CN107328274A - A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique - Google Patents
A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique Download PDFInfo
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- CN107328274A CN107328274A CN201710502664.1A CN201710502664A CN107328274A CN 107328274 A CN107328274 A CN 107328274A CN 201710502664 A CN201710502664 A CN 201710502664A CN 107328274 A CN107328274 A CN 107328274A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D9/04—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being formed by spirally-wound plates or laminae
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- 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
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- 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
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
- F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The invention provides a kind of heat exchanger, the preparation facilities of wind-powered electricity generation methane and its technique, device includes anaerobic fermentation tank, bioreactor, wind power generation plant and electrolytic water device, also include Hydrogen Line, methane conduit and its carbon dioxide conduit being connected with bioreactor, for inputting hydrogen, methane and carbon dioxide into bioreactor, valve and speed detector are set on each pipeline simultaneously, and the valve and speed detector carry out data with controller and coupled；Controller is according to the hydrogen entered in bioreactor, the molal quantity of methane and carbon dioxide, automatically control Hydrogen Line, methane conduit and its carbon dioxide conduit valve, to input corresponding gas into bioreactor, the gas content in bioreactor is set to reach optimal ratio.The present invention is capable of the flow of intelligent control methane and hydrogen, so that the preparation of methane reaches optimal yield by being separately provided hydrogen, methane and carbon dioxide pipeline.
Description
Technical field
The invention belongs to field of energy utilization, more particularly to a kind of heat exchanger and methane preparation technology including heat exchanger and
System, belongs to heat exchanger and its application field.
Background technology
With the rapid development of modern social economy, the mankind are increasing to the demand of the energy.But coal, oil, day
The traditional energy storage levels such as right gas constantly reduce, increasingly in short supply, rising steadily for price are caused, while conventional fossil fuel is caused
Problem of environmental pollution it is also further serious, these development that all limit society significantly and the raising of human life quality.Biogas
It is inexpensive regenerative resource, but usually requires to purify biogas in practice, produce methane, meets different purposes (ratios
Such as：Be used as motor vehicle fuel) relevant technical requirements.Traditional methane purification technology needs to consume mass energy, does not meet and works as prosthomere
Can emission reduction and the requirement of environmental protection.
During methane production, generally require and condensed by heat exchanger, current heat exchanger is all using logical
Common heat exchanger, can not well suitable gas condensation purification, it is therefore desirable to develop a kind of changing for new type
Hot device, makes it meet the condensation of gas in biogas production process purification.
It is also to exist always in methane production technique in addition, for the production process of methane, how to improve the output capacity of methane
Pursue, be the effective ways for improving production biomethane efficiency using hydrogen purification biogas, this method is based on
Sabatier reacts：CO2+4H2-CH4+2H2O.Traditionally, the reaction is typically real using ruthenium (Ru) base and nickel (Ni) base catalyst
It is existing.But do not have the technique or equipment of a sleeve forming at present to realize that hydrogen extracts methane.
The content of the invention
The present invention is intended to provide the heat exchanger and its utilization electric energy that are used in a kind of hydrogen purification biogas are electrolysed and produced
Hydrogen purification biogas is the technique for improving production biomethane efficiency, and the technology utilization biological method is realized
Sabatier reacts.
To achieve these goals, technical scheme is as follows：A kind of plate-fin heat exchanger, the plate fin heat-exchanging
Device includes setting fin between plate parallel to each other, the plate, and the fin includes the sloping portion for favouring plate,
Projection is processed by impact style on sloping portion, so that the fluid of sloping portion both sides passes through impact style on sloping portion
The hole connection of formation；The projection stretches out from sloping portion along simulation model for mixing gases flows direction.
A kind of preparation facilities of wind-powered electricity generation methane, including anaerobic fermentation tank, bioreactor, wind power generation plant and electrolysis water
Device, the wind power generation plant is connected with electrolytic water device, and electrolytic water device is connected with bioreactor, by the hydrogen of generation
It is input in bioreactor, the anaerobic fermentation tank is connected with bioreactor, the biogas that the anaerobic fermentation tank is produced enters
Enter bioreactor, contain methane and carbon dioxide into the biogas of bioreactor；Also include and bioreactor
Connected Hydrogen Line, methane conduit and carbon dioxide conduit, for inputting hydrogen, methane and titanium dioxide into bioreactor
Carbon, while setting valve and speed detector on each pipeline, the valve and speed detector enter line number with controller
According to connection；Controller automatically controls hydrogen pipe according to the hydrogen entered in bioreactor, the molal quantity of methane and carbon dioxide
Road, methane conduit and carbon dioxide conduit valve, to input corresponding gas into bioreactor, make in bioreactor
Gas content reach optimal ratio.
Preferably, setting density of hydrogen detection means, methane concentration detection device, carbon dioxide in bioreactor
Concentration detection apparatus, controller detects the molal quantity of hydrogen in bioreactor, methane, carbon dioxide respectively, and according to detection
Result adjust each valve, the gas content in bioreactor is reached optimal ratio.
If preferably, controller detection enters the hydrogen and methane, the body of the synthesis of carbon dioxide of bioreactor
Product ratio is more than 1.43:1, then controller automatically turn down the aperture of hydrogen valve；If detecting hydrogen and methane, carbon dioxide
Synthesis volume ratio be less than 1.43:1, then increase the aperture of hydrogen valve.
If preferably, controller detection enters bioreactor hydrogen and methane, the volume of the synthesis of carbon dioxide
Ratio is more than 1.43:1, it is meant that hydrogen is excessive, then controller increases the aperture of methane valve automatically；If detection hydrogen with
Methane, the volume ratio of the synthesis of carbon dioxide are less than 1.43:1, then controller control reduces the aperture of methane air valve.
If preferably, controller detection enter bioreactor biological methane Mol concentration, not less than 98%,
Then meet and require, if the Mol concentration of methane is less than 98%, there are two kinds of reasons, if being increased by hydrogen carbon dioxide more；Such as
Fruit hydrogen is more, just reduces hydrogen, therefore, if the Mol concentration that controller detection enters the methane of bioreactor is less than 98%
When, the molal quantity of carbon dioxide is further detected, (volume of carbon dioxide and hydrogen is preferred if carbon dioxide is more relative to hydrogen
Ratio is 1：1), it is increased by the aperture of hydrogen valve；If hydrogen is more relative to carbon dioxide, controller turns down hydrogen valve
Aperture.
Preferably, setting biogas cleaning apparatus between anaerobic fermentation tank and bioreactor.
Preferably, the bioreactor is connected with condenser.
Preferably, the condenser is plate-fin heat exchanger, the plate-fin heat exchanger includes plate parallel to each other,
Fin is set between the plate, and the fin includes the sloping portion for favouring plate, by punching press side on sloping portion
Formula processes projection, so that the fluid of sloping portion both sides is connected by the hole of impact style formation on sloping portion；It is described prominent
Rise and stretch out from sloping portion along simulation model for mixing gases flows direction.
Preferably, the bearing of trend of the projection and the angle of flow direction of mixture are a, same sloping portion
Multiple projections are set, and along the flow direction of mixture, described angle a is less and less.
The catalyst used in a kind of methane preparation technology of above-mentioned preparation facilities, bioreactor is hydrogen auxotype production first
Alkane bacterium.
Preferably, into the biogas of bioreactor, the molar content more than 45% of methane, carbon dioxide rubs
Your percentage composition is more than 30%.
Compared with prior art, the present invention has the advantage that：
1) present invention, being capable of intelligent control methane and hydrogen by being separately provided hydrogen, methane and carbon dioxide pipeline
Flow so that the preparation of methane reaches optimal yield, it is to avoid waste.
2) present invention is using wind-force or device of solar generating connection electrolytic water device, by being electrolysed the hydrogen system produced
Standby methane, has saved the energy.
3) present invention develops a kind of heat exchanger for the condensation purification for adapting to gas, can improve the efficiency of condensation.
4) present invention is realized the production of methane by biological method, effectively increases first by setting bioreactor
The production efficiency of alkane.
5) present invention proposes a kind of process of brand-new production biomethane, by anaerobic fermentation and biogas
Change process combines, and while reduction methane purification process power consumption, methane production is significantly increased, thus improve anaerobic fermentation and
The whole efficiency of gasification of biomass.
6) membrane separator of the invention is made of doughnut and Matrimid polymeric materials, is a kind of as glass
The same polymeric membrane, by the effect of membrane separator, separation can reach molecular level.
Brief description of the drawings
Fig. 1 is the process chart for preparing biomethane of the present invention；
Fig. 2 is a kind of plate-fin heat exchanger heat exchange plate structural representation of the invention；
Fig. 3 is the structural representation of a plate wing unit of the invention；
Fig. 4 is the schematic diagram that the present invention sets raised structures sloping portion plane；
Fig. 5 is another schematic diagram that the present invention sets raised structures sloping portion plane；
Fig. 6 is the denation structural representation of the present invention；
Fig. 7 is the tangent plane structural representation in denation runner of the present invention；
Fig. 8 is another embodiment process chart for preparing biomethane of the present invention.
Reference is as follows：
1 biogas stream, 2 hydrogen streams, 3 methane streams, 4 anaerobic fermentation tanks, 5 biogas cleaning apparatus, 6 bioreactors, 7 electrolysis waters
Device, 8 wind power generation plants, 9 condensers, 10 seals, 11 fluid passages, 12 plates, 13 sloping portions, 14 horizontal components,
15 projections, 16 fins
Embodiment
The embodiment to the present invention is described in detail below in conjunction with the accompanying drawings.It should be noted that herein
It is molar content in the case of gas content, no specified otherwise.
Fig. 1 illustrates a kind of technological process for preparing biomethane, as shown in figure 1, described preparation technology includes
Anaerobic fermentation tank 4, bioreactor 6, electrolytic water device 7 and wind power generation plant 8, the biogas that the anaerobic fermentation tank 4 is produced
Into in bioreactor 16, contain methane and carbon dioxide into the biogas of bioreactor 13, preferably, content is most
Many is methane and carbon dioxide successively；Wind power generation plant 8 is connected with electrolytic water device 7, and wind power generation plant 8 is to electrolysis water
Electricity is conveyed in device 7, the hydrogen stream 2 that the electrolysis of electrolytic water device 7 is produced enters in bioreactor 6, in bioreactor 6,
Carry out the reaction of synthesizing methane：CO2+4H2-CH4+2H2O；The catalyst used in bioreactor 6 is hydrogen auxotype methane phase
Bacterium.
Preferably, biogas is before bioreactor 6 is entered, also purified by biogas cleaning apparatus 5, to remove
Impurity, such as hydrogen sulfide, ammonia, oxosilane etc..
Preferably, into the biogas of bioreactor, the molar content more than 45% of methane, carbon dioxide rubs
Your percentage composition is more than 13%.
Preferably, the methane from bioreactor 6 out is reclaimed after condenser 9.
Preferably, in bioreactor 6, the ratio of carbon dioxide and hydrogen is：1 to 4 (molal quantity ratio).
Set on the pipeline of biogas stream 1 and hydrogen valve is set on biogas valve, the pipeline of hydrogen stream 2, controlled by valve
Biogas and the quantity of hydrogen that system enters in bioreactor.
The system also includes carbon dioxide concentration detecting device, density of hydrogen detection means, methane concentration detection device,
The carbon dioxide concentration detecting device, density of hydrogen detection means, methane concentration detection device and controller carry out data company
Connect；The system also includes flow monitor, and the flow monitor is connected with controller data, described in biogas stream 1
Pipeline on methane concentration detection device, carbon dioxide concentration detecting device and flow monitor are set, it is described in hydrogen stream 2
Pipeline on flow monitor is set, the controller is according to carbon dioxide concentration detecting device, methane concentration detection device
And two flow monitors calculate carbon dioxide molal quantity, moles hydrogen and the methane into bioreactor 6
Molal quantity, and according to molal quantity come adjust automatically biogas stream 1 and the size of the aperture of hydrogen stream 2.
If the molal quantity that controller detection enters bioreactor hydrogen is on the high side, controller automatically turns down hydrogen valve
Aperture, reduce hydrogen stream 2 flow；If the molal quantity of the hydrogen of detection is on the low side, increase the aperture of hydrogen valve, increase
The flow of hydrogen stream 2.
Or if controller detection is on the high side into the molal quantity of bioreactor hydrogen, then controller increases methane automatically
The aperture of valve, the flow of increase biogas stream 1；If the molal quantity of the hydrogen of detection is on the low side, opening for methane air valve is reduced
Degree, the flow of reduction biogas stream 1.
Molal quantity for controlling hydrogen, above-mentioned two ways can be combined together control hydrogen and carbon dioxide
Quantity, so as to reach the balance of the quantity of hydrogen and carbon dioxide as early as possible.
If the molal quantity that controller detection enters the carbon dioxide of bioreactor is excessive, corresponding automatic increase hydrogen
The content of gas, then increase the aperture of hydrogen valve, increases the flow of hydrogen stream 2, on the contrary, then controller automatically turns down hydrogen valve
Aperture, reduce hydrogen stream 2 flow.
Certainly, as one preferably, if detection enters the molal quantity of the carbon dioxide of bioreactor excessively, accordingly
Automatic reduction methane air valve aperture, on the contrary, then controller increases the aperture amount of methane valve automatically.
Molal quantity for controlling carbon dioxide, above-mentioned two ways can be combined together control hydrogen and titanium dioxide
The quantity of carbon, so as to reach the balance of the quantity of hydrogen and carbon dioxide as early as possible.
If the molal quantity that controller measurement enters the methane of bioreactor is excessive, controller downgrades low level bog gas automatically
The aperture of valve, on the contrary, controller adjusts the aperture of increase biogas valve automatically.
Certainly, above-mentioned all control can also be using manual mode control.
Preferably, also including Hydrogen Line, methane conduit and its carbon dioxide conduit being connected with bioreactor, use
In inputting hydrogen, methane and carbon dioxide into bioreactor, while valve and speed detector are set on each pipeline,
The valve and speed detector carry out data with controller and coupled.Controller according to enter bioreactor in hydrogen,
The molal quantity of methane and carbon dioxide, automatically controls Hydrogen Line, methane conduit and its carbon dioxide conduit valve, so as to life
Corresponding gas is inputted in thing reactor, the gas content in bioreactor is reached optimal ratio.
Preferably, density of hydrogen detection means, methane concentration detection device, dioxy can be set in bioreactor
Change concentration of carbon detection means, hydrogen, methane, the molal quantity of carbon dioxide in bioreactor are detected respectively, and according to detection
As a result carry out adjust automatically each valve as previously described, the gas content in bioreactor is reached optimal ratio.
Preferably, in anaerobic fermentation tank, reaction temperature is between 35-60 degrees Celsius.Preferably two kinds 35-40 are Celsius
Spend or 50-60 degrees Celsius.Reaction pressure is less than 2bar, preferably 1-1.8bar, further preferably, 1.1-1.5bar.Reaction
Raw material includes organic matter, cupboard rubbish of for example eating, sludge, excrement of animals, the organic matter such as stalk.Raw material adds water after crushing injects fermentation
Organic matter is decomposed and produces biogas by tank, anaerobic bacteria.Detailed process is as follows：
First stage is the hydrolysed ferment stage, refers to that the organic matter of complexity is hydrolyzed in the presence of extracellular microbial exoenzyme
And fermentation, macromolecular substances are broken into chain formation small-molecule substance.For example：The small molecule goods and materials such as monose, amino acid, are the latter half
Prepare.
Second stage is production hydrogen, production acetic acid stage, and the stage is such as glue acetic acid bacteria, part fusiform gemma in acid-producing bacteria
The small-molecule substance produced on last stage, generation acetic acid and hydrogen are decomposed in the presence of bacillus etc..In second stage, CO2+CH4.CO2
+4H2->CH4+4H2O。
Second stage rate of producing acid quickly, causes material liquid pH value to decline rapidly, feed liquid is had decomposed odour.
Biomass gasification reaction is carried out in biomass reacting furnace, biomass gasification reaction is in certain thermodynamic condition
Under, by means of the effect of air part (or oxygen), vapor, the high polymer of biomass is occurred pyrolysis, also oxidation, original weight
Whole reaction, is eventually converted into carbon monoxide, hydrogen.Biomass gasification reaction is the existing common technology in this area.
In bioreactor, carbon dioxide, profit are reduced with hydrogen to methane by methane backeria.
Bioreactor as preferred closed container, can pressure-bearing be not higher than 2 atmospheric pressure.
The methane backeria of bioreactor and other anaerobic bacterias are generally from the transplanting of other fermentation tanks.
Preferably, the reaction temperature in bioreactor is 13-60 degrees Celsius, reaction pressure is 1-2 atmospheric pressure.
Further preferably, reaction temperature is 40-50 degrees Celsius, and reaction pressure is 1.1-1.5 atmospheric pressure.
Preferably, in bioreactor, a part of methane backeria is first inputted, as seed, in the process of synthesizing methane
In, the methane in anaerobic fermentation tank is reacted with seed methane backeria, methane backeria is further generated, while bioreactor
In the part of methane of generation can also be reacted with seed methane backeria, further generate methane backeria.
In process of production, for the generation situation of methane gas, methane backeria constantly can also be transplanted from outside.
Preferably, the bioreactor sets methane backeria to transplant passage, to transplant methane backeria from outside.As excellent
Choosing, can transplant methane backeria according to the output situation of methane.If it find that the efficiency of methane output is less than certain numerical value, then beat
Valve opening door, methane backeria is transplanted into bioreactor.
The output efficiency of methane can judge according to the carbon dioxide of input, the quantity of hydrogen, using actual generation
The ratio of methane and the methane produced in theory, the methane produced in theory using input carbon dioxide and hydrogen quantity come
Calculate.
Preferably, the condensation temperature of condenser 9 is 25 degrees Celsius.Mainly water vapor condensation is excluded.
The specific embodiment of reaction is referring to chart 1.
Table 1
Table 2：One preferred embodiment reaction condition and result
Preferably, the hydrogen content in air-flow 2 is more than 95%, 100% can be substantially reached.
During the methane produced in bioreactor 6 is condensed within the condenser, air-flow non-azeotrope multicomponent in liquefaction is mixed
The thermal resistance mechanism of medium condensation has significant difference with pure component material condensation, and it is pure that theory analysis and experiment are proved coefficient of heat transfer ratio
The obvious reduction of component condensation.The existing research to non-azeotrope blending agent condensing heat-exchange is focusing more on containing a kind of on-condensible gas
Operating mode, reduces average thickness of liquid film using measures such as low groove, Artificial roughness surfaces and is proved effect when pure component is condensed
Prominent measure, effect is not sometimes obvious in the case of containing on-condensible gas, and the condensing heat-exchange process of the air-flow in synthesizing methane
Increasingly complex with mechanism, condensation process generally comprises two or more on-condensible gases, and heat exchange situation is more complicated.
In view of the above-mentioned problems, the invention provides a kind of new plate-fin heat exchanger, so as to solve in methane building-up process
The condensation of the different multicomponent blending agent of boiling point.
If without specified otherwise, being related to formula, "/" represents division, and "×", " * " represent multiplication.
As shown in Fig. 2 a kind of plate-fin heat exchanger condensed for non-azeotrope multicomponent mixture, the plate fin heat-exchanging
Device includes plate 12 parallel to each other, forms fluid passage 11 between the adjacent plate 12, the adjacent plate 12 it
Between set fin 16.The fin 16 include with the inclined sloping portion of plate 12 13, the sloping portion is parallel to each other.Inclining
Projection 15 is processed by impact style in inclined portion point 13, so that the fluid of the both sides of sloping portion 13 on sloping portion 13 by leading to
Cross the hole connection of impact style formation；The projection 15 stretches out from sloping portion 13.
Because sloping portion 13 is parallel to each other, therefore constitutes parallel four between adjacent sloping portion 13 and plate up and down
Side shape passage.
By setting projection 15, have the following advantages：
1) laminar sublayer on the one hand can be destroyed, on the other hand compared with " punching " fin, not because of punching loss heat-transfer surface
Product, and " thorn " and " hole " can disturb fluid on different height respectively, strengthen different thermal resistance links.
2) aperture that punching press " aculea " is formed, by the influence of " aculea " downstream pressure, can be achieved fin media of both sides
Pressure and mass exchange, the stability to viscous sublayer and liquid film damages, enhanced heat exchange.
3) fluid of non-azeotrope multicomponent mixture is directed to, can be realized by " aculea " and expand gas-liquid interface and gas phase
The contact area of boundary layer and cooling wall simultaneously strengthens disturbance.
4) easy processing realizes that manufacture difficulty and cost will not substantially rise.
Above-mentioned measure is taken in plate-fin heat exchanger, the letter of non-azeotrope blending agent condensing heat-exchange can greatly be improved
Easy and effective technology.Compared with taking " punching " fin, it is possible to increase 20-13% heat exchange efficiency.
Preferably, the angle that the flow direction of described projection 15 and mixture is formed is acute angle.
Preferably, as shown in figure 3, described fin 16 is apsacline fin, the fin 16 includes horizontal component 14
With sloping portion 13, the horizontal component 14 is parallel with plate 12 and is sticked together with plate 12, the sloping portion 13 with
Horizontal component 14 is connected.
As shown in fig. 7, the bearing of trend of the projection 15 and the angle of flow direction of mixture are a, as shown in figure 4,
Along the flow direction of mixture, same sloping portion 13 sets multiple projections 15, described along the flow direction of mixture
Angle a it is increasing.
It is found through experiments that, by becoming larger for angle a, compared with angle a is identical, it is possible to achieve higher changes
The thermal efficiency, can about improve 10% or so heat exchange efficiency.
Preferably, along the flow direction of mixture, the amplitude that angle a becomes big is less and less.It is found through experiments that, becomes
Change the big amplitude of angle a change, it is ensured that in the case of heat exchange efficiency, further reduce flow resistance, can about reduce
5% or so flow resistance.
Preferably, the projection 15 is isosceles triangle, the base of the isosceles triangle is arranged on sloping portion 13
On, preferably, base is identical with the angle of inclination of sloping portion, the drift angle of the isosceles triangle is b, along mixture
Flow direction, same sloping portion 13 sets multiple projections 15, along the flow direction of mixture, and on base, length is kept not
In the case of change, described projection drift angle b is less and less.It is found through experiments that, by tapering into for projection drift angle b, with top
Angle b is identical to be compared, it is possible to achieve higher heat exchange efficiency, can about improve 8% or so heat exchange efficiency.
Preferably, along the flow direction of mixture, the amplitude that drift angle b diminishes is less and less.It is found through experiments that, pushes up
The amplitude that angle b diminishes is less and less, it is ensured that in the case of heat exchange efficiency, further reduces flow resistance, can about drop
Low 4% or so flow resistance.
Preferably, along the flow direction of fluid, same sloping portion sets multiple rows of projection 15, as shown in Figures 4 and 5,
Often the distance between row's projection is S2, and along the flow direction of mixture, described S2 is increasing.Why it is arranged such,
Main purpose is big by S2 change, realizes in the case where ensureing heat exchange efficiency, further reduces flow resistance.Pass through experiment
It was found that, flow resistance reduction by 10% or so.
The S2 is using the base of the projection of adjacent row as calculating distance.
Preferably, as shown in figure 5, multiple rows of projection 15 is shifted structure.
Find in an experiment, the distance of adjacent plate 12 can not be excessive, crossing conference causes the reduction of heat exchange efficiency, too small meeting
Cause flow resistance excessive, similarly, for the base length of isosceles triangle, drift angle, projection, the distance of fin sloping portion with
The angle of fluid flow direction all can not be excessive or too small, excessive or too small can all cause the reduction or flowing of heat exchange efficiency
The change of resistance is big, therefore distance in adjacent plate 12, the base length of isosceles triangle, drift angle, projection, fin sloping portion
The size relationship of an optimization is met between the angle of fluid flow direction.
Therefore, the present invention is the thousands of numerical simulations and test data by multiple various sizes of heat exchangers,
Meet in the case of industrial requirements pressure-bearing (below 10MPa), in the case where realizing maximum heat exchange amount, the optimal heat exchange summed up
The dimensionally-optimised relation of plate.
The distance of adjacent plate is H, and the length on isosceles triangle base is h, and the distance of adjacent sloping portion is w,
The angle of acute angle between sloping portion and plate is c, meets equation below：
7*h/H=c1*Ln (L*sin (a)/(w*sin (c))+c2,
Sin (b/2)=c3+c4*sin (a)-c5* (sin (a))2,
Wherein Ln is logarithmic function, and c1, c2, c3, c4, c5 are coefficients,
0.24<c1<0.25,0.68<c2<0.70,0.87<c3<0.88,0.68<c4<0.70,1.14<c5<1.15；
19°<a<71 °, 55 °<b<165°,90°<c<70°；
10mm<w<15mm, 6mm<H<14mm；
0.19<L*sin(a)/w<0.41,0.12<7*h/H<0.47；
H is that, with the distance between relative face of adjacent plate, W is along plate with the relative face of adjacent sloping portion
Distance on direction, L for isosceles triangle summit to base midpoint distance.
Preferably, c1=0.245, c2=0.694,
C3=0.873, c4=0.691, c5=1.1454.
Preferably, 85 °<c<80°.
By the optimal geometric scale of " projection " that goes out of above-mentioned formula, heat exchange efficiency can be improved, while can be real
The reinforcing of gas phase boundary different scale internal thermal resistance is now included only to viscous sublayer or comprising liquid film and extremely, it is to avoid measure
Degree, causes unnecessary drag losses.
Preferably, the base of the adjacent projection of described same row is all on one wire, the adjacent projection of same row
Distance is S1, the 4 × h<S1<6 × h, wherein S1 are with the distance at the midpoint on the base of two neighboring isosceles triangle projection.
Preferably, the base of the isosceles triangle of the projection of adjacent row is parallel to each other, the summit of isosceles triangle is on earth
The distance at side midpoint be L, adjacent row apart from S2 be 4*L<S2<7*L.Preferably S2=5*L
When the base of the isosceles triangle of adjacent row is different, the weighted average on two bases are taken to calculate.
Preferably, the angle of the isosceles triangle of same row is identical with base.I.e. shape is identical, is equal
Shape.
For formula above, for the different projection of front and rear row size, also still it is applicable.
For the specific dimensional parameters do not mentioned, it is designed according to normal heat exchanger.
Another preferred embodiment of methane is prepared as the present invention, as shown in Figure 8.With Fig. 1 one embodiment
Compare, difference is to eliminate bioreactor 6, and biological respinse is directly carried out in anaerobic fermentation tank 4.The methane of generation passes through
Condenser 9 is condensed.
Preferably, 4 points of anaerobic fermentation tank is two parts, Part I produce the reaction of biogas, and Part II is
Produce the reaction of methane, the part that biogas stream and hydrogen stream 2 are mixed.
In anaerobic fermentation tank, a part of methane backeria is first inputted, as seed, during synthesizing methane, from detesting
The methane produced in aerobe fermentation tank is reacted with seed methane backeria, further generates methane backeria.
Preferably, in process of production, for the generation situation of methane gas, first constantly can also be transplanted from outside
Alkane bacterium.
Preferably, the anaerobic fermentation tank sets methane backeria to transplant passage, to transplant methane backeria from outside.As excellent
Choosing, can transplant methane backeria according to the output situation of methane.If it find that methane output is less than regime values, then valve is opened
Door, methane backeria is transplanted into anaerobic fermentation tank.
Preferably, density of hydrogen detection means, methane concentration are set in Part II that can be in anaerobic fermentation tank
Detection means, carbon dioxide concentration detecting device, detect hydrogen, methane, the molal quantity of carbon dioxide in anaerobic fermentation tank respectively,
And adjust automatically adjustment triple valve is come according to the result of detection as previously described, the gas content in anaerobic fermentation tank is reached most
Good ratio.
Preferably, valve is set on the passage of hydrogen stream 2, the hydrogen entered by Valve controlling in anaerobic fermentation tank
The flow of stream 2.
If the content of hydrogen is relatively low in the bioreactor of measurement, controller increases the aperture of valve automatically, if
Measurement hydrogen content is higher, then controller reduces the aperture of valve automatically.It is of course also possible to use manual mode is controlled.
There is no other situations introduced identical with Fig. 1 embodiment in Fig. 8 embodiments, just do not introducing specifically.
Although the present invention is disclosed as above with preferred embodiment, the present invention is not limited to this.Any art technology
Personnel, without departing from the spirit and scope of the present invention, can make various changes or modifications, therefore protection scope of the present invention should
It is defined when by claim limited range.
Claims (10)
1. a kind of plate-fin heat exchanger, the plate-fin heat exchanger includes setting wing between plate parallel to each other, the plate
Piece, the fin includes the sloping portion for favouring plate, projection is processed by impact style on sloping portion, so that inclining
The fluid of inclined portion point both sides is connected by the hole of impact style formation on sloping portion；The projection is from sloping portion along mixing
Gas flow direction stretches out.
2. a kind of preparation facilities of wind-powered electricity generation methane, including anaerobic fermentation tank, bioreactor, wind power generation plant and electrolysis water dress
Put, the wind power generation plant is connected with electrolytic water device, and electrolytic water device is connected with bioreactor, electrolytic water device will be produced
Raw hydrogen is input in bioreactor, and the anaerobic fermentation tank is connected with bioreactor, and the anaerobic fermentation tank is produced
Biogas enter bioreactor, contain methane and carbon dioxide into the biogas of bioreactor；Characterized in that,
Also include Hydrogen Line, methane conduit and the carbon dioxide conduit being connected with bioreactor, for defeated into bioreactor
Enter hydrogen, methane and carbon dioxide, while setting valve and speed detector, the valve and velocity measuring on each pipeline
Device carries out data with controller and coupled；Controller rubs according to the hydrogen, methane and carbon dioxide entered in bioreactor
That number, automatically controls Hydrogen Line, methane conduit and carbon dioxide conduit valve, corresponding to be inputted into bioreactor
Gas, makes the gas content in bioreactor reach optimal ratio.
3. preparation facilities as claimed in claim 2, it is characterised in that set density of hydrogen to detect dress in bioreactor
Put, methane concentration detection device, carbon dioxide concentration detecting device, described controller detects hydrogen in bioreactor respectively
Gas, methane, the molal quantity of carbon dioxide, each valve is adjusted according to the result of detection, contains the gas in bioreactor
Amount reaches optimal ratio.
4. preparation facilities as claimed in claim 3, it is characterised in that if controller detection enters the hydrogen of bioreactor
It is more than 1.43 with the volume ratio of methane, the synthesis of carbon dioxide:1, then controller automatically turn down the aperture of hydrogen valve；If
Detect hydrogen and the volume ratio of methane, the synthesis of carbon dioxide is less than 1.43:1, then increase the aperture of hydrogen valve.
5. preparation facilities as claimed in claim 3, it is characterised in that if controller detection enter bioreactor hydrogen with
Methane, the volume ratio of the synthesis of carbon dioxide are more than 1.43:1, then controller increase the aperture of methane valve automatically；If inspection
The hydrogen of survey and the volume ratio of methane, the synthesis of carbon dioxide are less than 1.43:1, then reduce the aperture of methane air valve.
6. preparation facilities as claimed in claim 3, it is characterised in that if controller detection enters the methane of bioreactor
Mol concentration be less than 98% when, further detection carbon dioxide molal quantity, if carbon dioxide is more relative to hydrogen, be increased by
The aperture of hydrogen valve；If hydrogen is more relative to carbon dioxide, controller turns down the aperture of hydrogen valve.
7. preparation facilities as claimed in claim 2, it is characterised in that biogas is set between anaerobic fermentation tank and bioreactor
Cleaning apparatus.
8. preparation facilities as claimed in claim 2, it is characterised in that the bioreactor is connected with condenser, described cold
Condenser is the folder of plate-fin heat exchanger as claimed in claim 1, the bearing of trend of the projection and the flow direction of mixture
Angle is a, and same sloping portion sets multiple projections, and along the flow direction of mixture, described angle a is less and less.
9. a kind of methane preparation technology using the preparation facilities as described in claim 2-8, it is characterised in that in bioreactor
The catalyst used is hydrogen auxotype methanogen.
10. preparation technology as claimed in claim 9, it is characterised in that enter the biogas of bioreactor, moles the hundred of methane
Divide content more than 45%, the molar content of carbon dioxide is more than 30%.
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| CN110295073A (en) * | 2019-07-09 | 2019-10-01 | 哈尔滨工业大学 | Methane purification membrane bioreactor and its application method |
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|---|---|---|---|---|
| CN105387739A (en) * | 2015-12-03 | 2016-03-09 | 山东大学 | Plate-fin heat exchanger and methane preparation process by utilization of wind electricity |
| CN205152232U (en) * | 2015-12-03 | 2016-04-13 | 山东大学 | Utilize preparation facilities of power generation facility's living beings methane |
| CN106017158A (en) * | 2015-12-03 | 2016-10-12 | 山东大学 | Plate-fin heat exchanger and preparation process of methane reacting in anaerobic fermentation tank |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105387739A (en) * | 2015-12-03 | 2016-03-09 | 山东大学 | Plate-fin heat exchanger and methane preparation process by utilization of wind electricity |
| CN205152232U (en) * | 2015-12-03 | 2016-04-13 | 山东大学 | Utilize preparation facilities of power generation facility's living beings methane |
| CN106017158A (en) * | 2015-12-03 | 2016-10-12 | 山东大学 | Plate-fin heat exchanger and preparation process of methane reacting in anaerobic fermentation tank |
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| CN110295073A (en) * | 2019-07-09 | 2019-10-01 | 哈尔滨工业大学 | Methane purification membrane bioreactor and its application method |
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