CN101892267A - A biogas fermentation process with methane in-situ enrichment function - Google Patents
A biogas fermentation process with methane in-situ enrichment function Download PDFInfo
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- fermented liquid
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000000855 fermentation Methods 0.000 title claims abstract description 40
- 230000004151 fermentation Effects 0.000 title claims abstract description 36
- 238000011065 in-situ storage Methods 0.000 title claims abstract description 9
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 239000002253 acid Substances 0.000 claims abstract description 9
- 230000007062 hydrolysis Effects 0.000 claims abstract description 7
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 7
- 239000010902 straw Substances 0.000 claims description 4
- 239000010865 sewage Substances 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 230000002550 fecal effect Effects 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 239000010802 sludge Substances 0.000 claims description 2
- 244000025254 Cannabis sativa Species 0.000 claims 1
- 239000010909 process residue Substances 0.000 claims 1
- 238000010992 reflux Methods 0.000 claims 1
- 239000007787 solid Substances 0.000 claims 1
- 241000894007 species Species 0.000 claims 1
- 238000005507 spraying Methods 0.000 claims 1
- 239000002351 wastewater Substances 0.000 claims 1
- 230000000696 methanogenic effect Effects 0.000 abstract 1
- 230000020477 pH reduction Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 43
- 238000010521 absorption reaction Methods 0.000 description 20
- 230000008569 process Effects 0.000 description 15
- 239000007789 gas Substances 0.000 description 7
- 239000012528 membrane Substances 0.000 description 7
- 238000000926 separation method Methods 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 240000008042 Zea mays Species 0.000 description 3
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 3
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 3
- 235000009973 maize Nutrition 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000010815 organic waste Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000002906 microbiologic effect Effects 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
- 230000002053 acidogenic effect Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- -1 amino hydramine Chemical compound 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000002054 inoculum Substances 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920006393 polyether sulfone Polymers 0.000 description 1
- 229920000151 polyglycol Polymers 0.000 description 1
- 239000010695 polyglycol Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000003462 zymogenic effect Effects 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/20—Degassing; Venting; Bubble traps
-
- 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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- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Wood Science & Technology (AREA)
- Genetics & Genomics (AREA)
- General Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- Biotechnology (AREA)
- Sustainable Development (AREA)
- Microbiology (AREA)
- Molecular Biology (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
本发明属于生物能源开发利用领域，具体涉及一种具有甲烷原位富集功能的沼气发酵工艺，难生物降解原料由进料口(1)进入鼓风式脱碳器(2)内进行水解产酸发酵，酸化液由进料泵(5)泵入到厌氧反应器(6)内进行产甲烷发酵，溶解了CO2的发酵液由循环泵(7)泵到鼓风式脱碳器(2)内，利用鼓风机(4)吹脱发酵液中的CO2后，发酵液重新回流到厌氧反应器(6)；易生物降解原料由进料泵(5)泵入到厌氧反应器(6)内进行沼气发酵，溶解了CO2的发酵液由循环泵(9)泵到真空式脱碳器(10)内释放出CO2后重新回流到厌氧反应器(6)；两种路线均可产生CH4含量＞85％的沼气。本发明解决了厌氧发酵所产沼气甲烷含量低的问题。
The invention belongs to the field of bioenergy development and utilization, and specifically relates to a methane fermentation process with the function of in-situ enrichment of methane, in which refractory biodegradable raw materials enter a blast decarburizer (2) through a feed port (1) for hydrolysis to produce Acid fermentation, the acidification liquid is pumped into the anaerobic reactor (6) by the feed pump (5) to carry out methanogenic fermentation, and the fermented liquid dissolved in CO is pumped by the circulation pump (7) to the blower type decarburizer ( 2), after using the blower (4) to blow off the CO2 in the fermentation liquid, the fermentation liquid returns to the anaerobic reactor (6); the easily biodegradable raw material is pumped into the anaerobic reactor by the feed pump (5) (6) carry out biogas fermentation, and dissolved CO The fermented liquid is pumped into the vacuum type decarburizer (10) by the circulating pump (9) to release CO After returning to the anaerobic reactor (6); All routes can produce biogas with CH 4 content>85%. The invention solves the problem of low content of biogas methane produced by anaerobic fermentation.
Description
Technical field
The invention belongs to bioenergy development and use field, be specifically related to a kind of marsh gas fermentation process with methane in-situ enrichment function.
Background technology
Utilize in the biogas of various organic waste anaerobically fermenting production and contain 30%～40% CO usually
2In order to improve the using value of biogas, with this part CO
2Remove and produce high CH
4Biogas, promptly biological methane gas has become an important directions of bioenergy development in order to instead of natural gas.A large amount of biological methane gas gas station has been arranged in commercial operation in Sweden and Germany.
Mainly contain methods such as pressure swing adsorption process (PSA method), absorption process and membrane separation process in the method that realizes commercial applications aspect the biogas purification both at home and abroad at present.Pressure swing adsorption process is meant under pressurized conditions and makes CO
2Thereby be adsorbed on adsorbent surfaces such as gac or molecular sieve and remove CO in the biogas
2, the mode by decompression in utilizing process makes adsorbent reactivation, and biogas purification factory is usually with 4,6 or 8 in parallel uses of pressure swing adsorption decarbonization tower.When adopting the PSA method, because H
2The process that S is adsorbed agent absorption is irreversible, and the existence of moisture also can damage the structure of sorbent material, and therefore, biogas need dewater and the desulfurization processing before entering the pressure swing adsorption decarbonization tower.Absorption process is to utilize CO
2In absorption liquid, has the CH of ratio
4These characteristics of stronger solvability realize the separation of the two.Absorption process mainly contains WATER-WASHING METHOD, chemical absorption method and physical absorption method.Chemical absorption method is meant with weakly alkaline solution as absorption agent CO
2Absorption is isolating method from biogas, absorption agent and CO in the absorption process
2Chemical reaction has taken place.Chemical absorption method mainly contains amino hydramine method (most typical is the N methyldiethanol amine method, i.e. the MDEA method), the thermokalite potassium method (G-V method) and the ammoniacal liquor absorption process of improvement.The physical absorption method is to utilize CO
2The bigger characteristic of solubleness in absorption agent is with the method for its removal.During absorption general adopt high pressure (2～5MPa) and cold condition, the way that desorb is then adopted decompression or heated up.Selecting the excellent absorption agent is the key of this method.Typical physical absorption method has pressurization WATER-WASHING METHOD, N methylpyrrolidone process, polyglycol dimethyl ether process (Selexol method), low-temp methanol method (Rectisol method) and propylene carbonate method (Flour method) etc.Membrane separation process utilizes all gases component in the biogas to select the difference of transmission rates with CH to permeable membrane
4With CO
2Separate.This method has characteristics such as separation efficiency height, energy consumption is low, equipment is simple, Technological adaptability is strong.Separation of C O
2Mould material adopt cellulose acetate membrane, polysulfone membrane, poly (ether sulfone) film, poly-peptide film and polyamide membrane etc. usually.The membrane separation technique device is simple, and the output investment ratio solvent absorption is low, but is difficult to obtain highly purified CO
2
The common problem that aforesaid method exists is that the purifying system is comparatively complicated, system's operation energy consumption height, and these methods only just have economic feasibility when being applied to the large-sized biogas engineering, and this becomes the major obstacle that these biogas purification techniquess of restriction are applied.
Summary of the invention
The objective of the invention is by for anaerobic reactor connects a decarbonizer anaerobic fermented liquid to be recycled to decarbonizer, utilization vacuumizes or the mode of air blast removes the CO that is dissolved in the fermented liquid
2, be implemented in in-situ enrichment CH in the anaerobic fermentation process
4Purpose, the high CH of production
4The biogas of content can be directly or the alternative fuel of back as Sweet natural gas of further purifying.
Purpose of the present invention can realize by following measure:
A kind of marsh gas fermentation process with methane in-situ enrichment function.Treated fermentation raw material is sent into anaerobic reactor and is carried out biogas fermentation, the CO that fermentation produces
2Be dissolved in the fermented liquid, extract anaerobic fermented liquid from the top of reactor, spray in the decarbonizer, by vacuumizing or the mode of air blast makes the CO that is dissolved in the fermented liquid
2Discharge and discharge decarbonizer, discharged CO
2Fermented liquid be back to the reactor from anaerobic reactor bottom again, continue producing methane through anaerobic fermentation on the one hand, the CO in the biogas is produced in dissolving again simultaneously
2, in a word, make anaerobically fermenting produce most of CO in the biogas in this way
2From decarbonizer, discharge, thereby make CH in the biogas that anaerobic reactor produced
4Content is brought up to more than 85%, has realized producing the purpose of high quality biological flue gas.
The present invention can be used for handling readily biodegradable raw material such as organic waste water and handles the not fermentation of readily biodegradable raw material such as stalk.
Be used to handle stalk etc. not during the readily biodegradable raw material, at first will be added in the blowing-type decarbonizer (2) by opening for feed (1) through pretreated raw material, raw material is hydrolyzed under the effect of aerobic microbiological and amphimicrobe and produces acid, acidizing fluid is pumped in the anaerobic reactor (6) via fresh feed pump (5) and produces methane fermentation, produces the CO that produces in the methane fermentation process
2Be dissolved in the fermented liquid, utilize recycle pump (7) will be dissolved with CO from the top of anaerobic reactor
2Fermented liquid be recycled in the blowing-type decarbonizer (2), utilize gas blower (4) that the bottom of air from blowing-type decarbonizer (2) is blown into, carry out reverse the contact with anaerobic fermented liquid, utilize CO in fermented liquid and the air
2Partial pressure difference with the most of CO in the fermented liquid
2Be discharged in the air, finally enter atmosphere from Waste gas outlet (8).The fermentation raw material hydrolysis is produced the residue of acid back generation and is discharged blowing-type decarbonizer (2) by slag-drip opening (3).Anaerobic reactor (6) produces is rich in CH
4Biogas discharge by escape pipe (12), finish the feed liquid of producing methane fermentation and discharge by rising pipe (13).
When being used to handle readily biodegradable raw material such as organic waste water, at first will be pumped in the anaerobic reactor (6) by fresh feed pump (5) through pretreated raw material, raw material is finished hydrolysis successively, produces acid and is produced methane process, the CO that produces in the fermenting process
2Be dissolved in the fermented liquid, utilize recycle pump (9) will be dissolved with CO from the top of anaerobic reactor
2Fermented liquid be recycled in the vacuum type decarbonizer (10), utilize vacuum pump (11) to make vacuum type decarbonizer (10) keep negative pressure state, thereby make the CO that is dissolved in the fermented liquid
2Discharge, and finally be discharged in the atmosphere, through taking off CO by vacuum pump (11)
2The fermented liquid of handling is back in the anaerobic reactor (6) again by fresh feed pump (5).Anaerobic reactor (6) produces is rich in CH
4Biogas discharge by escape pipe (12), finish the feed liquid of biogas fermentation and discharge by rising pipe (13).
Methane fermentation system involved in the present invention has the characteristics of following several respects:
1. the present invention utilizes CH
4And CO
2The significant difference of solubleness in the aqueous solution by connecting a decarbonizer on the anaerobic reactor next door, has realized in-situ enrichment CH
4Purpose.
When 2. the present invention adopts the blowing-type decarbonizer, CO in removing fermented liquid
2The time, can also realize the function of biological desulphurization, to remove the H in the biogas
2S.
3. when difficult for biological degradation raw materials such as processing stalk, decarbonizer can be designed to an acidogenic reactor, in air blast, realize difficult anaerobic biodegradation composition in the stalk---the aerobic decomposition of xylogen is reached the purpose that improves difficult for biological degradation raw material anaerobe transformation efficiencys such as stalk.
4. anaerobic fermentation system produces is rich in CH
4Biogas can be directly as the alternative fuel of Sweet natural gas.
Description of drawings
Fig. 1 is the process flow sheet that the present invention has the marsh gas fermentation process of methane in-situ enrichment function.
Embodiment
Below detailed explanation only be to set forth universal principle of the present invention, and nonrestrictive, can be in the actual application, and gas equipment is reasonably adjusted and revised the particular cases such as requirement of biogas quality according to the character of fermentation raw material.
Embodiment 1
At first maize straw is cut into 2～3cm, and to adjust C/N according to anaerobically fermenting appropriate nutrition proportioning be 15～20: 1, deployed raw material is added in the blowing-type decarbonizer (2) by opening for feed (1), having cultivated hydrolysis in the blowing-type decarbonizer (2) produces zymogenic bacteria such as acid or is added with such inoculum, the temperature of control blowing-type decarbonizer (2) is 38～40 ℃, maize straw is hydrolyzed under the effect of aerobic microbiological and amphimicrobe and produces acid, acidizing fluid is pumped in the anaerobic reactor (6) via fresh feed pump (5) and produces methane fermentation, anaerobic reactor adopts up-flow anaerobic sludge blanket (UASB), leavening temperature is controlled at 38 ℃, and organic loading is controlled at 6～10kgCOD/ (m
3D), the pH value of fermented liquid is controlled at 6.8～7.2, produces the CO that produces in the methane fermentation process
2Be dissolved in the fermented liquid, utilize recycle pump (7) will be dissolved with CO from the top of UASB
2Fermented liquid be recycled in the blowing-type decarbonizer (2), utilize gas blower (4) that the bottom of air from blowing-type decarbonizer (2) is blown into, the air capacity that blasts makes the dissolved oxygen content that enters anaerobic reactor with the backflow fermented liquid be controlled at 40mg/ (L
ReactorD) below, contain CO
2Waste gas finally enter atmosphere from Waste gas outlet (8).The maize straw hydrolysis is produced the residue of acid back generation and is discharged blowing-type decarbonizer (2) by slag-drip opening (3).The CH that anaerobic reactor (6) produces
4The biogas of content＞85% is discharged by escape pipe (12), finishes the feed liquid of producing methane fermentation and is discharged by rising pipe (13).
Embodiment 2
To be pumped in the anaerobic reactor (6) by fresh feed pump (5) through the pig farm fecal sewage that grid is handled and sand setting is handled, anaerobic reactor (6) adopts anaerobic filter (AF), and leavening temperature is controlled at 38 ℃, and organic loading is controlled at 5～8kgCOD/ (m
3D), the pH value of fermented liquid is controlled at 6.8～7.2, and sewage is finished hydrolysis successively, produces acid and product methane process and produced biogas, the CO in the biogas in AF
2Be dissolved in the fermented liquid, utilize recycle pump (9) will be dissolved with CO from the top of AF
2Fermented liquid be recycled in the vacuum type decarbonizer (10), utilize vacuum pump (11) to make vacuum type decarbonizer (10) form vacuum, vacuum degree control-0.08MPa～-0.09MPa, thereby make the CO that is dissolved in the fermented liquid
2Discharge, and finally be discharged in the atmosphere, through taking off CO by vacuum pump (11)
2The fermented liquid of handling is back in the AF again by fresh feed pump (5).The CH that AF produces
4The biogas of content＞90% is discharged by escape pipe (12), finishes the feed liquid of biogas fermentation and is discharged by rising pipe (13).
Claims (6)
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517107A (en) * | 2011-12-08 | 2012-06-27 | 华北电力大学 | Technological method for producing biogas by utilization of organic matter |
| CN103382488A (en) * | 2013-07-26 | 2013-11-06 | 朱兆华 | Method for preparing methane by using straws and degradable garbage |
| CN104003842A (en) * | 2014-05-16 | 2014-08-27 | 沈阳航空航天大学 | Cyclic utilization system for methanol preparation by use of catalysis of tail gases of aerobic and anaerobic digestion |
| CN105602838A (en) * | 2016-02-02 | 2016-05-25 | 中国科学院成都有机化学有限公司 | Biogas methanation decarbonization system and method |
| CN108977248A (en) * | 2018-09-18 | 2018-12-11 | 苏州科特环保股份有限公司 | A kind of biogas in-line purification device |
| CN109628182A (en) * | 2018-11-28 | 2019-04-16 | 安徽天马环保装备有限公司 | A kind of biogas pressure washing method of purification and system |
| CN112723681A (en) * | 2021-01-08 | 2021-04-30 | 山东问清环境科技有限公司 | A multistage anaerobic system for tail dish thick liquid is handled |
| CN113966387A (en) * | 2019-04-08 | 2022-01-21 | 伊诺西斯公司 | Method and apparatus for producing methane |
| 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 |
Citations (3)
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| CN108977248A (en) * | 2018-09-18 | 2018-12-11 | 苏州科特环保股份有限公司 | A kind of biogas in-line purification device |
| CN109628182A (en) * | 2018-11-28 | 2019-04-16 | 安徽天马环保装备有限公司 | A kind of biogas pressure washing method of purification and system |
| CN113966387A (en) * | 2019-04-08 | 2022-01-21 | 伊诺西斯公司 | Method and apparatus for producing methane |
| CN113966387B (en) * | 2019-04-08 | 2024-04-12 | 伊诺西斯公司 | Method and apparatus for producing methane |
| CN112723681A (en) * | 2021-01-08 | 2021-04-30 | 山东问清环境科技有限公司 | A multistage anaerobic system for tail dish thick liquid is handled |
| 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 |
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