CN205152232U - Utilize preparation facilities of power generation facility's living beings methane - Google Patents
Utilize preparation facilities of power generation facility's living beings methane Download PDFInfo
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- CN205152232U CN205152232U CN201521002731.6U CN201521002731U CN205152232U CN 205152232 U CN205152232 U CN 205152232U CN 201521002731 U CN201521002731 U CN 201521002731U CN 205152232 U CN205152232 U CN 205152232U
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- 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
Abstract
The utility model provides an utilize preparation facilities of power generation facility's living beings methane, including anaerobic fermentation tank, bioreactor, power generation facility and brineelectrolysis device, power generation facility is connected with the brineelectrolysis device, and the brineelectrolysis device is connected with bioreactor, anaerobic fermentation tank links to each other with bioreactor. The utility model discloses a power generation facility connects the brineelectrolysis device, through the hydrogen preparation methane that the electrolysis produced, has practiced thrift the energy.
Description
Technical field
The utility model belongs to field of energy utilization, particularly relates to the methane preparation system comprising interchanger, belongs to interchanger and Application Areas thereof.
Background technology
Along with the high speed development of modern social economy, the demand of the mankind to the energy is increasing.But the traditional energy margins such as coal, oil, Sweet natural gas constantly reduce, day by day in short supply, cause rising steadily of price, simultaneously the problem of environmental pollution that causes of conventional fossil fuel is also further serious, and these limit the development of society and the raising of human life quality all greatly.Biogas is low cost renewable energy source, but usually needs in reality to purify to biogas, produces methane, using the relevant technologies requirement of satisfied different purposes (such as: as automobile fuel).Tradition methane purification technology needs to consume mass energy, does not meet the requirement of current energy-saving and emission-reduction and protection of the environment.
In the process of methane production, generally need to carry out condensation through interchanger, current interchanger is all use general common interchanger, can not well suitable gas condensation purify, therefore need the interchanger developing a kind of new type, the condensation making it meet gas in biogas production process is purified.
In addition, for the production process of methane, how to improve the output capacity of methane, be also pursuing in methane production technique always, and utilize hydrogen purification biogas to be improve the effective ways producing biomethane efficiency, this method is reacted based on Sabatier: CO
2+ 4H
2-CH
4+ 2H
2o.Traditionally, this reaction generally uses ruthenium (Ru) base and nickel (Ni) catalyst based realization.But the technique or the equipment that do not have a sleeve forming at present realize hydrogen proposition methane.
Utility model content
The utility model aims to provide the interchanger that uses in a kind of hydrogen purification biogas and utilizes electric energy electrolysis to produce hydrogen purification biogas is improve the technique of producing biomethane efficiency, and this technology utilization biological method realizes Sabatier reaction.
To achieve these goals, the technical solution of the utility model is as follows:
A kind of preparation facilities utilizing the biomethane of power generation assembly, comprise anaerobic fermentation tank, bio-reactor, power generation assembly and electrolytic water device, described wind power generation plant is connected with electrolytic water device, electrolytic water device is connected with bio-reactor, and described anaerobic fermentation tank is connected with bio-reactor.
As preferably, biogas cleaning apparatus is set between anaerobic fermentation tank and bio-reactor.
As preferably, described bio-reactor is connected with condenser.
As preferably, described condenser is plate-fin heat exchanger, described plate-fin heat exchanger comprises plate parallel to each other, between described plate, fin is set, described fin comprises the sloping portion favouring plate, sloping portion processes projection by impact style, and the hole that the fluid of sloping portion both sides is formed by impact style on sloping portion is communicated with; Described projection stretches out from sloping portion along simulation model for mixing gases flows direction.
As preferably, the angle of the bearing of trend of described projection and the flow direction of mixture is a, and same sloping portion arranges multiple projection, and along the flow direction of mixture, described angle a is more and more less.
As preferably, the pipeline between anaerobic fermentation tank and bio-reactor is arranged biogas valve, the pipeline that electrolytic water device is connected with bio-reactor arranges hydrogen valve.
As preferably, also comprise the Hydrogen Line, methane conduit and the carbon dioxide conduit thereof that are connected with bio-reactor, each pipeline arranges valve and speed detector simultaneously.
As preferably, described power generation assembly is wind power generation plant or device of solar generating.
A kind of preparation technology of biomethane, comprise anaerobic fermentation tank, bio-reactor, wind power generation plant and electrolytic water device, described wind power generation plant is connected with electrolytic water device, so that to electrolytic water device conveying electricity, electrolytic water device is connected with bio-reactor, be input in bio-reactor by the hydrogen of generation, the biogas that described anaerobic fermentation tank produces enters bio-reactor, enters in the described biogas of bio-reactor containing methane and carbon dioxide; In bio-reactor, carry out the reaction of synthesizing methane.
As preferably, the catalyzer used in bio-reactor is hydrogen nutritional type methanogen.
As preferably, biogas, before entering bio-reactor, also purifies through biogas cleaning apparatus.
As preferably, enter the biogas of bio-reactor, the molar content more than 45% of methane, the molar content of carbonic acid gas is more than 30%.
As preferably, described bio-reactor is connected with condenser, for the methane after condensation synthesis.
As preferably, the pipeline between anaerobic fermentation tank and bio-reactor is arranged biogas valve, the pipeline that electrolytic water device is connected with bio-reactor arranges hydrogen valve, control to enter the quantity of biogas in bio-reactor and hydrogen by valve.
As preferably, also comprise the Hydrogen Line, methane conduit and the carbon dioxide conduit thereof that are connected with bio-reactor, for to inputting hydrogen, methane and carbon dioxide in bio-reactor, each pipeline arranges valve and speed detector, described valve and speed detector carry out data with controller and connect simultaneously.
As preferably, described condenser is described interchanger.
Compared with prior art, the utility model has following advantage:
1) the utility model utilizes wind-force or device of solar generating to connect electrolytic water device, and the hydrogen produced by electrolysis prepares methane, has saved the energy.
2) develop the interchanger that a kind of condensation adapting to gas is purified, the efficiency of condensation can be improved.
3) the utility model is by arranging bio-reactor, is realized the production of methane by biological method, the production efficiency that improve methane of increasing.
4) the utility model proposes a kind of processing method of production biomethane completely newly, anaerobically fermenting and biomass gasification process are combined, while reducing the power consumption of methane purification process, significantly increase methane production, thus improve the whole efficiency of anaerobically fermenting and gasifying biomass.
5) membrane separation apparatus of the present utility model adopts tubular fibre and Matrimid polymeric material to make, and is a kind of polymeric membrane as glass.By the effect of membrane separation apparatus, separation can reach molecular level.
Accompanying drawing explanation
Fig. 1 is the process flow sheet preparing biomethane of the present utility model;
Fig. 2 is a kind of plate-fin heat exchanger heat exchange plate of the utility model structural representation;
Fig. 3 is the structural representation of the utility model plate wing unit;
Fig. 4 is the schematic diagram that the utility model arranges raised structures sloping portion plane;
Fig. 5 is another schematic diagram that the utility model arranges raised structures sloping portion plane;
Fig. 6 is denation structural representation of the present utility model;
Fig. 7 is the tangent plane structural representation in the utility model denation runner.
Fig. 8 is another embodiment process flow sheet preparing biomethane of the present utility model.
Reference numeral is as follows:
1 biogas stream, 2 hydrogen streams, 3 methane stream, 4 anaerobic fermentation tanks, 5 biogas cleaning apparatus, 6 bio-reactors, 7 electrolytic water devices, 8 wind power generation plants, 9 condensers, 10 sealing members, 11 fluid channels, 12 plates, 13 sloping portions, 14 horizontal components, 15 projections, 16 fins.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in detail.It should be noted that, gas content herein, is molar content when specified otherwise.
Fig. 1 illustrates a kind of technical process preparing biomethane, as shown in Figure 1, described preparation technology comprises anaerobic fermentation tank 4, bio-reactor 6, electrolytic water device 7 and wind power generation plant 8, the biogas that described anaerobic fermentation tank 4 produces enters in bio-reactor 6, enter in the biogas of bio-reactor 6 containing methane and carbon dioxide, as preferably, what content was maximum is methane and carbon dioxide successively; Wind power generation plant 8 is connected with electrolytic water device 7, and conveying electricity in electrolytic water device 7, the hydrogen stream 2 that electrolytic water device 7 electrolysis produces enters in bio-reactor 6, in bio-reactor 6, carries out the reaction of synthesizing methane: CO
2+ 4H
2-CH
4+ 2H
2o; The catalyzer used in bio-reactor 6 is hydrogen nutritional type methanogen.
As preferably, biogas, before entering bio-reactor 6, also purifies through biogas cleaning apparatus 9, to remove impurity, and such as hydrogen sulfide, ammonia, oxosilane etc.
As preferably, enter the biogas of bio-reactor, the molar content more than 45% of methane, the molar content of carbonic acid gas is more than 13% %.
As preferably, from bio-reactor 6, methane out reclaims after condenser 9.
As preferably, in bio-reactor, the ratio of carbonic acid gas and hydrogen is: 1 to 4 (mole number ratio).
The pipeline of biogas stream 1 is arranged biogas valve, the pipeline of hydrogen stream 2 is arranged hydrogen valve, control to enter the quantity of biogas in bio-reactor and hydrogen by valve.
Described system also comprises carbon dioxide concentration detecting device, density of hydrogen proofing unit, methane concentration detection device, and described carbon dioxide concentration detecting device, density of hydrogen proofing unit, methane concentration detection device and controller carry out data cube computation, described system also comprises flow monitor, described flow monitor is connected with controller data, described methane concentration detection device is set on the pipeline of air-flow 1, carbon dioxide concentration detecting device and flow monitor, described flow monitor is set on the pipeline of air-flow 2, described controller is according to carbon dioxide concentration detecting device, methane concentration detection device and two flow velocity Soviet Union proofing units calculate the carbonic acid gas mole number entering bio-reactor, moles hydrogen and methane mole number, and automatically adjust the size of T-valve to air-flow 1 and air-flow 2 aperture according to mole number.
If it is on the high side to detect the mole number entering bio-reactor hydrogen, then the aperture of hydrogen valve turned down automatically by controller, reduces the flow of air-flow 2; If the mole number of the hydrogen detected is on the low side, then increase the aperture of hydrogen valve, increase the flow of air-flow 2.
If or it is on the high side to detect the mole number entering bio-reactor hydrogen, then controller increases the aperture of methane valve automatically, increase the flow of air-flow 1; If the mole number of the hydrogen detected is on the low side, then reduce the aperture of methane gas valve, reduce the flow of air-flow 1.
For the mole number controlling hydrogen, two kinds of above-mentioned modes can combine and control the quantity of hydrogen and carbonic acid gas, thus reach the balance of the quantity of hydrogen and carbonic acid gas as early as possible.
If it is too much to detect the mole number entering the carbonic acid gas of bio-reactor, then the corresponding content automatically increasing hydrogen, then increase the aperture of hydrogen valve, increase the flow of air-flow 2, on the contrary, then the aperture of hydrogen valve turned down automatically by controller, reduces the flow of air-flow 2.
Certainly, as one preferably, if it is too much to detect the mole number entering the carbonic acid gas of bio-reactor, then the corresponding aperture automatically reducing methane gas valve, on the contrary, then controller increases the aperture amount of methane valve automatically.
For the mole number controlling carbonic acid gas, two kinds of above-mentioned modes can combine and control the quantity of hydrogen and carbonic acid gas, thus reach the balance of the quantity of hydrogen and carbonic acid gas as early as possible.
If it is too much to measure the mole number entering the methane of bio-reactor, then controller downgrades the aperture of low level bog air valve automatically, and on the contrary, the aperture increasing biogas valve adjusted automatically by controller.
Certainly, above-mentioned all control also can adopt manual mode to control.
As preferably, also comprise the Hydrogen Line, methane conduit and the carbon dioxide conduit thereof that are connected with bio-reactor, for to inputting hydrogen, methane and carbon dioxide in bio-reactor, each pipeline arranges valve and speed detector, described valve and speed detector carry out data with controller and connect simultaneously.Controller is according to the mole number of the hydrogen entered in bio-reactor, methane and carbon dioxide, automatic control Hydrogen Line, methane conduit and carbon dioxide conduit valve thereof, to input corresponding gas in bio-reactor, make the ratio that the gas content in bio-reactor reaches best.
As preferably, can density of hydrogen proofing unit, methane concentration detection device, carbon dioxide concentration detecting device be set in bio-reactor, detect the mole number of hydrogen, methane, carbonic acid gas in bio-reactor respectively, and come as previously described automatically to adjust each valve according to the result detected, make the ratio that the gas content in bio-reactor reaches best.
As preferably, in anaerobic fermentation tank, temperature of reaction is between 35-60 degree Celsius.Be preferably two kinds 35-40 degree Celsius or 50-60 degree Celsius.Reaction pressure lower than 2bar, preferred 1-1.8bar, further preferably, 1.1-1.5bar.The raw material of reaction comprises organism, cupboard rubbish of such as eating, mud, excrement of animals, the organism such as stalk.Add water after raw material pulverizing injection fermentor tank, and organic substance decomposing is produced biogas by anerobe.Detailed process is as follows:
First stage is the hydrolysed ferment stage, refers to that complicated organism is hydrolyzed and ferments under the effect of extracellular microbial exoenzyme, macromolecular substance is broken chain formation small-molecule substance.Such as: the small molecules such as monose, amino acid goods and materials, for the latter half prepares.
Subordinate phase is for producing hydrogen, producing the acetic acid stage, and this stage is at acid-producing bacteria, the small-molecule substance that such as, under the effect of glue acetic bacteria, part clostridium etc. decomposition produces on last stage, generates acetic acid and hydrogen.In subordinate phase, CO
2+ CH
4.CO
2+ 4H
2->CH
4+ 4H
2o.
Subordinate phase rate of producing acid is very fast, causes material liquid pH value to decline rapidly, makes feed liquid have decomposed odour.
Biomass gasification reaction is carried out in biomass Reaktionsofen, biomass gasification reaction is under certain thermodynamic condition, by means of the effect of air part (or oxygen), water vapour, make the superpolymer generation pyrolysis of biomass, oxidation, reduction reforming reaction, finally be converted into carbon monoxide, hydrogen.Biomass gasification reaction is the existing common technology in this area.
In bio-reactor, methanobacteria is by carbonic acid gas, and profit is reduced with hydrogen to methane.
Bio-reactor as preferred encloses container, can pressure-bearing not higher than 2 normal atmosphere.
The methanobacteria of bio-reactor and other anerobe are transplanted from other fermentor tank usually.
As preferably, the temperature of reaction in bio-reactor is 13-60 degree Celsius, and reaction pressure is 1-2 normal atmosphere.
Further preferably, temperature of reaction is 40-50 degree Celsius, and reaction pressure is 1.1-1.5 normal atmosphere.
As preferably, in bio-reactor, first input a part of methanobacteria, as seed, in the process of synthesizing methane, react from the methane in anaerobic fermentation tank and seed methanobacteria, generate methanobacteria further, a part for the methane of the generation simultaneously in bio-reactor also can be reacted with seed methanobacteria, generates methanobacteria further.
In process of production, for the generation situation of methane gas, constantly methanobacteria can also be transplanted from outside.
As preferably, described bio-reactor arranges methanobacteria and transplants passage, to transplant methanobacteria from outside.As preferably, methanobacteria can be transplanted according to the output situation of methane.If find that the efficiency of methane output is lower than certain numerical value, then open valve, transplant methanobacteria in bio-reactor.
The output efficiency of methane can judge according to the quantity of the carbonic acid gas of input, hydrogen, adopts the ratio of the actual methane produced and the methane produced in theory, and the methane produced in theory adopts the carbonic acid gas of input and the quantity of hydrogen to calculate.
As preferably, the condensing temperature of condenser 9 is 25 degrees Celsius.Mainly water vapor condensation is got rid of.
The specific embodiment of reaction is see chart 1.
Table 1
Table 2: a preferred embodiment reaction conditions and result
As preferably, the hydrogen content in air-flow 2 is more than 95%, substantially can reach 100%.
The methane produced in bio-reactor 6 is within the condenser in condensation, the thermal resistance mechanism of air-flow non-azeotrope polycomponent blending agent condensation in liquefaction has obvious difference with pure component material condensation, and theoretical analysis and experiment have proved that the coefficient of heat transfer obviously reduces than pure component condensation.The existing research to non-azeotrope blending agent condensing heat-exchange is focusing more on the operating mode containing a kind of noncondensable gas, adopt the measures such as low groove, Artificial roughness surface to reduce average thickness of liquid film and be proved remarkably productive measure when pure component condensation, sometimes not obvious containing effect in noncondensable gas situation, and the condensing heat-exchange process of the air-flow of synthesizing methane and mechanism more complicated, condensation process comprises two or more noncondensable gases usually, and heat exchange situation is more complicated.
For the problems referred to above, the utility model provides a kind of new plate-fin heat exchanger, thus solves the condensation of the different polycomponent blending agent of methane building-up process mid-boiling point.
If do not have specified otherwise, relate to formula, "/" represents division, "×", " * " represent multiplication.
As shown in Figure 2, a kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, described plate-fin heat exchanger comprises plate 12 parallel to each other, forms fluid channel 11 between described adjacent plate 12, arranges fin 16 between described adjacent plate 12.Described fin 16 comprises the sloping portion 13 tilted with plate 12, and described sloping portion is parallel to each other.By impact style processing projection 15 on sloping portion 13, thus the fluid of sloping portion 13 both sides is communicated with by the hole that sloping portion 13 is formed by impact style; Described projection 15 stretches out from sloping portion 13.
Because sloping portion 13 is parallel to each other, between therefore adjacent sloping portion 13 and upper and lower plate, constitute parallelogram passage.
By arranging projection 15, there is following advantage:
1) on the one hand can breakable layer laminar sublayer, on the other hand compared with " punching " fin, not because heat interchanging area is lost in punching, and " thorn " and " hole " can disturbance fluid on different heights respectively, strengthens different thermal resistance links;
2) aperture that punching press " aculea " is formed, by the impact of " aculea " downstream pressure field, can realize pressure and the mass exchange of fin media of both sides, damage, enhanced heat exchange to the stability of viscous sublayer and liquid film.
3) for the fluid of non-azeotrope multicomponent mixture, can the contact area of expansion liquid-gas interface and gas phase boundary and cooling wall be realized by " aculea " and strengthen disturbance;
4) easily process realization, manufacture difficulty and cost can not obviously rise.
In plate-fin heat exchanger, take above-mentioned measure, the simple and easy effective technology again of non-azeotrope blending agent condensing heat-exchange can greatly be improve.With take compared with " punching " fin, the heat exchange efficiency of 20-13% can be improved.
As preferably, the angle that described projection 15 and the flow direction of mixture are formed is acute angle.
As preferably, as shown in Figure 3, described fin 16 is apsacline fin, and described fin 16 comprises horizontal component 14 and sloping portion 13, described horizontal component 14 is parallel with plate 12 and stick together with plate 12, and described sloping portion 13 is connected with horizontal component 14.
As shown in Figure 7, the angle of the described bearing of trend of projection 15 and the flow direction of mixture is a, as shown in Figure 4, along the flow direction of mixture, same sloping portion 13 arranges multiple projection 15, and along the flow direction of mixture, described angle a is increasing.
Found through experiments, large by the change gradually of angle a, compared with identical with angle a, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 10%.
As preferably, along the flow direction of mixture, it is more and more less that angle a becomes large amplitude.Found through experiments, change the amplitude that the change of angle a is large, when can ensure heat exchange efficiency, reduce resistance to flow further, approximately can reduce the resistance to flow of about 5%.
As preferably, described projection 15 is isosceles triangle, the base of described isosceles triangle is arranged on sloping portion 13, and as preferably, base is identical with the angle of inclination of sloping portion, the drift angle of described isosceles triangle is b, along the flow direction of mixture, same sloping portion 13 arranges multiple projection 15, along the flow direction of mixture, when base length remains unchanged, described projection drift angle b is more and more less.Found through experiments, by diminishing gradually of projection drift angle b, compared with identical with drift angle b, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 8%.
As preferably, along the flow direction of mixture, the amplitude that drift angle b diminishes is more and more less.Found through experiments, the amplitude that drift angle b diminishes is more and more less, when can ensure heat exchange efficiency, reduces resistance to flow further, approximately can reduce the resistance to flow of about 4%.
As preferably, along the flow direction of fluid, same sloping portion arranges many row's projections 15, and as shown in Figures 4 and 5, often the distance of arranging between projection is S2, and along the flow direction of mixture, described S2 is increasing.Why so arrange, main purpose is large by the change of S2, realizes, when ensureing heat exchange efficiency, reducing resistance to flow further.Found through experiments, resistance to flow reduces about 10%.
Described S2 is is computed range with the base of the projection of adjacent row.
As preferably, as shown in Figure 5, many row's projections 15 are shifted structure.
Find in an experiment, the distance of adjacent plate 12 can not be excessive, cross the reduction that conference causes heat exchange efficiency, too small meeting causes resistance to flow excessive, in like manner, for the base length of isosceles triangle, drift angle, projection, the distance of fin sloping portion and the angle of fluid flow direction all can not be excessive or too small, excessive or too smallly the change of the reduction of heat exchange efficiency or resistance to flow all can be caused large, therefore in the distance of adjacent plate 12, the base length of isosceles triangle, drift angle, projection, an optimized size relationship is met between fin sloping portion and the angle of fluid flow direction.
Therefore, the utility model is thousands of numerical simulations by the interchanger of multiple different size and testing data, meeting in industrial requirements pressure-bearing situation (below 10MPa), when realizing maximum heat, the dimensionally-optimised relation of the heat exchange plate of the best summed up.
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, and the angle of the acute angle between sloping portion and plate is c, meets following formula:
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 be with the relative face of adjacent plate between distance, W is that L is the distance of summit to base mid point of isosceles triangle with the relative face of adjacent sloping portion along the distance on plate direction.
As preferably, c1=0.245, c2=0.694,
c3＝0.873，c4＝0.691，c5＝1.1454。
As preferably, 85 ° of <c<80 °.
By the geometric scale of the best of " projection " that go out of above-mentioned formula, heat exchange efficiency can be improved, can realize only to viscous sublayer or comprise liquid film and to the strengthening comprising gas phase boundary different scale internal thermal resistance, avoiding measures is excessive, causes unnecessary drag losses simultaneously.
As preferably, the base of the adjacent projection of described same row all on one wire, the protrusion distance that same row is adjacent is S1, described 4 × h<S1<6 × h, and wherein S1 is with the distance of the mid point on the base of adjacent two isosceles triangle projections.
As preferably, the base of the isosceles triangle of the projection of adjacent row is parallel to each other, and the summit of isosceles triangle is L to the distance of base mid point, and the distance S2 of adjacent row is 4*L<S2<7*L.Be preferably S2=5*L
When the base of the isosceles triangle of adjacent row is different, take the weighted average on two bases to calculate.
As preferably, the angle of the isosceles triangle of same row is identical with base.Namely shape is identical, is equal shape.
For formula above, for the projection that front and rear row size is different, be also still suitable for.
For the concrete dimensional parameters do not mentioned, design according to normal interchanger.
Another preferred embodiment of methane is prepared, as shown in Figure 8 as the utility model.Compared with first embodiment of Fig. 1, difference is to eliminate bio-reactor 6, directly in anaerobic fermentation tank 4, carries out biological respinse.The methane produced carries out condensation through condenser 9.
As preferably, anaerobic fermentation tank 4 is divided into two portions, and first part carries out the reaction producing biogas, and second section is the reaction producing methane, the part that biogas and air-flow 2 mix.
In anaerobic fermentation tank, first input a part of methanobacteria, as seed, in the process of synthesizing methane, react from the methane produced in anaerobic fermentation tank and seed methanobacteria, generate methanobacteria further.
As preferably, in process of production, for the generation situation of methane gas, constantly methanobacteria can also be transplanted from outside.
As preferably, described anaerobic fermentation tank arranges methanobacteria and transplants passage, to transplant methanobacteria from outside.As preferably, methanobacteria can be transplanted according to the output situation of methane.If find that methane output is lower than regime values, then open valve, transplant methanobacteria in anaerobic fermentation tank.
As preferably, in second section in anaerobic fermentation tank, density of hydrogen proofing unit, methane concentration detection device, carbon dioxide concentration detecting device can be set, detect the mole number of hydrogen, methane, carbonic acid gas in anaerobic fermentation tank respectively, and carry out adjustment T-valve automatically as previously described according to the result detected, make the ratio that the gas content in anaerobic fermentation tank reaches best.
As preferably, the passage of air-flow 2 arranges valve, entered the flow of the air-flow 2 in anaerobic fermentation tank by Valve controlling.
If the content of hydrogen is lower in the bio-reactor measured, then controller increases the aperture of valve automatically, if it is higher to measure hydrogen content, then controller reduces the aperture of valve automatically.Certainly, manual mode also can be adopted to control.
Other situations do not introduced in Fig. 8 embodiment are identical with the embodiment of Fig. 1, just not in concrete introduction.
As preferably, wind power generation plant also can adopt device of solar generating to replace, such as solar panel etc.
Although the utility model discloses as above with preferred embodiment, the utility model is not defined in this.Any those skilled in the art, not departing from spirit and scope of the present utility model, all can make various changes or modifications, and therefore protection domain of the present utility model should be as the criterion with claim limited range.
Claims (8)
1. one kind utilizes the preparation facilities of the biomethane of power generation assembly, it is characterized in that: comprise anaerobic fermentation tank, bio-reactor, power generation assembly and electrolytic water device, described power generation assembly is connected with electrolytic water device, electrolytic water device is connected with bio-reactor, and described anaerobic fermentation tank is connected with bio-reactor.
2. preparation facilities as claimed in claim 1, is characterized in that, arrange biogas cleaning apparatus between anaerobic fermentation tank and bio-reactor.
3. as the preparation facilities of one of claim 1-2, it is characterized in that, described bio-reactor is connected with condenser.
4. preparation facilities as claimed in claim 3, it is characterized in that, described condenser is plate-fin heat exchanger, described plate-fin heat exchanger comprises plate parallel to each other, between described plate, fin is set, described fin comprises the sloping portion favouring plate, and sloping portion processes projection by impact style, and the hole that the fluid of sloping portion both sides is formed by impact style on sloping portion is communicated with; Described projection stretches out from sloping portion along simulation model for mixing gases flows direction.
5. preparation facilities as claimed in claim 4, it is characterized in that, the angle of the bearing of trend of described projection and the flow direction of mixture is a, and same sloping portion arranges multiple projection, and along the flow direction of mixture, described angle a is more and more less.
6. preparation facilities as claimed in claim 1, is characterized in that, the pipeline between anaerobic fermentation tank and bio-reactor is arranged biogas valve, the pipeline that electrolytic water device is connected with bio-reactor arranges hydrogen valve.
7. preparation facilities as claimed in claim 1, is characterized in that, also comprise the Hydrogen Line, methane conduit and the carbon dioxide conduit thereof that are connected with bio-reactor, each pipeline arranges valve and speed detector simultaneously.
8. preparation facilities as claimed in claim 1, it is characterized in that, described power generation assembly is wind power generation plant or device of solar generating.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107201308A (en) * | 2017-06-26 | 2017-09-26 | 山东大学 | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control |
| CN107328274A (en) * | 2017-06-27 | 2017-11-07 | 山东大学 | A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique |
| CN110467948A (en) * | 2019-06-21 | 2019-11-19 | 浙江臻泰能源科技有限公司 | Combine the electric energy storing system and method for bio-natural gas processed with biogas using electric power more than needed |
-
2015
- 2015-12-03 CN CN201521002731.6U patent/CN205152232U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107201308A (en) * | 2017-06-26 | 2017-09-26 | 山东大学 | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control |
| CN107328274A (en) * | 2017-06-27 | 2017-11-07 | 山东大学 | A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique |
| CN110467948A (en) * | 2019-06-21 | 2019-11-19 | 浙江臻泰能源科技有限公司 | Combine the electric energy storing system and method for bio-natural gas processed with biogas using electric power more than needed |
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