CN205576160U - Preliminary treatment reactor and marsh gas production facility suitable for lignocellulose and oxygen fermentation - Google Patents
Preliminary treatment reactor and marsh gas production facility suitable for lignocellulose and oxygen fermentation Download PDFInfo
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- CN205576160U CN205576160U CN201620418024.3U CN201620418024U CN205576160U CN 205576160 U CN205576160 U CN 205576160U CN 201620418024 U CN201620418024 U CN 201620418024U CN 205576160 U CN205576160 U CN 205576160U
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Abstract
The utility model discloses a preliminary treatment reactor and marsh gas production facility suitable for lignocellulose and oxygen fermentation, this preliminary treatment reactor include hydrolysis tank (1), and hydrolysis tank (1) is equipped with feed inlet, water inlet and discharge gate, is equipped with agitating unit (2) in hydrolysis tank (1), and hydrolysis tank (1) bottom is equipped with and provides gaseous interval aeration equipment to the jar inner space. Constitute the marsh gas production facility with this preliminary treatment reactor and anaerobic fermentation reactor (21) intercommunication. The preliminary treatment reactor independently comes out the hydrolytic acidification process of lignocellulose raw materials, adopts interval aeration equipment to create the environment that suitable a large amount of useful microbial bred the intergrowth, and it is active to have improved the hydrolase, shortens the time of hydrolysising, simultaneously also having reduced the impact to methanogen, having improved system stability, anaerobic fermentation production marsh gas efficiency improves, has reduced the running cost, treatment degree is big in advance for the volume of anaerobic fermentation reactor (21) reduces greatly, has also reduced investment cost.
Description
Technical field
This utility model relates to the use of the technical field of lignocellulose-like biomass raw material production biogas, specifically
Relate to a kind of lignocellulose that is applicable to hold concurrently the preatreating reactors of aerobe fermentation and biogas production equipment.
Background technology
Biomass resource substantial amounts in the world, of a great variety.The wooden fibre that plant is produced by photosynthesis
Dimension element is one of Renewable resource the abundantest on the earth.The mankind pass through various technological approaches by lignocellulose
Raw material is converted into different types of energy fuel.In lignocellulosic material, agricultural crop straw can be by detesting
Aerobe fermentation technique produces biogas, and biogas in order to generate electricity or can purify into natural gas as vehicle fuel or also
Enter gas distributing system.This has proved to be a kind of utilization ways with the highest comprehensive value.
Crops lignocellulosic material includes straw, such as corn straw, wheat stalk and rice straw etc.,
Have widely distributed, yield is huge and is prone to the features such as collection.People can be these straws as discarded in the past
Thing abandons or burn processing, and this not only causes the waste of the energy also to pollute the environment.Now, farming is utilized
Thing straw carries out during the practice of biogas production the most extensively carries out.But lignocellulosic material due to himself
Construction features makes the conversion process of anaerobic fermentation there is certain technical difficulty.
Agricultural crop straw is made up of substantial amounts of Organic substance and a small amount of inorganic matter and water, and it is organic
Main component is the carbohydrate of cellulose family and soluble sugar and a small amount of thick protein and crude fat.
Wherein fiber-like carbohydrate mainly includes cellulose, hemicellulose and lignin etc., and these are also to constitute
The main component of plant cell wall.For the straw of agricultural crop straw, especially mummification, the conversion master of biogas
Deriving from carbohydrate cellulose therein and the anaerobic degradation of hemicellulose, lignin is then difficult to hydrolyze
And anaerobism is converted into biogas.
In straw, cellulose mainly by glucose molecule by β-1-4 glycosidic bond couple together linear
High molecular polymer.The homogeneity polysaccharide that hemicellulose is not made up of a certain monosaccharide, it be by pentose,
The monosaccharide such as hexose and the complex plycan with side chain of alduronic acid composition.Hemicellulose crosses one another connection, inhales
Be attached on cellulose, strap-on structure albumen and lignin, formed matrix structure a part, be microorganism and
The physical barrier of enzymolysis.Lignin is by having that ehter bond and carbon-carbon bond are formed by connecting by phenylpropane units
The high polymer of three-D space structure.Lignin can form covalent chemical with the fraction of half fiber and be good for, this
Connect structural rigidity and the integrity degree providing lignocellulose so that lignocellulose is not susceptible to swollen and makees
With.The materials such as these three material and pectin jointly bond composition space structure be referred to as cellulose crystallite knot
Structure.The high-crystallinity of straw defines a kind of barrier, especially mummification straw for the microorganism species of anaerobism
Molecular chemistry key there is higher hydrophobicity, microorganism and enzyme hardly enter and inside stalk fibre, carry out water
Solution effect.Additionally, hydrolytic enzyme to be existed between lignin and cellulose and hemicellulose certain competitive adsorption,
This inhibits the hydrolysis of straw the most to a certain extent.If lignocellulose can not be hydrolyzed efficiently,
Follow-up fermentative acidification and methanation will be unable to be normally carried out.
Pretreatment measure for lignocellulose at present mainly has physics pretreatment, Chemical Pretreatment and biology
Pretreatment, but these preprocess methods are improving lignocellulosic material characteristic, are improving raw material digestibility and increasing
There is also series of problems while adding gas production, be respectively arranged with its different limitation.
Chinese patent application publication No. CN101870988A (date of publication 2010.10.27) discloses a kind of wood
Matter cellulosic material is held concurrently oxygen-anaerobic sequence alternate fermentation technology, and its production process is held concurrently gas anaerobism in solid phase respectively
The independent reactor in fermentation zone and two, liquid phase anaerobic fermentation zone is carried out, but does not discloses concrete solid phase
The apparatus structure of double oxygen anaerobic fermentation zone.The aerogenesis cycle is long.
Chinese patent application publication No. 101012436A (date of publication on August 8th, 2007) discloses one
Processing the anaerobic reactor of lignin fibre raw material, it includes, between methane phase sweathouse and acidogenic fermentation, adding water
The compost that the lignocellulosic material of moistening inoculation is carried out 3～7 days between acidogenic fermentation processes, and enters after terminating again
Row water spray (bringing oxygen into).The percolate produced enters between liquid storage, and a filtrate part pumps between methane fermentation
(filtrate pumped into add water mixing), another part is back between acidogenic fermentation (pump into water or methane simultaneously
Sweathouse water outlet).Device is complicated, takes up room big.
No matter using what pretreatment mode, the hydrolysis of lignocellulose, acidization mainly or are passed through to detest
Aerobe fermentation realizes, and the transformation period is long, in order to keep the lasting supply of biogas, needs bigger reactor volume.
The biogas conversion ratio that in lignocellulosic material, unit is organic is low, and especially straw, gas production is lower.
Straw is also easy to be formed in the reactor floating layer, and then forms crust layer, for avoiding scum layer, needs longer
Mixing time and stirring energy consumption, cause investment and operating cost the highest.It addition, the turnover of response system
It is high that material and material transmit difficulty, and pipeline valve the most easily blocks, and needs the mode using some chemistry to carry out
Pretreatment, causes the most again maintenance cost high, and easily causes secondary pollution.
Utility model content
In order to the device production cycle solving to utilize in prior art lignocellulosic material production biogas is long, raw
The defects such as the regulation of product condition is inconvenient, equipment occupation space is big, this utility model provides one and is applicable to wood
The hydrolysis pretreatment unit of matter cellulosic material, a kind of lignocellulose that is applicable to is held concurrently the pre-of aerobe fermentation
Treatment reactor so that enter before anaerobic fermentation produces biogas at lignocellulosic material and first carry out sufficient water
Solve pretreatment, improve gas production, shorten the production cycle.
This double aerobe fermentation preatreating reactors, it is adaptable to hold concurrently aerobe fermentation pretreating process by aeration and anaerobism is sent out
The biogas production method of ferment technique composition.This method is first will to add through the lignocellulosic material pulverized
Enter in animal wastes culture fluid, temperature 35～45 DEG C, pH value 6～8, aeration 10～40 minutes with stop
Aeration 10～40 minutes alternately and under conditions of aeration time >=stopping aeration time, carry out aerobe fermentation of holding concurrently
Pretreatment, pretreatment hydraulic detention time is 12～48 hours；Then pretreated fermented feed liquid is imported
Anaerobic fermentation reactor (21) carries out anaerobic fermentation and produces biogas.For adapting to the pretreatment of this biogas production process
Step, this utility model devises a kind of aerobe fermentation preatreating reactors of holding concurrently.
This is applicable to lignocellulose and holds concurrently the preatreating reactors of aerobe fermentation, including hydrolytic decomposition pot (1), hydrolytic decomposition pot (1)
It is provided with charging aperture, water inlet and discharging opening, in hydrolytic decomposition pot (1), is provided with agitating device (2), hydrolytic decomposition pot (1) bottom
It is provided with space in tank and the interval aerator of gas is provided.Interval aerator uses intermittent duty to control,
By being spaced the intermittent duty of aerator, meet the mesh of material system interval aeration in preatreating reactors
, it is achieved hold concurrently oxygen and anaerobism sweat alternately, improve raw material hydrolysis efficiency, when shortening hydrolysis
Between, improve gas producing efficiency.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Described interval aerator includes aerator (11), Aeration fan (13) and the aeration tube the two connected
(12), aeration tube (12) is positioned at the part of hydrolytic decomposition pot (1) and encloses and be located at hydrolytic decomposition pot (1) bottom, multiple aerators (11)
It is installed on the aeration tube (12) that hydrolytic decomposition pot (1) is internal.The design bottom hydrolytic decomposition pot of this aeration tube can be protected
The gas that card is filled with is evenly distributed under the cooperation of agitating device in material system, makes material system oxygen supply fill
Foot, fully meets the oxygen demand of aerobic microbiological and hydrolytic enzyme.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Being additionally included in line gas analyser (10), on-line gas analysis instrument (10) is provided with sampling flexible pipe (101), samples soft
Pipe (101) stretches into the headroom in hydrolytic decomposition pot (1).Owing to material system is not completely filled with in fermentation tank,
Sub-fraction space can be stayed in top, so, can pass through gas on-line analyzer analyte during reactor work
The gas componant of feed liquid face upper air, monitors reaction system running status, to better control over operating mode, and
Time adjust reactor operation, make system environment keep optimum state.
As a kind of preferred version, in above-mentioned double aerobe fermentation preatreating reactors, hydrolytic decomposition pot (1) is additionally provided with temperature
Degree monitoring device (14) and dissolved oxygen DO value monitoring device (15).The two device is easy to monitor in reactor
The temperature of material system and dissolved oxygen situation, adjust the operating modes such as aeration rate, aeration time, temperature, make pre-place
Reason environment is maintained at and is most suitable for growth of microorganism and the state of enzyme performance activity.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Including circulating water temperature-regulating system.Hydrolytic process produces a large amount of reaction heat sometimes, when heat radiation can cause not in time
Hydrolytic tank internal temperature persistently rises, unfavorable to microorganism, needs to use circulating water temperature-regulating system to cool down,
Ambient temperature in regulation reactor.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Described circulating water temperature-regulating system includes the heating coil (3) being arranged in hydrolytic decomposition pot (1), and by pipeline with
Cold water storage cistern (16) that heating coil (3) connects and boiler (17), pipeline is provided with control valve.Heating coil (3)
Arrange and need to meet the requirement not affecting agitating device (2) normally work, it is ensured that reactor can run well.
Preferably heating coil (3) coiling is arranged on hydrolytic decomposition pot (1) inwall.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Described cold water storage cistern (16) is provided with the first outlet pipe and the first return pipe, and the first outlet pipe is provided with water supply pump (5)
With cold water flow meter (9), boiler (17) is provided with the second outlet pipe and the second return pipe, the second outlet pipe sets
Heat-exchanger pump (4) and hot water flow meter (8), the first outlet pipe and the second outlet pipe is had to converge formation water main,
Connecting with the water inlet end of heating coil (3), water main is provided with cold water temperature meter (7), the first return pipe and
Second return pipe converges formation and adds the return main of hot plate, and return main is provided with hot water temperature's meter (6).Adopt
By this circulating water temperature-regulating system, monitored the water velocity entered in hydrolytic decomposition pot by effusion meter and thermometer
And temperature, regulation flow is to adapt to system in hydrolytic decomposition pot, by the regulative mode regulation tank Nei Wenduda relaxed
To the suitableeest, do not interfere with microorganism and the activity of enzyme in system.Cold water it is passed through during temperature height, logical when temperature is low
Enter hot water.
As a kind of preferred version, the preatreating reactors of above-mentioned aerobe fermentation of holding concurrently be applicable to lignocellulose,
Described agitating device (2) includes a rotary shaft and installs stirring vane on the rotary shaft, in hydrolytic decomposition pot (1)
In be provided with central draft tube (20) around stirring vane.The rotary shaft of agitating device is driven rotation by actuating unit
Turning, sectional installs multiple stirring vanes on the rotary shaft.Central draft tube (20) is tubular construction, around
Stirring vane to arrange, when rotary shaft drives stirring vane to rotate, central draft tube (20) interior feed velocity
Accelerate, the lignocellulosic material scum silica frost such as the floating straw in feed liquid top layer can be guided to flow downward, make whole
Hydrolytic decomposition pot (1) interior feed liquid fluidised form reaches circulation, and scum silica frost is mixed homogeneously with feed liquid, increases amount of oxygen in feed liquid,
Promote that lignocellulosic material is fully hydrolyzed.
This utility model additionally provides a kind of biogas production equipment, by being applicable to wooden fibre described in any of the above
The preatreating reactors of the double aerobe fermentation of dimension element connects composition with anaerobic fermentation reactor (21).Double aerobe fermentation is located in advance
Reason reactor is after the process that is hydrolyzed by raw material, and hydrolysis feed liquid can be passed through pipeline (18) and pump into anaerobism and send out
Ferment reactor (21) produces biogas to proceed anaerobic fermentation.Hydrolyzation material liquid pump enters anaerobic fermentation reactor (21)
(i.e. marsh-gas fermentation tank), the fermentation liquid in anaerobic fermentation reactor (21) can also be back to hydrolytic decomposition pot (1).
Anaerobic fermentation reactor (21) has a variety of form, and the material through hydrolysis process can enter various forms of
Fermentation tank, therefore, for the version not requirement of anaerobic fermentation reactor (21), as long as realizing anaerobism
The purpose of fermentation gas, can select existing known any anaerobic fermentation for biogas production to fill
Put.
As a kind of preferred version, in above-mentioned biogas production equipment, described anaerobic fermentation reactor (21) is provided with
The biogas slurry return duct (19) connected with the water inlet of hydrolytic decomposition pot (1).
From technology stability, Practical Project, biogas slurry is temperature out and double oxygen from fermentation reactor
Reaction temperature in fermentation preatreating reactors is close, relative to the clear water under room temperature, to preatreating reactors
In microorganism for, the change of temperature impact is less.Microorganism does not likes sometimes hot and sometimes cold.In biogas slurry still
Containing undegradable organic matter, can flow back in system.From operating cost, backflow biogas slurry is permissible
Utilize the heat in biogas slurry, reduce the system demand from extraneous additional heat, it is possible to reduce a part is run into
This, the outer discharge capacity of biogas slurry finally, for system also greatly reduces.Therefore biogas slurry return duct is set with natural pond of refluxing
Liquid is conducive to increasing biological cycle, reduces thermal loss, reduces and arranges outside biogas slurry.
Compared with prior art, this utility model has the advantages that
1, preatreating reactors of the present utility model, isolates Hydrolysis Acidification from anaerobic reactor
Come, and use interval aerator to carry out being spaced aeration, create one and be conducive to microorganism amount reproduction
Symbiotic environment, be advantageous to hydrolytic enzyme play catalytic action.Lignocellulosic material hydrolysis time is short,
Efficiency is high, only needs the time of staying of 1～2 day, and hydrolyzed solution can be quick after entering anaerobic fermentation reactor (21)
Carry out biogas conversion；Due to high efficiency hydrolysis acidification pretreatment, biogas transformation efficiency is greatly improved.
2, can produce along with substantial amounts of heat, so arranging recirculated water in double aerobe fermentation preprocessing process
On the one hand thermoregulating system can take away the heat in reactor by circulating water, the most too low in temperature
Time can also be heated by circulating hot water, on pipeline arrange thermometer can monitor reaction system temperature in real time
Degree, then worked in coordination by water supply pump (5) or heat-exchanger pump (4) and effusion meter and adjust system temperature and reach
Good value.Easy to control, water can recycle, economy.
3, biogas production equipment of the present utility model, makes many inhibition chemical substances in preatreating reactors
Obtaining degraded buffering, reduce the directly impact to methanogen floras, anaerobic fermentation produces the in hgher efficiency of biogas,
And then reduction operating cost.Owing to pretreatment degree is big so that the volume of anaerobic fermentation reactor (21) is significantly
Reduce, also reduce cost of investment.
Accompanying drawing explanation
Fig. 1 is that this utility model is applicable to lignocellulose and holds concurrently the structural representation of preatreating reactors of aerobe fermentation
Figure；
Fig. 2 be this utility model be applicable to lignocellulose hold concurrently aerobe fermentation preatreating reactors horizontal section knot
Structure schematic diagram；
Fig. 3 is the structural representation of this utility model biogas production equipment.
Reference: 1 hydrolytic decomposition pot, 2 agitating devices, 3 heating coils, 4 heat-exchanger pumps, 5 water supply pumps, 6 hot water
Thermometer, 7 cold water temperature meters, 8 hot water flow meters, 9 cold water flow meters, 10 on-line gas analysis instrument, 101
Sampling flexible pipe, 11 aerators, 12 aeration tubes, 13 Aeration fans, 14 device for detecting temperature, 15 dissolved oxygen
DO value monitoring device, 16 cold water storage cisterns, 17 boilers, 18 pipelines, 19 biogas slurry return ducts, 20 center water conservancy diversion
Cylinder, 21 anaerobic fermentation reactors.
Detailed description of the invention
Below in conjunction with preferred specific embodiment, the utility model is described in further detail, to help understanding this
The content of utility model.
As it is shown in figure 1, the lignocellulose that is applicable to of the present utility model is held concurrently the preatreating reactors of aerobe fermentation
(being called for short aerobe fermentation preatreating reactors of holding concurrently), including hydrolytic decomposition pot 1, hydrolytic decomposition pot 1 is provided with charging aperture, water inlet
Mouth and discharging opening, be provided with agitating device 2 in hydrolytic decomposition pot 1, agitating device 2 includes that one is driven by actuating unit
The rotary shaft rotated, rotary shaft is provided with stirring vane, and the outside of stirring vane is around arranging central draft tube
20.It is provided with space in tank bottom hydrolytic decomposition pot 1 and the interval aerator of gas is provided.Hydrolytic decomposition pot is externally provided with
Line gas analyser 10, on-line gas analysis instrument 10 is provided with sampling flexible pipe 101, and sampling flexible pipe 101 stretches into
Headroom in hydrolytic decomposition pot 1.Device for detecting temperature 14 and dissolved oxygen it is additionally provided with on the sidewall of hydrolytic decomposition pot 1
DO value monitoring device 15.
As depicted in figs. 1 and 2, described interval aerator include aerator 11, Aeration fan 13 and
The aeration tube 12 the two connected, aeration tube 12 is positioned at the part of hydrolytic decomposition pot 1 and encloses and be located at hydrolytic decomposition pot 1 end
Portion, multiple aerators 11 are installed on the aeration tube 12 within hydrolytic decomposition pot 1.Between interval aerator uses
Have a rest operation control, computer installation can be passed through, adjust parameter and automatically control aeration time and stop aeration
Time.
Double aerobe fermentation preatreating reactors of the present utility model, also includes circulating water temperature-regulating system, this system bag
Include the heating coil 3 being arranged in hydrolytic decomposition pot 1, and the cold water storage cistern connected by pipeline with heating coil 3
16 and boiler 17, pipeline is provided with control valve.
Cold water storage cistern 16 is provided with the first outlet pipe and the first return pipe, and the first outlet pipe is provided with water supply pump 5 He
Cold water flow meter 9, boiler 17 is provided with the second outlet pipe and the second return pipe, and the second outlet pipe is provided with
Heat-exchanger pump 4 and hot water flow meter 8, the first outlet pipe and the second outlet pipe converge formation water main, and add
The water inlet end connection of hot coil 3, water main is provided with cold water temperature meter 7, the first return pipe and second time
Water pipe converges formation and adds the return main of hot plate, and return main is provided with hot water temperature and counts 6.
As it is shown on figure 3, the discharging opening of double aerobe fermentation preatreating reactors of the present utility model is by pipeline 18
With anaerobic fermentation reactor 21 UNICOM, pipeline 18 is provided with pump, and anaerobic fermentation reactor 21 is provided with biogas slurry
Return duct 19, one end extends in anaerobic fermentation reactor 21, and the other end joins with the water inlet of hydrolytic decomposition pot 1
Logical.It is equipped with pump on pipeline 18 and biogas slurry return duct 19.
When carrying out biogas production, first agricultural crop straw is carried out broken silk of rubbing and processes so that stalk fibre
Length is within 2cm, in case hydrolysis utilizes.
In hydrolytic decomposition pot 1, add fresh cattle manure by charging aperture, by water inlet dilute cattle manure, adjust
Save to total solid mass percent at the excrement slurry of 8%, open the second outlet pipe of boiler 17, by adding
Hot coil 3 is by hydrolytic decomposition pot 1 heat temperature raising and is maintained at about 40 DEG C, cultivates general week age, it is thus achieved that
Faecal microbiota culture fluid.
Pass through the stalk handled well in charging aperture puts into hydrolytic decomposition pot 1 and open agitating device 2 to fill
Divide mix and blend, open interval aerator during adding straw, keep aeration state, be simultaneously introduced
A small amount of cellulolytic enzyme preparation (purchase commercial goods) carries out catalyzing hydrolysis.Control the body in hydrolytic decomposition pot 1
In system, total solid mass percent is 6～15%, pH value 6～8.Open Aeration fan 13, adjust interval
Aerator program parameter, changes into continuous aeration being spaced aeration, and the time is 10～40 minutes aerations, 10～40
Minute closing, and aeration time >=stopping aeration time, in making preatreating reactors, mixed liquor is at aeration shape
Dissolved oxygen concentration under state is less than 1.5 mg/litre, constantly repeats this aeration mode, carries out double aerobe fermentation pre-
Processing, hydraulic detention time was at 12～48 hours, it is thus achieved that hydrolysed ferment liquid.
Stop aeration and stirring, open the pump on pipeline 18, pump out less than mixed liquor in hydrolytic decomposition pot 1
The 50% of (the hydrolysed ferment liquid of the most above-mentioned acquisition) cumulative volume enters follow-up anaerobic fermentation reactor 21,
Carrying out anaerobic fermentation and produce biogas, the material hydraulic detention time in anaerobic fermentation reactor 21 is typically smaller than
30 days.Need to supplement a certain amount of straw and anaerobic fermentation reactor 21 after pump is complete every time in hydrolytic decomposition pot 1
The biogas slurry (being pumped into by biogas slurry return duct 19) of backflow, adds clear water dilution when lettuce is too high, to protect
The total solid mass percent held in hydrolytic decomposition pot 1 maintains 10～12%.During whole, every day is required for
The relevant operational factor of hydrolytic decomposition pot 1 is monitored by timing, monitors temperature including by device for detecting temperature 14
Degree, dissolved oxygen DO value monitoring device 15 monitors dissolved oxygen, it is also possible to include monitoring solids concentration TS%,
Organic concentration VS%, temperature T, volatile fatty acid VFA and double aerobe fermentation preatreating reactors are produced
Raw various gas componants etc..Regulation operating mode is in optimal operational condition with holding system as required.
By mixed liquor being carried out temperature by the way of circulating water in heating coil 3 or hot water in hydrolytic decomposition pot 1
Degree adjusts, and controls at 38～42 DEG C.
Adjusting operating mode by test, after making system reach optimal operational condition, agricultural crop straw is raw as raw material
The content of the methane in sewage gas produced reaches as high as 57%, and the methane obtained far above existing biogas production technique contains
Amount.The biogas production time is greatly shortened, and runs system small portable, investment reduction.
The above is only preferred implementation of the present utility model, it is noted that for the art
For those of ordinary skill, on the premise of without departing from this utility model principle, it is also possible to make some improvement
And retouching, these improvements and modifications also should be regarded as protection domain of the present utility model.
Claims (10)
1. it is applicable to lignocellulose hold concurrently the preatreating reactors of aerobe fermentation, including hydrolytic decomposition pot (1), water
Solve tank (1) and be provided with charging aperture, water inlet and discharging opening, in hydrolytic decomposition pot (1), be provided with agitating device (2), its feature
Being, hydrolytic decomposition pot (1) bottom is provided with space in tank and provides the interval aerator of gas.
The lignocellulose that is applicable to the most according to claim 1 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, described interval aerator includes aerator (11), Aeration fan (13) and the two is connected
Logical aeration tube (12), aeration tube (12) is positioned at the part of hydrolytic decomposition pot (1) and encloses and be located at hydrolytic decomposition pot (1) bottom, many
Individual aerator (11) is installed on the aeration tube (12) that hydrolytic decomposition pot (1) is internal.
The lignocellulose that is applicable to the most according to claim 1 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, being additionally included in line gas analyser (10), on-line gas analysis instrument (10) is provided with sampling flexible pipe
(101), the headroom in hydrolytic decomposition pot (1) is stretched in sampling flexible pipe (101).
The lignocellulose that is applicable to the most according to claim 1 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, hydrolytic decomposition pot (1) is additionally provided with device for detecting temperature (14) and dissolved oxygen DO value monitoring device (15).
The lignocellulose that is applicable to the most according to claim 1 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, also include circulating water temperature-regulating system.
The lignocellulose that is applicable to the most according to claim 5 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, described circulating water temperature-regulating system includes the heating coil (3) being arranged in hydrolytic decomposition pot (1), with
And passing through cold water storage cistern (16) and the boiler (17) that pipeline connects with heating coil (3), pipeline is provided with control valve.
The lignocellulose that is applicable to the most according to claim 6 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, described cold water storage cistern (16) is provided with the first outlet pipe and the first return pipe, and the first outlet pipe sets
Having water supply pump (5) and cold water flow meter (9), boiler (17) is provided with the second outlet pipe and the second return pipe, and second
Outlet pipe is provided with heat-exchanger pump (4) and hot water flow meter (8), the first outlet pipe and the second outlet pipe converge formation
Water main, connects with the water inlet end of heating coil (3), and water main is provided with cold water temperature meter (7), the
One return pipe and the second return pipe converge formation and add the return main of hot plate, and return main is provided with hot water temperature
Meter (6).
The lignocellulose that is applicable to the most according to claim 1 is held concurrently the preatreating reactors of aerobe fermentation,
It is characterized in that, described agitating device (2) includes a rotary shaft and installs stirring vane on the rotary shaft,
It is provided with central draft tube (20) around stirring vane in hydrolytic decomposition pot (1).
9. a biogas production equipment, it is characterised in that by arbitrary described being applicable to of claim 1～8
The hold concurrently preatreating reactors of aerobe fermentation of lignocellulose connects composition with anaerobic fermentation reactor (21).
Biogas production equipment the most according to claim 9, it is characterised in that described anaerobic fermentation is anti-
Device (21) is answered to be provided with the biogas slurry return duct (19) that the water inlet with hydrolytic decomposition pot (1) connects.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107090475A (en) * | 2017-04-25 | 2017-08-25 | 青岛天人环境股份有限公司 | A kind of technique of bionic anaerobic fermentation Biogas |
| CN107460120A (en) * | 2017-10-10 | 2017-12-12 | 英普（北京）环境科技有限公司 | A kind of cellulose, micro- oxygen pretreatment unit of lignin fermentation methane production and method |
| CN108690804A (en) * | 2018-06-14 | 2018-10-23 | 山东中农绿能工程设计有限公司 | Bio-natural gas production system and control method |
| CN113354846A (en) * | 2021-08-06 | 2021-09-07 | 甘肃华瑞农业股份有限公司 | Device for manufacturing degradable agricultural mulching film by decomposing plant fibers and using method thereof |
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2016
- 2016-05-10 CN CN201620418024.3U patent/CN205576160U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107090475A (en) * | 2017-04-25 | 2017-08-25 | 青岛天人环境股份有限公司 | A kind of technique of bionic anaerobic fermentation Biogas |
| CN107460120A (en) * | 2017-10-10 | 2017-12-12 | 英普（北京）环境科技有限公司 | A kind of cellulose, micro- oxygen pretreatment unit of lignin fermentation methane production and method |
| CN108690804A (en) * | 2018-06-14 | 2018-10-23 | 山东中农绿能工程设计有限公司 | Bio-natural gas production system and control method |
| CN113354846A (en) * | 2021-08-06 | 2021-09-07 | 甘肃华瑞农业股份有限公司 | Device for manufacturing degradable agricultural mulching film by decomposing plant fibers and using method thereof |
| CN113354846B (en) * | 2021-08-06 | 2022-08-30 | 甘肃华瑞农业股份有限公司 | Device for manufacturing degradable agricultural mulching film by decomposing plant fibers and using method thereof |
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