CN107201308A - The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control - Google Patents
The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control Download PDFInfo
- Publication number
- CN107201308A CN107201308A CN201710494537.1A CN201710494537A CN107201308A CN 107201308 A CN107201308 A CN 107201308A CN 201710494537 A CN201710494537 A CN 201710494537A CN 107201308 A CN107201308 A CN 107201308A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- bioreactor
- methane
- biogas
- carbon dioxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
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
- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—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
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
- C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
- C12P5/023—Methane
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
- 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
- Y02P20/59—Biological synthesis; Biological purification
Abstract
The invention provides a kind of methane preparation facilities of utilization wind-powered electricity generation intelligent control and its technique, including anaerobic fermentation tank, bioreactor, wind power generation plant and electrolytic water device, biogas valve is set on the first pipeline between anaerobic fermentation tank and bioreactor, hydrogen valve is set on the second pipeline that electrolytic water device is connected with bioreactor, and carbon dioxide concentration detecting device, density of hydrogen detection means, methane concentration detection device and controller carry out data cube computation；The flow monitor is connected with controller data；The controller calculates carbon dioxide molal quantity, moles hydrogen and the methane molal quantity into bioreactor according to carbon dioxide concentration detecting device, methane concentration detection device and two flow monitors, and according to molal quantity come adjust automatically biogas and the size of hydrogen gas stream.The present invention is capable of the flow of intelligent control methane and hydrogen, so that the preparation of methane reaches optimal yield.
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 proposes 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 preparation of the biomethane of intelligent control
Device, including anaerobic fermentation tank, bioreactor, wind power generation plant and electrolytic water device, the wind power generation plant and electricity
Water installations connection is solved, electrolytic water device is connected with bioreactor, the hydrogen of generation is input in bioreactor, described to detest
Aerobe fermentation tank is connected with bioreactor, and the biogas that the anaerobic fermentation tank is produced enters bioreactor, into biological respinse
Contain methane and carbon dioxide in the biogas of device；Characterized in that, between anaerobic fermentation tank and bioreactor
Set on one pipeline and hydrogen valve is set on biogas valve, the second pipeline that electrolytic water device is connected with bioreactor；
Set on methane concentration detection device, carbon dioxide concentration detecting device and flow monitor, the second pipeline and set on one pipeline
Put flow monitor, carbon dioxide concentration detecting device, density of hydrogen detection means, methane concentration detection device and controller
Carry out data cube computation；The flow monitor is connected with controller data；The controller is detected according to gas concentration lwevel
Device, methane concentration detection device and two flow monitors calculate the carbon dioxide mole into bioreactor
Number, moles hydrogen and methane molal quantity, and according to molal quantity come adjust automatically biogas and the size of hydrogen gas stream.
Preferably, if the molal quantity that detection enters bioreactor hydrogen is on the high side, controller automatically turns down hydrogen
The aperture of valve, reduces the flow of hydrogen；If the molal quantity of the hydrogen of detection is on the low side, increase the aperture of hydrogen valve, increase
The flow of hydrogenation.
Preferably, if the molal quantity that detection enters bioreactor hydrogen is on the high side, controller increases biogas automatically
The aperture of valve；If the molal quantity of the hydrogen of detection is on the low side, the aperture of biogas air valve is reduced.
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, it is characterised in that on sloping portion
Projection is processed by impact style, so that Kong Lian of the fluid of sloping portion both sides by impact style formation on sloping portion
It is logical；The projection stretches 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.
Preferably, the catalyst used in bioreactor is hydrogen auxotype methanogen.
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 is capable of the flow of intelligent control methane and hydrogen, so that the preparation of methane reaches optimal production
Amount, 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) a kind of heat exchanger for the condensation purification for adapting to gas is developed, the efficiency of condensation can be improved.
4) present invention realizes the production of methane by biological method by setting bioreactor, and increasing is improved
The production efficiency of methane.
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
The Figure of description for constituting the part of the application is used for providing further understanding of the present application, and the application's shows
Meaning property embodiment and its illustrate be used for explain the application, do not constitute the improper restriction to the application.
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
It is noted that described further below is all exemplary, it is intended to provide further instruction to the application.Unless another
Indicate, all technologies and scientific terminology that this present invention is used have and the application person of an ordinary skill in the technical field
The identical meanings being generally understood that；It is molar content in the case of gas content in the present invention, no specified otherwise.
It should be noted that term used herein above is merely to describe embodiment, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singulative
It is also intended to include plural form, additionally, it should be understood that, when in this manual using term "comprising" and/or " bag
Include " when, it indicates existing characteristics, step, operation, device, component and/or combinations thereof.
As described by background section, during methane production, generally require cold by heat exchanger progress
Solidifying, current heat exchanger is all to use general common heat exchanger, can not the condensation of suitable gas well purify, therefore
Need to develop a kind of heat exchanger of new type, it is met the condensation of gas in biogas production process purification.With reference to attached
Figure is described in detail to the embodiment of the present invention.
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, is conveyed into electrolytic water device 7
Electricity, the hydrogen stream 2 that the electrolysis of electrolytic water device 7 is produced enters in bioreactor 6, in bioreactor 6, carries out synthesizing methane
Reaction：CO2+4H2-CH4+2H2O；
The catalyst used in bioreactor 13 is hydrogen auxotype methanogen.
Preferably, biogas is before bioreactor 6 is entered, also purified by biogas cleaning apparatus 9, 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, 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 air-flow 1
Methane concentration detection device, carbon dioxide concentration detecting device and flow monitor, the pipe in air-flow 2 are set on pipeline
Flow monitor is set on road, the controller 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 mole into bioreactor
Number, and according to molal quantity come adjust automatically air-flow 1 and the size of the aperture of air-flow 2.
If the molal quantity that detection enters bioreactor hydrogen is on the high side, controller automatically turns down opening for hydrogen valve
Degree, reduces the flow of air-flow 2；If the molal quantity of the hydrogen of detection is on the low side, increase the aperture of hydrogen valve, increase air-flow 2
Flow.
Or if detection is on the high side into the molal quantity of bioreactor hydrogen, then controller increases methane valve automatically
Aperture, increases the flow of air-flow 1；If the molal quantity of the hydrogen of detection is on the low side, the aperture of methane air valve is reduced, gas is reduced
The flow of 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.
It is corresponding to increase containing for hydrogen automatically if detecting that the molal quantity for the carbon dioxide for entering bioreactor is excessive
Amount, then increase the aperture of hydrogen valve, increases the flow of air-flow 2, on the contrary, then controller automatically turns down the aperture of hydrogen valve,
Reduce the flow of air-flow 2.
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 measurement enters the methane of bioreactor is excessive, controller downgrades low level bog air valve automatically
Aperture, 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 and air-flow 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 air-flow 2, the air-flow 2 entered by Valve controlling in anaerobic fermentation tank
Flow.
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 (9)
1. a kind of methane preparation facilities of utilization wind-powered electricity generation intelligent control, including anaerobic fermentation tank, bioreactor, wind-power electricity generation dress
Put and electrolytic water device, the wind power generation plant is connected with electrolytic water device, and electrolytic water device is connected with bioreactor, will
The hydrogen of generation is input in bioreactor, and the anaerobic fermentation tank is connected with bioreactor, the anaerobic fermentation tank production
Raw biogas enters bioreactor, contains methane and carbon dioxide into the biogas of bioreactor；Its feature exists
In setting biogas valve, electrolytic water device and biological respinse on the first pipeline between anaerobic fermentation tank and bioreactor
Hydrogen valve is set on second pipeline of device connection；Methane concentration detection device, gas concentration lwevel are set on the first pipeline
Flow monitor is set on detection means and flow monitor, the second pipeline, and carbon dioxide concentration detecting device, hydrogen are dense
Spend detection means, methane concentration detection device and controller and carry out data cube computation；The flow monitor and controller data
Connection；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 molal quantity into bioreactor, and according to molal quantity come
The size of adjust automatically biogas and hydrogen gas stream.
2. preparation facilities as claimed in claim 1, it is characterised in that if detection enters the molal quantity of bioreactor hydrogen
On the high side, then controller automatically turns down the aperture of hydrogen valve, reduces the flow of hydrogen；If the molal quantity of the hydrogen of detection is inclined
It is few, then increase the aperture of hydrogen valve, increase the flow of hydrogen.
3. preparation facilities as claimed in claim 1, it is characterised in that if detection enters the molal quantity of bioreactor hydrogen
On the high side, then controller increases the aperture of biogas valve automatically；If the molal quantity of the hydrogen of detection is on the low side, biogas air valve is reduced
The aperture of door.
4. preparation facilities as claimed in claim 1, it is characterised in that biogas is set between anaerobic fermentation tank and bioreactor
Cleaning apparatus.
5. preparation facilities as claimed in claim 1, it is characterised in that the bioreactor is connected with condenser.
6. preparation facilities as claimed in claim 5, it is characterised in that the condenser is plate-fin heat exchanger, the plate-fin is changed
Hot device includes setting fin between plate parallel to each other, the plate, and the fin includes the sloping portion for favouring plate,
Characterized in that, projection is processed by impact style on sloping portion, so that the fluid of sloping portion both sides is by tilting
The hole connection of impact style formation on part；The projection stretches out from sloping portion along simulation model for mixing gases flows direction.
7. preparation facilities as claimed in claim 6, it is characterised in that the bearing of trend of the projection and the flowing side of mixture
To angle be a, same sloping portion sets multiple projections, and along the flow direction of mixture, described angle a is increasingly
It is small.
8. the methane preparation technology described in a kind of one of utilization claim 1-7 preparation facilities, it is characterised in that bioreactor
The middle catalyst used is hydrogen auxotype methanogen.
9. preparation technology as claimed in claim 8, 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%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710494537.1A CN107201308A (en) | 2017-06-26 | 2017-06-26 | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710494537.1A CN107201308A (en) | 2017-06-26 | 2017-06-26 | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107201308A true CN107201308A (en) | 2017-09-26 |
Family
ID=59907869
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710494537.1A Pending CN107201308A (en) | 2017-06-26 | 2017-06-26 | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107201308A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205133525U (en) * | 2015-12-03 | 2016-04-06 | 山东大学 | Preparation facilities of living beings methane |
| CN205152232U (en) * | 2015-12-03 | 2016-04-13 | 山东大学 | Utilize preparation facilities of power generation facility's living beings methane |
| CN205170836U (en) * | 2015-12-03 | 2016-04-20 | 山东大学 | Preparation facilities of living beings methane |
-
2017
- 2017-06-26 CN CN201710494537.1A patent/CN107201308A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205133525U (en) * | 2015-12-03 | 2016-04-06 | 山东大学 | Preparation facilities of living beings methane |
| CN205152232U (en) * | 2015-12-03 | 2016-04-13 | 山东大学 | Utilize preparation facilities of power generation facility's living beings methane |
| CN205170836U (en) * | 2015-12-03 | 2016-04-20 | 山东大学 | Preparation facilities of living beings methane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Su et al. | Assessment of a combined cooling, heating and power system by synthetic use of biogas and solar energy | |
| CN103476704A (en) | Method for producing methanol or hydrocarbons from a carbon material, including a reforming step, the operating conditions of which are selectively adjusted | |
| CN109179320A (en) | A kind of natural gas hydrogen production plant and method | |
| Coskun et al. | Energy analysis of hydrogen production using biogas-based electricity | |
| CN205152232U (en) | Utilize preparation facilities of power generation facility's living beings methane | |
| CN105300143B (en) | A kind of plate-fin heat exchanger and its methane preparation technology using solar energy | |
| Abuşoğlu et al. | Exergy analyses of green hydrogen production methods from biogas-based electricity and sewage sludge | |
| CN105387739B (en) | Methane preparation process by utilization of wind electricity | |
| CN107328274A (en) | A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique | |
| Asvad et al. | Multiscale kinetic modeling for biohydrogen production: a study on membrane bioreactors | |
| CN106017158B (en) | A kind of plate-fin heat exchanger and the methane preparation technology reacted in anaerobic fermentation tank | |
| US20210147787A1 (en) | Bioreactors with Integrated Catalytic Nitrogen Fixation | |
| CN105423781B (en) | Methane manufacturing technology | |
| CN107201308A (en) | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control | |
| CN205170836U (en) | Preparation facilities of living beings methane | |
| CN205133525U (en) | Preparation facilities of living beings methane | |
| Wolfrum et al. | Bioreactor design studies for a hydrogen-producing bacterium | |
| JP2022529136A (en) | Methods and systems for generating hydrogen | |
| CN208327391U (en) | A kind of carbon monodixe conversion system | |
| CN105645581B (en) | It is a kind of synchronously to realize organic waste treatment and the system and device and method of synthesis gas upgrading | |
| Wolfrum et al. | Bioreactor design studies for a novel hydrogen-producing bacterium | |
| McKellar et al. | The Production of Syngas Via High Temperature Electrolysis and Biomass Gasification | |
| Hawkes et al. | Liquid fuel production from biomass via high temperature steam electrolysis | |
| CN213834531U (en) | Novel methanol cracking hydrogen production device | |
| CN103060188A (en) | External circulation airlift type reactor with built-in plate-fin heat exchanger and temperature control method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |