CN205133525U - Preparation facilities of living beings methane - Google Patents
Preparation facilities of living beings methane Download PDFInfo
- Publication number
- CN205133525U CN205133525U CN201521002699.1U CN201521002699U CN205133525U CN 205133525 U CN205133525 U CN 205133525U CN 201521002699 U CN201521002699 U CN 201521002699U CN 205133525 U CN205133525 U CN 205133525U
- Authority
- CN
- China
- Prior art keywords
- condenser
- fermentation tank
- flow
- anaerobic fermentation
- methane
- 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.)
- Expired - Fee Related
Links
Classifications
-
- 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 a preparation facilities of living beings methane, including anaerobic fermentation tank, gasifier, compressor, membrane separator and condenser, anaerobic fermentation tank is connected in proper order to the gasifier behind compressor, membrane separator and condenser, in bioreactor, and the reaction of synthesizing methane. The utility model discloses a setting is the direct reaction in anaerobic fermentation tank, has saved bioreactor, realizes the production of methane simultaneously in anaerobic fermentation tank through biological method, has saved the cost, has improved the production efficiency of methane simultaneously.
Description
Technical field
The utility model belongs to field of energy utilization, particularly relates to a kind of interchanger and comprises methane preparation technology and the system of interchanger, belong 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 hydrogen purification biogas to be 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 of biomethane, comprise anaerobic fermentation tank, vapourizing furnace, compressor, membrane separation apparatus and condenser, vapourizing furnace is connected anaerobic fermentation tank through compressor, membrane separation apparatus successively after condenser, in bio-reactor, carry out the reaction of synthesizing methane.
As preferably, vapourizing furnace connects compressor by synthetic gas cleaning apparatus.
As preferably, compressor, membrane separation apparatus and condenser are two respectively, described vapourizing furnace successively through first step compressor, first step membrane separation apparatus, first step condenser, high stage compressor, the second season membrane separation apparatus be connected anaerobic fermentation tank after the condenser of the second stage.
As preferably, the pipeline between condenser and anaerobic fermentation tank arranges valve.
As preferably, described condenser is plate-fin condenser, plate-fin condenser 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, thus 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 length that described projection extends is L, and along the flow direction of mixture, same sloping portion arranges multiple projection, and along the flow direction of mixture, described length L is increasing.
As preferably, the pipeline between condenser and anaerobic fermentation tank is arranged at least one in carbon dioxide concentration detecting device, density of hydrogen proofing unit and flow monitor.
As preferably, anaerobic fermentation tank is divided into two portions, and first part carries out the part that anaerobically fermenting produces the reaction of biogas, the part that second section is biogas and reacts from the synthetic gas synthesizing methane of vapourizing furnace.
As preferably, arrange in the second section in anaerobic fermentation tank density of hydrogen proofing unit, methane concentration detection device, carbon dioxide concentration detecting device at least one.
As preferably, methanobacteria is set in described anaerobic fermentation tank and transplants passage.
The plate-fin heat exchanger that a kind of Mixed Gas Condensation uses, 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, it is characterized in that, sloping portion processes projection by impact style, thus 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 length that described projection extends is L, and along the flow direction of mixture, same sloping portion arranges multiple projection, and along the flow direction of mixture, described length L is increasing.
As preferably, comprise anaerobic fermentation tank, vapourizing furnace, compressor, membrane separation apparatus and condenser, in described anaerobic fermentation tank, produce biogas, containing methane and carbon dioxide in described biogas; The synthetic gas that vapourizing furnace produces is successively after compressor, membrane separation apparatus and condenser, and enter anaerobic fermentation tank, the synthetic gas entered in anaerobic fermentation tank contains hydrogen, and in anaerobic fermentation tank, biogas and synthetic gas carry out the reaction of synthesizing methane.
As preferably, the catalyzer used in the reaction of synthesizing methane is hydrogen nutritional type methanogen.
As preferably, the synthetic gas that vapourizing furnace produces enters compressor after synthetic gas cleaning apparatus.
As preferably, comprise two stages of compression, membrane sepn and condensation process, described synthetic gas enters bio-reactor successively after first step compressor, first step membrane separation apparatus, first step condenser, high stage compressor, second stage membrane separation apparatus and second stage condenser.
As preferably, produce biogas in anaerobic fermentation tank, the molar content more than 45% of methane, the molar content of carbonic acid gas is more than 30%, and the molar content entering the hydrogen of the synthetic gas of anaerobic fermentation tank is more than 70%.
As preferably, described from synthetic gas cleaning apparatus synthetic gas be out divided into two strands of air-flows, the second air-flow and the tenth air-flow respectively, tenth air-flow is directly used in generator to carry out generating electricity or enter interchanger heating, second road air-flow enters first step compressor and compresses, first step membrane separation apparatus is entered from compressor air-flow out, from membrane separation apparatus sub-argument two strands of air-flows out, the 4th air-flow and the 5th air-flow respectively, 4th air-flow is used for generator to carry out generating electricity or enter interchanger heating, 5th air-flow enters first step condenser, within the condenser the moisture in the 5th air-flow is carried out condensation, to get rid of moisture wherein, high stage compressor is entered from first step condenser air-flow out, air-flow after compression enters second stage membrane separation apparatus, two strands of air-flows are gone out from second stage membrane separation apparatus sub-argument, one air-flow is used for electrical power generators or enters interchanger heating, one enters anaerobic fermentation tank after the condenser condenses of the second stage.
As preferably, the position that the second air-flow is connected with the tenth air-flow arranges T-valve, and described T-valve and Controlling System carry out data cube computation, and Controlling System controls the opening and closing direction of T-valve and the size of aperture thereof.
As preferably, described condenser at least one be foregoing interchanger.
Compared with prior art, the utility model has following advantage:
1) develop the interchanger that a kind of condensation adapting to gas is purified, the efficiency that condensation proposes can be improved.
2) the utility model is by being arranged on direct reaction in anaerobic fermentation tank, eliminates bio-reactor, is realized the production of methane simultaneously, provide cost savings, improve the production efficiency of methane simultaneously in anaerobic fermentation tank by biological method.
3) the utility model proposes a kind of device 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.
4) 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:
1-12 air-flow, 13 vapourizing furnaces, 14 synthetic gas cleaning apparatus, 15 first step compressors, 16 first step membrane separation apparatuss, 17 first step condensers, 18 high stage compressors, 19 second stage membrane separation apparatuss, 20 generators, 21 interchanger, 22 second stage condensers, 23 bio-reactors, 24 third stage condensers, 25 biogas cleaning apparatus, 26 anaerobic fermentation tanks, 27 sealing members, 28 fluid channels, 29 plates, 30 sloping portions, 31 horizontal components, 32 projections, 33 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 26, bio-reactor 23, vapourizing furnace 13, compressor, membrane separation apparatus and condenser, the biogas that described anaerobic fermentation tank 26 produces enters in bio-reactor 23, enter in the biogas of bio-reactor 23 containing methane and carbon dioxide, as preferably, what content was maximum is methane and carbon dioxide successively; The synthetic gas that vapourizing furnace 13 produces is successively after compressor, membrane separation apparatus and condenser, enter bio-reactor 23, enter synthetic gas content in bio-reactor 23 maximum be hydrogen and carbonic acid gas successively, in bio-reactor 23, carry out the reaction of synthesizing methane: CO
2+ 4H
2-CH
4+ 2H
2o;
The catalyzer used in bio-reactor 23 is hydrogen nutritional type methanogen.
As preferably, biogas, before entering bio-reactor 23, also purifies through biogas cleaning apparatus 25, to remove impurity, and such as hydrogen sulfide, ammonia, oxosilane etc.
As preferably, the synthetic gas that vapourizing furnace 13 produces enters compressor after synthetic gas cleaning apparatus 14.By synthetic gas cleaning apparatus to remove impurity, such as sulfide, tar etc.
As preferably, synthetic gas is through the process of stage compression, membrane sepn and condensation.Further preferably, comprise two stages of compression, membrane sepn and condensation process as shown in Figure 1, described synthetic gas enters bio-reactor successively after first step compressor 15, first step membrane separation apparatus 16, first step condenser 17, high stage compressor 18, second stage membrane separation apparatus 19 and second stage condenser 22.By stage compression, membrane sepn and condensation process, the concentration of the hydrogen in the synthesizer entered in bio-reactor can be improved further, the concentration of carbonic acid gas can be improved simultaneously.
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%, and the molar content entering the hydrogen of the synthetic gas of bio-reactor is more than 70%, preferably 75%.
As preferably, the molar content entering the carbonic acid gas of the synthetic gas of bio-reactor is more than 4%.
As shown in Figure 1, described from synthetic gas cleaning apparatus synthetic gas be out divided into two strands of air-flows 2 and 10, one air-flow 10 is directly used in generator and generates electricity, one road air-flow 2 enters first step compressor 2 and compresses, first step membrane separation apparatus 15 is entered from compressor air-flow 3 out, from membrane separation apparatus sub-argument two strands of air-flows 4 out, 5, one air-flow 4 generates electricity for generator, one air-flow 5 enters first step condenser 16, within the condenser the moisture in air-flow 5 is carried out condensation, to get rid of moisture wherein, high stage compressor 18 is entered from first step condenser 16 air-flow 7 out, air-flow 7 after compression enters second stage membrane separation apparatus 19, two strands of air-flows are gone out from second stage membrane separation apparatus 19 sub-argument, one air-flow 8 is for electrical power generators, one enters bio-reactor 23 after second stage condenser 27 condensation.
The air-flow 1 of biogas after biogas cleaning apparatus 25 produced in anaerobic fermentation tank 26, enters in bio-reactor 23.
The air-flow generated in bio-reactor 23, through third stage condenser 24, forms last air-flow 12.
Preferably, the main component in air-flow 1 is methane and carbon dioxide, and preferably wherein methane content is maximum, more than more than 45%.
Preferably, comprise nitrogen, carbon monoxide, hydrogen, carbonic acid gas in air-flow 2, also comprise a small amount of methane, wherein a nitrogen content is the highest simultaneously, is secondly carbon monoxide and hydrogen.
Air-flow 3 is identical with the content of air-flow 2.
Preferably, mainly comprise hydrogen, carbonic acid gas, nitrogen and carbon monoxide in air-flow 5, also have a small amount of methane and water vapour, wherein hydrogen content is the highest, beyond 50%, is secondly carbonic acid gas simultaneously.
Preferably, main containing hydrogen in air-flow 9, preferably containing carbonic acid gas, also there is a small amount of carbon monoxide, nitrogen and water vapour simultaneously.
As preferably, in bio-reactor, the ratio of carbonic acid gas and hydrogen is: 1 to 4 (mole number ratio).
The position that air-flow 10 is connected with air-flow 2 arranges T-valve, and described T-valve and Controlling System carry out data cube computation, and Controlling System controls the opening and closing direction of T-valve and the size of aperture thereof.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 carbon dioxide concentration detecting device is set on the pipeline of air-flow 9, density of hydrogen proofing unit and flow monitor, the pipeline of air-flow 1 arranges methane concentration detection device, carbon dioxide concentration detecting device, described controller is according to carbon dioxide concentration detecting device, density of hydrogen proofing unit, methane concentration detection device calculates 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 10 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 controller adjusts T-valve automatically, increases the flow of air-flow 10, reduces the flow of air-flow 2; If the mole number of the hydrogen detected is on the low side, then increase the flow of air-flow 2, reduce the flow of air-flow 10.
If it is too much to detect the mole number entering the carbonic acid gas of bio-reactor, the then corresponding content automatically increasing hydrogen, namely controller adjusts T-valve automatically, increase the flow of air-flow 2, reduce the flow of air-flow 10, on the contrary, controller adjusts T-valve automatically, increase the flow of air-flow 10, reduce the flow of air-flow 2.
If it is too much to measure the mole number entering the methane of bio-reactor, then controller adjusts T-valve automatically, increase the flow of air-flow 2, reduce the flow of air-flow 10, by the hydrogen in increase air-flow 2 and carbonic acid gas, on the contrary, controller adjusts T-valve automatically, increase the flow of air-flow 10, reduce the flow of air-flow 2.
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, the pipeline that T-valve can be used in air-flow 10 and air-flow 2 arranges valve to replace respectively, realizes above-mentioned controlling functions.Described valve connects with controller data, the aperture of described controller autocontrol valve, to adjust the flow of air-flow 10 and air-flow 2.
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, the passage of air-flow 9 arranging valve, for controlling the air-flow 9 entered in bio-reactor, thus controlling the quantity of the hydrogen entered in bio-reactor.
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.
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 30-60 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, membrane separation apparatus adopts tubular fibre and Matrimid polymeric material to make.Membrane separation apparatus can adopt existing membrane separation apparatus, such as DavidOC, GorriD, NijmeijerK, OrtizI, UrtiagaA.Hydrogenseparationfrommulticomponentgasmixtures containingCO, N2andCO2using
asymmetrichollowfibermembranes.J.Membr.Sci.2012; 419-420:49-56.
Membrane separation apparatus is mainly applicable to by Hydrogen Separation out.
Although although membrane separation apparatus is prior art, really use first in Hydrogen Separation, and find through experiment, separating effect other membrane separation apparatus far super, separating effect improves 20%-30%.
As preferably, the condensing temperature of condenser at different levels 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
Air-flow is within the condenser in condensation, and 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 29 parallel to each other, forms fluid channel 28 between described adjacent plate 29, arranges fin 33 between described adjacent plate 29.Described fin 33 comprises tilting the sloping portion 30 with plate 29, and described sloping portion is parallel to each other.By impact style processing projection 32 on sloping portion 30, thus the fluid of sloping portion 30 both sides is communicated with by the hole that sloping portion 30 is formed by impact style; Described projection 32 stretches out from sloping portion 30.
Because sloping portion 30 is parallel to each other, between therefore adjacent sloping portion 30 and upper and lower plate, constitute parallelogram passage.
By arranging projection 32, 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 20-30% can be improved.
As preferably, the angle that described projection 32 and the flow direction of mixture are formed is acute angle.
As preferably, as shown in Figure 3, described fin 33 is apsacline fin, and described fin 33 comprises horizontal component 31 and sloping portion 30, described horizontal component 31 is parallel with plate 29 and stick together with plate 29, and described sloping portion 30 is connected with horizontal component 31.
As preferably, the length that described projection 32 extends is L, and along the flow direction of mixture, same sloping portion 30 arranges multiple projection 32, and along the flow direction of mixture, described length L is increasing.Found through experiments, large by the change gradually of length L, compared with identical with length L, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 9%.
As preferably, along the flow direction of mixture, it is more and more less that length L becomes large amplitude.Found through experiments, the amplitude that the change of length L is large 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 5%.
As preferably, described projection 32 is isosceles triangle, the base of described isosceles triangle is arranged on sloping portion 30, 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 30 arranges multiple projection 32, 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 32, 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 32 are shifted structure.
Find in an experiment, the distance of adjacent plate 29 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 29, 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<0.41,0.29<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 23, directly in anaerobic fermentation tank 26, carries out biological respinse.
As preferably, anaerobic fermentation tank 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 9 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 9 arranges valve, entered the flow of the air-flow 9 in anaerobic fermentation tank by Valve controlling.
As preferably, the passage of air-flow 9 arranging valve, for controlling the air-flow 9 entered in bio-reactor, thus controlling the quantity of the hydrogen entered in bio-reactor.
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.
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 (10)
1. the preparation facilities of a biomethane, it is characterized in that: comprise anaerobic fermentation tank, vapourizing furnace, compressor, membrane separation apparatus and condenser, vapourizing furnace is connected anaerobic fermentation tank through compressor, membrane separation apparatus successively after condenser, in bio-reactor, carries out the reaction of synthesizing methane.
2. preparation facilities as claimed in claim 1, is characterized in that, vapourizing furnace connects compressor by synthetic gas cleaning apparatus.
3. preparation facilities as claimed in claim 1, it is characterized in that, compressor, membrane separation apparatus and condenser are two respectively, described vapourizing furnace successively through first step compressor, first step membrane separation apparatus, first step condenser, high stage compressor, the second season membrane separation apparatus be connected anaerobic fermentation tank after the condenser of the second stage.
4. preparation facilities as claimed in claim 2, is characterized in that, the pipeline between condenser and anaerobic fermentation tank arranges valve.
5. preparation facilities as claimed in claim 1, it is characterized in that, described condenser is plate-fin condenser, plate-fin condenser 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, thus 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.
6. preparation facilities as claimed in claim 5, is characterized in that, the length that described projection extends is L, and along the flow direction of mixture, same sloping portion arranges multiple projection, and along the flow direction of mixture, described length L is increasing.
7. preparation facilities as claimed in claim 1, is characterized in that, the pipeline between condenser and anaerobic fermentation tank is arranged at least one in carbon dioxide concentration detecting device, density of hydrogen proofing unit and flow monitor.
8. preparation facilities as claimed in claim 1, it is characterized in that, anaerobic fermentation tank is divided into two portions, and first part carries out the part that anaerobically fermenting produces the reaction of biogas, the part that second section is biogas and reacts from the synthetic gas synthesizing methane of vapourizing furnace.
9. preparation facilities as claimed in claim 1, is characterized in that, arrange in the second section in anaerobic fermentation tank density of hydrogen proofing unit, methane concentration detection device, carbon dioxide concentration detecting device at least one.
10. the preparation facilities as described in one of claim 1-7, is characterized in that, arranges methanobacteria and transplant passage in described anaerobic fermentation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521002699.1U CN205133525U (en) | 2015-12-03 | 2015-12-03 | Preparation facilities of living beings methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521002699.1U CN205133525U (en) | 2015-12-03 | 2015-12-03 | Preparation facilities of living beings methane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205133525U true CN205133525U (en) | 2016-04-06 |
Family
ID=55619336
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201521002699.1U Expired - Fee Related CN205133525U (en) | 2015-12-03 | 2015-12-03 | Preparation facilities of living beings methane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205133525U (en) |
Cited By (1)
| 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 |
-
2015
- 2015-12-03 CN CN201521002699.1U patent/CN205133525U/en not_active Expired - Fee Related
Cited By (1)
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN205152232U (en) | Utilize preparation facilities of power generation facility's living beings methane | |
| CN104371780A (en) | System and method for preparing coal-based synthetic natural gas by using abandoned wind electricity or photo-electricity and industrial organic wastewater | |
| CN107142288A (en) | The method of mixed bacterial fermentation synthesis gas production acetic acid and octanoic acid | |
| Abuşoğlu et al. | Exergy analyses of green hydrogen production methods from biogas-based electricity and sewage sludge | |
| Foglia et al. | Fermentative hydrogen production: influence of application of mesophilic and thermophilic bacteria on mass and energy balances | |
| CN108658361A (en) | The integrated livestock and poultry cultivating system of biomass cogeneration of heat and power | |
| CN205133525U (en) | Preparation facilities of living beings methane | |
| CN205170836U (en) | Preparation facilities of living beings methane | |
| CN105300143B (en) | A kind of plate-fin heat exchanger and its methane preparation technology using solar energy | |
| CN201962264U (en) | System for producing natural gas by wind, power and coal | |
| US20210147787A1 (en) | Bioreactors with Integrated Catalytic Nitrogen Fixation | |
| CN105387739B (en) | Methane preparation process by utilization of wind electricity | |
| CN105423781A (en) | Plate-fin heat exchanger used for mixed gas condensation and methane manufacturing technology of plate-fin heat exchanger | |
| CN106017158B (en) | A kind of plate-fin heat exchanger and the methane preparation technology reacted in anaerobic fermentation tank | |
| CN210635950U (en) | Biogas preparation device combining biogas purification and carbon dioxide methanation | |
| CN107328274A (en) | A kind of plate type heat exchanger, the wind-powered electricity generation methane preparation facilities of independent tubes control and its technique | |
| CN204198705U (en) | Wind, light abandon electricity and the industrial organic waste water system for coal preparing natural gas | |
| CN104031834A (en) | Hydrogen manufacturing method through photosynthetic bacterium continuous reaction | |
| CN110396528A (en) | A kind of method of sludge anaerobic microbe conversion synthesis gas beam system acetic acid | |
| CN115215386B (en) | Preparation of nickel cobaltate nano-particles and method for promoting hydrogen production by dark fermentation | |
| CN103184242A (en) | Biological utilization method of coal underground gasification product gas | |
| CN108408689A (en) | A kind of anhydrous hydrogen generating system | |
| Golub | Effect of bioreactor mode of operation on mixed-acid fermentations | |
| CN107201308A (en) | The methane preparation facilities and its technique of a kind of utilization wind-powered electricity generation intelligent control | |
| CN203700350U (en) | Simple anaerobic fermentation device for laboratory |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160406 Termination date: 20181203 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |