WO2016041410A1 - 一种卧式大型连续沼气干式发酵装置及方法 - Google Patents

一种卧式大型连续沼气干式发酵装置及方法 Download PDF

Info

Publication number
WO2016041410A1
WO2016041410A1 PCT/CN2015/084553 CN2015084553W WO2016041410A1 WO 2016041410 A1 WO2016041410 A1 WO 2016041410A1 CN 2015084553 W CN2015084553 W CN 2015084553W WO 2016041410 A1 WO2016041410 A1 WO 2016041410A1
Authority
WO
WIPO (PCT)
Prior art keywords
hydrolysis
fermentation
tank
methane fermentation
feed
Prior art date
Application number
PCT/CN2015/084553
Other languages
English (en)
French (fr)
Inventor
杨宏
Original Assignee
北京工业大学
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 北京工业大学 filed Critical 北京工业大学
Priority to US15/510,806 priority Critical patent/US9879211B2/en
Publication of WO2016041410A1 publication Critical patent/WO2016041410A1/zh

Links

Images

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
    • C12M23/34—Internal compartments or partitions
    • 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
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • 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
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • C12M27/20—Baffles; Ribs; Ribbons; Auger vanes
    • 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
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/14—Pressurized fluid
    • 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
    • C12M33/00—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus
    • 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
    • C12M45/06—Means for pre-treatment of biological substances by chemical means or hydrolysis
    • 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
    • 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

Definitions

  • the invention belongs to the technical field of dry biogas fermentation, and particularly relates to a horizontal large-scale continuous biogas dry fermentation device and method.
  • Dry anaerobic fermentation usually means that the dry matter content of the fermented raw material is 20% to 40%, the raw material is solid or semi-solid, and the fermentation biogas slurry is less in the process, the dry fermentation methane content is high (60%), sulfur Low content.
  • the traditional biogas fermentation has the following problems: 1) biogas fermentation can not really achieve continuous production, most large-scale devices can only use intermittent; 2) large dry fermentation tanks are bulky, with high dry matter content and uneven material mixing; 3) The biogas fermentation time period is long. During the mixing, the fermentation of the warehouse materials is incomplete due to the backmixing of the new (new) materials. 4) The large-scale biogas fermentation is mostly inoculated by the fermentation liquid reflux method. It is difficult for large materials to be used. To the inoculation uniformity; 5) Large-scale biogas fermentation uses a first-stage fermentation process, so that the fermentation temperature is mostly moderate temperature fermentation, hydrolysis acidification and methanation can not be separated, and the reaction efficiency is low. The root cause of the above problems is the difficulty of large material volume, high solid content, overall material agitation and material displacement.
  • the invention is based on the above background, and is developed into a fermentation process form and a typical device suitable for large-scale biogas production by utilizing changes in agitation conditions and changes in material displacement driving forms.
  • the large-scale continuous biogas dry fermentation device and the process method of the invention adopts a two-phase anaerobic fermentation process, and the whole system is divided into a hydrolysis acidification fermentation part (medium temperature) and a methane fermentation part (high temperature).
  • the main part of the invention is: material inoculation design, a large number of viscous semi-solid materials propulsion mode, a large number of material mixing methods and overall fermentation cabin design.
  • Bacterial inoculation of new materials is achieved by mixing the "clinker” completed by fermentation with the unfermented "raw meal".
  • the U-shaped folding plane layout (see floor plan 1) is adopted in the overall layout of the fermentation tank, in order to enable the feed inoculation homogenization tank (1, 10) and the fermentation discharge tank (3, 12) to be adjacent.
  • the “clinker” which is beneficial to the fermentation can be more convenient to feed to the inoculation homogenization tank (1, 10), and to ensure the “raw material” inoculation.
  • This guiding process is carried out by means of material inoculators (spiral feeds) (4) and (13) which are connected in the fermentation chute (3, 12) and the feed inoculation homogenization tank (1, 10).
  • the material inoculator (4, 13) takes a portion of the "clinker” out of the fermentation hopper and rotates it into the feed inoculation homogenization compartment (1, 10).
  • the fermentation completes the "clinker” with the bacteria and the unfermented "raw material", in the material inoculating device (4, 13), the material distributor (5, 14) and the fermentation chamber material propeller (7-1, 16-1) Under the joint action, the process of material inoculation, material homogenization and material entering the fermentation chamber is completed.
  • the material pusher is a two-axis double-blade (30, see Fig. 10, Fig. 11).
  • the relative splicing synchronous rotation mode can realize the irreversible advancement of the material by the double blade (30) bite relative rotation (see Fig. 10), and the thruster is arranged at The bottom of the main compartment of the fermentation tank (28, see Figure 3). Due to the long design of the double-wing impeller along the direction of the rotating shaft (see Figure 11), a large amount of material can be propelled, and the propeller can change the propulsive ability by changing the rotational speed. The bite design of the two wings of the propeller can realize the material returning during the material advancement process.
  • this design separately sets 5 sets of hydrolyzed material propellers (16-1) under the main partition wall (28, see Figure 3) of the hydrolysis fermentation tank (11) and the methane fermentation tank (2). To 16-5) and 7 sets of methane material propellers (7-1 to 1-7).
  • the design adopts the gas agitation which is currently popular in the world.
  • This design adopts a height of 10m in the overall fermentation tank material height, which is reduced by more than half compared with the height of the fermentation vessel material which is now ubiquitous due to the lower material accumulation height.
  • Adopting the gas agitation is more uniform, and at the same time, the gas pressure device outlet pressure requirement is also greatly reduced, so that high-pressure special equipment is not needed in the selection of the pressurizing equipment, and the universal pressurizing device can be used. Gas pressurization is achieved, which greatly reduces the cost of the equipment.
  • the gas agitation system works by: gas fermentation zone (22, 23, see Figure 2) to the fermentation tank gas gathering zone (18, 9, see Figure 2
  • the gas in the pump is pressurized.
  • the hydrolyzed fermentation tank collects biochemical waste gas mainly produced by fermentation, and the methane fermentation tank mainly collects methane gas. Methane fermentation gas.
  • the pressurized gas is delivered to the air distributor (14, 8) provided at the bottom of the fermentation chamber through a pressurized gas pipeline, and the pressurized gas is released through the air distributor to agitate the material in the fermentation chamber.
  • the core part of the invention is also designed in the form of a fermentation tank.
  • the fermentation tank volume has been limited by material propulsion and material agitation technology.
  • the maximum volume of fully automated anaerobic fermentation tank is only about 5000m 3 , which greatly limits
  • large-scale biogas production is currently carried out in the form of multiple sets of fermentation tanks.
  • the material in the fermentation tank is under the action of the material propeller at the bottom of the main partition wall (28), and the whole material moves forward along the "flow" direction of the material.
  • a blocking low wall (29) is set in each cell in the design, so that the material is in a single grid range.
  • Fermentation device features:
  • a large-scale continuous biogas dry fermentation device characterized by comprising: a hydrolysis feed tank (24), a hydrolysis heating feeder (25), a hydrolysis feed heater (26), and a hydrolysis feeder (27) Hydrolyzed feed inoculation homogenization tank (10), hydrolyzed material inoculator (13), hydrolysis fermentation tank (11), hydrolysis feed distributor (14), hydrolyzed material propeller (16-1 to 16-5) , hydrolyzed material discharge equalizer (15), hydrolysis discharger (20), hydrolysis gas agitating gas distributor (17), hydrolysis gas circulation fan (22); methane fermentation feeder (21) methane fermentation feed inoculation Homogenization tank (1), methane fermentation material inoculator (4), methane fermentation tank (2), methane fermentation feed distributor (5), methane fermentation material propeller (7-1 to 7-7), methane Fermentation material discharge equalizer (6), methane fermentation output tank (3), methane fermentation feed heater (19), methane fermentation biogas agitated air distributor (8), methane fermentation gas circulation
  • the hydrolysis feed tank (24) and the hydrolysis feed heater (26) are connected by a hydrolysis heating feeder (25), and the hydrolysis heating feeder (25) is located in the hydrolysis feed tank (24) and penetrates through the hydrolysis Within the feed heater (26), the hydrolysis feed heater (26) is in communication with the hydrolysis feed inoculating homogenization tank (10) via a hydrolysis feed (27), and the hydrolysis feed is inoculated into the homogenization tank (10).
  • the feed inoculation homogenization tank (10) and the hydrolysis discharge tank (12) are connected by a hydrolyzed material inoculator (13), and the hydrolysis discharge tank (12) is fermented by a hydrolysis discharger (20) and methane.
  • the feed heater (19) is connected, and the methane fermentation feed heater (19) is connected to the methane fermentation feed inoculation homogenization tank (1) via the methane fermentation feeder (21), and the methane fermentation feed inoculation is homogenized.
  • the methane fermentation feed distributor (5) is connected to the inlet of the methane fermentation tank (2), and the outlet of the methane fermentation tank (2) is connected to the methane fermentation discharge tank (3) through a methane fermentation material discharge equalizer (6).
  • the methane fermentation feed inoculation homogenization tank (1) is connected to the methane fermentation feed tank (3) through a methane fermentation material inoculator (4).
  • the methane fermentation tank and the hydrolysis fermentation tank are generally reinforced concrete tanks.
  • a longitudinal main partition wall is arranged in the middle of the hydrolysis fermentation tank, and the main partition wall divides the hydrolysis fermentation tank into two parts, so that the stroke of the material in the hydrolysis fermentation tank is U-shaped; each space is alternately spaced
  • the horizontal main partition wall and the short partition wall are divided into a plurality of compartments, and a hydrolyzed fermentation material propeller (16-1 to 16-5) is arranged under each main partition wall of each space to advance the material in the hydrolyzed material.
  • the hydrolysis fermentation tank is moved up and down, and a hydrolysis gas agitating air distributor (17) is further arranged at the bottom of the hydrolysis fermentation tank.
  • the upper part of the hydrolysis fermentation tank is a hydrolysis gas gathering area (18), and the gas is collected by hydrolysis.
  • the gas in the zone (18) is pressurized by the hydrolysis gas circulation fan (22) and then released by the hydrolysis gas agitating distributor (17).
  • the methane fermentation tank is the same as the hydrolyzed fermentation tank.
  • the longitudinal main partition wall is arranged in the middle to divide the methane fermentation tank into two parts, so that the travel of the material in the methane fermentation tank is U-shaped; each space is alternately spaced by the horizontal main partition wall.
  • (28) and the short partition wall (29) is divided into a plurality of compartments, and a methane fermentation material propeller (7-1 to 7-7) is arranged under the main partition wall to make the material in the methane fermentation tank under the action of the material propeller Go back and forth.
  • methane fermentation biogas agitating gas distributor (8) At the bottom of the methane fermentation tank, there is also a methane fermentation biogas agitating gas distributor (8), the upper part of the methane fermentation tank is a methane gas gathering zone (9), and the gas in the methane gas gathering zone (9) is passed through a methane fermentation gas circulation fan. (23) Pressurization is released by the methane fermentation biogas agitating air distributor (8).
  • the material propellers (7-4) and (16-3) are respectively arranged under the end sections of the longitudinal main partition wall opposite to the feed of the methane fermentation tank and the hydrolysis fermentation tank.
  • Each of the material propellers includes: two long-axis propulsion impellers, two propeller drive shafts, and a propeller casing; the long-shaft propulsion impeller has a long cylindrical structure as a whole, and is an propeller having an axial length. That is, the impeller vane design adopts an elongated design along the direction of the drive shaft, and the vertical axial cross section is a dumbbell-shaped structure, and both ends and the intermediate outer surface of the dumbbell-shaped structure are curved (outer and inner involute curved surfaces).
  • Each long-axis propulsion impeller has a propeller drive shaft. The axes of the two long-axis propulsion impellers are parallel to each other and rotate in opposite directions.
  • the two long-axis propulsion impellers rotate in opposite directions, one clockwise. a counterclockwise rotation process, the two vane impeller surfaces are always kept in a relatively bite-sealed seal; a propeller housing is arranged outside each long-axis propulsion impeller, and the inner surface of the propeller housing is semi-circular, so that each The long-axis propulsion impeller is always tangent to the corresponding semi-circular cavity inner wall during the rotation process.
  • the outer surface of the propeller casing is provided with a barrier so that the barrier and the propeller jointly divide the space barrier on both sides of the propeller into two parts, and the viscous semi-solid material is made with the relative rotation of the two long-axis propellers.
  • the rotation of the impeller is followed by the rotation of the long axis type from one side space to the other side space.
  • the material propeller is a lateral rotary propeller fixed in the cabin driven by the outboard drive device.
  • the rotary material propeller is composed of two relatively rotating long-axis propulsion impellers fixed by two shafts, and the two long-axis propulsion impellers are relatively rotated.
  • the design material is stirred, and the hydrolysis fermentation is carried out by using a hydrolysis exhaust gas through a fan, and then released into the material through a hydrolysis stirring gas distributor uniformly installed at the bottom of the fermentation chamber to achieve uniform stirring of the materials.
  • This setting method is a common practice for material gas agitation, and is not the content of this invention.
  • the agitating gas pressurizing device can adopt the general fan form, which realizes the reduction of engineering cost and the improvement of system stability. And the mixing uniformity is also enhanced.
  • the methane fermentation tank is also used in the same way, except that the recycle gas is a methane mixture produced by methane fermentation.
  • the fermentation process produced by dry fermentation is less.
  • the inoculation method of this design adopts the fermentation completion material as the seed source, and the bacterial inoculation process is realized by mixing the seed source material with the new material.
  • the fermented material is controlled into the feed compartment through the material inoculator (4, 13), and the new material is inoculated and passed through the inoculum and feed distributor in the feed inoculation homogenization tank (1, 10). Stirring to achieve material homogenization.
  • the hydrolysis acidification portion has a fermentation temperature of 33 ⁇ 2 ° C and a fermentation residence time of 5-6 days.
  • the methane fermentation temperature was 60-65 ° C, and the methane fermentation residence time was 20 days.
  • a method for continuous fermentation using the above apparatus comprising the steps of:
  • the pseudo-fermented biomass mixture is proportionally introduced into the hydrolysis feed tank (24), and the material is heated by the hydrolysis heating feeder (25) into the hydrolysis feed heater (26), and then in the hydrolysis feeder (27).
  • the hydrolytic acidification of the heated material is completed, and the methane fermentation feed (21) is introduced into the methane fermentation feed to inoculate the homogenization tank (1), and the methane fermentation material inoculator (4) and the methane fermentation feed distributor (5)
  • the methane fermentation material propeller (7-1) Under the combined action of the methane fermentation material propeller (7-1), the material is inoculated and homogenized while being propelled into the methane fermentation tank (2).
  • the methane fermentation material propeller (7-2 to 7-6) set in the fermentation chamber the material moves slowly along the process direction, the whole fermentation time is 20 days, and finally the last methane fermentation material in the methane fermentation tank advances.
  • the methane fermentation material discharge equalizer (6) enters the methane fermentation discharge tank (3), and a small part of the discharge material passes through the methane fermentation material inoculator. (4) Entering the methane fermentation feed inoculation homogenization tank (1) to complete the inoculation of the methanogen; the rest of the discharge completes the entire fermentation process.
  • the present invention can achieve continuous fermentation.
  • the material is heated to 33 ⁇ 2 ° C; the hydrolysis fermentation residence time is 5-6 days; after the material is passed through the methane fermentation feed heater (19), The material was heated to 60-65 ° C and the methane fermentation residence time was 20 days.
  • the tank capacity of the hydrolysis fermentation tank and the methane fermentation tank of the present invention is adjusted by the speed of the hydrolyzed material propellers (16-1 to 16-5) and the methane fermentation material propellers (7-1 to 7-7) in this process mode. , can be adjusted within a certain range.
  • the invention has the following advantages: 1) realizing continuous fermentation without mixing; 2) because the overall process form is simple, the requirements of each mechanical component are low, and the inoculation adopts the material mixing mode, and the process technology is determined to be realized. 3) Two-phase anaerobic (first phase intermediate temperature hydrolysis acidification, second phase high temperature biogas fermentation) effectively maintains the reaction environment of each fermentation section, and the high temperature section effectively inhibits the activity of the hydrolyzed acidification bacteria; 4) Fermentation material filling The height is low (only half of the current international mainstream process), so the equipment with low stirring air pressure is low, because the design makes the gas agitation more uniform; 5) through the overall shifting operation mode of the fermentation chamber material, uniform discharge and The overall push-flow material flow achieves the non-mixing of the entire reaction process, making the fermentation more thorough.
  • the invention firstly adopts a reinforced concrete reaction tank structure in the overall design of the hydrolysis acidification and biogas fermentation tank, and the whole reactor presents the inlet and outlet ports close to the ground, and the operation is convenient and energy-saving.
  • Fig. 1 is a schematic diagram of a large-scale continuous biogas dry fermentation device; in Fig. 1, the two-line blackening is provided with a material propeller.
  • Figure 2 is a cross-sectional view taken along line 5-5 of Figure 1;
  • Figure 3 is a plan view of the methane fermentation tank
  • Figure 4 is a cross-sectional view of the methane fermentation tank 1-1 of Figure 3;
  • Figure 5 is a cross-sectional view of the methane fermentation tank 2-2 of Figure 3;
  • Figure 6 is a plan view of the hydrolysis fermentation tank
  • Figure 7 is a cross-sectional view of the hydrolysis fermentation tank 3-3 of Figure 6;
  • Figure 8 is a cross-sectional view of the hydrolysis fermentation tank 4-4 of Figure 6;
  • Figure 9 is an enlarged view of a portion A of Figure 4.
  • Figure 10 is a schematic view of the structure of the material pusher
  • Figure 11 is a schematic view showing the structure of the material propeller long-axis propulsion impeller.
  • the fermentation tank process form of this design can be said to be unrestricted in terms of cabin capacity.
  • the effective volume of the methane fermentation tank is 5000m 3 and the material height is 10m (see plan 1, 2, section 1-1, 2). -2, 3-3, 5-5), in actual application, due to the above material propulsion method and material mixing method (actually, if the fermentation tank adopts the grid type series design, the single grid stirring can also adopt other mechanical stirring forms, because the single The volume of the material is small and the overall capacity can be further enlarged.
  • the larger storage capacity can be realized by the change of the number of divisions and the layout of the plane. Therefore, this design method can be said that there is no technical obstacle to the change of the cabin capacity.
  • the pseudo-fermented biomass mixture is proportionally introduced into the hydrolysis feed compartment (24), and the material is heated by the hydrolysis heating feeder (25) into the hydrolysis feed heater (26), where the material is heated to 33 ⁇ 2 °C, then pushed into the hydrolysis feed inoculation homogenization chamber (10) by the hydrolysis feeder (27).
  • the new material is mixed with the hydrolyzed acidified (hydrolyzed fermented) material transferred from the hydrolyzed material inoculator (13), and in the hydrolysis feed distributor (14) and Under the combined action of the hydrolyzed material propeller (16-1), the material is inoculated and homogenized while being propelled into the hydrolysis fermentation tank (11).
  • the material is stirred in the hydrolysis fermentation tank by the pressurized gas stream released by the hydrolysis gas agitating air distributor (17), and at the same time, the material is pushed by the hydrolyzed material propeller (16-2 to 16-4) provided in the fermentation chamber. Slowly proceed along the direction of the process, the whole hydrolysis fermentation time is 5-6 days, and finally, under the push of the last hydrolyzed material propeller (16-5) in the hydrolysis fermentation tank, it is hydrolyzed by the hydrolyzed material discharge equalizer (15).
  • Cabin (12) The hydrolyzed material is mostly driven by the hydrolysis discharger (20) into the methane fermentation feed heater (19), and a small portion is passed through the hydrolysis material inoculator (13) to the hydrolysis feed inoculation homogenization.
  • the material entering the methane fermentation feed heater (19) is heated to 60-65 ° C.
  • the hydrolyzed acid bacteria are inhibited or eliminated by the high temperature of 60-65 ° C.
  • the hydrolytic acidification of the heated material is completed, and the methane fermentation feed (21) is introduced into the methane fermentation feed to inoculate the homogenization tank (1), where the lyophilized acidified material is converted with the methane fermentation material inoculator (4).
  • the methane that was infused was fermented
  • the inoculated materials are mixed.
  • the two parts of the material are combined with the methane fermentation feed distributor (5) and the methane fermentation material propeller (7-1), and the material is inoculated and homogenized while being advanced into the methane fermentation tank (2).
  • the material is stirred in a methane fermentation tank by a pressure air stream released by a methane fermentation biogas agitating air distributor (8), and simultaneously driven by a methane fermentation material propeller (7-2 to 7-6) provided in the fermentation chamber.
  • the material moves slowly along the process direction, and the whole hydrolysis fermentation time is 20 days.
  • Methane fermentation discharge equalizer (6) under the driving of the last methane fermentation material propeller (7-7) in the methane fermentation tank.
  • Methane fermentation discharge tank (3) a small part of the discharge is passed through the methane fermentation material inoculator (4) into the methane fermentation feed inoculation homogenization tank (1) to complete a new round of methanogen inoculation jobs. This cycle is carried out continuously.
  • the reinforced concrete structure is produced, the effective volume of the hydrolysis fermentation tank is 1500m 3 , and the effective volume of the methane fermentation tank is 5000m 3 .
  • the design agitation is pneumatic agitation, collecting the gas produced by fermentation (hydrolyzed into hydrolyzed waste gas, methane fermentation is a mixture of methane fermentation), because the overall fermentation material filling height of this process design is greatly reduced compared with other dry fermentations. Therefore, the stirring gas pressurizing device can be adopted in the form of a general-purpose fan, which realizes reduction of engineering cost and improvement of system stability, and the stirring uniformity is also enhanced.
  • the design adopts a two-wing lateral thruster design under pneumatic agitation conditions.
  • the material propeller is fixed in the cabin to fix the lateral propeller driven by the outer tank.
  • the transverse material propeller is composed of two relatively rotating long push fins fixed by two shafts, and the two sets of flaps can rotate the former one when rotating relative to each other.
  • the material in the compartment is evenly pushed to the next compartment, so that the material with poor flow condition is evenly “flowed” forward.
  • the hydrolyzed fermentation tank is equipped with 5 sets of hydrolyzed fermentation material propellers, 4 of which have a shaft length of 5m and 1 set of shafts. 4.2m long.
  • the hydrolysis acidification fermentation temperature is 33 ⁇ 2° C.; the methane fermentation temperature is 60-65° C.
  • the raw material is 70% of the dewatered sludge of the urban sewage treatment plant with a water content of 80%, and 30% of the crushed urban kitchen waste is mixed.
  • the feed amount was 250 m 3 /d
  • the hydrolysis fermentation residence time was 6 d
  • the methane fermentation residence time was 20 d.
  • the gas production capacity of the fermentation unit is 25000 m 3 /d.

Abstract

本申请提供了一种卧式连续沼气干式发酵装置，在发酵舱主隔墙底部设置了物料推进器，可实现物料的不可逆推进。通过旋转转速的变化能改变推进能力。反应器的进、出料口接近地面，实现了均匀出料和物料流动，使发酵更彻底。本申请还提供了利用所述装置进行连续发酵的方法。

Description

一种卧式大型连续沼气干式发酵装置及方法 技术领域
本发明属于干式沼气发酵技术领域，特别涉及一种卧式大型连续沼气干式发酵装置及方法。
背景技术
针对世界范围内的资源短缺、能源结构单一、环境恶化等制约可持续发展的突出问题，围绕建设资源节约型和环境友好型社会的迫切需求，大力加强清洁能源生产与环境保护结合等系列技术开发与集成应用，提升科技对可持续发展的支撑和引领能力，是目前各国科学技术发展的重要组成部分，这其中部分核心内容是生物质资源的高效利用和由这些物质引起的污染有效控制。生物质新能源产业的技术提升和大型规模化实现，要求要发展先进高效的沼气生物发酵技术，以及围绕着核心发酵技术研制大型的沼气发酵装备。
干式厌氧发酵通常是指发酵原料的干物质含量在20％～40％，原料呈固态或半固态，处理过程中产生发酵沼液污水少，干式发酵甲烷含量高(60％)、硫含量低。
传统的沼气发酵存在如下问题：1)沼气发酵不能真正实现连续生产，多数大型装置只能采用间歇式；2)大型干式发酵仓体积庞大，物料干物质含量高，物料搅拌不均匀；3)沼气发酵时间周期长，搅拌中由于(新、旧)物料返混而出现出仓物料发酵不完全；4)大型沼气发酵多采用发酵液回流方式进行接种，对于大物料量而言，很难做到接种均匀；5)大型沼气发酵多采用一级发酵工艺，致使发酵温度多采用中温发酵，水解酸化和甲烷化无法分开，反应效率低。产生上述问题的根本原因是大物料量、含固率高整体物料搅拌和物料位移困难。
本次发明就是基于上述背景，利用搅拌工况条件的改变和物料位移驱动形式的变化开发研制的适合于大规模化沼气生产的发酵工艺形式和典型装置。
发明内容：
本发明的大型连续沼气干式发酵装置及工艺方法，采用两相厌氧发酵工艺，整个系统分为水解酸化发酵部分(中温)和甲烷发酵部分(高温)。
本次发明的主要部分为：物料接种方式设计、大量粘稠半固体物料推进方式、大量物料搅拌方式和整体发酵舱设计。通过上述工程设计方式的创新和有机的结合，解决了目前大型干式发酵中，粘稠半固体物料整体不混料位移和发酵舱单仓大容积实现的矛盾，为大型或特大型发酵舱的建立提供了较好的技术方法。整个发酵系统分两部分，一是水解酸化部分；二是甲烷发酵部分。这两个部分的工艺形式是一样的，只是发酵舱容积和发酵所使用的细菌群系(水解酸化：水解酸化菌群；甲烷发酵：甲烷菌群)不同。为了便于说明以及避免重复下 面综合成一种工艺形式进行说明。
物料接种方式：
采用发酵完成的“熟料”同未发酵“生料”进行混合的方式实现新物料细菌接种。设计中，首先在发酵舱整体布局上采用U型折返式平面布局(见平面图1)，目的是使进料接种均质化舱(1、10)和发酵出料舱(3、12)能够临近，有利于发酵完成的“熟料”能够更方便导料至进料接种均质化舱(1、10)，保障“生料”接种。这一导料过程是通过在发酵出料舱(3、12)和进料接种均质化舱(1、10)连通设置的物料接种器(螺旋输料)(4)和(13)实现。物料接种器(4、13)将部分“熟料”从发酵出料舱取出旋转输送至进料接种均质化舱(1、10)中。发酵完成带菌的“熟料”同未发酵“生料”，在物料接种器(4、13)、物料布料器(5、14)以及发酵舱物料推进器(7-1、16-1)的共同作用下，完成物料接种、物料均质化和物料进入发酵舱过程。
物料推进方式：
粘稠半固体物料大量有序输送一直是大型发酵舱建设的技术障碍，本次利用自行设计的大型粘稠物料推进器，有效实现了这一工艺过程。
物料推进器为双轴双叶片(30，见附图10、图11)相对咬合同步旋转方式，通过双叶片(30)咬合相对旋转(见图10)能够实现物料的不可逆推进，推进器设置于发酵舱主隔墙(28，见图3)底部。由于双翼片叶轮沿旋转轴方向的长形设计(见图11)，可以实现大量物料的推进，该推进器可以通过旋转转速的改变，实现不同推进能力的改变。该推进器两翼片的咬合设计可以实现物料推进过程中不返料。
在发酵仓整体设计上，本次设计分别在水解发酵舱(11)和甲烷发酵舱(2)的主隔墙(28，见图3)下面分别设置了5套水解物料推进器(16-1至16-5)和7套甲烷物料推进器(7-1至1-7)。
物料搅拌：
设计采用目前在国际上比较流行的气搅拌，本次设计在整体发酵舱物料高度设计采用10m高度，该高度相对于现已普遍存在的发酵舱物料高度减少一半以上，由于较低物料堆积高度的采用，使气搅拌更加均匀，同时在气加压设备出口气压要求上也相映地有了较大的降低，这样，在加压设备选型上就不需要高压专用设备而可以采用通用加压设备实现气体加压，这样较大程度的降低了设备造价。
为了适应和保持水解酸化和甲烷化发酵的厌氧环境，气搅拌系统工作方式是：通过气体加压设备(22、23，见图2)将发酵舱集气区(18、9，见图2)中的气体抽吸加压。水解发酵舱收集的是发酵产生的以二氧化碳为主的生化废气，甲烷发酵舱收集的是以甲烷气体为主 的甲烷发酵气体。加压后的气体通过压力布气管道传送至发酵舱底部设置的布气器(14、8)，压力气体通过布气器释放，从而对发酵舱内的物料实现搅拌。
发酵舱形式：
本发明的核心部分也即发酵舱形式设计。在固体半固体干式发酵技术中，发酵舱容积一直受物料推进和物料搅拌技术方法的限制，目前在干式发酵领域，全自动化厌氧发酵舱最大容积仅在5000m3左右，这极大地限制了大型沼气化的生产，目前大型沼气生产多采用建立多组发酵舱的形式实施。
发酵舱中物料的运行方式，发酵舱中的物料在主隔墙(28)底部物料推进器的作用下，整体物料沿着物料“流动”方向向前推移。由于只有在主隔墙(28)底部设置了物料推进器，为了防止物料推进形成短路情况，设计中在每一单元格中设置了阻断矮墙(29)，目的是使物料在单格范围内有整体翻动作用，这样结合物料搅拌，整个物料在整体推进过程中就形成不断前进、不断搅拌、不断翻动过程，实现了物料的局部均质化和前后发酵程度不同的物料不出现返混的现象。
发酵装置特征：
一种大型连续沼气干式发酵装置，其特征在于，主要包括：水解进料舱(24)、水解加热进料器(25)、水解进料加热器(26)、水解进料器(27)、水解进料接种均质化舱(10)、水解物料接种器(13)、水解发酵舱(11)、水解进料布料器(14)、水解物料推进器(16-1至16-5)、水解物料出料均衡器(15)、水解出料器(20)、水解气搅拌布气器(17)、水解气循环风机(22)；甲烷发酵进料器(21)甲烷发酵进料接种均质化舱(1)、甲烷发酵物料接种器(4)、甲烷发酵舱(2)、甲烷发酵进料布料器(5)、甲烷发酵物料推进器(7-1至7-7)、甲烷发酵物料出料均衡器(6)、甲烷发酵出料舱(3)、甲烷发酵进料加热器(19)、甲烷发酵沼气搅拌布气器(8)、甲烷发酵气循环风机(23)、纵向主隔墙(31)、矮墙(29)、横向主隔墙(28)。
其中：水解进料舱(24)和水解进料加热器(26)通过水解加热进料器(25)连通，水解加热进料器(25)位于水解进料舱(24)之内并贯穿水解进料加热器(26)之内，水解进料加热器(26)通过水解进料器(27)与水解进料接种均质化舱(10)连通，水解进料接种均质化舱(10)通过水解进料布料器(14)与水解发酵舱(11)的进口连接，水解发酵舱(11)的出口通过水解物料出料均衡器(15)与水解出料舱(12)连接，水解进料接种均质化舱(10)与水解出料舱(12)之间通过水解物料接种器(13)进行连接，同时水解出料舱(12)通过水解出料器(20)与甲烷发酵进料加热器(19)连通，甲烷发酵进料加热器(19)经由甲烷发酵进料器(21)与甲烷发酵进料接种均质化舱(1)连通，甲烷发酵进料接种均质化舱(1) 通过甲烷发酵进料布料器(5)与甲烷发酵舱(2)的进口连接，甲烷发酵舱(2)的出口通过甲烷发酵物料出料均衡器(6)与甲烷发酵出料舱(3)连接，甲烷发酵进料接种均质化舱(1)与甲烷发酵出料舱(3)之间通过甲烷发酵物料接种器(4)连通。
甲烷发酵舱、水解发酵舱一般均为钢筋混凝土舱体。为了使物料有序推进，水解发酵舱中间设有纵向主隔墙，该主隔墙将水解发酵舱分成两部分空间，使物料在水解发酵舱的行程为U型；每个空间又由交替间隔设置的横向主隔墙和矮隔墙分成多个分格，在每个空间的各个主隔墙的下面设有水解发酵物料推进器(16-1至16-5)，使物料在水解物料推进器的作用下在水解发酵舱内上下迂回前进，并且在水解发酵舱的底部还设有水解气搅拌布气器(17)，水解发酵舱的上部为水解集气区(18)，水解集气区(18)中的气体经由水解气循环风机(22)加压之后通过水解气搅拌布气器(17)释放。
甲烷发酵舱同水解发酵舱一样，中间设有纵向主隔墙将甲烷发酵舱分成两部分空间，使物料在甲烷发酵舱的行程为U型；每个空间又由交替间隔设置的横向主隔墙(28)和矮隔墙(29)分成多个分格，主隔墙下面设有甲烷发酵物料推进器(7-1至7-7)，使物料在物料推进器的作用下在甲烷发酵舱内上下迂回前进。并且在甲烷发酵舱的底部还设有甲烷发酵沼气搅拌布气器(8)，甲烷发酵舱上部为甲烷集气区(9)，甲烷集气区(9)中的气体经由甲烷发酵气循环风机(23)加压通过甲烷发酵沼气搅拌布气器(8)释放。
为了保证物料的连通，在甲烷发酵舱、水解发酵舱进料相反的纵向主隔墙末端段下面分别设置了物料推进器(7-4)和(16-3)见图1。
上述每个物料推进器包括：两个长轴型推进叶轮、两个推进器驱动轴、推进器外壳；长轴型推进叶轮，整体为长柱形结构，即为具有轴向长度的推进叶轮，即在叶轮翼片设计上采用沿驱动轴方向的长形设计，垂直轴向的截面为哑铃型结构，哑铃型结构的两端和中间外表面均为(外、内渐开线形表面)弧形；每个长轴型推进叶轮均按有一个推进器驱动轴，两个长轴型推进叶轮的轴互相平行，且相向同步旋转，两个长轴型推进叶轮的旋转方向相反，一个顺时针，一个逆时针，旋转的过程中两翼片叶轮表面之间始终保持相对咬合并密封；在每个长轴型推进叶轮外面均设有推进器外壳，推进器外壳的内表面为半圆弧形，使得每个长轴型推进叶轮在旋转的过程中始终与所对应的半圆形空腔内壁相切。推进器外壳的外面均设有阻挡物，使得阻挡物和推进器共同将推进器两边的空间阻挡分割成两部分空间，随着两个长轴型推进叶轮的相对旋转，使得粘稠半固体物料跟着长轴型推进叶轮的旋转从一边空间输送到另一边空间。
物料推进器是固定在舱体内由舱外驱动装置驱动的横向旋转推进器，旋转物料推进器是由双轴固定的两根相对旋转的长轴型推进叶轮组成，两长轴型推进叶轮相对旋转时能够将前 一格舱的物料均匀推至下一格舱，从而使流动状态较差的物料实现均匀向前“流动”。
物料搅拌。本设计物料搅拌，水解发酵采用水解废气通过风机加压，再通过均匀安装于发酵舱底部的水解搅拌布气器释放于物料中，实现物料均匀搅拌。该设置方式是物料气搅拌的通用做法，不是本次发明内容。但是，由于本次工艺设计的整体发酵物料填装高度较其他干式发酵由大幅度减低，从而实现了搅拌气加压装置可以采用通用风机形式，实现了工程造价的降低和系统稳定性的提高，并且搅拌均匀度也得到了增强。同样，甲烷发酵舱也采用了同样的方式，只是循环气体是甲烷发酵产生的甲烷混合气。
物料接种。干式发酵产生的发酵液较少，本次设计的接种方式采用以发酵完成物料为种源，通过种源物料同新料进行混合方式实现细菌接种过程。发酵完成的物料通过物料接种器(4、13)有控制地带入进料舱，实现新物料接种并在进料接种均质化舱(1、10)内，通过接种器和进料布料器的搅拌实现物料均质化。
发酵温度和时间。水解酸化部分发酵温度为33±2℃，发酵停留时间5-6天。甲烷发酵温度为60-65℃，甲烷发酵停留时间20天。
采用上述装置进行连续发酵的方法，其特征在于，包括以下步骤：
将拟发酵生物质混合料按比例投入水解进料舱(24)，物料在水解加热进料器(25)推动下进入水解进料加热器(26)加热，然后在水解进料器(27)推动下进入水解进料接种均质化舱(10)中，在水解物料接种器(13)、水解进料布料器(14)和水解物料推进器(16-1)的联合作用下，物料被接种和均质化，同时被推进水解发酵舱(11)中；物料在水解发酵舱中被由水解气搅拌布气器(17)释放的压力气流进行搅拌，同时，在发酵仓中设置的水解物料推进器(16-2至16-4)的推动下，物料沿流程方向缓慢前行，整个水解发酵时间为5-6天，最后在水解发酵舱最后一个水解物料推进器(16-5)的推动下，通过水解物料出料均衡器(15)、水解出料器(20)绝大部分进入甲烷发酵进料加热器(19)，一少部分通过水解物料接种器(13)进入到水解进料接种均质化舱(10)中，去完成接种工作；进入甲烷发酵进料加热器(19)的物料，在甲烷发酵进料加热器(19)的加热过程中，水解酸化菌被60-65℃高温抑制或消灭；
完成水解酸化被加热的物料，通过甲烷发酵进料器(21)进入甲烷发酵进料接种均质化舱(1)中，在甲烷发酵物料接种器(4)、甲烷发酵进料布料器(5)和甲烷发酵物料推进器(7-1)的联合作用下，物料被接种和均质化，同时被推进甲烷发酵舱(2)中。在发酵仓中设置的甲烷发酵物料推进器(7-2至7-6)的推动下，物料沿流程方向缓慢前行，整个发酵时间为20天，最后在甲烷发酵舱最后一个甲烷发酵物料推进器(7-7)的推动下，通过甲烷发酵物料出料均衡器(6)进入甲烷发酵出料舱(3)，出料的一少部分通过甲烷发酵物料接种器 (4)进入到甲烷发酵进料接种均质化舱(1)中，去完成甲烷菌的接种工作；出料的其余部分完成整个发酵过程。
本发明可以实现连续式的发酵。
在进行连续发酵过程中物料经过水解加热进料器(26)后，物料被加热到33±2℃；水解发酵停留时间5-6天；物料经过在甲烷发酵进料加热器(19)后，物料被加热到60-65℃，甲烷发酵停留时间20天时。
本发明水解发酵舱、甲烷发酵舱的舱容在此工艺方式下，通过水解物料推进器(16-1至16-5)和甲烷发酵物料推进器(7-1至7-7)的转速调节，可以在一定范围内实现调节。
本发明具有如下优点：1)真正实现不混料连续发酵；2)由于整体工艺形式简单，各机械部件要求水平低，接种采用物料混合方式，确定了该工艺技术好实现。3)两相厌氧(第一相中温水解酸化、第二相高温沼气发酵)，有效维持了各发酵段的反应环境，高温段有效抑制了水解酸化菌的活性；4)发酵物料填装高度低(仅为目前国际主流工艺的一半)，所以搅拌风压低设备要求低，由于该设计方式使利用气搅拌更加均匀；5)通过发酵舱物料整体推移式运行方式，实现了均匀出料和整体推流式物料流动，实现了整个反应过程的不混料，使发酵更为彻底。
为了实现上述目标，本发明首先在水解酸化和沼气发酵舱整体设计上，采用钢筋混凝土反应池结构，整个反应器呈现进、出料口接近地面设置，运行操作方便、节能。
附图说明
图1大型连续沼气干式发酵装置示意图；图1中双线加黑的均为设置物料推进器。
图2为图1所示的5-5剖面图；
图3甲烷发酵舱平面图；
图4为图3中甲烷发酵舱1-1剖面图；
图5为图3中甲烷发酵舱2-2剖面图；
图6水解发酵舱平面图；
图7为图6水解发酵舱3-3剖面图；
图8为图6水解发酵舱4-4剖面图；
图9为图4部位A放大图；
图10物料推进器结构示意图；
图11物料推进器长轴型推进叶轮的结构示意图。
其中：
1甲烷发酵进料接种均质化舱；2甲烷发酵舱；3甲烷发酵出料舱；4甲烷发酵物料接种 器；5甲烷发酵进料布料器；6甲烷发酵物料出料均衡器；7(7-1至7-7)甲烷发酵物料推进器；8甲烷发酵沼气搅拌布气器；9甲烷集气区；10水解进料接种均质化舱；11水解发酵舱；12水解出料舱；13水解物料接种器；14水解进料布料器；15水解物料出料均衡器；16(16-1至16-5)水解物料推进器；17水解气搅拌布气器；18水解集气区；19甲烷发酵进料加热器；20水解出料器；21甲烷发酵进料器；22水解气循环风机；23甲烷发酵气循环风机；24水解进料舱；25水解加热进料器；26水解进料加热器；27水解进料器；28横向主隔墙、29矮墙、30长轴型推进叶轮，31纵向主隔墙。
具体实施方式
下面结合实施例对本发明做进一步说明，但本发明并不限于以下实施例。
本次设计的发酵舱工艺形式，在舱容方面可以说不受限制，实施案例中甲烷发酵舱的有效容积为5000m3、物料高度10m设计(见平面图1、2，剖面图1-1、2-2、3-3、5-5)，实际应用中，由于采用上述物料推进方式和物料搅拌方式(实际如果发酵舱采用分格串联设计，单格搅拌也可以采用其他机械搅拌形式，因为单格物料容积较小)整体舱容可以进一步放大。设计中可以通过分格数量和平面布局的改变实现较大仓容设计，因此该种设计方式可以说对舱容的变化无技术障碍。
以下实施例的整体装置见图1和2，各部结构可参见图3至图11。
将拟发酵生物质混合料按比例投入水解进料舱(24)，物料在水解加热进料器(25)推动下进入水解进料加热器(26)加热，在此物料被加热到33±2℃，然后在水解进料器(27)推动下进入水解进料接种均质化舱(10)中。在水解进料接种均质化舱(10)中，新物料和由水解物料接种器(13)转输过来的水解酸化(水解发酵过)物料混合，并在水解进料布料器(14)和水解物料推进器(16-1)的联合作用下，物料被接种和均质化，同时被推进水解发酵舱(11)中。物料在水解发酵舱中被由水解气搅拌布气器(17)释放的压力气流进行搅拌，同时，在发酵仓中设置的水解物料推进器(16-2至16-4)的推动下，物料沿流程方向缓慢前行，整个水解发酵时间为5-6天，最后在水解发酵舱最后一个水解物料推进器(16-5)的推动下，通过水解物料出料均衡器(15)进入水解出料舱(12)。水解完成的物料在水解出料器(20)的推动下，绝大部分进入甲烷发酵进料加热器(19)，一少部分通过水解物料接种器(13)进入到水解进料接种均质化舱(10)中，去完成接种工作。而进入甲烷发酵进料加热器(19)的物料被加热到60-65℃，在甲烷发酵进料加热器(19)的加热过程中，水解酸化菌被60-65℃高温抑制或消灭。
完成水解酸化被加热的物料，通过甲烷发酵进料器(21)进入甲烷发酵进料接种均质化舱(1)中，在此完成水解酸化的物料同经甲烷发酵物料接种器(4)转输过来的甲烷发酵完 成的接种物料混合。这两部分物料在甲烷发酵进料布料器(5)和甲烷发酵物料推进器(7-1)的联合作用下，物料被接种和均质化，同时被推进至甲烷发酵舱(2)中。物料在甲烷发酵舱中被由甲烷发酵沼气搅拌布气器(8)释放的压力气流进行搅拌，同时，在发酵仓中设置的甲烷发酵物料推进器(7-2至7-6)的推动下，物料沿流程方向缓慢前行，整个水解发酵时间为20天，最后在甲烷发酵舱最后一个甲烷发酵物料推进器(7-7)的推动下，通过甲烷发酵物料出料均衡器(6)进入甲烷发酵出料舱(3)，出料的一少部分通过甲烷发酵物料接种器(4)进入到甲烷发酵进料接种均质化舱(1)中，去完成新一轮的甲烷菌的接种工作。如此循环进行连续发酵。
实施例1
1.舱体
制作采用钢筋混凝土结构，水解发酵舱有效容积1500m3，甲烷发酵舱有效容积5000m3。
2.搅拌
混合物料干式发酵的关键问题之一是搅拌。本设计搅拌为气动搅拌，收集发酵产生的气体(水解为水解废气，甲烷发酵为甲烷发酵的混合气)，由于本次工艺设计的整体发酵物料填装高度较其他干式发酵有大幅度减低，从而实现了搅拌气加压装置可以采用通用风机形式，实现了工程造价的降低和系统稳定性的提高，并且搅拌均匀度也得到了增强。
3.推进器
本设计在气动搅拌条件下，采用两翼横向推进器设计。物料推进器是固定在舱体内固定由舱外驱动的横向推进器，横向物料推进器是由双轴固定的两根相对旋转的长推动翼片组成，两组翼片相对旋转时能够将前一格舱的物料均匀推至下一格舱，从而实现流动状态较差的物料均匀向前“流动”。
甲烷发酵舱设置7组甲烷发酵物料推进器，其中6组为轴长10m，1组轴长4.2m；水解发酵舱设置5组水解发酵物料推进器，其中4组轴长为5m，1组轴长4.2m。
4.反应条件
水解酸化发酵温度33±2℃；甲烷发酵温度60-65℃。
5.原料
原料为含水率为80％城市污水厂脱水污泥70％，附加30％粉碎的城市厨余垃圾混合而成。
6.装置能力
进料量250m3/d、水解发酵停留时间6d、甲烷发酵停留时间20d。发酵装置产气量25000m3/d。

Claims (5)

  1. 一种卧式大型连续沼气干式发酵装置，其特征在于，主要包括：水解进料舱(24)、水解加热进料器(25)、水解进料加热器(26)、水解进料器(27)、水解进料接种均质化舱(10)、水解物料接种器(13)、水解发酵舱(11)、水解进料布料器(14)、水解物料推进器(16-1至16-5)、水解物料出料均衡器(15)、水解出料器(20)、水解气搅拌布气器(17)、水解气循环风机(22)；甲烷发酵进料器(21)甲烷发酵进料接种均质化舱(1)、甲烷发酵物料接种器(4)、甲烷发酵舱(2)、甲烷发酵进料布料器(5)、甲烷发酵物料推进器(7-1至7-7)、甲烷发酵物料出料均衡器(6)、甲烷发酵出料舱(3)、甲烷发酵进料加热器(19)、甲烷发酵沼气搅拌布气器(8)、甲烷发酵气循环风机(23)、纵向主隔墙(31)、矮墙(29)、横向主隔墙(28)；
    其中：水解进料舱(24)和水解进料加热器(26)通过水解加热进料器(25)连通，水解加热进料器(25)位于水解进料舱(24)之内并贯穿水解进料加热器(26)之内，水解进料加热器(26)通过水解进料器(27)与水解进料接种均质化舱(10)连通，水解进料接种均质化舱(10)通过水解进料布料器(14)与水解发酵舱(11)的进口连接，水解发酵舱(11)的出口通过水解物料出料均衡器(15)与水解出料舱(12)连接，水解进料接种均质化舱(10)与水解出料舱(12)之间通过水解物料接种器(13)进行连接，同时水解出料舱(12)通过水解出料器(20)与甲烷发酵进料加热器(19)连通，甲烷发酵进料加热器(19)经由甲烷发酵进料器(21)与甲烷发酵进料接种均质化舱(1)连通，甲烷发酵进料接种均质化舱(1)通过甲烷发酵进料布料器(5)与甲烷发酵舱(2)的进口连接，甲烷发酵舱(2)的出口通过甲烷发酵物料出料均衡器(6)与甲烷发酵出料舱(3)连接，甲烷发酵进料接种均质化舱(1)与甲烷发酵出料舱(3)之间通过甲烷发酵物料接种器(4)连通；
    甲烷发酵舱、水解发酵舱一般均为钢筋混凝土舱体；为了使物料有序推进，水解发酵舱中间设有纵向主隔墙，该纵向主隔墙将水解发酵舱分成两部分空间，使物料在水解发酵舱的行程为U型；每个空间又由交替间隔设置的横向主隔墙和矮隔墙分成多个分格，在每个空间的各个横向主隔墙的下面设有水解发酵物料推进器(16-1至16-5)，使物料在水解物料推进器的作用下在水解发酵舱内上下迂回前进，并且在水解发酵舱的底部还设有水解气搅拌布气器(17)，水解发酵舱的上部为水解集气区(18)，水解集气区(18)中的气体经由水解气循环风机(22)加压之后通过水解气搅拌布气器(17)释放；
    甲烷发酵舱同水解发酵舱一样，中间设有纵向主隔墙将甲烷发酵舱分成两部分空间，使物料在甲烷发酵舱的行程为U型；每个空间又由交替间隔设置的横向主隔墙和矮隔墙(29)分成多个分格，横向主隔墙下面设有甲烷发酵物料推进器(7-1至7-7)，使物料在物料推进器的作用下在甲烷发酵舱内上下迂回前进，并且在甲烷发酵舱的底部还设有甲烷发酵沼气搅 拌布气器(8)，甲烷发酵舱上部为甲烷集气区(9)，甲烷集气区(9)中的气体经由甲烷发酵气循环风机(23)加压通过甲烷发酵沼气搅拌布气器(8)释放；
    为了保证物料的连通，在甲烷发酵舱、水解发酵舱进料相反的纵向主隔墙末端段下面分别设置了物料推进器。
  2. 按照权利要求1的装置，其特征在于，将甲烷发酵舱、水解发酵舱的纵向主隔墙下面除了作为最后并排被纵向主隔墙隔开的需连通的两格之间的纵向主隔墙部分外没有设物料推进器，其他在每个需要物料联通的横向主隔墙下面均设有物料推进器，物料推进器贯穿整个待连通的主隔墙下面。
  3. 按照权利要求1的装置，其特征在于，上述每个物料推进器包括：两个长轴型推进叶轮、两个推进器驱动轴、推进器外壳；长轴型推进叶轮，整体为长柱形结构，即为具有轴向长度的推进叶轮，即在叶轮翼片设计上采用沿驱动轴方向的长形设计，垂直轴向的截面为哑铃型结构，哑铃型结构的两端和中间外表面均为弧形；每个长轴型推进叶轮均按有一个推进器驱动轴，两个长轴型推进叶轮的轴互相平行，且相向同步旋转，两个长轴型推进叶轮的旋转方向相反，一个顺时针，一个逆时针，旋转的过程中两翼片叶轮表面之间始终保持相对咬合并密封；在每个长轴型推进叶轮外面均设有推进器外壳，推进器外壳的内表面为半圆弧形，使得每个长轴型推进叶轮在旋转的过程中始终与所对应的半圆形空腔内壁相切。推进器外壳的外面均设有阻挡物，使得阻挡物和推进器共同将推进器两边的空间阻挡分割成两部分空间，随着两个长轴型推进叶轮的相对旋转，使得粘稠半固体物料跟着长轴型推进叶轮的旋转从一边空间输送到另一边空间。
  4. 上利用权利要求1-3的任一装置进行连续发酵的方法，其特征在于，包括以下步骤：
    将拟发酵生物质混合料按比例投入水解进料舱(24)，物料在水解加热进料器(25)推动下进入水解进料加热器(26)加热，然后在水解进料器(27)推动下进入水解进料接种均质化舱(10)中，在水解物料接种器(13)、水解进料布料器(14)和水解物料推进器(16-1)的联合作用下，物料被接种和均质化，同时被推进水解发酵舱(11)中；物料在水解发酵舱中被由水解气搅拌布气器(17)释放的压力气流进行搅拌，同时，在发酵仓中设置的水解物料推进器(16-2至16-4)的推动下，物料沿流程方向缓慢前行，整个水解发酵时间为5-6天，最后在水解发酵舱最后一个水解物料推进器(16-5)的推动下，通过水解物料出料均衡器(15)、水解出料器(20)绝大部分进入甲烷发酵进料加热器(19)，一少部分通过水解物料接种器(13)进入到水解进料接种均质化舱(10)中，去完成接种工作；进入甲烷发酵进料加热器(19)的物料，在甲烷发酵进料加热器(19)的加热过程中，水解酸化菌被60-65℃高温抑制或消灭；
    完成水解酸化被加热的物料，通过甲烷发酵进料器(21)进入甲烷发酵进料接种均质化舱(1)中，在甲烷发酵物料接种器(4)、甲烷发酵进料布料器(5)和甲烷发酵物料推进器(7-1)的联合作用下，物料被接种和均质化，同时被推进甲烷发酵舱(2)中。在发酵仓中设置的甲烷发酵物料推进器(7-2至7-6)的推动下，物料沿流程方向缓慢前行，整个发酵时间为20天，最后在甲烷发酵舱最后一个甲烷发酵物料推进器(7-7)的推动下，通过甲烷发酵物料出料均衡器(6)进入甲烷发酵出料舱(3)，出料的一少部分通过甲烷发酵物料接种器(4)进入到甲烷发酵进料接种均质化舱(1)中，去完成甲烷菌的接种工作；出料的其余部分完成整个发酵过程。
  5. 按照权利要求4的方法，其特征在于，在进行连续发酵过程中物料经过水解加热进料器(26)后，物料被加热到33±2℃；水解发酵停留时间5-6天；物料经过在甲烷发酵进料加热器(19)后，物料被加热到60-65℃，甲烷发酵停留时间20天时。
PCT/CN2015/084553 2014-09-17 2015-07-21 一种卧式大型连续沼气干式发酵装置及方法 WO2016041410A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US15/510,806 US9879211B2 (en) 2014-09-17 2015-07-21 Large horizontal device for continuous methane fermentation and method thereof

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201410476086.5 2014-09-17
CN201410476086.5A CN104232473B (zh) 2014-09-17 2014-09-17 一种卧式大型连续沼气干式发酵装置及方法

Publications (1)

Publication Number Publication Date
WO2016041410A1 true WO2016041410A1 (zh) 2016-03-24

Family

ID=52221384

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2015/084553 WO2016041410A1 (zh) 2014-09-17 2015-07-21 一种卧式大型连续沼气干式发酵装置及方法

Country Status (3)

Country Link
US (1) US9879211B2 (zh)
CN (1) CN104232473B (zh)
WO (1) WO2016041410A1 (zh)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104355066B (zh) * 2014-09-17 2017-03-01 北京工业大学 一种大型粘稠半固体均质物料推进器及应用
CN104232473B (zh) * 2014-09-17 2017-01-25 北京工业大学 一种卧式大型连续沼气干式发酵装置及方法
CN107557280A (zh) * 2017-09-06 2018-01-09 河南世博环保科技有限公司 一种卧式粪便固体废弃物发酵无害化处理设备
CN108251285B (zh) * 2018-03-09 2018-12-04 安徽万礼食品有限责任公司 一种新型高效厌氧发酵设备
CN108485945B (zh) * 2018-03-26 2021-06-18 太原理工大学 一种适用于有机固体废弃物资源化利用的反应系统
CN111548913A (zh) * 2020-05-15 2020-08-18 苏州中洁宇科技有限公司 一种餐厨垃圾微生物菌种的制作方法及其应用
CN112321345B (zh) * 2020-11-06 2022-07-22 沂源翰林农业发展有限公司 一种有机肥发酵装置
CN112321346A (zh) * 2020-11-16 2021-02-05 王天庚 一种有机肥发酵用离心滤液装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200971358Y (zh) * 2006-11-24 2007-11-07 河南桑达能源环保有限公司 高效高浓度折流式厌氧反应装置
CN101712923A (zh) * 2009-09-11 2010-05-26 云南昆船设计研究院 一种有机废弃物干式厌氧发酵装置及工艺
CN103881901A (zh) * 2012-12-20 2014-06-25 天津市德盛源环境工程有限公司 有机固废高效干式厌氧发酵设备
CN104232473A (zh) * 2014-09-17 2014-12-24 北京工业大学 一种卧式大型连续沼气干式发酵装置及方法
CN104355066A (zh) * 2014-09-17 2015-02-18 北京工业大学 一种大型粘稠半固体均质物料推进器及应用

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5091315A (en) * 1985-09-03 1992-02-25 The Board Of Trustees Of Stanford University Bioconversion reactor
CN200967822Y (zh) * 2006-11-24 2007-10-31 河南桑达能源环保有限公司 单元成型高效沼气发生器
DE102010010294A1 (de) * 2010-03-04 2011-09-08 Fachhochschule Flensburg Verfahren und Vorrichtung zur anaeroben Fermentation

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200971358Y (zh) * 2006-11-24 2007-11-07 河南桑达能源环保有限公司 高效高浓度折流式厌氧反应装置
CN101712923A (zh) * 2009-09-11 2010-05-26 云南昆船设计研究院 一种有机废弃物干式厌氧发酵装置及工艺
CN103881901A (zh) * 2012-12-20 2014-06-25 天津市德盛源环境工程有限公司 有机固废高效干式厌氧发酵设备
CN104232473A (zh) * 2014-09-17 2014-12-24 北京工业大学 一种卧式大型连续沼气干式发酵装置及方法
CN104355066A (zh) * 2014-09-17 2015-02-18 北京工业大学 一种大型粘稠半固体均质物料推进器及应用

Also Published As

Publication number Publication date
US20170253842A1 (en) 2017-09-07
CN104232473A (zh) 2014-12-24
CN104232473B (zh) 2017-01-25
US9879211B2 (en) 2018-01-30

Similar Documents

Publication Publication Date Title
WO2016041410A1 (zh) 一种卧式大型连续沼气干式发酵装置及方法
CN104312911B (zh) 用于干式厌氧发酵的搅拌装置
EP2449086B1 (en) A device for the production of biogas from organic waste
CN105753519A (zh) 一种畜禽类粪便快速烘干发酵装置
CN104109632B (zh) 一种大型外驱动整体卧式旋转连续沼气干式发酵装置及方法
CN103964903A (zh) 一种有机垃圾处理厌氧与好氧发酵耦合装置
CN108753609B (zh) 一体化三相干式厌氧发酵自适应设备及其产沼气方法
CN204550532U (zh) 有机物发酵搅拌装置
CN204237794U (zh) 一种厌氧发酵罐
WO2017152476A1 (zh) 大型自旋式夹层加温充气发酵罐
CN103387932B (zh) 干式厌氧反应处理装置
CN105624033A (zh) 一种有机垃圾干式厌氧发酵装置
CN202099280U (zh) 秸秆卧式连续干发酵沼气装置
CN105624034A (zh) 一种采用干式厌氧发酵装置处理有机垃圾的方法
CN211947003U (zh) 一种高浓度干式厌氧发酵装置
CN203923033U (zh) 一种新型畜禽粪便厌氧发酵系统
CN201062264Y (zh) 立式机械搅拌沼气装置
KR101716744B1 (ko) 교반 및 스크린벽을 이용한 고상혐기소화장치
CN204198733U (zh) 用于干式厌氧发酵的搅拌装置
CN205501313U (zh) 一种有机垃圾干式厌氧发酵装置
CN207756026U (zh) 复合式搅拌装置
CN206143202U (zh) 一种模块式高效干式厌氧发酵罐
CN204958745U (zh) 一种畜禽粪便无害化处理设备
CN105436193B (zh) 可实现固体废弃物层递式发酵的搅拌装置及反应器
CN108315237A (zh) 重力推流式干发酵气肥联产装置及其方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 15842828

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 15510806

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 15842828

Country of ref document: EP

Kind code of ref document: A1