CN101805753B - Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes - Google Patents
Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes Download PDFInfo
- Publication number
- CN101805753B CN101805753B CN201010106904.4A CN201010106904A CN101805753B CN 101805753 B CN101805753 B CN 101805753B CN 201010106904 A CN201010106904 A CN 201010106904A CN 101805753 B CN101805753 B CN 101805753B
- Authority
- CN
- China
- Prior art keywords
- methane
- reactor
- hydrolysis
- acid
- organic wastes
- 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.)
- Active
Links
- 239000010815 organic waste Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000029087 digestion Effects 0.000 title claims abstract description 38
- 239000007787 solid Substances 0.000 title claims abstract description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 210
- 230000007062 hydrolysis Effects 0.000 claims abstract description 76
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 76
- 230000002053 acidogenic effect Effects 0.000 claims abstract description 43
- 150000007524 organic acids Chemical class 0.000 claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 5
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims description 38
- 238000012856 packing Methods 0.000 claims description 38
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 29
- 235000011089 carbon dioxide Nutrition 0.000 claims description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 25
- 239000001257 hydrogen Substances 0.000 claims description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims description 25
- 239000002253 acid Substances 0.000 claims description 23
- 230000000694 effects Effects 0.000 claims description 20
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 12
- 238000011026 diafiltration Methods 0.000 claims description 12
- 238000000855 fermentation Methods 0.000 claims description 12
- 230000004151 fermentation Effects 0.000 claims description 12
- 235000016709 nutrition Nutrition 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 11
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 claims description 10
- LCTONWCANYUPML-UHFFFAOYSA-N Pyruvic acid Chemical compound CC(=O)C(O)=O LCTONWCANYUPML-UHFFFAOYSA-N 0.000 claims description 10
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims description 10
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 claims description 10
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 claims description 10
- 230000003301 hydrolyzing effect Effects 0.000 claims description 8
- 239000000945 filler Substances 0.000 claims description 7
- 150000001413 amino acids Chemical class 0.000 claims description 6
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 6
- 229930195729 fatty acid Natural products 0.000 claims description 6
- 239000000194 fatty acid Substances 0.000 claims description 6
- 150000004665 fatty acids Chemical class 0.000 claims description 6
- 235000011187 glycerol Nutrition 0.000 claims description 6
- 239000004310 lactic acid Substances 0.000 claims description 5
- 235000014655 lactic acid Nutrition 0.000 claims description 5
- 235000019260 propionic acid Nutrition 0.000 claims description 5
- 229940107700 pyruvic acid Drugs 0.000 claims description 5
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 claims description 5
- 229940005605 valeric acid Drugs 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 4
- 150000001720 carbohydrates Chemical class 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- 239000002846 particulate organic matter Substances 0.000 claims description 4
- 150000004965 peroxy acids Chemical class 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 37
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract description 15
- 230000000696 methanogenic effect Effects 0.000 abstract 3
- 230000002401 inhibitory effect Effects 0.000 abstract 1
- 238000012423 maintenance Methods 0.000 abstract 1
- 235000005985 organic acids Nutrition 0.000 abstract 1
- 239000000047 product Substances 0.000 description 21
- 239000010813 municipal solid waste Substances 0.000 description 18
- 238000010411 cooking Methods 0.000 description 11
- 239000007788 liquid Substances 0.000 description 10
- 241000894006 Bacteria Species 0.000 description 8
- 239000010802 sludge Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 238000011081 inoculation Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 229920002472 Starch Polymers 0.000 description 4
- 239000000835 fiber Substances 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 150000004676 glycans Chemical class 0.000 description 4
- 235000013372 meat Nutrition 0.000 description 4
- 229920001282 polysaccharide Polymers 0.000 description 4
- 239000005017 polysaccharide Substances 0.000 description 4
- 108090000623 proteins and genes Proteins 0.000 description 4
- 102000004169 proteins and genes Human genes 0.000 description 4
- 235000019698 starch Nutrition 0.000 description 4
- 239000008107 starch Substances 0.000 description 4
- 235000013311 vegetables Nutrition 0.000 description 4
- 229960004756 ethanol Drugs 0.000 description 3
- 230000005764 inhibitory process Effects 0.000 description 3
- 229960000448 lactic acid Drugs 0.000 description 3
- 150000002632 lipids Chemical class 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 108010059892 Cellulase Proteins 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 102000004882 Lipase Human genes 0.000 description 2
- 108090001060 Lipase Proteins 0.000 description 2
- 239000004367 Lipase Substances 0.000 description 2
- LPQOADBMXVRBNX-UHFFFAOYSA-N ac1ldcw0 Chemical compound Cl.C1CN(C)CCN1C1=C(F)C=C2C(=O)C(C(O)=O)=CN3CCSC1=C32 LPQOADBMXVRBNX-UHFFFAOYSA-N 0.000 description 2
- 108010089934 carbohydrase Proteins 0.000 description 2
- 235000014633 carbohydrates Nutrition 0.000 description 2
- 229940106157 cellulase Drugs 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000010791 domestic waste Substances 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- -1 glycase Proteins 0.000 description 2
- 239000002054 inoculum Substances 0.000 description 2
- 235000019421 lipase Nutrition 0.000 description 2
- 230000004060 metabolic process Effects 0.000 description 2
- 239000010841 municipal wastewater Substances 0.000 description 2
- 238000013022 venting Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 101000925662 Enterobacteria phage PRD1 Endolysin Proteins 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000010336 energy treatment Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000000413 hydrolysate Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000001766 physiological effect Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000009790 rate-determining step (RDS) Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Classifications
-
- 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
Landscapes
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a method for producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes, which comprises the following steps: the perishable organic wastes are hydrolyzed in a hydrolysis acidogenic reactor, and a mixture obtained after hydrolysis is acidified to generate a large number of organic acid products with low molecular weight; the bottom of the hydrolysis acidogenic reactor is communicated with the bottom of a methanogenic reactor through a circulation pump and a pipeline; the top of the methanogenic reactor is communicated with the top of the hydrolysis acidogenic reactor; and the acetic acid producing reaction is carried out in the methanogenic reactor and the methane producing reaction is continuously carried out. The invention can separate the hydrolysis acidogenic process from the acetic acid and methane producing process in the anaerobic digestion process so as to prevent organic acids generated by the perishable organic wastes from inhibiting methanogenesis. The device has simple processing procedure, low cost, easy maintenance and stable and reliable performance, is suitable for anaerobic digestion treatment of various perishable organic wastes, and has highly efficient and stable biogas production capacity of the perishable organic wastes through the anaerobic digestion.
Description
Technical field
The present invention relates to a kind of treating method for organic refuse, more particularly, the present invention relates to a kind of is the method for three sections anaerobic digestion methane productions of high solid two phases of raw material with the perishable organic wastes.
Technical background
Perishable organic wastes mainly refer to live with production process in produce to be prone to the waste of corrupt and readily biodegradable, comprise rubbish from cooking, hogwash, vegetables, fruit and meat processing waste etc.Because quickening of urbanization process and growth in the living standard; Perishable organic wastes not only significantly increases on absolute yield; And also significantly raising of the shared ratio in domestic waste, this part rubbish accounts for more than 50% of domestic waste total amount at present.The maximum characteristics of perishable organic wastes are that moisture content and organic content are higher, and moisture content is generally more than 70%, organic content in butt generally more than 90%.These characteristics makes present main cities domestic rubbish disposal technology all have some problems; For example, cause in the landfill process, producing in a large number can polluted underground water and the greenhouse gases methane of edaphic percolate and unordered discharging for higher organic content; And higher moisture content need be added a large amount of extra auxiliary fuels when causing burning disposal.In fact, sanitary landfill of today is had relatively high expectations to addressing, and occupation of land face ground is bigger, in many big cities, has been difficult to find the place that is fit to sanitary landfill; For burning disposal, owing to there is secondary pollution problems, government and street levels is also held careful attitude to burning disposal at present.Therefore, press for a kind of new non-secondary pollution of exploitation and the little processing mode of floor space.Effective processing to perishable organic wastes can make a significant contribution for garbage treatment.The characteristics of high moisture content and high organic content make that perishable organic wastes is more suitable for carrying out Anaerobic Digestion, and in treating refuse, can obtain clean reproducible energy (biogas).
Organic matter anaerobic digestion product methane process comprises 4 steps: the outer hydrolysis of born of the same parents, product acid, product acetate and product methane.The outer hydrolysing step of born of the same parents refers under poly carbohydrase, glycase, cellulase, protein enzyme and action of lipase, to be monose, amino acid, glycerine and longer chain fatty acid with polysaccharide, starch, food fibre, protein and hydrolysis of lipid; Produce the micromolecular compound that sour step refers to that hydrolysis produces and under the effect of acid-producing bacteria, be decomposed into simpler acetate, propionic acid, butyric acid, pyruvic acid, lactic acid, valeric acid, ethanol and a spot of carbonic acid gas and hydrogen; Produce organic acid product (except that acetate) that the acetate step refers to produce sour step and further be converted into the process of acetate, carbonic acid gas and hydrogen; Produce the methane step and refer to that acetate generates the process of methane and carbonic acid gas and carbonic acid gas and hydrogen generation methane through acetate nutritional type methanogen.The anaerobic digestion of efficient stable is produced methane technology and need be guaranteed the hydrolysis acid process and produce the balance between the acetic acid and methane producing process; The small molecular organic acid that the hydrolysis acid process produces can in time be produced the utilization of methane process; Thereby avoid the organic acid accumulation to suppress the mikrobe in the fermentation system; Especially to the inhibition of methanogen,, when being accumulated to 13000mg/L, organic acid concentration will suppress methanogenesis activity fully because methanogen is lower to organic acid tolerance concentration.
The perishable organic wastes staple is polysaccharide, starch, food fibre, protein; They belong to the material of easy acidication; The hydrolysis rate of producing acid is very fast in anaerobic digestion process; By comparison, producing the methane process is the rate-limiting step of whole anaerobic digestion process, is easy to generate organic acid when causing perishable organic wastes to carry out Anaerobic Digestion and suppresses.Suppress for fear of organic acid, traditional single-phase anaerobic digestion can only be accomplished down in lower fermentation raw material concentration (being lower than 4%), and for the perishable organic wastes as this type of rubbish from cooking, its total solids level is generally 15% ~ 25%.At this moment, not only need consume a large amount of water and be used to turn down material concentration, and lower material concentration greatly reduces perishable organic wastes Anaerobic Digestion efficient and produces the biogas ability.Therefore, exploitation unrestraint efficient anaerobic digestion process for producing biogas becomes the key of perishable organic wastes minimizing and energy processing.
Summary of the invention
Main purpose of the present invention is to overcome deficiency of the prior art, and providing a kind of is the method for three sections anaerobic digestion methane productions of high solid two phases of raw material with the perishable organic wastes, to improve anaerobic digestion stability, processing efficiency and to produce the biogas ability.
In order to solve the problems of the technologies described above, the present invention realizes through following technical scheme:
The technical process of the inventive method may further comprise the steps:
(1) in hydrolysis acidogenic reactor with the perishable organic wastes hydrolysis, generate carbohydrate, amino acid, longer chain fatty acid and the glycerine of solubility; And, generate a large amount of small molecular organic acid products with the mixture acidifying that obtains after the said hydrolyzed; Hydrolysis acidogenic reactor adopts solid diafiltration bed; Perishable organic wastes fills in above the diafiltration filler of diafiltration bed; The water that comes from spray header carries out sprinkle to perishable organic wastes; The organic acid that the acid-producing of hydrolysis simultaneously generates is soluble in water, and stores in the hydrolysis acidogenic reactor bottom through diafiltration filler and porous plate formation percolate;
Preferred processing condition is in the step (1):
With perishable organic wastes hydrolysis under the condition of raw material solid concentration 15% ~ 40%, 25 ℃ ~ 60 ℃ of temperature, pH value 4.5 ~ 6.5, generate carbohydrate, amino acid, longer chain fatty acid and the glycerine of solubility;
With the mixture that obtains after said hydrolyzed acidifying under the condition of 25 ℃ ~ 60 ℃ of temperature, pH value 4.5 ~ 6.5; Generate a large amount of small molecular organic acid products; Comprise pyruvic acid, acetate, propionic acid, butyric acid, valeric acid, lactic acid, ethanol, and small quantity of hydrogen and carbonic acid gas.
(2) hydrolysis acidogenic reactor bottom and methane-producing reactor bottom are communicated with through recycle pump and pipeline; Methane-producing reactor top and hydrolysis acidogenic reactor top are communicated with; In methane-producing reactor, produce acetic acidreaction, the organic acid product except that acetate that step (1) acidifying is produced generates acetate, hydrogen and carbonic acid gas under the effect of acetogen; And proceed to produce methane reaction, and acetate is generated methane and carbonic acid gas at the effect bottom fermentation of acetate nutritional type methanogen, hydrogen and carbonic acid gas are generated methane at the effect bottom fermentation of hydrogen nutritional type methanogen; The main body of methane-producing reactor is the fibrous packing bed bioreactor on top, and fibrous packing can be adhered to acetogen and methanogen, improves the concentration of interior acetogen of methane-producing reactor and methanogen, produces the biogas performance thereby improve; The methane-producing reactor bottom is provided with filter bed, is used for holding back the particulate organic matter of percolate, avoids stopping up the fibrous packing bed; When the percolate that step (1) produces was flowed through methane-producing reactor, the organic acid in the percolate generated methane and carbonic acid gas under the serial action of acetogen and methanogen;
The preferred processing condition of step (2) is:
The organic acid product except that acetate that step (1) acidifying is produced generates acetate, hydrogen and carbonic acid gas under the effect of acetogen, this reaction control temperature is 25 ℃ ~ 60 ℃, pH value 6.5 ~ 8.0.
Gained acetate generates methane and carbonic acid gas at the effect bottom fermentation of acetate nutritional type methanogen; Hydrogen in the last step and carbonic acid gas generate methane at the effect bottom fermentation of hydrogen nutritional type methanogen; The equal controlled temperature of product methane reaction that these two types of methanogens are participated in is 25 ℃ ~ 60 ℃, pH value 6.5 ~ 8.0.
(3) regularly remove part perishable organic wastes hydrolytic residue, effectively handle volume to improve reactor drum from the discharge opening of hydrolysis acidogenic reactor; Regularly remove perishable organic wastes percolate throw out, effectively store volume to improve percolate from the slag-drip opening of hydrolysis acidogenic reactor; Routine cleaning is laid equal stress on and is newly loaded the filter packing in the filter bed in the methane-producing reactor, guarantees good filter effect.
The time of general periodic cleaning is:
Whenever removed part perishable organic wastes hydrolytic residue at a distance from 10 days ~ 60 days from the discharge opening of hydrolysis acidogenic reactor, effectively handle volume to improve reactor drum; Whenever removed perishable organic wastes percolate throw out at a distance from 30 days ~ 90 days from the slag-drip opening of hydrolysis acidogenic reactor, effectively store volume to improve percolate; Whenever clean the filter packing in the filter bed in the new filling methane-producing reactor of laying equal stress at a distance from 30 days ~ 90 days, guarantee good filter effect.
Further improvement of the present invention is:
The hydrolysis acidogenic reactor bottom links to each other through recycle pump and pipeline with the methane-producing reactor bottom, and said pump entry section is provided with branch line, is used for adding anaerobic digestion inoculum, acid-base modifier and water etc. to methane-producing reactor.When methane-producing reactor operation appearance is unusual, specifically, when methane-producing reactor mild or moderate peracid or mistake alkali, can regulate through the internal circulating load of control percolate; When serious peracid in the methane-producing reactor or mistake alkali, can pump into acidity-basicity regulator from the branch line of pump entry section to regulate potential of hydrogen.
Compared with prior art, the invention has the beneficial effects as follows:
The present invention can separate the hydrolysis acid process (sour phase is produced in hydrolysis) of anaerobic digestion process with product acetic acid and methane producing process (producing methane mutually), the organic acid of avoiding perishable organic wastes to produce suppresses methanogenesis.Hydrolysis is produced acid and is adopted high solid diafiltration bed bioreactor mutually, can make perishable organic wastes at higher material concentration bottom fermentation, and material concentration reaches as high as 40%, therefore, need not a large amount of water of extra interpolation and is used to turn down material concentration.In addition; The water that in solid diafiltration bed bioreactor, is used for the sprinkle perishable organic wastes comes from methane-producing reactor; Water in the total system can be realized self-circulation, and therefore, this invention is a water saving type perishable organic wastes anaerobic digestion methane production treatment unit.Filler in the methane-producing reactor in the fibrous packing bed can adhere to methanogen, improves the cell concn of methanogen in the reactor drum, thereby improves the anaerobic digestion methane production ability.Percolate gets into before the fibrous packing bed, and the particulate organic matter of the setting of filter bed in can the effectively catching percolate is to avoid stopping up the fibrous packing bed.The filter packing entrance and exit is set on filter bed, can lays equal stress on new filling filter packing to guarantee good filter effect by routine cleaning.Compare with the single-phase anaerobic digestion device of traditional perishable organic wastes, adopt this contrive equipment can significantly improve the concentration of treatment of perishable organic wastes anaerobic digestion, high energy brings up to 40% from 4%, and the pond holds produces the high energy of biogas rate from 0.8m
3/ (m
3D) bring up to 2.5m
3/ (m
3And can effectively avoid the inhibition of organic acid d), to methanogenesis.
The inventive method process operating management is simple, and anaerobic digestion methane production is stable and reliable for performance.Be applicable to the Anaerobic Digestion of all kinds of perishable organic wastes, both can efficiently handle organic waste, reduce its severe contamination, can produce clean reproducible energy (biogas) again, can realize the recovery energy of organic waste, thereby turn waste into wealth environment.
The present invention has the perishable organic wastes anaerobic digestion methane production ability of efficient stable; Be fit to very much rubbish from cooking processing field, hogwash processing enter and fruit, vegetables and meat packing plant etc. and carry out application, have good economy, environment and social benefit.
Description of drawings
Fig. 1 is the inventive method schema.
Reference numeral: hopper 1; Hydrolysis acidogenic reactor 2; Methane-producing reactor 3; Recycle pump 4; Water distributor 5; Spray header 6; Opening for feed 7; Porous plate 8; Discharge opening 9; Slag-drip opening 10; Diafiltration filler 11; Filter bed 12; Fibrous packing bed 13; Filter packing 14; Fibrous packing frame 15; Fibrous packing 16; Filter packing inlet 17; Filter packing outlet 18; Gas discharge outlet 19; SV 20; Tensimeter 21; Gas discharge outlet is provided with under meter 22 respectively; Heat chuck 23; Thermal insulation layer 24; Temperature/acidometer 25; Thief hatch 26; Branch line 27.
Embodiment
Further present invention is described below in conjunction with accompanying drawing and embodiment.
The staple of perishable organic wastes is polysaccharide, starch, food fibre, protein and lipid, and the anaerobic digestion product methane process of this type raw material comprises 4 steps: the outer hydrolysis of born of the same parents, product acid, product acetate and product methane.The outer hydrolysing step of born of the same parents refers under poly carbohydrase, glycase, cellulase, protein enzyme and action of lipase, to be monose, amino acid, glycerine and longer chain fatty acid with polysaccharide, starch, food fibre, protein and hydrolysis of lipid; Produce the micromolecular compound that sour step refers to that hydrolysis produces and under the effect of acid-producing bacteria, be decomposed into simpler acetate, propionic acid, butyric acid, pyruvic acid, lactic acid, valeric acid, ethanol and a spot of carbonic acid gas and hydrogen; Produce organic acid product (except that acetate) that the acetate step refers to produce sour step and further be converted into the process of acetate, carbonic acid gas and hydrogen; Produce the methane step and refer to that acetate generates the process of methane and carbonic acid gas and carbonic acid gas and hydrogen generation methane through acetate nutritional type methanogen.
The mikrobe type of participating in above-mentioned whole process comprises hydrolysis acid-producing bacteria, acetogen and methanogen; Wherein the hydrolysis acid-producing bacteria can be secreted the outer lytic enzyme of born of the same parents and carries out the raw material hydrolysis; And with hydrolysate fermentation generation organic acid, methanogen comprises acetate nutritional type methanogen and hydrogen nutritional type methanogen.Derive from the anaerobic activated sludge that methane-generating pit or municipal wastewater treatment plant etc. locate, generally all contain the mikrobe of the above-mentioned type, therefore usually with the inoculum of this type anaerobic activated sludge as anaerobic digestion methane production.But the physiological property of hydrolysis acid-producing bacteria and methanogen is inequality, and the pH value scope that hydrolysis acid-producing bacteria growth metabolism allows is wider, be 4.5 ~ 9.0, and the growth velocity of this bacterium is very fast, is generally its generation time 10 ~ 30 minutes; And the pH scope that the methanogen growth metabolism allows is narrower, be 6.5 ~ 8.0, and growth velocity is slower, and its generation time is generally at 4 ~ 6 days.The present invention is in view of above characteristics; The hydrolysis acid process of perishable organic wastes is accomplished in two reactor drums respectively with product methane process; And to the operation pH independent control of two reactor drums; Avoid hydrolysis to produce the sour methanogen that suppresses of high concentration organic that acid generates on the one hand, be convenient on the other hand two process independent optimization controls.Simultaneously, adopt the fibrous packing bed,, improve the concentration of this two bacterioid in the methane-producing reactor, thereby improve the anaerobic digestion methane production performance through the absorption of fibrous packing to acetogen and methanogen as methane-producing reactor.
The operational process of technology is following in the present embodiment:
The present embodiment using appts is seen Fig. 1; During startup; Add a spot of perishable organic wastes from hopper 1 to hydrolysis acidogenic reactor 2, and inoculation liquid pumped into methane-producing reactor 3 from the branch line 27 of recycle pump 4 entrances, treat that inoculation liquid is flooded fibrous packing after; Continue to pump into inoculation liquid until form the perishable organic wastes percolate in hydrolysis acidogenic reactor 2 bottoms; And the percolate height is during near porous plate 8, and the valve of close fork pipeline 27 stops to pump into inoculation liquid, so far accomplishes the interpolation of inoculation liquid.Subsequently; Percolate is pumped into methane-producing reactor 3 from hydrolysis acidogenic reactor 2 bottoms through recycle pump 4; And the liquid in the methane-producing reactor 3 is from fibrous packing bed 13 top overflow to hydrolysis acidogenic reactor 2; And carry out sprinkle by water distributor 5 and 6 pairs of perishable organic wastes of spray header; The organic acid that liquid that sprinkle gets off dissolving perishable organic wastes hydrolysis acid process produces, and the diafiltration filler 11 of flowing through forms percolates with porous plate 8 and is stored in hydrolysis acidogenic reactor 2 bottoms, so far accomplishes a liquid circulation.Circulate through repeatedly a kind of like this and to accomplish the domestication of methanogen and adhering to and grow on fibrous packing 16 thereof.After domestication is accomplished, progressively add perishable organic wastes, until the loading height of perishable organic wastes position near opening for feed 7.When progressively adding perishable organic wastes, increase the liquid circulation number of times, until continuous circulation, finally realize the normal continuously operation of this contrive equipment.
Described inoculation liquid is the anaerobic activated sludge that methane-generating pit or municipal wastewater treatment plant etc. locate.
Embodiment 1
(1) add a spot of rubbish from cooking from hopper 1 to hydrolysis acidogenic reactor 2, and control hydrolysis acidogenic reactor 2 temperature is 37 ℃.
(2) anaerobic activated sludge in the collection methane-generating pit; Pump into methane-producing reactor 3 through branch line 27; After treating that anaerobic activated sludge floods fibrous packing 16, continue to pump into anaerobic activated sludge until forming the rubbish from cooking percolate in hydrolysis acidogenic reactor 2 bottoms, and the percolate height is during near porous plate 8; The valve of close fork pipeline 27 stops to pump into anaerobic activated sludge, and the temperature of said process control methane-producing reactor 3 is 37 ℃.
(3) in the hydrolysis acidogenic reactor in the said process; Rubbish from cooking generates acetate, propionic acid, butyric acid, valeric acid, pyruvic acid, lactic acid, ethanol and amounts of carbon dioxide and hydrogen under the effect of hydrolysis acid-producing bacteria in anaerobic activated sludge; Wherein carbonic acid gas and hydrogen are discharged from the venting port 19 at hydrolysis acidogenic reactor 2 tops, and organic acid is dissolved in the percolate.Hydrolysis acid production controlled temperature is 37 ℃, and pH is 5.5.
(4) above-mentioned percolate is pumped into methane-producing reactor 3 through recycle pump 4; In methane-producing reactor 3; Organic acid in the percolate generates methane and carbonic acid gas under the serial action of acetogen and methanogen; Methane and carbonic acid gas are discharged from the venting port at methane-producing reactor 3 tops, and the percolate after organic acid is utilized flow to hydrolysis acidogenic reactor 2 from the riser at methane-producing reactor 3 tops.Producing acetate and methanogenesis controlled temperature is 37 ℃, and control pH is 7.2.
Produce acetate and carry out in methane-producing reactor 3 with the product methane reaction, methane-producing reactor 3 is divided into filter bed 12 and fibrous packing bed 13 from bottom to up, and filter bed 12 is held back the particulate organic matter in the percolate, avoids stopping up fibrous packing bed 13.Fibrous packing 16 in the fibrous packing bed 13 can be adhered to acetogen and methanogen, improves the concentration of this two bacterioid in the methane-producing reactor 3, thereby improves the anaerobic digestion methane production performance.
(5), accomplish the domestication of methanogen in the methane-producing reactor 3 and adhering to and grow on fibrous packing 16 thereof through 10 days percolate circulation repeatedly.The temperature of control hydrolysis acidogenic reactor 2 is 37 ℃ in this process, and pH is 5.5; The temperature of control methane-producing reactor 3 is 37 ℃, and pH is 7.2.
(6) after domestication is accomplished, progressively add rubbish from cooking, until the loading height of rubbish from cooking position near hydrolysis acidogenic reactor 2 opening for feeds 7.When progressively adding rubbish from cooking, increase the percolate cycle index, until continuous circulation, finally realize the normal continuously operation of this technology.The temperature of control hydrolysis acidogenic reactor 2 is 37 ℃ in this process, and pH is 5.5; The temperature of control methane-producing reactor 3 is 37 ℃, and pH is 7.2.
(7) after the normal operation, every at a distance from 30 days, remove part rubbish from cooking hydrolytic residue from the discharge opening 9 of hydrolysis acidogenic reactor 2.
(8) after the normal operation, every at a distance from 50 days, remove rubbish from cooking percolate throw out from the slag-drip opening 10 of hydrolysis acidogenic reactor 2; Every at a distance from 50 days, clean from the filter packing outlet 18 discharge filter packings 14 of filter bed 12, and enter the mouth from filter packing and 17 to load again.
Embodiment 2
The step of present embodiment is identical with embodiment 1, and wherein handling raw material is meat processing rubbish, and
The temperature of control methane-producing reactor 3 is 25 ℃ in the step (2); Hydrolysis acid production control pH is 6.5 in the step (3); Product acetate and methanogenesis controlled temperature are 25 ℃ in the step (4), and control pH is 8.0; Through 20 days percolate circulation repeatedly, the temperature of control hydrolysis acidogenic reactor 2 was 25 ℃ in the step (5), and pH is 6.5; The temperature of methane-producing reactor is 25 ℃, and pH is 8.0; The temperature of control hydrolysis acidogenic reactor is 25 ℃ in the step (6), and pH is 6.5, and the temperature of methane-producing reactor is 25 ℃, and pH is 8.0; Whenever removed part meat processing rubbish hydrolytic residue in the step (7) at a distance from 40 days; Every in the step (8) at a distance from 60 days, remove the percolate throw out; Every at a distance from 60 days, clean the filter packing 14 in the new filling filter bed 12 of laying equal stress on.
Embodiment 3
The step of present embodiment is identical with embodiment 1, and wherein handling raw material is vegetables processing rubbish, and
The temperature of control hydrolysis acidogenic reactor 2 is 60 ℃ in the step (1); The temperature of control methane-producing reactor 3 is 60 ℃ in the step (2); Hydrolysis acid production controlled temperature is 60 ℃ in the step (3), and pH is 4.5; Product acetate and methanogenesis controlled temperature are 60 ℃ in the step (4), and pH is 6.5; Through 15 days percolate circulation repeatedly, the temperature of control hydrolysis acidogenic reactor 2 was 60 ℃ in the step (5), and pH is 4.5; The temperature of methane-producing reactor 3 is 60 ℃, and pH is 6.5; The temperature of control hydrolysis acidogenic reactor 2 is 60 ℃ in the step (6), and pH is 4.5; The temperature of methane-producing reactor 3 is 60 ℃, and pH is 6.5; Whenever removed part vegetables processing rubbish hydrolytic residue in the step (7) at a distance from 20 days; Every in the step (8) at a distance from 40 days, remove the percolate throw out; Every at a distance from 40 days, clean the filter packing 14 in the new filling filter bed 12 of laying equal stress on.
Compare with traditional low single-phase anaerobic digestion methane production method of solids concn of perishable organic wastes; The present invention can handle perishable organic wastes under up to 40% condition in raw material solid concentration; And the hydrolysis acid process (sour phase is produced in hydrolysis) of anaerobic digestion process is separated with product acetic acid and methane producing process (producing methane mutually); And be provided with two sections mutually producing methane; Be filter bed and fibrous packing bed, this high solid two is three sections perishable organic wastes energy treatment processs that anaerobic digestion methane production technology is a kind of efficient stable mutually.Adopt this invention can significantly improve the concentration of treatment of perishable organic wastes anaerobic digestion, high energy brings up to 40% with raw material solid concentration from 4%, and high energy holds the pond and produces the biogas rate from 0.8m
3/ (m
3D) bring up to 2.5m
3/ (m
3And can effectively avoid the inhibition of organic acid d), to methanogenesis.
At last, it is also to be noted that what more than enumerate only is practical implementation example of the present invention.Obviously, the invention is not restricted to above embodiment, many distortion can also be arranged.All distortion that those of ordinary skill in the art can directly derive or associate from content disclosed by the invention all should be thought protection scope of the present invention.
Claims (3)
1. a perishable organic wastes high solid two method of three sections anaerobic digestion methane productions mutually is characterized in that may further comprise the steps:
(1) in hydrolysis acidogenic reactor with the perishable organic wastes hydrolysis, generate carbohydrate, amino acid, longer chain fatty acid and the glycerine of solubility; And, generate a large amount of small molecular organic acid products with the mixture acidifying that obtains after the said hydrolyzed; Hydrolysis acidogenic reactor adopts solid diafiltration bed; Perishable organic wastes fills in above the diafiltration filler of diafiltration bed; The water that comes from spray header carries out sprinkle to perishable organic wastes; The organic acid that the acid-producing of hydrolysis simultaneously generates is soluble in water, and stores in the hydrolysis acidogenic reactor bottom through diafiltration filler and porous plate formation percolate;
(2) hydrolysis acidogenic reactor bottom and methane-producing reactor bottom are communicated with through recycle pump and pipeline; Methane-producing reactor top and hydrolysis acidogenic reactor top are communicated with; Said pump entry section is provided with branch line; When methane-producing reactor mild or moderate peracid or mistake alkali, regulate through the internal circulating load of control percolate; When serious peracid in the methane-producing reactor or when crossing alkali, pump into acidity-basicity regulator to regulate potential of hydrogen from the branch line of pump entry section; In methane-producing reactor, produce acetic acidreaction, the organic acid product except that acetate that step (1) acidifying is produced generates acetate, hydrogen and carbonic acid gas under the effect of acetogen; And proceed to produce methane reaction, and acetate is generated methane and carbonic acid gas at the effect bottom fermentation of acetate nutritional type methanogen, hydrogen and carbonic acid gas are generated methane at the effect bottom fermentation of hydrogen nutritional type methanogen; The main body of methane-producing reactor is the fibrous packing bed bioreactor on top, and fibrous packing can be adhered to acetogen and methanogen, improves the concentration of interior acetogen of methane-producing reactor and methanogen, produces the biogas performance thereby improve; The methane-producing reactor bottom is provided with filter bed, is used for holding back the particulate organic matter of percolate, avoids stopping up the fibrous packing bed; When the percolate that step (1) produces was flowed through methane-producing reactor, the organic acid in the percolate generated methane and carbonic acid gas under the serial action of acetogen and methanogen;
(3) regularly remove part perishable organic wastes hydrolytic residue, effectively handle volume to improve reactor drum from the discharge opening of hydrolysis acidogenic reactor; Regularly remove perishable organic wastes percolate throw out, effectively store volume to improve percolate from the slag-drip opening of hydrolysis acidogenic reactor; Routine cleaning is laid equal stress on and is newly loaded the filter packing in the filter bed in the methane-producing reactor, guarantees good filter effect.
2. perishable organic wastes high solid two as claimed in claim 1 is the method for three sections anaerobic digestion methane productions mutually; It is characterized in that in the said step (1) perishable organic wastes hydrolysis under the condition of raw material solid concentration 15%～40%, 25 ℃～60 ℃ of temperature, pH value 4.5～6.5, generate carbohydrate, amino acid, longer chain fatty acid and the glycerine of solubility; With the mixture that obtains after said hydrolyzed acidifying under the condition of 25 ℃～60 ℃ of temperature, pH value 4.5～6.5; Generate a large amount of small molecular organic acid products; Comprise pyruvic acid, acetate, propionic acid, butyric acid, valeric acid, lactic acid, ethanol, and small quantity of hydrogen and carbonic acid gas.
3. perishable organic wastes high solid two as claimed in claim 1 is the method for three sections anaerobic digestion methane productions mutually; It is characterized in that the organic acid product except that acetate that in the said step (2) step (1) acidifying is produced generates acetate, hydrogen and carbonic acid gas under the effect of acetogen; This reaction control temperature is 25 ℃～60 ℃, pH value 6.5～8.0; Gained acetate generates methane and carbonic acid gas at the effect bottom fermentation of acetate nutritional type methanogen; Hydrogen in the last step and carbonic acid gas generate methane at the effect bottom fermentation of hydrogen nutritional type methanogen; The equal controlled temperature of product methane reaction that these two types of methanogens are participated in is 25 ℃～60 ℃, pH value 6.5～8.0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010106904.4A CN101805753B (en) | 2010-02-03 | 2010-02-03 | Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010106904.4A CN101805753B (en) | 2010-02-03 | 2010-02-03 | Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101805753A CN101805753A (en) | 2010-08-18 |
| CN101805753B true CN101805753B (en) | 2012-09-05 |
Family
ID=42607706
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010106904.4A Active CN101805753B (en) | 2010-02-03 | 2010-02-03 | Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101805753B (en) |
Families Citing this family (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757889A (en) * | 2011-04-27 | 2012-10-31 | 中国科学院青岛生物能源与过程研究所 | Method for producing methane from kitchen waste by two continuous anaerobic fermentation steps |
| CN102190410B (en) * | 2011-05-05 | 2012-11-14 | 郑州蓝德环保科技有限公司 | Method for performing anaerobic treatment on organic garbage by using percolation bed |
| CN102321674B (en) * | 2011-08-25 | 2013-10-23 | 中国科学院广州能源研究所 | Two-phase reaction method for raising efficiency of energy grass to prepare bio-gas |
| CN102321675B (en) * | 2011-08-26 | 2014-11-12 | 中国农业机械化科学研究院 | Method and device for producing bio-gas by organic waste |
| CN102492728B (en) * | 2011-12-02 | 2014-05-21 | 同济大学 | Rancidity-prone waste biogas utilization method based on in-subarea inoculation and quick start |
| CN102492506A (en) * | 2011-12-12 | 2012-06-13 | 中国科学院广州能源研究所 | Method and device for removing carbon dioxide in methane by organic waste water |
| CN102559771B (en) * | 2012-01-11 | 2014-01-22 | 北京化工大学 | Method for improving anaerobic digestion performance of biomass wastes by biological phase separation and optimization technology |
| DK2802639T3 (en) | 2012-01-12 | 2017-07-31 | Blaygow Ltd | ANAEROBIC PROCESS |
| CN102660454B (en) * | 2012-05-07 | 2014-03-19 | 黑龙江龙能伟业燃气股份有限公司 | Anaerobic dry fermentation equipment and anaerobic dry fermentation process using same |
| CN102876726A (en) * | 2012-10-21 | 2013-01-16 | 韩洪波 | Anaerobic fermentation method sequentially performing filter pressing and marsh production |
| CN105026321B (en) | 2012-11-16 | 2018-11-16 | 布雷高有限公司 | Cereal processing |
| CN104646390A (en) * | 2013-11-19 | 2015-05-27 | 深圳德瑞新能科技有限公司 | High-efficiency low-energy-consumption kitchen garbage comprehensive treatment method |
| CN103820502B (en) * | 2014-03-05 | 2016-11-09 | 东南大学 | A kind of diphasic anaerobic fermentation biogas method |
| CN104004791A (en) * | 2014-05-16 | 2014-08-27 | 浙江工商大学 | Coupled two-phase anaerobic kitchen garbage strengthening treatment method combining microbial electrolysis cell and microbial cell and device |
| CN104498342B (en) * | 2015-01-22 | 2016-04-27 | 李俊 | U-shaped some fermentation zones methane generation systems |
| CN105330358A (en) * | 2015-12-11 | 2016-02-17 | 苏州华周胶带有限公司 | Agricultural waste recycling and reproduction method |
| CN106282245B (en) * | 2016-03-23 | 2023-06-02 | 香港生产力促进局 | Novel organic garbage recycling method and system |
| CN107267376B (en) * | 2017-08-08 | 2020-07-10 | 四川六叶草环保科技有限公司 | Household garbage fermentation equipment and method |
| CN107555591A (en) * | 2017-09-15 | 2018-01-09 | 大连理工大学 | A kind of diphasic anaerobic processing unit and technique that direct inter-species electron transmission is built based on ethanol-type fermentation |
| CN108147627A (en) * | 2018-02-23 | 2018-06-12 | 南京林业大学 | The anaerobic acid-production methane phase technique of the anaerobic acid-production methane phase device of synchronous recycling ammonia nitrogen and synchronous recycling ammonia nitrogen |
| CN108485945B (en) * | 2018-03-26 | 2021-06-18 | 太原理工大学 | Reaction system suitable for organic solid waste resource utilization |
| CN109650690A (en) * | 2019-02-19 | 2019-04-19 | 常州市环境卫生管理处 | Kitchen castoff efficient anaerobic produces the processing method that acid produces gas |
| CN110184171B (en) * | 2019-04-16 | 2023-12-19 | 齐鲁工业大学 | Perishable organic single-double-phase anaerobic digestion device |
| CN110295201B (en) * | 2019-06-26 | 2021-01-19 | 山东省科学院能源研究所 | Method for preparing biogas from lignocellulose hydrolysate |
| CN111592974A (en) * | 2020-03-12 | 2020-08-28 | 嘉兴恒创环保科技有限公司 | Three-phase integrated plug flow type biogas fermentation system and fermentation method |
| CN111826474A (en) * | 2020-06-24 | 2020-10-27 | 中国科学院广州能源研究所 | Thermodynamic early warning method based on Gibbs free energy change of key biochemical reaction |
| JP7150899B6 (en) * | 2021-01-07 | 2022-10-31 | 水ｉｎｇ株式会社 | Anaerobic treatment apparatus and anaerobic treatment method |
| CN114350481B (en) * | 2022-01-07 | 2024-01-26 | 天津大学 | System and method for preparing biogas from two-phase double-circulation kitchen waste |
| CN115488140B (en) * | 2022-09-09 | 2024-02-20 | 中节能(肥西)环保能源有限公司 | System and method for treating kitchen waste by coupling tidal type fermentation percolating bed and efficient anaerobic reactor |
| CN116216925A (en) * | 2022-12-30 | 2023-06-06 | 青岛理工大学 | Agricultural waste and sewage cooperative treatment device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4710300A (en) * | 1976-10-29 | 1987-12-01 | Ceskoslovenska Akademie Ved | Method for processing of organic materials containing nitrogen compounds |
| CN101337838A (en) * | 2008-08-11 | 2009-01-07 | 鄂尔多斯市东胜区传祥垃圾处理有限责任公司 | Combined anaerobic fermentation process for organic solid wastes |
| EP2039776A2 (en) * | 2007-09-20 | 2009-03-25 | EcoFuel Labs LLC | Method of processing slops |
| CN101565719A (en) * | 2008-04-25 | 2009-10-28 | 北京化工大学 | Method for producing methane by two-phase multi-stage anaerobic fermentation of organic solid wastes |
-
2010
- 2010-02-03 CN CN201010106904.4A patent/CN101805753B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4710300A (en) * | 1976-10-29 | 1987-12-01 | Ceskoslovenska Akademie Ved | Method for processing of organic materials containing nitrogen compounds |
| EP2039776A2 (en) * | 2007-09-20 | 2009-03-25 | EcoFuel Labs LLC | Method of processing slops |
| CN101565719A (en) * | 2008-04-25 | 2009-10-28 | 北京化工大学 | Method for producing methane by two-phase multi-stage anaerobic fermentation of organic solid wastes |
| CN101337838A (en) * | 2008-08-11 | 2009-01-07 | 鄂尔多斯市东胜区传祥垃圾处理有限责任公司 | Combined anaerobic fermentation process for organic solid wastes |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101805753A (en) | 2010-08-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101805753B (en) | Method of producing biogas through high-solid two-phase three-stage anaerobic digestion by using perishable organic wastes | |
| Mahmudul et al. | A comprehensive review of the recent development and challenges of a solar-assisted biodigester system | |
| CN102321675B (en) | Method and device for producing bio-gas by organic waste | |
| EP2521768B1 (en) | Apparatus and preculture tank for biomethanation of biomass | |
| CN100532531C (en) | Device for co-producing hydrogen and methane by biomass and solid organic waste fermenting method | |
| CN101792246B (en) | Method for generating biogas through intensified hydrolysis and anaerobic digestion of municipal domestic organic refuse | |
| CN104646390A (en) | High-efficiency low-energy-consumption kitchen garbage comprehensive treatment method | |
| CN104130942B (en) | Agricultural organic waste anaerobically fermenting reclaims biogas reaction unit and recovery method | |
| Rico et al. | Dry batch anaerobic digestion of food waste in a box-type reactor system: Inoculum preparation and reactor performance | |
| CN102212561B (en) | Processing method for fermenting straws in dry-process and wet-process combined way | |
| CN104263642B (en) | The integrated treatment unit of rubbish from cooking and excrement and urine water and treatment process | |
| CN105969809B (en) | A method of biogas is prepared using stalk joint excess sludge | |
| CN101812401B (en) | Device for producing biogas by two-phase three-section anaerobic digestion of high solids of perishable organic wastes | |
| CN102168109A (en) | Method for producing hydrogen and methane through continuous solid state fermentation of kitchen garbage | |
| CN104276737A (en) | Energy source output type sewage sludge treatment method | |
| CN115069739A (en) | Bidirectional reinforced multi-source cooperative full-amount recycling treatment system and technology for kitchen waste | |
| CN100532565C (en) | Method for co-producing hydrogen and methane by biomass and solid organic waste fermenting method | |
| CN101786771B (en) | Equipped device for enhanced hydrolysis and anaerobic digestion of urban living organic garbage for producing biological fuel gas | |
| CN102660452A (en) | Multistage serially-connected biochemical reaction device and flow type anaerobic fermentation method | |
| CN108467170B (en) | Fermentation tank, and dry anaerobic fermentation system and method for co-processing municipal domestic garbage and municipal sludge by using fermentation tank | |
| CN201644487U (en) | High-solid two-phase three-section biogas anaerobic digestion production device via perishable organic garbage | |
| CN204220605U (en) | The comprehensive food waste treatment system of high efficiency low power consuming | |
| Sattler et al. | Anaerobic processes for waste treatment and energy generation | |
| CN208440534U (en) | Organic refuse treating system | |
| CN101260363B (en) | Device and method for producing marsh gas from fruit and vegetable castoff |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |