CN112680326A - Method and system for improving yield and purity of anaerobic methane of organic solid waste - Google Patents
Method and system for improving yield and purity of anaerobic methane of organic solid waste Download PDFInfo
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- CN112680326A CN112680326A CN202110123311.7A CN202110123311A CN112680326A CN 112680326 A CN112680326 A CN 112680326A CN 202110123311 A CN202110123311 A CN 202110123311A CN 112680326 A CN112680326 A CN 112680326A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 334
- 239000002910 solid waste Substances 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000007062 hydrolysis Effects 0.000 claims abstract description 110
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- 238000004519 manufacturing process Methods 0.000 claims abstract description 73
- 239000002253 acid Substances 0.000 claims abstract description 69
- 238000000855 fermentation Methods 0.000 claims abstract description 44
- 238000005496 tempering Methods 0.000 claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 27
- 230000029087 digestion Effects 0.000 claims abstract description 26
- 230000014759 maintenance of location Effects 0.000 claims abstract description 21
- 238000003756 stirring Methods 0.000 claims description 50
- 239000002002 slurry Substances 0.000 claims description 45
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 230000000696 methanogenic effect Effects 0.000 claims description 21
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- 239000000047 product Substances 0.000 claims 2
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- 230000008569 process Effects 0.000 abstract description 18
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 74
- 239000001569 carbon dioxide Substances 0.000 description 37
- 229910002092 carbon dioxide Inorganic materials 0.000 description 37
- 239000001257 hydrogen Substances 0.000 description 31
- 229910052739 hydrogen Inorganic materials 0.000 description 31
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- 240000007594 Oryza sativa Species 0.000 description 1
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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
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- Processing Of Solid Wastes (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention relates to a method and a system for improving the yield and purity of anaerobic methane of organic solid waste, which comprises a slurrying and tempering tank and an anaerobic fermentation tank provided with an outer methane-producing tank and an inner hydrolysis and acid-producing tank, wherein the top of the inner hydrolysis and acid-producing tank is provided with an overflow weir and is communicated with the outer methane-producing tank, the organic solid waste after slurrying and tempering is pumped from the bottom of the inner hydrolysis and acid-producing tank for hydrolysis and acid-producing reaction, and a product of the hydrolysis and acid-producing is overflowed to the outer methane-producing tank from the overflow weir at the top of the inner hydrolysis and acid-producing tank for anaerobic methane production. Compared with the prior art, the method obviously improves the yield and purity of the anaerobic methane of the organic solid waste, reduces the retention time of the organic solid waste in the anaerobic digestion process, saves a large amount of energy consumption and cost for the operation of an anaerobic digestion system of the organic solid waste and the subsequent biogas purification, and promotes the resource utilization of the organic solid waste.
Description
Technical Field
The invention relates to a method for producing methane by organic solid waste in an anaerobic manner, in particular to a method and a system for improving the yield and purity of the anaerobic methane of the organic solid waste by controlling pressure intensity, belonging to the technical field of organic solid waste recycling.
Background
Organic solid waste generally refers to organic waste that is biochemically degradable, including but not limited to kitchen waste, organic components of municipal waste, excess sludge, crop straw, livestock manure, and the like. The organic solid waste is rich in organic matters, is easy to hydrolyze, contains a large amount of biomass energy, and is an important energy source in the solid waste. At present, the treatment means of organic solid wastes generally comprises landfill, incineration, aerobic fermentation, anaerobic digestion and the like. Because the biological methane potential of cow dung, kitchen garbage and excess sludge is respectively 3-6, 6-10, 10-15 and 15-30 billion cubic meters, the methane industrialization market prospect is huge, when fossil resources are exhausted and energy is in short, anaerobic digestion is carried out on organic solid waste to generate methane, and the methane production method has important significance for degrading organic solid waste, recycling biomass energy and realizing sustainable development of environment and economy.
However, the conventional anaerobic digestion of organic solid wastes faces the problems of slow reaction speed, low methane yield, low methane content (low purity) in the produced biogas, and the like. The anaerobic digestion time needs about 20 days, the methane content in the produced biogas is generally 50-70%, on one hand, the methane content is far away from the biogas standard (the methane content is more than 95%), on the other hand, most of carbon in the organic solid waste is converted into carbon dioxide, and the methane yield and the energy utilization rate of the organic solid waste are reduced. Therefore, the method has important significance for high-efficiency recycling of the organic solid waste by improving the yield and purity of anaerobic methane of the organic solid waste and improving the utilization rate of carbon.
At present, methods for improving the yield and purity of anaerobic methane of organic solid wastes include material component optimization, utilization of an electrochemical reactor, pretreatment and the like. Patent document CN110628828A discloses a method for optimizing material components to promote anaerobic digestion of perishable organic solid wastes to produce biogas, which mixes mature wastes and raw wastes in the perishable organic solid wastes in different proportions, and on the basis, adds rice straws to carry out material configuration, so as to promote anaerobic biogas production efficiency, and the maximum accumulated methane yield reaches 451ml/g VS; patent document CN111926045A discloses an electrochemical reactor and method for preparing methane by anaerobic fermentation of organic solid wastes, the method converts organic solid waste extract into easily degradable acetic acid and hydrogen ions by a special catalytic electrode under the action of voltage, and synthesizes hydrogen gas from the hydrogen ions on the surface of a cathode and reacts with carbon dioxide to generate methane, thereby improving the purity of methane in the produced methane; patent document CN107382003A discloses a sludge anaerobic digestion method based on combined pretreatment of thermal hydrolysis and chemical conditioning, which comprises adding alkali into sludge for pretreatment, adjusting to neutrality, performing thermal hydrolysis, and performing acid pretreatment, thereby increasing sludge anaerobic digestion gas production rate and increasing sludge anaerobic digestion gas production rate.
However, the above treatment process has the following disadvantages:
(1) anaerobic digestion is promoted to produce biogas by optimizing material components and the like, the principle is mainly that the carbon-nitrogen ratio of the materials and the pH value in a system are balanced, although the efficiency of methane production can be improved, the purity of methane in the biogas is not obviously improved, and the cost of subsequent biogas purification is still high;
(2) through the methods of thermal hydrolysis, chemical pretreatment and the like, although the hydrolysis and the methane rate enhancement can be promoted, the purity of methane in the methane cannot be obviously improved, the energy input is high, chemical agents need to be added, the process requirement is complex, and the overall process cost is high;
(3) the purity of methane in the methane can be obviously improved through the electrochemical method, and the cost of subsequent methane purification is reduced, however, the electrochemical method firstly needs electric energy input, and secondly, the electrodes have the problems of scaling, corrosion and the like, and the electron transfer efficiency is influenced, so that the regulation and control difficulty and the maintenance cost of long-term operation are increased for the whole process.
Disclosure of Invention
The invention aims to solve the problems of low methane purity, high energy input, complex process, difficult long-term operation and maintenance and the like in the methane in the prior art, and provides a process and a system for improving the yield and the purity of the anaerobic methane of the organic solid waste by controlling pressure, which can improve the yield and the purity of the anaerobic methane of the organic solid waste and save the cost of subsequent methane purification. The whole process has the characteristics of simple process, low energy input, high reaction speed and low operation and maintenance cost.
The purpose of the invention can be realized by the following technical scheme:
a system for improving the yield and purity of anaerobic methane of organic solid wastes by controlling pressure intensity comprises a slurrying and tempering tank, an anaerobic fermentation tank and a biogas residue and biogas slurry treatment system which are connected through pipelines, wherein a sludge inlet pump and a sludge outlet pump are arranged in the pipelines;
the pulping and tempering tank is stirring and mixing equipment, organic solid waste is added into the pulping and tempering tank, and the pulping and tempering are carried out on the organic solid waste through continuous stirring, acid addition for adjusting the pH value and water addition;
the anaerobic fermentation tank comprises an inner hydrolysis acidogenic tank and an outer methanogenic tank, the tops of the inner tank and the outer methanogenic tank are communicated, the pressure intensities are consistent, the inner tank is a stirring and mixing device, an overflow weir is arranged at the top, organic solid waste after slurrying and tempering is pumped from the bottom of the inner hydrolysis acidogenic tank, hydrolysis acidogenic reaction is carried out under the stirring effect, products of the hydrolysis acidogenic reaction overflow to the outer methanogenic tank from the overflow weir at the top of the inner tank, the outer methanogenic tank is provided with a high-pressure-resistant internal reflux stirring device, the liquid level of materials in the outer methanogenic tank is controlled to be always lower than that of the inner tank, and the materials are pumped from the bottom to obtain biogas residues after reaction;
the anaerobic fermentation tank is a high-pressure resistant device and is provided with a pressure gauge and a controllable exhaust valve, the exhaust valve is in a closed state during reaction until the pressure in the anaerobic fermentation tank reaches a first preset value, then the exhaust valve is opened to exhaust high-purity biogas until the pressure in the tank is reduced to a second preset value, and then the anaerobic fermentation tank is closed, and the operation is repeated.
The biogas residue and biogas slurry system is provided with a biogas residue dehydration unit, a biogas slurry alkali-adding deamination unit and a water treatment unit, wherein sludge cake and biogas slurry are obtained after dehydration of biogas residue, ammonia gas and deamination biogas slurry are obtained after adding alkali to a part of biogas slurry, the ammonia gas is introduced into an outer methane-producing tank, and the deamination biogas slurry and the other part of biogas slurry enter the water treatment unit for treatment.
In the invention, the inner hydrolysis acidogenic tank and the outer methanogenic tank are arranged for separating the hydrolysis acidogenic process from the methanogenic process, so as to independently enhance the hydrolysis acidogenic rate and the production rate of carbon dioxide and hydrogen, and the inner hydrolysis acidogenic tank is communicated with the outer methanogenic tank, thereby avoiding the loss of the carbon dioxide and the hydrogen produced in the hydrolysis acidogenic process in the material pipeline conveying process, providing a substrate for the carbon dioxide and the hydrogen to be converted into methane under the action of hydrogen-utilizing methanogenic bacteria and accelerating the efficiency. The height ratio, the inner diameter ratio and the effective volume ratio of the hydrolysis acidogenic inner tank and the methanogenic outer tank influence the volume utilization rate of the anaerobic fermentation tank in the operation process and the possibility of communicating the liquid levels of the inner tank and the outer tank, if the effective volume ratio of the inner tank and the outer tank is too small, the volume utilization rate of the anaerobic fermentation tank and the treatment efficiency of organic solid wastes are reduced, and if the ratio is too large, the liquid levels of the inner tank and the outer tank are easily communicated, and the effect of separate reaction of the inner tank and the outer tank is lost. The effective volume ratio of the gas storage area and the liquid phase reaction area in the anaerobic fermentation tank influences the smooth discharging degree of the methane, the pressure intensity in the system and the operation stability degree, the volume utilization rate of the anaerobic fermentation tank and the treatment efficiency of organic solid wastes are reduced when the ratio is too high, and the space for storing the gas is too small when the ratio is too low, so that the methane is not beneficial to storing.
Preferably, the effective volume ratio of the pulping conditioning tank to the hydrolysis acid production inner tank is 1: 1-2: 1.
Preferably, the height ratio of the hydrolysis acidogenesis inner tank to the methanogenesis outer tank is 1: 3-2: 3, the inner diameter ratio is 1: 3-1: 2, and the effective volume ratio is 1: 8-1: 2.
Preferably, the effective volume ratio of the gas storage area to the liquid phase reaction area in the anaerobic fermentation tank is 1: 1-2: 1.
Preferably, the pressure resistance range of the anaerobic fermentation tank and the internal reflux stirring device is 4-6 bar.
Preferably, the pressure value of the first preset value is 2-3 bar, and the pressure value of the second preset value is 1.2-1.5 bar.
A method for improving the yield and purity of anaerobic methane of organic solid wastes by controlling pressure is based on the system for processing, and specifically comprises the following steps:
s1, adding the organic solid waste into a slurrying and tempering tank, adjusting the water content and the pH value of the slurry, and uniformly stirring;
s2, pumping the pulped and modified organic solid waste into a hydrolysis acidogenic inner tank of an anaerobic fermentation tank, and carrying out anaerobic hydrolysis acidogenic in the hydrolysis acidogenic inner tank;
and S3, overflowing the product after hydrolysis and acidogenesis from the top of the hydrolysis and acidogenesis inner tank to the methane production outer tank for anaerobic methane production, communicating the hydrolysis and acidogenesis inner tank with the top of the methane production outer tank, keeping the pressure in the inner tank and the pressure in the outer tank consistent, controlling the liquid level of the outer tank to be lower than that of the inner tank all the time, exhausting when the pressure in the anaerobic fermentation tank rises to 2-3 bar, stopping exhausting until the pressure drops to 1.2-1.5 bar, and obtaining biogas residues and high-purity biogas after the reaction.
And S4, dehydrating the biogas residues obtained in the step S3 to obtain biogas slurry and mud cakes, directly allowing a part of the biogas slurry to enter a water treatment link, adding alkali to a part of the biogas slurry to adjust the pH value to 9.5-10 so as to overflow ammonia gas, allowing the obtained deamination biogas slurry to enter a water treatment step, and introducing the ammonia gas into a methane-producing outer tank of an anaerobic fermentation tank.
The working principle of the invention is as follows:
the organic solid waste after slurrying and tempering has high fluidity, and is pumped into a hydrolysis acid-producing inner tank to carry out anaerobic hydrolysis acid production, and a large amount of organic acid, hydrogen and carbon dioxide are produced under the action of hydrolysis acid-producing bacteria. In the continuous operation process, when the amount of the added organic solid waste exceeds the volume of the hydrolysis acidogenic, the product of the hydrolysis acidogenic overflows to an outer methanogenic tank, and methanogenic bacteria produce methane by using organic acid, hydrogen and carbon dioxide. The top of the hydrolysis acidogenic inner tank is communicated with the top of the methanogenic outer tank, so that organic acid, hydrogen and carbon dioxide generated in the hydrolysis acidogenic stage can be fully utilized in the next stage, and particularly, the hydrogen and the carbon dioxide are difficult to obtain synchronously conveyed gas when products are conveyed through a pipeline. The anaerobic fermentation tank is exhausted when the pressure in the anaerobic fermentation tank rises to 2-3 bar, on one hand, the reaction rate can be accelerated by improving the system pressure, the rate of hydrolyzing acid and producing methane of organic matters is improved, on the other hand, hydrogen and carbon dioxide generated in the hydrolyzing acid production process and carbon dioxide generated in the acetic acid utilization type methane production process are greatly dissolved in a liquid phase, the hydrogen partial pressure in the system is improved, the carbon dioxide and the hydrogen dissolved in the liquid phase are converted into methane by utilizing the hydrogen utilization type methane producing bacteria, the content of the carbon dioxide in the produced methane is reduced, and the methane purity is improved. Controlling the temperature of materials in an inner hydrolysis acid-producing tank to be 40-45 ℃, and carrying out hydrolysis acid-producing reaction at a higher temperature, so as to accelerate the hydrolysis and acid production of organic solid wastes and the generation and release of carbon dioxide and hydrogen, improve the amount of organic acid, carbon dioxide and hydrogen entering an outer methane-producing tank, and inhibit the methane-producing process at the stage; the temperature in the methane production outer tank is controlled to be 15-25 ℃, on one hand, the system has higher reaction rate under the high-pressure condition, the condition of maintaining the conventional anaerobic digestion at 37 ℃ is not needed to be heated, on the other hand, the lower temperature can improve the solubility of carbon dioxide and hydrogen in liquid, so that the carbon dioxide and hydrogen are dissolved in liquid phase as far as possible under the high-pressure condition, methane is produced under the action of hydrogen-utilizing methanogens, and the utilization rate of carbon dioxide and the purity of methane are further improved. Retrieve some ammonia nitrogen in the natural pond liquid and lead to the methane production outer tank that returns anaerobic fermentation jar for the ammonia gas, can further improve the pH value of outer jar interior liquid on the one hand, reinforcing carbon dioxide solubility and solubility in the outer jar, improve the efficiency that carbon dioxide turned into methane.
Preferably, in step S1, the organic solid waste is any one or a combination of kitchen waste, organic components of municipal waste, excess sludge, crop straws and livestock and poultry manure, the mass ratio (VS/TS) of volatile solids to total solids is 40-90%, the water content is adjusted to 95-90%, and the pH value is adjusted to 5-6.
Preferably, in step S1, the stirring manner is continuous mechanical stirring, and the stirring speed is 50 to 100 r/min.
Preferably, in step S2, the organic solid waste is pumped into the hydrolysis acidification inner tank of the anaerobic digestion tank intermittently from the bottom of the inner tank 1 time per day, and the volume of the organic solid waste is 1/2-1 of the effective volume of the inner tank each time, so that the retention time of the organic solid waste in the hydrolysis acidification inner tank is 1-2 days.
Preferably, in step S2, the temperature of the material in the hydrolysis acidification inner tank is 40 to 45 ℃, the stirring mode of the inner tank is continuous mechanical stirring, and the stirring speed is 50 to 100 r/min.
Preferably, in the step S3, the temperature of the materials in the methane-producing outer tank is 15-25 ℃, the stirring mode of the outer tank is continuous inner reflux stirring of the materials, and the total volume of the reflux materials per day is 1-2 times of the effective volume of the outer tank.
Preferably, in step S3, the anaerobic fermentation tank is operated intermittently, the pressure in the system is formed by gas generated by anaerobic reaction of the materials, the exhaust valve is opened when the pressure is increased to 2 to 3bar, and the exhaust valve is closed when the pressure is reduced to 1.2 to 1.5 bar.
Preferably, in step S3, the pumping-out of the biogas residue from the bottom of the methane-producing outer tank is performed intermittently for 1 time per day, and after certain exhaust in the day, 1/2-1/5 with the volume of the effective volume of the outer tank is pumped out every time, so that the retention time of the organic solid waste in the methane-producing outer tank is 2-5 days.
Preferably, in the step S3, the VS degradation rate of the biogas residues is 50-80%, and the volume ratio of methane in the high-purity biogas is 80-90%.
Preferably, in the step S4, the biogas slurry for adding alkali accounts for 5-10% of the total volume of the biogas slurry.
In the invention, the purpose of adjusting the water content of the organic solid waste and stirring in the step S1 is to mix the organic solid waste uniformly, reduce the viscosity of the organic solid waste and increase the water content in the system, too high stirring speed will accelerate the abrasion of the stirring paddle and increase the operation cost, too low stirring speed cannot mix the organic solid waste uniformly and reduce the viscosity thereof effectively, so that the subsequent stability of the system is affected; the purpose of adjusting the pH value to be acidic is to accelerate the hydrolysis and acid production of the organic solid waste, the hydrolysis and acid production cannot be enhanced if the pH value is too high, and the activity of hydrolysis and acid production bacteria in the system is affected if the pH value is too low. Therefore, the water content of the organic solid waste in the slurrying tempering tank is controlled to be 95-90%, the stirring speed is 50-100 r/min, and the pH value is 5-6.
In the invention, the retention time of the organic solid waste in the hydrolysis acid-production inner tank in the step S2 is an important parameter influencing the hydrolysis acid-production efficiency, if the retention time is too long, the treatment efficiency of the organic solid waste is reduced, the operation cost is increased, and if the retention time is too short, the organic solid waste cannot be effectively hydrolyzed to produce acid; the purpose of increasing the temperature of the hydrolysis acid-producing inner tank is to accelerate the hydrolysis acid-producing efficiency and the release of carbon dioxide and hydrogen, the activity of hydrolysis acid-producing bacteria is affected when the temperature is too high, and the hydrolysis acid-producing efficiency cannot be effectively promoted when the temperature is too low; the purpose of stirring in the hydrolysis acid-producing inner tank is to promote the contact and mixing of hydrolysis acid-producing bacteria and organic solid wastes, improve the reaction rate and facilitate the release of carbon dioxide and hydrogen, the over-high stirring rate can accelerate the abrasion of the stirring paddle and increase the operation cost, and the over-low stirring rate can not be used for uniformly mixing to strengthen the utilization of the hydrolysis acid-producing bacteria and the organic solid wastes and also can influence the release of the carbon dioxide and the hydrogen. Therefore, the method for controlling the organic solid waste to be pumped into the hydrolysis acidification inner tank of the anaerobic digestion tank is intermittent pumping for 1 time every day, wherein the pumping volume is 1/2-1 of the effective volume of the inner tank each time, so that the retention time of the organic solid waste in the hydrolysis acidification inner tank is 1-2 days, the temperature of materials in the hydrolysis acidification inner tank is 40-45 ℃, and the continuous mechanical stirring speed of the inner tank is 50-100 r/min.
In the invention, the retention time of the product after hydrolysis and acid production in the methane production outer tank in the step S3 is a key parameter influencing the methane production, the treatment efficiency of the product after hydrolysis and acid production can be reduced and the operation cost can be improved if the retention time is too long, and the product after hydrolysis and acid production can not be effectively methane produced if the retention time is too short; the purpose of reducing the temperature in the outer methanogenic tank is to improve the solubility of carbon dioxide and hydrogen in the liquid phase of the outer methanogenic tank and strengthen the utilization of methanogenic bacteria, the purpose cannot be achieved when the temperature is too high, and the activity of the methanogenic bacteria is influenced when the temperature is too low; the stirring mode of continuous internal reflux is adopted to uniformly stir the materials in the inner tank, the efficiency of the upper gas entering the liquid phase through the liquid surface is enhanced, the influence of foam generated by methane stirring and other modes on the speed of dissolving carbon dioxide and hydrogen in the liquid phase is avoided, the use degree of an internal reflux pump is improved and the operation cost is improved if the total volume of the reflux materials is too high every day, and a good stirring function cannot be realized if the total volume of the reflux materials is too low; the purpose of improving the pressure in the anaerobic reaction tank is to improve the reaction rate in the system, improve the solubility of carbon dioxide and hydrogen produced in the hydrolysis acidogenesis stage and carbon dioxide produced in the acetic acid utilization methanogenesis stage in the methane production outer tank, so that the carbon dioxide and the hydrogen are converted into methane as much as possible under the action of the hydrogen utilization methanogens, improve the methane production efficiency, improve the purity of the methane in the methane, provide higher requirements for the control and operation of equipment due to overhigh pressure, have better operation and maintenance costs, and cannot effectively improve the methane production efficiency and the purity of the methane in the methane due to overlow pressure. Therefore, the temperature of the materials in the methane production outer tank is controlled to be 15-25 ℃, the total volume of the backflow materials every day is 1-2 times of the effective volume of the outer tank when the outer tank is continuously subjected to inner backflow stirring, the exhaust valve is opened when the pressure of the anaerobic fermentation tank is increased to 2-3 bar, the exhaust valve is closed when the methane is discharged until the pressure is reduced to 1.2-1.5 bar, the pumping-out mode of the biogas residues from the methane production outer tank is 1 time every day, and 1/2-1/5 with the volume being the effective volume of the outer tank is pumped out every time after certain exhaust in the day, so that the retention time of the organic solid wastes in the methane production outer tank is 2-5 days, the VS degradation rate of the biogas residues obtained after the reaction is 50-80%, and the volume ratio of methane in high-purity methane is 80-90%.
In the step S4, the ratio of the alkali-added biogas slurry to the total volume of the biogas slurry affects the reaction in the outer methanogenic tank, when the ratio is too high, the ammonia nitrogen concentration in the methanogenic phase is too high to inhibit the activity of methanogens, thereby affecting the production of methane, and when the ratio is too low, the pH value in the outer methanogenic tank cannot be effectively increased, thereby increasing the solubility and the solubility of carbon dioxide. Therefore, the biogas slurry for adding alkali is controlled to account for 5-10% of the total volume of the biogas slurry.
The innovation points of the invention are mainly as follows:
(1) the existing methods for enhancing the yield of methane, such as optimizing material components, performing physical, chemical, biological and treatment on materials and the like close to a tank, can improve the methane production efficiency, but are difficult to improve the purity of methane, so that the cost of subsequent methane purification is high, the energy input of a pretreatment mode is high, and the overall process cost is high; although the electrochemical method can obviously improve the purity of methane in the biogas and reduce the cost of biogas purification, the energy input is high, and electrodes are easy to scale and corrode, so that the strengthening efficiency is influenced, and the regulation difficulty and the maintenance cost are increased. The invention adopts high-pressure anaerobic digestion, and under the action of automatic pressurization of the system due to gas production by material reaction, the system is kept in a high-pressure environment, the solubility and the dissolution rate of carbon dioxide and hydrogen in a liquid phase are increased, the methane is promoted to be produced by utilizing methane-producing bacteria by utilizing hydrogen, the carbon dioxide is promoted to be converted into methane, the content of carbon dioxide in methane is reduced, and the purity of the methane is promoted; meanwhile, the reaction power of the system is greatly enhanced under the high-pressure condition, and the rate of producing methane by hydrolyzing acid and producing methane of the organic solid waste is greatly improved.
(2) The existing two-phase anaerobic digestion system mostly utilizes an external source to control the temperature of two-phase reaction to be consistent, which is a conventional method for two-phase anaerobic digestion. The method adopts two phases to respectively adjust the temperature and the pH value, controls the conditions of high temperature and low pH value of the hydrolysis acid-producing phase and low temperature and high pH value of the methane-producing phase, can lead the system to accelerate the reaction rate of hydrolysis acid-producing and release of carbon dioxide and hydrogen from the phase under the conditions of high pressure and high temperature and low pH value, greatly improves the solubility and the dissolution rate of the carbon dioxide and the hydrogen in the liquid phase under the conditions of low temperature and high pH value, further promotes the carbon dioxide and the hydrogen to be converted into the methane, and achieves the aim of simultaneously improving the yield and the purity of the methane.
Compared with the prior art, the invention has the following advantages:
(1) the traditional anaerobic digestion residence time of the organic solid waste needs 15-20 days, and the method and the system adopting two-phase temperature regulation and high-pressure control can reduce the overall anaerobic digestion residence time of the organic solid waste to 3-7 days, wherein the hydrolysis produces acid for 1-2 days, and the methane production is carried out for 2-5 days, so that the anaerobic digestion efficiency and the methane production efficiency are greatly improved.
(2) According to the invention, the high-pressure anaerobic digestion method and the high-pressure anaerobic digestion system are adopted, under the condition that the pressure is naturally formed by the gas production of the system, no extra energy is added, the carbon dioxide and the hydrogen are promoted to be dissolved in the liquid phase and converted into the methane, the volume ratio of the methane in the methane can reach 80-90%, and the purity of the methane is greatly improved.
(3) By combining the advantages, the invention reduces the retention time of the organic solid waste in the system on the premise of lower energy consumption and cost, improves the methane yield and purity of anaerobic digestion of the organic solid waste, saves a large amount of cost for subsequent purification of methane, and can effectively promote the resource utilization of the organic solid waste.
Drawings
FIG. 1 is a block diagram of the process flow of the present invention.
Detailed Description
The present invention will be described in detail with reference to specific examples.
Example 1:
a method and a system for improving the yield and purity of anaerobic methane of organic solid wastes by controlling pressure intensity are disclosed, as shown in figure 1, and comprise a slurrying and tempering tank, an anaerobic fermentation tank and a biogas residue and biogas slurry treatment system, and the method comprises the following steps:
(1) adding residual sludge with VS/TS of 40% into a slurrying and tempering tank, adjusting the water content of the residual sludge to 95%, adjusting the pH value to 6, and stirring at the speed of 50 r/min.
(2) Pumping the organic solid waste subjected to slurrying and tempering into a hydrolysis acid production inner tank of an anaerobic fermentation tank, carrying out anaerobic hydrolysis acid production in the hydrolysis acid production inner tank, wherein the effective volume ratio of the slurrying and tempering tank to the hydrolysis acid production inner tank is 1:1, the volume of the organic solid waste pumped each time is 1/2 of the effective volume of the inner tank, the retention time of the organic solid waste in the hydrolysis acidification tank is 2 days, the temperature of materials in the hydrolysis acidification tank is 40 ℃, and the continuous stirring speed of the inner tank is 50 r/min.
(3) The product after hydrolysis and acid production overflows to an outer methane-producing tank from the top of an inner hydrolysis and acid-producing tank for anaerobic methane production, the inner hydrolysis and acid-producing tank is communicated with the top of the outer methane-producing tank, the pressure intensity in the inner tank and the outer tank is consistent, the pressure resistance of an anaerobic fermentation tank and an inner reflux stirring device is 4bar, the height ratio of the inner hydrolysis and acid-producing tank to the outer methane-producing tank is 1:3, the inner diameter ratio is 1:3, the effective volume ratio is 1:8, the liquid level of the outer tank is controlled to be always lower than that of the inner tank, the material temperature of the inner tank is 15 ℃, the total volume of the reflux material during reflux stirring in the inner tank is 1 time of the effective volume of the outer tank, the gas is discharged when the pressure intensity in the anaerobic fermentation tank is increased to 2bar, the gas is stopped to be discharged until the pressure intensity is reduced to 1.2bar, high-purity methane and biogas residues are obtained, the biogas residues are pumped out from the bottom, the retention time of the organic solid waste in the methane production outer tank is 5 days;
(4) dehydrating the obtained biogas residues to obtain biogas slurry and mud cakes, directly enabling 95% of the volume of the obtained biogas slurry to enter a water treatment link, adjusting the pH value to 10 by adding alkali to enable ammonia gas to overflow, enabling the obtained deamination biogas slurry to enter the water treatment link, and enabling the ammonia gas to return to a methane production outer tank of an anaerobic fermentation tank.
(5) By the method and the system, the VS degradation rate of the obtained biogas residues is 50%, and the volume of methane in the high-purity biogas accounts for 80%.
Example 2:
a method and a system for improving the yield and purity of anaerobic methane of organic solid wastes by controlling pressure intensity are disclosed, as shown in figure 1, and comprise a slurrying and tempering tank, an anaerobic fermentation tank and a biogas residue and biogas slurry treatment system, and the method comprises the following steps:
(1) adding the kitchen waste with the VS/TS of 80% into a slurrying and tempering tank, adjusting the water content of the kitchen waste to 92%, adjusting the pH value to 5, and adjusting the stirring speed to 100 r/min.
(2) Pumping the organic solid waste subjected to slurrying and tempering into a hydrolysis acid production inner tank of an anaerobic fermentation tank, carrying out anaerobic hydrolysis acid production in the hydrolysis acid production inner tank, wherein the effective volume ratio of the slurrying and tempering tank to the hydrolysis acid production inner tank is 2:1, the volume of the organic solid waste pumped each time is 1/1 of the effective volume of the inner tank, the retention time of the organic solid waste in the hydrolysis acidification tank is 1 day, the temperature of materials in the hydrolysis acidification tank is 45 ℃, and the continuous stirring speed of the inner tank is 100 r/min.
(3) The product after hydrolysis and acid production overflows to an outer methane-producing tank from the top of an inner hydrolysis and acid-producing tank for anaerobic methane production, the inner hydrolysis and acid-producing tank is communicated with the top of the outer methane-producing tank, the pressure intensity in the inner tank and the outer tank is consistent, the pressure resistance of an anaerobic fermentation tank and an inner reflux stirring device is 6bar, the height ratio of the inner hydrolysis and acid-producing tank to the outer methane-producing tank is 2:3, the inner diameter ratio is 1:2, the effective volume ratio is 1:2, the liquid level of the outer tank is controlled to be always lower than that of the inner tank, the material temperature of the inner tank is 25 ℃, the total volume of the reflux material during reflux stirring in the inner tank is 1 time of the effective volume of the outer tank, the gas is discharged when the pressure intensity in the anaerobic fermentation tank is increased to 3bar, the gas is stopped to be discharged until the pressure intensity is reduced to 1.5bar, high-purity methane and biogas residues are obtained, the biogas residues are pumped out from the bottom, the retention time of the organic solid waste in the methane production outer tank is 2 days;
(4) dehydrating the obtained biogas residues to obtain biogas slurry and mud cakes, directly enabling 90% of the volume of the obtained biogas slurry to enter a water treatment link, adjusting the pH value to 9.5 by adding alkali to enable ammonia gas to overflow, enabling the obtained deamination biogas slurry to enter the water treatment link, and enabling the ammonia gas to return to a methane production outer tank of an anaerobic fermentation tank.
(5) By the method and the system, the VS degradation rate of the obtained biogas residues is 80%, and the volume of methane in the high-purity biogas accounts for 90%.
Example 3:
a method and a system for improving the yield and purity of anaerobic methane of organic solid wastes by controlling pressure intensity are disclosed, as shown in figure 1, and comprise a slurrying and tempering tank, an anaerobic fermentation tank and a biogas residue and biogas slurry treatment system, and the method comprises the following steps:
(1) adding the mixture of the excess sludge with the VS/TS of 60 percent and the livestock and poultry manure into a slurrying and tempering tank, adjusting the water content of the mixture to 90 percent, adjusting the pH value to 5 and stirring at the speed of 80 r/min.
(2) Pumping the organic solid waste subjected to slurrying and tempering into a hydrolysis acid production inner tank of an anaerobic fermentation tank, carrying out anaerobic hydrolysis acid production in the hydrolysis acid production inner tank, wherein the effective volume ratio of the slurrying and tempering tank to the hydrolysis acid production inner tank is 2:1, the volume of the organic solid waste pumped each time is 1/1 of the effective volume of the inner tank, the retention time of the organic solid waste in the hydrolysis acidification tank is 1 day, the temperature of materials in the hydrolysis acidification tank is 42 ℃, and the continuous stirring speed of the inner tank is 80 r/min.
(3) The product after hydrolysis and acid production overflows to an outer methane-producing tank from the top of an inner hydrolysis and acid-producing tank, anaerobic methane production is carried out, the inner hydrolysis and acid-producing tank is communicated with the top of the outer methane-producing tank, the pressure intensity in the inner tank and the outer tank is consistent, the pressure resistance of an anaerobic fermentation tank and an inner reflux stirring device is 5bar, the height ratio of the inner hydrolysis and acid-producing tank to the outer methane-producing tank is 2:3, the inner diameter ratio is 1:2, the effective volume ratio is 1:2, the liquid level of the outer tank is controlled to be always lower than that of the inner tank, the temperature of materials in the inner tank is 22 ℃, the total volume of the reflux materials during reflux stirring in the inner tank is 1 time of the effective volume of the outer tank, the anaerobic fermentation tank is exhausted when the pressure intensity in the inner tank is increased to 2.5bar until the pressure intensity is reduced to 1.2bar, high-purity methane and biogas residues are obtained, the biogas residues are pumped out from the bottom of the outer, the retention time of the organic solid waste in the methane production outer tank is 4 days;
(4) dehydrating the obtained biogas residues to obtain biogas slurry and mud cakes, directly enabling 92% of the volume of the obtained biogas slurry to enter a water treatment link, adjusting the pH value to 10 by adding alkali to enable ammonia gas to overflow, enabling the obtained deamination biogas slurry to enter the water treatment link, and enabling the ammonia gas to return to a methane production outer tank of an anaerobic fermentation tank.
(5) By the method and the system, the VS degradation rate of the obtained biogas residues is 70%, and the volume of methane in the high-purity biogas accounts for 85%.
Comparative example 1:
compared with the embodiment 1, the anaerobic digestion tank is in a continuous exhaust and non-pressurization state, the rest conditions are the same, and as a result, the system is crashed due to the fact that the retention time of materials in the anaerobic digestion tank is too short, the degradation rate of biogas residues before collapse is less than 20%, and methane in the produced biogas accounts for 55%. This indicates that pressure control has a large impact on material degradation, methane yield and purity within the system.
Comparative example 2:
compared with the embodiment 2, the temperature of the hydrolysis acidogenic inner tank and the temperature of the hydrolysis acidogenic outer methane are controlled to be 35-37 ℃ in the conventional way, the other conditions are the same, the degradation rate of the obtained biogas residues is 60%, and the temperature in the outer methane-producing tank influences the solubility of carbon dioxide, so that the methane in the obtained biogas accounts for 70%. This indicates that temperature control of the two-phase system has a large impact on the material degradation and methane purity within the system.
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (10)
1. A system for increasing anaerobic methane yield and purity of organic solid waste, the system comprising:
the slurrying tempering tank is stirring and mixing equipment and is used for slurrying and tempering the added organic solid waste;
the anaerobic fermentation tank comprises an outer methane-producing tank and an inner hydrolysis acid-producing tank arranged in the outer methane-producing tank, the inner hydrolysis acid-producing tank is a stirring and mixing device, an overflow weir is arranged at the top and is communicated with the outer methane-producing tank, organic solid waste after slurrying and tempering is pumped from the bottom of the inner hydrolysis acid-producing tank to perform hydrolysis acid-producing reaction, and a product of hydrolysis acid-producing is overflowed to the outer methane-producing tank through the overflow weir at the top of the inner hydrolysis acid-producing tank;
the internal reflux stirring device is arranged outside the methane production outer tank and used for controlling the liquid level of the materials in the methane production outer tank to be always lower than that of the hydrolysis acid production inner tank; and
and the biogas residue and biogas slurry treatment system is arranged outside the methane production outer tank and used for treating biogas residues pumped out from the bottom after the reaction of the methane production outer tank.
2. The system for improving the anaerobic methane yield and purity of organic solid wastes according to claim 1, wherein the outlet of the slurrying and tempering tank is connected with the bottom of the hydrolysis acidogenic inner tank through a pipeline, a sludge inlet pump is arranged in the pipeline, and a sludge outlet pump is arranged between the outside of the methanogenic outer tank and the biogas residue and liquid treatment system.
3. The system for improving anaerobic methane yield and purity of organic solid waste according to claim 1, wherein said anaerobic fermentation tank is provided with a pressure gauge and a controllable exhaust valve, said exhaust valve is closed during the reaction until the pressure in the anaerobic fermentation tank reaches a first predetermined value, then the exhaust valve is opened to discharge high purity methane until the pressure in the tank is reduced to a second predetermined value, and then the operation is closed, and the operation is repeated.
4. The system for improving the yield and purity of anaerobic methane of organic solid wastes according to claim 3, wherein the pressure resistance of the anaerobic fermentation tank and the internal reflux stirring device is in the range of 4-6 bar, the pressure of the first preset value is in the range of 2-3 bar, and the pressure of the second preset value is in the range of 1.2-1.5 bar.
5. The system for improving the yield and the purity of anaerobic methane of organic solid wastes according to claim 1, wherein the biogas residue and biogas slurry treatment system is provided with a biogas residue dehydration unit, a biogas slurry alkali-adding deamination unit and a water treatment unit, sludge and biogas slurry are obtained after dehydration of biogas residues, ammonia gas and deamination biogas slurry are obtained after deamination of a part of biogas slurry after alkali addition, ammonia gas is introduced into the methane production outer tank, and deamination biogas slurry and another part of biogas slurry enter the water treatment unit for treatment.
6. The system for improving the yield and the purity of the anaerobic methane of the organic solid waste according to claim 1, wherein the effective volume ratio of the slurrying and tempering tank to the hydrolysis and acidogenesis inner tank is 1: 1-2: 1, the height ratio of the hydrolysis and acidogenesis inner tank to the methanogenesis outer tank is 1: 3-2: 3, the inner diameter ratio is 1: 3-1: 2, the effective volume ratio is 1: 8-1: 2, and the effective volume ratio of a gas storage area to a liquid phase reaction area in the anaerobic fermentation tank is 1: 1-2: 1.
7. A method for increasing anaerobic methane yield and purity of organic solid waste, characterized in that the organic solid waste is treated by the system according to any one of claims 1-6, comprising the steps of:
s1, adding the organic solid waste into a slurrying and tempering tank, adjusting the water content and the pH value, and uniformly stirring;
s2, pumping the pulped and modified organic solid waste into a hydrolysis acid-producing inner tank, and carrying out anaerobic hydrolysis acid production in the hydrolysis acid-producing inner tank;
s3, overflowing the product after hydrolysis and acidogenesis from the top of the hydrolysis and acidogenesis inner tank to the methane production outer tank for anaerobic methane production, exhausting when the pressure in the anaerobic fermentation tank is increased to 2-3 bar, and stopping exhausting when the pressure is reduced to 1.2-1.5 bar, so as to obtain biogas residue and high-purity biogas after the reaction;
and S4, dehydrating the biogas residues obtained in the step S3 to obtain biogas slurry and mud cakes, directly allowing a part of the biogas slurry to enter a water treatment link, adding alkali to a part of the biogas slurry to adjust the pH value to 9.5-10 so as to overflow ammonia gas, allowing the obtained deamination biogas slurry to enter the water treatment link, and introducing the ammonia gas into a methane-producing outer tank of an anaerobic fermentation tank.
8. The method for improving anaerobic methane yield and purity of organic solid waste according to claim 7, wherein in step S1, the organic solid waste is any one or combination of kitchen waste, organic components of municipal waste, excess sludge, crop straws and livestock and poultry manure, the mass ratio of volatile solids to total solids is 40-90%, the water content is adjusted to 95-90%, the pH value is adjusted to 5-6, the stirring mode is continuous mechanical stirring, and the stirring speed is 50-100 r/min.
9. The method of claim 7, wherein in the step S2, the organic solid waste is pumped into the hydrolysis acidification tank of the anaerobic digestion tank intermittently from the bottom of the inner tank 1 time a day, each time the organic solid waste is pumped into 1/2-1 times of the effective volume of the inner tank, the retention time of the organic solid waste in the hydrolysis acidification tank is 1-2 days, the temperature of the materials in the hydrolysis acidification tank is 40-45 ℃, the stirring mode of the inner tank is continuous mechanical stirring, and the stirring speed is 50-100 r/min.
10. The method according to claim 7, wherein in step S3, the temperature of the materials in the methane-producing outer tank is 15-25 ℃, the stirring mode of the outer tank is continuous internal reflux stirring of the materials, the total volume of the reflux materials per day is 1-2 times of the effective volume of the outer tank, the exhaust mode of the anaerobic fermentation tank is intermittent operation, the pressure in the system is formed by the anaerobic reaction products of the materials, the exhaust valve is opened when the pressure is increased to 2-3 bar, and the exhaust valve is closed when the pressure is reduced to 1.2-1.5 bar;
in the step S3, the pumping-out mode of the biogas residues from the bottom of the methane-producing outer tank is intermittent operation for 1 time per day, and after certain exhaust in the day, 1/2-1/5 with the volume being the effective volume of the outer tank is pumped out every time, so that the retention time of the organic solid wastes in the methane-producing outer tank is 2-5 days.
In the step S4, the biogas slurry used for adding alkali accounts for 5-10% of the total volume of the biogas slurry.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114672399A (en) * | 2022-03-24 | 2022-06-28 | 上海市机电设计研究院有限公司 | Integrated vertical two-phase anaerobic reaction device and process |
| CN114933402A (en) * | 2022-06-08 | 2022-08-23 | 绿能生态环境科技有限公司 | Anaerobic in-situ methane production reactor |
| CN114956322A (en) * | 2022-06-13 | 2022-08-30 | 上海环境工程设计研究院有限公司 | Efficient wet anaerobic reactor for treating kitchen waste slurry and control method thereof |
| CN115232741A (en) * | 2022-09-23 | 2022-10-25 | 北京林业大学 | Agricultural and forestry waste recyclingSynergistic CO 2 Device and method for fixing and upgrading methane |
| CN115818829A (en) * | 2022-10-28 | 2023-03-21 | 同济大学 | Supplemented with the preference for CO 2 Pressure-holding two-phase anaerobic digestion device for methane bacteria and use method |
| CN116177829A (en) * | 2022-12-08 | 2023-05-30 | 同济大学 | Lateral flow micro-aeration coupled main flow electric drive anaerobic digestion method |
| CN116731820A (en) * | 2023-06-08 | 2023-09-12 | 中国铁工投资建设集团有限公司 | Organic solid waste loop-ring two-phase anaerobic fermentation system and fermentation device |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008026221A1 (en) * | 2006-08-29 | 2008-03-06 | Council Of Scientific & Industrial Research | A self mixing anaerobic digester useful for treatment of solid organic waste |
| CN104263642A (en) * | 2014-10-17 | 2015-01-07 | 北京昊业同宇科技有限公司 | Integrated treatment device and treatment method for kitchen garbage and excrement waste water |
| CN104357488A (en) * | 2014-06-27 | 2015-02-18 | 江苏省农业科学院 | Method for producing biogas by virtue of large-scale anaerobic fermentation of wood fiber raw materials |
| CN104630283A (en) * | 2015-02-15 | 2015-05-20 | 中国石油大学(北京) | System and method for bi-phase pressure anaerobic fermentation processing perishable waste for preparing marsh gas |
| CN105036500A (en) * | 2015-07-28 | 2015-11-11 | 同济大学 | Method for improving anaerobic digestion efficiency of organic wastes and content of methane in biogas |
| CN108179103A (en) * | 2018-01-19 | 2018-06-19 | 清华大学 | A kind of bicyclic two-phase integrated anaerobic reactor of nesting |
| CN110272923A (en) * | 2019-06-27 | 2019-09-24 | 南京万德斯环保科技股份有限公司 | A kind of waste dish garbage as resource utilizes method and system |
-
2021
- 2021-01-29 CN CN202110123311.7A patent/CN112680326A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008026221A1 (en) * | 2006-08-29 | 2008-03-06 | Council Of Scientific & Industrial Research | A self mixing anaerobic digester useful for treatment of solid organic waste |
| CN104357488A (en) * | 2014-06-27 | 2015-02-18 | 江苏省农业科学院 | Method for producing biogas by virtue of large-scale anaerobic fermentation of wood fiber raw materials |
| CN104263642A (en) * | 2014-10-17 | 2015-01-07 | 北京昊业同宇科技有限公司 | Integrated treatment device and treatment method for kitchen garbage and excrement waste water |
| CN104630283A (en) * | 2015-02-15 | 2015-05-20 | 中国石油大学(北京) | System and method for bi-phase pressure anaerobic fermentation processing perishable waste for preparing marsh gas |
| CN105036500A (en) * | 2015-07-28 | 2015-11-11 | 同济大学 | Method for improving anaerobic digestion efficiency of organic wastes and content of methane in biogas |
| CN108179103A (en) * | 2018-01-19 | 2018-06-19 | 清华大学 | A kind of bicyclic two-phase integrated anaerobic reactor of nesting |
| CN110272923A (en) * | 2019-06-27 | 2019-09-24 | 南京万德斯环保科技股份有限公司 | A kind of waste dish garbage as resource utilizes method and system |
Non-Patent Citations (3)
| Title |
|---|
| 史绪川等: "新型两相一体厌氧消化反应器处理餐厨垃圾中试研究", 《中国环境科学》 * |
| 胡纪萃: "《废水厌氧生物处理理论与技术》", 31 May 2003, 北京：中国建筑工业出版社 * |
| 钱泽澍: "《沼气发酵微生物学》", 30 April 1986, 杭州：浙江科学技术出版社 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114672399A (en) * | 2022-03-24 | 2022-06-28 | 上海市机电设计研究院有限公司 | Integrated vertical two-phase anaerobic reaction device and process |
| CN114933402A (en) * | 2022-06-08 | 2022-08-23 | 绿能生态环境科技有限公司 | Anaerobic in-situ methane production reactor |
| CN114956322A (en) * | 2022-06-13 | 2022-08-30 | 上海环境工程设计研究院有限公司 | Efficient wet anaerobic reactor for treating kitchen waste slurry and control method thereof |
| CN115232741A (en) * | 2022-09-23 | 2022-10-25 | 北京林业大学 | Agricultural and forestry waste recyclingSynergistic CO 2 Device and method for fixing and upgrading methane |
| CN115818829A (en) * | 2022-10-28 | 2023-03-21 | 同济大学 | Supplemented with the preference for CO 2 Pressure-holding two-phase anaerobic digestion device for methane bacteria and use method |
| CN116177829A (en) * | 2022-12-08 | 2023-05-30 | 同济大学 | Lateral flow micro-aeration coupled main flow electric drive anaerobic digestion method |
| CN116731820A (en) * | 2023-06-08 | 2023-09-12 | 中国铁工投资建设集团有限公司 | Organic solid waste loop-ring two-phase anaerobic fermentation system and fermentation device |
| CN116731820B (en) * | 2023-06-08 | 2024-02-09 | 中国铁工投资建设集团有限公司 | Organic solid waste loop-ring two-phase anaerobic fermentation system and fermentation device |
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