CN104912705A - System and method for realizing sustainable economic development through integrated total production of renewable materials by using solar thermal - Google Patents

System and method for realizing sustainable economic development through integrated total production of renewable materials by using solar thermal Download PDF

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Publication number
CN104912705A
CN104912705A CN201510098366.1A CN201510098366A CN104912705A CN 104912705 A CN104912705 A CN 104912705A CN 201510098366 A CN201510098366 A CN 201510098366A CN 104912705 A CN104912705 A CN 104912705A
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Prior art keywords
hydrogen
carbon
material resources
electrode
methane
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CN201510098366.1A
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Chinese (zh)
Inventor
罗伊·E·麦卡利斯特
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McAlister Technologies LLC
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McAlister Technologies LLC
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Priority claimed from US12/707,656 external-priority patent/US8075749B2/en
Priority claimed from US12/707,651 external-priority patent/US8075748B2/en
Priority claimed from US12/707,653 external-priority patent/US8172990B2/en
Application filed by McAlister Technologies LLC filed Critical McAlister Technologies LLC
Publication of CN104912705A publication Critical patent/CN104912705A/en
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    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
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    • F03B13/14—Adaptations of machines or engines for special use; Combinations of machines or engines with driving or driven apparatus; Power stations or aggregates characterised by using wave or tide energy using wave energy
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Abstract

In a embodiment of the invention, a system for providing renewable sources of material resources is provided. The system comprises: a first source of renewable energy; a first material flow from a first material source; an electrolyzer connected with the first source of the renewable energy and the first material flow, wherein the electrolyzer is formed as that a first material resource is generated through electrolyzing; a processor which is used for further processing or using the material resources to generate a second material recouce, wherein the processor comprises a solar collector which is formed as that the first material resource is provided the heat so as to be dissociated; and a material resource storage which is connected with the electorlyzer to receive the material resources from the electrolyzer or provide the material recources to the processor for further processing or using.

Description

Solar heat is used to be realized the system and method for sustainable economic development by the integrated overall production of recyclable materials resource
The application's application number in be the applying date be on August 16th, 2010 is the divisional application that 201080048872.5 (PCT/US2010/002260) name is called China's application of " using solar heat to be realized the system and method for sustainable economic development by the integrated overall production of recyclable materials resource ".
the cross reference of related application
This application claims the U.S. Provisional Application number 61/304 that the title submitted on February 13rd, 2010 is " FULL SPECTRUM ENERGY AND RESOURCE INDEPENDENCE ", 403, the title submitted on February 17th, 2010 is the U.S. Patent Application No. 12/707 of " ELECTROLYTIC CELL AND METHOD OF USE THEREOF ", 651, the title submitted on February 17th, 2010 is the PCT application PCT/US10/24497 of " ELECTROLYTIC CELL AND METHOD OF USE THEREOF ", the title submitted on February 17th, 2010 is the U.S. Patent Application No. 12/707 of " APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS ", 653, the title submitted on February 17th, 2010 is the PCT application PCT/US10/24498 of " APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS ", the title submitted on February 17th, 2010 is the U.S. Patent Application No. 12/707 of " APPARATUS AND METHOD FOR GAS CAPTURE DURING ELECTROLYSIS ", 656, the title submitted on February 17th, 2010 U.S. Provisional Patent Application that to be title that the PCT application PCT/US10/24499 and 2009 of " APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS " submits to 27, on Augusts be " ELECTROLYZER AND ENERGY INDEPENDENCE TECHNOLOGIES " number 61/237, the preference of 476 and rights and interests.These applications are incorporated herein each via incorporated.
Background technique
Water plants and cover plant, particularly farmland and forest, the source of the natural habitat of the Carbon dioxide collector that is absolutely necessary, countless wildlife and the fiber for the application such as from paper product to structural material.Because the introducing of non-native insect and the climatic change of greenhouse gases aggravation make forest be subject to the infringement of infectious diseases, fire, wind, flood and Droughts, therefore there is forest-devastation in nearly all continent all.
In whole South America, Central America and North America, woods fire has damaged the standing tree of cannot withstand a single blow because of arid and disease of huge number or death.This forms the massive losses of paper pulp and structural material.Fire and the rotten greenhouse gases that also produce are as carbon dioxide and methane, and it will damage global atmosphere further.The vital Practical Solution being to provide the renewable supply source that vegetal biomass can be rapidly converted into fuel, electricity before it loses because of fire, rotten, flood and erosion and have valency material.Inevitable target is promotion health forest, the building fast again and promote from for improving forest condition and prevent harmful spreading of fire and the tending and intermittent cutting of forest that specifies and shrubbery felling are produced fuel and cut the carbonaceous value deposited of crop and other ground quilts.
The demand of hydrogen, oxygen, methane, carbon and other products provided as the thermochemistry of biomass castoff and/or electrolytic dissociation by raw material is increased.By thermochemical method dissociate living beings make great efforts in the past really from William Murdock in 1792 by water vapor and carbon donor as the reaction hydrogen manufacturing of mud coal, coal and charcoal.Recently, Steam Reforming is extensively adopted with from oil, rock gas and other fossil feedstock hydrogen manufacturing by petroleum industry.
Carbon dioxide and methane cause climatic change to the release in global atmosphere, and such climatic change threatens the extinction up to 1/3 in whole living species.Overcome effort that air degenerates because of greenhouse gases Martin M.Halmann and Meyer Steinberg " greenhouse Gas Carbon Dioxide mitigation:Science and Technology", John A.List " recent Advances in Environmental Economics" and John Gale " greenhouse Gas Control Technologies:Proceedings of the 6 th international Conference on Greenhouse Gas Control Technologies" in address.
The replacing method of methane processed and hydrogen is by destructive distillation and anaerobic pyrolysis.Somebody utilizes overboard, wind, the sun and fossil energy to produce for the electricity by electrolytic decomposition water.Victoria M.Laube and Stanley Martin " conversion of Cellulose to Methane and Carbon Dioxide by Triculture of Acetivibrio Cellulolyticus Desulfovibro sp., and Methanocarcina Barkeri" describe the purposes using bacterial gas cellulose in (Canadian National Research Council).It is further well known that at larger species as there is symbiosis between bovine animals and termite, bovine animals picked-up lignocellulosic also produces methane and carbon dioxide because of the parasitism of methanogen this kind of in its digestive system.
Publication as " hydrogen Production From Water By Means of Chemical Cycles", Glandt, Eduardo D., and Myers, Allan L., Department of Chemical and Biochemical Engineering, University of Pennsylvania, Philadelphia, PA 19174, industrial Engineering Chemical Process Development, Vol.15, No.1, 1976; " hydrogen As A Future Fuel", address the effort for providing the technology reducing the problem that these methods meet with to do in Gregory, D.P., Institute of Gas Technology.
Problem with this type systematic comprises: low energy conversion efficiency, and it is unacceptably high that fixed equipment and Infrastructure improve cost, and expansion scale is to solve significant problem as having difficulties when forest is changed, and operating cost is high.In addition, art methods needs release of carbon dioxide very in large quantities.In this class process, sizable Capital expenditure, the supervening and high operating cost of the consumption of large electricity and greenhouse gases are needed to the compressor needed for hydrogen and/or methane and the pressurization of other products.In addition, unacceptable maintenance needs and the high cost of repairs have defeated these class methods.Existing waste turns energy technologies and overcomes because global atmosphere percent of greenhouse gases gathers the ability critical constraints of caused growing climatic change problem, if not counterproductive.Generally speaking, too expensive, the too waste and polluting very much of prior art.
Therefore, the object of embodiments more of the present invention is to provide the system and method being realized sustainable economic development by the integrated overall production of renewable nutrients resource, it can comprise use electrochemistry or electrolytic cell produces the purposes of nutrients resource discretely and uses it to produce the method for nutrients resource discretely, to solve one or more the problems referred to above.
Summary of the invention
In one embodiment of the invention, provide a kind of for providing the system of the renewable origin of material resources, described system comprises: the first source of renewable energy; From the first flow of material of the first source of the material; The electrolyser be connected with described first flow of material with the first source of described renewable energy, wherein said electrolyser is constructed to produce the first material resources by electrolysis; For processing further or using described material resources to produce the processor of the second material resources, wherein said processor comprises solar collector and wherein said solar collector is constructed to provide heat to dissociate to described first material resources; And be connected to receive material resources from described electrolyser with described electrolyser or provide material resources with the material resources storage processed further or use to described processor.
In another embodiment, provide a kind of for providing the system of the renewable origin of material resources, described system comprises: the first source of renewable energy; From the first flow of material of the first source of the material; The electrolyser be connected with described first flow of material with the first source of described renewable energy, wherein said electrolyser is constructed to produce the first material resources by electrolysis; For processing further or using described material resources to produce the processor of the second material resources, wherein said processor comprises solar collector and wherein said solar collector is constructed to provide heat to dissociate to described first material resources; And be connected to receive material resources from described electrolyser with described electrolyser or provide material resources with the material resources storage processed further or use to described processor.
In yet another embodiment, provide a kind of for providing the method for the renewable origin of material resources, described method comprises: the first source providing renewable energy; The first flow of material from the first source of the material is provided; There is provided the electrolyser be connected with the first source of described renewable energy with described first flow of material, wherein said electrolyser produces material resources from described first flow of material by electrolysis; With provide described material resources to process further or to use to first processor.
By detailed description below, other Characteristics and advantages of the present invention will become apparent.But should understand, here detailed description and illustrate that the specific embodiment of the preferred embodiments of the invention provides by means of only the mode of example, because by this detailed description, the variations and modifications in the spirit and scope of the present invention will be apparent to those skilled in the art.
Accompanying drawing explanation
Fig. 1 shows process steps of the present invention.
Fig. 2 is the longitudinal cross-section view of the embodiment that principle according to the present invention is run.
The longitudinal section zoomed-in view of the part of the embodiment of parts of Fig. 3 for providing in Fig. 1.
Fig. 4 is the sectional view of the embodiment that principle according to the present invention is run.
Fig. 5 is the partial cross section figure of the embodiment that principle according to the present invention is run.
Fig. 6 shows the process steps that principle according to the present invention is run.
Fig. 7 is the schematic diagram of the embodiment that principle according to the present invention is run.
Fig. 8 shows the operation according to principle of the present invention.
Fig. 9 shows the parts that principle according to the present invention is run.
Figure 10 is the schematic diagram of embodiment of the present invention.
Figure 11-14 is the flow chart of the various embodiments according to aspect of the present disclosure.
Figure 1B shows the electrolytic cell according to one embodiment of the invention.
Fig. 2 B shows the zoomed-in view of a part for the embodiment of Fig. 1.
Fig. 3 B shows a modification of the embodiment of Fig. 2.
Fig. 4 B shows the electrolytic cell according to one embodiment of the invention.
Fig. 5 B shows the zoomed-in view of the alternate embodiment of a part for the electrolytic cell of Fig. 4.
Fig. 6 B shows the cross section for the screw electrode in reversible fuel cell.
Fig. 7 B show for by Organic Ingredients as by photosynthesis produce those be converted into the system of methane, hydrogen and/or carbon dioxide.
Fig. 8 B show for by Organic Ingredients as by photosynthesis produce those be converted into the system of methane, hydrogen and/or carbon dioxide.
Fig. 9 B show for by Organic Ingredients as by photosynthesis produce those be converted into the system of methane, hydrogen and/or carbon dioxide.
Figure 10 B shows the method for the manufacture of electrode according to an embodiment of the present disclosure.
Embodiment
The application is incorporated to the U.S. Provisional Patent Application number 60/626 that the title submitted on November 9th, 2004 is " MULTIFUEL STORAGE; METERING AND IGNITION SYSTEM " by reference of text, the title submitted in 021 (attorney docket 69545-8013US) and on February 17th, 2009 is the theme of U.S. Provisional Patent Application number 61/153,253 (the attorney docket 69545-8001US) of " FULL SPECTRUM ENERGY ".It is " METHODS AND APPARATUSES FOR DETECTION OF PROPERTIES OF FLUID CONVEYANCE SYSTEMS " (attorney docket 69545-8003US) that the application is also incorporated to the following title meanwhile submitted on August 16th, 2010 by reference of text, " COMPREHENSIVE COST MODELING OF AUTOGENOUS SYSTEMS AND PROCESSES FOR THE PRODUCTION OF ENERGY, MATERIAL RESOURCES AND NUTRIENT REGIMES " (attorney docket 69545-8025US), " ELECTROLYTIC CELL AND METHOD OF USE THEREOF " (attorney docket 69545-8026US), " SUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATED PRODUCTION OF RENEWABLE ENERGY, MATERIALS RESOURCES, AND NUTRIENT REGIMES " (attorney docket 69545-8040US), " SYSTEMS AND METHODS FOR SUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATED FULL SPECTRUM PRODUCTION OF RENEWABLE ENERGY " (attorney docket 69545-8041US), " METHOD AND SYSTEM FOR INCREASING THE EFFICIENCY OF SUPPLEMENTED OCEAN THERMAL ENERGY CONVERSION (SOTEC) " (attorney docket 69545-8044US), " GAS HYDRATE CONVERSION SYSTEM FOR HARVESTING HYDROCARBON HYDRATE DEPOSITS " (attorney docket 69545-8045US), " APPARATUSES AND METHODS FOR STORING AND/OR FILTERING A SUBSTANCE " (attorney docket 69545-8046US), " ENERGY SYSTEM FOR DWELLING SUPPORT " (attorney docket 69545-8047US), the theme of each U.S. Patent application of " ENERGY CONVERSION ASSEMBLIES AND ASSOCIATED METHODS OF USE AND MANUFACTURE " (attorney docket 69545-8048US) and " INTERNALLY REINFORCED STRUCTURAL COMPOSITES AND ASSOCIATED METHODS OF MANUFACTURING " (69545-8049US).
For understanding the mode obtained according to above-mentioned details of the present invention and other advantages and object completely, below in conjunction with its specific embodiments, the present invention is described in more detail.
Fig. 1 shows process 16, wherein, living beings (comprising municipal administration, farm and forest waste as forest waste wood and sick and/or dead tree) are cut, pull away or otherwise gather and pay in step 2 place.In step 4, this kind of biomass castoff is shredded or is otherwise subdivided into fritter and section so that conveyor such as Belt Conveyors, pusher bar conveyor or screw conveyor are efficiently carried and compacting.In step 6, dried and dissociated by reproducibility and transform and produce hydrocarbon, alcohol vapor and methane, hydrogen and other gases and solid such as carbon and to introduce with by cellulose and/or lignocellulosic material or in company with the mineral introduced together with cellulose and/or lignocellulosic material through the biomass castoff of segmentation.Step 8 provides steam and gas being separated as methane and/or hydrogen and carbon dioxide.Step 10 provides the gas of usual methane rich by pipeline or other delivery methods as those the shipment adopted in gas industry.Step 12 provides hydrogen and carbon products from the production of the methane-rich gas of such Cemented filling.Step 14 provides the use of hydrogen in motor and/or fuel cell to think, and motor vehicle provide power, provide heat, for shaft work and generating, apply and production fertilizer for chemical process.
The analysis of fire in most of impaired forest environment, earthquake and mud-stone flow disaster is shown, by create under ground piping with carry this kind of impaired forest and/or ground by Quick Acquisition and transform the methane that produces advance solution disclosed in this invention will be highly favourable.This kind of renewable methane is shipped to market (using rock gas or other fossil fuels at present) by pipeline and greatly can reduces the environmetal impact from greenhouse gases and can promote rely on evolution to renewable energy safety from current fossil.
Create and will to create more jobs chance and investors'confidence by the renewable origin of the methane carried at low cost with pipeline.By development by methane to carbon products transform, simultaneously use hydrogen be used for clean energy resource apply " the carbon epoch " that advance will bring other progress.
Fig. 2 shows for renewable the embodiment 200 of producing the method and apparatus of methane and/or hydrogen of dissociating by living beings, wherein, as shown in the figure, material such as various cellulosic material and lignocellulosic tissue through segmentation are also heated to discharge required gas by degassed, dry.The system of Fig. 2 is formed at the thermal efficiency and suppression carbon dioxide and provides important improvement.These improve by shown in process queue shown in Fig. 1 extracting carbon, hydrocarbon provides as the elimination of the counter-current drying before methane and/or hydrogen and air, moisture and other oxygen donators.
Finally, this kind of waste is sufficiently heated and discharges required gas, carbon and solid residue as mineral oxide and other compounds in anaerobic environment.This process is summarized by equation 1, and equation 1 is not for any particular type of lignin, cellulose or other biological raw material, amount or ratio trim in addition.Therefore, equation 1 and 2 summarize the versatility of process shown in Fig. 1 and the Organic Ingredients showing carbon containing, hydrogen and oxygen to methane, hydrogen with cut the qualitative conversion of depositing the valuable supply source of carbon.
C xh yo z+ heat → CH 4+ H 2+ CO 2+ CO equation 1
CH 4+ ▲ H 298K→ 2H 2+ C (▲ H 298K=79.4kJ/mol) equation 2
Be to the system implementation plan of gas as the rapid conversion of methane, hydrogen, carbon dioxide and carbon monoxide shown in Fig. 2 for biomass castoff.Be in operation, swivelling pipe 214 is driven by motor 202 by suitable deceleration system 204 and 206, and motor 202 can be rotary engine, piston engine or turbogenerator, and this depends on the size of system and required throughput.Motor 202 is preferably fueled by fuel adjusting, injection and ignition system 202, and as U.S. Patent application 08/785, disclosed in 376, this application is incorporated herein by reference.To be transferred to the material in hopper 250 preferably by the adverse current elbow of spirality heat exchange duct system 244 and 245 from the used heat of engine-cooling system and/or exhaust, hopper 250 is received in spirality heat exchange duct system 244 and 245 is obtaining maximum heat yield respective area from motor 202.
Depend on the size of converter, deceleration component is if sprocket wheel and chain or driving gear 206 and bearing bearing assembly 208 and 212 are preferably by torque transfer thermal insulator 210 and swivelling pipe 214 thermal insulation.Swivelling pipe 214 at end opposite place by insulation bearing and bearing assembly 224 and 226 obtain similar supporting and thermal insulation as shown in the figure.Insulator bag 230 provides insulation to prevent bearing 212 and other needs protections in order to avoid the region be heated obtains radiation and heat by conduction.
As equation 1 and 2 summarize a relatively little part in the methane that generates and/or hydrogen and/or carbon monoxide be delivered to motor 202 and be delivered to the burner nozzle of combustion-chamber assembly 220 by control valve 222, as shown in Figure 2.There is provided enough air to guarantee the perfect combustion of the fuel value existed, the noxious emission in making two kinds to apply is all minimum.The products of combustion of heat flows through spirality heat exchange duct system 216, transmits heat with the organic material of advancing with countercurrent direction under the push effect to the fin 218 on the outside of swivelling pipe 214 as shown in the figure.
Preferably provide screw thread 218 spacing reduced progressively and/or the cross-section area reduced between swivelling pipe 214 and fixed tube 236, with the solid material of constantly compacting entrained with, as shown in the figure.This will provide the air and/or moisture evicting from from the organic material heated by described process carried secretly, because this kind of gas by be forced to with by being advanced by the direction of the material upstream of the hopper 250 that heats and feed screw 256 feeding, wherein, feed screw 256 is driven by suitable traction motor 252 or the suitable drive train from motor 202.The cross section that the pitch reducing screw conveyor or the waste reducing compacting pass through also prevents the escape by heating the gas that organic material (comprising the reaction with the reactant gas added) produces further by providing fine and close sealing.
Expection, overall process of the present invention also by other materials conveying and compacting measure obtain, and use in some applications unidirectional push rod send with debulking systems replacement shown in screw conveyor will be more convenient.Basic step is by completing as follows: compacting and heating are to eliminate air and moisture, produce the shutoff sealing being derived from the advance material of raw material, heat described advance material and produce the required pressure and temperature condition of required chemical derivative (being selected from material if carbon, one or more gaseous hydrocarbons, fuel alcohol and gas are as ethane, methane, hydrogen and oxycarbide) to reach to dissociate, seal or help to seal utilizing the derivative of advance material and/or residue in the district that the district pipetting required chemical substance is provided and extract required chemical substance.Preferably by from required chemical substance along with it cools and counter-flowing heat exchange and by the counter-flowing heat exchange from the burning of selected fuel with restoring ground or regeneration, there is provided heat to add to the material being advanced through such process phases, maximize to make the heat utilization in gained system.
Can provide and run relatively for a long time and greatly reduce the generation of carbon, for make produced chemical substance obtain needed for carbon/hydrogen ratio rate, this may be preferred.This long-play can intermittently provide, such as have a mind to produce carbon with before the collection of required chemical substance help sealing described district and/or this collect after help sealing described district time between.This is the feature of embodiments more of the present invention, and it makes carbon can be transferred as the constituent element of fluid, these fluids by pipeline be delivered to storage (comprising the multiple pressure of depleted gas reservoir), to factory with manufacture carbon strengthen durable goods and for other objects.After in succession evicting air and moisture from, biological material is converted into the gas product shown in equation 1 and measures much lower solid residue.In many cases, the amount of solid residue is about 2 to 10% of the initial mass of organic waste.This kind of residue is the important sources of trace mineral, and it is preferably used for revitalizing the soil and guarantee the quick growth of the after-culture standing tree of healthy forest, garden, aquaculture and/or other ground quilts.The minimizing of quickening greenhouse gases, carbon and cutting of hydrogen are deposited and expanding economy by this.Carbon is deposited to produce reproducible methane, hydrogen as disclosed herein like that continuously and to cut in the sustainable source that reforestation region is used as lignocellulosic.
Have in the systems compared with big unit and high productive capacity, combustion gas from burner assembly 220 can be made at pipe thread 216 Inner eycle, pipe thread 216 is constructed to be connected with threaded pipe 218 by the hole in pipe 214, to provide the more flash heat transfer of the raw material of advancing to the outside along the screw thread 218 in sealed tube 236 from firing chamber 220.Allow and enter in the annular space between helical fin 238 and insulation tube 241 from the Organic Ingredients gas such as methane, hydrogen and the carbon dioxide that are discharged by thermal dissociation process of heating, with to flow with the direction flowing into adverse current of the raw material heated by swivelling pipe assembly 214.This will provide further heat to preserve, because being reproduced property is added to raw material in pipe 236 by heat, these raw materials are by compacting progressively and dissociate because of heat transfer, thus strengthen the generation of pressure, as shown in the figure.
Combustion gas such as water vapor, nitrogen, oxygen and the carbon dioxide of the inside and/or pipe fin 216 and/or 218 arrival hopper district that are advanced through pipe 214 enter spirality heat transfer pipe 246, to provide further adverse current energy to add to the raw material being advanced through hopper 250, as shown in the figure.Be advanced through hole 230 and the annular region between pipe 236 and pipe 241 and/or hollow fin 238 arrive hopper 250 district produce gas such as methane, hydrogen and carbon dioxide and/or carbon monoxide and circulate in pipe-line system 248, it is contiguous with to the material countercurrent heat-transfer effectively of advancing to swivelling pipe screw conveyor 214 that pipe-line system 248 is wrapped in spirality pipe system 246, as shown in the figure.Insulator 242 and 260 prevents thermal loss to outside.
Issuable gas product such as carbon dioxide is separated with methane and/or hydrogen by the system as shown in pressure oscillating or temperature absorption and/or Fig. 4 with the mixture of carbon monoxide.Such product gas mixture by the rotational speed that controls Rotatruder 214 and the compacting of therefore transmitting to the solid in thermal dissociation stage to provide higher than required pressure is suitable for the pressure of nargin.
This Efficient Conversion that will heat energy provided to pressure energy, because the volume ratio original solid volume of the desired gas formed is far much bigger.Be in operation, pressure transducer 270 sends pressure data to keep feeding conveyor 256, the extruding speed of the conveyor 214 and heating value of combustion-chamber assembly 220 to process controller 272, with the pressure of gas product obtaining required throughput, conversion temperature and send.Pressure regulator 274 provides gas product from the last adjustment of sending of regenerating transformed device 200.
An aspect of the present disclosure is is potential energy using low cost thermal transition as energy storage, utilize such pressure to promote separation process and regeneration of energy.The mixture of pressurization is separated while pressurization needed for the selected gas of maintenance.This forced feed of refined quality gas is used for providing power for motor comprises internal-combustion engine with the motor with external heat supply.
Also adopt such Conversion of Energy, refining and pressurization by pipeline or pressurization tank car or by distally market delivery refinery gas and the storage of liquefying.Also expect certain areas with comprise 09/969,860 one or more in the various embodiments of interior co-pending Patent application run together, and these patent applications are incorporated herein by reference.
The hydrogen of waste assists the major defect of the art methods of gasification to be need high pressure resistant, heat-resisting and expensive equipment.As shown in the figure, embodiment of the present invention provide the self-reinforced structure of tubular structure.Strengthen by combine in modular structure heat exchange, enhancing, rigidization, transmission and heat-resisting benefit spirality strengthen structure and provide, described modular structure builds by rapid-assembling process.This will to accelerate in waste management applying and compare method reduction delivery system cost in the past of required corrective measure to a great extent.
This will provide carbon compound as carbon dioxide or carbon monoxide and gas being effectively separated as methane and/or hydrogen.As shown in Figure 4, the mixture of gas product sends to be exposed to water in pressurized container 402 by pipe 404 or other absorbent fluid are selected, with optionally separating carbon dioxide and/or carbon monoxide.
The delivered under pressure that therefore methane and/or hydrogen keep in pressurized container 402 is to collecting pipe 408.After absorbing carbon dioxide and/or carbon monoxide, the absorption fluids of pressurization be delivered to nozzle manifold 426 by 410 in case be delivered to as shown in the figure heat exchanger as 414,416,418,420,422,424 etc., here, from the exhaust of motor 202 heat can with burner 444 burn a part of gas product and waste gas (carbon monoxide as discharged through 458 by the follow-up expansion of pressure fluid) be delivered to shown heat exchanger together with the heat that discharges.Also wind energy or wave energy is used to supply additional heat by resistance or indcution heater by solar collector 442 or in the place of wind energy or wave energy abundant resource.Then fluid through heating expands through turbine 430,432,434,436,438,440 etc. as shown in the figure and, to reclaim and/or conversion of energy, thus improves overall efficiency further.
Also by suitable generator as alternator 280 and/or alternator 428 provide the added improvement of the overall efficiency of generating.Hydrogen is preferably utilized to reduce wind loss to cool these generators.After realizing these functions, the fuel that then hydrogen be used as motor 202 or the carbon-free fuel be used as in firing chamber 444 and/or 220.
From typical organic waste as grape sugar, lignin and cellulosic material by as described in the generality of the raw methanogenic overall reaction of embodiment be summarised in shown in equation 3.
C 6h 12o 6+ heat → 3CH 4+ 3CO 2equation 3
In some applications, the electrolysis preferably by the derivative of raw material produces the generation that oxygen reduces or eliminates carbon dioxide, and this has open in co-pending patent application.This kind of material particularly also can be controlled to produce ethane with the carbon of the hydrogen-gasified of hydrogen and the surplus of existence at the same time or in follow-up process steps.When need impaired forest to be rapidly converted into load and transport the forced feed source of the methane in market afield, ethane and hydrogen by pipeline and then utilize these pipelines to continue to send this kind of gas with the speed of reduction according to required forest thinning speed, results plan and maintenance program, this chemical process modification will be favourable.
The pipeline transmission capacity that this method is established becomes a kind of important stocking system, with the daily and seasonal variety of meeting the need of market.Usually need the pipeline gas of gained after the embodiment by Fig. 2 and Fig. 4 removes carbon dioxide, particulate matter, ash content, sulfur dioxide and water, provide the output of about 900BTU/scf.
For most of waste, the original output not during recycle hydrogen is in 350 to 650BTU/scf scope, and calorific value is lower.The raising of calorific value reaches by the multiple choices of pressure and temperature in decomposition process or the speed that is recycled to the reaction zone at 239 places by increasing hydrogen.But the co-pending spark that application discloses sprays (SparkInjection) technology to make to realize determine power production from the quota of internal-combustion engine, fuel selection is not from the gaseous mixture of 250BTU/scf to liquid diesel etc.
The type of the gaseous mixture waste with being converted as shown in table 1 produced by the operation under about 1,000PSI and 1025 °F (69 barometric pressure, 550 DEG C) of the embodiment of Fig. 2, the waiting time and relevant Operational Limits and different.A kind of new preparation can realize replacing diesel fuel with ignition by compression and being included in the hydrogen of the absorption in active carbon/methanol suspension body.
Such gaseous mixture can produce fast and can supplement with the component of higher-energy as methyl alcohol, carbon/methanol suspension body or propane etc., and the ignition mixture being feature to make be able to hydrogen burning obtains in fact any required energy content in composite fuel application.The hydrogen of reaction generation and/or methane is usually needed to be sprayed with the speed being enough to produce required methane/ethane ratio by manifold 239 and reboot in reaction zone to provide the gas of pipeline quality or to be used for the raw material of chemosynthesis.
Table 1
Gaseous product Forest waste Municipal solid rubbish Muck
Hydrogen (H 2) 22 (volume %) 33 (volume %) 20 (volume %)
Methane (CH 4) 60 53 61
Ethane (C 2H 6) 17 11 18
Carbon monoxide 1 2 1
In some cases, preferably liquid fuel and the precursor of methyl alcohol as being easy to storage and transport is provided from the embodiment of Fig. 2.Methyl alcohol or " another name for " extract through partial combustion or by anoxic heating process by heating lignocellulosic waste.Equation 4 and 5 summarises by selecting the obtainable methyl alcohol of different anoxic operating temperature, pressure and catalyzer to export.
C 6h 12o 6+ heat → 6CO+6H 2equation 4
6CO+6H 2→ 3CH 3oH+3CO equation 5
Under higher feed rate and/or lower firing chamber 220 HRR, material can not reach the higher temperature producing gas shown in equation 1, and therefore this process produces methyl alcohol.From methyl alcohol, isolate carbon monoxide to form liquid methanol preferably by cooling methanol vapor and utilize the fuel of isolated carbon monoxide as motor 202, the combustion heat release by burner assembly 220 and by with water as in equation 6 summarize react formation hydrogen.The hydrogen produced by the reaction of summarizing in equation 6 can be used to as shown in equation 5, produce methyl alcohol, improve the operation of motor 202, improve the yield of methyl alcohol and/or ethane in converter 200 and/or as shown in the figure as the heating fuel in converter 200.
CO+H 2o → H 2+ CO 2equation 6
Should point out, each reaction system illustrated herein is improved further by homogeneous phase and the use of heterogeneous catalysis and the application of Adaptive Control, with the result needed for improving or optimizing.Exemplarily, about the reaction zone between manifold 239 and air stripper port 240, expection uses such catalyst choice: described catalyst choice will strengthen the formation of methane and ethane by promoting the reaction of the effect of hydrogen structure reactive component, described reactive component synthesis forms methane and ethane.Catalyzer comprise trivalent chromium and other have the pottery of rare earth component, platinum group metal, nobelized nickel and transition metal intermetallic compounds be all applicable.Compared with art methods, this unexpectedly and significantly reduce equipment cost and complexity.Similarly, produce except methyl alcohol except by the partial oxidation of methane, also expection utilizes group of the lanthanides-ruthenium preparation, Fischer-Tropsch catalyzer and copper, copper intermetallic compounds and/or Cuprum alloy to strengthen the synthesis of methyl alcohol from carbon monoxide and hydrogen.
Fig. 3 shows methyl alcohol from the separation carbon monoxide and methyl alcohol by the shipment of transfer pump 298 to market.Be in operation, embodiment 300 is preferably introduced greater density and is separated with the eddy current compared with light component and allows the mixture of carbon monoxide and methyl alcohol enter container 302 from regenerating pump/motor 312 by pipe 304.If discharge pressure is not enough to the transfer rate needed for acquisition, then pump/motor 312 will provide pump action to this kind of steam, if and required discharge pressure is lower than from the system of Fig. 2 or the supply pressure of another suitable converter 320, then pump/motor 312 will provide the recovery of pressure energy.
The cooling of methanol condensed is provided by the heat exchange loop 306 symbolically illustrated, heat exchange loop 306 preferably utilizes underground water or cooling tower fluid as radiator.Under water in cooling circuit 306 preferably remains on the pressure higher than the steam entering room 302 by pump 296, therefore, any airtight inefficacy of cooling circuit all can not cause cooling water pollution.Can be used as hot water supply source from 324 cooling waters leaving separator 302 or turn back to groundwater regime, cooling tower or evaporation pond, this be different with application.At abundant cooled gas mixture, produce the larger methanol vapor of density and drop near the wall of container 302 after, the carbon monoxide that density is less is extracted by center tube.The methyl alcohol of condensation sends the gas processing further to remove water and/or absorption by pump 298, this depends on required purity.
Methyl alcohol and methane, ethane can be shipped to market with intercoursing by identical or additional pipeline with the pipeline gas mixture of hydrogen.When using same pipeline, when will be converted to another kind of chemical product from a class chemical product, the separation slug preferably such as using pressure to advance by the technology of empirical tests before refilling next thing to be delivered or clean pipeline by finding time.
Fig. 5 shows an embodiment similar to the system of Fig. 1 and 2, and it comprises compacting cylinder 500 with conversion of biomass as sawdust, muck and wood chip.The operation of this system is substantially the same with the embodiment of Fig. 2, and the compacting unlike living beings is cyclically provided by reciprocating push rod.Push-rod piston 502 under the forcing of oil hydraulic cylinder 506 in stationary cylinder 518 reciprocal compacting living beings, these living beings are drying and preheating by counter-flowing heat exchange in hopper 250.
When push rod 502 is in shown position, living beings are loaded in cylinder 518 by conveyor 256.Motor 202 drives oil hydraulic pump 504 and sends pressurized working fluid to handle cylinder 506 by pipeline 510 and 511.In forward path, living beings are pressed into closely knit material by push rod 502, the taper 512 walking around heater 516 along with it moves, this closely knit material by further compacting, taper 512 can be fixing or rotate with improves throughput and when living beings are advanced through conversion process maintenance living beings compaction state.Usually can allow evicting from of air and water vapor at numerous pipes of 249 positions, also be used as material safety check to prevent the backflow of the material advanced under the effect of push rod 502 simultaneously.The coordination of response controller 272 and control, the temperature of living beings will be fully promoted, to cause the dissociation reaction of summarizing in equation 1,3,4 and 5 with the counter-flowing heat exchange of the combustion gas from burner assembly 220 being advanced through Spiral type Heat Exchanger fin 216 and 218.
Therefore, organic substance is converted into fluid as methane, ethane, propane, methyl alcohol, ethanol, hydrogen, hydrogen sulfide, carbon monoxide and carbon dioxide, and be improved with substitute fossil fuels by hydrogen sulfide, carbon monoxide and the carbon dioxide removing harmful levels, described in remove by the reproducibility embodiment of Fig. 4 or by other suitable selectivity remove process as Pressure Swing Adsorption, temperature swing adsorption, solution absorbs and UF membrane carries out.This by with source if a part is from the heat exchange of the counter-flowing heat exchange of the burning of one or more fuel elements of this kind of fluid, the material before producing, in process and afterwards from higher temperature to lower temperature and by providing with the heat exchange of energy conversion device as internal-combustion engine, external-combustion engine, expansion motor and fuel cell.
Fig. 6 show by methane (from landfill yard, sewage treatment works, waste treatment operation (comprise based on Fig. 1,2,3, the embodiment of 4 and 5 those) and other methane sources) as in equation 2 summarize be converted into the process steps 60 of hydrogen and carbon.The burning of hydrogen is that hydrocarbon is as seven to nine times of gasoline, fuel alcohol, methane and diesel fuel.This make wherein to spray with hydrogen combusted or take hydrogen as the turbogenerator of fuel as the mixture of hydrogen and methane, hydrogen and methyl alcohol or hydrogen and carbon monoxide of feature, the operation of combustion rotor motor and Reciprocating engine can have the efficiency of raising and less carbon emission or non-carbon-emitting.
The thermal efficiency that brought by such operation is improved for intermittent combustion formula motor if combustion rotor motor and reciprocating two strokes or four stroke engine are as 202 particular importances, thus will close to top dead center, directly spray and/or igniting at top dead center or provide in after top dead center, to reduce or to avoid the thermal loss in compression process and negative work.In the power stroke process of motor, this will guarantee that fuel potential energy is converted into function with higher efficiency far away.Therefore, by rapid combustion in the excess air that burns in a combustion chamber take hydrogen as the fuel of feature, obtains significantly higher operational efficiency by than having the motor that the routine that adopts propane, rock gas or diesel fuel arranges.
In the step 62 of Fig. 6, by Fig. 1,2,3, the embodiment of 4 and 5 produces and methane purify extremely required degree by launch vehicle in bulk or the extremely suitable destination of Cemented filling as industry park.Methane then in step 64 by with dissociate the hydrogen and/or carbon counter-flowing heat exchange that produce and be preheated to suitable temperature from ambient temperature, such as about 1200 DEG C (2200 °F).In the step 66, to there is provided enough heat to add as graphite, iron oxide, aluminium oxide, magnesium oxide, various carbide or other ceramic contact by radiation and/or with the material through heating, with make carbon deposition this kind of on the material of heating or near and as equation 2 summarize discharge hydrogen.Step 68 provide the collection of this kind of hot hydrogen with the methane counter-flowing heat exchange about the advance described in step 64.In step 70, the carbon formed by dissociating of methane is with sediments or peel off with the material through heating used from step 66 or the powder that peels off or sheet material are collected.
In alternative plan, in step 72 combustion step 66, the common carbon of generation and/or a part for hydrogen, produce the required pressure and temperature that dissociates of methane to heat or help the gain of heat.Alternative heating source for realizing the methane dissociation of step 66 comprises concentrated solar energy, conductive ceramic if the resistance heating of graphite or zirconic electrical induction, this kind of base material and this kind of base material are from the radoal heating of suitable incandescent source, the various modification (comprising the plasma relating to hydrogen and/or methane) of plasma heating and/or by the suitable fuel of burning (comprise methane or methane dissociation product as hydrogen and/or carbon).
Device for the method provided in step 62,64,66,68,70 and/or 72 comprises various types of fluidized bed, spiral or piston induced flow reactor, has the plasma chamber that carbon collects measure and feature and the production of carbon black stove improved.The benefit of the particular importance of embodiments more of the present invention comprises adds from hydrocarbon as the methane production hydrogen also valuable carbon form of common generation with energy much lower needed for dissociate water.Dissociating of hydrocarbon feed produces hydrogen and product as U.S. Patent application 09/370, and the open acquired height combination of carbon products and hydrogen that will provide in 431 is worth.Fig. 7 shows another the special efficient system being beneficial to described method.
Fig. 7 shows the parts of process system 700.Be in operation, hydrocarbon such as methane is delivered to refractory tube bucket 704 by pipe 702, in refractory tube bucket 704, fire-resistant screw conveyor 710 rotate with the particle of mobile preferred geometries and size and/or substrate material 711 with receive along with methane by the heating such as radiation, conduction by equation 2 the process summarized from methane dissociation and the carbon of deposition or precipitation.The hydrogen of common generation is transported to inner bore as shown in the figure by the hole 708 of hollow screw conveyor 710.Therefore, advance to the hot hydrogen of Sealing 726 and carbon and exchange with the methane thermal of advancing to Sealing 714.Spiral 710 is used as conduction and photothermal energy exchanging system, does the reaction that mechanical work is summarized to realize equation 2 fast in addition.
The heat that suitable thermal source 706 provides adds the methane dissociation made through preheating.Also carry out the gain of heat by the hollow centre internal combustion annealing in hydrogen atmosphere at screw assembly 710 fire-resistant as shown in the figure.Oxygen or other oxygenants as air by swivel joint 718 send for burning.Oxygen provides preferably by air separation or by co-pending patent application electrolysis.Hydrogen is sent by swivel joint 719 by conduit 717 as shown in the figure.
Depend on the size of converter, deceleration component is if sprocket wheel and chain or driving gear 732 and bearing bearing assembly 730 are preferably by torque transfer thermal insulator assembly 728 and rotating screw assembly 710 thermal insulation.The similar insulation supporter of bearing and swivel joint 716 assembly is provided, to make to minimize from the heat transfer of screw assembly 710 with 718.Insulator bag 724 provides heat transfer to block, to prevent radiation and conductive heat loss and to protect other to need protection in order to avoid the region that is heated.As equation 1 with 2 summarize a relatively little part in the methane that generates and/or hydrogen and/or carbon monoxide be delivered to and 202 engine power generation thermomechanical components similar with 280 as shown in Figure 2, to provide heat and electricity to support to comprise the operation of electric motor 736, electrolyser and/or separator 744, pump or compressor 746 as shown in the figure and generator 712.
Cross-section area in the district flight pitch that reduces progressively being preferably provided and/or reducing to be used as plug for seal part between rotating screw conveyor 710 and fixing socket 704, the solid material carried in it with constantly compacting, as shown in the figure.This will force methane to advance with advancing to the direction of the hydrogen adverse current of swivel joint 719 with the carbon of 710 expert's headings 726, as shown in the figure.Reduce the pitch of screw conveyor or reduce 726 and 714 cross sections that are neighbouring or 726 and 714 places also prevent hydrogen or methane by providing fine and close sealing escape with compacting carbon granule or shape.In larger application, in the district near Sealing 714, screw conveyor 710 can be provided to slightly reverse pitch and prevent methane or hydrogen loss to make carbon pressure contracting produce effective sealing.
Insulation system 724 is beneficial to the hydrocarbon of advancing to Sealing 714 as methane with advance to the high performance counter current heat exchange between the carbon and/or hydrogen of Sealing 726.Gear or sprocket driving 732 and drive motor 736 thermal insulation, and bearing 716 and 730 is designed to thermal insulation and/or high temperature application.Screw conveyor 710 and cylinder 704 are made up of refractory metal or stupalith such as graphite, carbide, nitride, intermetallic compounds and metallic oxide.The heating at 706 places by concentrated solar energy, catalysis or flaming combustion or by electric heating as plasma, resistance or principle of induction preferably use renewable electricity to provide.The oxygen that air separator and/or electrolyser 744 produce is stored in acescent 722, send via pressure regulator 720, and need for dissociation process provide the burning of hydrogen and heat generation time use, such as the sun, wind, flowing water and other renewable resourcess unavailable or inadequate time.
Fig. 8 illustrates overall process 800, and wherein in step 862, photosynthesis provides the organic material of usual carbon containing, hydrogen and oxygen.Step 864 provide anoxic to digest or pyrolysis or partial oxidation to produce the oxide of fuel gas as methane and carbon.Oxide such as carbon dioxide and being separated in step 866 of fuel gas of carbon provide.As the filter be suitable for disclosed in co-pending patent application, Pressure Swing Adsorption, temperature swing adsorption or preferential adsorption are provided by the system being illustrated as 868.Depend on the pressure of purified fuel gas and the pressure needed for the technique of step 872, adopt pressurizer 870, pressurizer 870 comprises to be selected as electrolysis pressurization, mechanical pump or compressor operating, or the releaser from adsorptivity and/or Metal hydride systems that pressurizes.In step 872, as shown in the figure, in final heating with before dissociating, methane by with hydrogen and carbon counter-flowing heat exchange and through preheating.In step 874, as shown in the figure, the product that follow-up heating measures obtains with the carbon that the methane that preheating is hung oneself in customization obtains is selected.
Fig. 9 shows the details of embodiment 900, it comprises sunlight and concentrates mirror 912, concentrated radiation receiver 914, fixed reception pipe 922 and rotating screw conveyor and extruding pipe 924, wherein Integral-type screw 926 forces reactive ingredients such as organic material to enter in district 930, in district 930, it quickly heats up to high temperature by the solar energy concentrated.Fully concentrating of solar energy obtains easily through parabolical mirror, spherical mirror or settled date reflection mirror array with the typical operating temperature producing 500 DEG C to 2500 DEG C, and this is brought up by the physicochemical properties of material and the structure specification of sealed tube 922.
Fixed base 904 covers drive system and provides material to the transmission with autoreactor 914.The fuel of reactor 914 and raw material such as landfill yard methane are delivered by being connected to pipeline 918.When fluid material is processed by reactor 914 as wastewater composition, provide send preferably by being connected to pipeline 915.The electricity produced or send is transmitted by cable group 917.The hydrogen that reactor 914 produces and/or other fluids are delivered to pipeline 916 to store and distribution.Platform 906 rotates around central vertical axis with the solar tracking providing reactor 914, and reactor 914 is assembled with mirror 912.Provide and rotate follow the tracks of the sun and produce point focusing solar energy around the coordination of the horizontal axis 909 in supporting 910 as shown in the figure, this point focusing solar energy reflects from mirror assembly 912.Organic solid to be heated and semisolid are loaded in hopper 908, this kind of material is fed in screw conveyor 924 by hopper 908, and Figure 10 shows a part for screw conveyor 924.
Other forms of renewable heating is also easy to adapt to, such as use induction or the resistance heating of the electricity of self generator, shown generator provides power by overboard, wind, wave action or provides power by the motor of the fuel using described operation to produce herein.Similarly, the fuel that produces of a part of reactor 914 of expection burning with abundant heating-up zone 930, to realize the reaction of equation 1,2 and 5.The alternative heat input of this group in district 930 illustrate when intermittently have cloud cluster to cover or night to supplement or instead of the advantageous measure of the solar energy needed for guaranteeing to run continuously.
With the partial combustion of produced hydrogen and/or carbon monoxide, district 930 supplementary heating or replacement solar heat are sent oxygen preferably by the pipe 937 in the bore which 931 of pipe 932 from electrolyser 907 and realized.Generator 905 is driven to provide an important collaborative benefit by running heat engine 903 based on landfill yard methane and/or hydrogen.Superfluous generate output is used to produce oxygen and hydrogen in electrolyser 907.The hydrogen produced by such operation can be easy to be stored in for sale in pipeline 916, and oxygen can be used to the process efficiency of the partial combustion heat-dissipating greatly improved by the fuel produced in reactor 914 and/or fuel cell power generation application.
When using oxygen to carry out passage divided combustion generation heat, the elimination of nitrogen will be decreased through the cost carrying out purified hydrogen from the gaseous mixture condensation in pipe 932 or filtered water greatly.As shown in the figure, pipe 937 sends oxygen with the fuel of the aequum that burns, and does thermal loss so minimum and eliminate the heating needs of nitrogen, and if use air as oxygenant, then will there is nitrogen.
Therefore pipe 922 realizes holding and is in Organic Ingredients under anoxia condition and to the function of living beings transferring energy as solar energy, described living beings are sent to concentrated heating-up zone 930 to promote to be summarised as following reaction:
C nh mo x+ heat 1→ xCO+m/2H 2+ (n-x) C equation 7
C 6h 10o 5+ heat 2→ 5CO+5H 2+ C equation 8
Containing CO and H 2gaseous product in also may visible NH in a small amount 3, H 2s, N 2and H 2o, this gaseous product is forced by the solid of compacting and enters in the center bore 931 of rotated threaded tubular 932 as shown in the figure.Preferably make H 2s and iron react to form iron sulfide or are collected in the carbon that process produces along with the release of hydrogen.Preferably usual with the form of ammonia collection fixed nitrogen, with the form of iron sulfide collection sulphur, and these materials are used as soil nutrient together with the mineral ash content collected by embodiments more of the present invention.
As shown in the figure, solid as carbon and ash content 936 by volute 932 threadingly 934 rotary motion and extract from district 930.Preferred use high-temperature insulation part 940 covers the end of receiver 914 as shown in the figure, and along with the rich carbon solid extracted by screw conveyor 932 and move to receiver and reactor assemblies the district 930 through heating living beings between counter-flowing heat exchange, insulating regions 942 provides heat to preserve.In the time course of unavailable solar energy, insulating sleeve 948 be used to the area of coverage 930 and preferred by telescopic pipe conductor support and guide to from shown deposit position, described conductor is not shown.
The water removed at the initial stage of compacting and adverse current preheating and other gases are released to extract by collecting pipe 946 preferably by venetian blind or hole 944.For many raw materials as muck and sewage, this water is usually preferred in order to the supplementary workability of soil and productivity containing fixed nitrogen and other soil nutrients.
When preferred pure carbon and pure hydrogen, can by living beings pretreatment to remove the material of formation ash content as calcium, magnesium, phosphorus, iron and other mineral.Usually being wasted property ground landfill is at landfill yard for the ash content composition of living beings, or when from foul sewer system waste discharge and rubbish disposal operation, it may escape into ocean.In some embodiments of the present invention, ash content is easy to collect and turns back in useful application as soil nutrient.This is separated dissociating with living beings in suitable solvent by machinery and realizes with the combination of separate ash component.
Further embodiment provides living beings such as carbohydrate and cellulose to digest by the anoxic of following General reactions:
N (C 6h 10o 5)+n H 2o+ heat 3→ n (C 6h 12o 6) equation 9
N (C 6h 12o 6) → 3n (CH 4)+3nCO 2+ heat 10equation 10
After shown process, the soil nutrient of remaining liquid, aqueous middle trapping transfers to impoverishment of soil effectively by respective technology (comprise and being added in irrigation water).Carbon dioxide produces phase transformation easily through cooling and is separated or removes by being adsorbed on suitable solvent such as the product from process in water.Under 25 barometric pressure and 12 DEG C (54 °F), carbon dioxide can the degree soluble of about 21.6 every volume water of volumes of gas in water.Improve pressure and/or reduce temperature and will increase the amount of the water-soluble carbon dioxide of every volume.After isolate carbon dioxide from methane, reduce pressure or improve the carbon dioxide that temperature discharges dissolving.
The amount of depositing heat required in the process of carbon of cutting that Organic Ingredients anoxic dissociates to produce specified rate is significantly less than the energy collected from air and dissociate needed for carbon dioxide.Implement to be far from extracting carbon dioxide the device be broken down into needed for carbon and oxygen is so complicated from air from the Organic Ingredients device cut needed for the process of depositing carbon, but want simply too much and firmer.
Hydrocarbon is being comprised biomass solid and methane conversion is in the process of carbon and hydrogen, the product of dissociation reaction tends to occupy larger volume than reactant.Device 920 for the assembly 914 carrying out these heat absorption reaction can be easy to the carbon-rich material sealed reaction district 930 with extruder screw thread 934 compacting through the carbon-rich material of extruder screw thread 926 along the entrance compacting to district 930 and the outlet along district 930, and the swivel joint that can be exported by bore which 931 to make the hydrogen of being gone out by bore which 931 and other gases and pressure regulation measure are forced into required degree and keep.
Before methane enters reactor 920, preferably pressurize cold methane to sending pressure needed for hydrogen from reactor 920 with suitable condensation technique, condensation technique comprises by discharging pressurization, phase transformation, mechanical compress and hybrid system from adsorptivity base material.If the gas produced in anoxic digestion is separated by liquefaction, then this realizes easily through making methane gasify to required pressure.Also this object is can be used for by the pressurization of various pump and compressor 870.
Great changes have taken place for the type of producible carbon, depends on the market demand and realize relevant temperature and the pressure that carbon cuts the process of depositing.The methane being delivered to the fabrication stage 874 can process to produce diamond-like coating on fiber, carbon black, suitable substrate, graphite crystal and in U.S. Patent application 08/921 on demand, 134,08/921, common co-pending open corresponding other forms many of 134 and 09/370,431.
Also expect, for some application, preserve advantage as heat, screw conveyor 932 should be designed to feed path and preheater, wherein hydrogen is sent by bore which 931, and the carbon that the reaction in district 930 produces is by carrying with the extruder 924 of the raw material counter-flowing heat exchange entered of designing aptly.Such an arrangement provides the raw material that enters before arriving district 930 by the product parallel stream with raw material process in reverse direction from inner and heat from the adverse current of outside.
The carbon that reaction is formed is carried by screw conveyor 932, the methane that described carbon and pipe 924 counter-flowing heat exchange enter with preheating and therefore improve the overall efficiency and speed that solar energy complete process reacts.The hydrogen produced is collected in the bore which 931 of delivery pipe 932, and with the reactant counter-flowing heat exchange towards district 930 process and remove heat.The reproducible hydrogen produced can be used in fuel cell or in heat engine, and in fact it purify air and provide the exhaust cleaner than ambient air.
Along with process produces carbon, it constantly forms the gas tight seal between the inwall of conveyor screw thread 926 and pipe 922.This needs the extruser pitch of maximum compacting part to guarantee preferably by reducing.Usual needs provide maximum carbon pressure reality and sealing effect to the material of the conversion of hydrogen in experience after district 930 in the outlet of screw conveyor in district 930.
Except as directed screw conveyor, in process shown in expection, the conveying of reactant can be undertaken by other measures numerous.Exemplarily, screw conveyor 924 can be replaced to force living beings to enter reaction zone with reciprocating type plunger, and carbon extracts from hot junction by other extracting methods, comprise and replace screw conveyor 932 with chain driving conveyor.
When needing steam and other valuable products producing liquid fuel or solvent alkene as loose in one or more (turpene), usual adjustable reaction temperature is to lower temperature or the throughput rate improving composition.Available compound can produce as hydrogen, carbon, methyl alcohol, biodiesel and turpentine oil and be collected in tube bore 931, as in the equation for a part with the canonical biometric matter waste materials of shown average formula summarize:
C 6h 10o 5+ heat 6→ CH 3oH+4CO+3H 2+ C equation 11
The introducing of the colloidal carbon of hydrogen in methyl alcohol of boarding absorption will provide higher every volume calorific value and in the application for renewable diesel fuel, provide the ability of ignition by compression.If need higher liquid fuel and/or solvent yield, then the carbon monoxide that produces in the canonical process of equation 11 and hydrogen can be made preferably to react to produce other methyl alcohol and hydrogen under the existence of suitable catalyzer.
4CO+3H 2→ 4CH 3oH+H 2+ heat 12equation 12
Living beings advance to the speed in district 930 and extract the speed of solid residue preferably by computer control by screw conveyor 932, and the instrument of this computer response pressure, temperature and other class indexs measures and required quality of product and control this process adaptively in gas, steam and solid residue stream.
Carbon monoxide by as in equation 8 the disproportionation shown in the process summarized decompose or be converted into required cutting and deposit carbon form:
2CO → C+CO 2+ heat 13equation 13
As in equation 13 the disproportionation summarized be heat release and can provide under the multiple combination of temperature and pressure condition, carry out at being included in 10-40 atmospheric pressure and 500 DEG C to 800 DEG C.
If market conditions support that hydrogen manufacturing is used for fuel cell or heat engine to purify air, then carbon monoxide and water vapor can be made to react with the exothermic reaction as shown in equation 9 and to produce hydrogen:
CO+H 2o → CO 2+ H 2+ heat 14equation 14
The carbon monoxide passing through summarized process generation can be converted into numerous product to meet the need of market, as being selected from the process needing hydrogen manufacturing and/or carbon as shown.The part that the heat of the hotwork preferably utilizing described exothermic process to discharge needed for shown heat absorption reaction adds.
Therefore, embodiments more of the present invention provide cuts the practical approach of depositing carbon from air, and described method comprises photosynthesis, collects photosynthetic organism matter and heats described living beings to produce the product being selected from carbon, hydrogen, methyl alcohol, loose alkene and ash content.Generally allow and rot to enter air and cause the biomass castoff of carbon dioxide and/or methane accumulation can be utilized now, to produce hydrogen, carbon products and soil nutrient efficiently.
It is wherein the preferred embodiment by product of system (unshowned to be oxygen and potable water be also) of the power supply of system and thermal source with hydrogen internal combustion engine that Figure 11 shows.Figure 11 emphasizes, once process starts, namely it be from supporting, because the hydrogen of relatively small amount is utilized for system provide power.Energy efficiency is obtained by the relation between bio-digestion pond and electrolyser.Energy efficiency also by solar heat parabolic reflector technology obtain: by methane cracking be its constituent element: hydrogen and carbon.According to an embodiment, the cracking of methane did not occur at night.According to aspect of the present disclosure, the extensive renewable energy that distributes obtaining hydrogen fuel is thus produced.According to other embodiments, the extensive renewable resources that distributes obtaining carbon (carbon fiber do not distinguished or carbon ash) is thus produced.According to also other aspect, by utilizing different devices, what obtained the special carbon distinguished thus in addition distributes extensive manufacture.When the extensive renewable resources distributed extracts and gathers and renewable energy gathers combined, result is continuable economic development and continuable production.
In other words, from renewable resources and energy, people obtain the refining renewable resources and energy with higher economic value, it is used to produce durable goods then, these durable goods are used for gathering new renewable resources and energy again, and this is a kind of mode of sustainable, pollution-free and non-exhaustion.According to aspect of the present disclosure, this continuable economic model can be write as the Algebraic recursion formulas (recurrence formula is the formula for determining next condition of a sequence by one or more condition formerly) of this continuable economic model.The use of embodiments more of the present invention in production system produces economic multiplier effect to (a) biomass material, (b) methane feed and (c) carbon; Then methane/hydrogen is used to gather more renewable energy and recyclable materials resource; Then carbon becomes durable goods, and it is gathered in the crops more (a) and (b) and produces more (c).Therefore, the disclosure has specialized the mathematics of economic " sustainability ".
Figure 11 may not illustrate the Economic Implication of large scale storage.The energy production not only can distributed (many positions) but also can amplify (can produce in a large number) be obviously confined to compared with the local and method that can not amplify, be a kind of progressive.Figure 12 shows the preferred embodiment wherein with the solar heat centralized system power supply that is system and thermal source.Figure 13 shows wherein non-specified power supply and thermal source and thinks the preferred embodiment that the change in future of system and adaptability are left room for.Figure 14 shows the flow chart of renewable energy production process.
Embodiment above can be realized by electrolyser as disclosed herein.
In one embodiment of the invention, provide a kind of electrolytic cell, described electrolytic cell comprises: closed housing; First electrode; Second electrode; With the current source of the first electrode and the second electrode electric connection; The electrolyte be communicated with the second electrode fluid with the first electrode; Gas, wherein said gas in electrolytic process in the first electrode place or near formation; And separator, wherein said separator comprises inclined surface guides electrolyte and gas flowing with the difference between the combined density due to electrolytical density and electrolyte and gas, and gas is flowed substantially in the second electrode distal direction.
In another embodiment, provide a kind of electrolytic cell, described electrolytic cell comprises: closed housing; First electrode; Second electrode; With the current source of the first electrode and the second electrode electric connection; The electrolyte be communicated with the second electrode fluid with the first electrode; Gas, wherein said gas in electrolytic process in the first electrode place or near formation; Gas extraction region; And separator, wherein said separator comprises the inclined surface of two formation " V " shapes; Wherein said separator due to electrolytical density and electrolyte and gas combined density between difference and guide the flowing of electrolyte and gas, gas is flowed substantially in the second electrode distal direction, and wherein said separator is also constructed to promote electrolyte in the first electrode, circulation between gas extraction region and the second electrode to provide fresh electrolyte to the first electrode and the second electrode.
In still another embodiment, provide a kind of electrolytic cell, described electrolytic cell comprises: closed housing; First electrode; Second electrode; With the current source of the first electrode and the second electrode electric connection; The electrolyte be communicated with the second electrode fluid with the first electrode; Gas, wherein said gas in electrolytic process in the first electrode place or near formation; And separator, wherein said separator comprises inclined surface guides electrolyte and gas flowing with the difference between the combined density due to electrolytical density and electrolyte and gas, and gas is flowed substantially in the second electrode distal direction.
In another embodiment, a kind of electrolytic cell and using method is provided.Although described electrolytic cell can, with in numerous applications, be described as being used in the production of hydrogen and oxygen in the present embodiment.The reversible separation of produced of the hydrogen of pressurization and oxygen is provided and the impurity that runs of tolerance and product according to the electrolytic cell of the present embodiment.The described right to choose embodiments further providing operation electrolytic process, described electrolytic process comprises the steps: to supply to be pressurized to treats dissociation substance than amplitude much lower needed for compact storage, between electrode, apply electromotive force to produce the low fluid product that density ratio is dissociated material, and limit the expansion of the less fluid product of density until reach pressure needed for compact storage.This embodiment and other embodiments by run heat engine or fuel cell and utilize cook from the heat in this kind of source, sterilized water and to other material Transfer heat, space heating is provided or promotes that fuel to improve the energy utilization efficiency of residence Ru Jia, restaurant, hotel, hospital, cannery and other commercial facilitys to the anoxic of this kind of motor or fuel cell or electricity induction release.In addition, it will be understood by those skilled in the art that the aspect of embodiment disclosed herein can be applicable to the electrochemical cell of other types to provide similar advantage.
With depend on that relatively slow diffusion, convection current and concentration gradient process are contrary with the Conventional electrochemical electrode producing required component to produce mass transfer and/or to send ion to a great extent, present embodiment provides more efficient mass transfer, comprise ion fast and supplement process and pump action the sending to required electrode by the low density gas from the liquid medium escape that density is larger as described herein.Which ensure that higher electrical efficiency, to dissociate and higher separation effect faster, prevent undesirable side reaction in addition.Improve the generation of ion and will the current limit value of system effectiveness and every electrode area be improved to the speed of sending of electrode and efficiency.
See Figure 1B, it illustrates wherein container 4b such as metal tube and serve as the electrolytic cell 2b of closed housing.Optionally, container 4b also can serve as electrode, as shown in fig. 1b.Perforated electrode is coaxially located as cylindrical conductive screen electrode 8b and pipe graphite 4b and is held liquid such as acid or alkali and pipe graphite 4b by liquid electrolyte and separates.Liquid electrolyte occupies the inner space of container 4b to the liquid-gas interface in insulator 24b.Can provide in container 4b have plating, the dielectric bushings of layer of electrode material of plasma jet or compound or conduction cylindrical interior backing electrodes 4b'(not shown) to serve as the electric isolution element of assembly, thus make it possible to change easily as Maintenance Significant Items, or of serving as in a large amount of segmented electrode element connects to provide optional polarity and/or series, parallel or series parallel connection.In this reversible embodiment, for the electrolysis of water, electrode 8b can be regarded as electron source or negative electrode, hydrogen is produced at electrode 8b place, and electrode 4b can be regarded as anode, and oxygen is produced at electrode 4b place.Container 4b can pressurize.The pressurization of the content of container 4b is retrained by sealing cover 30b and 46b.Comprise the supporting of the parts of electrode 8b, gas separator 10b and electrical connection 32b, electrical insulation and stabilization to be provided by dielectric insulator 20b and 24b, as shown in the figure.The pressurization of electrolytic cell 2b by gas in electrolytic process generation caused by self-pressurization, realized as pump or by its combination in any by external source.
Separator 10b is constructed to liquid and can pass through but substantially stop gas from the flowing of the anode-side of the negative electrode lateral separator of separator or conveying, and vice versa, comprises and substantially stoping in electrolyte or the flowing of dissolved gases after bubble nucleating.Optionally, electrode 8b can be constructed to serve as separator 10b, makes not need independent separator.Or separator 10b can comprise electrode 8b or electrode 8b can comprise separator 10b.In addition, separator 10b also can comprise anode electrode 4b or anode electrode 4b can comprise separator 10b.
Insulator 24b be made into shown shape and be separated as required, collect and/or extract electrode as 4b and 8b (comprising the utilization of combining with separator 10b) the gas that produces.In shown concentric column geometrical shape, insulator 24b has central conical cavity, and on electrode 8b, the gas of release will be collected in this central conical cavity.What hold this central chamber with one heart is annulus, and the surface of self-electrode 4b' or the gas from the release of the inside of container electrode 4b are collected in described annulus.
Optionally, catalytic filter 48b can be laid as shown in the figure in the upper collection passage of 24b.Comprise cross separator 10b advance and manage to arrive catalytic filter 48b oxygen can with catalytic way by with H-H reaction and cause the formation of water, then described water can return electrolyte.Hydrogen excessive in a large number can serve as the heat affecting electrolytic cell that radiator discharges to suppress this catalytic reaction.Purified hydrogen is in accessory 26b place supply as shown in the figure.Similarly, in the upper area of surrounding annulus collecting oxygen as shown in the figure, may preferably provide catalytic filter 49b any hydrogen arriving this oxygen anchor ring is converted into water.Oxygen is taken away at accessory 22b place as shown in the figure.Or, catalytic filter can be placed in accessory 22b and 26b place, neighbouring or the inside.
In shown operation, if water is the material of hydrogen to be dissociated into and oxygen, then prepare suitable electrolyte as sodium bicarbonate, caustic soda, caustic potoash or sulphur aqueous acid and under remaining on required liquid level by sensor 50b as shown in the figure, sensor 50b tracer liquid pressure and to controller 52b send signal with process pump 40b thus as required from suitable source as reservoir 42b adds water to produce or keep required liquid holdup or pressure.Therefore controller 52b controls sensor 58b to temperature and pressure and responds, sensor 58b can be included in the integrated unit with liquid level sensor 50b or liquid holdup sensor 51b, control pump 36b and 40b and heat exchanger 56b, and wherein heat exchanger 56b can comprise circulating pump system if radiator or heater (not shown) are to receive or to transmit heat.Similarly, heating or cooling fan can be adopted to strengthen heat certainly with reception or the discharge in the source of electrolytic cell 2b in conjunction with such operation.
In some embodiments of electrolytic cell 2b application to be recycled wherein, such as, when the electricity of surplus is cheap in when not needing in addition, the water holding capacity of electrolytic cell 2b can be made to have and alternatively to run quite greatly.When electric non-availability or its shutoff of surplus, the supply of hydrogen and oxygen can be extracted from container 4b and allow system get back to external pressure.The water that then can add external pressure fills material to make system, system can be made around insulator 24b to have large annular volume, this is for promoting that the low pressure of such circulation is filled and electrolysis procedure, and to send under realizing the conversion to merit of pressure or chemical energy, compact storage and providing the high pressure needed for the fast transfer to vehicle, instrument or utensil receiver, hydrogen or oxygen may need.
At applying electric current after much smaller liquid holdup generates a large amount of hydrogen and oxygen, can pressurize to system as required and keep pressurization until detection that water holding in solution is exhausted into sensor 50b or the 51b point that makes controller 52b or interruption electrolysis cycle or add water from reservoir 42b as illustrated by pressure pump 40b.May preferably through valve as shown stop valve 44b add water, to realize multiple quantity delivered or the maintenance of pump 40b as required.
See Figure 1B, 2B and 3B, Fig. 2 B shows an embodiment of the separator 10b of Figure 1B, and wherein said separator comprises the inclined surface 14b of two formation " V " shapes.If electrolyte is based on water, then electronics is added to perforated electrode 8b as weaved silk screen cylinder and taking constantly hydrogen ion is converted into hydrogen atom and diatomic molecule subsequently by electric connection 6b away from container 4b by joint 32b, described diatomic molecule can on electrode 8b or near nucleation to form bubble.The electrolytical density that hydrogen and oxygen bubbles can not show a candle to usually based on water is large, therefore will be up under buoyancy-driven.Oxygen bubbles is drive up similarly and is separated with hydrogen by the geometrical shape of coaxial separator 10b, and coaxial separator 10b is shown in the amplification sectional view of Fig. 2 B.Shown in Fig. 2 B, structure can be used in any application of the gas flow wherein needing to be formed in the running of electrolytic cell 2b.In addition, described separator construction can be used in other electrochemical cells known in the art structure.Or, if the density of material formed in electrolytic process is larger than electrolyte, then separator 10b can be allowed to overturn and to form " Λ " shape.Similarly, if a kind of density of material formed at negative electrode place by electrolysis is less and another density of material that is that formed at anode place is larger than electrolyte than electrolyte, then can make separator 10b by the "/" tilted or " " the shape material-deflecting that forms to make density less is away from the larger material of density.
The hydrogen discharged from 40' or container 4b inside and the mixing of oxygen are by the permeable barrier of liquid---separator 10b is stoped, as shown in the figure, separator 10b is by deflecting oxygen from surperficial 12b' and 14b tilted and hydrogen prevents it from entering, flows or transmit and divided gas flow efficiently.Or, separator 10b can comprise by electric insulated conductor or the helix that forms from the ethylene-chlorinated of inertia dielectric material as filled 30% glass, the cross section of wherein said helix shaped strip material is " V " shape structure, as shown in the figure, to serve as Electric insulator and gas separator.
The path supplying fluid to advance can increase the needs meeting fluid circulation and distribute on demand, way is once in a while or continuously corrugated band, particularly in each edge, to produce gap between each helical layer line, or at the stacking place of formed dish, cross section shown in described dish pie graph 2B, in sectional view, 13b place shows the ripple of amplification.Usually advantageously, the ripple making each such rises and falls around the radial axle (as shown in the figure about axle 15b and 15b') suitably tilted more or less.The liquid of formed separator 10b can be made to can pass through for this but gas is required thickness by the wall total thickness stopped, such as (0.008 ") is thick or less for about 0.2mm.
Separator 10b can have any suitable size, comprises very little size, and with regard to surface energy situation, be enough to allow liquid electrolyte to be transmitted to or pass ionization electrode 8b but because of gas buoyancy-driven and upwards advance and do not allow passing through of gas.Provide a kind of alternative embodiment be applicable in such as relatively little fuel cell and electrolyser, way is to provide the flat wire with cross section shown in Fig. 2 B of a large amount of tight spacing, and wherein such line is woven or adheres to provides the entrance of the main opening of liquid and the line be arranged on the one or both sides of " V " shape line on mainly vertical direction.The liquid of formed separator 10b can be made to can pass through for this but gas is that (0.004 ") is thick or less for about 0.1mm by the wall total thickness stopped.
Buoyancy-driven upwards makes to collide the bubble deflection direction on inclined surface 12b and 14b.This feature will overcome the problem of the conventional method of prior art, and these conventional methods cause poor efficiency because of one or more in resistance, fouling, viscous flow, corrosion and polarization loss.In addition, buoyancy pumping action due to rising bubble produces electrolysis the upwards flowing of matter, therefore some structures may promote the circulation of electrolyte in concentric layer, and escape at liquid top place along with gas, relatively without gas and the larger electrolyte of density will flow to bottom thus recirculation to substitute the electrolyte of the less density being mixed with bubble or containing dissolved gases.Heat exchanger 56b can run as required with since container 4b electrolyte from top to bottom cycle heating or remove heat, as shown in the figure.Pump 36b can use the speed improving electrolyte circulation as required, or pump 36b can be combined to add supplementing water with pump 40b.
Be applied with high current density in some embodiments, comprise the system of adding organic material fast.In such embodiments, may be favourable by pump 36b cyclic electrolysis matter, as shown in the figure, the relative gasless electrolyte arriving pump 36b by accessory 28b and pipeline 34b be turned back to container 4b by pipeline 38b and accessory 16b by described pump 36.Preferably may enter the electrolyte returning 0000000 tangentially to send to produce eddy flow at accessory 16b place, this eddy flow continues to swirl and therefore strengthens separation synergistically, comprises the effect of the separator 10b by utilizing as mentioned above.Depend on the pressure of operation, the density ratio oxygen of hydrogen little about 14 times and there is larger buoyancy and tend to be easy to separated device 10b guide have higher upward velocity with by filter 48b at accessory 26b place pressurized collection.When very high current density and electrolytic cell 2b are subjected to the inclination or G-power that may meet with in as transport applications, improve the electrolyte speed of advancing with the gas and vapor permeation that the gas strengthening cyclonic separation and also therefore prevent from anode produces and negative electrode produce by pump 36b.
Some comprise the embodiment of the on-conductive gas barrier of separator 10b and fluid transport embodiment and make it possible to manufacture than previous method considerably cheaper and firm and much efficient reversible electrolysis device, and previous method comprises and relies on PEM to carry out divided gas flow as those of hydrogen and oxygen.In one aspect, separator 10b can be designed to improve electrolytical flowing in electrolytic process.Such as, separator 10b can be constructed to promote that ion is held in liquid from the helical flow that port one 6b upwards advances to port 28b at liquid electrolyte.This will guarantee that the various piece of electrode receives the ion density of fresh supplemented, and this obtains required for maximum electrical efficiency.Along with hydrogen and oxygen are formed in the respective electrode of electrochemical cell, such electrode washing action also can remove the bubble of hydrogen and oxygen fast.
Fig. 3 B shows the edge view of the component plate of the another aspect of separator 10b or the representative part of helical strips, it, for providing the electrical insulation of adjacent electrode (comprising dull and stereotyped and coaxal electrode structure), obtains the separation of gaseous matter described above simultaneously.In assembly 11b, plate 12b' with 14b' is formed similar to separator 10b and as the cross section of the such function of separator 10b.Flat conduction or non-conductive polymer plate 12b' are made for has a large amount of aperture on parallel center line, and this some holes tilts such as, for forming such as about 35 ° of substantive angles to 70 ° of angles, as shown in first jiao of 15b with the major axis of plate 12b' as shown in the figure.Polymer sheet 14b' is made for similarly has a large amount of aperture on parallel center line, and this some holes tilts in fact for forming the angle of about 35 ° to 70 °, as shown in second jiao of 15b' with the major axis of plate 14b' as shown in the figure.
In other embodiments, angle 15b and 15b' can be different with material to be separated in electrolytic process.Such as, for the electrolysis without gas component or only a kind of compound of gas component, described angle can have a down dip.If electrolytic dissociation compound is as Al in cryolite-alumina electrolyte 2o 3to form aluminium and oxygen, then the density ratio cryolite-alumina due to aluminium is greatly electrolytical, therefore aluminium is separated cathode electrode or relevant separator should be constructed (angle by such as having a down dip) for sending aluminium downwards and away from the oxygen of upwards advancing.
A large amount of diameter is that this kind of aperture of about 1/12 to 1/3 of sheet thickness dimension can comprise laser boring, the perforation of hot pin or penetrate in plate 12b' and 14b' obtained by high velocity particle easily through suitable technology.Separately usually thick about 0.025 to 0.25mm (0.001 " to 0.10 ") plate 12b' and 14b' by welding or bonding, linear system, elastic ribbon or on produced external diameter spiral winding one or more to conduct electricity or non-conductive silk is fixed together the assembly that is formed as comprising electrode 8b.Plate 12b' and 14b' can also combine once in a while or continually by tackiness agent or by thermal fusion welding or solvent welding.Therefore, overlap part at the slope hole of plate 12b' and the hole of plate 14b', will the path that liquid and/or electrolyte can be advanced be formed, and stop gas transport to pass through formed gas shield film simultaneously.See Figure 1B and 4B, for embodiment 2b or 100b, can by adhering to or butt welding seam or there is the gas shield board component of the tubular structure of proper diameter by providing the overlapping the slot as the barrier being intended to divided gas flow to be formed.
For the electrolysis of water, there is multiple suitable electrolyte.Can use caustic potoash in one embodiment, closed housing 4b adopts low carbon steel.Can with nickel plating cylinder 4b or by utilizing suitable Stainless Steel Alloy to provide longer life-span and the corrosion resistance of Geng Gao.In other respects, can pass through with high strength reinforcing material as glass, pottery or carbon filament or its combination hold cylinder 4b and provide higher sealing ability.
Depend on specific application and intensity needs, use the ethylene-chlorinated being filled with about 30% glass may be favourable to insulated separation device 20b and 24b.Electrode 8b can be made up of woven nickel or 316 type Stainless Steel Wires.Separator 10b can be made up of the ethylene-chlorinated band being filled with about 30% glass.
In another embodiment, the controlled applying of electricity is also intended to utilize to produce methane or hydrogen respectively or with the preferred mixture of organic bath.In some respects, this embodiment can with comprise sequence number 09/969,860 run in combination in the embodiment of interior co-pending Patent application, and this patent application is incorporated herein by reference.The anoxic digestion process of the organic material of usual generation methane can through controlling to produce the electrolyte that discharge hydrogen under voltage much lower needed for dissociate water, or will lack needed for pulse width modulation duty cycle on time and the electric consumption ratio dissociate water that produces.
The acidity of the organic solution that microbial digestion produces or pH can be interacted by natural buffered with bicarbonate and keep.Bicarbonate buffer can be supplemented by the common generation of carbon dioxide in digestion process.For the multiple steps in the anoxic digestion process of organic compound, this process can be concluded with the exemplary digestion of simple carbohydrate or grape sugar, this exemplary digestion may have the process steps of many emulative and complementarities as:
C 6h 12o 6+ (anoxic acidifier, facultative bacteria) → CH 3cOOH equation 1
CH 3cOOH+NH 4hC 6o 3→ CH 3cOONH 4+ H 2o+CO 2equation 2
3CH 3cOONH 4+ 3H 2o (bacterium) → 3CH 4+ 3NH 4hCO 3equation 3
When needing the methane from this kind of solution, pH may be needed to control near 7.0.Under pH and 35-37 DEG C (99 °F) of external pressure, about 7.0, methane generation will be conducive to.Most of domestic sewage contains the bio-waste in a large number and both micronutrient required for organism having and provide methane generation.In anoxic reacter, keep the concentration of relatively large dissolving and the distribution concentration of hydrogen or the monose of existence can suppress the work of methanogen.
On the other hand, the material being decomposed with the bacterium of other organic compounds by grape sugar and produced by other acid processes can be made as acetic acid (CH by applying electric field 3cOOH) dissociate to increase the production of fuel value from organic substance, the wherein said generation hydrogen ion that dissociates.
CH 3cOOH → CH 3cOO -+ H +equation 4
Hydrogen ions or be delivered to electronegative electrode and obtain electronics and produce hydrogen.
2H ++ 2e -→ H 2equation 5
Electronegative electrode supplies two electronics.At another electrode place, electrochemical reaction comprises the oxidation of acetate ion to produce carbon dioxide and hydrogen ion, as equation 6 summarize.
CH 3cOO -+ 2H 2o → 2CO 2+ 7H ++ electronic formula 6
In this electrode reaction, acetate ion loses electronics, reacts subsequently and be decomposed into carbon dioxide and hydrogen ion with water.Carbon dioxide makes solution saturated and from liquid solution sediment-water interface release, as described in embodiment above.Hydrogen ion cycle and/or migration are until electronics is received and produce hydrogen atom and then diatomic molecule, as institute in equation 5 summarizes, with separately common collection in such a system from opposite electrode.Separate collection is highly favourable, such as, separate collection to make the result as liquid pumping instead of gas compression obtain pressurization or will be especially effective under being in high pressure, and be separated greatly reducing and fixed equipment that then hydrogen, methane or the carbon dioxide that produce of mechanical compress is usually required.
Much less is wanted in the electrolysis of compound as the energy Ratios water that acetic acid is produced required for hydrogen and carbon dioxide by anoxic digest and decompose, and part is because digest and decompose produces hydrogen ion and heat release energy.Acid as the starting of the exothermic decomposition of acetic acid and keep can under lower voltage applies or by interval or electrolysis once in a while instead of as decomposition water usually needed for continuous electrolysis realization.Quite large (at least 1KWH=3 of the free energy of formation of water under ambient temperature, 412BTU releases hydrogen), by contrast, digester material needs relative minimum activation and/or catalysis as urea and acetic acid are electrolyzed to produce hydrogen with carbon dioxide with acid, when particularly using organic catalyst.Therefore, use selected catalyzer to comprise to select in the Raney-Nickel catalyzer of modification, nickel-Xi-aluminum alloy, platinum race in conjunction with described electrode system herein, platinum-nickel and other platinum-transition metal single crystal alloys surface and various organic catalyst will improve the speed and/or efficiency that hydrogen produces further.
On the other hand, may preferably utilize numerous battery, switchably serial or parallel connection or the series parallel connection of its electrode pair such as, to mate available source amperage and voltage and to be dissociated required voltage by series-connected cell, shown in Figure 1B.In of this embodiment, depend on aqueous electrolyte that is selected or that produce in biochemistry mode from organic substance, each battery may need about 0.2 to 2 volt, therefore 6 of a house-hold size volts of photovoltaic sources can have 3 to 30 batteries of connecting, and the industrial source of 220 volts can have about 100 to 1,000 electrode battery be connected in series.Gas product can easily through in parallel or be connected in series layout and send.Depend on the required flexibility regulating the quantity of connecting and/or being connected in parallel, supporting and flow control features 18b can be selected from insulation or non-insulating material.
Under various current density, under being included in medium and low current density, may preferably allow the buoyancy-driven of generated bubble to realize electrolytical circulation to prevent ion from exhausting and viscous flow problem.When starting or under higher current density, can process pump 36b and heat exchanger 56b to provide required running temperature and to provide the electrolyte of rich ion at electrode surface place.This makes to realize extra high Conversion of Energy speed, wherein the trough-electricity of energy as obtained from the sun, wind, overboard or wave resource be used to fast and the high voltage supply producing oxygen and hydrogen or hydrogen and carbon dioxide or hydrogen and methane and carbon dioxide efficiently separately to store and to use.
In of this embodiment, the large energy solving outburst suddenly in vehicle regenerative braking or power plant's stall must be rapidly converted into the problem of chemical fuel potential energy.The conventional fuel cells advanced for truck, bus or train can not tolerate the high current density be applied to suddenly on fuel cell electrode.The present embodiment overcomes this restriction and provides high current conditions tolerance strong especially, obtain simultaneously high electrolytic efficiency and without reproducibility PEM fuel cell meet with PEM degenerate or electrode interface lost efficacy problem.Due to firm in structure and there is Coolers meeting especially fully, therefore the operation under being easy to adapt to extra high electric current.The present embodiment is easy to start and runs efficiently under harsh cold or tropical conditions and without the relevant all difficulties of PEM, restriction and inefficacy conversely speaking.
On the other hand, for obtaining much higher investment return in energy conversion system is as hydroelectric power plant, wind energy turbine set, Wave power generator systems or conventional power plant, the present embodiment allows trough-electricity dissociating fast and being converted into hydrogen and oxygen efficiently or the dissociating fast and be converted into hydrogen and carbon dioxide efficiently of the material that generated by the anoxic digestion of organic substance or degrade by water.The space that the compact pattern of the present embodiment occupies can unlike washing machine large and by otherwise the trough-electricity that may be wasted be converted into the hydrogen of enough operation two family expenses size vehicles and the energy demand of house be provided.
As mentioned above, some embodiments provided herein will provide more efficient mass transfer, comprise pumping action the sending to required electrode that fast ionic supplements process and passes through the low density gas of escaping from the liquid medium of greater density.This, by guaranteeing higher electrical efficiency, dissociating and higher separation effect faster, stops undesirable side reaction in addition.Improve the generation of ion and will the current limit value of system effectiveness and every electrode area be improved to the speed of sending of electrode and efficiency.Application organic substance being converted into carbon dioxide and hydrogen or methane is special benefit because of following reason: organic substance improves to the delivery rate of the microorganism participating in this process, hatch speed and the microorganism after hatching to the long lifetime and the transmission rate of self repair bioflim media improve, the gas produced obtains being separated sooner, organic substance obtains transmitting sooner, in addition, intermediate ionic is more efficient to the transmission of electrode.
See Fig. 4 B, illustrated therein is another embodiment---electrolytic cell 100b, do not wish wherein apply voltage or do not wish that electric current is in the application of the inwall of closed housing 102b, this electrolytic cell 100b is advantageous particularly.The present embodiment also by promote bipolar in electrolytic cell 100b or multi-electrode group or battery as 110b and 114b be connected in series simplify gas collection and voltage matches needs.
Closed housing 102b is the concentric aspects of cylindrical and in it parts wherein, and electrode assemblie 110b and 114b can be formed from numerous nesting type truncated-cone element or one or two electrode can be formed as screw electrode described above.Electrode 110b with 114b can have identical, similar or different structures.On the other hand, electrode 114b can be able to be the spiral electrode of surrounding electric poles 110b continuously from the assembling of nested frustoconical part or its.
For preventing short circuit, the electrically separated of electrode 110b and 114b can be realized by many kinds of measures, comprises by controlled operation tolerance of size and/or by using the line of dielectric that is placed between electrode 110b and 114b or long filament and/or realizing as separator 10b or 111b by another form disclosed in about Fig. 2 B and 5B.
Electrolytic cell 100b can be pressurized.Pressure-tight is provided by upper cover and lower cover 104b and 106b, as shown in the figure.Insulator 120b and 122b supports by covering 104b and 106b, as shown in the figure.For to be electrically connected the circuit block that is connected with fluid and hardware be exemplary and can realize by penetrating lid 104b and 106b to meet concrete application needs as required.
In the present embodiment, two electrode 110b and 114b are all formed as having inclined surface, and gas such as discharged for produced material guides to corresponding collecting area by described inclined surface, as shown in the figure.Exemplarily, if from suitable electrolyte dissociate water, then electrode 110b can receive the electronics supplied by joint 108b, and joint 108b is sealed in lid 106b by plug for seal part 132b.Therefore electronics is taken away by plug for seal part 130b self-electrode 114b, and plug for seal part 130b provides when gas is as the insulation of point of contact 124b when carbon dioxide or oxygen discharge on electrode 114b.
Therefore such gas advanced by buoyancy and inwall more or less upwards and along container 102b after being sent by electrode 114b is advanced.Hydrogen after being sent by electrode 110b at numerous circle or conial layer electrode 110b boost in the central cores that formed and collect at insulator 120b place as shown in the figure.The purified hydrogen be under design pressure is sent by pressure fittings 116b.Catalytic filter 134b can be used transform any oxygenant arriving central cores if oxygen is to form water.Similar catalytic filter material can be used to produce water from any hydrogen of the outer collection anchor ring arrived in insulator 120b as shown in the figure.Pressurization and filtered oxygen sent by pressure fittings 118b.
Optionally, for improving the efficiency of electrolytic cell 100b, one or more gas collection vessel (not shown) can be made to be communicated with to collect the gas formed in electrolytic process with electrolytic cell 100b fluid.Gas collection vessel can be implemented with the gas trapped before the substance expansion of gas under high pressure.Gas collection vessel can also be configured to captured gas expansion time institute's work by methods known in the art.Or gas collection vessel can be configured to provide the gas under the pressure being in and being suitable for storing, transport or using, and wherein said gas needs under high pressure to send.Also expect that described aspect can be implemented in various electrochemical cell.
See Fig. 2 B, on the other hand, can accessory 22b, accessory 26b part, near or the inside or introduce gas expander in the gas collection vessel be communicated with accessory 22b or accessory 26b fluid.Similarly, see Fig. 4 B, can accessory 116b, 118b part, near or the inside or introduce gas expander in the gas collection vessel be communicated with accessory 116b or accessory 118b fluid.
On the other hand, provide a kind of electrolytic method and device of pressure fluid, described fluid is connected with the device extracting merit from such pressure fluid.Described fluid can be the liquid of pressurization, the gas absorbing liquid, steam or gas.Pressure fluid can carry out to the conversion of steam or gas among accessory 116b or afterwards, for can being selected from turbine, generator, vane motor or various Armstrong motor or " breathing " air from the device of such accessory transfer pressure and flowing and injecting the motor of pressurized hydrogen from 116b.Similarly, pressure fluid can carry out to the conversion of steam or gas among accessory 118b or afterwards, for being selected from turbine, generator, vane motor or various Armstrong motor or expansion and/or burning pressure fluid from the device of such accessory transfer pressure and flowing as the motor of the oxygen from 118b.
On the other hand, provide and a kind ofly overcome the high cost of transformer and rectifier circuit and the apparatus and method of power loss.This to be mated with the adjustment of source voltage by load voltage and realizes, what described adjustment fitted through electrode in electrode battery or battery is connected in series realization, such as the negative polarity in DC source is connected to successively nethermost three circle electrode 110b, to ensuing three circle electrode 114b, to ensuing three circle electrode 110b, to ensuing three circle electrode 114b, arrive ensuing three circle electrode 110b again and from contrary (the highest) end, the positive conductor from DC source be connected to three circle electrode 114b successively, to ensuing three circle electrode 110b, to ensuing three circle electrode 114b, to ensuing three circle electrode 110b, arrive ensuing three circle electrode 114b again.The number of turn of truncated cone and/or stacking number can be regulated to produce the area needed for the amperage of coupling source.
In the another aspect of the present embodiment, except the separation of the gas produced except providing electrolysis, the pumping action that embodiments more of the present invention produce also provides nutrient sending to microorganism, depend on the relative scale of operation, these microorganisms live with suitable medium as in carbon cloth, activated carbon granule, expansion silica, graphite felt, coal, charcoal, fruit stone, wood chip, shredded paper, sawdust and/or its mixture, in the part that these media are usually located at electrode 110b and/or between the part of electrode 114b and container 102b.Corresponding function and benefit comprise the thermostabilization of system, the circulation of raw material, product as carbon dioxide pipette and hydrogen from the production of the acid that can produce by the hatching of this kind of microorganism, nutrition and growth.
Low with under moderate electric current densities, the buoyancy that low density solution and bubble cause can make electrolyte at container 102b Inner eycle.Under higher current density, advantageously control electrolytical temperature, pressure and circulation adaptively as previously disclosed.Electrolytical outer circulation can from accessory 126b to accessory 138b, as shown in the figure, and comprises wherein container 102b and includes one or numerous optionally to connect and/or the situation of electrode battery that series-parallel circuit connects.
On the other hand, the present embodiment can be optimized for high current density, to transmit proportionately higher fluid electrolyte flow rate by one or more hole or groove 139b, described hole or the annular space between groove 139b and electrode 110b and 114b tangentially guide fluid.Electrolyte upwards flow along the spirality space that electrode is formed and by from the annular space between 110b and 114b by 110b and 114b provide enter the electrolyte of spirality path supplement.The electrolytical moment of momentum entering the space between electrode 110b and 114b by increase the bubble of electrolysate as the hydrogen produced on electrode 110b and 114b respectively and oxygen rise suction Driving force and on momentum being added to.
For guarantee to self-electrode 110b and 114b exchange charge after become hydrogen and oxygen atom or other gas as the rapid recharge of the ion of carbon dioxide and for pipetting this kind of gas to collect and to remove and make the electric polarization loss in electrolytic process minimum simultaneously, this electrolyte circulation height is favourable.Therefore be easy to accept very high current density with the fluid of electrolysis cycle efficiently.On the other hand, the further adaptation of high current density is provided, the reduction that the electrolyte circulation of described improvement will prevent harmful viscous flow of electrolysate and/or phase transformation as water vapor nucleation and effective electrode area by the huge cooling capacity of the design caused by the electrolyte circulation because improving.
On the other hand, electrode 110b and 114b can form form of springs, described form of springs can advantageously be run or at the resonant frequency fx by various inducement disturbance, such inducement comprises the acceleration thrust of less density mixture of piezoelectric driver, the eccentric wheel of rotation, effect that bubble is formed and electrolyte and bubble, because the electrolyte of higher density holds liquid will be delivered to the surface of electrode 110b and 114b under produced pumping action.Response storm, electrode 110b and 114b by with natural frequency or the frequency vibration of inducing to strengthen bubble further from the removing and therefore make to obtain higher current density and the energy conversion efficiency of Geng Gao of surface comprising nucleation site.
Electrode such as the induced vibration of 110b and 114b of spiral spring form can also cause inchworm effect, thus strengthens bubble to the corresponding collection path of electrolytic cell 100b and the acceleration leaving port.In this vibration processes, the periodicity of the average distance between the adjacent layer of electrode circle and angle increases and reduces to produce node that is fixing or that advance, and this depends on amplitude and the frequency of inducement.
Fig. 5 B shows the representative section figure being combined one group of electrode 110b' and 114b' run for the electrical insulation Spacer 111b between electrode 110b' and 114b', and electrical insulation Spacer 111b comprises selection as shown in Figure 2 B for multiple application with electrolytically comprise the insulator 10b that helical flow sends structure.The assembly of concentric electrode 110b', Spacer 111b and electrode 114b' will provide very firm self intensification system to realize fluid as water, from the liquid of anoxic digester or efficiently dissociating of seawater with the efficiency improved and resistance to fouling tendency.Electrode 110b' and 114b' can from conductive carbon paper, cloth or felt; Carbon weaven goods or carbon felt and metal filament, be clipped in graphite granule between carbon weaven goods or metal filament; Or the polymer of plating or metal slabs are as mild steel, nickel plating steel or stainless steel structure, it is more or less drilled with a large amount of holes on parallel center line as previously described, this some holes tilts correspondingly be separated hydrogen from common gas such as oxygen, chlorine or the carbon dioxide produced as shown in the figure, and the gas of described common generation depends on electrolytical chemical component.
At electrode 110b', Spacer 111b and electrode 114b' with coaxal electrode arranges employing as shown in Figure 4 B, hydrogen is delivered to port one 16b, and depends on the material dissociated, and product such as oxygen, chlorine or carbon dioxide are delivered to port one 18b.In some cases, preferably in 110b' and 114b', provide a large amount of holes, the aperture in each hole is slightly conically increased to the exit surface away from Spacer 111b from the surface of contact interval thing 111b.
Preferred selection screw pitch, interelectrode width and the thickness of band forming Spacer 111b make with available electric energy and system heat transfer need the speed that matches from 138b to and send electrolyte by electrode 110b' and 114b' to accessory 126b, to optimize interelectrode gained width spaces.This makes there be sending of the abundant ion for electrolytic process at electrode 110b' and 114b' place, guarantee that hydrogen is separated to the district in electrode 110b', and the gas jointly produced such as oxygen, carbon dioxide or chlorine is delivered to the space outside electrode 114b' simultaneously.
On the other hand, can by providing gas flow groove in hydrogen electrode, provide gas flow groove in oxygen electrode, being provided for the appropriate fittings of the bottom hydrogenation to hydrogen electrode and the bottom place oxygenation at oxygen electrode in addition and running described system with regenerating.In this case, maybe advantageously adopt form concentric spirals shape electrode, particularly namely single canister assembly meets in the little fuel cell of energy demand wherein.
See Fig. 6 B, illustrated therein is the cross section for the spiral electrode in reversible fuel cell operation situation.Electrode 110b for electrode 114b or similar spiral pattern is provided the improvement of surface/volume, section modulus and column stability by this.Electrode 114b is illustrated in this sectional view, wherein, gas 152b flows along spiral groove, described spiral groove is formed by corrugated bar made-up belt, and described bar made-up belt is used for forming spiral and providing sending of oxygen for fuel battery operation and send oxygen to anchor ring 136b and accessory 118b in electrolysis procedure.For the electrode 110b under fuel cell and electrolysis mode, same structure is also applicable to be converted into by organic acid carbon dioxide and hydrogen under electrolysis mode and guarantees that a large amount of gas is delivered to required collection or source port as previously mentioned.
On the other hand, by promoting the moisture derivative of organic substance as carbonic acid, acetic acid, butyric acid and lactic acid and compound if Urea Transformation is the electrode performance that the microbial growth of hydrogen and maintenance provide improvement.Selected for generation of on the electrode of hydrogen ion and/or release of carbon dioxide, micro-organisms rate is improved by this kind of electrode surface being made for the pattern enhancing had increasing effective surface area, wherein said pattern strengthens the long filament or the whisker that comprise high aspect ratio, in position together with the membrane substance resistance helping that such long filament or whisker will reduce matrix electrode provides microorganism and biomembrane with digestion process needed for.
Not by theoretical restriction, it is believed that the special characteristic of electrode and/or separator such as pattern process or enhancing can by the electrolytical turbulent flows in promotion desired location place, comprise cavitation or supercavitation, it promotes the nucleation of this position then.Otherwise the particular configuration of electrode and/or separator can suppress the turbulent flow at the some place of desired location such as electro transfer, and comprise cavitation or supercavitation, it suppresses the nucleation of this position then.Expection, the element comprising these features can need any position of nucleation to implement in electrolytic cell.In addition, these identical characteristic sum principles can be applied to gas collection vessel or the similar container that is communicated with electrolytic cell fluid or the container be communicated with passage therebetween or valve fluid.
Suitable long filament and/or whisker comprise metal or doped semiconductor as the nanometer diameter long filament of carbon, silicon or carbonitride or boron nitride providing the surface area of increase, reduce ion transport loss and resistance loss, raising micro-organisms rate and make nucleation more effective in more efficiently release of carbon dioxide.Such long filament also can be used to grappling graphite granule, and this will improve micro-organisms rate, raising enzyme and catalyst use efficiency further and be conducive to hydrogen ion production process.Similarly, hydrogen ion is provided to electronics and produces hydrogen atom and the electrode place of the bubble of nucleation formation diatomic hydrogen wherein, and long filament and whisker can be utilized to the voltage increasing useful area and reduce needed for whole process.
Except carbon whisker, it has also been found that from metal as tin, zinc, nickel and from the growth of the refractory metal of vapor deposition or from suitable substrate if the long filament of the coating growth on iron electrode is by the process efficiency of the resistance and raising that provide reduction.This kind of long filament or whisker can be made for by following manner and be more suitable for biomembrane supporting and process enhancing: the overlay coating adding useful surface active agent and/or pass through sputtering with suitable material as carbon, boron nitride or silicon carbide or deposit as the decomposition of the carbon donor from exemplary precursors (as acetylene, benzene or the alkane gas comprising methane, ethane, propane and butane) from material.
The favourable separation of the low density gaseous state derivative that the embodiment of Fig. 4 B and modification thereof can provide fluid to dissociate, comprise hydrogen from organic liquid as in equation 1-6 summarize be separated, to send the mixture of hydrogen or rich hydrogen to port one 16b, and carbon dioxide or carbon dioxide enriched mixture (comprising fixed nitrogen component) are delivered to port one 18b.In some applications, may expect that the polarity putting upside down these electrodes is to put upside down the delivery port separating gas.Putting upside down like this can be long-term or interval, to reach various object.Depend on the fluid relative speed at the selection of the screw pitch of electrode 110b and 114b and the resonant frequency of each electrode or forced vibration frequency and each electrode place, hydrogen can be delivered to port one 16b and system and can operate to and comprise methane and carbon dioxide.But the carbon dioxide being delivered to port one 18b may comprise methane and the color density gas higher than hydrogen.Needing to provide the Hy-Boost mixture of hydrogen and methane to make in the application of the run unthrottled realizing internal-combustion engine, various burner, stove or fuel cell, there is hydraulic pressure and will facilitate following selection with Fig. 4 B embodiment that control circui measure (such as provided with controller 52b by pump 36b) runs: with controlled hydrogen and methane ratio produce be separated needed for fuel mixture and send at port one 16b.
By adding medium as colloidal carbon, carbon filament (comprising nanostructured), stratiform carbon crystal, grapheme platelet crystalline substance, active carbon, zeolite, pottery and/or boron nitride particle in electrochemical cell, provide a kind of unexpected but scheme of powerful anaerobism bacterium colony of particularly advantageous generation microorganism, described microorganism produces Organic Ingredients and transforms needed for hydrogen and/or methane.This kind of medium can be doped or composite with various reagent, to provide the catalytic production rate of enhancing.Exemplarily, can by providing the functional of expectation with the selected reagent more or less with electronic structure as boron, nitrogen, manganese, sulphur, arsenic, selenium, silicon, tellurium and/or phosphor doping.The circulation that causes of gas of electrolytic process release can promote that this kind of medium is to the coordination (sorting) of vantage point and density, thus realizes more efficient electric charge and fluently use.
Not particularly limited by theory, but according to conjecture, the increase of such synergistic results and surface area in critical localisation and stringer, region or long filament increase relevant, described stringer, region or long filament are strengthened nucleation process and/or are carried out the favourable absorption in biomembrane and gained reaction zone of electronics or hydrogen ion and enzyme, hydrogen, methane or carbon dioxide.Also show, in various embodiment disclosed by the invention, microorganism hatched to be recycled in the operation carried out and the position that is efficiently utilized in the flow path that produces.
Except whisker and long filament as carbon, graphite, various metal carbide and silicon carbide and other carry except high performance inorganic substances and particle with catalytic way, adopt and provide required nutrient or catalyzer will to be also favourable with the active substance of auxiliary microbial process and particle.Exemplarily, the porous of polymer, pottery or active carbon and/or the adsorbable electric conductivity organic catalyst of stratiform base material are as tetramethoxy phenyl Cobalt Porphyrin (CoTMPP) or poly-(3,4-Ethylenedioxy Thiophene) (PEDOT) and/or the ground orientation and other catalytic species are provided that plays a driving role, comprise enzyme and graft polymer, other catalytic species described also can be used to introduce and provide catalytic specie, comprise other enzyme.
Suitable material or graft polymer can comprise conventional dendrimers, fiber configuration body and other organic functional materials those to reduce to greatest extent or the catalyzer of alternative platinum and other costlinesses and conductor.The segmentation position that this kind of substitute materials and utilization thereof comprise mixture or circulate relative to the fluid that embodiments more disclosed herein produce.Multiple special conduction and/or catalytic structure comprise can grow or adhere to electrode 4b, 8b, 110b or 114b and/or with coated carbon felt or weaving structure or the needle-like sediments be distributed in Biofilm Colonization and fiber.Exemplarily, conduction and/or catalysis are by keep and to provide hydrogenase and other enzymes, CoTMPP and/or other catalyzer as poly-(3,4-Ethylenedioxy Thiophene) long filament of (PEDOT) provides as fiber, and described long filament synthesizes nanofiber more than 100 of self-organization, thin diameter, aspect ratio from aqueous surfactant solution and provides low charge-conduction resistance.Synthesis in the aqueous solution comprising anionic (SDS) can be suitable for the concentration by changing SDS and pass through in addition to add FeCl 3(a kind of exemplary program is shown in people such as being set forth in Moon Gyu Han to produce various configuration with the structure producing polymerization, Facile Synthesis of Poly (3,4-ethylenedioxythiophene) (PEDOT) Nanofibers from an Aqueous Surfactant Solution, Small 2, No.10, in 1164-69 (2006), it is incorporated herein by reference).Other examples comprise functional catalyzer and the micro-conductor in nano composite material form, described nano composite material is derived from cellulose nano-fibrous and semiconductive conjugated polymer, and described semiconductive conjugated polymer comprises the polyaniline (PANI) and poly-(p-phenylacetylene) (PPE) derivative with quaternary ammonium pendent.Can will have the cellulose of anion form surface charge, carbon or ceramic whisker and positively charged conjugated polymer combines to form stable dispersion, such dispersion can from polar solvent as formic acid solution curtain coating.
Preparation comprises the application of graft polymer and organic metal alkoxide, the end group of metal alkyl and the catalysis benefit of acetic acid and the polyalcohol catalyst containing COOH end group.Except the mixture of end group, special sense and difunctionality end group can also be selected to produce multi-functional characteristic, comprise catalysis, active stabilizer, grafting agent and diffuse-aggregate promoter.Similarly, the special activation of the hydrogen that produced by anoxic Institute of Micro-biology of carbon or other materials and/or enzyme will be provided the environment of the rich hydrogen in local with the generation of enhancer or inhibitor methane and strengthen the additional generation of hydrogen from various organic substance.
See Figure 1B-3B, optionally, it may be favourable for providing the felt of one or more supplementary carbon filament to the outer and inner surface of cylindrical parts 8b, 10b, 11b, 110b and/or 114b and/or weave screen cloth.Supplementary felt like this and/or weave screen cloth and proportionately can collect together with electrode 4b, 8b, 110b and/or 114b and/or separator 10b or 11b or distribute electronics and help grappling or preferentially settle particle, long filament and/or other structures, to reduce the pressure loss or dispense liquid stream and promote that microorganism is in the operating function of required Conversion of Energy more equably.
In the complementarity of the clean production for providing hydrogen and carbon dioxide and competitive reaction and process, comprise multiple process steps, these process steps are summarised in equation 8.
Carbon+2H 2o → CO 2+ 4H ++ 4 electronic formulas 8
Carbon as in equation 8 summarize be consumed, comprise may using with the carbon supplied from anoxic digester or electrolyser or the component mixed as the various liquid manufacturing the result exported or carbonaceous material.Exemplarily, carbon can comprise from make a living electrogenesis pole and carry out grinding, machining, Electric discharge machines processing (EDM) and the waste material of various thermochemistry operation, the electrode coating (comprising slot liner) on electrode or particulate matter or long filament or flocculating agent or the selected carbide by thermal dissociation and course of reaction generation, comprise colloid or other suspensions that the dehydrogenation because of the various degree of organic substance produces.
Such carbon and/or carbon donor raw material can by from the bacterium of the Liquid acquisition carbon dioxide that supply and other nutrients, phytoplankton or larger algae renewable supply, or by making carbon dioxide recycle renewable supply to the plant of water culture and/or soil support.Utilize the carbon with high surface/volume of this kind of form and wherein its for reaction shown in driving with for sending hydrionic object to electrode surface and the district of sending provides voltage gradient to be favourable, wherein said electrode surface comprises supplementary conducting medium as long filament and conducting filtration material so that the generation of bubble hydrogen, nucleation and release, thus improves the global rate of hydrogen manufacturing.
Increase the appropriate action of active surface and/or flocculating agent comprise there is organic component such as bacterium, albumen, monose and complex sugar, cellulose, thermal dissociation cellulose, live and those of the phytoplankton of dissociating, and various forms of colloidal carbon, active carbon and carbide.Exemplarily, phytoplankton and/or larger algae can grow, dry, with Bond as corn sirup mixes, with the mode dehydrogenation of heat extremely various degree mill to provide flocculating agent in small, broken bits.Or, activated carbon raw material can be milled to provide particulate matter in small, broken bits, these particulate matters be used as enzyme receiver or flocculating agent medium or its can with disclosed material be above combined to strengthen required production or enzyme efficiency, support hatching or improving hydrogen or methane production and/or consume carbon as shown in equation 8 to produce hydrogen ion for electrolysis of desired microorganisms.
If needed, use salt solution once in a while or to based on the harmful fouling adding a small amount of salt in the electrolyte of water and can produce chlorine and Quick disinfection or prevent shown electrolyzer system.The employing of some embodiments, such as Fig. 5 B, to make produced system can inherently without harmful fouling, even when adopting electrolyte as waste water, industrial process water, wood ash water, seawater, water of coal ash, canal and ditch water in a canal or anoxic digester liquid.In addition, if needed, such system can be removed from accessory 118b to 138b adverse current by electrolyte or rinse water and may be delivered to the particulate matter of electrode and obtain Rapid Cleaning.
The application of some embodiments comprises the electrolyser that large population water treatment operates nano-scale, comprise the improvement to ordinary waste digester, to be supplied to from ordinary waste digester containing the solution of organic substance or " liquid " and to produce hydrogen and/or methane and/or carbon dioxide and other plant nutrients.Under this ability, the by product that some embodiments can provide anoxic digester to produce fast and Efficient Conversion hydrogen ion is changed into hydrogen, and overcome the acid degradation of methane production operation.Be in operation, the liquid from anoxic digester is used to produce hydrogen and carbon dioxide and advantageously returns near 7.0 to make pH or remain near 7.0, instead of under the more acid condition that may hinder methane production system.This makes the raising realizing total energy transformation efficiency, adds chemical reagent to regulate the needs of the expensive measures of the pH in digester because which overcome to being used for.In so medium and large-scale application, advantageously design and supervise the multipurpose multifunctional operating system made and comprise electronic distribution circuit, described multipurpose multifunctional operating system can also provide particle as carbon, boron nitride, zeolite, polymer and comprise this kind of material pottery under the condition differently activated needed for confining force to strengthen the property.
On the other hand, electrolyser can be applied to provide the rapid conversion usually being digested produced acid by anoxic as disclosed herein, and described anoxic digestion comprises the application adopting municipal wastewater and rubbish and the waste from slaughterhouse, dairy, laying hen field and other animal feeding centers etc.If the acid that anoxia condition produces makes pH drop to far below 7, then the production of methane is by slack-off or suppressed.If the feed rate of organic material exceedes the ability of methanogen group, then may form such acid.By from such acid extractants hydrogen, can be improved by the speed of anoxic digestion process organic material.The combination of methane and hydrogen is produced providing the net energy of higher waste per ton far away, and waste is increased the ability of this process by processing faster.
The useful especially embodiment of some embodiments is in such waste-Conversion of Energy application: described applications exploiting organic substance as sewage and equation 1-6 the rubbish, farm waste and the forest waste wood that have been hydrolyzed in the anoxic electricity digestion process of summarizing to produce hydrogen, and the generation of oxygen is few or the generation of anaerobic.Firm structure and recirculation run and make the solid to dissolving can have very high tolerance, and described solid comprises as the organic solid in electrolytical anoxic process liquids and particulate matter.Produce hydrogen and nothing and brine electrolysis and discharge correspondingly discharge oxygen like that, using promote with waste be the hydrogen in source as electrical equipment as the more high efficiency of the cooled gas in generator and use safety.
In the Another Application of some embodiments in this article, electrolyzer system 900b provides and makes living beings generation tissue and/or cell rupture to realize sooner or couveuse process more completely, digestion and/or support by enzyme, machinery, heat, sound, electricity, pressure and/or chemical action and process in regulator 950b as shown in fig.7b.This kind of ruptured cell containing to come self tuning regulator 950b and the fluid of related raw material produced by converter 902b are recycled to electrolyser 914b by the ring distributor 922b of base 910b, as shown in the figure.Anoxic microorganism is supported by medium 940b and 942b and receives by conduit 910b from the liquid of hydrogen separator 904b recirculation with by the liquid of conduit 908b from carbon dioxide separator 906b recirculation, as shown in the figure.Electrode 918b and/or medium 942b discharges hydrogen, and electrode 916b and/or medium 940b release of carbon dioxide.There is provided electromotive force bias voltage by circuit 926b to electrode 916b and 918b by source 924b, described bias voltage can be 0.1 to about 3VDC, and this depends on that compound dissociates needs and interim increase voltage to overcome the needs of formed dielectric film.Hydrogen is transferred to collect and be delivered to separator 904b by advancing along more or less conical surperficial 925b, trochoidal surface 925b can be the surface of conduction, this depends on required series/parallel modification, or is taken in by insulator 930b and supported, as shown in the figure.
Be in operation, liquid mixes and upwards advances to provide process reaction thing and provide nutrient for microorganism in distributor anchor ring 922b, and described microorganism lives with active carbon cloth and/or particle 940b and 942b and/or encases and substantially keep in the conductive felt of this kind of particle closest to electrode 916b and/or 918b.Less particulate matter and long filament can be added to infiltrate the position of whole electrolyzer system, thus strengthen charge-conduction, enzyme and catalysis, comprise those disclosed above.Separator 902b can be reverse osmosis membrane or positive ion or anion-exchange membrane or its can build by the embodiment shown in Fig. 2 B, 3B, 4B or 5B, and in some cases, such separator can use with being bonded to each other, for provide various liquid circulation passage and/or at various pressures produce hydrogen and carbon dioxide or make that there is between hydrogen and carbon dioxide pressure reduction time, may need like this.
Similarly, if electrode 916b is used as electron source together with adjacent felt and/or medium 940b, then can obtain many circulations select, with under the effect in lift of gas, convection current or the liquid delivery sent by pump and circulate ion produce hydrogen, as shown in the figure.Under this selects, along with since 902b and 950b the acid of sending or being produced by microorganism (live with fiber or granule medium 942b and by electrode 918b electric bias in the relevant felt material contrary to electrode 916b) produce hydrogen ion, by release of carbon dioxide.If electronics is provided by electrode 918b, then will produce another exemplary selection and produce hydrogen, described hydrogen is collected by insulator 930b to be delivered to gas collector 904b, as shown in the figure.In this case, electrode 916b and be electron collector to the relevant medium of its electricity, because be delivered through insulator 930b to trap 906b along with carbon dioxide, carbon dioxide is released and in shown fluid circuit, provides suction, as shown in the figure.
See Fig. 7 B, system 900b can be used to by Organic Ingredients as by photosynthesis produce those be converted into methane, hydrogen and/or carbon dioxide and/or pass through microorganism.Depend on lodged microorganism, usually containing acid as acetic acid and butyric acid and compound such as the liquid of urea dissociate in electrolyser 914b.Electrolyser 914b provides electric current and produces hydrogen from this compounds and acid and can be provided as the operation of digester and electrolyser under enough voltage, or in anoxic digester (not shown), can run or can utilize anoxic in 914b to digest the liquid produced, as shown in the figure.For the organic waste be converted from population and/or industry park with to population supply fuel and raw material to manufacture the durable goods of carbon enhancing, such operation is particularly useful.
See Fig. 8 B, on the other hand, layout for the one or more conductive electrodes be used in electrolyser (comprise disclosed herein those) shows that it can electrically connect as one pole or the bipolar component of electrolyser in order to comprise dull and stereotyped (not shown) or coaxal electrode 1002b, 1003b, 1004b or 1005b as shown in the figure.Some or all of such conductive electrode provides vast surface as the layer (such as carbon and/or BN " filter ") of the Graphene separated or other thickness because of high surface/volume material.This can be used to boarding microorganism (described microbial decomposition comprises the various organic materials of volatile fatty acid to discharge electronics and proton, for producing hydrogen at cathode surface place) and can be embodied as use together with any above-mentioned embodiment.
On the other hand, microorganism produces and is added to decomposing volatile fatty acid and other organic indispensable enzymes various the active carbon or polymer beads or long filament introducing and formed in the height surface/volume material of electrode 1002b, 1004b, 1006b, 1008b.Or any microorganism described herein, enzyme or promoter can be introduced in described surface.Along with such enzyme or other materials or promoter is depleted, degraded or destroy, this fermentoid of magnitude of recruitment, material or promoter can be added as required.This system allows the optimization realizing promoter, comprise allow microorganism be separated but provide this fermentoid to grow up strong and sturdy in the position of the operating utilization of electrolyser as shown in the figure.
In another embodiment, described indispensable enzyme, microorganism or promoter artificially are produced as copy or are " the design enzyme " that differently change, and it is grafted to suitable natural polymer as cellulose or lignocellulosic or the polymer or the compound that are grafted to various plant produced.
To fall or from the enzyme of the colony lift alive of microorganism or factory copies or in the maintenance enzyme system of design enzyme that differently changes, need to make electrolytical resistance in electrolyser minimize the viable bacteria of boarding microorganism.This by promote acetic acid and various acid and other by the material be consumed with the generation of hydrogen under required high pressure as the such as equation 9 of urea in the process that illustrates in general manner, this may be implemented in any embodiment disclosed herein equally.
CH3COOH+2H2O=2CO2+4H2 equation 9
On the other hand, for detecting chemically reactive substance and identifying that the existence of this kind of material or enzyme, ability and vitality comprise the operating conditions of the amount of chemism nutrient and the adaptive system of other operating conditionss thus the system optimizing the operation of maintenance enzyme system can use together with the present embodiment to make to realize regulating.Equally, described system can be implemented together with any embodiment disclosed herein.
In this article in other embodiments of disclosed any embodiment or aspect, the enzyme of iting is desirable to run at a pressure sufficient selected microorganism and/or maintenance with increase dissolving or otherwise keep in the solution CO 2amount, thus improve electrolytical conductivity.This will improve system effectiveness and service requirement in a number of ways, and these modes comprise:
1) hydrogen produced under high pressure may be delivered into compact, store to pressurization and do not cause run multistage hydrogen gas compressor capital cost, maintenance or energy expenditure.
2) hydrogen produced under high pressure directly can enter capstan with transmission to market.
3) hydrogen produced under high pressure can be used for pressurizeing other reactants to make it possible to reaction or accelerated reaction.Exemplarily, to produce ammonia or other products during the hydrogen of pressurization can be added in suitable reactor nitrogen.
4) pressurization will simplify electrolyser design greatly to prevent the release of carbonate dioxide on electrolyser electrode surface or to make described release minimize.
5) by under high pressure collect through the electrolyser of pressurization or suitable subtense angle hydrogen with in another position or collect carbon dioxide by another subtense angle after decompression and achieve being separated of hydrogen and carbon dioxide production.
See Fig. 9 B, illustrated therein is system 1100b, this system 1100b comprises high pressure electrolyser 1102b, and high pressure electrolyser 1102b can receive the electrolyte through pressurizeing from suitable pump 1114b and/or in electrolyser 1102b, form suitable electrolytical precursor flow.As the result of the effect of the voltage between the enzyme of the microorganism on shown one or more electrode such as 1002b, 1004b, 1006b, 1008b etc. or 1104b and/or maintenance and plug 1106b and 1124b shown in being applied to, produce the hydrogen through pressurization.High Pressure Hydrogen is delivered to suitable application via pressure regulator 1120b by conduit 1122b.
Carbonated pressurization electrolyte flow through oil hydraulic motor-generator 1126b, by utilize the electrolytical kinetic energy of flowing and along with carbon dioxide be delivered to suitable carbon dioxide purposes as liquid culture system or greenhouse 1130b with grow algae, switchgrass, elegant jessamine or other crop 1132b and/or 1134b various time expansion from carbon dioxide to external pressure and produce merit.The electrolyte of depleted carbon dioxide by pump 1114b via three-way valve 1112b recirculation.
Living beings, comprise the material grown in 1130b, by levigate or otherwise make the slurry of active substance, described slurry is made up of the cell material of fragmentation, and the cell material of these fragmentations is produced by suitable machinery, sound, chemistry, heat or radiation treatment in processor 1136b.Active Organic Ingredients is like this added to acescent 1108b, aptly through filter 1110b and through three-way valve 1112b, arrives pump 1114b, to enter pressure electrolyser 1102b, as shown in the figure.
The operation of system 1100b is provided by controller 1101b response pressure, temperature and pH sensor 1142b, 1144b, 1146b and chemical active agent sensor 1140b and 1150b, as shown in the figure.This makes the condition needed for the enough enzyme performance optimum performances adding to provide maintenance by port one 118b of indemnity mass-energy.
In another embodiment, suitable electrode comprise the system that formed as the wire of square or rectangle or various " star " shape or flat strip from circular or other cross sections with provide be formed plastically weave embodiment or spirality embodiment as disclosed herein.Then by the material of selection as iron or other alloys based on transition metal are heat-treated to carburizing and produce the carbon of various amount in solid solutions, described solid solution comprises saturation region, and these saturation regions are limited further by the heat treatment added or grow to make the growth of such saturation region especially near surface.Along with carbon donor as hydrocarbon or carbon monoxide decompose on this surface, the carbon district of generation will speed up the deposition of other carbon.Equation 10 and 11 shows this kind of total process to being equal to or greater than the heat of the Heat of Formation of carbon donor through the heat treated base material amount of providing:
CxHy+ hot à xC+0.5yH2 equation 10
CO+ hot à C+0.5O2 equation 11
In some respects, it is desirable to continue Carbon deposition to produce the carbon film effectively covering whole electrode with enough degree of depth (combining in initial saturation region), to produce the very durable composite material with required form and surface/volume.
In another embodiment, the initial preparation close to the carbon-rich zone of saturation conditions is changed to provide the fully consistent orientation of carbon crystal structure by heat or cold working embodiment with orientation, thus provides the sediments of the Carbon deposition in succession significantly epitaxially affected.The carbon of the orientation of deposition like this such as main exposed edge or in the graphene layer more parallel with initial surface by tested to provide the support of desired microorganisms process competitively.This can realize for various types of desired microorganisms process choosing " design carbon ".
See Figure 10 B, on the other hand, disclose for the manufacture for the carbon/steel electrode in embodiment disclosed herein.These electrodes can comprise surface treated carbon to adhere to selectivity enzyme, microorganism or other promoter to improve the operation of electrolyser.For manufacturing according to the electrode of this embodiment, make steel or steel alloy substrate saturated by carbon institute.The crystal grain of saturated carbon, by such as induction heat treatment arrangement, thinks the grain orientation that carbon provides required, as shown in phasei.Also other known heat treatment methods can be adopted.In this step process, electrode also can be allowed to stand liquid cooling to prevent electrode damage or to provide other benefits.
As shown in stage II, then comprise clamping roll-in by known process and form shape electrode.Shaping can arrange as required further, the mode of carbon grain that is smooth or that change orientation is implemented.
As shown in stage III, carbon then by known Carbon deposition deposition techniques on electrode, deposition technique comprises vapor deposition, and by this, carbon is by the deposited on silicon of electrode or growth.In this step process, carbon can strengthen grain-oriented mode further and deposit or select location place optionally deposit carbon on electrode, and this depends on the required purposes of electrode.Such as, a kind of enzyme, microorganism or promoter can be deposited a position, and another kind of enzyme, microorganism or promoter can be deposited over another position, to realize the controlled use of enzyme, microorganism and promoter.In addition, the electrode with the carbon of deposition processes to arrange further or orientation crystal grain by induction heating or other measures further, and this can comprise liquid cooling equally.This process can repeatedly until carbon amounts needed for obtaining and/or grain orientation and/or die locations.
As shown in stage IV, after completing surface treatment, the enzyme then making electrode be exposed to one or more to select for the application-specific of electrode, microorganism or promoter, such as, to improve in electrolytic process required compound as the enzyme of the output of hydrogen.In any above-mentioned steps, described method can the special position of target electrode.In addition, can apply different treatment conditions to different positions, make it possible to adopt different enzymes or can implement different enzyme density in different positions, this depends on required structure or the purposes of electrode.Like this, the electrode produced comprises and has the carbon structure of compatibility to certain enzyme, microorganism or promoter and described enzyme, microorganism or promoter be attached to desired location on electrode and sentence for good and all or substantially keep described enzyme to use in electrolysis or other electrode runnings in desired location.
Although describe the present invention in conjunction with specific embodiment and embodiment, one skilled in the art will readily appreciate that the present invention can change and revise and without departing from the spirit and scope of the present invention.Therefore, scope of the present invention is only limited by the claims of attaching.

Claims (37)

1. one kind comprises for the method for the renewable origin providing material resources:
First source of renewable energy is provided;
The first flow of material from the first source of the material is provided;
The heat exchanger be connected with the first source of described renewable energy with described first flow of material is provided, wherein said heat exchanger from described first flow of material by the generation material resources that dissociates; With
There is provided described material resources to process further or to use to first processor.
2. method according to claim 1, wherein said material resources comprises hydrogen.
3. method according to claim 1, wherein said material resources comprises the material based on carbon.
4. method according to claim 1, wherein said material resources comprises hydrocarbon.
5. method according to claim 1, wherein said material resources comprises the material based on nitrogen.
6. method according to claim 1, wherein said first source of the material comprises organic material.
7. method according to claim 1, also comprises by adding heat energy to the described material resources from described first processor and processes the step of described material resources further.
8. method according to claim 7, wherein said first processor comprises solar collector.
9. method according to claim 8, wherein said solar collector is connected with described heat exchanger.
10. method according to claim 9, wherein said solar collector comprises sunlight and concentrates mirror.
11. methods according to claim 10, wherein said sunlight concentrates mirror to comprise parabolical mirror, spherical mirror or settled date reflection mirror array.
12. methods according to claim 8, described method also comprises the first supplemental heat source to supplement or to substitute the heat from described solar collector.
13. methods according to claim 11, wherein said material resources comprises methane, and the step of the described material resources of described further process comprises the described methane that dissociates to produce carbon and hydrogen.
14. methods according to claim 4, wherein provide described material resources to comprise with the step processed further or use to described first processor and described hydrocarbon are converted into hydrogen and carbon.
15. methods according to claim 14, wherein said material resources also comprises carbon dioxide.
16. methods according to claim 14, also comprise the step described hydrogen being converted into energy.
17. methods according to claim 14, wherein said heat exchanger is constructed to can selectively reverse speed operation and as synthesizer and the described step described hydrogen being converted into energy comprises the operation of described heat exchanger as chemical converter.
18. methods according to claim 14, described method also comprises the step described carbon being converted into one or more durable goods.
19. methods according to claim 18, one or more durable goods wherein said comprise for one or more durable goods in the step in the first source for providing described renewable energy.
20. methods according to claim 15, also comprise the step providing described carbon dioxide for agricultural use.
21. methods according to claim 1, wherein said first source of the material comprises living beings.
22. methods according to claim 1, wherein said first source of the material comprises bio-waste.
23. 1 kinds for providing the system of the renewable origin of material resources, described system comprises:
First source of renewable energy;
From the first flow of material of the first source of the material;
Heat exchanger, described heat exchanger is connected with described first flow of material with the first source of described renewable energy, and wherein said heat exchanger is constructed to by generation first material resources that dissociates;
Processor, for processing further or using described material resources to produce the second material resources, wherein said processor comprises solar collector and wherein said solar collector is constructed to provide heat to dissociate to described first material resources; With
Material resources storage, described material resources storage is connected to receive described material resources from described heat exchanger or provides described material resources to process further or to use to described processor with described heat exchanger.
24. systems according to claim 23, wherein said material resources comprises the material based on carbon.
25. systems according to claim 23, wherein said material resources comprises hydrocarbon.
26. systems according to claim 23, wherein said material resources comprises the material based on nitrogen.
27. systems according to claim 23, wherein said material resources comprises ammonia.
28. systems according to claim 25, wherein said processor is constructed to described hydrocarbon to be converted into hydrogen and carbon.
29. systems according to claim 28, also comprise for distributing the distribution system of hydrogen for first position.
30. systems according to claim 23, also comprise for distributing described material resources with the material resources distribution system used further.
31. systems according to claim 30, wherein said material resources distribution system is connected with one or more in the first source of described renewable energy, described first source of the material, described processor or described heat exchanger.
32. systems according to claim 23, wherein said solar collector is connected with described heat exchanger.
33. systems according to claim 32, wherein said solar collector comprises sunlight and concentrates mirror.
34. systems according to claim 33, wherein said sunlight concentrates mirror to comprise parabolical mirror, spherical mirror or settled date reflection mirror array.
35. system according to claim 32, also comprise the first supplemental heat source being configured to supplement or substitute from the heat of described solar collector.
36. system according to claim 23, wherein said material resources comprises methane, and described processor is constructed to dissociate described methane to produce carbon and hydrogen.
37. system according to claim 23, wherein said solar collector is constructed to by processing described first material resources to described first material resources heating.
CN201510098366.1A 2009-08-27 2010-08-16 System and method for realizing sustainable economic development through integrated total production of renewable materials by using solar thermal Pending CN104912705A (en)

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US12/707,656 US8075749B2 (en) 2009-02-17 2010-02-17 Apparatus and method for gas capture during electrolysis
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US12/707,651 US8075748B2 (en) 2009-02-17 2010-02-17 Electrolytic cell and method of use thereof
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