CN112279369A - Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow - Google Patents
Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow Download PDFInfo
- Publication number
- CN112279369A CN112279369A CN202011013149.5A CN202011013149A CN112279369A CN 112279369 A CN112279369 A CN 112279369A CN 202011013149 A CN202011013149 A CN 202011013149A CN 112279369 A CN112279369 A CN 112279369A
- Authority
- CN
- China
- Prior art keywords
- biogas
- water
- uasb
- methane
- absorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- 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
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Microbiology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Biodiversity & Conservation Biology (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a method for absorbing CO by alkali liquor2The device comprises a UASB reaction barrel, a water-sealed bottle, a biogas collection chamber, an absorption device, a biogas storage chamber and a water tank; the bottom of the UASB reaction cylinder is provided with a water inlet which is connected with a water tank for storing wastewater to be treated through a water inlet pump; the top gas phase outlet of the three-phase separator at the upper part of the cylinder body is connected with a water-sealed bottle which is sequentially communicated with the biogas collecting chamber and the absorbing device; the absorption device is used for containing alkaline absorption liquid to absorb CO2 gas in the biogas; the upper part of the absorption device is externally connected with a methane storage chamber, and the lower part of the absorption device is communicated with a water tank. The invention utilizes NaOH solution to absorb CO in the biogas2Absorbing saturated NaHCO3The solution is refluxed to the UASB reactor to be increasedThe alkalinity of the inlet water and the buffer capacity of an anaerobic system are improved, so that the efficient and stable operation of the anaerobic biological treatment process is ensured, and meanwhile, the ratio of methane in the purified methane is more than 90%, which is beneficial to the subsequent resource energy utilization of methane.
Description
Technical Field
The invention relates to a method for absorbing CO by alkali liquor2A device and a method for enhancing UASB process performance by backflow belong to the technical field of biological wastewater treatment.
Background
The anaerobic granular sludge process has the advantages of high wastewater treatment efficiency, long sludge retention time, good sludge-water separation effect, small reactor occupied area and the like, can realize the recovery of biomass energy methane while efficiently decarbonizing wastewater, and is widely applied to the treatment of high-concentration organic industrial wastewater at present. The anaerobic fermentation methanogenesis process needs a plurality of anaerobic intervarietal bacteria to cooperate, organic matters in the waste water are firstly hydrolyzed by zymogen to generate small molecular acid alcohol such as propionic acid, butyric acid, ethanol and the like, and then are subjected to hydrogen-producing acetogenic bacteria to generate simple substances such as acetic acid, hydrogen and the like to be used as substrates of methanogenic bacteria. However, the balance among anaerobic intervarietal bacteria is weak, and compared with hydrolytic zymogens and hydrogen-producing acetogens, the methanogens have slower metabolism and growth rate and higher requirements on the environment. When the anaerobic system is in an overload state (such as a starting stage or load impact), the acid production rate is higher than the methane production rate, so that volatile fatty acid is accumulated, and if the buffer capacity of the system is insufficient, the methane production activity is inhibited by too low pH, so that the anaerobic system is finally unstable and crashed.
How to strengthen the stable operation of the anaerobic biological treatment process is always a research hotspot in the environmental field, many researchers try to improve the buffer capacity of an anaerobic system by mixing low-alkalinity wastewater (such as chemical synthetic wastewater, synthetic plastic wastewater, artificial fiber wastewater and the like) and high-alkalinity wastewater (such as livestock and poultry breeding wastewater and the like), but different types of wastewater are often difficult to obtain at the same time and spatial scale. Therefore, the development of the high-efficiency, simple and economic anaerobic biological treatment device and method has higher application value for the high-efficiency and stable treatment of the low-alkalinity high-organic industrial wastewater.
In industrial production, a large amount of waste alkali (mainly NaOH) is generated, but the direct backflow of the waste alkali to an anaerobic biological system can cause the pH value of the system to be too high. NaHCO 23Is an ideal wastewater alkalinity substance, but the direct purchase cost is too high. CO in methane in anaerobic treatment process of industrial wastewater2The actual proportion is 25-50%, and the recycling utilization of the methane is severely restricted. Therefore, it is highly desirable to provide a method for absorbing CO with lye2A device and a method for enhancing the UASB process performance by reflux.
Disclosure of Invention
The invention aims to solve the bottleneck problems of long start-up time, poor stability, difficult methane recycling and the like of an anaerobic system in the anaerobic treatment process of wastewater, and provides a method for absorbing CO by alkali liquor2A device and a method for enhancing the UASB process performance by reflux. The invention absorbs CO in the biogas by using NaOH solution2Formation of NaHCO from the component3And the solution is refluxed to the UASB reactor, so that the alkalinity of the wastewater is increased, the buffering capacity of an anaerobic system is improved, and the microbial habitat is improved, thereby realizing the high-efficiency stable decarbonization and yield of the high-concentration organic industrial wastewater and the high-quality recycling of methane.
The invention adopts the following specific technical scheme:
absorbing CO by alkali liquor2The device for reinforcing the technological performance of the UASB comprises a UASB reaction cylinder, a water-sealed bottle, a biogas collection chamber, an absorption device, a biogas storage chamber and a water tank;
the bottom of the UASB reaction cylinder is provided with a water inlet which is connected with a water tank for storing wastewater to be treated through a water inlet pump; the lower part in the cylinder body is provided with a water distribution plate, the middle part is a sludge bed, and the upper part is provided with a three-phase separator; an overflow weir and a water outlet are arranged on the side wall of the cylinder body above the three-phase separator; a gas phase outlet at the top end of the three-phase separator is connected with a water-sealed bottle, the water-sealed bottle is communicated with a biogas collecting chamber through a gas flowmeter, and the biogas collecting chamber is communicated with an absorption device through a fan; in the absorption deviceContaining alkaline absorption liquid to absorb CO in marsh gas2A gas; the upper part of the absorption device is externally connected with a biogas storage chamber through a gas pipeline, the lower part of the absorption device is provided with a liquid outlet, and the absorption device is communicated with the water tank through a liquid outlet pipe and is used for refluxing the liquid part in the absorption device into the water tank; the biogas collecting chamber, the absorbing device and the biogas storage chamber are all closed containers.
Preferably, the gas flowmeter is a wet gas flowmeter.
Preferably, the fan is an explosion-proof variable frequency fan.
Preferably, the air inlet pipe of the absorption device extends into the cylinder of the absorption device, and the tail end of the air inlet pipe is provided with a microporous aeration disc.
Furthermore, the height-diameter ratio of the absorption device is 4:1, and the microporous aeration disc is made of ABS material.
Preferably, the absorption liquid is 0.1mol/L NaOH solution for absorbing CO2Gas post formation of NaHCO3And (3) solution.
Preferably, a stirring device is arranged in the water tank and is used for uniformly mixing the backflow liquid which flows back from the absorption device and the inlet water.
The invention also aims to provide a device for absorbing CO in biogas based on any one of the devices2And refluxing to enhance the UASB process performance, which comprises the following steps:
pumping wastewater in the water tank into the UASB reaction barrel through a water inlet pump, uniformly distributing water under the action of a water distribution plate, separating sludge, methane and liquid in a three-phase separator after sludge bed treatment, re-settling the sludge, discharging the liquid from a water outlet through an overflow weir on the side wall of the barrel, and overflowing the methane from the top of the three-phase separator; biogas enters the biogas collection chamber after passing through the water-sealed bottle, and the flow of the biogas is regulated and controlled by the fan to control the air pressure in the biogas collection chamber and maintain the air pressure in the gas path to be stable; then the marsh gas is blown into an absorption device under the action of a fan, and CO in the marsh gas is absorbed by absorption liquid2Converting the gas into a weakly alkaline solution; CO removal2The biogas after being gas is introduced into a biogas storage chamber from a gas pipeline at the upper part of the absorption device for storage, so that the methane is internally storedThe alkyl ratio is improved; absorption of CO2The absorption liquid after gas partially flows back to the water tank through a liquid outlet at the lower part of the absorption device and is mixed with the wastewater to be treated in the water tank, and the alkalinity of the mixed wastewater is improved, so that the buffer capacity of an anaerobic system in the UASB reaction cylinder is enhanced, and the habitat of microorganisms in a sludge bed is improved; at the same time, CO2C in the gas is used as a carbon source to enter a sludge bed, so that the anaerobic methane production capacity is improved.
Preferably, the pH of the wastewater in the water tank is adjusted to 8.0-8.35 by adjusting the reflux ratio of the reflux liquid.
Preferably, the ratio of methane in the methane entering the methane storage chamber is more than 90%.
Compared with the prior art, the invention has the following beneficial effects:
1) the invention utilizes NaOH solution to absorb CO in the biogas2Absorbing saturated NaHCO3The solution flows back to the UASB reactor to increase the alkalinity of inlet water and improve the buffer capacity of an anaerobic system, thereby ensuring the efficient and stable operation of the anaerobic biological treatment process, and simultaneously, the ratio of methane in the purified methane is more than 90 percent, which is beneficial to the resource utilization of the subsequent methane;
2) the invention absorbs CO in the biogas by using NaOH solution2Formation of NaHCO from the component3The solution is refluxed to a UASB reactor, so that the alkalinity of the wastewater is increased, the buffering capacity of an anaerobic system is improved, and the microbial habitat is improved, thereby realizing the high-efficiency stable decarbonization and yield of the high-concentration organic industrial wastewater and the high-quality recycling of methane;
3) CO in methane in anaerobic treatment process of industrial wastewater2The actual ratio is 25-50%, which seriously restricts the resource energy utilization of the methane; the invention uses NaOH and CO in the methane2Reaction to form NaHCO3The backflow to the anaerobic system can reduce the adding cost of wastewater treatment process reagents, is beneficial to obtaining high-purity methane which is directly utilized as energy substances, reduces the emission of greenhouse gases and realizes the resource energy regeneration of wastewater treatment.
Drawings
FIG. 1 is a schematic diagram of the structure of the apparatus of the present invention;
in the figure: the device comprises a water inlet pump 1, a water distribution plate 2, a sludge bed 3, a three-phase separator 4, an overflow weir 5, a water outlet 6, a UASB reaction cylinder 7, a water seal bottle 8, a gas flowmeter 9, a biogas collection chamber 10, a fan 11, an absorption device 12, an absorption liquid 13, an aeration head 14, a biogas storage chamber 15 and a water tank 16.
Detailed Description
The invention will be further elucidated and described with reference to the drawings and the detailed description. The technical features of the embodiments of the present invention can be combined correspondingly without mutual conflict.
As shown in figure 1, the method for absorbing CO by lye of the present invention2The device for reinforcing UASB process performance by backflow comprises a UASB reaction system and CO2A collection system and an alkali liquor reflux system, wherein, the UASB reaction system comprises an upflow anaerobic bioreactor and a water-sealed bottle 8, CO2The collecting system comprises a biogas collecting chamber 10, an absorbing device 12 and a biogas storage chamber 15, and the alkali liquor reflux system comprises a water tank 16.
The upflow anaerobic bioreactor comprises a UASB reaction cylinder 7, a water distribution plate 2, a sludge bed 3, a three-phase separator 4, an overflow weir 5 and a water outlet 6. The bottom of the UASB reaction cylinder 7 is provided with a water inlet which is communicated with a water tank 16 for storing wastewater to be treated through a water inlet pump 1 and is used for feeding water into the UASB reaction cylinder 7. The lower part in the UASB reaction cylinder 7 is provided with a water distribution plate 2 for uniformly distributing the wastewater entering the UASB reaction cylinder 7. The middle part in the UASB reaction cylinder 7 is a sludge bed 3 filled with activated sludge added with biomass carbon particles, which is the main treatment part of the UASB reaction system. The upper part in the UASB reaction cylinder 7 is provided with a three-phase separator 4, and the side wall of the cylinder above the three-phase separator 4 is provided with an overflow weir 5 and a water outlet 6. The included angle of the three-phase separator 4 is 55 degrees, the three-phase separator is used for separating sludge, gas and liquid, the sludge sinks again, the liquid is discharged from the overflow weir 5 on the side wall of the cylinder body 8 through the water outlet 7, and the gas (namely the methane) overflows from the top of the three-phase separator 4.
The top gas phase outlet of the three-phase separator 4 is connected with a water-sealed bottle 8, and the water-sealed bottle 8 is communicated with a biogas collecting chamber 10 through a gas flowmeter 9. Wherein, a water-sealed bottle 8 is arranged between the air outlet of the UASB reaction cylinder 7 and the biogas collection chamber 10 to prevent the biogas gas entering the biogas collection chamber 10 from flowing back and sucking back under the change of the air pressure. The gas flowmeter 9 is a wet gas flowmeter for measuring the flow rate of the biogas, thereby calculating the yield of the biogas. The biogas collection chamber 10 is communicated with the absorption device 12 through a fan 11, the fan 11 can adopt an explosion-proof variable frequency fan, and the air pressure in the biogas collection chamber (10) can be controlled by regulating and controlling the gas flow, so that the air pressure of a gas path is kept stable.
The absorption device 12 is used for containing alkaline absorption liquid 13 to absorb CO in the biogas2A gas. In this example, the absorbing liquid 13 was a 0.1mol/L NaOH solution to absorb CO2After-gas generation of NaHCO3And (3) solution. The air inlet pipe of the absorption device 12 extends into the barrel of the absorption device 12, in the embodiment, the height-diameter ratio of the absorption device 12 is 4:1, the tail end of the air inlet pipe is provided with a microporous aeration disc 14 made of ABS (acrylonitrile butadiene styrene) and used for dispersing methane to form tiny methane bubbles and reinforcing CO in the methane2And (4) absorbing. The upper part of the absorption device 12 is externally connected with a biogas storage chamber 15 through a gas pipeline, the lower part is provided with a liquid outlet, and the absorption device is communicated with a water tank 16 through a liquid outlet pipe and is used for refluxing the liquid part in the absorption device 12 to the water tank 16. The water tank 16 may be provided therein with a stirring device for uniformly mixing the reflux liquid returned from the absorption device 12 with the feed water. The biogas collection chamber 10, the absorption device 12 and the biogas storage chamber 15 are all closed vessels, and besides, the gas tightness of the gas passage should be ensured during the flowing process (i.e. the gas collection and absorption process) between the devices after the biogas is formed.
The device absorbs CO in the methane2And refluxing to enhance the UASB process performance, specifically as follows:
the wastewater in the water tank 16 is pumped into the UASB reaction cylinder 7 through the water inlet pump 1, water is uniformly distributed under the action of the water distribution plate 2, sludge, methane and liquid are separated in the three-phase separator 4 after being treated by the sludge bed 3, the sludge sinks again, the liquid is discharged from the water outlet 6 through the overflow weir 5 on the side wall of the cylinder, and the methane overflows from the top of the three-phase separator 4And (6) discharging. Biogas enters the biogas collection chamber 10 after passing through the water-sealed bottle 8, and the biogas flow is regulated and controlled by the fan 11 to control the air pressure in the biogas collection chamber 10 and maintain the air pressure in the gas path to be stable. Then the marsh gas is blown into an absorption device 12 under the action of a fan 11, and CO in the marsh gas is absorbed by absorption liquid 132Gas and converted to a weakly alkaline solution. CO removal2The biogas after being gas is introduced into the biogas storage chamber 15 from the gas pipeline at the upper part of the absorption device 12 for storage, so that the methane proportion in the biogas is increased, and the methane proportion is generally more than 90%. Absorption of CO2The absorption liquid 13 after gas partially flows back to the water tank 16 through a liquid outlet at the lower part of the absorption device 12, and is mixed with the wastewater to be treated in the water tank 16, and the pH value of the wastewater in the water tank 16 is 8.0-8.35 by adjusting the reflux ratio of the reflux liquid. The alkalinity of the mixed wastewater is improved, so that the buffering capacity of an anaerobic system in the UASB reaction cylinder 7 is enhanced, and the habitat of microorganisms in the sludge bed 3 is improved. At the same time, CO2C in the gas is used as a carbon source to enter the sludge bed 3, so that the anaerobic methane production capacity is improved.
The technical principle adopted by the invention can be summarized as follows:
absorbing CO by alkali liquor2The reflux can strengthen the high-efficiency stable operation of the anaerobic biological treatment system and the high-quality recycling of methane resource energy, and the reasons are that: (1) CO absorption by NaOH2The latter product is NaHCO3Saturated NaHCO3The pH value of the solution is 8.3, and the solution has no adverse effect on the pH environment of an anaerobic system after being mixed with wastewater; (2) when the system is overloaded, an imbalance between acid production and methane production can lead to acid accumulation, NaHCO3Reacting with hydrogen ions to play a buffering role, thereby improving the anaerobic microorganism habitat; (3) the bicarbonate as inorganic carbon is dissolved in the liquid phase, which can increase the reducing power of the anaerobic system and pull CO2Reduced methanogenesis proceeds, thereby enhancing anaerobic methanogenesis.
The invention absorbs CO in the biogas by NaOH solution2Formation of NaHCO3The solution flows back to the UASB reactor, so that the buffer capacity of an anaerobic system is improved, the anaerobic microbial habitat is improved, and CO is enhanced2The reduction type methane production function solves the problem of instability of acidification under the overload condition of the reactor.
The absorption of CO by the lye is explained below by means of specific examples on the basis of the apparatus according to the invention2And the effect of the reflow on the UASB process performance.
Example 1
This example constructed two sets of UASB process units, where the experimental set was different from the control set in that the UASB reactor was followed by a CO loop2An absorption system and an alkali liquor reflux system.
The effective volume of the UASB reactor in the device is 7.5L, the inoculated sludge is taken from anaerobic sludge of a Hainingtongqiao sewage treatment plant, the MLSS of the sludge is 27.52g/L, and the MLVSS is 12.67 g/L. The water inlet of the reactor is simulated waste water (cane sugar and NH)4HCO3、KH2PO4、K2HPO4·3H2O and NaHCO3The composition of the water-soluble polymer comprises C, N and P, wherein the ratio of C to N to P is 100:5:1), and the experimental group passes through and absorbs CO2Saturated NaHCO3Mixing the solution thoroughly, NaHCO3The concentration is 0.97-1.97 times of that of the control group. The pH of inlet water of the two groups of reactors is maintained at about 8.5, the reaction temperature is about 35 ℃, the hydraulic retention time is 24 hours, and the organic load of the inlet water is from 2kg COD/m3The/d is gradually increased to 6kg COD/m3And d, continuously monitoring the COD concentration of the effluent, the methane yield and the methane ratio for 60 days.
In the starting stage of the reactor, 6 days are needed when the COD removal rate of the experimental group reactor reaches more than 90 percent, and 12 days are needed for the control group, which shows that the alkali liquor absorbs CO2The reflux may accelerate UASB reactor start-up.
Along with the increase of the reactor load, the COD removal rate of the experimental group is gradually stabilized at 98.12 +/-1.20%, the biogas yield is stabilized at 3.48 +/-0.38L/kg COD/d, while the COD removal rate of the control group is reduced from 96.73 +/-0.45% to 81.56 +/-1.73%, and the biogas yield is reduced from 3.32 +/-0.42L/kg COD/d to 3.16 +/-0.41L/kg COD/d, which indicates that the alkali liquor absorbs CO2The reflux can maintain the stability of the anaerobic system and promote the generation of methane.
The concentration of methane at the air outlet of the experimental reactor reaches 59.78 +/-2.19 percent, which is higher than that of the control group by 48.16 +/-1.06 percent, which indicates that the alkali liquor absorbs CO2Can effectively strengthen CO2Reducing type methane production process. In addition, the fruitThe methane content in the purified methane in the experimental group is 92.36 +/-5.19%, and the subsequent high-quality resource utilization of methane is facilitated.
The above-described embodiments are merely preferred embodiments of the present invention, which should not be construed as limiting the invention. Various changes and modifications may be made by one of ordinary skill in the pertinent art without departing from the spirit and scope of the present invention. Therefore, the technical scheme obtained by adopting the mode of equivalent replacement or equivalent transformation is within the protection scope of the invention.
Claims (10)
1. Absorbing CO by alkali liquor2The device for reinforcing the UASB process performance by backflow is characterized by comprising a UASB reaction cylinder (7), a water-sealed bottle (8), a biogas collection chamber (10), an absorption device (12), a biogas storage chamber (15) and a water tank (16);
the bottom of the UASB reaction cylinder (7) is provided with a water inlet which is connected with a water tank (16) for storing wastewater to be treated through a water inlet pump (1); the lower part in the cylinder body is provided with a water distribution plate (2), the middle part is provided with a sludge bed (3), and the upper part is provided with a three-phase separator (4); an overflow weir (5) and a water outlet (6) are arranged on the side wall of the cylinder body above the three-phase separator (4); a gas phase outlet at the top end of the three-phase separator (4) is connected with a water-sealed bottle (8), the water-sealed bottle (8) is communicated with a methane collecting chamber (10) through a gas flowmeter (9), and the methane collecting chamber (10) is communicated with an absorption device (12) through a fan (11); the absorption device (12) is used for containing alkaline absorption liquid (13) to absorb CO in the biogas2A gas; the upper part of the absorption device (12) is externally connected with a biogas storage chamber (15) through a gas pipeline, the lower part of the absorption device is provided with a liquid outlet, and the absorption device is communicated with the water tank (16) through a liquid outlet pipe and is used for refluxing the liquid part in the absorption device (12) to the water tank (16); the biogas collection chamber (10), the absorption device (12) and the biogas storage chamber (15) are all closed containers.
2. The process of claim 1 wherein the lye absorbs CO2The device for enhancing the UASB process performance by backflow is characterized in that the gas flowmeter (9) is a wet gas flowmeter.
3. The process of claim 1 wherein the lye absorbs CO2The device for reinforcing UASB process performance by backflow is characterized in that the fan (11) is an explosion-proof variable frequency fan.
4. The process of claim 1 wherein the lye absorbs CO2The device for reinforcing UASB process performance by backflow is characterized in that an air inlet pipe of the absorption device (12) extends into a cylinder body of the absorption device (12), and a microporous aeration disc (14) is arranged at the tail end of the air inlet pipe.
5. The process of claim 4 wherein the lye absorbs CO2The device for reinforcing the UASB process performance by backflow is characterized in that the height-diameter ratio of the absorption device (12) is 4:1, and the microporous aeration disc (14) is made of ABS material.
6. The process of claim 1 wherein the lye absorbs CO2The device for reinforcing the technological performance of UASB by refluxing is characterized in that the absorption liquid (13) is 0.1mol/L NaOH solution and absorbs CO2After-gas generation of NaHCO3And (3) solution.
7. The process of claim 1 wherein the lye absorbs CO2The device for enhancing the UASB process performance by backflow is characterized in that a stirring device is arranged in the water tank (16) and used for uniformly mixing backflow liquid which flows back from the absorption device (12) with inlet water.
8. Device for absorbing CO in biogas based on any one of claims 1 to 72And refluxing to strengthen the UASB process performance, which is characterized in that:
waste water in a water tank (16) is pumped into a UASB reaction cylinder (7) through a water inlet pump (1), water is uniformly distributed under the action of a water distribution plate (2), sludge, methane and liquid are separated in a three-phase separator (4) after being treated by a sludge bed (3), the sludge sinks again, the liquid is discharged from a water outlet (6) through an overflow weir (5) on the side wall of the cylinder, and the methane overflows from the top of the three-phase separator (4); the marsh gas enters a marsh gas collecting chamber (10) after passing through a water-sealed bottle (8) and is regulated and controlled by a fan (11)The biogas flow is used for controlling the air pressure in the biogas collection chamber (10) and maintaining the air pressure of the gas path to be stable; then the marsh gas is blown into an absorption device (12) under the action of a fan (11), and CO in the marsh gas is absorbed by absorption liquid (13)2Converting the gas into a weakly alkaline solution; CO removal2The biogas after being gasified is introduced into a biogas storage chamber (15) from a gas pipeline at the upper part of the absorption device (12) for storage, so that the methane ratio in the biogas is increased; absorption of CO2The absorption liquid (13) after gas partially flows back into the water tank (16) through a liquid outlet at the lower part of the absorption device (12) and is mixed with the wastewater to be treated in the water tank (16), and the alkalinity of the mixed wastewater is improved, so that the buffer capacity of an anaerobic system in the UASB reaction cylinder (7) is enhanced, and the habitat of microorganisms in a sludge bed (3) is improved; at the same time, CO2C in the gas is used as a carbon source to enter the sludge bed (3), so that the anaerobic methanogenesis capability is improved.
9. Absorption of CO from biogas according to claim 82And refluxing to strengthen the UASB process performance, which is characterized in that the pH value of the wastewater in the water tank (16) is 8.0-8.35 by adjusting the reflux ratio of the reflux liquid.
10. Absorption of CO from biogas according to claim 82And reflowing to enhance the UASB process performance, which is characterized in that the methane ratio in the methane entering the methane storage chamber (15) is more than 90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011013149.5A CN112279369A (en) | 2020-09-24 | 2020-09-24 | Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011013149.5A CN112279369A (en) | 2020-09-24 | 2020-09-24 | Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112279369A true CN112279369A (en) | 2021-01-29 |
Family
ID=74422176
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011013149.5A Pending CN112279369A (en) | 2020-09-24 | 2020-09-24 | Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112279369A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113502210A (en) * | 2021-08-17 | 2021-10-15 | 天津农学院 | Carbon dioxide internal circulation biogas fermentation carbon reduction method |
| CN114590982A (en) * | 2022-03-03 | 2022-06-07 | 西安交通大学 | Continuous sludge anaerobic digestion gas collection and measurement system |
| KR102488904B1 (en) * | 2022-02-11 | 2023-01-17 | (주)인우코퍼레이션 | A bioreactor for capture and conversion of carbon dioxide |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0286899A (en) * | 1988-09-22 | 1990-03-27 | Kawasaki Heavy Ind Ltd | Treatment of sludge |
| JPH1177087A (en) * | 1997-09-05 | 1999-03-23 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for anaerobic biotreatment of organic waste water |
| WO2010014773A1 (en) * | 2008-07-31 | 2010-02-04 | Novozymes A/S | Modular reactor and process for carbon dioxide extraction |
| WO2010131234A1 (en) * | 2009-05-15 | 2010-11-18 | Bioenergia S.R.L. | Process for the biologic treatment of organic wastes and plant therefor |
| WO2011145956A1 (en) * | 2010-05-21 | 2011-11-24 | Lanzatech New Zealand Limited | Alcohol production process |
| CN102806226A (en) * | 2012-08-02 | 2012-12-05 | 上海交通大学 | Kitchen garbage treatment device and use method of kitchen garbage treatment device |
| WO2014104877A2 (en) * | 2012-12-24 | 2014-07-03 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
| CN104383804A (en) * | 2014-12-02 | 2015-03-04 | 华中农业大学 | CO2 absorption and storage utilization system and method adopting anaerobic fermentation biogas slurry as carrier |
| CN104496019A (en) * | 2014-12-23 | 2015-04-08 | 李开明 | Method for culturing granular sludge in anaerobic reactor |
| CN104587819A (en) * | 2015-01-06 | 2015-05-06 | 上海交通大学 | Fixing method of carbon dioxide in flue gas of municipal solid waste incinerator |
| CN208603834U (en) * | 2018-08-01 | 2019-03-15 | 苏伊士水务工程有限责任公司 | Resource utilization coal hydrogen production system CO2Chemical system for tail gas and fusel waste liquid |
| CN109970187A (en) * | 2019-03-21 | 2019-07-05 | 浙江大学 | A kind of devices and methods therefor adding biomass carbon particle strengthening UASB processing performance |
| CN110124488A (en) * | 2019-06-04 | 2019-08-16 | 北京赛科康仑环保科技有限公司 | One kind is administered for VOCs in biochemical treatment and tail gas recycles technique |
-
2020
- 2020-09-24 CN CN202011013149.5A patent/CN112279369A/en active Pending
Patent Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0286899A (en) * | 1988-09-22 | 1990-03-27 | Kawasaki Heavy Ind Ltd | Treatment of sludge |
| JPH1177087A (en) * | 1997-09-05 | 1999-03-23 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for anaerobic biotreatment of organic waste water |
| WO2010014773A1 (en) * | 2008-07-31 | 2010-02-04 | Novozymes A/S | Modular reactor and process for carbon dioxide extraction |
| WO2010131234A1 (en) * | 2009-05-15 | 2010-11-18 | Bioenergia S.R.L. | Process for the biologic treatment of organic wastes and plant therefor |
| CN102939143A (en) * | 2010-05-21 | 2013-02-20 | 新西兰郎泽科技公司 | Alcohol production process |
| WO2011145956A1 (en) * | 2010-05-21 | 2011-11-24 | Lanzatech New Zealand Limited | Alcohol production process |
| CN102806226A (en) * | 2012-08-02 | 2012-12-05 | 上海交通大学 | Kitchen garbage treatment device and use method of kitchen garbage treatment device |
| WO2014104877A2 (en) * | 2012-12-24 | 2014-07-03 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
| CN104383804A (en) * | 2014-12-02 | 2015-03-04 | 华中农业大学 | CO2 absorption and storage utilization system and method adopting anaerobic fermentation biogas slurry as carrier |
| CN104496019A (en) * | 2014-12-23 | 2015-04-08 | 李开明 | Method for culturing granular sludge in anaerobic reactor |
| CN104587819A (en) * | 2015-01-06 | 2015-05-06 | 上海交通大学 | Fixing method of carbon dioxide in flue gas of municipal solid waste incinerator |
| CN208603834U (en) * | 2018-08-01 | 2019-03-15 | 苏伊士水务工程有限责任公司 | Resource utilization coal hydrogen production system CO2Chemical system for tail gas and fusel waste liquid |
| CN109970187A (en) * | 2019-03-21 | 2019-07-05 | 浙江大学 | A kind of devices and methods therefor adding biomass carbon particle strengthening UASB processing performance |
| CN110124488A (en) * | 2019-06-04 | 2019-08-16 | 北京赛科康仑环保科技有限公司 | One kind is administered for VOCs in biochemical treatment and tail gas recycles technique |
Non-Patent Citations (6)
| Title |
|---|
| NGHIEM, NP等: "Capture of Carbon Dioxide from Ethanol Fermentation by Liquid Absorption for Use in Biological Production of Succinic Acid", 《APPLIED BIOCHEMISTRY AND BIOTECHNOLOGY》 * |
| SOHAIL, M 等: "Valorization of CO2 in flue gas through alkalinity production: Parametric optimization for application in anaerobic digesters", 《ENVIRONMENTAL TECHNOLOGY & INNOVATION》 * |
| 商体松等: "污泥厌氧发酵沼气产生规律研究", 《现代农业科技》 * |
| 肖裕秀: "二氧化碳联用石灰石接触池工艺改善水质化学稳定性研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅱ辑》 * |
| 费利华等: "厌氧膜生物反应器处理高浓度竹制品废水", 《浙江农业科学》 * |
| 韦斯利（WESLEY，W.）等: "《工业水污染控制》", 31 May 1991, 华东化工学院出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113502210A (en) * | 2021-08-17 | 2021-10-15 | 天津农学院 | Carbon dioxide internal circulation biogas fermentation carbon reduction method |
| KR102488904B1 (en) * | 2022-02-11 | 2023-01-17 | (주)인우코퍼레이션 | A bioreactor for capture and conversion of carbon dioxide |
| CN114590982A (en) * | 2022-03-03 | 2022-06-07 | 西安交通大学 | Continuous sludge anaerobic digestion gas collection and measurement system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100402448C (en) | Paper-making effluent purifying treatment process | |
| CN112279369A (en) | Absorbing CO by alkali liquor2Device and method for reinforcing UASB process performance by backflow | |
| CN102642985A (en) | Method and system for treatment and recycling of feces and waste from livestock and poultry culture | |
| CN107915320B (en) | Air-floating type half-short-cut nitrification-anaerobic ammonia oxidation reactor | |
| EP2558421A1 (en) | An anaerobic wastewater treatment system | |
| AU2017416198A1 (en) | Jet flow anaerobic bioreactor for treating high-concentration organic wastewater | |
| CN204454736U (en) | A kind of high efficiency anaerobic reactor | |
| CN201424414Y (en) | Self-circulation anaerobic reactor and sewage disposal device employing same | |
| CN105884152B (en) | IFBR-UASB-A/OBR handles wastewater from chemical industry group technology | |
| Aivasidis et al. | Biochemical reaction engineering and process development in anaerobic wastewater treatment | |
| CN103992015A (en) | Process for improving dewaterability of excess biochemical sludge | |
| CN115611489A (en) | Method for improving anaerobic digestion of sludge to produce methane by ultrasonic persulfate pretreatment | |
| CN212425812U (en) | Sewage treatment system for realizing material and energy recovery based on sulfur circulation | |
| CN106115918A (en) | Integration pillar high concentrated organic wastewater processor | |
| CN105884151A (en) | Method for treating industrial wastewater by novel combined process | |
| CN202246250U (en) | Anaerobic reactor capable of controlling mixing amount of methane | |
| CN107287249B (en) | Process and system for reinforcing organic waste recycling based on anaerobic ammonia oxidation coupling | |
| CN201372232Y (en) | Fully-automatic small anaerobic-aerobic sewage processing system | |
| CN205367880U (en) | Syllogic marsh gas reactor | |
| CN110697995A (en) | Cellulose ethanol wastewater treatment process and system | |
| CN204727726U (en) | A kind of pesticide wastewater biological treatment combination unit | |
| CN216445206U (en) | Urine extraction wastewater advanced treatment and nitrogen resource recovery system | |
| CN104071955A (en) | Sludge biochemical treatment system and method | |
| CN109867414A (en) | Using the integrated apparatus in Dynamic Membrane anaerobism MBR- positive infiltration technology processing mankind Heisui River | |
| JP7150899B6 (en) | Anaerobic treatment apparatus and anaerobic treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210129 |
|
| RJ01 | Rejection of invention patent application after publication |