으로는 유기성 폐기물을 이용하여 바이오 가스(또는 메탄 가스)를 생산하고, 유기성 폐기물을 통해 생산된 바이오 가스를 에너지화하는 기술 등을 꼽을 수 있다.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.
유기성 폐기물은 탄소, 수소, 소량의 무기물(질소, 황, 인: 무기물 총량 0.1% 미만)로 구성되어 있고, 혐기성 미생물 분해시 무기물이 배출되어 반응기에 축적된다. 축적되는 무기물은 제거되어야 하는데, 혐기성 미생물은 극소량의 무기물만 취하고 나머지는 축적되고, 축적된 무기물은 혐기성 미생물에 독성으로 작용하여 미생물의 활성을 저해한다.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.
한국공개특허 제10-2021-0113104호에 개시된 순환식 바이오 가스 생산 설비는 1차 반응기와 2차 반응기를 거친 반응액이 스트리핑 칼럼으로 공급되며, 거기서 증류공정을 통하여 무기산은 농축되고 깨끗한 물만 탑상물질로 배출되어 다시 1차 반응기로 공급되는 시스템으로서 결국 반응기 내에서의 무기물 축적을 막아준다. 그러나, 상기 순환식 바이오 가스 생산 설비는 무기물의 축적을 막기 위해 상당한 순환량이 필요하다는 문제점이 있다. 순환량이 많다는 것은 스트리핑 칼럼에서 엄청난 양의 깨끗한 물을 탑상물질로 배출한다는 것이며, 이것은 막대한 에너지 손실을 초래할뿐만 아니라, 물을 응축시키기 위한 추가 에너지 비용이 너무 커지게 된다.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.
본 발명의 일 구현예는 교반기 없이 고효율의 교반 및 원활한 재순환이 가능하도록 구성된 반응기를 제공한다.One embodiment of the present invention provides a reactor configured to enable high-efficiency agitation and smooth recirculation without an agitator.
본 발명의 다른 구현예는 바이오 가스의 생산 효율을 향상시킬 수 있는 혐기성 소화 장치를 제공한다.Another embodiment of the present invention provides an anaerobic digestion device capable of improving the production efficiency of biogas.
본 발명의 일 측면은,One aspect of the present invention,
커버부;cover part;
상기 커버부와 이격되게 배치된 것으로 내부 공간에서 상방으로 유체가 흐르도록 구성된 중공형 내벽;a hollow inner wall disposed to be spaced apart from the cover and configured to allow fluid to flow upward in the internal space;
상기 커버부에 결합된 것으로 상기 중공형 내벽을 부분적으로 둘러싸도록 구성되되, 상기 중공형 내벽과의 사이 공간에서 하방으로 유체가 흐르도록 구성된 중공형 중간벽;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;
상기 커버부에 결합된 것으로 상기 중공형 중간벽을 둘러싸도록 구성되되, 상기 중공형 중간벽과의 사이 공간에서 고액분리가 일어나 액체는 상방으로 흐르고 고체는 하방으로 흐르도록 구성된 중공형 외벽; 및a 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
상기 중공형 내벽의 내부 공간에 배치된 헬리컬 배플을 포함하는 반응기를 제공한다.A reactor including a helical baffle disposed in an inner space of the hollow inner wall is provided.
상기 중공형 내벽은 그 하단부가 상기 중공형 외벽에 결합된 것일 수 있다.The hollow inner wall may have a lower end coupled to the hollow outer wall.
상기 중공형 내벽은 그 하단부 둘레를 따라 형성된 복수개의 제1 관통홀을 포함할 수 있다.The hollow inner wall may include a plurality of first through holes formed along a circumference of a lower end thereof.
상기 중공형 중간벽은 그 하단부의 높이가 상기 중공형 내벽의 하단부의 높이 보다 높도록 구성될 수 있다.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.
상기 중공형 중간벽은 그 하단부 둘레를 따라 형성된 복수개의 제2 관통홀 및 그 상단부에 형성된 제3 관통홀을 포함할 수 있다.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.
상기 중공형 외벽은 상부는 길이방향을 따라 폭이 일정하도록 연장되고 하부는 길이방향을 따라 중심을 향해 폭이 점점 좁아지도록 구성될 수 있다.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.
상기 반응기는 상기 중공형 외벽의 폭이 좁아지는 부분에 결합된 복수개의 제1 경사 배플 및 상기 제1 경사 배플과 엇갈리도록 상기 중공형 내벽에 결합된 복수개의 제2 경사 배플을 더 포함할 수 있다.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. .
상기 반응기는 상기 중공형 외벽의 하단부에 유체 연통되게 결합된 유출배관 및 복수개의 유입배관을 더 포함할 수 있다.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.
상기 반응기는 상기 중공형 외벽의 중간부의 서로 다른 높이에 하나씩 유체 연통되게 결합된 복수개의 다른 유출배관을 더 포함할 수 있다.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.
상기 반응기는 상기 커버부에 유체 연통되게 결합된 또 다른 유출배관을 더 포함할 수 있다.The reactor may further include another outlet pipe coupled to the cover part in fluid communication.
상기 반응기는 내부 교반기를 포함하지 않을 수 있다.The reactor may not include an internal stirrer.
본 발명의 다른 측면은,Another aspect of the present invention is
1차 반응기;primary reactor;
상기 1차 반응기의 후단에 배치된 2차 반응기; a secondary reactor disposed after the primary reactor;
상기 2차 반응기의 후단에 배치된 스트리핑 칼럼; 및a stripping column disposed at the rear end of the secondary reactor; and
상기 2차 반응기의 유출물과 상기 스트리핑 칼럼의 유출물을 열교환시키도록 구성된 열교환기를 포함하는 혐기성 소화 장치를 제공한다.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.
상기 1차 반응기는 상술한 반응기일 수 있다.The primary reactor may be the above-described reactor.
상기 혐기성 소화 장치는 상기 1차 반응기의 유출물이 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환되도록 구성될 수 있다.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.
상기 혐기성 소화 장치는 상기 1차 반응기의 유출물을 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환시키는 펌프를 더 포함할 수 있다.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.
상기 2차 반응기는 활성탄층을 포함할 수 있다.The secondary reactor may include an activated carbon layer.
상기 혐기성 소화 장치는 상기 2차 반응기의 유출물이 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환되도록 구성될 수 있다.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.
상기 혐기성 소화 장치는 상기 2차 반응기의 유출물을 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환시키는 다른 펌프를 더 포함할 수 있다.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.
상기 혐기성 소화 장치는 상기 2차 반응기의 유출물이 상기 열교환기를 바이패스하여 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환되도록 구성될 수 있다.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.
상기 혐기성 소화 장치는 상기 스트리핑 칼럼의 유출물이 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환되도록 구성될 수 있다.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.
본 발명의 일 구현예에 따른 반응기는 교반기 없이 고효율의 교반 및 원활한 재순환이 가능하도록 구성되어 운전비용을 대폭 절감할 수 있다.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.
또한 본 발명의 일 구현예에 따른 혐기성 소화 장치는 무기물의 제거효율이 우수하여 비용절감과 함께 높은 바이오 가스 생산 효율을 달성할 수 있다. 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.
도 1은 본 발명의 일 구현예에 따른 반응기의 길이방향 단면도이다.1 is a longitudinal cross-sectional view of a reactor according to one embodiment of the present invention.
도 2는 도 1의 반응기의 작동 원리를 설명하기 위한 도면이다.Figure 2 is a view for explaining the operating principle of the reactor of Figure 1.
도 3은 도 1의 반응기 중 “A” 부분을 확대하여 도시한 도면이다.FIG. 3 is an enlarged view of part “A” of the reactor of FIG. 1 .
도 4는 도 1의 반응기 중 “B-B” 선을 절단하여 도시한 단면도이다.4 is a cross-sectional view of the reactor of FIG. 1 taken along line “B-B”.
도 5는 도 1의 반응기 중 “C” 부분을 확대하여 도시한 도면이다.FIG. 5 is an enlarged view of part “C” of the reactor of FIG. 1 .
도 6은 본 발명의 일 구현예에 따른 혐기성 소화 장치를 개략적으로 도시한 도면이다.6 is a diagram schematically showing an anaerobic digestion apparatus according to an embodiment of the present invention.
이하, 도면을 참조하여 본 발명의 일 구현예에 따른 반응기 및 이를 포함하는 혐기성 소화 장치를 상세히 설명한다. 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.
본 명세서에서, “상방”이란 중력의 역방향을 의미하고, “하방”이란 중력방향을 의미한다.In the present specification, "upward" means the opposite direction of gravity, and "downward" means the direction of gravity.
또한 본 명세서에서, “유체”란 액체, 기체, 액체와 고체의 혼합물 또는 이들의 조합을 의미한다.Also, in this specification, “fluid” means a liquid, a gas, a mixture of a liquid and a solid, or a combination thereof.
또한 본 명세서에서, “중공형”란 속이 빈 모든 형상을 의미하는 것으로, 예를 들어, 실린더형 또는 이와 유사한 형태를 말한다.In addition, in this specification, "hollow" refers to any hollow shape, for example, a cylindrical shape or a shape similar thereto.
도 1은 본 발명의 일 구현예에 따른 반응기(100)의 길이방향 단면도이고, 도 2는 도 1의 반응기(100)의 작동 원리를 설명하기 위한 도면이고, 도 3은 도 1의 반응기(100) 중 “A” 부분을 확대하여 도시한 도면이고, 도 4는 도 1의 반응기(100) 중 “B-B” 선을 절단하여 도시한 단면도이고, 도 5는 도 1의 반응기(100) 중 “C” 부분을 확대하여 도시한 도면이다.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.
도 1 및 도 2를 참조하면, 본 발명의 일 구현예에 따른 반응기(100)는 커버부(101), 중공형 내벽(102), 중공형 중간벽(103), 중공형 외벽(104) 및 헬리컬 배플(105)을 포함한다.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).
커버부(101)에는 유출배관(EX3)이 유체 연통되게 결합될 수 있다.An outflow pipe EX3 may be coupled to the cover unit 101 in fluid communication.
유출배관(EX3)은 가스 유출배관일 수 있다.The outlet pipe EX3 may be a gas outlet pipe.
중공형 내벽(102)는 그 상단부가 커버부(101)와 이격되게 배치된 것일 수 있다. 이러한 중공형 내벽(102)은 그 내부 공간에서 상방으로 유체가 흐르도록 구성될 수 있다. 구체적으로, 유체는 중공형 내벽(102)의 하단부 보다 낮은 위치에서부터 중공형 내벽(102)의 상단부 보다 높은 위치까지 흐를 수 있다(도 2의 화살표 참조). 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 ).
또한, 중공형 내벽(102)는 그 하단부가 중공형 외벽(104)에 결합된 것일 수 있다.In addition, the hollow inner wall 102 may have a lower end coupled to the hollow outer wall 104 .
또한, 중공형 내벽(102)는 그 하단부 둘레를 따라 형성된 복수개의 제1 관통홀(h1)을 포함할 수 있다. 이러한 제1 관통홀(h1)을 통해 중공형 내벽(102)의 내부 공간과, 중공형 내벽(102)과 중공형 외벽(104) 사이의 공간이 서로 연통되어, 도 2에 도시된 바와 같이, 중공형 내벽(102)과 중공형 외벽(104) 사이의 공간으로부터 중공형 내벽(102)의 내부 공간으로 유체가 유입될 수 있다(도 2의 화살표 참조).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 ).
중공형 중간벽(103)은 그 상단부가 커버부(101)에 결합된 것일 수 있다. 이러한 중공형 중간벽(103)은 중공형 내벽(102)을 부분적으로 둘러싸도록 구성되되, 중공형 내벽(102)과의 사이 공간에서 하방으로 유체가 흐르도록 구성될 수 있다. 구체적으로, 중공형 내벽(102)의 상단부 위로 오버플로우된 유체는 중공형 내벽(102)과 중공형 중간벽(103) 사이의 공간에서 하방으로 흐를 수 있다(도 2의 화살표 참조). 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 ).
또한, 중공형 중간벽(103)은 그 하단부의 높이가 중공형 내벽(102)의 하단부의 높이 보다 높도록 구성될 수 있다.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 .
또한, 중공형 중간벽(103)은 그 하단부 둘레를 따라 형성된 복수개의 제2 관통홀(h2) 및 그 상단부에 형성된 제3 관통홀(h3)을 포함할 수 있다. 제2 관통홀(h2)을 통해 중공형 내벽(102)과 중공형 중간벽(103) 사이의 공간과, 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간이 서로 연통되어, 도 2에 도시된 바와 같이, 중공형 내벽(102)과 중공형 중간벽(103) 사이의 공간으로부터 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간으로 유체가 유입될 수 있다(도 2의 화살표 참조). 또한, 제3 관통홀(h3)을 통해 기체가 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간으로부터 중공형 중간벽(103)의 내부 공간으로 유출된 후 유출배관(EX3)을 통해 반응기(100)의 외부로 배출될 수 있다. 예를 들어, 제3 관통홀(h3) 및 유출배관(EX3)을 통해 외부로 배출되는 기체는 바이오 가스(메탄)를 포함할 수 있다. 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).
중공형 외벽(104)은 그 상단부가 커버부(101)에 결합된 것일 수 있다. 이러한 중공형 외벽(104)은 중공형 중간벽(103)을 둘러싸도록 구성되되, 중공형 중간벽(103)과의 사이 공간에서 고액분리가 일어나 액체는 상방으로 흐르고 고체는 하방으로 흐르도록 구성될 수 있다(도 2의 화살표 참조). 구체적으로, 중공형 내벽(102)과 중공형 중간벽(103) 사이의 공간에서 하방으로 흘러내린 유체(즉, 액체와 고체의 혼합물)는 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간으로 유입되어 상방으로 흘러올라가면서 고액분리가 일어나게 된다. 즉, 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간은 상방으로 흐르는 유체의 유속을 낮춰 그 공간내에서 고액분리가 일어나기에 충분히 넓도록 설계될 수 있다. 구체적으로, 중공형 중간벽(103)과 중공형 외벽(104) 사이의 공간에서는 슬러지와 같은 큰 고형물이 침전될 수 있다.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.
또한, 중공형 외벽(104)은 상부는 길이방향을 따라 폭이 일정하도록 연장되고 하부는 길이방향을 따라 중심을 향해 폭이 점점 좁아지도록 구성될 수 있다.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.
헬리컬 배플(helical baffle)(105)은 중공형 내벽(102)의 내부 공간에 배치될 수 있다. 이러한 헬리컬 배플(105)은 반응기(100)에 유입되는 유체에 와류(vortex)를 형성하여 유체에 함유된 성분들간의 혼합도(degree of mixing)를 증가시키는 역할을 수행한다. 구체적으로, 펌프 등에 의해 유체가 소정의 압력으로 반응기(100)에 유입되어 상방으로 상승하게 되면, 그 유체는 헬리컬 배플(105)의 작용에 의해 와류를 형성하여 내부 교반기가 없어도 잘 혼합되게 된다. 따라서, 반응기(100)는 내부 교반기를 포함하지 않을 수 있다.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.
구체적으로, 헬리컬 배플(105)은 스크류 형상으로 구성될 수 있다.Specifically, the helical baffle 105 may have a screw shape.
또한, 반응기(100)는 헬리컬 배플(105)에 고정되게 설치된 스크린 및 상기 스크린에 충진된 활성탄을 더 포함할 수 있다. 이에 따라, 반응액과 활성탄의 접촉 면적이 증가할뿐만 아니라 반응액의 유로가 막히지 않고 미생물이 축적되지 않으므로 바이오 가스의 생산 효율성이 더욱 향상될 수 있다.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.
또한, 반응기(100)는 중공형 외벽(104)의 폭이 좁아지는 부분에 결합된 복수개의 제1 경사 배플(106-1) 및 제1 경사 배플(106-1)과 엇갈리도록 중공형 내벽(102)에 결합된 복수개의 제2 경사 배플(106-2)을 더 포함할 수 있다.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.
제1 경사 배플(106-1) 및 제2 경사 배플(106-2)은 와류를 형성하여 유체가 하방(즉, AR1 방향)으로는 흐르도록 하되, 압력손실이 큰 상방(즉, AR2 방향)으로는 유체가 흐르지 못하게 하는 역할을 수행한다(도 5 참조). 예를 들어, 제1 경사 배플(106-1) 및 제2 경사 배플(106-2)의 경사각은 중공형 내벽의 중심축 연장선(즉, 수직선)을 기준으로 최대 30°일 수 있다(도 5 참조).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).
또한, 반응기(100)는 중공형 외벽(104)의 하단부에 유체 연통되게 결합된 유출배관(EX4) 및 복수개의 유입배관(EN1, EN2)을 더 포함할 수 있다.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.
유출배관(EX4)은 주로 이물질(즉, 미생물이 분해 못하는 각종 이물질(흙, 기타 불순물 등))의 배출 통로로 사용될 수 있다.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).
유입배관(EN1)으로는 원료 및/또는 후술하는 스트리핑 칼럼에서 배출된 스팀의 응축수가 유입될 수 있다. Raw materials and/or condensed water from steam discharged from the stripping column described below may flow into the inflow pipe EN1.
유입배관(EN2)으로는 반응기(100)의 유출물 및/또는 후술하는 2차 반응기의 유출물이 유입될 수 있다.An effluent of the reactor 100 and/or an effluent of a secondary reactor described later may flow into the inlet pipe EN2.
또한, 반응기(100)는 중공형 외벽(104)의 중간부의 서로 다른 높이에 하나씩 유체 연통되게 결합된 복수개의 다른 유출배관(EX1, EX2)을 더 포함할 수 있다.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 .
유출배관(EX1)으로는 물과 함께 극미량의 부유물질(suspended solid)이 배출될 수 있으며, 이러한 물질들은 유출배관(EX1)에 펌프(미도시)를 연결하더라도 그 펌프에 영향을 주지 않을 수 있다.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. .
유출배관(EX2)으로는 거대 고형물을 함유하지 않는 유체가 배출될 수 있다.A fluid that does not contain macro-solids can be discharged through the outflow pipe (EX2).
도 6은 본 발명의 일 구현예에 따른 혐기성 소화 장치(10)를 개략적으로 도시한 도면이다.6 is a schematic view of an anaerobic digestion apparatus 10 according to an embodiment of the present invention.
도 6을 참조하면, 본 발명의 일 구현예에 따른 혐기성 소화 장치(10)는 1차 반응기(100), 2차 반응기(200), 열교환기(300) 및 스트리핑 칼럼(400)을 포함한다.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.
1차 반응기(100)는 유기성 폐기물 원료를 미생물과 혐기성 발효시켜 저급 유기산과 무기산으로 가수분해시키고 바이오 가스를 생성하는 역할을 수행한다.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.
1차 반응기(100)로 투입되는 유기성 폐기물 원료는 이에 한정되는 것은 아니지만, 예를 들어, 0.1중량% 미만의 무기물(질소, 황 및 인)을 포함할 수 있다. 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.
상기 유기성 폐기물 원료는 음식물 쓰레기, 동물의 사체, 식물, 인분, 가축분뇨, 도살장 폐기물(예를 들어, 가축 피 등) 또는 이들의 조합을 포함할 수 있다.The organic waste raw material may include food waste, animal carcasses, plants, manure, livestock manure, slaughterhouse waste (eg, livestock blood), or a combination thereof.
구체적으로, 1차 반응기(100)는 유기물과 미생물을 소정 온도내에서 일정 시간동안 반응시켜 메탄(CH4) 및 이산화탄소(CO2)를 포함하는 바이오 가스를 생성하는 역할을 수행한다. 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.
보다 구체적으로, 1차 반응기(100)는 이에 구비된 유입배관을 통해 음식물 쓰레기나 가축 분뇨와 같은 유기성 폐기물 원료가 유입될 경우, 이 유기성 폐기물에 대한 혐기성 발효를 진행함으로써 유기성 폐기물을 가수분해하여 저급 유기산 및 무기산으로 전환시키거나 메탄을 포함하는 바이오 가스를 생성할 수 있다.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.
상기 저급 유기산은 아세트산(aetic acid), 프로피온산(popionic acid), 부티르산(butyric acid) 또는 이들의 조합을 포함할 수 있고, 이들 물질은 분자량이 작고 가벼워서 휘발이 잘되므로 휘발성 지방산(VFA: volatile fatty acid)으로 지칭될 수 있다.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
상기 미생물은 메탄균, 가수분해균, 탈질세균, 황환원세균, 공생초산생성균, 호모초산생성균 또는 이들의 조합을 포함할 수 있다.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.
1차 반응기(100)에 원료로 투입되는 유기성 폐기물은 주거 시설에서 배출되는 음식물 쓰레기, 인분 및 생활 폐수; 축사에서 배출되는 축분 및 폐수; 또는 이들의 조합을 포함할 수 있고, 미생물과 혼합되어 미생물을 사멸시키지 않는 유기물이라면 모두 적용 가능하다.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.
또한, 1차 반응기(100)의 상단부에는 바이오 가스 수집부가 설치되어 상술한 과정을 거쳐 생성된 바이오 가스를 포집할 수 있다.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.
1차 반응기(100)는 도 1 내지 도 5를 참조하여 설명된 상술한 반응기(100)와 동일하거나 유사한 것일 수 있다.The primary reactor 100 may be the same as or similar to the reactor 100 described above with reference to FIGS. 1 to 5 .
또한, 혐기성 소화 장치(10)는 1차 반응기(100)의 유출물이 1차 반응기(100)로 재순환되도록 구성될 수 있다. 구체적으로, 혐기성 소화 장치(10)는 1차 반응기(100)의 유출물을 1차 반응기(100)로 재순환시키는 펌프(P1)를 더 포함할 수 있다. 이와 같이 펌프(P1)로 1차 반응기(100)의 유출물을 1차 반응기(100)로 재순환시킴으로써 1차 반응기(100) 내에서는 내부 교반기 없이도 유입 물질들 간의 혼합이 원활하게 일어날 수 있을 뿐만 아니라 1차 반응기(100) 내에서 무기물의 축적이 원활하게 이루어질 수 있다.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 .
또한, 1차 반응기(100)는 50~65℃의 온도로 유지될 수 있다. 1차 반응기(100)의 온도는 배관(L1)을 통해 이에 공급되는 원료의 유량, 1차 반응기(100)의 유출물 중 배관(L2)을 통해 펌프(P1)에 의해 1차 반응기(100)로 재순환되는 유량, 1차 반응기(100)의 유출물 중 배관(L3)을 통해 2차 반응기(200)로 공급되는 유량, 2차 반응기(200)의 유출물 중 배관(L4, L41)을 통해 열교환기(300)를 거친 후 배관(L9)을 통해 1차 반응기(100)로 재순환되는 유량, 2차 반응기(200)의 유출물 중 열교환기(300)를 거치지 않고 배관(L4, L42, L9)을 통해 1차 반응기(100)로 재순환되는 유량, 스트리핑 칼럼(400)의 유출물 중 배관(L6)을 통해 열교환기(300)를 거친 후 배관(L61)을 통해 1차 반응기(100)로 재순환되는 유량, 및 스트리핑 칼럼(400)의 유출물 중 배관(L6)을 통해 열교환기(300)를 거친 후 배관(L62)을 통해 스트리핑 칼럼(400)으로 재순환되는 유량 등에 의해 결정될 수 있다. 여기서, 각각의 유량은 펌프(P1, P2, P3) 및 컨트롤 밸브(CV1~CV5) 등에 의해 조절될 수 있다.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.
2차 반응기(200)는 1차 반응기(100)에서 완전히 분해되지 않은 저급 유기산(휘발성 지방산)을 혐기성 미생물로 분해하여 메탄을 포함하는 바이오 가스를 생성하는 역할을 수행하는 것으로, 고정된 스크린(미도시)에 충진된 활성탄층을 포함할 수 있다.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.
구체적으로, 2차 반응기(200)에서는 1차 반응기(100)에서 완전히 분해되지 않은 저급 유기산이 활성탄층에 흡착된 후 미생물에 의해 분해되어 메탄 가스를 생성하게 된다.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.
보다 구체적으로, 2차 반응기(200)에서는 1차 반응기(100)에서 분리되어 유입된 저급 유기산이 메탄 생성 미생물들의 자양분이 되므로, 메탄을 포함하는 바이오 가스의 생산이 이루어지며, 1차 반응기(100)와 동일하게 2차 반응기(200)에서 생성되는 바이오 가스는 바이오 가스 수집부에 별도로 포집될 수 있다.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.
또한, 혐기성 소화 장치(10)는 바이오 가스 수집부에 수집된 바이오 가스를 자원으로 활용할 수 있도록, 상기 바이오 가스 수집부에 연결된 가스 파워 플랜트를 더 포함할 수 있으며, 상기 가스 파워 플랜트에서는 전력을 생산할 수 있다.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
또한, 2차 반응기(200)의 유출물의 유량은 스트리핑 칼럼(400)의 탑상유량(즉, 상부 유출물의 유량)에 의해 결정될 수 있다. 즉, 스트리핑 칼럼(400)의 탑상유량이 증가하면 2차 반응기(200)의 유출물의 유량도 증가하게 된다.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.
또한, 혐기성 소화 장치(10)는 2차 반응기(200)의 유출물이 열교환기(300)를 거쳐 1차 반응기(100) 및/또는 2차 반응기(200)로 재순환되도록 구성될 수 있다. 구체적으로, 혐기성 소화 장치(10)는 1차 반응기(100)의 유출물을 열교환기(300)를 거쳐 1차 반응기(100) 및/또는 2차 반응기(200)로 재순환시키는 다른 펌프(P2)를 더 포함할 수 있다. 이러한 재순환을 통해 1차 반응기(100) 및/또는 2차 반응기(200) 내의 무기물의 농도가 증가할 수 있다. 1차 반응기(100) 및 2차 반응기(200) 내에서 무기물은 강한 무기산(질산, 황산, 인산) 등으로 존재하는데, 이러한 무기산은 농도가 낮을 경우 화학적으로 상당히 안정하다. 그러나, 이러한 무기산은 농도가 높아짐에 따라 화학적으로 불안정해지며, 특히 혐기성 소화는 수소가 많은 환경으로서 무기산 농도가 축적됨에 따라 화학적으로 불안정해진 무기산은 수소와 반응하여 암모니아 및/또는 황화수소로 변화하여 화학평형을 이룰 수 있다. 따라서, 무기산이 암모니아나 황화수소로 변하지 않는 최대허용농도가 존재하게 되며, 2차 반응기(200)는 최대허용농도가 넘지 않는 조건하에서 가동되는 것이 바람직하고, 이에 맞추어 스트리핑 칼럼(400)의 탑상물질의 양도 결정되는 것이 바람직하다. 예를 들어, 최대허용농도는 1중량%일 수 있다. 즉, 2차 반응기(200) 내의 무기물(즉, 무기산)의 농도가 높아지면, 스트리핑 칼럼(400)의 탑상물질의 양이 적더라도 많은 양의 무기물을 배출시킬 수 있다. 참고로, 암모니아 및 황화수소는 미생물에 독성으로 작용할 수 있다. 그러나, 본 발명이 이에 한정되는 것은 아니며, 2차 반응기(200)의 최대허용농도는 상황에 따라 달라질 수 있다. 또한, 2차 반응기(200)의 최대허용농도는 1차 반응기(100)의 크기, 2차 반응기(200)의 크기 및 스트리핑 칼럼(400)의 순환량에 의해 결정될 수 있다.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.
그런데, 2차 반응기(200) 내의 무기물의 농도가 최대허용농도에 근접하지만 이를 초과하지 않는 수준까지 증가할 경우에는 2차 반응기(200)에서 스트리핑 칼럼(400)으로 배출되는 무기물의 양이 많아져서 무기물의 제거를 위한 스트리핑 칼럼(400)의 탑상물질의 운전 배출량이 감소할 수 있다. 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.
또한, 혐기성 소화 장치(10)는 2차 반응기(200)의 유출물이 열교환기(300)를 바이패스하여 1차 반응기(100) 및/또는 2차 반응기(200)로 재순환되도록 구성될 수 있다. 이러한 구성은 스트리핑 칼럼(400)의 탑상물질이 응축되어 포화수(saturated water) 상태로 1차 반응기(100) 및/또는 스트리핑 칼럼(400)으로 재순환되도록 하기 위한 것일 수 있다.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.
또한, 2차 반응기(100)는 30~35℃의 온도로 유지될 수 있다. 2차 반응기(200)의 온도는 배관(L3)을 통해 이에 공급되는 1차 반응기(100) 유출물의 유량, 2차 반응기(200)의 유출물 중 배관(L5)을 통해 스트리핑 칼럼(400)으로 공급되는 유량, 2차 반응기(200)의 유출물 중 배관(L4, L41)을 통해 열교환기(300)를 거친 후 배관(L8)을 통해 2차 반응기(200)로 재순환되는 유량, 및 2차 반응기(200)의 유출물 중 열교환기(300)를 거치지 않고 배관(L4, L42, L8)을 통해 2차 반응기(200)로 재순환되는 유량 등에 의해 결정될 수 있다. 여기서, 각각의 유량은 펌프(P1) 및 컨트롤 밸브(CV1~CV5) 등에 의해 조절될 수 있다.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 Of the effluent of the reactor 200, it may be determined by the flow rate that is recycled 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.
열교환기(300)는 2차 반응기(200)의 유출물과 스트리핑 칼럼(400)의 유출물을 열교환시키도록 구성될 수 있다. 즉, 열교환기(300)는 스트리핑 칼럼(400)에 의해 생성된 스팀(즉, 탑상물질)으로 1차 반응기(100) 및 2차 반응기(200)를 가열하는데 활용될 수 있다. 특히, 열교환기(300)는 스트리핑 칼럼(400)의 유출물(즉, 스팀)로부터 열을 흡수하여 1차 반응기(100)로 공급되는 물질의 온도를 높여 1차 반응기(100) 내에 존재하는 미생물의 활성을 향상시키는 역할을 수행한다. 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
스트리핑 칼럼(400)은 2차 반응기(200)의 유출물 중의 무기물을 제거하는 역할을 수행한다. 즉, 스트리핑 칼럼(400)은 2차 반응기(200)의 유출물을 무기물 성분이 농축된 농축수와 청수(스팀)로 분리할 수 있다.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).
상술한 바와 같이 스트리핑 칼럼(400)에 의해 생성된 스팀은 열교환기(300)를 통하여 1차 반응기(100) 및/또는 2차 반응기(200)를 가열하는데 활용될 수 있다.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 .
스트리핑 칼럼(400)에서 무기물이 제거된 스팀은 상부 배관(L6)을 통해 배출되어 열교환기(300)를 통과한 후 일부는 배관(L61)을 통해 1차 반응기(100)로 공급되고, 나머지 일부는 배관(L62)을 통해 스트리핑 칼럼(400)의 상부로 재순환될 수 있다.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.
또한, 스트리핑 칼럼(400)에서 무기물이 농축된 농축수는 하부 배관(L7)을 통해 외부로 배출될 수 있다.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.
또한, 혐기성 소화 장치(10)는 스트리핑 칼럼(400)의 전단에 배치된 것으로, 2차 반응기(200)의 유출물을 가열하여 스트리핑 칼럼(400)에 공급하도록 구성된 재비기(Reboiler)(미도시)를 더 포함할 수 있다. 상기 재비기는 2차 반응기(200)의 유출물을 스팀과 열교환시켜 가열할 수 있다.In addition, the anaerobic digestion device 10 is disposed in front 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.
이상에서 도면을 참조하여 본 발명에 따른 바람직한 구현예가 설명되었으나, 이는 예시적인 것에 불과하며, 당해 기술분야에서 통상의 지식을 가진 자라면 이로부터 다양한 변형 및 균등한 타 구현예가 가능하다는 점을 이해할 수 있을 것이다. 따라서, 본 발명의 보호범위는 첨부된 특허청구범위에 의해서 정해져야 할 것이다Preferred 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.
Claims (20)
- 커버부;cover part;상기 커버부와 이격되게 배치된 것으로 내부 공간에서 상방으로 유체가 흐르도록 구성된 중공형 내벽;a hollow inner wall disposed to be spaced apart from the cover and configured to allow fluid to flow upward in the internal space;상기 커버부에 결합된 것으로 상기 중공형 내벽을 부분적으로 둘러싸도록 구성되되, 상기 중공형 내벽과의 사이 공간에서 하방으로 유체가 흐르도록 구성된 중공형 중간벽;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;상기 커버부에 결합된 것으로 상기 중공형 중간벽을 둘러싸도록 구성되되, 상기 중공형 중간벽과의 사이 공간에서 고액분리가 일어나 액체는 상방으로 흐르고 고체는 하방으로 흐르도록 구성된 중공형 외벽; 및a 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; and상기 중공형 내벽의 내부 공간에 배치된 헬리컬 배플을 포함하는 반응기.A reactor comprising a helical baffle disposed in an inner space of the hollow inner wall.
- 제1항에 있어서, According to claim 1,상기 중공형 내벽은 그 하단부가 상기 중공형 외벽에 결합된 반응기.The hollow inner wall is a reactor in which a lower end is coupled to the hollow outer wall.
- 제2항에 있어서, According to claim 2,상기 중공형 내벽은 그 하단부 둘레를 따라 형성된 복수개의 제1 관통홀을 포함하는 반응기.The hollow inner wall includes a plurality of first through holes formed along a circumference of a lower end thereof.
- 제1항에 있어서, According to claim 1,상기 중공형 중간벽은 그 하단부의 높이가 상기 중공형 내벽의 하단부의 높이 보다 높도록 구성된 반응기.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.
- 제4항에 있어서, According to claim 4,상기 중공형 중간벽은 그 하단부 둘레를 따라 형성된 복수개의 제2 관통홀 및 그 상단부에 형성된 제3 관통홀을 포함하는 반응기.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.
- 제1항에 있어서, According to claim 1,상기 중공형 외벽은 상부는 길이방향을 따라 폭이 일정하도록 연장되고 하부는 길이방향을 따라 중심을 향해 폭이 점점 좁아지도록 구성된 반응기.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.
- 제6항에 있어서, According to claim 6,상기 중공형 외벽의 폭이 좁아지는 부분에 결합된 복수개의 제1 경사 배플 및 상기 제1 경사 배플과 엇갈리도록 상기 중공형 내벽에 결합된 복수개의 제2 경사 배플을 더 포함하는 반응기.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.
- 제1항에 있어서, According to claim 1,상기 중공형 외벽의 하단부에 유체 연통되게 결합된 유출배관 및 복수개의 유입배관을 더 포함하는 반응기.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.
- 제1항에 있어서, According to claim 1,상기 중공형 외벽의 중간부의 서로 다른 높이에 하나씩 유체 연통되게 결합된 복수개의 다른 유출배관을 더 포함하는 반응기.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.
- 제1항에 있어서, According to claim 1,상기 커버부에 유체 연통되게 결합된 또 다른 유출배관을 더 포함하는 반응기.A reactor further comprising another outlet pipe coupled to the cover part in fluid communication.
- 제1항에 있어서, According to claim 1,내부 교반기를 포함하지 않는 반응기.A reactor that does not contain an internal stirrer.
- 1차 반응기;primary reactor;상기 1차 반응기의 후단에 배치된 2차 반응기; a secondary reactor disposed after the primary reactor;상기 2차 반응기의 후단에 배치된 스트리핑 칼럼; 및a stripping column disposed at the rear end of the secondary reactor; and상기 2차 반응기의 유출물과 상기 스트리핑 칼럼의 유출물을 열교환시키도록 구성된 열교환기를 포함하는 혐기성 소화 장치.Anaerobic digestion apparatus comprising a heat exchanger configured to heat-exchange the effluent of the secondary reactor and the effluent of the stripping column.
- 제12항에 있어서,According to claim 12,상기 1차 반응기는 제1항 내지 제12항 중 어느 한 항에 따른 반응기인 혐기성 소화 장치.The primary reactor is an anaerobic digestion device according to any one of claims 1 to 12.
- 제12항에 있어서,According to claim 12,상기 1차 반응기의 유출물이 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환되도록 구성된 혐기성 소화 장치.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.
- 제14항에 있어서,According to claim 14,상기 1차 반응기의 유출물을 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환시키는 펌프를 더 포함하는 혐기성 소화 장치.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.
- 제12항에 있어서,According to claim 12,상기 2차 반응기는 활성탄층을 포함하는 혐기성 소화 장치.The secondary reactor is an anaerobic digestion device comprising an activated carbon layer.
- 제12항에 있어서,According to claim 12,상기 2차 반응기의 유출물이 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환되도록 구성된 혐기성 소화 장치.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.
- 제17항에 있어서,According to claim 17,상기 2차 반응기의 유출물을 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환시키는 다른 펌프를 더 포함하는 혐기성 소화 장치.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.
- 제12항에 있어서,According to claim 12,상기 2차 반응기의 유출물이 상기 열교환기를 바이패스하여 상기 1차 반응기 및 상기 2차 반응기 중 적어도 하나의 반응기로 재순환되도록 구성된 혐기성 소화 장치.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.
- 제12항에 있어서,According to claim 12,상기 스트리핑 칼럼의 유출물이 상기 열교환기를 거쳐 상기 1차 반응기 및 상기 스트리핑 칼럼 중 적어도 하나로 재순환되도록 구성된 혐기성 소화 장치.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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