CN106754294A - A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production - Google Patents
A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production Download PDFInfo
- Publication number
- CN106754294A CN106754294A CN201611212727.1A CN201611212727A CN106754294A CN 106754294 A CN106754294 A CN 106754294A CN 201611212727 A CN201611212727 A CN 201611212727A CN 106754294 A CN106754294 A CN 106754294A
- Authority
- CN
- China
- Prior art keywords
- solid
- vinegar grain
- temperature
- biogas
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 239000000052 vinegar Substances 0.000 title claims abstract description 93
- 235000021419 vinegar Nutrition 0.000 title claims abstract description 93
- 230000029087 digestion Effects 0.000 title claims abstract description 59
- 239000007788 liquid Substances 0.000 title claims abstract description 55
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 82
- 238000000855 fermentation Methods 0.000 claims abstract description 55
- 239000007787 solid Substances 0.000 claims abstract description 38
- 230000004151 fermentation Effects 0.000 claims abstract description 30
- 238000010438 heat treatment Methods 0.000 claims abstract description 29
- 238000005406 washing Methods 0.000 claims abstract description 28
- 239000007921 spray Substances 0.000 claims abstract description 18
- 239000002994 raw material Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 239000000945 filler Substances 0.000 claims description 19
- 239000000463 material Substances 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- 238000011026 diafiltration Methods 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000003546 flue gas Substances 0.000 claims description 9
- 238000009413 insulation Methods 0.000 claims description 8
- 239000002002 slurry Substances 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 7
- 238000012546 transfer Methods 0.000 claims description 7
- 238000001027 hydrothermal synthesis Methods 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 238000010563 solid-state fermentation Methods 0.000 claims description 5
- 244000005700 microbiome Species 0.000 claims description 4
- 238000005842 biochemical reaction Methods 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 3
- 238000004321 preservation Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims 1
- 239000006210 lotion Substances 0.000 abstract description 12
- 150000007524 organic acids Chemical class 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 21
- 241000589516 Pseudomonas Species 0.000 description 7
- 239000002253 acid Substances 0.000 description 4
- 150000001720 carbohydrates Chemical class 0.000 description 4
- 238000011068 loading method Methods 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 3
- 239000002054 inoculum Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 238000002255 vaccination Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 241000205265 Methanospirillum Species 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- OFPXSFXSNFPTHF-UHFFFAOYSA-N oxaprozin Chemical compound O1C(CCC(=O)O)=NC(C=2C=CC=CC=2)=C1C1=CC=CC=C1 OFPXSFXSNFPTHF-UHFFFAOYSA-N 0.000 description 2
- 230000002572 peristaltic effect Effects 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 235000001674 Agaricus brunnescens Nutrition 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 241001478240 Coccus Species 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 241000628997 Flos Species 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 241000305995 Methanimicrococcus Species 0.000 description 1
- 241001233112 Methanocalculus Species 0.000 description 1
- 241001174354 Methanocella Species 0.000 description 1
- 241000204999 Methanococcoides Species 0.000 description 1
- 241000203353 Methanococcus Species 0.000 description 1
- 241000203400 Methanocorpusculum Species 0.000 description 1
- 241000204639 Methanohalobium Species 0.000 description 1
- 241000658999 Methanolinea Species 0.000 description 1
- 241000192041 Micrococcus Species 0.000 description 1
- 229920002522 Wood fibre Polymers 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000001963 growth medium Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000010335 hydrothermal treatment Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000009790 rate-determining step (RDS) Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012549 training Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/16—Solid state fermenters, e.g. for koji production
-
- 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
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/58—Reaction vessels connected in series or in parallel
-
- 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
- C12M29/02—Percolation
-
- 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
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
- C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
-
- 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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
-
- 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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/20—Heating; Cooling
-
- 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
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
- C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
- C12P5/023—Methane
-
- 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
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Wood Science & Technology (AREA)
- Zoology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
- General Engineering & Computer Science (AREA)
- Microbiology (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Sustainable Development (AREA)
- Molecular Biology (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Clinical Laboratory Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention relates to a kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production, belong to technical field of biological fermentation.Described device mainly includes：Solid-state fermenter, thermophilic digestion device, packed column reactor, biogas purifier, solid-liquid separating machine, cistern；The invention also discloses a kind of method that vinegar grain solid-liquid split-phase anaerobic digestion methane production is carried out using described device, mainly comprise the following steps：(1) vinegar grain is carried out into spray washing in solid-state fermenter；(2) the washing vinegar grain High-temperature water heat treatment after filtering；(3) water lotion intermediate temperature anaerobic fermentation；(4) high-temperature solid fermentation；(5) marsh gas purifying is utilized.The present invention can not only realize vinegar grain solid-liquid split-phase anaerobic digestion, the features such as easily washing separation abundant herein in connection with vinegar grain organic acid content, other raw materials need not be added in fermentation process, realize hydro-thermal circulation, it is cost-effective, therefore the technology of traditional vinegar grain anaerobic fermentation is breached, the ability for producing biogas is improve.
Description
Technical field
The present invention relates to discarded object biofermentation technique, and in particular to a kind of vinegar grain solid-liquid split-phase anaerobic digestion methane production
Apparatus and method, belong to technical field of biological fermentation.
Background technology
Vinegar grain is using the organic waste discharged during grain raw material production vinegar, in recent years, with country's vinegar processed
Greatly developing for industry, produces the vinegar grain of discharge up to 3,000,000 tons every year, with acid big (acetic acid content 36000mg/kg), slightly
The features such as content of cellulose (25.78% (butt)) high, gross protein value low (12.79% (butt)), difficult decomposition.Above-mentioned spy
Point causes that current vinegar grain processing mode be present, for example, fraction vinegar grain is used as animal feed and edible mushroom is planted
Training material, as feed drying high cost；Culture medium of edible fungus consumption is few, it is impossible to from substantial solve problem；Most of vinegar grain
Go out of use, for a long time, landfill is its main processing mode, and the content of organic matter higher causes to be produced during landfill
A large amount of sour water leakage pollution underground water and edaphic percolate and the greenhouse gas methane of the unordered discharge of generation.Effective place
Reason vinegar grain, reduces the pollution of environment, realizes the recycling of vinegar grain, is the important way for solving vinegar industry discarded object processed in recent years
Footpath.
Anaerobic fermentation is the frontier of domestic and international Recent study, can be generated while degradation of organic substances matter hydrogen,
The biomass energy gas such as methane, is to improve one of environment, effective way of utilization of waste as resource.Vinegar grain spy maximum in itself
Point is that low percentages of protein, crude fiber content be higher, acetic acid content is abundant.Anaerobic digestion includes 4 processes：Extracellular hydrolysis,
Produce acid, produce acetic acid and methane phase, traditional homogenous anaerobic digestion can only process relatively low fermentation raw material concentration (less than 20%), vinegar
The poor slag of grain is not easily decomposed and acetic acid content is abundant, and homogenous anaerobic digestion methane phase process is easily made in a reactor
Crusted into vinegar grain and floated, system is easily acidified, and causes the stability and gas producing efficiency of vinegar grain biogas fermentation relatively low.
Vinegar grain raw material is belonging to organic acid content raw material higher, and whole anaerobic digestion process methane phase process is rate-limiting step
Suddenly, cause vinegar grain and easily produce organic acid to suppress when carrying out single-phase continuous Anaerobic Digestion, lag phase is larger.In order to avoid having
Machine acid suppresses, and traditional homogenous anaerobic digestion can only the low yield operation under relatively low load.Therefore, unrestraint efficient anaerobic is developed
Firedamp gas equipment is produced in digestion and technique turns into the key that the vinegar residue resource of high content organic acid is processed.
The content of the invention
It is a primary object of the present invention to the problem for overcoming prior art to exist, there is provided a kind of vinegar grain solid-liquid split-phase anaerobism disappears
Change the apparatus and method for producing biogas, effectively using the organic acid of vinegar grain abundant raw material can be conducive to vinegar grain methane engineering technology
Popularization and application, reduce environmental pollution.
The present invention provides a kind of device of vinegar grain solid-liquid split-phase anaerobic digestion methane production, and the device mainly includes：Solid-state is sent out
Fermentation tank 2, thermophilic digestion device 4, packed column reactor 6, biogas purifier 9, solid-liquid separating machine 11, cistern；
The lower end of the solid-state fermenter 2 is placed with solid diafiltration bed 3, and slag-drip opening 16, and bottom connection retaining are arranged at bottom
The one end of pond A 5, the inner upper end of solid-state fermenter 2 is installed with spray head 1, is connected with the one end of cistern B 8, and there is biogas on top
Outlet is connected with biogas purifier 9, and circulation line 17 connects the bottom of solid-state fermenter 2 and upper end respectively, forms circulation canal；
The bottom of described filler reactor 6 is connected with the other ends of cistern A 5, the position dress on the middle part of packed column reactor 6
There is fiberfill 7, fiberfill 7 can adhere to methanogen, and the upper end liquid outlet of packed column reactor 6 connects cistern B 8, and fills out
Material reactor 6 upper end liquid outlet is located on fiberfill 7, and methane outlet and biogas purifier 9 are arranged at the top of packed column reactor 6
Connection, the outer wall of packed column reactor 6 have one layer of heat preservation layer, heat coil pipe 12 and connected with the heat-insulation layer, the upper end of packed column reactor 6 with consolidate
The one end of liquid separator 11 is connected, and the bottom of packed column reactor 6 is provided with discharge port 15；
Thermophilic digestion device 4, solid-state fermenter 2 and packed column reactor 6 are connected with heat-exchanger rig 10, and heat-exchanger rig 10 is high temperature
Boiling vessel 4 and packed column reactor 6 provide heat.Heat-exchanger rig 10 can also be received in thermophilic digestion device 4 and solid-state fermenter 2
Waste heat.
Further, the thermophilic digestion device 4 is connected by the first mud-water- to-water heat exchanger 13 with heat-exchanger rig 10, solid-state hair
Fermentation tank 2 is connected by the second mud-water- to-water heat exchanger 14 with heat-exchanger rig 10, and packed column reactor 6 is filled by heating coil pipe 12 with heat exchange
10 are put to be connected.
Further, described device also includes a boiler 18, can be transferred in boiler 18 by the biogas residue after separation of solid and liquid
Row drying and burning；The top exhanst gas outlet of boiler 18 is connected with heat exchanger 10, and boiler 18 forms high-temperature steam and is stored in after burning
It is used for High-temperature water heat treatment in the heat exchanger 10.
Present invention also offers a kind of method that vinegar grain solid-liquid split-phase anaerobic digestion methane production is carried out using said apparatus, should
Method mainly comprises the following steps：
(1) vinegar grain is carried out into spray washing in solid-state fermenter 2, solid-state fermenter is percolated bed, vinegar grain dress using solid
Fill in above the diafiltration filler of diafiltration bed, have porous plate under diafiltration filler, the water for coming from spray head carries out sprinkle water to vinegar grain
Wash, washing separates soluble carbohydrate and acetic acid, and percolate is formed by diafiltration filler and porous plate and store in cistern A 5
In；
(2) vinegar grain after spray washing filtering is transferred to thermophilic digestion device 4 carries out High-temperature water heat treatment, a fixed number in vinegar grain
The crude fibre of amount is decomposed into the carbohydrate of small molecule；
(3) percolate in step (1) is pumped to packed column reactor 6 from cistern A 5 carries out intermediate temperature anaerobic fermentation, retaining
Pond A and packed column reactor bottom pass through pump and pipeline communication；Packed column reactor has fiberfill 7, fiberfill energy on middle part
Attachment methanogen well, percolate is decomposed by the consumption of methanogen, produces methane and carbon dioxide, and spillage is from filling out
The upper end outlet outflow savings of material reactor stay secondary vinegar grain washing to use, in the reaction of realization water in another water tank B 8
Circulation；The methane and carbon dioxide of generation carries out biogas utilization after being purified through biogas purifier 9 from the upper outlet of packed column reactor；
(4) vinegar grain carries out high-temperature solid fermentation in transferring to solid-state fermenter 2 after High-temperature water heat treatment；High-temperature solid is sent out
The biogas that ferment is produced is passed through after biogas purifier 9 is purified by the outlet on the top of solid-state fermenter 2 and realizes biogas utilization；High temperature is consolidated
State residues are transferred to solid-liquid separating machine 11 to carry out separation of solid and liquid and obtains biogas slurry and biogas residue, and biogas slurry backflow is passed through described filler
Reactor 6 carries out intermediate temperature anaerobic fermentation and produces biogas, and spillage exists from the outflow savings of packed column reactor upper end outlet after consumption is decomposed
In another cistern B 8, the washing of secondary vinegar grain is stayed to use, the reaction interior circulation of realization water, biogas is from the top of packed column reactor 6
Into biogas purifier 9.
Further, the waste heat after High-temperature water heat treatment and high-temperature solid ferment is reclaimed by heat-exchanger rig 10 and is step
(3) intermediate temperature anaerobic fermentation is quenched to be heated；The recycling step is：Reclaimed from thermophilic digestion by the first mud-water- to-water heat exchanger 13
The heat of the material of discharge and the fermentation of the discharge from the solid-state fermenter 2 is reclaimed by the second mud-water- to-water heat exchanger 14 in device 4
The heat of residue, forms hot water storage in the heat exchanger 10, and the hot water is flowed into anaeration in normal temperature through heating coil pipe 12
It is mesophilic anaerobic digestion temperature raising and maintaining in the heat-insulation layer of the outer wall of fermentation tank 6.
Further, by high-temperature solid fermentation process produce percolate self-loopa, by the percolate containing microorganism with
Vinegar grain mixing in solid-state fermenter 2, promotes mass transfer, heat transfer and the generation of biochemical reaction of strain and raw material.
Further, the biogas residue that separation of solid and liquid is formed is moved into boiler 18 to dry and burnt, the high temperature that will be produced steams
Vapour and high-temperature flue gas reclaim the High-temperature water heat treatment for the step (2), part combustion high temperature flue gas by heat-exchanger rig 10
Heat can be used for biogas residue drying and use.The recycling step is：By boiler 18 to the biogas residue in high-temperature solid residues
Dry and burnt, the moisture that high-temperature flue gas are taken away in biogas residue forms high-temperature steam and is stored in the heat exchanger 10, high temperature
Steam is used for above-mentioned steps (2) High-temperature water heat treatment, and part combustion high temperature flue gas heat is used for drying, and the ash content of burning is used
Make vegetation ash fertilizer.
Further, in the step (1) according to liquid-solid than carrying out spray washing for 6-12mL/g, by acetic acid and solvable
Property carbohydrate carries out separated and dissolved.
Further, the temperature of the High-temperature water heat treatment in the step (2) is 120-160 DEG C, the time of hydro-thermal process
It it is 30 minutes, temperature is preferably 120 DEG C.
Further, the temperature of the intermediate temperature anaerobic fermentation of the step (3) is 35-38 DEG C, and hydraulic detention time is 1-2
My god.
Further, the temperature of the high-temperature solid fermentation of the step (4) is 50-55 DEG C, and residence time of material is 15-20
My god.
The methanogen includes but is not limited to methane Micrococcus (methanimicrococcus), methane class Coccus
(methanococcoides), methane salt Pseudomonas (methanohalobium), salt Methanococcus
(halomethanococcus), methane born of the same parents Pseudomonas (methanocella), methane rope Pseudomonas (methanolinea), methane gravel
Pseudomonas (methanocalculus), methanospirillum category (methanospirillum), methane grain Pseudomonas
(methanocorpusculum) etc., the Pseudomonas can be used alone or using mixing Pseudomonas.
Above-mentioned technical proposal can be seen that the invention has the advantages that：
(1) anaerobic digestion is carried out using solid-liquid split-phase, while realizing thermal cycle and water circulation, energy saving again；
(2) using the spray washing of solid-state fermenter, the soluble saccharide that can easily utilize anaerobic fermentation and acetic acid are washed
Separate；
(3) advanced water-filling is washed separation and carries out hydrothermal treatment process again and avoid carrying out hydro-thermal process to raw material and being produced because direct
Raw mortifier occurs, and improves the efficiency of hydro-thermal process.Hydro-thermal process is now carried out, water vapour can be directly acted on very
The cellulose and lignin of positive difficult degradation are so as to improve wood fibre structural damage degree.
(4) High-temperature water heat treatment vinegar grain and high-temperature solid residues residual heat integrative are utilized and intermediate temperature anaerobic fermentation phase
With reference to, the comprehensive energy consumption of system is reduced, improve systematic heat utilization efficiency.
The device and process can not only realize vinegar grain solid-liquid split-phase anaerobic digestion, herein in connection with vinegar grain organic acid content
The features such as abundant easily washing separation, other raw materials need not be added in fermentation process, realize hydro-thermal circulation, it is cost-effective therefore prominent
The technology of traditional vinegar grain anaerobic fermentation has been broken, the ability for producing biogas has been improve.
Brief description of the drawings
Fig. 1 is a kind of installation drawing of vinegar grain solid-liquid split-phase anaerobic digestion methane production of the invention；
Fig. 2 is a kind of method flow diagram of vinegar grain solid-liquid split-phase anaerobic digestion methane production of the invention.
Reference：
1. spray head, 2. solid-state fermenter, 3. solid diafiltration bed, 4. thermophilic digestion device, 5. cistern A, 6. filler reaction
Device, 7. fiberfill, 8. cistern B, 9. biogas purifier, 10. heat-exchanger rig, 11. solid-liquid separating machines, 12. heat coil pipe,
13. first mud-water- to-water heat exchanger, 14. second mud-water- to-water heat exchanger, 15. discharge ports, 16. slag-drip openings, 17. circulation lines, 18. pots
Stove.
Specific embodiment
Below in conjunction with the accompanying drawings, specific embodiment of the invention is described in detail.
Embodiment 1
As shown in figure 1, a kind of device of vinegar grain solid-liquid split-phase anaerobic digestion methane production, mainly includes solid-state fermenter 2, it is high
Warm boiling vessel 4, packed column reactor 6, biogas purifier 9, solid-liquid separating machine 11 and cistern 5,8；The bottom of the solid-state fermenter 2
The one end of connection cistern A 5, the inner upper end of solid-state fermenter 2 is installed with spray head 1, and lower end is placed with solid diafiltration bed 3；
The other ends of cistern A 5 are connected with the bottom of packed column reactor 6, and the position of packed column reactor 6 is equipped with fiberfill 7, fiberfill 7
On be attached with methanogen, the upper end liquid outlet connection cistern B 8 of packed column reactor 6, the upper end liquid of described filler reactor 6
Outlet is located on fiberfill 7；The other ends of cistern B 8 are connected with spray head 1 in solid-state fermenter 2；Thermophilic digestion device 4,
Solid-state fermenter 2 and packed column reactor 6 are connected with heat-exchanger rig 10, wherein, thermophilic digestion device 4 passes through the first mud-water- to-water heat exchanger
13 are connected with heat-exchanger rig 10, and solid-state fermenter 2 is connected by the second mud-water- to-water heat exchanger 14 with heat-exchanger rig 10, filler reaction
Device 6 is connected by heating coil pipe 12 with heat-exchanger rig 10；The one end of solid-liquid separating machine 11 is connected with the upper end of packed column reactor 6, can be by
Liquid in solid-liquid separating machine is pumped into packed column reactor 6, is reclaimed from thermophilic digestion device 4 by the first mud-water- to-water heat exchanger 13
The heat of the material of discharge, the residues of the discharge from the solid-state fermenter 2 are reclaimed by the second mud-water- to-water heat exchanger 14
Heat, formed hot water storage in the heat exchanger 10, the outer wall of packed column reactor 6 have one layer of heat preservation layer, passed through by by hot water
Cross that heat coil pipe 12 to flow into the heat-insulation layer of intermediate temperature anaerobic fermentation tank 6 be mesophilic anaerobic digestion temperature raising and maintaining.
Said apparatus also include a boiler 18, the biogas residue after separation can be transferred in boiler 18 and be dried and burnt；
The top exhanst gas outlet of boiler 18 is connected with heat exchanger 10, and boiler 18 forms high-temperature steam and is stored in the heat exchanger 10 after burning
For High-temperature water heat treatment.
Solid-state fermenter 2 is connected biogas purifier 9 with the top export of packed column reactor 6；The bottom end outlet of solid-state fermenter 2 connects
Circulation line 17 is connect, is connected with itself top；The bottom of solid-state fermenter 2 is provided with slag-drip opening 16, and the bottom of packed column reactor 6 is set
There is discharge port 15.
Said apparatus are used for the method flow of vinegar grain solid-liquid split-phase anaerobic digestion methane production as shown in Fig. 2 including as follows
Step：
Vinegar grain is added water in solid-state fermenter 2 according to 6-12mL/g volumes carries out spray washing, filtering water lotion storage
In cistern A 5, the washing vinegar residue after filtering carries out 30 minutes 120-160 DEG C of high-temperature water in being transferred to thermophilic digestion device 4
After heat treatment, transfer to and carry out in solid-state fermenter 2 high-temperature solid fermentation, temperature is 50-55 DEG C, residence time of material is
15-20 days；The percolate self-loopa (percolate self-loopa does not draw in fig. 2) that high-temperature solid fermentation process is produced, will contain
The percolate for having microorganism mixes with the vinegar grain in solid-state fermenter 2, promotes mass transfer, heat transfer and the biochemical reaction of strain and raw material
Generation.
Vinegar grain water lotion in cistern A5 is pumped into packed column reactor 6 carries out intermediate temperature anaerobic fermentation, by setting 1-2 days
Hydraulic detention time controls the vinegar grain water lotion sample size of packed column reactor, and the temperature of intermediate temperature anaerobic fermentation is 35-38 DEG C, filler
The top of reactor 6 is fiberfill 7, and methanogen is attached with fiberfill 7, and water lotion is consumed by methanogen and decomposed
Produce methane and carbon dioxide；
Spillage after packed column reactor anaerobic digestion is saved in another cistern B 8, stays secondary vinegar grain washing to make
With the reaction interior circulation of realization water；
High-temperature water heat treatment vinegar grain and high-temperature solid residues waste heat are reclaimed by heat-exchanger rig 10, pipe is passed sequentially through
Road connection the first mud-water- to-water heat exchanger 13, the second mud-water- to-water heat exchanger 14, packed column reactor 6 heat coil pipe 12, by first mud-
Water- to-water heat exchanger 13 is reclaimed the heat of the High-temperature water heat treatment material discharged from thermophilic digestion device 4 and is exchanged heat by the second mud-water
Device 14 reclaims the heat of the high-temperature solid residues of discharge from the solid-state fermenter 2, and is converted into hot water, by the heat
Water is mesophilic anaerobic digestion temperature raising and maintaining through heating the heat-insulation layer that coil pipe 12 is flowed into outside packed column reactor 6；
Solid state fermentation residue in solid-state fermenter 2 carries out the biogas slurry time that separation of solid and liquid is obtained by solid-liquid separating machine 11
Circulate and carry out intermediate temperature anaerobic fermentation product biogas into packed column reactor 6, biogas enters marsh gas purifying from the top export of packed column reactor 6
Device 9 carries out purified treatment；Spillage savings stay secondary vinegar grain washing to use, realization water in another cistern B 8 after digestion
Reaction interior circulation；
Biogas residue in high-temperature solid residues is dried and burnt by boiler 18, will produce high-temperature steam and height
Warm flue gas is stored in the heat-exchanger rig 10, the vinegar grain High-temperature water heat treatment after being washed for next group, part combustion high temperature
Flue gas heat is used for drying, and boiler combustion lime-ash regards vegetation ash fertilizer；
The methane that high-temperature solid fermentation and intermediate temperature anaerobic fermentation are produced is passed through into biogas purifier 9 carries out purified treatment, only
It is used for biogas utilization after change.
With reference to embodiment, the present invention will be further described, and protection scope of the present invention is not limited to following institute
State.
Embodiment 1
The vinegar grain 100kg that vinegar factory has just produced discharge is collected, the solids content (TS) of vinegar grain is 30.01%, and volatility is solid
Body content (VS) is 28.93%, adds 500L water to carry out spray washing to vinegar grain by spray thrower 1, through being percolated the filtering washing of bed 3
Liquid is stored in cistern A 5.
Vinegar grain after being washed in solid-state fermenter 2 carries out High-temperature water heat treatment, hydro-thermal process in being transferred to thermophilic digestion device 4
Heat (steam) using come from other biogas residues drying and burning produced by high-temperature steam, control High-temperature water heat treatment temperature
It is 120 DEG C to spend, and hydrothermal conditions are 30 minutes, and thermophilic digestion device after-heat is reclaimed by mud-water- to-water heat exchanger 13, and with heat
Water form is stored in heat exchanger 10.
Active vaccination sludge is pumped into from the bottom of packed column reactor 6, acid-producing bacteria and methanogen is rich in Active vaccination sludge,
Treat that Active vaccination sludge floods the not up to spillage floss hole of fiberfill 7 and can stop adding, placement treats that microorganism is effective in two days
Attachment；Then 20L vinegar grain water lotions are added from cistern A 5 to packed column reactor 6 by peristaltic pump, by the heat in heat exchanger 10
Water is heated during the outer wall heat-insulation layer of packed column reactor 6 is pumped into by heating coil pipe 12 to the material insulation in packed column reactor 6, is increased
Temperature is to 35-38 DEG C；Vinegar grain water lotion after heating carries out intermediate temperature anaerobic fermentation, sets hydraulic detention time 2 days, filler reaction
After device end of run, adding 20L vinegar grains water lotion from cistern A 5 to packed column reactor 6 again by peristaltic pump carries out middle temperature
Anaerobic fermentation, sets hydraulic detention time 2 days；As long as there is water lotion in cistern A 5, just by this step filler is passed through always anti-
Answering device 6 to carry out intermediate temperature anaerobic fermentation produces the spillage of biogas, packed column reactor 6 to save in cistern B 8, leaves a vinegar
Grain washing is used.
Washing vinegar grain after High-temperature water heat treatment is transferred in solid-state fermenter 2 carries out high-temperature solid fermentation generation natural pond
Gas, the percolate formed in fermentation process returns solid-state fermenter 2 by the self-loopa of circulation line 17, and the heat for being carried is used for
Temperature needed for maintaining high-temperature solid fermentation, heats using electric heating cover and controls high-temperature solid fermentation temperature to solid-state fermenter
50-55 DEG C, residence time of material is 15 days, then reclaims the discharge from solid-state fermenter 2 by the second mud-water- to-water heat exchanger 14
The heat of residues, formation hot water storage is in the heat exchanger 10.Turn through the high-temperature solid residues after heat exchange
Entering solid-liquid separating machine 11 carries out separation of solid and liquid, is separated into biogas slurry and biogas residue, the treatment of biogas slurry and the processing mode of vinegar grain water lotion
Unanimously, will biogas slurry be back to the fermentation methane production of packed column reactor 6 of intermediate temperature anaerobic fermentation, by the spillage after anaerobic digestion
It is stored in another cistern B 8, gives over to vinegar grain washing next time and use；Biogas residue is dried and burnt with boiler 18, high temperature
The moisture that flue gas is taken away in biogas residue forms high-temperature steam and is stored in heat exchanger 10, and high-temperature steam is used at above-mentioned high temperature hydro-thermal
Reason, the ash content after biogas residue burning is used as vegetation ash fertilizer.
Collect the biogas of intermediate temperature anaerobic fermentation and high-temperature solid fermentation generation and purified treatment is carried out in biogas purifier 9
After utilize.After normal operation, every 30 days, part vinegar grain water lotion residue is removed from the discharge port 15 of packed column reactor.Normally
After operation, every 50 days, washing vinegar grain percolate sediment is removed from the slag-drip opening 16 of solid-state fermentation reactor.
Embodiment 2
Experimental group：With the washing vinegar grain and water lotion after High-temperature water heat treatment as raw material, using the solid-state fermenter 2 of 25L
Solid-liquid split-phase anaerobic fermentation is carried out with the packed column reactor 6 of 25L, is separately added into packed column reactor 6 before charging and tamed and dociled in advance
The biogas fermentation inoculum of change, and stablize one week, after system inoculum aerogenesis is substantially zeroed, respectively according to organic loading 1.0g
VS/L.d, 1.0g COD/L.d feed.The initial pH value in solid-state fermenter 2 and packed column reactor 6 is determined in 6.5~8 models
In enclosing, in the first load operation 30 days, in the range of 55%~65%, pH stable is in 6.5~8 scopes for methane content
It is interior.
In the second stage of fermentation load, i.e. with 2.0g VS/L.d, 2.0g COD/L.d in the 31st~60 day run
Organic loading feeds, and methane content in the range of 55%~65%, still stablize in the range of 6.5~8 by pH value.
During operating above, pond holds methane production rate steadily in the long term in 0.6~1.0L/L.d, gas production does not occur unexpected
Rapid drawdown or the phenomenon of stopping aerogenesis.
Control group：With original vinegar grain as raw material, compared with experimental group, the complete mixing flow reactor (CSTR) using 50L enters
Row long-duration test, adds the biogas fermentation inoculum tamed in advance before charging, and stablizes one week, treats that system is inoculated with produce
After gas is substantially zeroed, fed at 1~60 day according to experimental group identical feed loading mode.Determine first in reactor
Beginning pH value in the range of 6.5~8, in the first load operation 30 days, methane content in the range of 55%~60%, pH stable
In the range of 6.5~7.5.
Fed with the organic loading of 2.0g VS/L.d in the second stage of fermentation load, i.e. the 31st~60 day run,
Methane content is reduced in the range of 50%~60%, and pH value is reduced in the range of 6.5~7.0, and gas production also decreases.
During operating above, pond holds methane production rate gradually to reduce in 0.5~0.8L/L.d, in having for 2.0g VS/L.d
At the end of machine load operation is fast, gas production is substantially reduced.
It is described above a kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production.The present invention is not limited to
Above example.It is any without departing from technical solution of the present invention, i.e., what those of ordinary skill in the art were known only is carried out to it
Improve or change, belong within protection scope of the present invention.
Claims (10)
1. a kind of device of vinegar grain solid-liquid split-phase anaerobic digestion methane production, it is characterised in that the device mainly includes：Solid state fermentation
Tank (2), thermophilic digestion device (4), packed column reactor (6), biogas purifier (9), solid-liquid separating machine (11) and cistern；
Solid-state fermenter (2) lower end is placed with solid and is percolated bed (3), and slag-drip opening (16) is arranged at bottom, and bottom connects cistern A
(5) one end, solid-state fermenter inner upper end is installed with spray head (1), is connected with cistern B (8) one end, and there is biogas on top
Outlet is connected with biogas purifier (9), and circulation line (17) connects solid-state fermenter bottom and upper end respectively, forms circulation logical
Road；
Packed column reactor (6) bottom is connected with cistern A (5) other end, and the position on packed column reactor middle part is equipped with fiber
Filler (7), fiberfill can adhere to methanogen, and packed column reactor upper end liquid outlet connects cistern B (8), and filler is anti-
Device upper end liquid outlet is answered to be located on fiberfill, packed column reactor top has methane outlet to be connected with biogas purifier (9),
Packed column reactor outer wall has one layer of heat preservation layer, heats coil pipe (12) and is connected with the heat-insulation layer, and packed column reactor upper end is divided with solid-liquid
Disembarking, (11) one end is connected, and packed column reactor bottom is provided with discharge port (15)；
Thermophilic digestion device (4), solid-state fermenter (2) and packed column reactor (6) are connected with heat-exchanger rig (10) respectively.
2. the device of a kind of vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 1, it is characterised in that described
Thermophilic digestion device (4) is connected by the first mud-water- to-water heat exchanger (13) with heat-exchanger rig (10), solid-state fermenter by the second mud-
Water- to-water heat exchanger (14) is connected with heat-exchanger rig (10), and packed column reactor is connected by heating coil pipe (12) with heat-exchanger rig (10).
3. the device of a kind of vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 1, it is characterised in that also wrap
Boiler (18) is included, boiler top exhanst gas outlet is connected with heat exchanger (10).
4. a kind of device using described in claim any one of 1-3 carries out the side of vinegar grain solid-liquid split-phase anaerobic digestion methane production
Method, it is characterised in that the method comprises the following steps：
(1) vinegar grain is carried out into spray washing in solid-state fermenter, vinegar grain is loaded on above the diafiltration filler of diafiltration bed (3), oozes
There is porous plate under filter filler, coming from the water of spray head carries out sprinkle washing to vinegar grain, and by diafiltration filler and porous plate shape
In cistern A (5) being stored in into percolate；
(2) vinegar grain after spray washing filtering is transferred to thermophilic digestion device (4) carries out High-temperature water heat treatment；
(3) percolate in step (1) is pumped to packed column reactor (6) and carries out intermediate temperature anaerobic fermentation from cistern A (5)；Filler
Reactor has fiberfill (7) on middle part, and fiberfill can well adhere to methanogen, and percolate is by methanogen
Consumption is decomposed, and produces methane and carbon dioxide, and spillage is from the outflow savings of packed column reactor upper end outlet in another water tank B
(8) in, secondary vinegar grain washing is stayed to use, the reaction interior circulation of realization water；The methane and carbon dioxide of generation reacts from filler
The upper outlet of device carries out biogas utilization after being purified through biogas purifier (9)；
(4) vinegar grain is transferred to and carry out in solid-state fermenter (2) high-temperature solid fermentation after High-temperature water heat treatment, and by solid state fermentation
The percolate self-loopa that process is produced, the percolate containing microorganism is mixed with the vinegar grain in solid-state fermenter, promotes strain
Mass transfer, heat transfer and the generation of biochemical reaction with raw material；The biogas that high-temperature solid fermentation is produced is by solid state fermentation upper end
Outlet realizes biogas utilization after being passed through biogas purifier (9) purification；High-temperature solid residues are transferred to solid-liquid separating machine
(11) carry out separation of solid and liquid and obtain biogas slurry and biogas residue, biogas slurry backflow is passed through described filler reactor (6) carries out intermediate temperature anaerobic fermentation
Biogas is produced, spillage is saved in another cistern B (8) from the outflow of packed column reactor upper end outlet after consumption is decomposed, and stays secondary
Vinegar grain washing is used, and the reaction interior circulation of realization water, biogas enters biogas purifier 9 from packed column reactor (6) top.
5. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 4, it is characterised in that by first
Mud-water- to-water heat exchanger (13) reclaims the heat of the material discharged from thermophilic digestion device (4) and by the second mud-water- to-water heat exchanger (14)
Reclaim from the solid-state fermenter discharge residues heat, formed hot water storage in the heat exchanger (10),
And by the hot water through heat coil pipe (12) flow into intermediate temperature anaerobic fermentation tank wall heat-insulation layer in for mesophilic anaerobic digestion heats guarantor
Temperature.
6. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 5, it is characterised in that by solid-liquid point
Boiler (18) is moved to from the biogas residue for being formed to dry and burnt, the high-temperature steam and high-temperature flue gas that will be produced pass through heat-exchanger rig
(10) High-temperature water heat treatment for the step (2) is reclaimed, part combustion high temperature flue gas heat can be used for biogas residue drying and use.
7. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 4, it is characterised in that the step
(1) according to liquid-solid than carrying out spray washing for 6-12mL/g in.
8. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 4, it is characterised in that the step
(2) temperature of the High-temperature water heat treatment in is 120-160 DEG C, and the time of hydro-thermal process is 30 minutes.
9. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 4, it is characterised in that the step
(3) temperature of intermediate temperature anaerobic fermentation is 35-38 DEG C, and hydraulic detention time is 1-2 days.
10. the method for vinegar grain solid-liquid split-phase anaerobic digestion methane production according to claim 4, it is characterised in that the step
Suddenly the temperature of the high-temperature solid fermentation of (4) is 50-55 DEG C, and residence time of material is 15-20 days.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611212727.1A CN106754294A (en) | 2016-12-25 | 2016-12-25 | A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611212727.1A CN106754294A (en) | 2016-12-25 | 2016-12-25 | A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106754294A true CN106754294A (en) | 2017-05-31 |
Family
ID=58919644
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611212727.1A Pending CN106754294A (en) | 2016-12-25 | 2016-12-25 | A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106754294A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108531384A (en) * | 2018-07-13 | 2018-09-14 | 泸州品创科技有限公司 | Compound caproic acid bacteria solution installation for fermenting |
| CN112500983A (en) * | 2020-06-28 | 2021-03-16 | 农业农村部规划设计研究院 | Cultivation combined type dry-wet coupling biogas production fermentation equipment |
| CN112941111A (en) * | 2021-04-07 | 2021-06-11 | 中国农业科学院农业环境与可持续发展研究所 | Method for improving gas production characteristics of anaerobic dry fermentation by using biogas residue hydrothermal product |
| CN115028487A (en) * | 2022-06-28 | 2022-09-09 | 镇江恒欣生物科技有限公司 | Suspended starchiness decomposition fermentation device after solid-liquid separation of vinegar residue and use method thereof |
| CN115488140A (en) * | 2022-09-09 | 2022-12-20 | 中节能(肥西)环保能源有限公司 | System and method for treating kitchen garbage by coupling tidal fermentation percolation bed and efficient anaerobic reactor |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2820862Y (en) * | 2005-05-27 | 2006-09-27 | 魏晓路 | Feedback type organic waste bilogical fermenting device |
| CN101012436A (en) * | 2007-01-31 | 2007-08-08 | 南京大学 | Anaerobic reactor for processing lignocellulose raw material |
| CN102703515A (en) * | 2012-06-04 | 2012-10-03 | 北京化工大学常州先进材料研究院 | Method for producing biogas through anaerobic digestion of fruit and vegetable waste |
| CN104651218A (en) * | 2015-01-27 | 2015-05-27 | 深圳市海吉星环保有限责任公司 | Coupling utilization system and method of anaerobic fermentation of fruit and vegetable wastes and afterheat of bio-gas generator |
| CN104974927A (en) * | 2015-07-25 | 2015-10-14 | 中国科学院成都生物研究所 | Coupled system for preparing straw biogas and utilizing power generation waste heat |
-
2016
- 2016-12-25 CN CN201611212727.1A patent/CN106754294A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2820862Y (en) * | 2005-05-27 | 2006-09-27 | 魏晓路 | Feedback type organic waste bilogical fermenting device |
| CN101012436A (en) * | 2007-01-31 | 2007-08-08 | 南京大学 | Anaerobic reactor for processing lignocellulose raw material |
| CN102703515A (en) * | 2012-06-04 | 2012-10-03 | 北京化工大学常州先进材料研究院 | Method for producing biogas through anaerobic digestion of fruit and vegetable waste |
| CN104651218A (en) * | 2015-01-27 | 2015-05-27 | 深圳市海吉星环保有限责任公司 | Coupling utilization system and method of anaerobic fermentation of fruit and vegetable wastes and afterheat of bio-gas generator |
| CN104974927A (en) * | 2015-07-25 | 2015-10-14 | 中国科学院成都生物研究所 | Coupled system for preparing straw biogas and utilizing power generation waste heat |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108531384A (en) * | 2018-07-13 | 2018-09-14 | 泸州品创科技有限公司 | Compound caproic acid bacteria solution installation for fermenting |
| CN108531384B (en) * | 2018-07-13 | 2023-08-08 | 泸州品创科技有限公司 | Composite caproic acid bacterial liquid fermentation device |
| CN112500983A (en) * | 2020-06-28 | 2021-03-16 | 农业农村部规划设计研究院 | Cultivation combined type dry-wet coupling biogas production fermentation equipment |
| CN112941111A (en) * | 2021-04-07 | 2021-06-11 | 中国农业科学院农业环境与可持续发展研究所 | Method for improving gas production characteristics of anaerobic dry fermentation by using biogas residue hydrothermal product |
| CN115028487A (en) * | 2022-06-28 | 2022-09-09 | 镇江恒欣生物科技有限公司 | Suspended starchiness decomposition fermentation device after solid-liquid separation of vinegar residue and use method thereof |
| CN115488140A (en) * | 2022-09-09 | 2022-12-20 | 中节能(肥西)环保能源有限公司 | System and method for treating kitchen garbage by coupling tidal fermentation percolation bed and efficient anaerobic reactor |
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101560466B (en) | Integrated methane dry fermentation device | |
| CN104651218B (en) | Fruits and vegetables garbage anaerobic fermentation is coupled with biogas generator waste heat and utilizes system and method | |
| CN102241464B (en) | Urban sludge treating method and equipment | |
| CN106754294A (en) | A kind of apparatus and method of vinegar grain solid-liquid split-phase anaerobic digestion methane production | |
| CN103451095B (en) | Method for preparing marsh gas through straw, excrement and kitchen waste | |
| CN104130942B (en) | Agricultural organic waste anaerobically fermenting reclaims biogas reaction unit and recovery method | |
| 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 | |
| CN202688157U (en) | Continuous type hydrothermal-flash evaporation device for municipal sludge | |
| CN105602844B (en) | Kitchen castoff high temperature combined anaerobic digestion equipment and anaerobic digestion process | |
| CN104974927B (en) | The system that a kind of stalk marsh gas prepare coupled electricity-generation UTILIZATION OF VESIDUAL HEAT IN | |
| CN101760481A (en) | Method for producing hydrogen and/or methane through fermentation of fiber wastes and device thereof | |
| CN206052022U (en) | A kind of device of organic solid castoff dry-type anaerobic fermentation | |
| CN104745639B (en) | A kind of united two-stage anaerobic fermentation methane production technique of wet method-dry method | |
| CN101767907B (en) | Coupling treatment device and coupling treatment method for sweet sorghum fuel ethanol wastewater circumfluence bioreactor | |
| CN101985381A (en) | Integrated treating device and method of fuel ethanol distillation wastewater of corn straw and high ammonia nitrogen pretreatment wastewater | |
| CN207581802U (en) | A kind of device of the mixed material fermentation and biogas production with hydro-thermal process | |
| CN102180576A (en) | Advanced dry anaerobic digestion method based on sludge modification pretreatment | |
| CN103243123B (en) | A kind of high level transforms the New Cycle technique of potato vinasse | |
| CN109207345B (en) | Device and process for coupling corn straw ethanol fermentation with municipal sludge anaerobic co-digestion | |
| CN104609691B (en) | A kind of process utilizing papermaking excess sludge biogas | |
| CN111484219A (en) | System and method for treating sludge through two-phase anaerobic digestion | |
| CN102586095B (en) | Gas stripping convective circulation anaerobic digestion reactor | |
| KR101181834B1 (en) | Pre-thermal treatment of microalgae and high temperature and high efficiency hydrogen/methane fermentation process using waste heat of power-plant effluent gas | |
| CN101456651B (en) | Rubbish initial leachate treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170531 |