CN102712020B - Systems and methods for sustainable economic development through integrated full-scale production of renewable material resources using solar heat - Google Patents

Abstract

In one embodiment of the present invention, there is provided a system for providing a renewable source of material resources, the system comprising: a first source of renewable energy; a first material stream from a first material source; an electrolyzer connected to the first source of renewable energy and the first material stream, wherein the electrolyzer is configured to generate a first material resource by electrolysis; a processor for further processing or using the material resource to produce a second material resource, wherein the processor comprises a solar collector and wherein the solar collector is configured to provide heat to the first material resource for dissociation; and a material resource reservoir coupled to the electrolyzer to receive material resources from the electrolyzer or to provide material resources to the processor for further processing or use.

Description

Translated fromChinese

使用太阳热通过可再生材料资源的一体化全面生产实现可持续经济发展的系统和方法Systems and methods for sustainable economic development through integrated full-scale production of renewable material resources using solar heat

相关申请的交叉引用Cross References to Related Applications

本申请要求2010年2月13日提交的标题为“FULL SPECTRUMENERGY AND RESOURCE INDEPENDENCE”的美国临时申请号61/304,403、2010年2月17日提交的标题为“ELECTROLYTIC CELL ANDMETHOD OF USE THEREOF”的美国专利申请号12/707,651、2010年2月17日提交的标题为“ELECTROLYTIC CELL AND METHOD OF USETHEREOF”的PCT申请号PCT/US10/24497、2010年2月17日提交的标题为“APPARATUS AND METHOD FOR CONTROLLING NUCLEATIONDURING ELECTROLYSIS”的美国专利申请号12/707,653、2010年2月17日提交的标题为“APPARATUS AND METHOD FOR CONTROLLINGNUCLEATION DURING ELECTROLYSIS”的PCT申请号PCT/US10/24498、2010年2月17日提交的标题为“APPARATUS AND METHOD FOR GASCAPTURE DURING ELECTROLYSIS”的美国专利申请号12/707,656、2010年2月17日提交的标题为“APPARATUS AND METHOD FORCONTROLLING NUCLEATION DURING ELECTROLYSIS”的PCT申请号PCT/US10/24499和2009年8月27日提交的标题为“ELECTROLYZER ANDENERGY INDEPENDENCE TECHNOLOGIES”的美国临时专利申请号61/237,476的优先权和权益。这些申请各自通过引用全文并入本文中。This application claims U.S. Provisional Application No. 61/304,403, filed February 13, 2010, entitled "FULL SPECTRUMENERGY AND RESOURCE INDEPENDENCE," and U.S. Patent Application No. 61/304,403, filed February 17, 2010, entitled "ELECTROLYTIC CELL ANDMETHOD OF USE THEREOF" Application No. 12/707,651, PCT Application No. PCT/US10/24497, filed February 17, 2010, entitled "ELECTROLYTIC CELL AND METHOD OF USETHEREOF," filed February 17, 2010, entitled "APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS, U.S. Patent Application No. 12/707,653, titled PCT Application No. PCT/US10/24498, filed February 17, 2010, titled "APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS" U.S. Patent Application No. 12/707,656 for "APPARATUS AND METHOD FOR GASCAPTURE DURING ELECTROLYSIS," PCT Application No. PCT/US10/24499, filed February 17, 2010, and titled "APPARATUS AND METHOD FOR CONTROLLING NUCLEATION DURING ELECTROLYSIS," and 2009 Priority and Benefit of U.S. Provisional Patent Application No. 61/237,476, filed August 27, entitled "ELECTROLYZER ANDENERGY INDEPENDENCE TECHNOLOGIES." Each of these applications is incorporated herein by reference in its entirety.

背景技术Background technique

水生植物和地被植物，特别是农田和森林，是必不可少的二氧化碳收集器、无数野生生物的天然栖息地及用于从纸制品到建筑材料等应用的纤维的源。由于非本土害虫的引入和温室气体加剧的气候变化使得森林易受传染病、火、风、洪水和干旱灾害的侵害，故几乎所有大洲均已发生森林荒废。Aquatic plants and ground covers, especially croplands and forests, are essential carbon dioxide collectors, natural habitats for countless wildlife and sources of fibers for applications ranging from paper products to construction materials. Deforestation has occurred on almost all continents as the introduction of non-native pests and climate change exacerbated by greenhouse gases leave forests vulnerable to infectious diseases, fire, wind, floods and drought.

在整个南美洲、中美洲和北美洲，森林火灾已毁坏数目庞大的因干旱和疾病而不堪一击或死亡的立木。这构成纸浆和建筑材料的巨大损失。火灾和腐烂还产生温室气体如二氧化碳和甲烷，其将进一步损害全球大气。至关重要的是提供可以将植物性生物质在其因火灾、腐朽、洪水和侵蚀而损失之前快速转化为燃料、电和有价材料的可再生供给源的实用解决方案。必然的目标是促进健康森林、作物和其他地被的快速再建以及促进从为改善森林状况和防止有害火灾的蔓延而规定的抚育间伐和灌丛砍伐生产燃料和截存的碳价值。Throughout South, Central, and North America, forest fires have destroyed vast numbers of standing trees that have been rendered vulnerable or dead by drought and disease. This constitutes a huge loss of pulp and construction material. Fire and decay also produce greenhouse gases such as carbon dioxide and methane, which will further damage the global atmosphere. It is critical to provide practical solutions that can rapidly convert plant-based biomass into a renewable supply of fuel, electricity, and valuable materials before it is lost to fire, decay, flooding, and erosion. The corollary is to promote the rapid re-establishment of healthy forests, crops and other ground cover as well as promote the production of fuel and sequestered carbon value from tending thinning and scrub felling mandated to improve forest conditions and prevent the spread of harmful fires.

对氢、氧、甲烷、碳和其他可通过原料如生物质废弃物的热化学和/或电解解离提供的产品的需求已增长。通过热化学方法解离生物质的以往努力真正从1792年William Murdock通过水蒸汽与供碳体如泥煤、煤和木炭的反应制氢开始。新近，水蒸汽转化已被石油工业广泛采用以从石油、天然气和其他化石原料制氢。Demand for hydrogen, oxygen, methane, carbon, and other products that can be provided by thermochemical and/or electrolytic dissociation of feedstocks such as biomass waste has grown. Previous efforts to dissociate biomass by thermochemical methods really started in 1792 with William Murdock producing hydrogen by the reaction of water vapor with carbon donors such as peat, coal and charcoal. More recently, steam reforming has been widely adopted by the petroleum industry to produce hydrogen from oil, natural gas, and other fossil feedstocks.

二氧化碳和甲烷向全球大气中的释放导致气候变化，这样的气候变化威胁着全部生命物种中高达1/3的灭绝。克服大气因温室气体而退化的努力在Martin M.Halmann和Meyer Steinberg的“Greenhouse Gas Carbon Dioxide Mitigation：Science and Technology”、在John A.List的“Recent Advances in Environmental Economics”和在John Gale的“Greenhouse Gas Control Technologies：Proceedings of the 6^th International Conference on Greenhouse Gas Control Technologies”中有述及。The release of carbon dioxide and methane into the global atmosphere leads to climate change that threatens the extinction of up to a third of all living species. Efforts to overcome atmospheric degradation due to greenhouse gases are described in "Greenhouse Gas Carbon DioxideMitigation: Science and Technology " by Martin M. Halmann and Meyer Steinberg, in "Recent Advances inEnvironmental Economics " by John A. List, and in "Greenhouse Gas ControlTechnologies: Proceedings of the 6^thInternational Conference on GreenhouseGas Control Technologies ".

制甲烷和氢的替代方法是通过分解蒸馏和缺氧热解。还有人利用落水、风、太阳和化石能源来产生用于通过电解分解水的电。Victoria M.Laube和Stanley Martin在“Conversion of Cellulose to Methane and Carbon Dioxide by Triculture of Acetivibrio Cellulolyticus Desulfovibro sp.，and Methanocarcina Barkeri”(加拿大国家研究委员会)中描述了使用微生物气化纤维素的用途。还熟知的是，在较大物种如牛属动物和白蚁之间存在共生关系，牛属动物摄取木质纤维素并因其消化系统中这类产甲烷微生物的寄生而产生甲烷和二氧化碳。Alternative methods for producing methane and hydrogen are through decomposition distillation and anoxic pyrolysis. Still others use falling water, wind, sun, and fossil energy to generate electricity for splitting water through electrolysis. The use of microorganisms to gasify cellulose is described by Victoria M. Laube and Stanley Martin in "Conversion of Cellulose to Methane and Carbon Dioxide byTriculture of Acetivibrio Cellulolyticus Desulfovibro sp., and MethanocarcinaBarkeri " (National Research Council of Canada). It is also well known that a symbiotic relationship exists between larger species such as bovines, which ingest lignocellulose and produce methane and carbon dioxide due to their parasitism of such methanogenic microorganisms in their digestive systems, and termites.

出版物如“Hydrogen Production From Water By Means of Chemical Cycles”，Glandt，Eduardo D.，和Myers，Allan L.，Department of Chemical andBiochemical Engineering，University of Pennsylvania，Philadelphia，PA 19174，Industrial Engineering Chemical Process Development，Vol.15，No.1，1976；“Hydrogen As A Future Fuel”，Gregory，D.P.，Institute of Gas Technology中已述及为提供减少这些方法所遭遇的问题的技术所作的努力。Publications such as "Hydrogen Production From Water By Means of ChemicalCycles ", 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 ", Gregory, DP, Institute of Gas Technology has described efforts to provide techniques that reduce the problems encountered with these methods.

伴随这类系统的问题包括：能量转化效率低下，固定设备和基础设施改良成本不可接受地高，扩大规模以解决重大问题如森林转换时存在困难，及运转成本高。此外，现有技术方法需要非常大量地释放二氧化碳。在这类过程中对氢和/或甲烷及其他产品加压所需的压缩机需要相当大的资本支出、大的电消费和温室气体的伴随产生、以及高的运转成本。此外，不可接受的维护需要和高的修理费用已挫败这类方法。现有废弃物转能量技术克服因全球大气中温室气体积聚所致的日益增长的气候变化问题的能力严重受限，如果不是起相反作用的话。总而言之，现有技术太昂贵、太浪费且太污染。Problems associated with such systems include: inefficiency in energy conversion, unacceptably high costs of capital equipment and infrastructure improvements, difficulties in scaling up to address major problems such as forest conversion, and high operating costs. Furthermore, prior art methods require very large releases of carbon dioxide. The compressors required to pressurize hydrogen and/or methane and other products in such processes require considerable capital expenditure, large electricity consumption and concomitant production of greenhouse gases, and high operating costs. Furthermore, unacceptable maintenance requirements and high repair costs have frustrated such approaches. Existing waste-to-energy technologies are severely limited, if not counterproductive, in their ability to overcome the growing problem of climate change caused by the accumulation of greenhouse gases in the global atmosphere. All in all, existing technologies are too expensive, too wasteful and too polluting.

因此，本发明的一些实施方案的目的是提供通过可再生养分资源的一体化全面生产实现可持续经济发展的系统和方法，其可包括使用电化学或电解电池分离地产生养分资源的用途及使用其分离地产生养分资源的方法，以解决一个或多个上述问题。Accordingly, it is an object of some embodiments of the present invention to provide systems and methods for sustainable economic development through the integrated overall production of renewable nutrient resources, which may include the use of electrochemical or electrolytic cells to separately generate nutrient resources and use Its method of separately generating nutrient resources to solve one or more of the above-mentioned problems.

发明内容Contents of the invention

在本发明的一个实施方案中，提供了一种用于提供材料资源的可再生源的系统，所述系统包括：可再生能的第一源；来自第一材料源的第一材料流；与所述可再生能的第一源和所述第一材料流相连的电解器，其中所述电解器被构造为通过电解产生第一材料资源；用于进一步处理或使用所述材料资源以产生第二材料资源的处理器，其中所述处理器包括太阳能收集器且其中所述太阳能收集器被构造为向所述第一材料资源提供热以便解离；和与所述电解器相连以自所述电解器接收材料资源或向所述处理器提供材料资源以进一步处理或使用的材料资源储存器。In one embodiment of the invention there is provided a system for providing a renewable source of material resources, the system comprising: a first source of renewable energy; a first material stream from the first material source; and an electrolyzer coupled to the first source of renewable energy and the first material flow, wherein the electrolyzer is configured to produce a first material resource by electrolysis; for further processing or using the material resource to produce a second A processor of two material resources, wherein the processor includes a solar collector and wherein the solar collector is configured to provide heat to the first material resource for dissociation; The electrolyser receives the material resource or provides the material resource to the processor for further processing or use by the material resource storage.

在另一个实施方案中，提供了一种用于提供材料资源的可再生源的系统，所述系统包括：可再生能的第一源；来自第一材料源的第一材料流；与所述可再生能的第一源和所述第一材料流相连的电解器，其中所述电解器被构造为通过电解产生第一材料资源；用于进一步处理或使用所述材料资源以产生第二材料资源的处理器，其中所述处理器包括太阳能收集器且其中所述太阳能收集器被构造为向所述第一材料资源提供热以便解离；和与所述电解器相连以自所述电解器接收材料资源或向所述处理器提供材料资源以进一步处理或使用的材料资源储存器。In another embodiment, a system for providing a renewable source of material resources is provided, the system comprising: a first source of renewable energy; a first material stream from the first material source; and the An electrolyzer coupled to a first source of renewable energy and said first material flow, wherein said electrolyzer is configured to produce a first material resource by electrolysis; for further processing or using said material resource to produce a second material A processor of a resource, wherein the processor includes a solar collector and wherein the solar collector is configured to provide heat to the first material resource for dissociation; A material resource store that receives material resources or provides material resources to the processor for further processing or use.

在又一实施方案中，提供了一种用于提供材料资源的可再生源的方法，所述方法包括：提供可再生能的第一源；提供来自第一材料源的第一材料流；提供与所述第一材料流和所述可再生能的第一源相连的电解器，其中所述电解器自所述第一材料流通过电解产生材料资源；和向第一处理器提供所述材料资源以进一步处理或使用。In yet another embodiment, a method for providing a renewable source of material resources is provided, the method comprising: providing a first source of renewable energy; providing a first material stream from the first material source; providing an electrolyzer coupled to the first material stream and the first source of renewable energy, wherein the electrolyzer produces a material resource from the first material stream by electrolysis; and provides the material to a first processor resources for further processing or use.

通过下面的详细描述，本发明的其他特征和优势将变得显而易见。但应理解，这里的详细描述和示出本发明的优选实施方案的具体实施例仅通过示例的方式给出，因为通过该详细描述，本发明的精神和范围内的各种变化和修改对于本领域技术人员来说将是显而易见的。Other features and advantages of the present invention will become apparent from the following detailed description. It should be understood, however, that the detailed description and the specific examples, which illustrate preferred embodiments of the invention, are given by way of illustration only, since various changes and modifications within the spirit and scope of the invention will be introduced from the detailed description It will be obvious to those skilled in the art.

附图说明Description of drawings

图1示出了本发明的过程步骤。Figure 1 shows the process steps of the present invention.

图2为根据本发明的原理运行的一个实施方案的纵截面视图。Figure 2 is a longitudinal sectional view of one embodiment operating in accordance with the principles of the present invention.

图3为图1中提供的部件的实施方案的一部分的纵截面放大视图。FIG. 3 is an enlarged view in longitudinal section of a portion of an embodiment of the component provided in FIG. 1 .

图4为根据本发明的原理运行的一个实施方案的截面图。Figure 4 is a cross-sectional view of one embodiment operating in accordance with the principles of the present invention.

图5为根据本发明的原理运行的一个实施方案的部分截面图。Figure 5 is a partial cross-sectional view of one embodiment operating in accordance with the principles of the present invention.

图6示出了根据本发明的原理运行的过程步骤。Figure 6 illustrates process steps operating in accordance with the principles of the present invention.

图7为根据本发明的原理运行的一个实施方案的示意图。Figure 7 is a schematic diagram of one embodiment operating in accordance with the principles of the invention.

图8示出了根据本发明的原理的运行。Figure 8 illustrates operation in accordance with the principles of the invention.

图9示出了根据本发明的原理运行的部件。Figure 9 shows components operating in accordance with the principles of the invention.

图10为本发明的实施方案的示意图。Figure 10 is a schematic diagram of an embodiment of the present invention.

图12-15为根据本公开的方面的各种实施方案的流程图。12-15 are flowcharts according to various embodiments of aspects of the present disclosure.

图1B示出了根据本发明的一个实施方案的电解电池。Figure IB shows an electrolysis cell according to one embodiment of the invention.

图2B示出了图1的实施方案的一部分的放大视图。FIG. 2B shows an enlarged view of a portion of the embodiment of FIG. 1 .

图3B示出了图2的实施方案的一个变型。FIG. 3B shows a variation of the embodiment of FIG. 2 .

图4B示出了根据本发明的一个实施方案的电解电池。Figure 4B shows an electrolysis cell according to one embodiment of the invention.

图5B示出了图4的电解电池的一部分的替代实施方案的放大视图。FIG. 5B shows an enlarged view of an alternative embodiment of a portion of the electrolysis cell of FIG. 4 .

图6B示出了用于可逆燃料电池中的螺旋电极的横截面。Figure 6B shows a cross-section of a spiral electrode used in a reversible fuel cell.

图7B示出了用于将有机原料如通过光合作用所产生的那些转化为甲烷、氢和/或二氧化碳的系统。Figure 7B shows a system for converting organic feedstocks, such as those produced by photosynthesis, into methane, hydrogen and/or carbon dioxide.

图8B示出了用于将有机原料如通过光合作用所产生的那些转化为甲烷、氢和/或二氧化碳的系统。Figure 8B shows a system for converting organic feedstocks, such as those produced by photosynthesis, into methane, hydrogen and/or carbon dioxide.

图9B示出了用于将有机原料如通过光合作用所产生的那些转化为甲烷、氢和/或二氧化碳的系统。Figure 9B shows a system for converting organic feedstocks, such as those produced by photosynthesis, into methane, hydrogen and/or carbon dioxide.

图10B示出了根据本公开的一个实施方案的用于制造电极的方法。Figure 10B shows a method for fabricating an electrode according to one embodiment of the present disclosure.

具体实施方式Detailed ways

本申请通过引用全文并入2004年11月9日提交的标题为“MULTIFUELSTORAGE，METERING AND IGNITION SYSTEM”的美国临时专利申请号60/626,021(代理人案号69545-8013US)和2009年2月17日提交的标题为“FULL SPECTRUM ENERGY”的美国临时专利申请号61/153,253(代理人案号69545-8001US)的主题。本申请还通过引用全文并入如下与此同时于2010年8月16日提交的标题为“METHODS AND APPARATUSES FORDETECTION OF PROPERTIES OF FLUID CONVEYANCE SYSTEMS”(代理人案号69545-8003US)、“COMPREHENSIVE COST MODELING OFAUTOGENOUS SYSTEMS AND PROCESSES FOR THE PRODUCTION OFENERGY，MATERIAL RESOURCES AND NUTRIENT REGIMES”(代理人案号69545-8025US)、“ELECTROLYTIC CELL AND METHOD OF USETHEREOF”(代理人案号69545-8026US)、“SUSTAINABLE ECONOMICDEVELOPMENT THROUGH INTEGRATED PRODUCTION OFRENEWABLE ENERGY，MATERIALS RESOURCES，AND NUTRIENTREGIMES”(代理人案号69545-8040US)、“SYSTEMS AND METHODS FORSUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATEDFULL SPECTRUM PRODUCTION OF RENEWABLE ENERGY”(代理人案号69545-8041US)、“METHOD AND SYSTEM FOR INCREASING THEEFFICIENCY OF SUPPLEMENTED OCEAN THERMAL ENERGYCONVERSION(SOTEC)”(代理人案号69545-8044US)、“GAS HYDRATECONVERSION SYSTEM FOR HARVESTING HYDROCARBON HYDRATEDEPOSITS”(代理人案号69545-8045US)、“APPARATUSES AND METHODSFOR STORING AND/OR FILTERING A SUBSTANCE”(代理人案号69545-8046US)、“ENERGY SYSTEM FOR DWELLING SUPPORT”(代理人案号69545-8047US)、“ENERGY CONVERSION ASSEMBLIES ANDASSOCIATED METHODS OF USE AND MANUFACTURE”(代理人案号69545-8048US)和“INTERNALLY REINFORCED STRUCTURALCOMPOSITES AND ASSOCIATED METHODS OF MANUFACTURING”(69545-8049US)的每个美国专利申请的主题。This application is incorporated by reference in its entirety into U.S. Provisional Patent Application No. 60/626,021 (Attorney Docket No. 69545-8013US), filed November 9, 2004, and entitled "MULTIFUELSTORAGE, METERING AND IGNITION SYSTEM" and filed February 17, 2009. is the subject of U.S. Provisional Patent Application No. 61/153,253 (Attorney Docket No. 69545-8001US) filed and entitled "FULL SPECTRUM ENERGY." This application is also incorporated by reference in its entirety as follows concurrently filed on August 16, 2010 entitled "METHODS AND APPARATUSES FORDETECTION OF PROPERTIES OF FLUID CONVEYANCE SYSTEMS" (Attorney Docket No. 69545-8003US), "COMPREHENSIVE COST MODELING OFAUTOGENOUS SYSTEMS AND PROCESSES FOR THE PRODUCTION OFENERGY，MATERIAL RESOURCES AND NUTRIENT REGIMES”(代理人案号69545-8025US)、“ELECTROLYTIC CELL AND METHOD OF USETHEREOF”(代理人案号69545-8026US)、“SUSTAINABLE ECONOMICDEVELOPMENT THROUGH INTEGRATED PRODUCTION OFRENEWABLE ENERGY ，MATERIALS RESOURCES，AND NUTRIENTREGIMES”(代理人案号69545-8040US)、“SYSTEMS AND METHODS FORSUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATEDFULL SPECTRUM PRODUCTION OF RENEWABLE ENERGY”(代理人案号69545-8041US)、“METHOD AND SYSTEM FOR INCREASING THEEFFICIENCY OF SUPPLEMENTED OCEAN THERMAL ENERGYCONVERSION(SOTEC)”(代理人案号69545-8044US)、“GAS HYDRATECONVERSION SYSTEM FOR HARVESTING HYDROCARBON HYDRATEDEPOSITS”(代理人案号69545-8045US)、“APPARATUSES AND METHODSFOR STORING AND/OR FILTERING A SUBSTANCE”( Attorney Case No. 69545-8046US), "ENERGY SYSTEM FOR DWELLING SUPPORT" (Attorney Case No. 69545-8047US), "ENERGY CON VERSION ASSEMBLIES AND ASSOCIATED METHODS OF USE AND MANUFACTURE" (Attorney Docket No. 69545-8048US) and "INTERNALLY REINFORCED STRUCTURAL COMPOSITES AND ASSOCIATED METHODS OF MANUFACTURING" (69545-8049US) are the subject of each of the U.S. patent applications.

为完全理解获得根据本发明的上述细节及其他优势和目的的方式，下面将结合其具体实施方案对本发明给予更详细的描述。In order to fully understand the way to obtain the above details and other advantages and objectives according to the present invention, the following will give a more detailed description of the present invention in conjunction with its specific embodiments.

图1示出了过程16，在其中，生物质(包括市政、农场和森林废弃物如森林废材和生病和/或死亡的树)被切割、拉走或以其他方式采集并在步骤2处交付。在步骤4中，这类生物质废弃物被切碎或以其他方式细分成小块和段以便输送机如带式输送机、推杆输送机或螺旋输送机高效输送并压实。在步骤6中，经细分的生物质废弃物被干燥并通过再生性解离而转化产生烃、醇蒸气以及甲烷、氢和其他气体及固体如碳和由纤维素和/或木质纤维素原料引入或随同纤维素和/或木质纤维素原料一起引入的矿物。步骤8提供蒸气和气体如甲烷和/或氢与二氧化碳的分离。步骤10提供通常富甲烷的气体通过管道或其他输送方法如天然气工业中采用的那些的装运。步骤12提供氢和碳产品自这样的管道输送的富甲烷气体的生产。步骤14提供氢在发动机和/或燃料电池中的使用以为机动车辆提供动力、提供热、用于轴功和发电、用于化学加工应用、及生产肥料。Figure 1 shows a process 16 in which biomass (including municipal, farm and forest waste such as forest waste and diseased and/or dead trees) is cut, pulled or otherwise harvested and processed at step 2 deliver. In step 4, such biomass waste is shredded or otherwise subdivided into small pieces and segments for efficient transport and compaction by conveyors such as belt conveyors, pusher conveyors, or screw conveyors. In step 6, the subdivided biomass waste is dried and converted by regenerative dissociation to produce hydrocarbons, alcohol vapors as well as methane, hydrogen and other gases and solids such as carbon and from cellulosic and/or lignocellulosic feedstocks Minerals introduced into or with cellulosic and/or lignocellulosic feedstock. Step 8 provides for the separation of vapors and gases such as methane and/or hydrogen from carbon dioxide. Step 10 provides for shipment of typically methane-rich gas via pipeline or other delivery methods such as those employed in the natural gas industry. Step 12 provides for the production of hydrogen and carbon products from methane-enriched gas transported from such pipelines. Step 14 provides for the use of hydrogen in engines and/or fuel cells to power motor vehicles, provide heat, for shaft work and electricity generation, for chemical processing applications, and to produce fertilizers.

对大多数受损森林环境中火灾、地震和泥石流灾害的分析表明，通过创建地下管道以输送这类受损森林和/或地被的快速采集和转化所产生的甲烷来推进本发明所公开的解决方案将高度有利。这类可再生甲烷通过管道装运到市场(目前使用的是天然气或其他化石燃料)会大大减小来自温室气体的环境影响并会促进从目前化石能依赖向可再生能安全的演化。Analysis of fire, earthquake, and mudslide hazards in most damaged forest environments indicates that the advancement of the presently disclosed A solution would be highly beneficial. Pipelines of such renewable methane to markets (currently using natural gas or other fossil fuels) would greatly reduce the environmental impact from greenhouse gases and would facilitate the transition from current fossil energy dependence to renewable energy security.

创建可通过用管道低成本地输送的甲烷的可再生源将增加就业机会和投资者信心。通过发展由甲烷向碳产品转化、同时使用氢用于清洁能源应用所推进的“碳时代”将带来其他进步。Creating renewable sources of methane that can be transported cheaply by pipeline would increase job creation and investor confidence. Other advances will be brought about by the "Carbon Age" driven by the development of the conversion of methane to carbon products while using hydrogen for clean energy applications.

图2示出了用于通过生物质的解离可再生地生产甲烷和/或氢的方法和装置的实施方案200，在其中，如图所示，经细分的材料如各种纤维素材料和木质纤维素组织被脱气、干燥并加热以释放所需的气体。图2的系统在热效率和抑制二氧化碳形成上提供了重要改进。这些改进由图1中所示过程队列中所示在提取碳、烃如甲烷和/或氢之前的逆流干燥及空气、湿气和其他供氧体的消除而提供。Figure 2 shows an embodiment 200 of a method and apparatus for the renewable production of methane and/or hydrogen by dissociation of biomass in which, as shown, subdivided materials such as various cellulosic materials and lignocellulosic tissue are degassed, dried and heated to release the required gases. The system of Figure 2 provides important improvements in thermal efficiency and suppression of carbon dioxide formation. These improvements are provided by countercurrent drying and elimination of air, moisture and other oxygen donors prior to extraction of carbon, hydrocarbons such as methane and/or hydrogen as shown in the process train shown in Figure 1 .

最后，这类废弃物在缺氧环境中被充分加热而释放所需的气体、碳和固体残渣如矿物氧化物和其他化合物。该过程由方程式1概括，方程式1未针对木质素、纤维素或其他生物质原料的任何特定类型、量或比率加以配平。因此，方程式1和2归纳了图1中所示过程的多用性并示出了含碳、氢和氧的有机原料向甲烷、氢和截存碳的有价值供给源的定性转化。Finally, such wastes are heated sufficiently in an anoxic environment to release the desired gases, carbon and solid residues such as mineral oxides and other compounds. This process is outlined by Equation 1, which is not balanced for any particular type, amount or ratio of lignin, cellulose or other biomass feedstock. Thus, Equations 1 and 2 summarize the versatility of the process shown in Figure 1 and illustrate the qualitative conversion of organic feedstocks containing carbon, hydrogen, and oxygen to valuable supplies of methane, hydrogen, and sequestered carbon.

C_xH_yO_z+热→CH₄+H₂+CO₂+CO                  方程式1C_x H_y O_z + heat → CH₄ +H₂ +CO₂ +CO Equation 1

CH₄+▲H_298K→2H₂+C  (▲H_298K＝79.4kJ/mol) 方程式2CH₄ +▲H_298K → 2H₂ +C (▲H_298K ＝79.4kJ/mol) Equation 2

图2中所示为用于生物质废弃物向气体如甲烷、氢、二氧化碳和一氧化碳的快速转化的系统实施方案。在运行中，旋转管214通过合适的减速系统204和206由发动机202驱动，发动机202可以是旋转式发动机、活塞发动机或涡轮发动机，这取决于系统的大小和所需的生产能力。发动机202优选由燃料调节、喷射和点火系统202供以燃料，如美国专利申请08/785,376中所公开，该申请通过引用并入本文中。来自发动机冷却系统和/或排气的废热优选通过螺旋形热交换管道系统244和245的逆流弯头被转移给料斗250中的材料，螺旋形热交换管道系统244和245在从发动机202取得最大热回收量的相应区处接到料斗250。Shown in Figure 2 is an embodiment of a system for the rapid conversion of biomass waste to gases such as methane, hydrogen, carbon dioxide and carbon monoxide. In operation, the rotating tube 214 is driven by a motor 202, which may be a rotary, piston or turbine engine, through suitable reduction systems 204 and 206, depending on the size of the system and the desired production capacity. The engine 202 is preferably fueled by a fuel regulation, injection and ignition system 202 as disclosed in US Patent Application Serial No. 08/785,376, which is incorporated herein by reference. Waste heat from the engine cooling system and/or exhaust is transferred to the material in the hopper 250, preferably through the counterflow bends of the helical heat exchange tubing 244 and 245, which takes maximum heat from the engine 202. The corresponding zone of heat recovery volume is connected to the hopper 250 .

取决于转化器的大小，减速部件如链轮和链条或主动齿轮206及轴承支承组件208和212优选通过扭矩传输绝热器210与旋转管214热绝缘。旋转管214在相反端处通过如图所示绝缘轴承和支承组件224和226得到类似支承和热绝缘。绝缘体包230提供绝缘以防止轴承212和其他需要保护以免于受热的区域取得辐射和传导热。Depending on the size of the converter, reduction components such as sprockets and chains or drive gear 206 and bearing support assemblies 208 and 212 are preferably thermally insulated from rotating tube 214 by torque transmission insulator 210 . The rotating tube 214 is similarly supported and thermally insulated at the opposite end by insulating bearing and support assemblies 224 and 226 as shown. The insulator pack 230 provides insulation to prevent the bearings 212 and other areas requiring protection from heat from gaining radiant and conductive heat.

如方程式1和2所概括的那样生成的甲烷和/或氢和/或一氧化碳中的相对较小一部分被递送到发动机202和通过控制阀222递送到燃烧室组件220的燃烧器喷嘴，如图2中所示。提供足够的空气以确保存在的燃料值的完全燃烧，使得两种应用中的有害排放均极小。热的燃烧产物流动通过螺旋形热交换管道系统216，以向在如图所示旋转管214的外部上的翅片218的推挤作用下以逆流方向行进的有机材料传递热。A relatively small portion of the methane and/or hydrogen and/or carbon monoxide produced as summarized by Equations 1 and 2 is delivered to the engine 202 and to the combustor nozzles of the combustor assembly 220 through the control valve 222, as shown in FIG. 2 shown in . Sufficient air is provided to ensure complete combustion of the fuel values present such that harmful emissions are minimal in both applications. The hot combustion products flow through the helical heat exchange tubing 216 to transfer heat to the organic material traveling in a counter-current direction under the push of fins 218 on the exterior of the rotating tube 214 as shown.

优选提供渐进地减小的螺纹218间距和/或减小旋转管214与固定管236间的横截面积，以不断地压实所夹带的固体材料，如图所示。这将提供夹带的空气和/或湿气从被所述过程加热的有机材料的逐出，因为这类气体将被迫使以与通过被加热的料斗250和进料螺杆256进给的材料逆流的方向行进，其中，进料螺杆256由合适的牵引马达252或合适的来自发动机202的传动列带动。减小螺旋输送机的螺距或减小压实的废弃物所通过的横截面还将提供致密的密封而防止通过进一步加热有机材料(包括与加入的反应性气体的反应)所产生的气体的逃逸。It is preferable to provide a progressively decreasing pitch of the threads 218 and/or reduce the cross-sectional area between the rotating tube 214 and the stationary tube 236 to continuously compact the entrained solid material, as shown. This will provide for the expulsion of entrained air and/or moisture from the organic material heated by the process, as such gases will be forced to flow counter-currently to the material being fed through the heated hopper 250 and feed screw 256. direction, wherein the feed screw 256 is driven by a suitable traction motor 252 or a suitable drive train from the engine 202 . Reducing the pitch of the screw conveyor or reducing the cross-section through which the compacted waste passes will also provide a tight seal against the escape of gases generated by further heating of the organic material including reaction with added reactive gases .

预期，本发明的全过程还可通过其他材料输送和压实措施取得，且在一些应用中使用单向推杆递送和压实系统代替所示的螺旋输送机将更便利。基本的步骤通过如下完成：压实和加热以消除空气和湿气，产生源自原料的前进材料的封堵密封，加热所述前进材料以达到解离产生所需化学衍生物(选自物质如碳、一种或多种气态烃、燃料醇和气体如乙烷、甲烷、氢和碳氧化物)的所需压力和温度条件，在利用前进材料的衍生物和/或残余物来密封或帮助密封提供以移取所需化学物质的区的区中提取所需的化学物质。优选通过自所需的化学物质随着其复原地或再生地冷却而逆流热交换和通过自选定燃料的燃烧而逆流热交换，来向行进通过这样的进程阶段的材料提供热加入，以使所得系统中的热利用最大化。It is contemplated that the overall process of the present invention can also be achieved by other means of material delivery and compaction, and that in some applications it will be more convenient to use a unidirectional push rod delivery and compaction system instead of the screw conveyor shown. The basic steps are accomplished by compacting and heating to eliminate air and moisture, creating a plug seal of the advancing material from the feedstock, heating the advancing material to achieve dissociation to produce the desired chemical derivatives (selected from substances such as carbon, one or more gaseous hydrocarbons, fuel alcohols, and gases such as ethane, methane, hydrogen, and carbon oxides), when utilizing derivatives and/or residues of advancing materials to seal or assist in sealing Provide a zone to pipette the desired chemical from the zone to extract the desired chemical. Heat addition is preferably provided to materials traveling through such process stages by counter-current heat exchange from the desired chemical species as it cools restoratively or regeneratively and by counter-current heat exchange from the combustion of selected fuels so that Heat utilization in the resulting system is maximized.

可以提供相对较长时间的运行而大大减少碳的产生，为使所产生的化学物质获得所需的碳-氢比率，这可能是优选的。这种长时间运行可以间歇性地提供，例如在有意产生碳以在所需化学物质的收集之前帮助密封所述区和/或此收集之后帮助密封所述区的时间之间。这是本发明的一些实施方案的特点，且其使得碳可以作为流体的组成部分而被输送，这些流体由管道递送至储存器(包括枯竭气藏的复压)、至工厂以制造碳增强的耐用品、和用于其他目的。在相继逐出空气和湿气之后，生物质材料被转化为方程式1中所示的产品气体和量低得多的固体残渣。在许多情况下，固体残渣的量为有机废弃物的初始质量的约2至10％。这类残渣是痕量矿物的重要来源，其优选用来使土壤恢复元气和确保健康森林的补植立木、花园、水产养殖和/或其他地被的快速生长。这将加快温室气体的减少、碳和氢的截存及经济的发展。重新造林区域用作木质纤维素的可持续源以如本文中所公开的那样连续地生产可再生的甲烷、氢和截存碳。Relatively long runs can be provided with substantially reduced carbon production, which may be preferred in order to obtain the desired carbon-hydrogen ratios for the chemicals produced. Such extended operation may be provided intermittently, for example between times when carbon is intentionally generated to help seal the zone prior to collection of the desired chemical species and/or after such collection. This is a feature of some embodiments of the present invention, and it allows carbon to be transported as an integral part of fluids delivered by pipelines to storage (including repressurization of depleted gas reservoirs), to plants to manufacture carbon-enhanced durable goods, and for other purposes. After successive expulsion of air and moisture, the biomass material is converted to product gas as shown in Equation 1 and a much lower amount of solid residue. In many cases, the amount of solid residue is about 2 to 10% of the original mass of organic waste. Such residues are an important source of trace minerals that are preferably used to rejuvenate soil and ensure rapid growth of replanted stumps, gardens, aquaculture and/or other ground cover for healthy forests. This will accelerate the reduction of greenhouse gases, the sequestration of carbon and hydrogen and the development of the economy. The reforested area is used as a sustainable source of lignocellulose to continuously produce renewable methane, hydrogen and sequestered carbon as disclosed herein.

在具有较大单元和高生产能力的系统型式中，可使来自燃烧器组件220的燃烧气体在管螺纹216内循环，管螺纹216被构造为通过管214中的孔与螺纹管218相连，以提供从燃烧室220向沿着密闭管236内的螺纹218的外侧行进的原料材料的更快速传热。让自加热的有机原料通过热解离过程释放的气体如甲烷、氢和二氧化碳进入螺旋翅片238与绝缘管241之间的环形空间中，以以与被旋转管组件214加热的原料的流动成逆流的方向流动。这将提供进一步的热量保存，因为热将被再生性地加给管236内的原料，这些原料被渐进地压实并因传热而解离，从而增强压力的产生，如图所示。In system versions with larger units and high production capacities, combustion gases from burner assembly 220 may be circulated within pipe threads 216 configured to connect with threaded pipe 218 through holes in pipe 214 to More rapid heat transfer is provided from the combustion chamber 220 to the feedstock material traveling outside along the threads 218 within the closed tube 236 . Gases such as methane, hydrogen, and carbon dioxide released by the thermal dissociation process of the self-heating organic feedstock enter the annular space between the spiral fins 238 and the insulating tube 241 to align with the flow of the feedstock heated by the rotating tube assembly 214. flow in the countercurrent direction. This will provide further heat conservation as heat will be regeneratively added to the feedstock within tube 236 which is progressively compacted and dissociated by heat transfer thereby enhancing pressure development as shown.

行进通过管214的内部和/或管翅片216和/或218到达料斗区的燃烧气体如水蒸汽、氮气、氧气和二氧化碳进入螺旋形传热管道246，以向行进通过料斗250的原料材料提供进一步的逆流能量添加，如图所示。行进通过孔230和管236与管241之间的环形区域和/或空心翅片238到达料斗250区的所产生气体如甲烷、氢和二氧化碳和/或一氧化碳在管道系统248中循环，管道系统248缠绕在螺旋形管道系统246邻近以向行进向旋转管螺旋输送机214的材料有效地逆流传热，如图所示。绝缘体242和260防止热损失到外部。Combustion gases, such as water vapor, nitrogen, oxygen, and carbon dioxide, traveling through the interior of tube 214 and/or tube fins 216 and/or 218 to the hopper area enter spiral heat transfer tube 246 to provide further The countercurrent energy is added, as shown in the figure. Resulting gases such as methane, hydrogen, and carbon dioxide and/or carbon monoxide traveling through holes 230 and the annular region between tubes 236 and 241 and/or hollow fins 238 to the hopper 250 zone are circulated in a piping system 248, which Wrapped adjacent to the helical tubing 246 to effectively transfer heat countercurrently to material traveling to the rotating tube auger 214, as shown. The insulators 242 and 260 prevent heat loss to the outside.

可能产生的产品气体如二氧化碳和一氧化碳的混合物通过压力摆动或温度吸收和/或图4中所示的系统与甲烷和/或氢分离。这样的产品气体混合物通过控制旋转输送机214的旋转速度和因此传递向热解离阶段的固体的压实以高于所需压力适宜裕度的压力而提供。A mixture of possible product gases such as carbon dioxide and carbon monoxide is separated from methane and/or hydrogen by pressure swing or temperature absorption and/or the system shown in FIG. 4 . Such a product gas mixture is provided by controlling the rotational speed of the rotary conveyor 214 and thus the compaction of the solids passed to the thermal dissociation stage at a pressure with a suitable margin above the desired pressure.

这将提供热能向压力能的高效转化，因为形成的所需气体的体积比初始固体体积远大得多。在运行中，压力传感器270向过程控制器272发送压力数据以保持进料输送机256、挤压输送机214的速度及燃烧室组件220的发热量，以获得所需的生产能力、转化温度和递送的产品气体的压力。压力调节器274提供产品气体从再生转化器200的递送的最后调整。This will provide an efficient conversion of thermal energy to pressure energy, since the required gas volume formed is much larger than the initial solid volume. In operation, pressure transducer 270 sends pressure data to process controller 272 to maintain the speed of feed conveyor 256, squeeze conveyor 214, and heat generation of combustor assembly 220 to achieve desired production capacity, conversion temperature and The pressure of the delivered product gas. Pressure regulator 274 provides final adjustments in the delivery of product gas from regenerative converter 200 .

本公开的一个方面是将低成本热转化为势能作为储能、利用这样的压力促进分离过程和能量再生。加压的混合物在保持选定气体的所需加压的同时分离。精炼品质气体的这种加压供给用来为发动机包括内燃机和具有外部热供应的发动机提供动力。An aspect of the present disclosure is the conversion of low cost heat into potential energy as energy storage, utilizing such pressure to facilitate separation processes and energy regeneration. The pressurized mixture is separated while maintaining the desired pressurization of the selected gas. This pressurized supply of refinery quality gas is used to power engines including internal combustion engines and engines with external heat supplies.

还采用这样的能量转化、精炼和加压来通过管道或加压罐车或通过液化向远方市场递送精炼气体及储存。还预期在某些地区与包括09/969,860在内的共同待决专利申请的各种实施方案中的一个或多个一起运行，这些专利申请通过引用并入本文中。Such energy conversion, refining and pressurization are also used to deliver refined gas to distant markets and storage by pipeline or pressurized tank trucks or by liquefaction. It is also contemplated to operate in certain territories with one or more of the various embodiments of co-pending patent applications, including 09/969,860, which are incorporated herein by reference.

废弃物的氢辅助气化的现有技术方法的主要缺点是需要耐高压、耐热和昂贵的设备。如图所示，本发明的实施方案提供管状构造的自增强结构。增强由在模块结构中组合热交换、增强、刚性化、传输和耐热好处的螺旋形增强结构提供，所述模块结构可通过快速组装过程而构建。这将在很大程度上加快废弃物管理中所需改进措施的推广应用并比过去的方法降低递送系统成本。The main disadvantages of the prior art methods of hydrogen assisted gasification of waste are the need for high pressure, heat resistant and expensive equipment. As shown, embodiments of the present invention provide self-reinforcing structures in a tubular configuration. Reinforcement is provided by a helical reinforcement structure that combines the benefits of heat exchange, reinforcement, rigidification, transmission and heat resistance in a modular structure that can be constructed through a rapid assembly process. This will greatly speed up the deployment of needed improvements in waste management and reduce delivery system costs compared to past methods.

这将提供碳化合物如二氧化碳或一氧化碳与气体如甲烷和/或氢的有效分离。如图4中所示，产品气体的混合物通过管404递送以暴露于压力容器402中的水或其他吸收剂流体选择，以选择性地分离二氧化碳和/或一氧化碳。This will provide an efficient separation of carbon compounds such as carbon dioxide or carbon monoxide from gases such as methane and/or hydrogen. As shown in FIG. 4 , the mixture of product gases is delivered through pipe 404 to be exposed to water or other absorbent fluid options in pressure vessel 402 to selectively separate carbon dioxide and/or carbon monoxide.

甲烷和/或氢因此在压力容器402中所保持的压力下递送到收集管408。在吸收二氧化碳和/或一氧化碳之后，加压的吸收流体通过410递送到喷嘴歧管426以便递送到如图所示热交换器如414、416、418、420、422、424等，在这里，来自发动机202的排气的热可与燃烧器444燃烧一部分产品气体和废气(如通过加压流体的后续膨胀经458释放的一氧化碳)所释放的热一道被递送到所示热交换器。也可通过太阳能收集器442或在风能或波能资源充裕的地方使用风能或波能通过电阻或感应加热器而供给附加的热。经加热的流体然后膨胀通过如图所示涡轮430、432、434、436、438、440等以回收和/或转化能量，从而进一步改进总体效率。Methane and/or hydrogen are thus delivered to collection pipe 408 at the pressure maintained in pressure vessel 402 . After absorbing carbon dioxide and/or carbon monoxide, pressurized absorption fluid is delivered through 410 to nozzle manifold 426 for delivery to heat exchangers as shown, such as 414, 416, 418, 420, 422, 424, etc., here from Heat from the exhaust of engine 202 may be delivered to the heat exchanger as shown along with heat released by combustor 444 from combusting a portion of the product gas and exhaust gases, such as carbon monoxide released via 458 by subsequent expansion of the pressurized fluid. Additional heat may also be supplied by solar collectors 442 or by resistive or induction heaters using wind or wave energy where resources are plentiful. The heated fluid is then expanded through turbines 430, 432, 434, 436, 438, 440, etc. as shown to recover and/or convert energy, further improving overall efficiency.

还通过合适的发电机如交流发电机280和/或交流发电机428提供发电的总体效率的附加改进。优选利用氢来冷却这些发电机而减少风力损失。在实现这些功能后，氢然后被用作发动机202的燃料或者用作燃烧室444和/或220中的无碳燃料。Additional improvement in the overall efficiency of power generation is also provided by suitable generators such as alternator 280 and/or alternator 428 . Hydrogen is preferably used to cool these generators to reduce wind losses. After performing these functions, the hydrogen is then used as fuel for engine 202 or as a carbon-free fuel in combustion chamber 444 and/or 220 .

自典型的有机废弃物如葡萄糖、木质素和纤维素原料通过所述实施方案生产甲烷的总反应的一般性概括在方程式3中示出。A general summary of the overall reaction to produce methane from typical organic waste such as glucose, lignin, and cellulosic feedstocks by the described embodiments is shown in Equation 3.

C₆H₁₂O₆+热→3CH₄+3CO₂                  方程式3C₆ H₁₂ O₆ + heat → 3CH₄ + 3CO₂ equation 3

在一些应用中，优选通过原料的衍生物的电解产生氧来减少或消除二氧化碳的产生，这在共同待决的专利申请中有公开。这类材料特别是用氢的氢气化及存在的过剩的碳也可在同时或后续的过程步骤中加以控制以产生乙烷。在需要将受损森林快速转化为通过管道装运至远方市场的甲烷、乙烷和氢的加压供给源并然后利用这些管道来根据所需的森林抚育间伐速率、收获计划和维护程序以降低的速率继续递送这类气体的情况下，这种化学过程变型将是有利的。In some applications, it may be preferable to reduce or eliminate carbon dioxide production by electrolysis of derivatives of the feedstock to generate oxygen, as disclosed in co-pending patent applications. Hydrogenation of such materials, especially with hydrogen, and the presence of excess carbon can also be controlled in a simultaneous or subsequent process step to produce ethane. Where there is a need to rapidly convert damaged forests into pressurized supplies of methane, ethane, and hydrogen shipped via pipelines to distant markets and then use these pipelines to reduce costs in accordance with desired forest tending and thinning rates, harvest schedules, and maintenance procedures This chemical process modification would be advantageous where the rate at which such gases continue to be delivered.

这种方法确立的管道输送能力成为一种重要的储存系统，以满足市场需求的日常和季节性变化。通常需要所得的管道气体在通过图2和图4的实施方案移除二氧化碳、颗粒物、灰分、二氧化硫和水后提供约900BTU/scf的输出。The pipeline capacity established by this approach becomes an important storage system to meet daily and seasonal changes in market demand. The resulting pipeline gas is typically required to provide an output of about 900 BTU/scf after removal of carbon dioxide, particulate matter, ash, sulfur dioxide and water by the embodiments of FIGS. 2 and 4 .

对于大多数废弃物，不再循环氢时的原始输出在350至650BTU/scf范围内，热值较低。热值的提高可通过分解过程中压力和温度的多种选择或者通过增加氢再循环到239处的反应区的速率来达到。但共同待决的专利申请公开了火花喷射(SparkInjection)技术以使得实现自内燃机的满额定功率生产，燃料选择从250BTU/scf的气体混合物到液体柴油不等。For most wastes, the raw output without recycling hydrogen is in the range of 350 to 650 BTU/scf, with a lower calorific value. Increases in heating value can be achieved by various choices of pressure and temperature during decomposition or by increasing the rate at which hydrogen is recirculated to the reaction zone at 239 . But a co-pending patent application discloses Spark Injection technology to enable full rated power production from an internal combustion engine, with fuel options ranging from a 250 BTU/scf gas mixture to liquid diesel.

通过图2的实施方案在约1,000PSI和1025°F(69个大气压，550℃)下的运行产生的气体混合物如表1中所示随被转化的废弃物的类型、停留时间和相关运行参数而异。一种新的制剂可实现用压缩点火代替柴油燃料并包含在活性炭/甲醇悬浮体中中的吸附的氢。The gas mixture produced by operation of the embodiment of FIG. 2 at approximately 1,000 PSI and 1025°F (69 atmospheres, 550°C) varies as shown in Table 1 with the type of waste being converted, residence time, and associated operating parameters. varies. A new formulation enables compression ignition to replace diesel fuel and contains adsorbed hydrogen in an activated carbon/methanol suspension.

这样的气体混合物可快速产生并可补充以较高能量的组分如甲醇、碳/甲醇悬浮体或丙烷等，以使所得以氢燃烧为特征的燃烧混合物在组合燃料应用中获得实际上任何所需的能含量。常常需要将反应产生的氢和/或甲烷通过歧管239以足以产生所需甲烷/乙烷比率的速率喷射而重新引导进反应区中以提供管道质量的气体或用于化学合成的原料。Such gas mixtures can be produced rapidly and can be supplemented with higher energy components such as methanol, carbon/methanol suspensions, or propane, etc., so that the resulting combustion mixture, characterized by hydrogen combustion, achieves virtually any desired value in combined fuel applications. required energy content. It is often desirable to redirect hydrogen and/or methane produced by the reaction into the reaction zone by injecting it through manifold 239 at a rate sufficient to produce the desired methane/ethane ratio to provide pipeline quality gas or feedstock for chemical synthesis.

表1Table 1

  气体产物gas product  森林废弃物Forest waste  市政固体废弃物Municipal solid waste  粪肥manure  氢气(H₂)Hydrogen (H₂ )  22(体积％)22 (volume%)  33(体积％)33 (volume%)  20(体积％)20 (volume%)  甲烷(CH₄)Methane (CH₄ )  6060  5353  6161  乙烷(C₂H₆)Ethane (C₂ H₆ )  1717  1111  1818  一氧化碳carbon monoxide  1 1  2 2  1 1

在一些情况下，优选自图2的实施方案提供甲醇作为易于储存和运输的液体燃料及化学前体。甲醇或“木醇”可通过加热木质纤维素废弃物经部分燃烧或通过缺氧加热过程而提取。方程式4和5概括了通过选择不同的缺氧操作温度、压力和催化剂可获得的甲醇输出。In some cases, preferred embodiments from FIG. 2 provide methanol as a liquid fuel and chemical precursor that is easily stored and transported. Methanol or "wood alcohol" can be extracted by heating lignocellulosic waste through partial combustion or through an anoxic heating process. Equations 4 and 5 summarize the methanol output achievable by choosing different anoxic operating temperatures, pressures and catalysts.

C₆H₁₂O₆+热→6CO+6H₂                 方程式4C₆ H₁₂ O₆ + heat → 6CO + 6H₂ equation 4

6CO+6H₂→3CH₃OH+3CO                 方程式56CO+6H₂ →3CH₃ OH+3CO Equation 5

在较高的进给速率和/或较低的燃烧室220热释放速率下，物料不会达到产生方程式1中所示气体的较高温度，因此该过程产生甲醇。优选通过冷却甲醇蒸气以形成液体甲醇而从甲醇中分离出一氧化碳并利用分离出的一氧化碳作为发动机202的燃料、通过燃烧器组件220的燃烧释放热及通过与水如方程式6中所概括的那样反应形成氢。通过方程式6中所概括的反应产生的氢可被用来如方程式5中所示那样产生甲醇、改善发动机202的运行、提高转化器200中甲醇和/或乙烷的收率和/或如图所示作为转化器200中的加热燃料。At higher feed rates and/or lower combustor 220 heat release rates, the feed does not reach the higher temperatures required to produce the gas shown in Equation 1, so the process produces methanol. Carbon monoxide is preferably separated from methanol by cooling methanol vapor to form liquid methanol and the separated carbon monoxide is utilized as fuel for engine 202, by combustion of combustor assembly 220 to release heat, and by reaction with water as outlined in Equation 6 hydrogen is formed. The hydrogen produced by the reactions outlined in Equation 6 can be used to produce methanol as shown in Equation 5, improve the operation of engine 202, increase the yield of methanol and/or ethane in converter 200, and/or as shown in Equation 5. Shown as heating fuel in reformer 200 .

CO+H₂O→H₂+CO₂                 方程式6CO+H₂ O→H₂ +CO₂ Equation 6

应指出，本文中示出的每个反应体系可通过均相和非均相催化剂的使用及适应性控制的应用进一步改善，以改善或优化所需的结果。作为示例，关于歧管239和气提器端口240之间的反应区，预期使用这样的催化剂选择：所述催化剂选择将通过促进氢构建反应性组分的作用的反应而增强甲烷和乙烷的形成，所述反应性组分合成形成甲烷和乙烷。催化剂包括三价铬及其他具有稀土组分的陶瓷、铂族金属、nobelized镍和过渡金属的金属间化合物都是可应用的。与现有技术方法相比，这出乎意料并显著地降低了设备成本和复杂性。类似地，除通过甲烷的部分氧化产生甲醇外，还预期利用镧系-钌制剂、Fischer-Tropsch催化剂及铜、铜金属间化合物和/或铜合金来增强甲醇自一氧化碳和氢的合成。It should be noted that each of the reaction systems presented herein can be further refined through the use of homogeneous and heterogeneous catalysts and the application of adaptive controls to improve or optimize the desired outcome. As an example, with respect to the reaction zone between manifold 239 and stripper port 240, it is contemplated that a catalyst selection will be used that will enhance the formation of methane and ethane by promoting the reaction of hydrogen to build up the action of reactive components , the reactive components are synthesized to form methane and ethane. Catalysts including trivalent chromium and other ceramics with rare earth components, platinum group metals, nobelized nickel and intermetallics of transition metals are applicable. This unexpectedly and significantly reduces equipment cost and complexity compared to prior art methods. Similarly, in addition to the production of methanol by partial oxidation of methane, the use of lanthanide-ruthenium formulations, Fischer-Tropsch catalysts, and copper, copper intermetallics, and/or copper alloys is also expected to enhance the synthesis of methanol from carbon monoxide and hydrogen.

图3示出了甲醇从一氧化碳中的分离及甲醇通过输送泵298向市场的装运。在运行中，实施方案300优选引入较大密度与较轻组分的涡流分离并让一氧化碳和甲醇的混合物从再生泵/马达312通过管304进入容器302。如果输送压力不足以获得所需的输送速率，则泵/马达312将对这类蒸气提供泵送作用，而如果所需的输送压力低于来自图2的系统或另一合适的转化器320的供给压力，则泵/马达312将提供压力能的回收。FIG. 3 shows the separation of methanol from carbon monoxide and its shipment to market by transfer pump 298 . In operation, embodiment 300 preferably introduces vortex separation of denser and lighter components and allows a mixture of carbon monoxide and methanol to enter vessel 302 from regeneration pump/motor 312 through pipe 304 . The pump/motor 312 will provide pumping action on such vapors if the delivery pressure is insufficient to obtain the desired delivery rate, whereas if the required delivery pressure is lower than that from the system of FIG. 2 or another suitable converter 320 Supply pressure, the pump/motor 312 will provide recovery of pressure energy.

使甲醇冷凝的冷却由象征性地示出的热交换回路306提供，热交换回路306优选利用地下水或冷却塔流体作为散热器。冷却回路306中的水优选由泵296保持在比进入室302的蒸气高的压力下，因此，冷却回路的任何密闭失效都不会引起冷却水污染。从324离开分离器302的冷却水可以用作热水供给源或者返回到地下水体系、冷却塔或蒸发塘，这随应用而异。在充分冷却气体混合物而在容器302的壁附近产生密度较大的甲醇蒸气和液滴后，密度较小的一氧化碳通过中心管被提取。冷凝的甲醇可通过泵298递送以进一步加工以移除水和/或吸收的气体，这取决于所需的纯度。Cooling to condense the methanol is provided by a symbolically shown heat exchange loop 306, which preferably utilizes groundwater or cooling tower fluid as a heat sink. The water in the cooling circuit 306 is preferably maintained by the pump 296 at a higher pressure than the vapor entering the chamber 302, so any failure of the cooling circuit to seal will not cause contamination of the cooling water. Cooling water exiting separator 302 from 324 can be used as a hot water supply or returned to a groundwater system, cooling tower or evaporation pond, depending on the application. After cooling the gas mixture sufficiently to produce denser methanol vapor and liquid droplets near the walls of vessel 302, less dense carbon monoxide is extracted through the base tube. The condensed methanol can be delivered by pump 298 for further processing to remove water and/or absorbed gases, depending on the desired purity.

甲醇以及甲烷、乙烷和氢的管道气体混合物可以通过相同或附加的管道可互相交换地装运到市场。在使用相同管道的情况下，要从一类化学品转换为另一类化学品时，优选在重新注入下一待递送物之前通过已经验证的技术例如使用压力推进的分离段塞或通过抽空来清扫管道。Methanol and pipeline gas mixtures of methane, ethane and hydrogen can be interchangeably shipped to market via the same or additional pipelines. Where the same tubing is used, switching from one type of chemical to another is preferably done by proven techniques such as the use of a pressure-actuated separation slug or by evacuation prior to reinjection of the next product to be delivered. Clean the pipes.

图5示出了与图1和2的系统相似的一个实施方案，其包含压实筒500以转化生物质如锯屑、粪肥和木屑。该系统的运行与图2的实施方案基本上相同，不同的是生物质的压实由往复推杆循环地提供。推杆活塞502在液压缸506的迫使下在固定缸518中往复而压实生物质，这些生物质已通过在料斗250中逆流热交换而经干燥和预热。Figure 5 shows an embodiment similar to the system of Figures 1 and 2, which includes a compaction drum 500 to convert biomass such as sawdust, manure and wood chips. The operation of the system is essentially the same as the embodiment of Figure 2, except that the compaction of the biomass is provided cyclically by a reciprocating push rod. Push rod piston 502 is forced by hydraulic cylinder 506 to reciprocate in stationary cylinder 518 to compact the biomass that has been dried and preheated by countercurrent heat exchange in hopper 250 .

当推杆502处于所示位置时，生物质由输送机256装载进缸518中。发动机202驱动液压泵504而通过管线510和511递送加压工作流体以操纵缸506。在前进行程中，推杆502将生物质压成密实的物料，随着其绕过加热器516的锥形体512移动，该密实的物料被进一步压实，锥形体512可以是固定的或旋转的以提高生产能力和在生物质行进通过转化过程时保持生物质的压实状态。通常在249位置处的众多管可允许空气和水蒸汽的逐出，同时还用作材料止回阀以防止在推杆502的作用下前进的材料的回流。响应控制器272的协调和控制，与行进通过螺旋形热交换器翅片216和218的来自燃烧器组件220的燃烧气体的逆流热交换将充分提升生物质的温度，以引起方程式1、3、4和5中所概括的解离反应。When push rod 502 is in the position shown, biomass is loaded into cylinder 518 by conveyor 256 . Engine 202 drives hydraulic pump 504 to deliver pressurized working fluid through lines 510 and 511 to actuate cylinder 506 . During the forward stroke, the push rod 502 compacts the biomass into a compacted mass which is further compacted as it moves around the cone 512 of the heater 516, which may be stationary or rotating To increase productivity and maintain compaction of the biomass as it travels through the conversion process. A multitude of tubes, generally at 249, allow for the expulsion of air and water vapor while also acting as a material check valve to prevent backflow of material advancing under the action of push rod 502. In response to the coordination and control of controller 272, countercurrent heat exchange with the combustion gases from burner assembly 220 traveling through helical heat exchanger fins 216 and 218 will raise the temperature of the biomass sufficiently to cause equations 1, 3, Dissociation reactions outlined in 4 and 5.

因此，有机物质被转化为流体如甲烷、乙烷、丙烷、甲醇、乙醇、氢、硫化氢、一氧化碳和二氧化碳，并通过移除有害含量的硫化氢、一氧化碳和二氧化碳得到改进以替代化石燃料，所述移除通过图4的再生性实施方案或通过其他合适的选择性移除过程如压力摆动吸附、温度摆动吸附、溶液吸收和膜分离进行。这由与源如一部分来自这类流体的一种或多种燃料组分的燃烧的逆流热交换、在生产之前、过程中和之后从较高温度到较低温度的物质的热交换及通过与能量转化装置如内燃机、外燃机、膨胀马达和燃料电池的热交换提供。Thus, organic matter is converted into fluids such as methane, ethane, propane, methanol, ethanol, hydrogen, hydrogen sulfide, carbon monoxide and carbon dioxide and improved to replace fossil fuels by removing harmful levels of hydrogen sulfide, carbon monoxide and carbon dioxide, so The removal is performed by the regenerative embodiment of Figure 4 or by other suitable selective removal processes such as pressure swing adsorption, temperature swing adsorption, solution absorption and membrane separation. This consists of countercurrent heat exchange with a source such as the combustion of one or more fuel components derived in part from such fluids, heat exchange with substances from higher to lower temperatures before, during and after production, and by contact with Heat exchange provision for energy conversion devices such as internal combustion engines, external combustion engines, expansion motors and fuel cells.

图6示出了将甲烷(来自填埋场、污水处理厂、废弃物处置操作(包括基于图1、2、3、4和5的实施方案的那些)以及其他甲烷源)如方程式2中所概括的那样转化为氢和碳的过程步骤60。氢的燃烧是烃如汽油、燃料酒精、甲烷和柴油燃料的七到九倍。这使得其中喷射和燃烧氢或以氢为特征的燃料如氢与甲烷、氢与甲醇或氢与一氧化碳的混合物的涡轮发动机、燃烧转子发动机和往复式发动机的运行能够具有提高的效率和较少的碳排放或无碳排放。Figure 6 shows the conversion of methane (from landfills, sewage treatment plants, waste disposal operations (including those based on the embodiments of Figures 1, 2, 3, 4, and 5), and other methane sources) as shown in Equation 2. The conversion to hydrogen and carbon process step 60 is outlined. Hydrogen burns seven to nine times more than hydrocarbons such as gasoline, fuel alcohol, methane, and diesel fuel. This enables the operation of turbine engines, combustion rotary engines, and reciprocating engines in which hydrogen or fuels characterized by hydrogen, such as mixtures of hydrogen and methane, hydrogen and methanol, or hydrogen and carbon monoxide, are injected and burned with increased efficiency and less Carbon emissions or no carbon emissions.

通过这样的运行带来的热效率改善对于间歇燃烧式发动机如燃烧转子发动机和往复式两冲程或四冲程发动机如202来说特别重要，由此将在接近上死点处、在上死点处或在上死点后提供直接喷射和/或点火，以减少或避免压缩过程中的热损失和负功。在发动机的动力冲程过程中，这将确保燃料势能以远远更高的效率转化为功能。因此，通过在燃烧室中燃烧过剩空气内快速燃烧的以氢为特征的燃料，将比具有采用丙烷、天然气或柴油燃料的常规布置的发动机获得显著更高的运行效率。The improvement in thermal efficiency brought about by such operation is particularly important for intermittent combustion engines such as combustion rotary engines and reciprocating two-stroke or four-stroke engines such as the 202, whereby the Direct injection and/or ignition are provided after top dead center to reduce or avoid heat loss and negative work during compression. During the engine's power stroke, this will ensure that the potential energy of the fuel is converted to function with far greater efficiency. Thus, by burning a fuel characterized by rapid combustion hydrogen within excess air in the combustion chamber, significantly higher operating efficiencies will be obtained than with conventional arrangements employing propane, natural gas or diesel fuel.

在图6的步骤62中，已通过图1、2、3、4和5的实施方案产生并净化至所需程度的甲烷由散装运载工具或管道输送至合适的目的地如工业园。甲烷然后在步骤64中通过与解离产生的氢和/或碳逆流热交换而从环境温度预热至合适的温度，例如约1200℃(2200°F)。在步骤66中，通过辐射和/或与经加热的物质如石墨、氧化铁、氧化铝、氧化镁、各种碳化物或其他陶瓷接触而提供足够的热加入，以使碳沉淀在这类经加热的物质上或附近并如方程式2所概括的那样释放氢。步骤68提供这类热氢的收集以与关于步骤64所述的前进的甲烷逆流热交换。在步骤70中，通过甲烷的解离而形成的碳以沉积物或以从步骤66中使用的经加热的物质剥离或剥落的粉末或片状材料收集。In step 62 of Figure 6, methane that has been produced and purified to the desired degree by the embodiments of Figures 1, 2, 3, 4 and 5 is transported by bulk carrier or pipeline to a suitable destination such as an industrial park. The methane is then preheated in step 64 from ambient temperature to a suitable temperature, such as about 1200°C (2200°F), by countercurrent heat exchange with the hydrogen and/or carbon produced by the dissociation. In step 66, sufficient heat is added by radiation and/or contact with heated substances such as graphite, iron oxide, alumina, magnesia, various carbides, or other ceramics to precipitate carbon on such heated materials. Hydrogen is released on or near the heated mass and as outlined in Equation 2. Step 68 provides collection of such hot hydrogen for countercurrent heat exchange with the advancing methane as described with respect to step 64 . In step 70 , the carbon formed by the dissociation of methane is collected as a deposit or as a powder or flake material peeled off or exfoliated from the heated mass used in step 66 .

在可供选择的方案中，步骤72燃烧步骤66中共同产生的碳和/或氢的一部分，以加热或帮助增热而产生甲烷的解离所需的压力和温度。用于实现步骤66的甲烷解离的替代加热源包括集光太阳能、传导性陶瓷如石墨或氧化锆的电感应加热、这类基材的电阻加热和这类基材自合适的白炽光源的辐射加热、等离子体加热的各种变型(包括涉及氢和/或甲烷的等离子体)和/或通过燃烧合适的燃料(包括甲烷或甲烷解离产物如氢和/或碳)。In an alternative, step 72 combusts a portion of the carbon and/or hydrogen co-produced in step 66 to heat or assist in heating to generate the pressure and temperature required for methane dissociation. Alternative heating sources for effecting the methane dissociation of step 66 include concentrated solar energy, electric induction heating of conductive ceramics such as graphite or zirconia, resistive heating of such substrates, and radiation of such substrates from suitable incandescent light sources Variations of heating, plasma heating (including plasmas involving hydrogen and/or methane) and/or by burning suitable fuels (including methane or methane dissociation products such as hydrogen and/or carbon).

用于步骤62、64、66、68、70和/或72中提供的方法的装置包括各种类型的流化床、螺旋或活塞感应流动反应器、具有碳收集措施和特征的等离子体室、和改进的炭黑生产炉。本发明的一些实施方案的特别重要的好处包括以比解离水所需低得多的能量添加自烃如甲烷生产氢并共同产生有价值的碳形式。烃原料的解离产生氢和产品如美国专利申请09/370,431中的公开所取得的将提供碳产品和氢的高组合价值。图7示出了利于所述方法的另一特别有效的系统。Apparatus for the methods provided in steps 62, 64, 66, 68, 70 and/or 72 include various types of fluidized beds, spiral or plug induction flow reactors, plasma chambers with carbon capture measures and features, and improved carbon black production furnaces. Particularly important benefits of some embodiments of the present invention include the production of hydrogen from hydrocarbons such as methane and co-production of valuable carbon forms with much lower energy addition than required to dissociate water. Dissociation of hydrocarbon feedstock to produce hydrogen and products as achieved in the disclosure of US Patent Application 09/370,431 will provide a high combined value of carbon products and hydrogen. Figure 7 shows another particularly efficient system that facilitates the method.

图7示出了工艺系统700的部件。在运行中，烃如甲烷由管702递送到耐火管桶704，在耐火管桶704内，耐火的螺旋输送机710旋转以移动优选几何形状和尺寸的颗粒和/或基材材料711以接收随着甲烷被辐射、传导等加热而按方程式2中所概括的过程自甲烷解离并沉积或沉淀的碳。共同产生的氢通过中空螺旋输送机710的孔708如图所示输送到内部膛孔。因此，行进向密封件726的热氢和碳将与行进向密封件714的甲烷热交换。螺旋710用作传导和辐射热的能量交换系统，此外做机械功以快速实现方程式2所概括的反应。FIG. 7 shows components of a process system 700 . In operation, a hydrocarbon, such as methane, is delivered by pipe 702 to a refractory barrel 704, within which a refractory screw conveyor 710 rotates to move particles and/or substrate material 711 of a preferred geometry and size to receive Carbon that dissociates from methane and deposits or precipitates as methane is heated by radiation, conduction, etc. by the process outlined in Equation 2. The co-produced hydrogen is transported through the bore 708 of the hollow screw conveyor 710 to the internal bore as shown. Thus, the hot hydrogen and carbon traveling to seal 726 will exchange heat with the methane traveling to seal 714 . The helix 710 acts as an energy exchange system for conductive and radiant heat, in addition to doing mechanical work to quickly achieve the reactions outlined in Equation 2.

合适的热源706提供的热加入使得经预热的甲烷解离。还可通过在如图所示耐火的螺旋组件710的中空中心内燃烧氢来增热。氧或其他氧化剂如空气通过旋转接头718递送以用于这样的燃烧。氧优选通过空气分离或按共同待决的专利申请电解而提供。氢如图所示由导管717通过旋转接头719递送。The addition of heat provided by a suitable heat source 706 dissociates the preheated methane. Heat can also be added by burning hydrogen within the hollow center of the refractory helical assembly 710 as shown. Oxygen or other oxidizer such as air is delivered through rotary joint 718 for such combustion. Oxygen is preferably provided by air separation or electrolysis as per co-pending patent application. Hydrogen is delivered by conduit 717 through swivel 719 as shown.

取决于转化器的大小，减速部件如链轮和链条或主动齿轮732及轴承支承组件730优选通过扭矩传输绝热器组件728与旋转螺旋组件710热绝缘。用718提供轴承和旋转接头716组件的类似绝缘支承，以使从螺旋组件710的传热最小化。绝缘体包724提供传热阻断，以防止辐射和传导热损失以及保护其他需要保护以免于受热的区域。如方程式1和2所概括的那样生成的甲烷和/或氢和/或一氧化碳中的相对较小一部分被递送到与如图2中所示的202和280相似的发动机发电机组件，以提供热和电来支持包括如图所示的电动马达736、电解器和/或分离器744、泵或压缩机746和发电机712的运行。Depending on the size of the variator, reduction components such as sprockets and chains or drive gear 732 and bearing support assembly 730 are preferably thermally insulated from rotating screw assembly 710 by torque transmission insulator assembly 728 . Similar insulating support for the bearing and swivel 716 assembly is provided with 718 to minimize heat transfer from the screw assembly 710 . The insulator pack 724 provides a thermal barrier to prevent radiative and conductive heat loss as well as protect other areas that require protection from heat. A relatively small portion of the methane and/or hydrogen and/or carbon monoxide produced as outlined in Equations 1 and 2 is delivered to an engine generator assembly similar to 202 and 280 shown in FIG. 2 to provide heat and electricity to support operation including electric motor 736, electrolyzer and/or separator 744, pump or compressor 746, and generator 712 as shown.

优选提供渐进地减小的螺纹间距和/或减小用作堵塞密封件的区中旋转螺旋输送机710与固定管筒704间的横截面积，以不断地压实其内输送的固体材料，如图所示。这将迫使甲烷以与710内行进向726的碳和行进向旋转接头719的氢逆流的方向行进，如图所示。减小螺旋输送机的螺距或者减小726和714附近或726和714处的横截面以压实碳颗粒或形状还将提供致密的密封而防止氢或甲烷的逃逸。在较大的应用中，在密封件714附近的区中，螺旋输送机710可以被提供以略微反向的螺距以使得碳压缩产生有效密封而防止甲烷或氢损失。preferably providing a progressively reduced thread pitch and/or reduced cross-sectional area between the rotating screw conveyor 710 and the stationary barrel 704 in the zone acting as a plug seal to continuously compact the solid material conveyed therein, as the picture shows. This will force the methane to travel in a direction countercurrent to the carbon in 710 traveling to 726 and the hydrogen traveling to the swivel 719, as shown. Reducing the pitch of the screw conveyor or reducing the cross section near or at 726 and 714 to compact the carbon particles or shapes will also provide a tight seal against escape of hydrogen or methane. In larger applications, the screw conveyor 710 may be provided with a slightly reversed pitch in the region near the seal 714 so that carbon compression creates an effective seal against methane or hydrogen loss.

绝缘系统724利于行进向密封件714的烃如甲烷和行进向密封件726的碳和/或氢之间的高效逆流热交换。齿轮或链轮传动732与驱动马达736热绝缘，且轴承716和730被设计用于热绝缘和/或高温应用。螺旋输送机710和筒704由难熔金属或陶瓷材料如石墨、碳化物、氮化物、金属间化合物和金属氧化物制成。706处的加热可通过集光太阳能、催化或有焰燃烧、或通过电加热如等离子体、电阻或感应原理优选使用可再生电提供。空气分离器和/或电解器744产生的氧被储存在积贮器722中，经由压力调节器720递送，并在需要为解离过程提供氢的燃烧和热的生成时使用，例如在太阳、风、流水和其他可再生资源不可得到或不够时。Insulation system 724 facilitates efficient countercurrent heat exchange between hydrocarbons, such as methane, traveling to seal 714 and carbon and/or hydrogen traveling to seal 726 . Gear or sprocket drive 732 is thermally isolated from drive motor 736, and bearings 716 and 730 are designed for thermal isolation and/or high temperature applications. The screw conveyor 710 and barrel 704 are made of refractory metals or ceramic materials such as graphite, carbides, nitrides, intermetallic compounds, and metal oxides. Heating at 706 may be provided by concentrated solar energy, catalytic or flaming combustion, or by electrical heating such as plasma, resistive or inductive principles, preferably using renewable electricity. Oxygen produced by the air separator and/or electrolyzer 744 is stored in accumulator 722, delivered via pressure regulator 720, and used when needed to provide hydrogen combustion and heat generation for the dissociation process, such as in the sun, When wind, flowing water and other renewable resources are not available or sufficient.

图8示例了全过程800，其中在步骤862中光合作用提供通常含碳、氢和氧的有机材料。步骤864提供缺氧消化或热解或部分氧化以产生燃料气体如甲烷和碳的氧化物。碳的氧化物如二氧化碳与燃料气体的分离在步骤866中提供。如共同待决的专利申请中所公开的适宜的过滤器、压力摆动吸附、温度摆动吸附或选择性吸附由示意为868的系统提供。取决于经纯化的燃料气体的压力和步骤872的工艺所需的压力，采用加压器870，加压器870包括选择如电解加压、机械泵或压缩机运行，或者加压来自吸附性和/或金属氢化物系统的释放物。在步骤872中，如图所示，在最终加热以解离之前，甲烷通过与氢和碳逆流热交换而经预热。在步骤874中，如图所示，选择后续的加热措施以定制自经预热的甲烷得到的碳制得的产品。Figure 8 illustrates an overall process 800 in which in step 862 photosynthesis provides an organic material, typically containing carbon, hydrogen and oxygen. Step 864 provides anaerobic digestion or pyrolysis or partial oxidation to produce fuel gases such as methane and carbon oxides. Separation of oxides of carbon, such as carbon dioxide, from the fuel gas is provided in step 866 . Suitable filters, pressure swing adsorption, temperature swing adsorption or selective adsorption as disclosed in co-pending patent applications are provided by the system indicated at 868 . Depending on the pressure of the purified fuel gas and the pressure required for the process of step 872, a pressurizer 870 is employed which includes options such as electrolytic pressurization, mechanical pump or compressor operation, or pressurization from adsorptive and and/or emissions from metal hydride systems. In step 872, methane is preheated by countercurrent heat exchange with hydrogen and carbon, as shown, prior to final heating for dissociation. In step 874, subsequent heating measures are selected to tailor products made from preheated methane derived carbon, as shown.

图9示出了实施方案900的详情，其包括太阳光集中镜912、集中辐射接收器914、固定接收管922及旋转螺旋输送机和挤出管924，其中整体式螺旋926迫使反应性成分如有机材料进入区930中，在区930中，其由集中的太阳能快速加热至高温。太阳能的充分集中易于通过抛物面镜、球面镜或定日反射镜阵列获得以产生500℃到2500℃的典型运行温度，这由材料的物理化学性质及密闭管922的构造规格造就。FIG. 9 shows details of an embodiment 900 comprising a solar concentrating mirror 912, a concentrating radiation receiver 914, a stationary receiver tube 922, and a rotating screw conveyor and extrusion tube 924, wherein an integral screw 926 forces reactive components such as The organic material enters zone 930 where it is rapidly heated to a high temperature by concentrated solar energy. Sufficient concentration of solar energy is readily obtained with parabolic, spherical or heliostat arrays to produce typical operating temperatures of 500°C to 2500°C, dictated by the physicochemical properties of the materials and construction specifications of the closed tube 922 .

固定底座904罩住驱动系统并提供材料向和自反应器914的传送。反应器914的燃料和原料如填埋场甲烷通过连接至管道918而被递送。在流体原料如污水组分通过反应器914处理的情况下，优选通过连接至管道915来提供递送。产生或递送的电通过缆组917传输。反应器914产生的氢和/或其他流体被递送至管道916以储存和分销。台906绕着中心竖直轴旋转以提供反应器914的太阳跟踪，反应器914装配了镜912。提供了如图所示绕着支承910中的水平轴909的协调旋转以跟踪太阳和产生点聚焦太阳能，该点聚焦太阳能自镜组件912反射。将待加热的有机固体和半固体装载进料斗908中，料斗908将这类材料进给到螺旋输送机924中，图10示出了螺旋输送机924的一部分。Stationary base 904 houses the drive system and provides transfer of material to and from reactor 914 . Reactor 914 fuel and feedstock, such as landfill methane, is delivered via connection to conduit 918 . Where a fluid feedstock, such as a sewage component, is processed through reactor 914, delivery is preferably provided by connection to conduit 915. The electricity generated or delivered is transmitted through the cable set 917 . Hydrogen and/or other fluids produced by reactor 914 are delivered to pipeline 916 for storage and distribution. Stage 906 rotates about a central vertical axis to provide sun tracking of reactor 914 , which is equipped with mirror 912 . Coordinated rotation about horizontal axis 909 in support 910 as shown is provided to track the sun and generate point focused solar energy which is reflected from mirror assembly 912 . Organic solids and semi-solids to be heated are loaded into a hopper 908 which feeds such materials into a screw conveyor 924 , a portion of which is shown in FIG. 10 .

其他形式的可再生加热也易于适应，例如使用来自发电机的电的感应或电阻加热，所示发电机由落水、风、波浪作用提供动力或由使用本文中所述的操作产生的燃料的发动机提供动力。类似地，预期燃烧一部分反应器914所产生的燃料以充分加热区930，以便实现方程式1、2和5的反应。区930的这组备选热输入示例了在断断续续有云团覆盖或夜晚的情况下补充或代替为确保连续运行所需的太阳能的优选措施。Other forms of regenerative heating are also readily adaptable, such as induction or resistive heating using electricity from a generator powered by falling water, wind, wave action or by an engine using fuel produced by the operations described herein Provide power. Similarly, it is contemplated to combust a portion of the fuel produced by reactor 914 to heat zone 930 sufficiently to effect the reactions of Equations 1, 2 and 5. This set of alternative heat inputs to zone 930 exemplifies preferred measures to supplement or replace the solar energy required to ensure continuous operation during intermittent cloud cover or at night.

用所产生的氢和/或一氧化碳的部分燃烧对区930补充加热或代替太阳热优选通过经管932的膛孔931内的管937自电解器907递送氧而实现。通过基于填埋场甲烷和/或氢运行热力发动机903来驱动发电机905将提供一个重要的协同好处。过剩的发电容量被用来在电解器907中产生氧和氢。通过这样的操作产生的氢可易于储存在管道916中以供销售，而氧可被用来大大提高通过反应器914和/或燃料电池发电应用中所产生的燃料的部分燃烧生热的过程效率。Supplemental heating of zone 930 or replacement of solar heat with partial combustion of hydrogen and/or carbon monoxide produced is preferably accomplished by delivery of oxygen from electrolyzer 907 via tube 937 within bore 931 of tube 932 . Driving the generator 905 by running the heat engine 903 on landfill methane and/or hydrogen will provide an important synergistic benefit. Excess generating capacity is used to generate oxygen and hydrogen in electrolyzer 907 . The hydrogen produced by such operations can be readily stored in line 916 for sale, while the oxygen can be used to greatly enhance the process efficiency of heat generation by partial combustion of fuel produced in reactor 914 and/or in fuel cell power generation applications .

当使用氧来通过部分燃烧产生热时，氮的消除将大大降低通过从管932内的气体混合物冷凝或过滤水来净化氢气的成本。如图所示，管937递送氧以燃烧所需量的燃料，这样做热损失最小并消除了氮的加热需要，而如果使用空气作为氧化剂，则将存在氮。The elimination of nitrogen will greatly reduce the cost of purifying hydrogen by condensing or filtering water from the gas mixture in tube 932 when oxygen is used to generate heat by partial combustion. As shown, tube 937 delivers oxygen to combust the required amount of fuel, doing so with minimal heat loss and eliminating the need for heating nitrogen which would be present if air were used as the oxidant.

管922因此实现容纳处于缺氧条件下的有机原料并向生物质传递能量如太阳能的功能，所述生物质被传送到集中加热区930以促进概括为如下的反应：Tube 922 thus fulfills the function of containing the organic feedstock under anaerobic conditions and transferring energy, such as solar energy, to the biomass which is conveyed to concentrated heating zone 930 to facilitate reactions which can be summarized as follows:

C_nH_mO_x+热₁→xCO+m/2H₂+(n-x)C         方程式7C_n H_m O_x + heat₁ → xCO + m/2H₂ + (nx)C Equation 7

C₆H₁₀O₅+热₂→5CO+5H₂+C               方程式8C₆ H₁₀ O₅ +Heat₂ → 5CO+5H₂ +C Equation 8

含CO和H₂的气体产物中也可能可见小量的NH₃、H₂S、N₂和H₂O，该气体产物由压实的固体迫使进入如图所示旋转螺纹管932的中心膛孔931中。优选使H₂S与铁反应以形成硫化铁或随着氢的释放收集在过程所产生的碳中。优选通常以氨的形式收集固定氮、以硫化铁的形式收集硫，并将这些物质与本发明的一些实施方案所收集的矿物灰分一道用作土壤养分。Small amounts of_NH3 , H2S,_N2 and_H2O may also be seen in the gaseous product containing_CO and_H2 which is forced by the compacted solids into the center bore of the rotating threaded tube 932 as shown In hole 931._The H2S is preferably reacted with the iron to form iron sulfide or is collected in the carbon produced by the process as the hydrogen is released. It is preferred to collect fixed nitrogen, usually in the form of ammonia, and sulfur in the form of iron sulfide, and use these as soil nutrients along with mineral ash collected in some embodiments of the present invention.

如图所示，固体如碳和灰分936通过螺旋管932沿螺纹934的旋转运动而从区930提取。优选使用高温绝缘件940如图所示覆盖接收器914的端部，且随着被螺旋输送机932提取的富碳固体与移动向接收器和反应器组件的经加热的区930的生物质之间的逆流热交换，绝缘区域942提供热量保存。在不可得到太阳能的时间过程中，绝缘套筒948被用来覆盖区930并优选由伸缩管引导器支承和引导向和自所示存放位置，所述引导器未示出。As shown, solids such as carbon and ash 936 are extracted from zone 930 by the rotational movement of helical tube 932 along threads 934 . High temperature insulation 940 is preferably used to cover the end of the receiver 914 as shown, and as the carbon-rich solids extracted by the screw conveyor 932 and the biomass moving towards the heated zone 930 of the receiver and reactor assembly Insulated area 942 provides heat retention for counter-current heat exchange between them. During times when solar energy is not available, insulating sleeve 948 is used to cover area 930 and is preferably supported and guided to and from the storage position shown by telescopic tube guides, not shown.

在压实和逆流预热的初期移除的水和其他气体优选通过百叶窗或孔944放出以便可通过收集管946提取。对于许多原料如粪肥和污水，该水通常含固定氮和其他土壤养分而优选用以补充土壤适耕性和生产力。Water and other gases removed during the initial stages of compaction and countercurrent preheating are preferably vented through louvers or holes 944 so that they can be extracted through collection pipe 946 . For many feedstocks such as manure and sewage, this water usually contains fixed nitrogen and other soil nutrients and is preferred to supplement soil fertility and productivity.

在优选纯碳和纯氢的情况下，可将生物质预处理以移除形成灰分的物质如钙、镁、磷、铁和其他矿物。生物质的灰分成分常常被浪费性地填埋在填埋场，或者，在从污水系统排放废水及垃圾处置操作时，其可能逃逸到海洋。在本发明的一些实施方案中，灰分易于收集并返回到有用的应用中作为土壤养分。这可通过机械分离与生物质在合适溶剂中的解离以分离灰分组分的组合实现。Where pure carbon and pure hydrogen are preferred, the biomass can be pretreated to remove ash forming species such as calcium, magnesium, phosphorus, iron and other minerals. The ash component of biomass is often wasted wastefully in landfills, or it may escape to the ocean during discharge from sewage systems and waste disposal operations. In some embodiments of the invention, the ash is readily collected and returned to useful applications as soil nutrients. This can be achieved by a combination of mechanical separation and dissociation of the biomass in a suitable solvent to separate the ash components.

另一个实施方案提供了生物质如碳水化合物和纤维素按如下一般反应的缺氧消化：Another embodiment provides anaerobic digestion of biomass such as carbohydrates and cellulose as follows:

n(C₆H₁₀O₅)+n H₂O+热₃→n(C₆H₁₂O₆)        方程式9n(C₆ H₁₀ O₅ )+n H₂ O+heat₃ →n(C₆ H₁₂ O₆ ) Equation 9

n(C₆H₁₂O₆)→3n(CH₄)+3nCO₂+热₁₀          方程式10n(C₆ H₁₂ O₆ ) → 3n(CH₄ )+3nCO₂ + heat₁₀ equation 10

所示过程之后剩余的含水液体中捕集的土壤养分通过各自技术(包括加到灌溉水中)有效地转移到耗竭土壤。二氧化碳易于通过冷却产生相变分离或通过吸附在合适的溶剂如水中而自过程的产物移除。在25个大气压和12℃(54°F)下，二氧化碳可以约21.6个体积气体每体积水的程度溶解在水中。提高压力和/或降低温度将增大每体积水溶解的二氧化碳的量。在从甲烷中分离出二氧化碳之后，降低压力或提高温度来释放溶解的二氧化碳。Soil nutrients trapped in the aqueous liquid remaining after the process shown are efficiently transferred to depleted soils by respective techniques including addition to irrigation water. Carbon dioxide is readily removed from the products of the process by cooling to produce a phase change separation or by adsorption in a suitable solvent such as water. At 25 atmospheres and 12°C (54°F), carbon dioxide can dissolve in water to an extent of about 21.6 volumes of gas per volume of water. Increasing the pressure and/or decreasing the temperature will increase the amount of dissolved carbon dioxide per volume of water. After the carbon dioxide is separated from the methane, the pressure is reduced or the temperature is increased to release the dissolved carbon dioxide.

有机原料缺氧解离以产生给定量的截存碳的过程中所需的热的量大大低于自大气收集和解离二氧化碳所需的能量。实施自有机原料截存碳的过程所需的装置远没有从大气提取二氧化碳并将其分解成碳和氧所需的装置那么复杂，而是要简单得多且更坚固。The amount of heat required during the anoxic dissociation of organic feedstock to produce a given amount of sequestered carbon is substantially lower than the energy required to collect and dissociate carbon dioxide from the atmosphere. The equipment required to implement the process of sequestering carbon from organic feedstocks is far less complex than that required to extract carbon dioxide from the atmosphere and break it down into carbon and oxygen, but is much simpler and more robust.

在将烃包括生物质固体和甲烷转化为碳和氢的过程中，解离反应的产物倾向于比反应物占据更大的体积。用于进行这些吸热反应的组件914的装置920可易于用经挤出机螺纹926沿向区930的入口压实的富碳材料和沿区930的出口的挤出机螺纹934压实的富碳材料密封反应区930，以使得通过膛孔931出去的氢和其他气体可被膛孔931出口上的旋转接头和压力调节措施加压至所需的程度并保持。During the conversion of hydrocarbons, including biomass solids and methane, to carbon and hydrogen, the products of dissociation reactions tend to occupy a larger volume than the reactants. The apparatus 920 of the assembly 914 for performing these endothermic reactions can readily be used with carbon-rich material compacted along the entrance to zone 930 via extruder flights 926 and carbon-rich material compacted along the exit of zone 930 through extruder flights 934. The carbon material seals the reaction zone 930 so that hydrogen and other gases exiting through the bore 931 can be pressurized to the desired level and maintained by the swivel joint and pressure regulation on the outlet of the bore 931.

在甲烷进入反应器920之前，优选用合适的加压技术加压冷甲烷至从反应器920递送氢的所需压力，加压技术包括通过从吸附性基材释放加压、相变、机械压缩和混合系统。如果缺氧消化中产生的气体通过液化分离，则这易于通过使甲烷气化至所需的压力而实现。通过各种泵和压缩机870的加压也可用于此目的。Before the methane enters the reactor 920, the cold methane is preferably pressurized to the pressure required to deliver hydrogen from the reactor 920 using a suitable pressurization technique, including pressurization by release from an adsorptive substrate, phase change, mechanical compression and hybrid systems. If the gases produced in the anoxic digestion are separated by liquefaction, this is easily achieved by gasifying the methane to the required pressure. Pressurization by various pumps and compressors 870 can also be used for this purpose.

可产生的碳的类型有很大变化，取决于市场需求及实现碳截存的过程的相应温度和压力。被递送至制造阶段874的甲烷可按需要加工以产生纤维、炭黑、合适基材上的金刚石样镀层、石墨晶体和呈美国专利申请08/921,34、08/921,134和09/370,431的共同待决公开所对应的许多其他形式。The type of carbon that can be produced varies widely, depending on market demand and the corresponding temperatures and pressures of the process to achieve carbon sequestration. The methane delivered to the manufacturing stage 874 can be processed as desired to produce fibers, carbon black, diamond-like coatings on suitable substrates, graphite crystals and the common Many other forms for pending disclosures.

还预期，对于某些应用而言，作为热量保存优势，螺旋输送机932应设计为进给路和预热器，其中氢通过膛孔931递送，而区930中的反应产生的碳由适宜地设计的与进入的原料逆流热交换的挤出机924输送。这种布置提供了进入的原料在到达区930之前由与原料反方向地经过的产物平行流从内部和从外部的逆流加热。It is also contemplated that for some applications, as a heat conservation advantage, screw conveyor 932 should be designed as a feed path and preheater, where hydrogen is delivered through bore 931 and carbon produced by the reaction in zone 930 is produced by suitably The extruder 924 is designed for countercurrent heat exchange with the incoming feedstock. This arrangement provides that the incoming feedstock is heated from the inside and counter-flow from the outside by the product passing in the opposite direction to the feedstock before reaching zone 930 .

反应形成的碳由螺旋输送机932携带，所述碳与管924逆流热交换以预热进入的甲烷及因此提高太阳能完成过程反应的总体效率和速率。产生的氢被收集在输送管932的膛孔931中，并与向着区930经过的反应物逆流热交换而移除热。产生的可再生的氢可被用于燃料电池中或热力发动机中，其实际上净化空气并提供比环境大气更洁净的排气。The carbon formed by the reaction is carried by the screw conveyor 932 and is heat exchanged counter-currently with the tubes 924 to preheat the incoming methane and thus increase the overall efficiency and rate of the solar completion process reactions. The hydrogen produced is collected in the bore 931 of the transfer tube 932 and removes heat by countercurrent heat exchange with the reactants passing towards zone 930 . The renewable hydrogen produced can be used in fuel cells or in heat engines that actually clean the air and provide an exhaust cleaner than the ambient atmosphere.

随着过程产生碳，其不断地形成输送机螺纹926与管922的内壁之间的气密密封。这优选通过减小需要最大压实之处的螺旋挤出机螺距来确保。通常需要在经历向氢的转化的材料经过区930之后在螺旋输送机经过区930中的出口上提供最大的碳压实和密封效果。As the process generates carbon, it continues to form an airtight seal between the conveyor threads 926 and the inner wall of the tube 922 . This is preferably ensured by reducing the screw extruder pitch where maximum compaction is required. It is generally desirable to provide maximum carbon compaction and sealing on the outlet in the screw conveyor passage zone 930 after the material undergoing conversion to hydrogen passes through the zone 930 .

除如所示的螺旋输送机外，预期所示过程中反应物的输送可由众多其他措施进行。示例性地，可用往复式柱塞代替螺旋输送机924来迫使生物质进入反应区，而碳可通过其他提取方法从热端提取，包括用链传动输送机代替螺旋输送机932。In addition to the screw conveyor as shown, it is contemplated that the transport of the reactants in the process shown can be carried out by numerous other means. Illustratively, a reciprocating plunger can be used in place of screw conveyor 924 to force biomass into the reaction zone, while carbon can be extracted from the hot end by other extraction methods, including replacing screw conveyor 932 with a chain drive conveyor.

在需要产生液体燃料或溶剂如一种或多种松烯(turpene)的蒸气以及其他有价值产品的情况下，通常可调节反应温度至较低的温度或者提高成分的生产速率。可用的化合物如氢、碳、甲醇、生物柴油和松节油可以产生并收集在管膛孔931中，如针对一部分具有所示平均化学式的典型生物质废弃物原料的方程式中所概括的那样：In cases where it is desired to produce vapors of liquid fuels or solvents, such as one or more turpenes, and other valuable products, it is often possible to adjust the reaction temperature to a lower temperature or to increase the production rate of the ingredients. Useful compounds such as hydrogen, carbon, methanol, biodiesel, and turpentine can be produced and collected in the tube bore 931 as outlined in the equation for a portion of a typical biomass waste feedstock with the average chemical formula shown:

C₆H₁₀O₅+热₆→CH₃OH+4CO+3H₂+C          方程式11C₆ H₁₀ O₅ + heat₆ → CH₃ OH + 4CO + 3H₂ +C Equation 11

寄宿吸附的氢于甲醇中的胶态碳的引入将提供更高的每体积热值和在针对可再生柴油燃料的应用中提供压缩点火的能力。如果需要更高的液体燃料和/或溶剂收率，则可使方程式11的典型过程中产生的一氧化碳和氢优选在合适的催化剂的存在下反应以产生另外的甲醇和氢。The introduction of colloidal carbon in methanol to host adsorbed hydrogen will provide higher heating value per volume and the ability to provide compression ignition in applications targeting renewable diesel fuels. If higher liquid fuel and/or solvent yields are desired, the carbon monoxide and hydrogen produced in the typical process of Equation 11 can be reacted, preferably in the presence of a suitable catalyst, to produce additional methanol and hydrogen.

4CO+3H₂→4CH₃OH+H₂+热₁₂               方程式124CO+3H₂ → 4CH₃ OH+H₂ + heat₁₂ equation 12

生物质行进到区930中的速率及通过螺旋输送机932提取固体残渣的速率优选由计算机控制，该计算机响应压力、温度和其他类指标的仪表测定及气体、蒸气和固体残渣流中所需的产品质量而适应性地控制该过程。The rate at which biomass travels into zone 930 and the rate at which solid residue is extracted by screw conveyor 932 is preferably controlled by a computer that responds to instrumentation of pressure, temperature, and other such indicators and the desired flow rates in the gas, vapor, and solid residue streams. Adaptively control the process for product quality.

一氧化碳可通过如方程式8中所概括的过程所示的歧化作用分解或转化为所需的截存碳形式：Carbon monoxide can be decomposed or converted to the desired sequestered carbon form by disproportionation as shown by the process outlined in Equation 8:

2CO→C+CO₂+热₁₃                        方程式132CO→C+CO₂ +heat₁₃ equation 13

如方程式13中所概括的歧化作用是放热的并可在温度和压力条件的多种组合下提供，包括在10-40个大气压压力和500℃到800℃下进行。Disproportionation as outlined in Equation 13 is exothermic and can be provided under various combinations of temperature and pressure conditions, including at 10-40 atmospheres of pressure and 500°C to 800°C.

如果市场行情支持制氢用于燃料电池或热力发动机以净化空气，则可使一氧化碳与水蒸汽以如方程式9中所示的放热反应反应产生氢：If market conditions favor the production of hydrogen for use in fuel cells or heat engines for air purification, carbon monoxide can be reacted with water vapor in an exothermic reaction as shown in Equation 9 to produce hydrogen:

CO+H₂O→CO₂+H₂+热₁₄                    方程式14CO+H₂ O→CO₂ +H₂ +Heat₁₄ Equation 14

通过所概括的过程产生的一氧化碳可被转化为众多产物以满足市场需求，如选自如所示需要制氢和/或碳的过程。优选利用所述放热过程释放的热作为所示吸热反应所需的热加入的一部分。Carbon monoxide produced by the outlined process can be converted to a number of products to meet market demands, such as selected from processes requiring hydrogen and/or carbon production as shown. It is preferred to utilize the heat released by the exothermic process as part of the heat addition required for the endothermic reaction shown.

因此，本发明的一些实施方案提供了自大气截存碳的实用方法，所述方法包括光合作用、收集光合生物质和加热所述生物质以产生选自碳、氢、甲醇、松烯和灰分的产物。一般让腐烂进入大气并导致二氧化碳和/或甲烷累积的生物质废弃物现在可以被利用，以高效地产生氢、碳产品和土壤养分。Accordingly, some embodiments of the present invention provide a practical method for sequestering carbon from the atmosphere comprising photosynthesis, collecting photosynthetic biomass, and heating the biomass to produce carbon, hydrogen, methanol, pinene, and ash product of. Biomass wastes that normally let decay into the atmosphere and lead to the accumulation of carbon dioxide and/or methane can now be harnessed to efficiently generate hydrogen, carbon products and soil nutrients.

图12示出了其中以氢内燃机为系统的电源和热源的一个优选实施方案(未示出的是氧和饮用水也是系统的副产物)。图12强调，一旦过程开始，其即是自支承的，因为相对少量的氢被用来为系统提供动力。能量效率通过生物消化池和电解器之间的关系获得。能量效率还通过太阳热抛物面反射器技术获得：将甲烷裂化为其组成部分：氢和碳。根据一个实施方案，甲烷的裂化在夜间不发生。根据本公开的方面，由此获得氢燃料的可分配大规模可再生能生产。根据另外的实施方案，由此获得碳(未加以区分的碳纤维或碳灰)的可分配大规模可再生资源生产。根据还另外的方面，通过利用不同的装置，由此获得加以了区分的专用碳的可分配大规模制造。当分配的大规模可再生资源提取和采集与可再生能采集相组合时，结果是可持续的经济发展和可持续的生产。Figure 12 shows a preferred embodiment in which a hydrogen internal combustion engine is used as the power source and heat source for the system (not shown are oxygen and potable water are also by-products of the system). Figure 12 emphasizes that once the process starts, it is self-supporting because a relatively small amount of hydrogen is used to power the system. Energy efficiency is obtained through the relationship between biodigesters and electrolyzers. Energy efficiency is also gained through solar thermal parabolic reflector technology: cracking methane into its constituent parts: hydrogen and carbon. According to one embodiment, cracking of methane does not occur overnight. According to aspects of the present disclosure, distributable large-scale renewable energy production of hydrogen fuel is thereby obtained. According to further embodiments, assignable large-scale renewable resource production of carbon (undifferentiated carbon fibers or carbon ashes) is thereby obtained. According to yet a further aspect, by utilizing different devices, distributable mass production of differentiated specialty carbons is thereby obtained. When allocated large-scale renewable resource extraction and harvesting is combined with renewable energy harvesting, the result is sustainable economic development and sustainable production.

这就是说，从可再生资源和能量，人们获得了具有更高经济价值的精制的可再生资源和能量，其继而被用来生产耐用品，这些耐用品再用来采集新的可再生资源和能量，这是一种可持续、无污染和非耗竭的方式。根据本公开的方面，这种可持续的经济模式可以写成此可持续的经济模式的代数递推公式(递推公式为用来用一个或多个在先的条件确定一个序列的下一条件的公式)。本发明的一些实施方案在生产系统内的使用对(a)生物质原料、(b)甲烷原料和(c)碳产生经济倍增效应；然后甲烷/氢被用来采集更多的可再生能和可再生材料资源；然后碳变为耐用品，其收获更多的(a)和(b)并产生更多的(c)。因此，本公开具体化了经济“可持续性”的数学。That is to say, from renewable resources and energy, people obtain refined renewable resources and energy with higher economic value, which in turn are used to produce durable goods, which are used to collect new renewable resources and energy. Energy, which is sustainable, non-polluting and non-depleting. According to aspects of the present disclosure, this sustainable economic model can be written as the algebraic recursion formula of this sustainable economic model (the recursive formula is used to determine the next condition of a sequence with one or more previous conditions formula). The use of some embodiments of the present invention within production systems has an economic multiplier effect on (a) biomass feedstock, (b) methane feedstock, and (c) carbon; the methane/hydrogen is then used to capture more renewable energy and Renewable material resources; the carbon is then turned into a durable good that harvests more (a) and (b) and produces more (c). Thus, the present disclosure embodies the mathematics of economic "sustainability."

图12未必示出大规模储存的经济学含义。既可分配(许多位置)又可放大(能大量生产)的能量生产与明显局限于当地并不可放大的方法相比，是一种进步。图13示出了其中以太阳热集中系统为系统的电源和热源的优选实施方案。图14示出了其中未指定电源和热源以为系统的未来变化性和适应性留余地的优选实施方案。图15示出了可再生能生产过程的流程图。Figure 12 does not necessarily show the economic implications of large-scale storage. Energy production that is both distributable (many locations) and scalable (capable of mass production) is an advance over approaches that are clearly localized and non-scalable. Fig. 13 shows a preferred embodiment in which the solar heat concentration system is used as the power source and heat source of the system. Figure 14 shows a preferred embodiment where the power and heat sources are not specified to allow for future variability and adaptability of the system. Figure 15 shows a flow diagram of the renewable energy production process.

上面的实施方案可由如本文中所公开的电解器实现。The above embodiments can be realized by an electrolyzer as disclosed herein.

在本发明的一个实施方案中，提供了一种电解电池，所述电解电池包括：密闭壳；第一电极；第二电极；与第一电极和第二电极电连通的电流源；与第一电极和第二电极流体连通的电解质；气体，其中所述气体在电解过程中于第一电极处或附近形成；和分离器，其中所述分离器包括倾斜表面以由于电解质的密度与电解质和气体的组合密度间的差异而引导电解质和气体的流动，使得气体基本上在第二电极远侧方向上流动。In one embodiment of the present invention, there is provided an electrolytic cell comprising: a closed case; a first electrode; a second electrode; a current source in electrical communication with the first electrode and the second electrode; An electrolyte in fluid communication between the electrode and the second electrode; a gas, wherein the gas is formed at or near the first electrode during electrolysis; and a separator, wherein the separator includes sloped surfaces to accommodate the electrolyte and gas due to the density of the electrolyte. The flow of the electrolyte and the gas is directed by the difference between the combined densities of the electrodes such that the gas flows substantially in a direction distal to the second electrode.

在另一个实施方案中，提供了一种电解电池，所述电解电池包括：密闭壳；第一电极；第二电极；与第一电极和第二电极电连通的电流源；与第一电极和第二电极流体连通的电解质；气体，其中所述气体在电解过程中于第一电极处或附近形成；气体提取区域；和分离器，其中所述分离器包括两个形成“V”形的倾斜表面；其中所述分离器由于电解质的密度与电解质和气体的组合密度间的差异而引导电解质和气体的流动，使得气体基本上在第二电极远侧方向上流动，且其中所述分离器还被构造为促进电解质在第一电极、气体提取区域和第二电极之间的循环以向第一电极和第二电极提供新鲜电解质。In another embodiment, there is provided an electrolytic cell comprising: a closed case; a first electrode; a second electrode; a current source in electrical communication with the first electrode and the second electrode; An electrolyte in fluid communication with the second electrode; a gas, wherein the gas is formed at or near the first electrode during electrolysis; a gas extraction region; and a separator, wherein the separator includes two slopes forming a "V" shape surface; wherein the separator directs the flow of the electrolyte and the gas due to the difference between the density of the electrolyte and the combined density of the electrolyte and the gas such that the gas flows substantially in a direction distal to the second electrode, and wherein the separator also configured to facilitate circulation of electrolyte between the first electrode, the gas extraction region and the second electrode to provide fresh electrolyte to the first electrode and the second electrode.

在又一个实施方案中，提供了一种电解电池，所述电解电池包括：密闭壳；第一电极；第二电极；与第一电极和第二电极电连通的电流源；与第一电极和第二电极流体连通的电解质；气体，其中所述气体在电解过程中于第一电极处或附近形成；和分离器，其中所述分离器包括倾斜表面以由于电解质的密度与电解质和气体的组合密度间的差异而引导电解质和气体的流动，使得气体基本上在第二电极远侧方向上流动。In yet another embodiment, there is provided an electrolytic cell comprising: a closed case; a first electrode; a second electrode; a current source in electrical communication with the first electrode and the second electrode; An electrolyte in fluid communication with the second electrode; a gas, wherein the gas is formed at or near the first electrode during electrolysis; and a separator, wherein the separator includes sloped surfaces to accommodate the density of the electrolyte and the combination of the electrolyte and the gas The difference between the densities directs the flow of the electrolyte and the gas such that the gas flows substantially in a direction distal to the second electrode.

在另一个实施方案中，提供了一种电解电池及使用方法。虽然所述电解电池可以用在许多应用中，但在本实施方案中描述为用在氢和氧的生产中。根据本实施方案的电解电池提供了加压的氢和氧的可逆分离生产并耐受运行的杂质和产物。所述实施方案还提供了运行电解过程的选择权，所述电解过程包括如下步骤：供给被加压至比紧凑储存所需低得多的幅度的待解离物质，在电极间施加电动势以产生密度比被解离物质的低的流体产物，和限制密度较小的流体产物的膨胀直至达到紧凑储存的所需压力。该实施方案及其他实施方案可通过运行热力发动机或燃料电池并利用来自这类源的热来做饭、消毒水和向其他物质传递热、提供空间加热或促进燃料向这类发动机或燃料电池的缺氧或电诱导释放而改善住所如家、饭店、旅馆、医院、罐头食品厂及其他商业设施的能量利用效率。此外，本领域技术人员应理解，本文中公开的实施方案的方面可应用于其他类型的电化学电池以提供类似的优势。In another embodiment, an electrolysis cell and method of use are provided. While the electrolysis cell can be used in many applications, it is described in this embodiment as being used in the production of hydrogen and oxygen. The electrolysis cell according to this embodiment provides reversible separate production of pressurized hydrogen and oxygen and is tolerant to impurities and products of operation. Said embodiment also provides the option of running an electrolysis process comprising the steps of supplying the species to be dissociated pressurized to a much lower magnitude than required for compact storage, applying an electromotive force across the electrodes to generate The fluid product is less dense than the material being dissociated, and the expansion of the less dense fluid product is restricted until the desired pressure for compact storage is achieved. This and other embodiments can be achieved by operating a heat engine or fuel cell and using the heat from such a source to cook food, sterilize water and transfer heat to other substances, provide space heating, or facilitate the transfer of fuel to such an engine or fuel cell Improvement of energy efficiency in dwellings such as homes, restaurants, hotels, hospitals, cannery and other commercial establishments by hypoxia or electrically induced release. Furthermore, those skilled in the art will appreciate that aspects of the embodiments disclosed herein can be applied to other types of electrochemical cells to provide similar advantages.

与在很大程度上取决于相对较慢扩散、对流和浓度梯度过程来产生传质和/或递送离子以生产所需组分的常规电化学电极相反，本实施方案提供了更高效的传质，包括快速的离子补充过程和通过自如本文中所述密度较大的液体介质逃逸的低密度气体的泵送作用向所需电极的递送。这确保了更高的电效率、更快的解离和更高的分离效率，此外防止不希望有的副反应。提高离子的产生及向电极的递送的速率和效率将提高系统效率和每电极面积的电流极限值。In contrast to conventional electrochemical electrodes that rely heavily on relatively slow diffusion, convection, and concentration gradient processes to generate mass transfer and/or deliver ions to produce desired components, this embodiment provides more efficient mass transfer , including a rapid ion replenishment process and delivery to the desired electrode by the pumping action of a low density gas escaping from a denser liquid medium as described herein. This ensures higher electrical efficiency, faster dissociation and higher separation efficiency, and moreover prevents undesired side reactions. Increasing the rate and efficiency of ion generation and delivery to electrodes will increase system efficiency and current limit per electrode area.

参见图1B，其示出了其中容器4b如金属管充当密闭壳的电解电池2b。任选地，容器4b还可充当电极，如图1B中所示。多孔电极如圆柱形导电丝网电极8b与管状电极4b共轴地定位并由液体电解质持液如酸或碱与管状电极4b隔开。液体电解质占据容器4b的内部空间至绝缘器24b中的液-气界面。可在容器4b内提供上有电镀、等离子体喷射或复合的电极材料的层的介电套筒或导电的圆柱形内部衬里电极4b′(未示出)以充当组件的电隔离元件，从而使得能够作为维护项目方便地更换，或者充当大量分段电极元件中的一个以提供任选的极性和/或串联、并联或串并联连接。在本可逆实施方案中，对于水的电解，电极8b可以看作是电子源或阴极，使得氢在电极8b处产生，而电极4b可以看作是阳极，使得氧在电极4b处产生。容器4b可以能加压。容器4b的内容物的加压由密封盖30b和46b约束。包括电极8b、气体分离器10b和电连接32b的部件的支承、电绝缘和稳定化由介电绝缘体20b和24b提供，如图所示。电解电池2b的加压可通过电解过程中气体的产生所致的自加压、通过外部源如泵或通过其任意组合实现。Referring to Fig. IB, there is shown an electrolytic cell 2b in which a container 4b, such as a metal tube, acts as a closed case. Optionally, container 4b can also act as an electrode, as shown in Figure IB. A porous electrode, such as a cylindrical conductive mesh electrode 8b, is positioned coaxially with the tubular electrode 4b and separated from the tubular electrode 4b by a liquid electrolyte retainer, such as an acid or base. The liquid electrolyte occupies the inner space of the container 4b to the liquid-gas interface in the insulator 24b. A dielectric sleeve or conductive cylindrical inner liner electrode 4b' (not shown) with a layer of plated, plasma sprayed or composited electrode material may be provided within the vessel 4b to act as an electrically isolating element of the assembly such that Can be easily replaced as a maintenance item, or as one of a large number of segmented electrode elements to provide optional polarity and/or series, parallel or series-parallel connections. In this reversible embodiment, for the electrolysis of water, electrode 8b can be considered as an electron source or cathode, so that hydrogen is produced at electrode 8b, and electrode 4b can be considered as an anode, such that oxygen is produced at electrode 4b. Container 4b may be pressurized. Pressurization of the contents of container 4b is constrained by sealing caps 30b and 46b. Support, electrical insulation and stabilization of the components including electrode 8b, gas separator 10b and electrical connection 32b are provided by dielectric insulators 20b and 24b, as shown. Pressurization of the electrolysis cell 2b can be achieved by self-pressurization due to gas generation during electrolysis, by an external source such as a pump, or by any combination thereof.

分离器10b被构造为液体可透过但基本上阻止气体从分离器的阴极侧向分离器的阳极侧的流动或输送，反之亦然，包括基本上阻止电解质中或气泡成核后溶解的气体的流动。任选地，电极8b可以被构造为充当分离器10b，使得不需要单独的分离器。或者，分离器10b可以包括电极8b或者电极8b可以包括分离器10b。此外，分离器10b也可以包括阳极电极4b或者阳极电极4b可以包括分离器10b。The separator 10b is configured to be permeable to liquids but substantially prevent the flow or transport of gases from the cathode side of the separator to the anode side of the separator and vice versa, including substantially preventing dissolved gases in the electrolyte or after nucleation of gas bubbles flow. Optionally, electrode 8b may be configured to act as separator 10b such that a separate separator is not required. Alternatively, separator 10b may comprise electrode 8b or electrode 8b may comprise separator 10b. Furthermore, the separator 10b may also comprise the anode electrode 4b or the anode electrode 4b may comprise the separator 10b.

绝缘器24b被制作成所示形状并根据需要分离、收集和/或提取电极如4b和8b(包括与分离器10b组合的利用)所产生的气体。在所示同心圆柱几何形状中，绝缘器24b具有中央锥形腔，电极8b上释放的气体将收集在该中央锥形腔内。同心地包绕该中央腔的是环形区，所述环形区收集自电极4b′的表面或自容器电极4b的内部释放的气体。Insulator 24b is shaped as shown and separates, collects and/or extracts gases generated by electrodes such as 4b and 8b (including utilization in combination with separator 10b) as desired. In the concentric cylindrical geometry shown, the insulator 24b has a central conical cavity in which the gas released on the electrode 8b will collect. Concentrically surrounding this central cavity is an annular zone which collects gas released from the surface of the electrode 4b' or from the interior of the container electrode 4b.

任选地，可如图所示在24b的上部收集通道中安放催化过滤器48b。包括横穿分离器10b行进而设法到达催化过滤器48b的氧可以以催化方式通过与氢反应而导致水的形成，所述水可然后返回电解质。大量过量的氢可充当散热器以抑制该催化反应所释放的热影响电解电池。经纯化的氢在如图所示配件26b处供应。类似地，可能优选在如图所示收集氧的周围环面的上部区域中提供催化过滤器49b以将到达该氧环面的任何氢转化为水。氧在如图所示配件22b处取走。或者，可将催化过滤器安放在配件22b和26b处、附近或里面。Optionally, a catalytic filter 48b may be placed in the upper collection channel of 24b as shown. Oxygen comprising traveling across the separator 10b trying to reach the catalytic filter 48b can be catalytically reacted with hydrogen to result in the formation of water which can then be returned to the electrolyte. The large excess of hydrogen acts as a heat sink to inhibit the heat released by this catalytic reaction from affecting the electrolytic cell. Purified hydrogen is supplied at fitting 26b as shown. Similarly, it may be preferable to provide a catalytic filter 49b in the upper region of the surrounding annulus where oxygen is collected as shown to convert any hydrogen reaching the oxygen annulus to water. Oxygen is taken away at fitting 22b as shown. Alternatively, catalytic filters may be placed at, near or within fittings 22b and 26b.

在所示的运行中，如果水为待解离成氢和氧的物质，则制备合适的电解质如碳酸氢钠、苛性钠、氢氧化钾或硫酸的水溶液并如图所示由传感器50b保持在所需的液位下，传感器50b检测液体压力并向控制器52b发出信号以运行泵40b从而根据需要自合适的源如贮存器42b加水以产生或保持所需的持液量或压力。控制器52b因此对温度和压力控制传感器58b作出响应，传感器58b可以被包括在具有液位传感器50b或持液量传感器51b、控制泵36b和40b及热交换器56b的一体化单元中，其中热交换器56b可以包括循环泵系统如散热器或加热器(未示出)以接收或传递热。类似地，可以结合这样的运行采用加热或冷却风扇以增强热自伴随电解电池2b的源的接收或排出。In the operation shown, if water is the species to be dissociated into hydrogen and oxygen, an aqueous solution of a suitable electrolyte such as sodium bicarbonate, caustic soda, potassium hydroxide or sulfuric acid is prepared and held at At the desired fluid level, sensor 50b senses fluid pressure and signals controller 52b to operate pump 40b to add water as needed from a suitable source, such as reservoir 42b, to create or maintain the desired holdup or pressure. Controller 52b is thus responsive to temperature and pressure control sensor 58b, which may be included in an integrated unit with level sensor 50b or holdup sensor 51b, control pumps 36b and 40b, and heat exchanger 56b, wherein the heat The exchanger 56b may include a circulating pump system such as a radiator or heater (not shown) to receive or transfer heat. Similarly, heating or cooling fans may be employed in conjunction with such operation to enhance the reception or removal of heat from the source accompanying the electrolytic cell 2b.

在其中电解电池2b待循环应用的一些实施方案中，例如，当过剩的电廉价和另外不需要时，可使电解电池2b的持水量有相当大变化地运行。在过剩的电不可得或其关断时，氢和氧的供给可从容器4b提取并让系统回到环境压力。然后可加入环境压力的水以使系统装满料，可使系统在绝缘器24b周围具有大的环空体积，这是为促进这样的循环的低压填充和电解操作，以在实现压力或化学能向功的转化、紧凑储存以及提供向车辆、工具或器具接收器的快速转移所需的高压下递送氢或氧可能需要的。In some embodiments where the electrolytic cell 2b is to be cycled, for example, when excess electricity is cheap and otherwise not needed, the water holding capacity of the electrolytic cell 2b can be operated with considerable variation. When excess power is not available or is shut down, the supply of hydrogen and oxygen can be drawn from container 4b and the system returned to ambient pressure. Water at ambient pressure may then be added to prime the system, which may have a large annular volume around the insulator 24b, to facilitate low pressure filling and electrolysis operations for such cycles to achieve pressure or chemical energy Conversion to work, compact storage, and delivery of hydrogen or oxygen at high pressures required to provide rapid transfer to vehicle, tool or appliance receivers may be required.

在施加电流并自小得多的持液量生成大量的氢气和氧气后，可根据需要对系统加压并保持加压直至溶液中的持水被耗尽至传感器50b或51b的检测使得控制器52b或中断电解循环或如图所示通过压力泵40b自贮存器42b加水的点。可能优选经过阀门如所示截止阀44b加水，以根据需要实现泵40b的多种输送量或维护。After applying current and generating large quantities of hydrogen and oxygen from a much smaller holdup, the system can be pressurized as needed and kept pressurized until the holdup in solution is depleted until detection by sensor 50b or 51b causes the controller 52b is either the point at which the electrolysis cycle is interrupted or water is added from reservoir 42b by pressure pump 40b as shown. It may be preferable to add water through a valve, such as shut-off valve 44b as shown, to allow for variable delivery or maintenance of pump 40b as required.

参见图1B、2B和3B，图2B示出了图1B的分离器10b的一个实施方案，其中所述分离器包括两个形成“V”形的倾斜表面14b。如果电解质是基于水的，则电子通过接头32b加到多孔电极8b如织造丝网圆柱并通过电接头6b从容器4b取走以不断地将氢离子转化为氢原子和随后双原子分子，所述双原子分子可在电极8b上或附近成核以形成气泡。氢和氧气泡通常远不如基于水的电解质的密度大，故将在浮力驱动下上行。氧气泡类似地被驱动着上行并通过共轴分离器10b的几何形状与氢分离，共轴分离器10b在图2B的放大截面图中示出。图2B所示构造可用在其中需要电解电池2b的运行过程中所形成的气体流的任何应用中。此外，所述分离器构造可用在本领域已知的其他电化学电池构造中。或者，如果电解过程中形成的材料密度比电解质大，则可以让分离器10b翻转形成“Λ”形。类似地，如果通过电解在阴极处形成的一种材料密度比电解质小而在阳极处形成的另一材料密度比电解质大，则可使分离器10b由倾斜的“/”或“\”形组成以使密度较小的材料偏转远离密度较大的材料。Referring to Figures IB, 2B and 3B, Figure 2B shows an embodiment of the separator 10b of Figure IB, wherein the separator includes two inclined surfaces 14b forming a "V" shape. If the electrolyte is water based, electrons are added to the porous electrode 8b as a woven wire mesh cylinder through the connector 32b and taken away from the container 4b through the electrical connector 6b to continuously convert hydrogen ions into hydrogen atoms and subsequently diatomic molecules, said Diatomic molecules may nucleate on or near electrode 8b to form gas bubbles. Hydrogen and oxygen bubbles are typically much less dense than water-based electrolytes and will be buoyantly driven upward. The oxygen bubbles are similarly driven up and separated from the hydrogen by the geometry of the coaxial separator 10b, which is shown in the enlarged cross-sectional view of Figure 2B. The configuration shown in Figure 2B can be used in any application where a flow of gas formed during operation of the electrolysis cell 2b is required. Additionally, the separator configuration can be used in other electrochemical cell configurations known in the art. Alternatively, if the material formed during electrolysis is denser than the electrolyte, the separator 10b can be inverted to form a "Λ" shape. Similarly, if one material is formed at the cathode by electrolysis that is less dense than the electrolyte and another material is formed at the anode that is denser than the electrolyte, the separator 10b can be made to consist of an inclined "/" or "\" shape To deflect less dense material away from denser material.

自40′或容器4b内部释放的氢和氧的混合通过液体可透过的屏障——分离器10b得以阻止，如图所示，分离器10b通过自倾斜的表面12b′和14b偏转氧和氢防止其进入、流动或传输而高效地分离气体。或者，分离器10b可以包括由电绝缘导体或自惰性介电材料如填充30％玻璃的乙烯-三氟氯乙烯组成的螺旋形物，其中所述螺旋形条带材料的横截面为“V”形构造，如图所示，以充当电绝缘器和气体分离器。Mixing of hydrogen and oxygen released from 40' or inside vessel 4b is prevented by a liquid permeable barrier - separator 10b, as shown, by deflecting oxygen and hydrogen from inclined surfaces 12b' and 14b Efficiently separates gases by preventing their entry, flow or transport. Alternatively, separator 10b may comprise a spiral formed of an electrically insulated conductor or self-inert dielectric material such as 30% glass-filled ethylene-chlorotrifluoroethylene, wherein the spiral strip material has a cross-section of "V" shaped configuration, as shown, to act as electrical insulators and gas separators.

供流体行进的通路可按需要增加以满足流体循环和分配的需要，做法是偶尔或连续地波纹化条带，特别是在各个边缘处，以在各层螺旋线之间产生间隙，或者在所形成的盘的堆叠处，所述盘构成图2B中所示的截面，截面图中13b处示出了放大的波纹。通常有利的是，让各个这样的波纹或多或少地绕着适当倾斜的径向轴(如图所示关于轴15b和15b′)起伏。这可使得所形成的分离器10b的液体可透过但气体被阻挡的壁总厚度为所需的厚度，例如约0.2mm(0.008″)厚或更小。The passages for fluid travel can be increased as needed to meet fluid circulation and distribution needs by occasionally or continuously corrugating the strip, especially at each edge to create gaps between the layers of helix, or at all Where a stack of disks is formed, said disks constitute the cross-section shown in Figure 2B, in which the corrugations are shown enlarged at 13b. It is generally advantageous to have each such corrugation undulate more or less about a suitably inclined radial axis (as shown with respect to axes 15b and 15b'). This can result in the separator 10b being formed with a total liquid permeable but gas barrier wall thickness of a desired thickness, for example about 0.2 mm (0.008") thick or less.

分离器10b可以具有任何合适的尺寸，包括非常小的尺寸，且就表面能状况而论，足以允许液体电解质传向或传离电极8b但因气体的浮力驱动和向上行进而不允许气体的通行。提供了一种适用于例如相对较小的燃料电池和电解器中的可供选择的实施方案，做法是提供大量紧密间隔的具有图2B中所示横截面的扁平线，其中这样的线被织造或粘附于提供液体的主要开放的入口并在“V”形线的一侧或两侧上排列在主要竖直的方向上的线。这可使得所形成的分离器10b的液体可透过但气体被阻挡的壁总厚度为约0.1mm(0.004″)厚或更小。Separator 10b may be of any suitable size, including very small sizes, and sufficient in terms of surface energy conditions to allow passage of liquid electrolyte to and from electrodes 8b but not to allow passage of gas due to its buoyant drive and upward travel . An alternative embodiment suitable for use in, for example, relatively small fuel cells and electrolyzers is provided by providing a large number of closely spaced flat wires having the cross-section shown in Figure 2B, wherein such wires are woven Or adhere to a line that provides a mainly open inlet for liquid and is aligned in a mainly vertical direction on one or both sides of the "V" shaped line. This can result in the separator 10b being formed with a total liquid permeable but gas barrier wall thickness of about 0.1 mm (0.004") thick or less.

向上的浮力驱动使得碰撞在倾斜表面12b和14b上的气泡偏转方向。这种特征将克服现有技术的常规方法的困难和问题，这些常规方法因电阻、结垢、滞流、腐蚀和极化损耗中的一者或多者而导致低效率。此外，由于上升气泡的浮力抽吸作用产生电解质的向上流动，故一些构造可能促进电解质在同心层中的循环，且随着气体在液体顶部处逃逸，相对无气体且密度较大的电解质将流向底部从而再循环以替代混合了气泡或含溶解的气体的较小密度的电解质。热交换器56b可以根据需要运行以自从容器4b的顶部向底部循环的电解质加热或移走热，如图所示。泵36b可以根据需要使用以提高电解质循环的速率，或者泵36b可与泵40b结合使用以添加补充水。The upward buoyancy drive deflects the direction of the air bubbles impinging on the inclined surfaces 12b and 14b. Such a feature would overcome the difficulties and problems of conventional methods of the prior art which lead to inefficiencies due to one or more of electrical resistance, fouling, stagnation, corrosion and polarization losses. Furthermore, some configurations may facilitate the circulation of electrolyte in concentric layers due to the upward flow of electrolyte due to the buoyant pumping action of rising bubbles, and as gas escapes at the top of the liquid, the relatively gas-free and denser electrolyte will flow toward The bottom is thus recirculated to replace the less dense electrolyte mixed with air bubbles or containing dissolved gas. The heat exchanger 56b can be operated as needed to heat or remove heat from the electrolyte circulating from the top to the bottom of the vessel 4b, as shown. Pump 36b can be used as needed to increase the rate of electrolyte circulation, or pump 36b can be used in conjunction with pump 40b to add make-up water.

在一些实施方案中施加了高电流密度，包括快速添加有机材料的系统。在这样的实施方案中，用泵36b循环电解质可能是有利的，如图所示，所述泵36将通过配件28b和管线34b到达泵36b的相对无气体的电解质通过管线38b和配件16b返回到容器4b。可能优选在配件16b处成切线地进入返回的电解质以产生旋流递送，该旋流继续打漩并因此协同地增强分离，包括通过可如上所述利用的分离器10b的作用。取决于运行的压力，氢的密度比氧小约十四倍而具有更大浮力并倾向于易于被分离器10b引导具有更高的向上速度以通过过滤器48b在配件26b处加压收集。在非常高的电流密度及电解电池2b经受到如运输应用中可能遭遇的倾斜或G-力的情况下，通过泵36b提高电解质行进的速度以增强旋流分离并因此防止阳极上产生的气体与阴极上产生的气体混合。High current densities are applied in some embodiments, including systems for the rapid addition of organic materials. In such an embodiment, it may be advantageous to circulate the electrolyte with pump 36b which, as shown, returns relatively gas-free electrolyte that reaches pump 36b via fitting 28b and line 34b to return via line 38b and fitting 16b to container 4b. It may be preferable to enter the returning electrolyte tangentially at fitting 16b to create a delivery of swirling flow which continues to swirl and thus synergistically enhances separation, including through the action of separator 10b which may be utilized as described above. Depending on the operating pressure, hydrogen is approximately fourteen times less dense than oxygen to be more buoyant and tends to be easily directed by separator 10b with a higher upward velocity to be collected under pressure at fitting 26b through filter 48b. At very high current densities and where the electrolysis cell 2b is subjected to inclination or G-forces such as might be encountered in transport applications, the speed at which the electrolyte travels is increased by the pump 36b to enhance cyclone separation and thus prevent the gas generated on the anode from being separated from the Gases produced at the cathode mix.

一些包括分离器10b的非导电气体屏障的实施方案和液体传输实施方案使得可以制造比先前的方法便宜得多并坚固且高效得多的可逆电解器，先前的方法包括依靠质子交换膜来分离气体如氢和氧的那些。在一个方面，分离器10b可以设计成改善电解过程中电解质的流动。例如，分离器10b可以被构造为促进离子在液体电解质持液中从端口16b向端口28b向上行进的螺旋流动。这将确保电极的各个部分接收到新鲜补充的离子密度，这是获得最大电效率所需要的。随着氢和氧在电化学电池的相应电极上形成，这样的电极洗涤动作还可快速移走氢和氧的气泡。Some embodiments of the non-conductive gas barrier including the separator 10b and liquid transport embodiments allow the fabrication of reversible electrolyzers that are much less expensive, robust and efficient than previous methods that included reliance on proton exchange membranes to separate gases Such as those of hydrogen and oxygen. In one aspect, separator 10b can be designed to improve the flow of electrolyte during electrolysis. For example, separator 10b may be configured to facilitate a helical flow of ions traveling upwardly from port 16b to port 28b in the liquid electrolyte holdup. This will ensure that all parts of the electrode receive a fresh replenishment of ion density, which is required for maximum electrical efficiency. Such electrode washing action also rapidly dislodges hydrogen and oxygen bubbles as they form on the corresponding electrodes of the electrochemical cell.

图3B示出了分离器10b的另一方面的部件板或螺旋条带的代表性部分的边视图，其用于提供相邻电极(包括平板和同心电极结构)的电绝缘，同时获得如上所述气体物质的分离。在组件11b中，板12b′和14b′形成与分离器10b相似并用作分离器10b那样的功能的横截面。扁平的导电或非导电聚合物板12b′制成为在平行的中心线上具有大量小孔，这些孔倾斜为与如图所示板12b′的长轴形成例如约35°到70°角的实质性角度，例如如第一角15b所示。聚合物板14b′类似地制成为在平行的中心线上具有大量小孔，这些孔实质上倾斜为与如图所示板14b′的长轴形成约35°到70°的角，如第二角15b′所示。Figure 3B shows an edge view of a representative portion of a component plate or helical strip of another aspect of separator 10b, which is used to provide electrical isolation of adjacent electrodes (including flat plate and concentric electrode structures) while achieving the same as described above. Separation of gaseous substances. In assembly 11b, plates 12b' and 14b' form a cross-section similar to and function as separator 10b. A flat conductive or non-conductive polymeric plate 12b' is made with a plurality of small holes on parallel centerlines that are inclined to form substantially an angle of, for example, about 35° to 70° with the long axis of the plate 12b' as shown. Sexual angle, such as shown in the first angle 15b. The polymeric plate 14b' is similarly made with a plurality of small holes on parallel centerlines that are substantially inclined to form an angle of about 35° to 70° with the major axis of the plate 14b' as shown, as shown in the second Angle 15b 'shown.

在其他实施方案中，角15b和15b′可随电解过程中待分离的材料而异。例如，对于无气体组分或仅一种气体组分的化合物的电解，所述角可以下倾。如果在冰晶石-氧化铝电解质中电解解离化合物如Al₂O₃以形成铝和氧，则由于铝的密度比冰晶石-氧化铝电解质的大，故铝分离阴极电极或相关的分离器应被构造(通过例如下倾的角)为向下发送铝而远离向上行进的氧。In other embodiments, angles 15b and 15b' may vary depending on the material to be separated during electrolysis. For example, for the electrolysis of compounds with no gas components or only one gas component, the angle can be tilted down. If a dissociated_compound such as_Al2O3 is electrolyzed in a cryolite-alumina electrolyte to form aluminum and oxygen, the aluminum separation cathode electrode or associated separator should Constructed (by, for example, a down-sloping angle) to send aluminum downward away from oxygen traveling upward.

大量直径为板厚度尺寸的约1/12到1/3的这类小孔可易于通过合适的技术包括激光打孔、热针穿孔或通过高速颗粒穿透在板12b′和14b′中制得。各自通常厚约0.025至0.25mm(0.001″至0.10″)的板12b′和14b′可通过焊接或者粘结、线系、松紧带或在所产生的外径上螺旋缠绕一根或多根导电或非导电的丝固定在一起以形成为包括电极8b的组件。板12b′和14b′还可以偶尔或连续地通过粘合剂或通过热熔接或溶剂熔接而结合。因此，在板12b′的倾斜孔与板14b′的孔搭接之处，将形成使得液体和/或电解质能够行进的通路，而同时阻止气体传输通过所形成的气体屏障膜。参见图1B和4B，对于实施方案2b或100b，可以通过粘附或焊接对接缝或通过提供用作旨在分离气体的屏障的搭接缝形成具有适宜直径的管状结构的气体屏障板组件。A large number of such small holes having a diameter of about 1/12 to 1/3 of the plate thickness dimension can be readily produced in the plates 12b' and 14b' by suitable techniques including laser drilling, hot needle perforation or by high velocity particle penetration . Plates 12b' and 14b', each typically about 0.025 to 0.25 mm (0.001" to 0.10") thick, may be welded or bonded, wire tied, elasticated, or helically wound with one or more conductive or The non-conductive wires are secured together to form an assembly comprising the electrode 8b. Plates 12b' and 14b' may also be joined occasionally or continuously by adhesive or by heat or solvent welding. Thus, where the angled apertures of plate 12b' overlap the apertures of plate 14b', pathways will be formed that allow liquid and/or electrolyte to travel while at the same time preventing gas transport through the formed gas barrier membrane. Referring to Figures IB and 4B, for either embodiment 2b or 100b, the gas barrier panel assembly may be formed of a tubular structure of suitable diameter by gluing or welding butt seams or by providing lap seams that serve as barriers intended to separate gases.

对于水的电解，有多种合适的电解质。在一个实施方案中可以使用氢氧化钾，密闭壳4b采用低碳钢。可以用镀镍缸4b或通过利用合适的不锈钢合金提供更长的寿命和更高的耐腐蚀性。在其他方面，可以通过用高强度增强材料如玻璃、陶瓷或碳丝或其组合包绕缸4b而提供更高的密闭能力。For the electrolysis of water, there are various suitable electrolytes. In one embodiment, potassium hydroxide can be used, and the airtight shell 4b is made of low carbon steel. Longer life and higher corrosion resistance can be provided with nickel plated cylinder 4b or by utilizing a suitable stainless steel alloy. In other respects, higher sealing capabilities can be provided by wrapping the cylinder 4b with a high strength reinforcing material such as glass, ceramic or carbon filaments or a combination thereof.

取决于特定的应用和强度需要，对绝缘分离器20b和24b使用填充了约30％玻璃的乙烯-三氟氯乙烯可能是有利的。电极8b可以由织造的镍或316型不锈钢丝制成。分离器10b可以由填充了约30％玻璃的乙烯-三氟氯乙烯条带制成。Depending on the particular application and strength requirements, it may be advantageous to use about 30% glass filled ethylene chlorotrifluoroethylene for insulating separators 20b and 24b. Electrode 8b can be made of woven nickel or type 316 stainless steel wire. Separator 10b may be made of ethylene-chlorotrifluoroethylene strips filled with about 30% glass.

在另一实施方案中，还旨在利用电的受控施加来分别地产生甲烷或氢或在与有机电解质的优选混合物中。在一些方面，该实施方案可以与包括序列号09/969,860在内的共同待决专利申请的实施方案结合地运行，该专利申请通过引用并入本文中。平常产生甲烷的有机材料的缺氧消化过程可以经控制以产生在比解离水所需低得多的电压下释放氢的电解质，或者脉宽调制工作循环接通时间和所产生的电消费比解离水所需的要少。In another embodiment, it is also intended to utilize the controlled application of electricity to generate methane or hydrogen separately or in a preferred mixture with an organic electrolyte. In some aspects, this embodiment may operate in conjunction with embodiments of co-pending patent applications including Serial No. 09/969,860, which is incorporated herein by reference. Anoxic digestion of organic materials that normally produce methane can be controlled to produce electrolytes that release hydrogen at much lower voltages than required to dissociate water, or pulse width modulated duty cycle on-time and resulting electricity consumption ratio Less is needed to dissociate water.

微生物消化产生的有机溶液的酸度或pH可以通过天然的碳酸氢盐缓冲相互作用来保持。碳酸氢盐缓冲液可以通过消化过程中二氧化碳的共同产生来补充。对于有机化合物的缺氧消化过程中的多个步骤，可以用简单的碳水化合物或葡萄糖的示例性消化来归纳该过程，该示例性消化可能有许多竞争性的和补充性的过程步骤如：The acidity, or pH, of organic solutions produced by microbial digestion can be maintained by natural bicarbonate buffering interactions. The bicarbonate buffer can be supplemented by the co-production of carbon dioxide during digestion. For the multiple steps in the anoxic digestion of organic compounds, the process can be generalized with an exemplary digestion of simple carbohydrates or glucose, which may have many competing and complementary process steps such as:

C₆H₁₂O₆+(缺氧成酸剂，兼性细菌)→CH₃COOH        方程式1C₆ H₁₂ O₆ + (anoxic acid former, facultative bacteria) → CH₃ COOH Equation 1

CH₃COOH+NH₄HC₆O₃→CH₃COONH₄+H₂O+CO₂            方程式2CH₃ COOH+NH₄ HC₆ O₃ →CH₃ COONH₄ +H₂ O+CO₂ Equation 2

3CH₃COONH₄+3H₂O(细菌)→3CH₄+3NH₄HCO₃           方程式33CH₃ COONH₄ +3H₂ O (bacteria) → 3CH₄ +3NH₄ HCO₃ equation 3

在需要来自这类溶液的甲烷的情况下，可能需要将pH控制在7.0附近。在环境压力、约7.0的pH和35-37℃(99°F)下，将有利于甲烷生成。大多数生活污水含有具有提供甲烷生成的生物体所需要的大量和微量营养素二者的生物废弃物。在缺氧反应器中保持相对较大的溶解和分布氢的浓度或存在的单糖的浓度可以抑制产甲烷微生物的工作。Where methane from such solutions is desired, it may be necessary to control the pH around 7.0. Methanogenesis will be favored at ambient pressure, a pH of about 7.0, and 35-37°C (99°F). Most domestic sewage contains biowaste with both macro and micronutrients required by methane producing organisms. Maintaining a relatively large concentration of dissolved and distributed hydrogen or the concentration of monosaccharides present in an anoxic reactor can inhibit the work of methanogenic microorganisms.

在另一方面，可以通过施加电场使得通过葡萄糖和其他有机化合物的细菌分解和通过其他产酸过程产生的物质如乙酸(CH₃COOH)解离来增加燃料值自有机物质的生产，其中所述解离产生氢离子。On the other hand, the production of fuel value from organic matter can be increased by applying an electric field to dissociate by bacterial breakdown of glucose and other organic compounds and by other acidogenic processes such as acetic acid (_CH3COOH ), wherein Dissociation produces hydrogen ions.

CH₃COOH→CH₃COO^-+H⁺                           方程式4CH₃ COOH → CH₃ COO^- +H⁺ Equation 4

氢离子迁移或被递送至带负电荷的电极并获得电子而产生氢气。The hydrogen ions migrate or are delivered to the negatively charged electrode and gain electrons to generate hydrogen gas.

2H⁺+2e^-→H₂                                方程式52H⁺ +2e^- → H₂ equation 5

带负电荷的电极供给两个电子。在另一电极处，电化学反应包括醋酸根离子的氧化以产生二氧化碳和氢离子，如方程式6所概括。The negatively charged electrode donates two electrons. At the other electrode, the electrochemical reaction involves the oxidation of acetate ions to produce carbon dioxide and hydrogen ions, as outlined in Equation 6.

CH₃COO^-+2H₂O→2CO₂+7H⁺+电子                方程式6CH₃ COO^- +2H₂ O→2CO₂ +7H⁺⁺ electron Equation 6

在此电极反应中，醋酸根离子失去电子，随后与水反应并分解为二氧化碳气体和氢离子。二氧化碳使溶液饱和并从液体溶液界面释放，如上面的实施方案中所述。氢离子循环和/或迁移直至电子从相反电极被接收而产生氢原子和然后双原子分子，如方程式5中所概括，以在这样的系统中分开共收集。分开收集是高度有利的，例如，分开收集以使得作为液体泵送而不是气体压缩的结果取得加压或处于高压力下将尤其有效，并将大大减少分离和然后机械压缩所产生的氢、甲烷或二氧化碳通常所需的固定设备。In this electrode reaction, acetate ions lose electrons and subsequently react with water and decompose into carbon dioxide gas and hydrogen ions. Carbon dioxide saturates the solution and is released from the liquid solution interface as described in the above embodiments. Hydrogen ions cycle and/or migrate until electrons are received from the opposite electrode to generate hydrogen atoms and then diatomic molecules, as outlined in Equation 5, for separate co-collection in such systems. Separate collection is highly advantageous, e.g. separate collection so that pressurization or at high pressure is achieved as a result of liquid pumping rather than gas compression would be especially effective and would greatly reduce hydrogen, methane produced by separation and then mechanical compression or CO2 normally required for fixtures.

化合物如乙酸通过缺氧消化分解产生氢和二氧化碳所需要的能量比水的电解要少得多，部分因为消化分解产生氢离子和放热能。酸如乙酸的放热分解的起动和保持可在较低的电压施加下或通过间歇的或偶尔的电解而不是如分解水通常所需的连续电解实现。环境温度下水的生成自由能相当大(至少1KWH＝3,412BTU的释氢)，相比之下，消化池物质和酸如尿素和乙酸电解成氢和二氧化碳需要相对极小的活化和/或催化作用，特别是使用有机催化剂时。因此，结合本文中所述电极系统使用选定的催化剂包括改性的Raney-Nickel催化剂、镍-锡-铝合金、铂金属族中选择的、铂-镍和其他铂-过渡金属单晶合金表面及各种有机催化剂将进一步提高氢生产的速率和/或效率。The decomposition of compounds such as acetic acid by anaerobic digestion to produce hydrogen and carbon dioxide requires much less energy than the electrolysis of water, in part because of the production of hydrogen ions and exothermic energy from the digestion decomposition. Initiation and maintenance of exothermic decomposition of acids such as acetic acid can be achieved at lower voltage applications or by intermittent or occasional electrolysis rather than continuous electrolysis as is often required for splitting water. The free energy of formation of water at ambient temperature is considerable (at least 1 KWH = 3,412 BTU of hydrogen release), in contrast, the electrolysis of digester substances and acids such as urea and acetic acid to hydrogen and carbon dioxide requires relatively minimal activation and/or catalysis , especially when using organic catalysts. Therefore, selected catalysts for use in conjunction with the electrode systems described herein include modified Raney-Nickel catalysts, nickel-tin-aluminum alloys, selected from the platinum metal group, platinum-nickel and other platinum-transition metal single crystal alloy surfaces And various organic catalysts will further increase the rate and/or efficiency of hydrogen production.

在另一方面，可能优选利用为数众多的电池，其电极对可切换地串联或并联或串并联以匹配可得到的源安培数和电压与通过串联电池解离所需的电压，例如图1B中所示。在此实施方案的一个方面，取决于所选或自有机物质以生物化学方式产生的含水电解质，各个电池可能需要约0.2至2伏特，故一个家用尺寸的6伏特光伏源可具有3至30个串联的电池，而一个220伏特的工业源可具有约100至1,000个串联连接的电极电池。产品气体可易于通过并联或串联连接布置递送。取决于调节串联和/或并联连接的数量的所需灵活性，支承和流量控制特征18b可以选自绝缘或非绝缘材料。On the other hand, it may be preferable to utilize a large number of cells with electrode pairs switchable in series or in parallel or series-parallel to match available source amperage and voltage to that required for dissociation by series cells, such as in Figure 1B shown. In one aspect of this embodiment, each cell may require about 0.2 to 2 volts depending on the aqueous electrolyte selected or biochemically generated from organic matter, so a household size 6 volt photovoltaic source may have 3 to 30 batteries in series, while a 220 volt industrial source may have about 100 to 1,000 pole batteries connected in series. Product gas can be easily delivered through parallel or series connection arrangements. The support and flow control features 18b may be selected from insulating or non-insulating materials depending on the desired flexibility in adjusting the number of series and/or parallel connections.

在各种电流密度下，包括在中等和低电流密度下，可能优选让所生成的气泡的浮力驱动来实现电解质的循环以防止离子耗尽和滞流问题。在启动时或更高的电流密度下，可以运行泵36b和热交换器56b以提供所需的运行温度和在电极表面处提供富离子的电解质。这使得实现特别高的能量转化速率，其中能量如可从太阳、风、落水或波浪资源得到的低谷电被用来快速且高效地产生氧和氢或氢和二氧化碳或氢和甲烷及二氧化碳的高压供给以分开储存和使用。At various current densities, including moderate and low current densities, it may be preferable to let the buoyancy of the generated gas bubbles drive the circulation of the electrolyte to prevent ion depletion and stagnation problems. At startup or at higher current densities, the pump 36b and heat exchanger 56b can be operated to provide the desired operating temperature and ion-rich electrolyte at the electrode surfaces. This enables particularly high rates of energy conversion, where energy such as valley electricity available from solar, wind, falling water or wave sources is used to quickly and efficiently produce high pressures of oxygen and hydrogen or hydrogen and carbon dioxide or hydrogen and methane and carbon dioxide Supplied for separate storage and use.

在此实施方案的一个方面，解决了车辆再生制动或电厂停转中突然爆发的大量能量必须快速转化为化学燃料势能的问题。用于卡车、公共汽车或火车推进的常规燃料电池不能耐受突然施加到燃料电池电极上的高电流密度。本实施方案克服了该限制并提供了特别强的高电流情况耐受性，同时获得高电解效率而无再生性PEM燃料电池遭遇的PEM退化或电极界面失效的问题。由于结构坚固并具有特别充分的冷却机会，故易于适应特别高的电流下的运行。反过来说，本实施方案易于启动并在严苛的寒冷或炎热条件下高效地运行而无PEM相关的各种困难、限制和失效。In one aspect of this embodiment, the problem of sudden large bursts of energy in regenerative braking of a vehicle or in a power plant stall that must be quickly converted to chemical fuel potential energy is addressed. Conventional fuel cells used for truck, bus or train propulsion cannot tolerate high current densities suddenly applied to the fuel cell electrodes. The present embodiment overcomes this limitation and provides exceptional high current condition tolerance while achieving high electrolysis efficiency without the problems of PEM degradation or electrode interface failure encountered with regenerative PEM fuel cells. Operation at particularly high currents is easily adapted due to the robust construction and the particularly adequate cooling opportunities. Conversely, this embodiment is easy to start up and efficiently operates under severe cold or hot conditions without the difficulties, limitations and failures associated with PEMs.

在另一方面，为在能量转化系统如水力发电站、风电场、波浪发电机系统或常规电厂中获得高得多的投资收益，本实施方案允许低谷电通过水的解离快速且高效地转化为氢和氧或者通过有机物质的缺氧消化或降解所生成的物质的解离快速且高效地转化为氢和二氧化碳。本实施方案的紧凑型式占据的空间可以不比洗衣机大且将否则可能被浪费掉的低谷电转化为足够运行两辆家用大小车辆的氢并提供住宅的能量需要。On the other hand, for a much higher return on investment in energy conversion systems such as hydroelectric plants, wind farms, wave generator systems or conventional power plants, this embodiment allows for fast and efficient conversion of low valley electricity through dissociation of water The dissociation of substances produced to hydrogen and oxygen or by anaerobic digestion or degradation of organic substances is quickly and efficiently converted to hydrogen and carbon dioxide. A compact version of this embodiment can take up no more space than a washing machine and convert low-peak electricity that would otherwise be wasted into enough hydrogen to run two family-sized vehicles and provide the energy needs of a home.

如上所述，本文中提供的一些实施方案将提供更高效的传质，包括快速离子补充过程和通过自较大密度的液体介质逃逸的低密度气体的抽吸作用向所需电极的递送。这将确保更高的电效率、更快的解离和更高的分离效率，此外还阻止不希望有的副反应。提高离子的产生及向电极的递送的速率和效率将提高系统效率和每电极面积的电流极限值。将有机物质转化为二氧化碳和氢或甲烷的应用因如下原因而特别受益：有机物质向参与该过程的微生物的递送速率提高，孵育速率和孵育后的微生物向长寿命且自修复生物膜介质的传递速率提高，所产生的气体得到更快分离，有机物质得到更快传递，此外，中间体离子向电极的传递更高效。As noted above, some embodiments provided herein will provide more efficient mass transfer, including rapid ion replenishment processes and delivery to desired electrodes through the pumping action of low density gases escaping from denser liquid media. This will ensure higher electrical efficiency, faster dissociation and higher separation efficiency, in addition to preventing undesired side reactions. Increasing the rate and efficiency of ion generation and delivery to electrodes will increase system efficiency and current limit per electrode area. Applications that convert organic matter to carbon dioxide and hydrogen or methane are particularly beneficial due to increased rates of delivery of organic matter to microorganisms involved in the process, incubation rates and delivery of incubated microorganisms to long-lived and self-healing biofilm media The increased rate results in faster separation of the generated gases, faster transfer of organic species, and more efficient transfer of intermediate ions to the electrodes.

参见图4B，其中示出了另一个实施方案——电解电池100b，在其中不希望施加电压或不希望有电流经过密闭壳102b的内壁的应用中，该电解电池100b特别有利。本实施方案还将促进电解电池100b内双极或多电极组或电池如110b和114b的串联连接以简化气体收集和电压匹配需要。Referring to FIG. 4B, there is shown another embodiment, an electrolytic cell 100b, which is particularly advantageous in applications where it is not desired to apply a voltage or to have a current flow through the inner walls of the containment enclosure 102b. This embodiment will also facilitate series connection of bipolar or multi-electrode sets or cells such as 110b and 114b within electrolysis cell 100b to simplify gas collection and voltage matching requirements.

在其中密闭壳102b为圆柱形且其内的部件同心的一个方面，电极组件110b和114b可以自为数众多的嵌套式截锥形部件形成或者一个或两个电极可以形成为如上所述螺旋电极。电极110b和114b可具有相同、相似或不同的构造。在另一方面，电极114b可以自嵌套的截锥形部分组装或者其可以是连续地环绕电极110b的螺旋形电极。In one aspect where the containment shell 102b is cylindrical and the components inside are concentric, the electrode assemblies 110b and 114b may be formed from a plurality of nested frusto-conical components or one or both electrodes may be formed as helical electrodes as described above . Electrodes 110b and 114b may have the same, similar or different configurations. In another aspect, electrode 114b may be assembled from nested frusto-conical sections or it may be a helical electrode that continuously surrounds electrode 110b.

为防止短路，电极110b和114b的电分离可以通过多种措施实现，包括通过受控的运行尺寸公差和/或通过使用安置在电极110b和114b之间的介电线或长丝和/或如关于图2B和5B所公开的通过另一形式的分离器10b或111b实现。To prevent short circuits, the electrical separation of electrodes 110b and 114b can be achieved by various means, including by controlled running dimensional tolerances and/or by using a dielectric wire or filament disposed between electrodes 110b and 114b and/or as What is disclosed with respect to Figures 2B and 5B is achieved by another form of separator 10b or 111b.

电解电池100b可以被加压。压力密闭由上盖和下盖104b和106b提供，如图所示。绝缘器120b和122b由盖104b和106b支承，如图所示。用于电连接和流体连接的电路部件和硬件是示例性的并可根据需要通过穿透盖104b和106b实现以满足具体的应用需要。The electrolytic cell 100b may be pressurized. Pressure tightness is provided by upper and lower covers 104b and 106b, as shown. Insulators 120b and 122b are supported by covers 104b and 106b, as shown. Circuit components and hardware for electrical and fluid connections are exemplary and can be implemented through penetration covers 104b and 106b as needed to meet specific application needs.

在本实施方案中，两个电极110b和114b均形成为具有倾斜表面，所述倾斜表面将所产生的物质例如所释放的气体引导向相应的收集区，如图所示。示例性地，如果自合适的电解质解离水，则电极110b可以接收通过接头108b供给的电子，接头108b由堵塞密封件132b密封在盖106b中。电子因此通过堵塞密封件130b自电极114b取走，堵塞密封件130b提供当气体如二氧化碳或氧在电极114b上释放时接触点124b的绝缘。In this embodiment, both electrodes 110b and 114b are formed with sloped surfaces that direct generated species, such as released gases, towards respective collection regions, as shown. Illustratively, if water is dissociated from a suitable electrolyte, electrode 110b may receive electrons supplied through junction 108b, which is sealed in cap 106b by plugging seal 132b. Electrons are thus taken away from the electrode 114b through the plugging seal 130b, which provides insulation of the contact point 124b when a gas such as carbon dioxide or oxygen is released on the electrode 114b.

这样的气体因此被浮力推进而在被电极114b递送后或多或少地向上并沿容器102b的内壁行进。氢在被电极110b递送后在众多匝或锥形层电极110b所形成的中央芯内向上推进并如图所示在绝缘器120b处收集。经纯化的处于设计压力下的氢通过压力配件116b递送。可以使用催化过滤器134b来转化到达中央芯的任何氧化剂如氧以形成水。可以使用类似的催化过滤材料自到达如图所示绝缘器120b中的外收集环面的任何氢产生水。加压并经过滤的氧通过压力配件118b递送。Such gas is thus propelled by buoyancy to travel more or less upwards and along the inner wall of the container 102b after being delivered by the electrodes 114b. After being delivered by the electrode 110b, the hydrogen is pushed up within the central core formed by the numerous turns or tapered layers of the electrode 110b and collected at the insulator 120b as shown. Purified hydrogen at design pressure is delivered through pressure fitting 116b. A catalytic filter 134b may be used to convert any oxidant such as oxygen that reaches the central core to form water. Water can be generated from any hydrogen reaching the outer collecting annulus in insulator 120b as shown, using a similar catalytic filter material. Pressurized and filtered oxygen is delivered through pressure fitting 118b.

任选地，为提高电解电池100b的效率，可以使一个或多个气体收集容器(未示出)与电解电池100b流体连通以收集电解过程中形成的气体。气体收集容器可以实施以在气体的实质性膨胀之前捕集高压下的气体。气体收集容器还可以按本领域已知的方法被构造成捕集气体膨胀时所作的功。或者，气体收集容器可以被构造成提供处于适于储存、运输或使用的压力下的气体，其中所述气体需要在高压下递送。还预期所述方面可在各种电化学电池中实施。Optionally, to increase the efficiency of electrolysis cell 100b, one or more gas collection vessels (not shown) may be in fluid communication with electrolysis cell 100b to collect gases formed during electrolysis. A gas collection vessel may be implemented to trap gas at high pressure prior to substantial expansion of the gas. The gas collection vessel can also be configured to capture the work done by the gas as it expands, as is known in the art. Alternatively, the gas collection container may be configured to provide gas at a pressure suitable for storage, transport, or use where the gas needs to be delivered at elevated pressure. It is also contemplated that the described aspects can be practiced in various electrochemical cells.

参见图2B，在另一方面，可以在配件22b、配件26b之处、附近或里面或者在与配件22b或配件26b流体连通的气体收集容器中引入气体膨胀器。类似地，参见图4B，可以在配件116b、118b之处、附近或里面或者在与配件116b或配件118b流体连通的气体收集容器中引入气体膨胀器。Referring to Figure 2B, in another aspect, a gas expander may be introduced at, near or within fitting 22b, fitting 26b, or in a gas collection vessel in fluid communication with fitting 22b or fitting 26b. Similarly, referring to Fig. 4B, a gas expander may be introduced at, near or within fittings 116b, 118b or in a gas collection vessel in fluid communication with either fitting 116b or fitting 118b.

在另一方面，提供了一种加压流体的电解方法和装置，所述流体与从这样的加压流体提取功的装置相连。所述流体可以是加压的液体、吸收了液体的气体、蒸气或气体。加压流体向蒸气或气体的转化可在配件116b之中或之后进行，用于自这样的配件转化压力和流动的装置可以选自涡轮、发电机、叶片液压马达或各种活塞液压马达、或者“呼吸”空气并自116b注入加压氢气的发动机。类似地，加压流体向蒸气或气体的转化可以在配件118b之中或之后进行，用于自这样的配件转化压力和流动的装置可以选自涡轮、发电机、叶片液压马达或各种活塞液压马达或者膨胀和/或燃烧加压流体如来自118b的氧的发动机。In another aspect, there is provided a method and apparatus for the electrolysis of a pressurized fluid in connection with means for extracting work from such a pressurized fluid. The fluid may be a liquid under pressure, a gas imbibed with a liquid, a vapor or a gas. The conversion of pressurized fluid to vapor or gas may take place in or after fitting 116b, and the means for converting pressure and flow from such fittings may be selected from turbines, generators, vane hydraulic motors or various piston hydraulic motors, or Engine that "breathes" air and injects pressurized hydrogen from 116b. Similarly, conversion of pressurized fluid to vapor or gas may occur in or after fitting 118b, and the means for converting pressure and flow from such fittings may be selected from turbines, generators, vane hydraulic motors, or various piston hydraulic A motor or engine that expands and/or burns a pressurized fluid such as oxygen from 118b.

在另一方面，提供了一种克服变压器和整流器电路的高成本及功率损耗的装置和方法。这通过负载电压与源电压的调节匹配实现，所述调节匹配通过电极电池或电池内电极的串联连接实现，例如将DC源的负极性依次连接到最下面的三匝电极110b、到接下来的三匝电极114b、到接下来的三匝电极110b、到接下来的三匝电极114b、再到接下来的三匝电极110b并从相反(最高)端开始将来自DC源的正导线依次连接到三匝电极114b、到接下来的三匝电极110b、到接下来的三匝电极114b、到接下来的三匝电极110b、再到接下来的三匝电极114b。可以调节截锥的匝数和/或堆叠数以产生匹配源安培数所需的面积。In another aspect, an apparatus and method are provided that overcome the high cost and power loss of transformer and rectifier circuits. This is accomplished by a regulated match of the load voltage to the source voltage through a series connection of the pole cells or electrodes within the cell, for example connecting the negative polarity of the DC source sequentially to the lowermost three-turn electrode 110b, to the next Three turns of electrode 114b, to the next three turns of electrode 110b, to the next three turns of electrode 114b, to the next three turns of electrode 110b and sequentially connect the positive lead from the DC source to Three turns of the electrode 114b, to the next three turns of the electrode 110b, to the next three turns of the electrode 114b, to the next three turns of the electrode 110b, to the next three turns of the electrode 114b. The number of turns and/or stacking of the truncated cones can be adjusted to produce the area required to match the source amperage.

在本实施方案的另一方面，除提供电解所产生的气体的分离外，本发明的一些实施方案所产生的抽吸作用还提供养分向微生物的递送，取决于操作的相对规模，这些微生物寄宿在合适的介质如碳布、活性炭颗粒、膨胀硅石、石墨毡、煤、木炭、果核、木屑、碎纸、锯屑和/或其混合物中，这些介质通常位于电极110b的部分内和/或电极114b与容器102b的部分之间。相应的功能和好处包括系统的热稳定化、原料的循环、产物如二氧化碳的移取及氢自可能通过这类微生物的孵育、营养和生长产生的酸的生产。In another aspect of this embodiment, in addition to providing separation of gases produced by electrolysis, the pumping action produced by some embodiments of the invention also provides for the delivery of nutrients to microorganisms that, depending on the relative scale of the operation, host In a suitable medium such as carbon cloth, activated carbon granules, expanded silica, graphite felt, coal, charcoal, fruit stones, wood chips, shredded paper, sawdust and/or mixtures thereof, these media are typically located within portions of the electrode 110b and/or between the electrode 114b and the portion of the container 102b. Corresponding functions and benefits include thermal stabilization of the system, recycling of feedstock, removal of products such as carbon dioxide, and production of hydrogen from acids that may be produced by incubation, nutrition, and growth of such microorganisms.

在低和中等电流密度下，低密度溶液和气泡导致的浮力可以使电解质在容器102b内循环。在较高的电流密度下，有利的是如前面所公开的适应性地控制电解质的温度、压力和循环。电解质的外循环可以从配件126b到配件138b，如图所示，并包括其中容器102b内含一个或众多以任选串联和/或串并联电路连接的电极电池的情况。At low and moderate current densities, the low density solution and the buoyancy caused by air bubbles allow the electrolyte to circulate within the container 102b. At higher current densities, it is advantageous to adaptively control the temperature, pressure and circulation of the electrolyte as previously disclosed. External circulation of electrolyte may be from fitting 126b to fitting 138b, as shown, and includes the case where container 102b contains one or more electrode cells optionally connected in series and/or series-parallel circuits.

在另一方面，本实施方案可以针对高电流密度加以优化，以通过一个或多个孔或凹槽139b传递相称地较高的电解质流体流率，所述孔或凹槽139b与电极110b和114b之间的环形空间相切地引导流体。电解质沿电极所形成的螺旋形空间向上流动并由来自110b和114b之间的环形空间由110b和114b所提供的进入螺旋形路径的电解质所补充。进入电极110b和114b之间的空间的电解质的角动量将增大电解产物如分别在电极110b和114b上产生的氢和氧的气泡上升抽吸的推动力并加到这样的动量上。In another aspect, this embodiment can be optimized for high current densities to deliver commensurately high electrolyte fluid flow rates through one or more holes or grooves 139b that communicate with electrodes 110b and 114b. The annular space between guides the fluid tangentially. Electrolyte flows up the helical space formed by the electrodes and is replenished by electrolyte entering the helical path provided by 110b and 114b from the annular space between 110b and 114b. The angular momentum of the electrolyte entering the space between electrodes 110b and 114b will augment and add to such momentum the impetus for the upward pumping of electrolysis products such as hydrogen and oxygen bubbles produced on electrodes 110b and 114b, respectively.

为确保向和自电极110b和114b交换电荷后变为氢和氧原子或其他气体如二氧化碳的离子的快速补给以及为移取这类气体以便收集和移除同时使电解过程中的电极化损耗最小，这种电解质循环高度有利。因此易于接受非常高的电流密度以高效地电解循环的流体。在另一方面，通过因改善的电解质循环所致的设计的巨大冷却能力而提供了高电流密度的进一步适应，所述改善的电解质循环将防止电解产物的有害滞流和/或相变如水蒸汽成核及有效电极面积的减小。To ensure rapid replenishment of ions to and from the electrodes 110b and 114b after exchange of charge to hydrogen and oxygen atoms or other gases such as carbon dioxide and to pipet such gases for collection and removal while minimizing electrode polarization losses during electrolysis , such electrolyte cycling is highly favorable. It is therefore easy to accept very high current densities to efficiently electrolyze the circulating fluid. On the other hand, further accommodation of high current densities is provided by the large cooling capacity of the design due to improved electrolyte circulation which will prevent harmful stagnation and/or phase changes of electrolysis products such as water vapour. Nucleation and reduction in effective electrode area.

在另一方面，电极110b和114b可以构成弹簧形式，所述弹簧形式可以有利地在谐振频率下运行或者由各种诱因扰动，这样的诱因包括压电传动器、旋转的偏心轮、气泡形成的作用以及电解质与气泡的较小密度混合物的加速推力，因为较高密度的电解质持液将在所产生的抽吸作用下被递送至电极110b和114b的表面。响应扰动，电极110b和114b将以固有频率或者所诱导的频率振动以进一步增强气泡从包括成核位点在内的表面的移走并因此使得得到更高的电流密度和更高的能量转化效率。In another aspect, the electrodes 110b and 114b may constitute a spring form that may advantageously operate at a resonant frequency or be perturbed by various causes including piezoelectric actuators, rotating eccentrics, air bubble formation action and the accelerating thrust of the less dense mixture of electrolyte and air bubbles, as the higher density electrolyte retaining fluid will be delivered to the surfaces of electrodes 110b and 114b under the resulting pumping action. In response to the perturbation, the electrodes 110b and 114b will vibrate at natural or induced frequencies to further enhance the removal of gas bubbles from the surface including nucleation sites and thus allow for higher current densities and higher energy conversion efficiencies .

螺旋形弹簧形式的电极如110b和114b的诱导振动还可以导致蠕动机械作用，从而增强气泡向电解电池100b的相应收集路径和离开端口的加速。在此振动过程中，电极匝的相邻层之间的平均距离和角度的周期性增大和减小将产生固定或行进的节点，这取决于诱因的振幅和频率。Induced vibration of the electrodes in the form of helical springs such as 110b and 114b can also result in a peristaltic mechanical action enhancing the acceleration of gas bubbles towards the corresponding collection path and out of the ports of the electrolysis cell 100b. During this oscillation, the periodic increase and decrease in the average distance and angle between adjacent layers of electrode turns will produce stationary or traveling nodes, depending on the amplitude and frequency of the inducement.

图5B示出了用于与电极110b′和114b′之间的电绝缘间隔物111b结合运行的一组电极110b′和114b′的代表性截面图，电绝缘间隔物111b包括选择如图2B中所示用于多种应用和电解质的包括螺旋形流动递送构造的绝缘器10b。同心的电极110b′、间隔物111b和电极114b′的组件将提供非常坚固的自增强系统以以提高的效率和耐结垢性实现流体如水、来自缺氧消化池的液体或海水的高效解离。电极110b′和114b′可自导电碳纸、布或毡；碳织造物或碳毡和金属长丝、夹在碳织造物或金属长丝之间的石墨颗粒；或者镀金属的聚合物或金属板坯如软钢、镀镍钢或不锈钢构造，其或多或少如前面所公开的那样在平行的中心线上被钻以大量的孔，这些孔如图所示倾斜以自共同产生的气体如氧、氯或二氧化碳相应地分离氢，所述共同产生的气体取决于电解质的化学构成。Figure 5B shows a representative cross-sectional view of a set of electrodes 110b' and 114b' for operation in conjunction with an electrically insulating spacer 111b between electrodes 110b' and 114b', comprising a selection of electrically insulating spacers 111b as shown in Figure 2B. An insulator 10b including a helical flow delivery configuration is shown for a variety of applications and electrolytes. The assembly of concentric electrode 110b', spacer 111b and electrode 114b' will provide a very robust self-reinforcing system to achieve efficient dissociation of fluids such as water, liquid from anoxic digesters or seawater with increased efficiency and resistance to fouling . Electrodes 110b' and 114b' may be formed from conductive carbon paper, cloth or felt; carbon woven or carbon felt and metal filaments, graphite particles sandwiched between carbon woven or metal filaments; or metallized polymer or metal The slab is constructed of mild steel, nickel plated steel or stainless steel which is drilled more or less as previously disclosed on parallel centerlines with a large number of holes which are inclined as shown to free from co-generated gas As oxygen, chlorine or carbon dioxide separate hydrogen accordingly, the co-produced gas depends on the chemical composition of the electrolyte.

在电极110b′、间隔物111b和电极114b′以如图4B所示同心电极布置采用的情况下，氢被递送到端口116b，且取决于发生解离的物质，产物如氧、氯或二氧化碳被递送到端口118b。在一些情况下，优选在110b′和114b′中提供大量的孔，使得各个孔的孔径从接触间隔物111b的表面上向远离间隔物111b的出口表面略微锥形地增大。Where electrode 110b', spacer 111b, and electrode 114b' are employed in a concentric electrode arrangement as shown in FIG. Delivered to port 118b. In some cases, it is preferable to provide a large number of pores in 110b' and 114b' such that the pore size of each pore increases slightly conically from the surface contacting the spacer 111b to the outlet surface away from the spacer 111b.

优选选择螺旋节距、电极间的宽度和构成间隔物111b的条带的厚度使得以与可得到的电能和系统传热需要相称的速率从138b向并通过电极110b′和114b′向配件126b递送电解质，以优化电极间的所得宽度空间。这使得在电极110b′和114b′处有丰富的用于电解过程的离子的递送，同时确保氢分离到电极110b′内的区，而共同产生的气体如氧、二氧化碳或氯被递送到电极114b′之外的空间。The pitch of the helix, the width between the electrodes and the thickness of the strips making up the spacer 111b are preferably chosen such that the electrical energy is delivered from 138b to and through electrodes 110b' and 114b' to subassembly 126b at a rate commensurate with the available electrical power and system heat transfer needs. electrolyte to optimize the resulting width space between the electrodes. This enables an abundant delivery of ions for the electrolysis process at electrodes 110b' and 114b', while ensuring that hydrogen is separated to regions within electrode 110b', while co-produced gases such as oxygen, carbon dioxide or chlorine are delivered to electrode 114b ' outside the space.

在另一方面，可以通过在氢电极中提供气体流动凹槽、在氧电极中提供气体流动凹槽、此外还提供用于向氢电极的底部加氢和在氧电极的底部处加氧的适宜配件而再生地运行所述系统。在这种情况下，可能有利的是采用同心螺旋形电极，特别是在其中单个罐组件即满足能量需要的小燃料电池中。On the other hand, it may be possible by providing gas flow grooves in the hydrogen electrode, gas flow grooves in the oxygen electrode, and in addition suitable channels for adding hydrogen to the bottom of the hydrogen electrode and adding oxygen at the bottom of the oxygen electrode. accessories to run the system regeneratively. In such cases, it may be advantageous to employ concentric helical electrodes, especially in small fuel cells where a single canister assembly is sufficient for the energy requirements.

参见图6B，其中示出了用于可逆的燃料电池运行情况下的螺旋形电极的横截面。这将为电极114b或类似螺旋型式的电极110b提供表面/体积比、截面模量及柱稳定性的改进。该截面图中示例了电极114b，其中，气体152b沿螺旋形凹槽流动，所述螺旋形凹槽通过波纹化条带坯形成，所述条带坯用来形成螺旋并为燃料电池操作提供氧的递送及在电解操作中向环面136b和配件118b递送氧。对于在燃料电池和电解模式下的电极110b，同样的构造也适用于在电解模式下将有机酸转化为二氧化碳和氢并确保大量的气体如前所述被递送到所需的收集或源端口。Referring to Figure 6B, there is shown a cross-section of a helical electrode for reversible fuel cell operation. This would provide improvements in surface/volume ratio, section modulus, and column stability for electrode 114b or a similar spiral pattern of electrode 110b. Electrode 114b is illustrated in this cross-sectional view where gas 152b flows along helical grooves formed by corrugating a strip stock used to form the spiral and provide oxygen for fuel cell operation. The delivery of oxygen to the annulus 136b and fitting 118b during electrolysis operation. The same configuration applies to electrode 110b in fuel cell and electrolysis mode to convert organic acids to carbon dioxide and hydrogen in electrolysis mode and to ensure that the bulk gas is delivered to the desired collection or source ports as previously described.

在另一方面，通过促进将有机物质的含水衍生物如碳酸、乙酸、丁酸和乳酸以及化合物如尿素转化为氢的微生物的生长和保持而提供了改进的电极性能。在选定用于产生氢离子和/或释放二氧化碳的电极上，通过将这类电极表面制成为具有将增大有效表面积的形貌增强来提高微生物生产率，其中所述形貌增强包括高纵横比的长丝或晶须，这样的长丝或晶须将减小基质电极的电阻并帮助把微生物和生物膜同消化过程所提供的所需膜物质一起固定就位。In another aspect, improved electrode performance is provided by promoting the growth and maintenance of microorganisms that convert aqueous derivatives of organic substances such as carbonic acid, acetic acid, butyric acid, and lactic acid, as well as compounds such as urea, into hydrogen. On electrodes selected for hydrogen ion generation and/or carbon dioxide release, microbial productivity is enhanced by fabricating the surface of such electrodes with topographical enhancements that will increase the effective surface area, wherein the topographical enhancements include high aspect ratios Such filaments or whiskers will reduce the electrical resistance of the substrate electrode and help hold the microorganisms and biofilm in place along with the desired film species provided by the digestion process.

不受理论限制，据信，电极和/或分离器的特定特征如形貌处理或增强会将促进所需位置处电解质的湍流，包括空化或超空化，其继而促进该位置处的成核。反之，电极和/或分离器的特定构造可以抑制所需位置例如电子转移的点处的湍流，包括空化或超空化，其继而抑制该位置处的成核。预期，包括这些特征的元件可以在电解电池中需要成核的任何位置处实施。此外，这些相同的特征和原理可以应用于气体收集容器或与电解电池流体连通的类似容器或与其间的通道或阀门流体连通的容器。Without being bound by theory, it is believed that specific features of the electrode and/or separator, such as topography or enhancement, will promote turbulent flow of the electrolyte at the desired location, including cavitation or supercavitation, which in turn promotes formation at that location. nuclear. Conversely, specific configurations of electrodes and/or separators can suppress turbulence, including cavitation or supercavitation, at a desired location, such as the point of electron transfer, which in turn suppresses nucleation at that location. It is contemplated that elements including these features can be implemented anywhere in the electrolysis cell where nucleation is desired. Furthermore, these same features and principles can be applied to a gas collection vessel or similar vessel in fluid communication with the electrolysis cell or with a channel or valve therebetween.

合适的长丝和/或晶须包括金属或掺杂半导体如碳、硅或者氮化碳或氮化硼的纳米直径长丝以提供增大的表面积、减少离子输运损耗和电阻损耗、提高微生物生产率和使成核作用更有效以更高效地释放二氧化碳。这样的长丝还可用来锚定石墨颗粒，这将进一步改善微生物生产率、提高酶和催化剂利用效率并有利于氢离子产生过程。类似地，在其中氢离子被提供以电子而产生氢原子并成核形成双原子氢的气泡的电极处，可以利用长丝和晶须来增大有效面积和降低整个过程所需的电压。Suitable filaments and/or whiskers include nano-diameter filaments of metals or doped semiconductors such as carbon, silicon, or carbon or boron nitride to provide increased surface area, reduce ion transport losses and resistive losses, improve microbial Productivity and making nucleation more efficient for more efficient release of carbon dioxide. Such filaments could also be used to anchor graphite particles, which would further improve microbial productivity, increase enzyme and catalyst utilization efficiency, and facilitate hydrogen ion production processes. Similarly, at the electrodes where hydrogen ions are donated with electrons to generate hydrogen atoms and nucleate to form bubbles of diatomic hydrogen, filaments and whiskers can be utilized to increase the effective area and reduce the voltage required for the overall process.

除碳晶须外，还已发现自金属如锡、锌、镍和自气相沉积的难熔金属生长或自合适的衬底如铁合金电极上的镀层生长的长丝将提供减小的电阻和提高的过程效率。这类长丝或晶须可以通过下述方式制成为更适合于生物膜支承和过程增强：加入有益的表面活性剂和/或用合适的物质如碳、氮化硼或碳化硅通过溅射或自物质如来自示例性前体(如乙炔、苯或包括甲烷、乙烷、丙烷和丁烷在内的链烷气体)的供碳体的分解沉积的表面镀层。In addition to carbon whiskers, it has also been found that filaments grown from metals such as tin, zinc, nickel and from vapor-deposited refractory metals or from plating on suitable substrates such as ferroalloy electrodes will provide reduced resistance and improved process efficiency. Such filaments or whiskers can be made more suitable for biofilm support and process enhancement by adding beneficial surfactants and/or with suitable substances such as carbon, boron nitride or silicon carbide by sputtering or Surface coatings deposited from decomposition of substances such as carbon donors from exemplary precursors such as acetylene, benzene, or alkane gases including methane, ethane, propane, and butane.

图4B的实施方案及其变型可以提供流体解离的低密度气态衍生物的有利分离，包括氢自有机液体如方程式1-6中所概括的那样分离，以向端口116b递送氢或富氢的混合物，而二氧化碳或富二氧化碳的混合物(包括固定氮组分)被递送至端口118b。在一些应用中，可能期望颠倒这些电极的极性以颠倒分离开气体的递送端口。这样的颠倒可以是长期的或者是间歇的，以达到各种目的。取决于电极110b和114b的螺旋节距的选择和各个电极的谐振频率或强迫振动频率以及各个电极处的相对流体速度，氢可被递送到端口116b而系统可以运行为包括甲烷和二氧化碳。但递送到端口118b的二氧化碳可能包括甲烷和其他密度比氢高的气体。在需要提供氢与甲烷的Hy-Boost混合物以使得实现内燃机、各种燃烧器、炉或燃料电池的非节流运行的应用中，具有液压和电路控制措施(例如由泵36b和控制器52b所提供)运行的图4B实施方案将方便下述选择：以受控的氢和甲烷比率产生和分离所需的燃料混合物并在端口116b处递送。The embodiment of FIG. 4B and variations thereof can provide advantageous separation of low-density gaseous derivatives of fluid dissociation, including separation of hydrogen from organic liquids as outlined in Equations 1-6, to deliver hydrogen or hydrogen-rich hydrogen to port 116b. mixture, while carbon dioxide or a carbon dioxide-enriched mixture (including fixed nitrogen components) is delivered to port 118b. In some applications, it may be desirable to reverse the polarity of these electrodes to reverse the delivery ports of the separated gases. Such inversions can be chronic or intermittent for various purposes. Depending on the selection of the helical pitch of electrodes 110b and 114b and the resonant or forced vibration frequency of each electrode and the relative fluid velocity at each electrode, hydrogen can be delivered to port 116b and the system can be operated to include methane and carbon dioxide. However, the carbon dioxide delivered to port 118b may include methane and other gases that are denser than hydrogen. In applications where it is necessary to provide a Hy-Boost mixture of hydrogen and methane to enable unthrottled operation of internal combustion engines, various burners, furnaces or fuel cells, there are hydraulic and electrical control measures (such as provided by pump 36b and controller 52b Provided) the Figure 4B embodiment operating will facilitate the option of generating and separating the desired fuel mixture with controlled ratios of hydrogen and methane and delivering it at port 116b.

通过向电化学电池中加入介质如胶态碳、碳长丝(包括纳米结构)、层状碳晶体、石墨烯小片晶、活性炭、沸石、陶瓷和/或氮化硼颗粒，提供了一种出乎意料但特别有利的产生微生物的强大厌氧菌落的方案，所述微生物产生有机原料向氢和/或甲烷的所需转化。这类介质可以被掺杂或复配以各种试剂，以提供增强的催化生产率。示例性地，可以通过用或多或少具有电子结构的选定试剂如硼、氮、锰、硫、砷、硒、硅、碲和/或磷掺杂而提供期望的功能性。电解过程释放的气体引起的循环可以促进这类介质向有利位置和密度的协调(sorting)，从而实现更高效的电荷流利用。By adding media such as colloidal carbon, carbon filaments (including nanostructures), layered carbon crystals, graphene platelets, activated carbon, zeolites, ceramics, and/or boron nitride particles to electrochemical cells, it provides an An unexpected but particularly advantageous protocol for generating robust anaerobic colonies of microorganisms that produce the desired conversion of organic feedstocks to hydrogen and/or methane. Such media can be doped or formulated with various reagents to provide enhanced catalytic productivity. Illustratively, the desired functionality can be provided by doping with selected reagents such as boron, nitrogen, manganese, sulfur, arsenic, selenium, silicon, tellurium and/or phosphorus with more or less electronic structure. Circulation induced by gases released by the electrolysis process can facilitate the sorting of such media to favorable locations and densities for more efficient charge flow utilization.

不受特定理论限制，但据猜测，这样的协同结果与临界位置中表面积的增加及纤维状夹杂物、区域或长丝的增多有关，所述纤维状夹杂物、区域或长丝加强成核过程和/或进行电子或氢离子以及酶、氢、甲烷或二氧化碳在生物膜和所得反应区中的有利吸附。还表明，在本发明公开的各种实施方案中，微生物被孵育以循环到所进行的操作中及所产生的流动路径中被高效利用的位置。Without being bound by a particular theory, it is speculated that such a synergistic result is related to an increase in surface area in critical locations and an increase in fibrous inclusions, domains or filaments that enhance the nucleation process And/or perform advantageous adsorption of electrons or hydrogen ions as well as enzymes, hydrogen, methane or carbon dioxide in the biofilm and the resulting reaction zone. It has also been shown that, in various embodiments disclosed herein, microorganisms are incubated to recycle to locations where they are efficiently utilized in the operations performed and the resulting flow paths.

除晶须和长丝如碳、石墨、各种金属碳化物和碳化硅及其他以催化方式提高性能的无机物质和颗粒外，采用提供所需养分或催化剂以辅助微生物过程的活性物质和颗粒也将是有利的。示例性地，聚合物、陶瓷或活性炭的多孔和/或层状基材可吸附导电性有机催化剂如四甲氧基苯基卟啉钴(CoTMPP)或聚(3，4-亚乙二氧基噻吩)(PEDOT)和/或起促进作用地取向和提供其他催化物质，包括酶和接枝聚合物，所述其他催化物质也可用来引入和提供催化物质，包括另外的酶。In addition to whiskers and filaments such as carbon, graphite, various metal carbides and silicon carbide and other inorganic substances and particles that enhance performance in a catalytic manner, active substances and particles that provide the required nutrients or catalysts to assist microbial processes are also used. will be beneficial. Illustratively, porous and/or layered substrates of polymers, ceramics, or activated carbons can adsorb conductive organic catalysts such as cobalt tetramethoxyphenylporphyrin (CoTMPP) or poly(3,4-ethylenedioxy Thiophene) (PEDOT) and/or to facilitate the orientation and provision of other catalytic species, including enzymes and grafted polymers, which can also be used to introduce and provide catalytic species, including additional enzymes.

合适的物质或接枝聚合物可包括常规的树枝状体、纤维形态体及其他有机功能材料的那些以最大限度地减少或替代铂和其他昂贵的催化剂和导体。这类替代物质及其利用包括混合物或相对于本文中公开的一些实施方案所产生的流体循环的分段位置。多种专用的导电和/或催化结构包括可生长或粘附到电极4b、8b、110b或114b和/或以覆盖碳毡或织造结构或分散到生物膜挂膜中的针状沉积物和纤维。示例性地，导电和/或催化功能可通过以保持和提供氢化酶及其他酶、CoTMPP和/或其他催化剂如聚(3，4-亚乙二氧基噻吩)(PEDOT)的长丝作为纤维提供，所述长丝自表面活性剂水溶液合成为自组织、细直径、纵横比超过100的纳米纤维并提供低的电荷传导阻力。在包含阴离子表面活性剂十二烷基硫酸钠(SDS)的水溶液中的合成可适于通过改变SDS的浓度和此外通过添加FeCl₃以产生聚合的结构来产生各种构型(一种示例性的程序见述于Moon Gyu Han等人，Facile Synthesis of Poly(3，4-ethylenedioxythiophene)(PEDOT)Nanofibers from an Aqueous SurfactantSolution，Small 2，No.10，1164-69(2006)中，其通过引用并入本文中)。其他实例包括功能性催化剂和呈纳米复合材料形式的微导体，所述纳米复合材料源自纤维素纳米纤维和半导体共轭聚合物，所述半导体共轭聚合物包括具有季铵侧链的聚苯胺(PANI)和聚(对-苯乙炔)(PPE)衍生物。可将具有阴离子表面电荷的纤维素、碳或陶瓷晶须与带正电荷的共轭聚合物组合以形成稳定的分散体，这样的分散体可以自极性溶剂如甲酸溶液流延。Suitable substances or grafted polymers may include those of conventional dendrimers, fiber morphologies, and other organic functional materials to minimize or replace platinum and other expensive catalysts and conductors. Such alternative substances and their utilization include mixtures or staged locations relative to the resulting fluid circulation of some embodiments disclosed herein. A variety of specialized conductive and/or catalytic structures including needle-like deposits and fibers that can be grown or adhered to electrodes 4b, 8b, 110b or 114b and/or to cover carbon felt or woven structures or dispersed into biofilm encumbrances . Exemplarily, conductive and/or catalytic functions can be achieved by holding and providing filaments of hydrogenase and other enzymes, CoTMPP and/or other catalysts such as poly(3,4-ethylenedioxythiophene) (PEDOT) as fibers Provided, the filaments are synthesized from aqueous surfactant solutions into self-organized, fine diameter nanofibers with aspect ratios in excess of 100 and provide low resistance to charge conduction. Synthesis in aqueous solutions containing the anionic surfactant sodium dodecyl sulfate (SDS) can be adapted to produce various configurations by varying the concentration_of SDS and additionally by adding FeCl to produce polymeric structures (an exemplary The procedure is described in Moon Gyu Han et al., Facile Synthesis of Poly(3,4-ethylenedioxythiophene) (PEDOT) Nanofibers from an Aqueous Surfactant Solution, Small 2, No. 10, 1164-69 (2006), which is incorporated by reference and into this article). Other examples include functional catalysts and microconductors in the form of nanocomposites derived from cellulose nanofibers and semiconducting conjugated polymers including polyaniline with quaternary ammonium side chains (PANI) and poly(p-phenylene vinylene) (PPE) derivatives. Cellulose, carbon, or ceramic whiskers with anionic surface charges can be combined with positively charged conjugated polymers to form stable dispersions that can be cast from solutions of polar solvents such as formic acid.

制剂包括接枝聚合物和有机金属醇盐、烷基金属的端基及乙酸的催化好处和含COOH端基的聚合物催化剂的应用。除端基的混合物外，还可以选择特殊官能和双官能端基来产生多功能特性，包括催化功能、活性稳定剂、接枝剂和分散聚合的促进剂。类似地，碳或其他物质通过缺氧微生物所产生的氢和/或酶的特殊活化将提供局部富氢的环境以增强或抑制甲烷的生成并增强氢自各种有机物质的附加产生。Formulations include grafted polymers and organometallic alkoxides, metal alkyl end groups and the catalytic benefits of acetic acid and the use of COOH end group-containing polymer catalysts. In addition to mixtures of end groups, specialty functional and bifunctional end groups can be selected to create multifunctional properties, including catalytic functions, active stabilizers, grafting agents, and accelerators for dispersion polymerization. Similarly, specific activation of hydrogen and/or enzymes produced by carbon or other species by anoxic microorganisms will provide a localized hydrogen-rich environment to enhance or inhibit methane production and enhance additional production of hydrogen from various organic species.

参见图1B-3B，任选地，向圆柱形部件8b、10b、11b、110b和/或114b的外和内表面提供一个或多个补充的碳长丝的毡和/或织造筛网可能是有利的。这样的补充毡和/或织造筛网可以与电极4b、8b、110b和/或114b和/或分离器10b或11b一起相称地收集或分配电子并帮助锚定或优先安置颗粒、长丝和/或其他结构，以减少压力损失或更均等地分配液体流和促进微生物在所需能量转化运行中的功能。Referring to Figures 1B-3B, optionally, a felt and/or woven screen to provide one or more additional carbon filaments to the outer and inner surfaces of the cylindrical members 8b, 10b, 11b, 110b and/or 114b may be advantageous. Such supplemental felts and/or woven screens can collect or distribute electrons commensurately with electrodes 4b, 8b, 110b and/or 114b and/or separators 10b or 11b and help anchor or preferentially place particles, filaments and/or or other structures to reduce pressure loss or to more evenly distribute liquid flow and facilitate the function of microorganisms in the desired energy conversion operation.

在为提供氢和二氧化碳的净生产的补充性和竞争性反应及过程中，包括多个过程步骤，这些过程步骤概括在方程式8中。A number of process steps are involved in the complementary and competing reactions and processes to provide the net production of hydrogen and carbon dioxide, which are summarized in Equation 8.

碳+2H₂O→CO₂+4H⁺+4个电子       方程式8Carbon + 2H₂ O → CO₂ +4H⁺ +4 electrons Equation 8

碳如方程式8中所概括的那样被消耗，包括可能以与来自缺氧消化池或电解器或作为各种制造输出的结果的液体混合的组分或含碳物质供给的碳。示例性地，碳可以包括来自为生产电极而进行的磨削、机加工、电火花机加工(EDM)和各种热化学操作的废料、电极上的电极涂层(包括槽衬)、或颗粒物、或长丝、或絮凝剂、或通过热解离和反应过程产生的选定碳化物，包括因有机物质各种程度的脱氢产生的胶体或其他悬浮体。Carbon is consumed as outlined in Equation 8, including carbon that may be supplied as components or carbonaceous species mixed with liquids from anoxic digesters or electrolyzers or as a result of various manufacturing outputs. Illustratively, carbon may include waste from grinding, machining, electrical discharge machining (EDM), and various thermochemical operations performed to produce electrodes, electrode coatings on electrodes (including slot linings), or particulate matter , or filaments, or flocculants, or selected carbides produced by thermal dissociation and reaction processes, including colloids or other suspensions resulting from various degrees of dehydrogenation of organic matter.

这样的碳和/或供碳体原料可以由自所供给的液体接收二氧化碳和其他养分的细菌、浮游植物或较大的藻类可再生地供给，或者通过使二氧化碳循环到溶液培养和/或土壤支持的植物而可再生地供给。利用这类形式的具有高表面/体积比的碳并向其中其为驱动所示反应和为向电极表面递送氢离子的目的而递送的区提供电压梯度将是有利的，其中所述电极表面包括补充的导电介质如长丝和导电过滤物质以便于氢气泡的产生、成核和释放，从而提高制氢的总体速率。Such carbon and/or carbon donor feedstock can be supplied reproducibly by bacteria, phytoplankton, or larger algae that receive carbon dioxide and other nutrients from the supplied liquid, or by recycling carbon dioxide to hydroponics and/or soil support renewable supply of plants. It would be advantageous to utilize such a form of carbon with a high surface/volume ratio and to provide a voltage gradient to the region where it is delivered for the purpose of driving the reaction shown and delivering hydrogen ions to the electrode surface comprising Supplementary conductive media such as filaments and conductive filter substances facilitate the generation, nucleation, and release of hydrogen bubbles, thereby increasing the overall rate of hydrogen production.

增大活性表面的合适措施和/或絮凝剂包括具有有机组成部分例如细菌、蛋白、单糖和复糖、纤维素、热解离的纤维素、活的和解离的浮游植物的那些，以及各种形式的胶态碳、活性炭和碳化物。示例性地，浮游植物和/或较大的藻类可以生长、干燥、与粘结剂如玉米糖浆混合、以热的方式脱氢至各种程度并碾磨以提供细碎的絮凝剂。或者，可以碾磨活性炭原料以提供细碎的颗粒物，这些颗粒物用作酶接收器或絮凝剂介质或者其可以与前面公开的物质结合使用以增强所需的生产或酶的效率、支持所需微生物的孵育、或提高氢或甲烷产量和/或如方程式8所示消耗碳以产生氢离子用于电解。Suitable means of enlarging the active surface and/or flocculants include those with organic components such as bacteria, proteins, mono- and complex sugars, cellulose, thermally dissociated cellulose, live and dissociated phytoplankton, and various Various forms of colloidal carbon, activated carbon and carbides. Illustratively, phytoplankton and/or larger algae can be grown, dried, mixed with a binder such as corn syrup, thermally dehydrogenated to various degrees and milled to provide finely divided flocculants. Alternatively, activated carbon feedstock can be milled to provide finely divided particulates that are used as enzyme receivers or flocculant media or which can be used in combination with previously disclosed materials to enhance desired production or enzyme efficiency, support desired microbial Incubation, or increased hydrogen or methane production and/or carbon consumption as shown in Equation 8 to produce hydrogen ions for electrolysis.

如果需要，偶尔使用盐水或向基于水的电解质中加入少量的盐可产生氯而快速消毒或防止所示电解器系统的有害结垢。一些实施方案的采用，例如图5B，将使得所产生的系统能够固有地无有害结垢，甚至当采用电解质如废水、工业过程水、木灰水、海水、粉煤灰水、运河和沟渠水、或缺氧消化池液体时。此外，如果需要，这样的系统可以通过电解质或清洗水从配件118b向138b逆流移走可能已被递送到电极的颗粒物而得到快速清洗。Occasional use of brine or addition of a small amount of salt to the water-based electrolyte, if desired, can generate chlorine to quickly sanitize or prevent harmful scaling of the illustrated electrolyzer system. Employment of some embodiments, such as Figure 5B, will enable the resulting system to be inherently free of detrimental fouling, even when employing electrolytes such as wastewater, industrial process water, wood ash water, seawater, fly ash water, canal and ditch water, or when the digester fluid is depleted of oxygen. Furthermore, such a system can be quickly cleaned, if desired, by dislodging particulate matter that may have been delivered to the electrodes by electrolyte or wash water flowing countercurrently from fitting 118b to 138b.

一些实施方案的应用包括大居群水处理操作到纳米尺寸的电解器，包括对常规废弃物消化池的改进，含有机物质的溶液或“液体”从常规废弃物消化池被供给以生产氢和/或甲烷和/或二氧化碳及其他植物养分。在此能力下，一些实施方案可以提供缺氧消化池所产生的副产物的快速且高效转化并将氢离子转化成氢，以及克服甲烷生产作业的酸降解。在运行中，来自缺氧消化池的液体被用来产生氢和二氧化碳以使pH有利地恢复到7.0附近或者保持在7.0附近，而不是可能妨碍甲烷生产系统的更酸性的条件下。这使得实现总体能量转化效率的提高，因为其克服了对用来添加化学试剂以调节消化池中的pH的昂贵措施的需要。在这样的中等和大型应用中，有利的是设计和监造包括电子分配电路的多功能部件，所述多功能部件还可以提供颗粒如碳、氮化硼、沸石、聚合物和包括这类物质的陶瓷在不同地活化的条件下的所需保持力以增强性能。Applications of some embodiments include large population water treatment operations to nano-sized electrolyzers, including modifications to conventional waste digesters from which solutions or "liquids" containing organic matter are fed to produce hydrogen and /or methane and/or carbon dioxide and other plant nutrients. In this capacity, some embodiments may provide rapid and efficient conversion of by-products produced by anoxic digesters and convert hydrogen ions to hydrogen, as well as overcome acid degradation of methane production operations. In operation, liquid from the anoxic digester is used to generate hydrogen and carbon dioxide to return the pH favorably to or remain near 7.0, rather than the more acidic conditions that might hamper the methane production system. This enables an increase in overall energy conversion efficiency to be achieved as it overcomes the need for costly measures to add chemicals to adjust the pH in the digester. In such medium and large applications, it is advantageous to design and supervise multifunctional components including electronic distribution circuits, which can also be supplied with particles such as carbon, boron nitride, zeolites, polymers and substances including such The required retention of ceramics under differently activated conditions to enhance performance.

在另一方面，电解器如本文中所公开的可应用以提供通常由缺氧消化所产生的酸的快速转化，所述缺氧消化包括采用市政废水和垃圾以及来自屠宰场、牛奶场、蛋鸡场和其他动物饲养中心等的废弃物的应用。如果缺氧条件所产生的酸使得pH降到远低于7，则甲烷的生产将变慢或被抑制。如果有机材料的进给速率超过产甲烷微生物群落的能力，则可能形成这样的酸。通过从这样的酸提取氢，通过缺氧消化处理有机材料的速率可得到提高。甲烷和氢的组合将提供远远更高的每吨废弃物的净能量生产，且废弃物将得到更快的处理而增大该过程的能力。In another aspect, an electrolyzer as disclosed herein may be applied to provide rapid conversion of acids typically produced by anaerobic digestion, including the use of municipal wastewater and waste as well as from slaughterhouses, dairies, egg Application of waste from chicken farms and other animal breeding centers etc. If the acid produced by the anoxic conditions lowers the pH far below 7, methane production will be slowed or inhibited. Such acids may form if the feed rate of organic material exceeds the capacity of the methanogenic microbial community. By extracting hydrogen from such acids, the rate at which organic materials can be processed by anaerobic digestion can be increased. The combination of methane and hydrogen will provide a much higher net energy production per ton of waste, and the waste will be processed faster increasing the capacity of the process.

一些实施方案的特别有用的实施方案是在这样的废弃物-能量转化应用中：所述应用利用有机物质如污水以及在方程式1-6所概括的缺氧电消化过程中水解了的垃圾、农场废弃物和森林废材来产生氢，而氧的产生极少或无氧的产生。坚固的构造和再循环运行使得对溶解的固体能够有很高的耐受性，所述固体包括用作电解质的缺氧过程液体中的有机固体和颗粒物。产生氢而无和电解水而释放的那样相应地释放氧，将促进以废弃物为源的氢作为电气设备如发电机中的冷却气体的更高效率和使用安全。A particularly useful implementation of some embodiments is in waste-to-energy applications that utilize organic matter such as sewage and waste, farm Hydrogen is produced from waste and forest waste with little or no oxygen production. Rugged construction and recirculating operation enable high tolerance to dissolved solids including organic solids and particulates in anoxic process liquids used as electrolytes. The generation of hydrogen without the corresponding release of oxygen as released by the electrolysis of water would facilitate a more efficient and safe use of waste-sourced hydrogen as a cooling gas in electrical equipment such as generators.

在本文中公开的一些实施方案的另一应用中，如图7B中所示电解器系统900b提供了在调节器950b中通过酶、机械、热、声、电、压力和/或化学作用和过程使生物质发生组织和/或细胞破裂以实现更快或更完全的孵育器处理、消化和/或支持。含来自调节器950b的这类破裂细胞和由转化器902b所产生的相关原料的流体通过底座910b的环形分配器922b循环到电解器914b，如图所示。缺氧微生物由介质940b和942b支承并接收通过导管910b自氢分离器904b再循环的液体和通过导管908b自二氧化碳分离器906b再循环的液体，如图所示。电极918b和/或介质942b释放氢，而电极916b和/或介质940b释放二氧化碳。由源924b通过电路926b向电极916b和918b提供电动势偏压，所述偏压可以为0.1到约3VDC，这取决于化合物解离需要和临时的增大电压以克服所形成的绝缘膜的需要。氢通过沿或多或少圆锥形的表面925b行进而被输送以收集和递送到分离器904b，圆锥形表面925b可以是导电的表面，这取决于所需的串/并联变型，或者由绝缘器930b容留和支承，如图所示。In another application of some embodiments disclosed herein, electrolyzer system 900b as shown in FIG. Disrupting biomass tissue and/or cells for faster or more complete incubator processing, digestion and/or support. Fluid containing such disrupted cells from regulator 950b and associated feedstock produced by converter 902b is circulated through ring distributor 922b of base 910b to electrolyzer 914b, as shown. Anoxic microorganisms are supported by media 940b and 942b and receive liquid recirculated from hydrogen separator 904b via conduit 910b and liquid recirculated from carbon dioxide separator 906b via conduit 908b, as shown. Electrode 918b and/or medium 942b releases hydrogen, while electrode 916b and/or medium 940b releases carbon dioxide. An electromotive bias is provided to electrodes 916b and 918b from source 924b through circuit 926b, which can range from 0.1 to about 3 VDC, depending on compound dissociation needs and the need to temporarily boost the voltage to overcome the insulating film formed. The hydrogen is transported for collection and delivery to the separator 904b by traveling along a more or less conical surface 925b, which can be a conductive surface, depending on the desired series/parallel variant, or by an insulator 930b is housed and supported as shown.

在运行中，液体在分配器环面922b中混合并向上行进以提供过程反应物和为微生物提供养分，所述微生物寄宿在活性炭布和/或颗粒940b和942b和/或包住并基本上保持这类颗粒最接近电极916b和/或918b的导电毡中。可加入较小的颗粒物和长丝以渗入整个电解器系统的位置，从而增强电荷传导性、酶和催化功能，包括前面公开的那些。分离器902b可以是反渗透膜或者阳离子或阴离子交换膜或者其可以按图2B、3B、4B或5B中所示的实施方案构建，且在一些情况下，这样的分离器可以彼此结合地使用，为提供各种液体循环通路和/或为在不同的压力下产生氢和二氧化碳或使氢和二氧化碳之间具有压差时，可能需要这样。In operation, the liquid mixes and travels upward in the distributor annulus 922b to provide process reactants and nutrients for the microorganisms that are lodged in the activated carbon cloth and/or particles 940b and 942b and/or encased and substantially retained Such particles are in the conductive felt closest to electrodes 916b and/or 918b. Smaller particles and filaments can be added to penetrate locations throughout the electrolyzer system to enhance charge conductivity, enzymatic and catalytic functions, including those previously disclosed. Separator 902b may be a reverse osmosis membrane or a cation or anion exchange membrane or it may be constructed in accordance with the embodiments shown in Figures 2B, 3B, 4B or 5B, and in some cases such separators may be used in conjunction with each other, This may be required to provide various liquid circulation paths and/or to generate hydrogen and carbon dioxide at different pressures or to have a pressure differential between hydrogen and carbon dioxide.

类似地，如果电极916b与相邻的毡和/或介质940b一道用作电子源，则可以得到许多循环选择，以自从在气体升力、对流的作用下或通过泵递送而循环的液体递送的离子产生氢，如图所示。在此选择下，随着自从902b和950b所递送或由微生物(寄宿在纤维或颗粒介质942b和由电极918b加电偏压而与电极916b相反的相关毡材料中)所产生的酸产生氢离子，将释放二氧化碳。如果电子由电极918b提供，则将产生另一示例性选择而产生氢，所述氢由绝缘器930b收集以递送到气体收集器904b，如图所示。在这种情况下，电极916b和与其电相关的介质为电子收集器，因为随着二氧化碳被递送经过绝缘器930b至收集器906b，二氧化碳被释放而在所示流体回路中提供抽吸，如图所示。Similarly, if the electrode 916b is used as an electron source along with the adjacent felt and/or medium 940b, many cycling options are available for ions delivered from a liquid circulated under the action of gas lift, convection, or delivered by a pump Hydrogen is produced as shown. Under this option, hydrogen ions are generated along with acids delivered from 902b and 950b or generated by microorganisms (hosted in the fibrous or granular medium 942b and associated felt material energized by electrode 918b opposite electrode 916b) , will release carbon dioxide. If electrons are provided by electrode 918b, another exemplary option would be to produce hydrogen, which is collected by insulator 930b for delivery to gas collector 904b, as shown. In this case, the electrode 916b and the medium electrically associated therewith is an electron collector because, as the carbon dioxide is delivered through the insulator 930b to the collector 906b, the carbon dioxide is released to provide suction in the fluid circuit shown, as shown in FIG. shown.

参见图7B，系统900b可用来将有机原料如通过光合作用所产生的那些转化为甲烷、氢和/或二氧化碳和/或通过微生物。取决于所寄宿的微生物，通常含酸如乙酸和丁酸以及化合物如尿素的液体在电解器914b中解离。电解器914b在足够的电压下提供电流而自这类化合物和酸产生氢并可提供作为消化池和电解器的运行，或者可以在缺氧消化池(未示出)内运行或者可以利用914b中缺氧消化所产生的液体，如图所示。对于转化来自居群和/或工业园的有机废弃物以向居群供给燃料和原料以制造碳增强的耐用品，这样的运行特别有用。Referring to Figure 7B, system 900b can be used to convert organic feedstocks such as those produced by photosynthesis to methane, hydrogen and/or carbon dioxide and/or by microorganisms. Depending on the host microorganisms, typically liquids containing acids such as acetic and butyric acids and compounds such as urea are dissociated in the electrolyzer 914b. Electrolyzer 914b provides electrical current at sufficient voltage to generate hydrogen from such compounds and acids and may provide operation as a digester and electrolyzer, or may operate within an anoxic digester (not shown) or may utilize Liquid produced by anoxic digestion, as shown. Such operations are particularly useful for converting organic waste from populations and/or industrial parks to supply fuel and raw materials to populations for the manufacture of carbon-enhanced durable goods.

参见图8B，在另一方面，供用于电解器中的一个或多个导电电极(包括本文中所公开的那些)的布置示为包括平板(未示出)或如图所示同心电极1002b、1003b、1004b或1005b，其可以电连接为电解器的单极或双极部件。一些或所有这样的导电电极因高表面/体积比材料如隔开的石墨烯或其他厚度的层(例如碳和/或BN“过滤器”)而提供广大的表面。这可用来寄宿微生物(所述微生物分解包括挥发性脂肪酸在内的各种有机材料以释放电子和质子，用于在阴极表面处产生氢)并可实施为与任何上述实施方案一起使用。Referring to FIG. 8B, in another aspect, an arrangement of one or more conductive electrodes (including those disclosed herein) for use in an electrolyzer is shown comprising a flat plate (not shown) or as shown concentric electrodes 1002b, 1003b, 1004b or 1005b, which can be electrically connected as a monopolar or bipolar part of the electrolyzer. Some or all such conductive electrodes provide extensive surfaces due to high surface/volume ratio materials such as spaced graphene or other thick layers (eg, carbon and/or BN "filters"). This can be used to host microorganisms that break down various organic materials including volatile fatty acids to release electrons and protons for hydrogen production at the cathode surface and can be implemented for use with any of the above embodiments.

在另一方面，微生物产生以分解挥发性脂肪酸和各种其他有机物的必需酶被加到引入构成电极1002b、1004b、1006b、1008b的高表面/体积材料中的活性炭或聚合物颗粒或长丝。或者，这里描述的任何微生物、酶或促进剂可被引入到所述表面中。随着这样的酶或其他材料或促进剂被耗尽、降解或破坏，可根据需要加入补充量的这类酶、材料或促进剂。该系统允许实现促进剂的优化，包括允许微生物在分离的但提供这类酶在如图所示电解器的运行中的利用的位置处茁壮成长。In another aspect, the essential enzymes produced by the microorganisms to break down volatile fatty acids and various other organics are added to activated carbon or polymer particles or filaments incorporated into the high surface/volume material making up the electrodes 1002b, 1004b, 1006b, 1008b. Alternatively, any of the microorganisms, enzymes or promoters described herein can be introduced into the surface. As such enzymes or other materials or promoters are depleted, degraded or destroyed, supplementary amounts of such enzymes, materials or promoters can be added as needed. This system allows optimization of the promoters to be achieved, including allowing microorganisms to thrive in locations that are isolated but provide for the utilization of such enzymes in the operation of the electrolyzer as shown.

在另一实施方案中，所述必需酶、微生物或促进剂人工地产生为复制品或为不同地改变的“设计酶”，其被接枝到合适的天然聚合物如纤维素或木质纤维素或被接枝到各种工厂生产的聚合物或化合物。In another embodiment, the essential enzymes, microorganisms or promoters are artificially produced as duplicates or as differently altered "designer enzymes" that are grafted to a suitable natural polymer such as cellulose or lignocellulose Or be grafted to various factory-produced polymers or compounds.

在寄宿微生物的活菌落、或自微生物的活菌落转移的酶、或工厂复制的或不同地改变的设计酶的保持型酶系统中，需要使电解器中电解质的电阻最小化。这将促进乙酸以及各种酸和其他将随氢在所需的高压下的产生而被消耗的物质如尿素的例如方程式9中一般性地示出的过程，这同样可实施在本文所公开的任何实施方案中。In maintained enzyme systems of living colonies of host microorganisms, or enzymes transferred from living colonies of microorganisms, or factory replicated or differently altered designer enzymes, there is a need to minimize the electrical resistance of the electrolyte in the electrolyzer. This will facilitate the process shown generally in, for example, Equation 9 for acetic acid as well as various acids and other substances that will be consumed with the generation of hydrogen at the required high pressures, such as urea, which is equally applicable to the processes disclosed herein in any implementation.

CH3COOH+2H2O＝2CO2+4H2           方程式9CH3COOH+2H2O＝2CO2+4H2 Equation 9

在另一方面，用于检测化学活性物质和识别这类物质或酶的存在、能力和生命力以使得实现调节包括化学活性养分的量在内的运行条件及其他运行条件的适应性系统从而优化保持型酶系统的运行的系统可与本实施方案一起使用。同样，所述系统可以与本文中公开的任何实施方案一起实施。In another aspect, adaptive systems for detecting chemically active substances and identifying the presence, capacity and viability of such substances or enzymes to enable adjustment of operating conditions including the amount of chemically active nutrients and other operating conditions to optimize maintenance A system for the operation of a type enzyme system can be used with this embodiment. Likewise, the system can be implemented with any of the embodiments disclosed herein.

在本文中公开的任何实施方案的其他实施方案或方面中，希望在足够的压力下运行选定的微生物和/或保持的酶以增加溶解的或以其他方式保持在溶液中的CO₂的量，从而提高电解质的传导性。这将以若干方式提高系统效率和运行能力，这些方式包括：In other embodiments or aspects of any of the embodiments disclosed herein, it is desirable to operate the selected microorganisms and/or retained enzymes at sufficient pressure to increase the amount of_CO dissolved or otherwise maintained in solution , thereby improving the conductivity of the electrolyte. This will improve system efficiency and operational capability in several ways, including:

1)高压下产生的氢可以被递送至紧凑、加压地储存而不招致运行多级氢气压缩机的基建费用、维护或能量花费。1) Hydrogen produced at high pressure can be delivered to compact, pressurized storage without incurring the capital costs, maintenance or energy costs of running multi-stage hydrogen compressors.

2)高压下产生的氢可以直接进入加压管道以传输向市场。2) Hydrogen produced under high pressure can go directly into pressurized pipelines for transport to the market.

3)高压下产生的氢可以用来加压其他反应物以使得能够反应或加速反应。示例性地，加压的氢可以被加到合适的反应器中的氮中以产生氨或其他产物。3) Hydrogen produced at high pressure can be used to pressurize other reactants to enable or accelerate reactions. Illustratively, pressurized hydrogen may be added to nitrogen in a suitable reactor to produce ammonia or other products.

4)加压以防止电解器电极表面上的二氧化碳释放或使所述释放最小化将大大简化电解器设计。4) Pressurization to prevent or minimize the release of carbon dioxide on the electrolyzer electrode surfaces would greatly simplify the electrolyzer design.

5)通过从经加压的电解器或合适的子系统在高压下收集氢和在另一位置处或通过另一子系统在减压后收集二氧化碳实现了氢与二氧化碳生产的分离。5) Separation of hydrogen from carbon dioxide production is achieved by collecting hydrogen at high pressure from a pressurized electrolyzer or suitable subsystem and carbon dioxide after depressurization at another location or through another subsystem.

参见图9B，其中示出了系统1100b，该系统1100b包括高压电解器1102b，高压电解器1102b可以自合适的泵1114b接收经加压的电解质和/或在电解器1102b内形成合适的电解质的前体流体。作为所示一个或多个电极例如1002b、1004b、1006b、1008b等或1104b上的微生物和/或保持的酶以及施加在所示塞1106b和1124b之间的电压的作用的结果，产生经加压的氢。高压氢经由压力调节器1120b通过导管1122b被递送到合适的应用。9B, there is shown a system 1100b that includes a high pressure electrolyzer 1102b that can receive pressurized electrolyte from a suitable pump 1114b and/or prior to forming a suitable electrolyte within the electrolyzer 1102b. body fluid. As a result of the action of microorganisms and/or retained enzymes on one or more electrodes shown, e.g. of hydrogen. High pressure hydrogen is delivered to a suitable application via pressure regulator 1120b through conduit 1122b.

含二氧化碳的加压电解质流经液压马达-发电机1126b，通过利用流动的电解质的动能和随着二氧化碳被递送到合适的二氧化碳用途如液体培养系统或温室1130b以生长藻类、柳枝稷、野葛或各种其他作物1132b和/或1134b时二氧化碳向环境压力的膨胀而产生功。已被耗尽二氧化碳的电解质由泵1114b经由三通阀1112b再循环。The pressurized electrolyte containing carbon dioxide flows through the hydraulic motor-generator 1126b to grow algae, switchgrass, kudzu or various The expansion of carbon dioxide to ambient pressure while growing other crops 1132b and/or 1134b produces work. Electrolyte that has been depleted of carbon dioxide is recirculated by pump 1114b via three-way valve 1112b.

生物质，包括1130b中生长的材料，被磨细或以其他方式制成活性物质的浆料，所述浆料由破碎的细胞材料组成，这些破碎的细胞材料是在处理器1136b中通过合适的机械、声、化学、热或辐射处理而产生。这样的活性有机原料被加到积贮器1108b，适宜地经过过滤器1110b并经过三通阀1112b，到达泵1114b，以进入压力电解器1102b，如图所示。Biomass, including grown material in 1130b, is ground or otherwise made into a slurry of active matter consisting of disrupted cellular material that is passed through suitable resulting from mechanical, acoustic, chemical, thermal or radiation treatments. Such active organic feedstock is fed to accumulator 1108b, suitably through filter 1110b and through three-way valve 1112b, to pump 1114b to enter pressure electrolyzer 1102b, as shown.

系统1100b的运行由控制器1101b响应压力、温度和pH传感器1142b、1144b、1146b以及化学活性剂传感器1140b和1150b而提供，如图所示。这使得补偿物质能够通过端口1118b加入以提供保持的酶发挥最佳性能所需的条件。Operation of system 1100b is provided by controller 1101b in response to pressure, temperature and pH sensors 1142b, 1144b, 1146b and chemically active agent sensors 1140b and 1150b, as shown. This allows compensating substances to be added through port 1118b to provide the conditions required for optimal performance of the retained enzyme.

在另一实施方案中，合适的电极包括自圆形或其他横截面如正方形或矩形或各种“星”形状的金属丝或扁平条带形成的系统以提供塑性地形成的织造实施方案或如本文中所公开的螺旋形实施方案。然后将选择的材料如铁或其他基于过渡金属的合金热处理至渗碳而在固体溶液中产生各种量的碳，所述固体溶液包含饱和区，这些饱和区由附加的热处理进一步限定或生长以使得这样的饱和区的生长特别靠近表面。随着供碳体如烃或一氧化碳在这样的表面上分解，产生的碳区将加速另外的碳的沉积。方程式10和11示出了向经热处理的基材提供量等于或大于供碳体的生成热的热的这类总过程：In another embodiment, suitable electrodes include systems formed from wires or flat strips of circular or other cross-sections such as square or rectangular or various "star" shapes to provide plastically formed woven embodiments or such as Spiral embodiments disclosed herein. Selected materials such as iron or other transition metal based alloys are then heat treated to carburize to produce various amounts of carbon in a solid solution containing saturated regions that are further defined or grown by additional heat treatment to The growth of such saturation regions is made particularly close to the surface. As carbon donors such as hydrocarbons or carbon monoxide decompose on such surfaces, the resulting carbon zones will accelerate the deposition of additional carbon. Equations 10 and 11 show such an overall process of providing heat to the heat-treated substrate in an amount equal to or greater than that of the carbon donor:

CxHy+热àxC+0.5yH2         方程式10CxHy+heat àxC+0.5yH2 Equation 10

CO+热àC+0.5O2             方程式11CO + heat à C + 0.5O2 Equation 11

在一些方面，希望继续碳沉积以产生以足够的深度(在初始饱和区结合)有效覆盖整个电极的碳膜，以产生具有所需形状和表面/体积比的非常耐用的复合材料。In some aspects, it is desirable to continue the carbon deposition to produce a carbon film that effectively covers the entire electrode at sufficient depth (incorporated in the initial saturation region) to produce a very durable composite material with the desired shape and surface/volume ratio.

在另一实施方案中，接近饱和条件的富碳区的初始制备和取向通过热或冷加工实施方案以提供碳结晶结构充分一致的取向来改变，从而提供显著外延地影响的相继碳沉积的沉积物。如此沉积的取向的碳例如主要暴露边缘的或呈与初始表面更平行的石墨烯层的被竞争性地受试以提供所需微生物过程的支持。这可实现针对各种类型的所需微生物过程选择“设计碳”。In another embodiment, the initial preparation and orientation of the carbon-rich region near saturation conditions is altered by thermal or cold processing of the embodiment to provide a sufficiently consistent orientation of the carbon crystalline structure to provide a significantly epitaxially affected deposit of successive carbon deposition . Oriented carbon so deposited, for example with predominantly exposed edges or with graphene layers more parallel to the original surface, was competitively tested to provide support for the desired microbial process. This enables selection of "designer carbons" for various types of desired microbial processes.

参见图10B，在另一方面，公开了供用于本文中所公开的实施方案中的碳/钢电极的制造。这些电极可包括经表面处理的碳以粘附于选择性酶、微生物或其他促进剂以改善电解器的运行。为制造根据该实施方案的电极，使钢或钢合金基材被碳所饱和。饱和的碳的晶粒通过例如感应热处理排列，以为碳提供所需的晶粒取向，如阶段I中所示。也可采用其他已知的热处理方法。在此步骤过程中，也可让电极经受液体冷却以防止电极损坏或提供其他好处。Referring to FIG. 10B , in another aspect, the fabrication of carbon/steel electrodes for use in embodiments disclosed herein is disclosed. These electrodes may include surface treated carbon to adhere to selective enzymes, microorganisms or other promoters to improve electrolyzer operation. To manufacture an electrode according to this embodiment, a steel or steel alloy substrate is saturated with carbon. The grains of saturated carbon are aligned by, for example, induction heat treatment to provide the carbon with the desired grain orientation, as shown in Stage I. Other known heat treatment methods may also be used. During this step, the electrodes may also be subjected to liquid cooling to prevent damage to the electrodes or to provide other benefits.

如阶段II中所示，然后通过已知的过程包括夹紧辊压而成形电极。成形可以如所需的进一步排列、平整或改变取向的碳晶粒的方式实施。As shown in Stage II, the electrodes are then shaped by known processes including pinch rolling. Shaping can be carried out in such a way as to further align, planarize or change the orientation of the carbon grains as desired.

如阶段III中所示，碳然后通过已知的碳沉积技术沉积在电极上，沉积技术包括气相沉积，通过这，碳将在电极的表面上沉积或生长。在此步骤过程中，碳可以进一步增强晶粒取向的方式沉积或者在电极上的选定位置处选择性地沉积碳，这取决于电极的所需用途。例如，可以在一个位置处沉积一种酶、微生物或促进剂，而另一种酶、微生物或促进剂可以被沉积在另一位置处，以实现酶、微生物和促进剂的受控使用。此外，具有沉积的碳的电极可通过感应加热或其他措施进一步处理以进一步排列或取向晶粒，这同样可以包括液体冷却。此过程可反复直至获得所需的碳量和/或晶粒取向和/或晶粒位置。As shown in stage III, carbon is then deposited on the electrodes by known carbon deposition techniques, including vapor deposition, by which carbon will be deposited or grown on the surface of the electrodes. During this step, carbon can be deposited in a manner that further enhances the grain orientation or can be selectively deposited at selected locations on the electrode, depending on the desired use of the electrode. For example, one enzyme, microorganism or promoter can be deposited at one location while another enzyme, microorganism or promoter can be deposited at another location to enable controlled use of the enzyme, microorganism and promoter. In addition, electrodes with deposited carbon can be further processed by induction heating or other measures to further align or orient the grains, which can also include liquid cooling. This process can be repeated until the desired amount of carbon and/or grain orientation and/or grain location is obtained.

如阶段IV中所示，在完成表面处理后，然后使电极暴露于一种或多种针对电极的特定应用而选择的酶、微生物或促进剂，例如提高电解过程中所需化合物如氢的产量的酶。在任何上述步骤中，所述方法可靶向电极的特定位置。此外，可以对不同的位置施加不同的处理条件，使得可以采用不同的酶或者可以在不同的位置处实施不同的酶密度，这取决于电极的所需构造或用途。这样，制造出的电极包括对特定酶、微生物或促进剂具有亲和性的碳结构并将所述酶、微生物或促进剂结合到电极上所需位置处以永久地或基本上保持所述酶于所需位置以供在电解或其他电极运行过程中使用。After completing the surface treatment, as shown in Phase IV, the electrode is then exposed to one or more enzymes, microorganisms, or accelerators selected for the specific application of the electrode, such as enhancing the production of desired compounds such as hydrogen during electrolysis enzymes. In any of the above steps, the method can target a specific location of the electrode. Furthermore, different treatment conditions can be applied to different locations, so that different enzymes can be employed or different enzyme densities can be implemented at different locations, depending on the desired configuration or use of the electrode. In this way, the fabricated electrode includes a carbon structure that has an affinity for a specific enzyme, microorganism or promoter and binds the enzyme, microorganism or promoter to the electrode at a desired location to permanently or substantially maintain the enzyme in the Required position for use during electrolysis or other electrode operation.

虽然结合特定的实施方案和实施例描述了本发明，但本领域技术人员易于理解，本发明可以有改变和修改而不偏离本发明的精神和范围。因此，本发明的范围仅由附随的权利要求书限定。Although the invention has been described with reference to specific embodiments and examples, it will be readily understood by those skilled in the art that changes and modifications can be made without departing from the spirit and scope of the invention. Accordingly, the scope of the invention is limited only by the appended claims.

Claims (43)

Translated fromChinese

1.一种用于提供材料资源的可再生源的方法，所述方法包括：1. A method for providing a renewable source of material resources, the method comprising:提供可再生能的第一源；Provide the first source of renewable energy;提供来自第一材料源的第一材料流；providing a first stream of material from a first source of material;提供与所述第一材料流和所述可再生能的第一源相连的电解器，其中所述电解器自所述第一材料流通过电解产生材料资源；providing an electrolyzer connected to the first material stream and the first source of renewable energy, wherein the electrolyzer produces a material resource from the first material stream by electrolysis;向第一处理器提供所述材料资源以进一步处理或使用。The material resource is provided to the first processor for further processing or use.2.根据权利要求1所述的方法，其中所述材料资源包含氢。2. The method of claim 1, wherein the material resource comprises hydrogen.3.根据权利要求1所述的方法，其中所述材料资源包含基于碳的材料。3. The method of claim 1, wherein the material resource comprises a carbon-based material.4.根据权利要求1所述的方法，其中所述材料资源包含烃。4. The method of claim 1, wherein the material resource comprises hydrocarbons.5.根据权利要求1所述的方法，其中所述材料资源包含基于氮的材料。5. The method of claim 1, wherein the material resource comprises a nitrogen-based material.6.根据权利要求1所述的方法，其中所述第一材料源包括有机材料。6. The method of claim 1, wherein the first material source comprises an organic material.7.根据权利要求1所述的方法，所述方法还包括通过对来自所述第一处理器的所述材料资源加热而进一步处理所述材料资源的步骤。7. The method of claim 1, further comprising the step of further processing the material resource from the first processor by heating the material resource.8.根据权利要求7所述的方法，其中所述第一处理器包括太阳能收集器。8. The method of claim 7, wherein the first processor comprises a solar collector.9.根据权利要求8所述的方法，其中所述太阳能收集器与所述电解器相连。9. The method of claim 8, wherein the solar collector is connected to the electrolyzer.10.根据权利要求9所述的方法，其中所述太阳能收集器包括太阳光集中镜。10. The method of claim 9, wherein the solar collector comprises a solar concentrating mirror.11.根据权利要求10所述的方法，其中所述太阳光集中镜包括抛物面镜、球面镜或定日反射镜阵列。11. The method of claim 10, wherein the solar concentrating mirror comprises a parabolic mirror, a spherical mirror, or an array of heliostats.12.根据权利要求8所述的方法，所述方法还包括第一补充热源以补充或替代来自所述太阳能收集器的热。12. The method of claim 8, further comprising a first supplemental heat source to supplement or replace heat from the solar collector.13.根据权利要求11所述的方法，其中所述材料资源包含甲烷，所述进一步处理所述材料资源的步骤包括解离所述甲烷以产生碳和氢。13. The method of claim 11, wherein the material resource comprises methane, the step of further processing the material resource comprising dissociating the methane to produce carbon and hydrogen.14.根据权利要求4所述的方法，其中向所述处理器提供所述第一材料资源以进一步处理或使用的步骤包括将所述烃转化为氢和碳。14. The method of claim 4, wherein the step of providing the first material resource to the processor for further processing or use includes converting the hydrocarbon to hydrogen and carbon.15.根据权利要求14所述的方法，其中所述材料资源还包含二氧化碳。15. The method of claim 14, wherein the material resource further comprises carbon dioxide.16.根据权利要求14所述的方法，所述方法还包括将所述氢转化为能量的步骤。16. The method of claim 14, further comprising the step of converting the hydrogen into energy.17.根据权利要求14所述的方法，其中所述电解器被构造为可以可选择地逆转运行而作为燃料电池，且所述将所述氢转化为能量的步骤包括所述电解器作为燃料电池的运行。17. The method of claim 14, wherein the electrolyzer is configured to operate selectively reversibly as a fuel cell, and the step of converting the hydrogen to energy comprises the electrolyzer as a fuel cell running.18.根据权利要求14所述的方法，所述方法还包括将所述碳转化为一种或多种耐用品的步骤。18. The method of claim 14, further comprising the step of converting the carbon into one or more durable goods.19.根据权利要求18所述的方法，其中所述一种或多种耐用品包括供用于提供所述可再生能的第一源的步骤中的一种或多种耐用品。19. The method of claim 18, wherein the one or more durable goods comprise one or more durable goods for use in the step of providing the first source of renewable energy.20.根据权利要求15所述的方法，所述方法还包括提供所述二氧化碳用于农业用途的步骤。20. The method of claim 15, further comprising the step of providing said carbon dioxide for agricultural use.21.根据权利要求1所述的方法，其中所述第一材料源包括生物质。21. The method of claim 1, wherein the first material source comprises biomass.22.根据权利要求1所述的方法，其中所述第一材料源包括生物废弃物。22. The method of claim 1, wherein the first material source comprises biological waste.23.一种用于提供材料资源的可再生源的系统，所述系统包括：23. A system for providing a renewable source of material resources, the system comprising:可再生能的第一源；primary source of renewable energy;来自第一材料源的第一材料流；a first material stream from a first material source;电解器，所述电解器与所述可再生能的第一源和所述第一材料流相连，其中所述电解器被构造为通过电解产生第一材料资源；an electrolyzer coupled to the first source of renewable energy and the first material stream, wherein the electrolyzer is configured to produce a first material resource by electrolysis;处理器，用于进一步处理或使用所述材料资源以产生第二材料资源，其中所述处理器包括太阳能收集器且其中所述太阳能收集器被构造为向所述第一材料资源提供热以便解离；和a processor for further processing or using the material resource to produce a second material resource, wherein the processor includes a solar collector and wherein the solar collector is configured to provide heat to the first material resource for decomposing from; and材料资源储存器，所述材料资源储存器与所述电解器相连以自所述电解器接收所述材料资源或向所述处理器提供所述材料资源以进一步处理或使用。A material resource storage coupled to the electrolyzer for receiving the material resource from the electrolyzer or providing the material resource to the processor for further processing or use.24.根据权利要求23所述的系统，其中所述材料资源包含基于碳的材料。24. The system of claim 23, wherein the material resource comprises a carbon-based material.25.根据权利要求23所述的系统，其中所述材料资源包含烃。25. The system of claim 23, wherein the material resource comprises hydrocarbons.26.根据权利要求23所述的系统，其中所述材料资源包含基于氮的材料。26. The system of claim 23, wherein the material resource comprises a nitrogen-based material.27.根据权利要求23所述的系统，其中所述材料资源包含氨。27. The system of claim 23, wherein the material resource comprises ammonia.28.根据权利要求25所述的系统，其中所述处理器被构造为将所述烃转化为氢和碳。28. The system of claim 25, wherein the processor is configured to convert the hydrocarbons to hydrogen and carbon.29.根据权利要求28所述的系统，所述系统还包括用于分配氢以用于第一位置处的分配系统。29. The system of claim 28, further comprising a dispensing system for distributing hydrogen for use at the first location.30.根据权利要求23所述的系统，所述系统还包括用于分配所述材料资源以进一步使用的材料资源分配系统。30. The system of claim 23, further comprising a material resource allocation system for allocating the material resource for further use.31.根据权利要求30所述的系统，其中所述材料资源分配系统与所述可再生能的第一源、所述第一材料源、所述处理器或所述电解器中的一个或多个相连。31. The system of claim 30, wherein the material resource allocation system is integrated with one or more of the first source of renewable energy, the first material source, the processor, or the electrolyzer connected.32.根据权利要求23所述的系统，其中所述太阳能收集器与所述电解器相连。32. The system of claim 23, wherein the solar collector is connected to the electrolyzer.33.根据权利要求32所述的系统，其中所述太阳能收集器包括太阳光集中镜。33. The system of claim 32, wherein the solar collector comprises a solar concentrating mirror.34.根据权利要求33所述的系统，其中所述太阳光集中镜包括抛物面镜、球面镜或定日反射镜阵列。34. The system of claim 33, wherein the solar concentrating mirrors comprise parabolic mirrors, spherical mirrors, or heliostat mirror arrays.35.根据权利要求32所述的系统，所述系统还包括被构造以补充或替代来自所述太阳能收集器的热的第一补充热源。35. The system of claim 32, further comprising a first supplemental heat source configured to supplement or replace heat from the solar collector.36.根据权利要求23所述的系统，其中所述材料资源包含甲烷，所述处理器被构造为解离所述甲烷以产生碳和氢。36. The system of claim 23, wherein the material resource comprises methane, the processor configured to dissociate the methane to produce carbon and hydrogen.37.一种用于提供材料资源的可再生源的系统，所述系统包括：37. A system for providing a renewable source of material resources, the system comprising:可再生能的第一源；primary source of renewable energy;来自第一材料源的第一材料流；a first material stream from a first material source;电解器，所述电解器与所述可再生能的第一源和所述第一材料流相连，其中所述电解器被构造为通过电解产生第一材料资源；an electrolyzer coupled to the first source of renewable energy and the first material stream, wherein the electrolyzer is configured to produce a first material resource by electrolysis;处理器，所述处理器用于进一步处理或使用所述材料资源以产生第二材料资源，其中所述处理器包括太阳能收集器且其中所述太阳能收集器被构造为向所述第一材料资源提供热以便解离；和a processor for further processing or using the material resource to produce a second material resource, wherein the processor includes a solar collector and wherein the solar collector is configured to provide heat for dissociation; and材料资源储存器，所述材料资源储存器与所述电解器相连以自所述电解器接收所述材料资源或向所述处理器提供所述材料资源以进一步处理或使用。A material resource storage coupled to the electrolyzer for receiving the material resource from the electrolyzer or providing the material resource to the processor for further processing or use.38.根据权利要求37所述的系统，其中所述太阳能收集器被构造为通过向所述第一材料资源加热来处理所述第一材料资源。38. The system of claim 37, wherein the solar collector is configured to process the first material resource by applying heat to the first material resource.39.根据权利要求38所述的系统，其中所述太阳能收集器与所述电解器相连。39. The system of claim 38, wherein the solar collector is connected to the electrolyzer.40.根据权利要求39所述的系统，其中所述太阳能收集器包括太阳光集中镜。40. The system of claim 39, wherein the solar collector comprises a solar concentrating mirror.41.根据权利要求40的系统，其中所述太阳光集中镜包括抛物面镜、球面镜或定日反射镜阵列。41. The system of claim 40, wherein said solar concentrating mirrors comprise parabolic mirrors, spherical mirrors, or heliostat mirror arrays.42.根据权利要求37所述的系统，所述系统还包括被构造以补充或替代来自所述太阳能收集器的热的第一补充热源。42. The system of claim 37, further comprising a first supplemental heat source configured to supplement or replace heat from the solar collector.43.根据权利要求41所述的系统，其中所述材料资源包含甲烷，所述处理器被构造为解离所述甲烷以产生碳和氢。43. The system of claim 41, wherein the material resource comprises methane, the processor configured to dissociate the methane to produce carbon and hydrogen.