Classifications

• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
  • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
  • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
  • C25B1/00—Electrolytic production of inorganic compounds or non-metals
  • C25B1/01—Products
  • C25B1/02—Hydrogen or oxygen
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0913—Carbonaceous raw material
  • C10J2300/0916—Biomass
  • C10J2300/092—Wood, cellulose
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0913—Carbonaceous raw material
  • C10J2300/093—Coal
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0913—Carbonaceous raw material
  • C10J2300/0943—Coke
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0983—Additives
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0983—Additives
  • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
  • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
  • C10J2300/1656—Conversion of synthesis gas to chemicals
  • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/50—Fuel cells

Definitions

• the field of the invention is oxidation of carbonaceous feedstocks, especially as it relates to chemical oxidation of cellulosic materials to prepare yeast fermentable materials for ethanol production.
• Electrochemical oxidation processes using iron ions as redox carrier can also be used to generate a variety of organic products.
• coal and/or petroleum coke can be partially oxidized to humic acid at temperatures of 150 0 C, or completely oxidized to carbon dioxide at temperatures in excess of 300 0 C (e.g., Electrochemical Hydrogen Technologies, Clarke and Foller p.345-371; Elsevier 1990).
• oxidation of carbonaceous fuels using an iron redox carrier is impacted by both the temperature of the electrolyte and the concentration of the ferric ions.
• Unfortunately while the temperature can be raised, solubility problems will remain even at high temperatures.
• higher temperatures often thermally destroy such products.
• the present invention is directed to compositions and methods of oxidizing various organic materials, and especially carbonaceous feedstock using highly concentrated metal ion solutions.
• the metal ion is a transition metal ion, and high concentrations of the metal are achieved by an additive that is stable under conditions at which the metal ion is regenerated after oxidation of the feedstock.
• a method of oxidizing a carbonaceous feedstock includes a step of combining a metal and a solubility-enhancing compound to form a metal-containing solution.
• the solubility-enhancing compound is present at a concentration and has a composition effective to increase solubility of the metal over solubility of the same metal in sulfuric acid in an amount of at least 10%, and wherein the solubility- enhancing compound has a composition effective to resist oxidation under conditions at which the metal is electrochemically oxidized from a reduced form.
• the carbonaceous feedstock is combined with the metal-containing solution to thereby at least partially oxidize the feedstock and form the reduced form of the metal, and optionally, the metal is electro chemically regenerated from the reduced form of the metal, wherein the step of regenerating is carried out under conditions effective to produce hydrogen.
• the hydrogen and/or the oxidized feedstock are then used as an energy carrier in a subsequent reaction.
• the carbonaceous feedstock is a cellulosic material, lignocellulosic material, paper, cotton, plant materials, coal, tar, and/or coke
• the metal is a transition metal ion (preferably a period 4 transition metal ion, and particularly an iron ion, a copper ion, and/or a manganese ion).
• the compound is an acid, and especially an organic acid comprising a sulfur atom (but not sulfuric acid).
• the solubility-enhancing compound is an optionally substituted alkyl sulfonic acid or an optionally substituted alkyl sulfamic acid, and present at a concentration effective to increase solubility of the metal over solubility of the same metal in sulfuric acid in an amount of at least 50%, and more typically at least 100%. While contemplated reactions can be carried out at various temperatures, it is preferred that the step of at least partially oxidizing the feedstock is performed at a temperature between 20 °C and 50 0 C, and more typically between 50 0 C and 300 0 C.
• Regeneration of the metal is preferably carried out via electrochemical oxidation of the reduced metal, preferably under conditions such that hydrogen is produced in only one side of the cell without or at reduced oxygen production (e.g., at least 10%, more typically at least 30%, and most typically at least 50% less as compared to same setup but without metal in electrolyte) in another side of the cell.
• reduced oxygen production e.g., at least 10%, more typically at least 30%, and most typically at least 50% less as compared to same setup but without metal in electrolyte
• a liquid intermediate in the oxidation of a carbonaceous feedstock comprises an organic acid other than sulfuric acid, a transition metal ion, and a carbonaceous feedstock selected from the group consisting of an oligosaccharide, a polysaccharide, coal, tar, and coke.
• the organic acid includes an optionally substituted alkyl sulfonic acid or an optionally substituted alkyl sulfamic acid, optionally further comprising a complexing agent, and/or the transition metal ion is selected from the group consisting of an iron ion, a copper ion, and a manganese ion.
• the inventors have discovered that electrochemical oxidation of organic matter in aqueous media using ionic species of metals, and especially iron ions as redox agents can be dramatically improved by using in the electrolyte an acid or corresponding salt of the acid that increases solubility of the metal ion. Additionally, or alternatively, a complexing agent may be added that increases solubility of the metal ion.
• the metal ion is an iron ion (e.g., ferric iron [Fe +3 ] and/or ferrous iron [Fe +2 ]).
• the metal ion is a ferric and/or ferrous iron
• the electrolyte is a 1.5M aqueous ferrous methane sulfonate solution that is electrochemically oxidized in a standard divided cell (e.g., withNAFIONTM [sulfonated tetrafluorethylene copolymer] separator) on a platinum coated titanium electrode to generate a ferric methane sulfonate solution.
• a standard divided cell e.g., withNAFIONTM [sulfonated tetrafluorethylene copolymer] separator
• Carbonaceous feedstock is then combined with the ferric methane sulfonate solution and reacted at a desired temperature for a time appropriate to generate the desired product or to exhaust the ferric iron. While the nature of the feedstock is generally not limiting to the inventive subject matter, it is typically preferred that where hydrogen and/or carbon dioxide is the desired product, coal, coke, tar, and/or other high-carbon content materials are used as a feedstock, while in applications where fermentable carbohydrates are the desired products, suitable feedstocks include various processed (e.g., cotton, paper, pulp, etc.) or unprocessed (e.g., plant fibers, leafs, etc.) cellulosic materials.
• processed e.g., cotton, paper, pulp, etc.
• unprocessed e.g., plant fibers, leafs, etc.
• High-carbon content materials typically include those in which at least 25 wt%, and more typically at least 30 wt% of the materials are carbon (in elemental form and/or bonded to other atoms).
• suitable high-carbon content materials include oligo- and polysaccharides, which may be linear, branched, and/or chemically modified, Hgnin and Hgnaceous materials, combustion and/or pyrolysis products, coke, tar, coal, hydrocarbons, etc.
• the reaction temperature may be elevated (e.g., between 30-300 0 C, more typically between 50-150 0 C, and most typically between 60-90 0 C) for at least part of the reaction time.
• preferred reaction times will typically be chosen such that the ferric iron concentration will remain above 0.2-0.3M, more preferably above 0.3-0.5M, and most preferably above 0.5-0.7M.
• the processing time may be less critical and the reaction can be driven to exhaustion of the ferric iron and/or the oxidizable material.
• the ratio of the ferric iron to oxidizable material may vary considerably.
• the ferric iron may be in molar excess over the oxidizable material (e.g. , up to 2-fold molar excess, more typically up to 5-fold molar excess, even more typically up to 10-fold molar excess, and in some instances up to 20-fold molar excess and even higher).
• the oxidizable material may be in molar excess over the ferric iron (e.g., up to 2-fold molar excess, more typically up to 5-fold molar excess, even more typically up to 10- fold molar excess, and in some instances up to 20-fold molar excess and even higher).
• suitable compounds include various alkylsulfonic acids (e.g., ethane sulfonic acid) and/or an alkylsulfamic acids (e.g., methylsulfamic acid), which may entirely replace sulfuric acid of previously known systems.
• alkylsulfonic acids e.g., ethane sulfonic acid
• alkylsulfamic acids e.g., methylsulfamic acid
• sulfuric acid and/or other organic or inorganic acids e.g., hydrochloric acid, phosphoric acid, nitric acid, etc.
• suitable compounds increase solubility of the metal ions over solubility of the same metal ions in sulfuric acid in an amount of at least 10%, more typically at least 25%, even more typically at least 50%, and most typically at least 100% absolute.
• contemplated compounds will be include (typically substituted) organic or inorganic acids, but may also include polymeric materials (soluble or insoluble) with cationic and/or anionic groups (which may be part of the polymer backbone or be pendant groups).
• suitable compounds also include bases and neutral compositions.
• oxidation resistance of suitable compounds the person of ordinary skill in the art is well equipped to recognize appropriate alternative acids. It is generally preferred that the compounds will resist oxidation under conditions at which the metal ion is electro chemically (or chemically) oxidized from the reduced form. Thus, in most preferred aspects, at least 85 mol%, more typically at least 95 mol%, and most typically at least 98 mol% of contemplated compounds will remain chemically unchanged in the electrolyte after 10 cycles of re-oxidation. Furthermore, suitable compounds will be heat stable at temperatures of between 10-150 0 C (and even higher), more typically between 20-100 0 C, and most typically between 30-90 0 C. Therefore, and among other choices, suitable compounds may also be fluorinated (e.g., fluorinated methylsulfonic and/or fluorinated methylsulfamic acid).
• fluorinated e.g., fluorinated methylsulfonic and/or fluorinated methylsulfamic acid
• contemplated compounds are present in the aqueous electrolyte at a concentration of at least 5-10 wt%, more typically at least 20 wt%, even more typically at least 40 wt%, and most typically at saturation.
• the compound will be present in concentrations between about 0.1 M to 0.5 M, more typically 0.5 M to 1.0 M, even more typically between 1.0 M and 1.5 M, and most typically above 1.5-2.0 M.
• the solubility of the metal ion ⁇ e.g., ferrous and ferric iron) in the electrolyte at 25 0 C may be between 0.2 M and 0.5 M, more preferably between 0.5 M and 1.0 M, even more preferably between 1.0 M and 2.0 M, and most preferably above 2.0 M. Consequently, it should be recognized that the electrolyte will have an acid pH of between pH 0 and pH 6.7, and more typically between pH 2.0 and pH 6.0.
• suitable complexing agents include various oligodentate compounds, crown ethers, exchange resins, etc.
• suitable complexing agents include desferoxamine and desferoxamine analogs, bacterial or synthetic siderophores, humates (including in situ electrochemically generated humates), EDTA (ethylenediaminetetraacetic acid), EDMA (ethylenediiminobis (2-hydroxy-4-methyl- phenyl) acetic acid), and DTPA (diethylenetriamine-pentaacetic acid).
• the complexing agents may be present at a concentration of between, about 0.1 M to 1.0 M, and more preferably between 1.0 M to 2.0 M (and higher). Most preferably, one or more complexing agents are combined with contemplated compounds ⁇ e.g., with methane sulfonic acid), but they may also be used separately.
• the metal ion is an iron ion, and especially ferric iron in the oxidized state and ferrous iron in the reduced state.
• various alternative metals and/or oxidation states are also deemed suitable, and especially contemplated metals and metal ions include transition metals, lanthanides (and particularly cerium);, and metals of the fourth (e.g., titanium, chromium, copper, etc.) and fifth (e.g., molybdenum, indium, tin, etc.) period.
• the ionic charge may therefore be between +1 and +7, and more typically between +1 and +4 (or the metal may be elemental in one state).
• the metal is in a complex (e.g., with an organic ligand or inorganic component), ionic charges may also be between -1 and typically -4. Still further, it should be recognized that mixtures of various metals may also be appropriate.
• the reaction rate between the ferric ions and the carbon fuel increased with higher temperatures, which is particularly advantageous as iron sulfates reach their maximum solubility at 80 0 C.
• methane sulfonic acid not only considerably increased solubility of ferrous and ferric iron, but also enhanced the reaction by the compatibility of methane sulfonic acid with the carbon and carbon oxidized surface, possibly via a detergent-like effect.
• the (preferably metal-mediated) oxidation can be carried out in a reactor that is separate from the electrochemical cell in which the electrolyte is regenerated, or that the oxidation of the feedstock and the regeneration can be carried out in the same reactor.
• (preferably metal-mediated) oxidation of the feedstock and regeneration of the electrolyte may be carried out at the same time.
• the configurations and methods according to the inventive subject matter were substantially inert to sulfur in the coal and did not impact the purity of carbon dioxide that issued from the reactor as sulfur compounds were oxidized to sulfuric acid that remained in the electrolyte.
• the carbon dioxide was also free of oxides of nitrogen as all nitrogen compounds were oxidized to nitrates.
• hydrogen produced in such electrolytic cells was free of oxygen as the catholyte was separated from the anolyte by an ion exchange membrane.
• contemplated systems and methods will not only generate partially oxidized feedstock but also produce hydrogen.
• Such products can be used (alone or in combination) as an energy carrier in downstream reactions.
• the at least partially oxidized feedstock can be employed in a fermentation reaction as nutrient for the fermenting microorganism.
• hydrogen may be employed as a direct fuel in a hydrogen fuel cell for energy production, or as an indirect fuel in which hydrogen is a component for fuel production (e.g., via Fischer-Tropsch reaction of CO and H2 produced in such systems [CO can be produced from CO2 in a reverse shift reaction]), wherein that fuel then provides energy.
• energy carrier refers to compounds that are either used as a fuel in combustion or feed component in a fermentation and/or used as precursor(s) in the synthesis of a hydrocarbon fuel (and especially methane). Consequently, subsequent reactions may be catalyzed or uncatalyzed in a reactor, or performed in an in vitro or in vivo enzyme-containing system.
• wood flour, corn husk, and sewage sludge (mainly cellulose) could be completely solubilized at temperatures below 100 0 C. It was assumed that some of the organic material had been oxidized to carbon dioxide but some remained as organic materials like sugars. Therefore, it is now contemplated that with more concentrated iron redox carriers it is now possible at temperatures lower that 100 0 C to consider (preferably selective) oxidation of cellulose like materials to products that are more easily converted to benign or useful products. For example, cellulose can be converted to sugars that are then biologically converted to alcohol. The first part of such process is the breaking of the cellulose polymer into smaller molecules and then to individual sugars by hydrolysis with strong acids.
• ferric ions are used to convert aniline to polyaniline for example, one very. toxic the other relatively benign.
• suitable temperatures for oxidation reactions will be between 20 0 C and 50 0 C, more typically between 50 0 C and 80 0 C, even more typically between 80 0 C and 100 0 C, and in some cases between 50 0 C and 300 0 C.
• the organic materials can be broken down to smaller molecules (e.g., cellulose and lignins present in plant materials into polysaccharides and sugars) that may be converted to biofuels by subsequent biological processes, and especially fermentation (see below).
• cellulose and lignins present in plant materials into polysaccharides and sugars
• biofuels by subsequent biological processes, and especially fermentation (see below).
• the overall processing costs will significantly drop.
• the impact on the cost of generating hydrogen electrochemically at high current density is easily forecast from extrapolation from the results of Clarke and Foller.
• pure H2 and CO2 can be prepared at a substantially lower price than in conventional electrolysis processes.
• these products can be combined to make carbon monoxide and hydrogen (syngas), which is an ideally suitable feedstock for Fischer- Tropsch synthesis as the so produced gas mixture is free of interfering sulfur compounds and/or nitrogen oxides.
• a typical reaction is started with 50 kg of lignocellulosic material to obtain water soluble materials of about 40 kg.
• the typical fermentable sugar content is in the range of 70%, which translates to about 30 kg fermentable sugar. According to the below net equation for the fermentation process, 180 g of sugar will give 46 g of ethanol.
• the net energy ratio for the ethanol production will be better than 2: 1. That is, if 100 BTU's of energy is used for the overall process, 200 BTU's of energy is available in the fuel ethanol. This is a very rough estimate of the energy content in the process and we are confident that as processing technologies improve ethanol production will become lass and less energy intensive. It should be noted that the Fe-MSA used in the above process is not consumed and is 100% recyclable. The process has further advantages associated with of electrochemical processes, including lack of thermal energy loss, and simplicity of operation. With the anticipated development of new fermentation processes, the overall yield of the process should further significantly increase.
• com is the primary raw material for ethanol production, accounting for about 92% of the total feedstock in the ethanol industry.
• Most ethanol in the United States is produced by either a wet milling or a dry milling process and utilizes shelled corn as the principal feedstock.
• the corn based ethanol has a net energy value of about -5000 BTUs.
• As the production of ethanol from corn is a relatively mature technology, it is not likely that significant reductions in production costs will be achieved using conventional technology.
• Another major drawback of the corn-based ethanol technology is the potential environmental damage during the process. The environmental system in which corn is being produced is being rapidly degraded.
• Cellulosic ethanol is an alternative fuel made from a wide variety of nonfood plant materials (or feedstocks), including agricultural wastes such as corn stover and cereal straws, industrial plant waste like saw dust and paper pulp, and energy crops grown specifically for fuel production like switch grass.
• feedstocks nonfood plant materials
• the fuel can be produced in nearly every city of the country.
• the current status of corn price as the dominant cost factor, the development of low-cost feedstock is the key to further reduce the cost.
• lignocellulosic biomass is the earth's most attractive alternative among fuel sources and most sustainable energy resource and is reproduced by the bioconversion of carbon dioxide.
• the low cost of lignocellulosic materials makes them a promising feedstock for ethanol production.
• lignocellulosic materials often require a more complex refining process, cellulosic ethanol contains more net energy and results in lower greenhouse emissions than traditional corn-based ethanol.
• E85 an ethanol fuel blend that is 85% ethanol, is already available in more than 1,000 fueling stations nationwide and can power millions of flexible fuel vehicles already on the roads.
• the high cost of cellulose enzymes is the key barrier to economic production of cellulosic ethanol
• the unique aspect of the ethanol processes contemplated herein is the use of a redox system that can act in a manner similar to a surface active reagent and as an electron source at the same time. While not limiting to the inventive subject matter, it is thought that the hydrophobic part of the methane sulfonic acid facilitates the solubilizing of the rigid cellulose molecules while the Fe 3+ provides the energy to break down the organic material to fermentable sugars. Thus, use of costly and unstable enzymes is reduced, or even entirely avoided, and contemplated processes can be integrated in a simple manner into known yeast fermentation processes. Remarkably, the methods and processes contemplated herein also produce two desirable side products, lignin and hydrogen. The following table exemplarily illustrates some of the advantages of contemplated methods and configurations:
• the exemplary ethanol process contemplated herein includes five different stages: (1)
• the combination of a powerful oxidant and an organic sulfonic acid solution allows the conversion of nearly all organics, whether present in hazardous or in mixed waste. Moreover, insoluble transuranics are dissolved in this process and may be recovered by separation and precipitation.
• the oxidant, or metal mediator is preferably a multivalent transition metal ion, which is cleanly recycled in a number of charge transfer steps in an electrochemical cell. It should be noted that the mediated electrochemical oxidation technique offers several advantages: First, the oxidation/dissolution processes are accomplished at near ambient pressures and temperatures (30-90 0 C). Second, all waste stream components and oxidation products (with the exception of evolved gases) are contained in an aqueous environment.
• the electrolyte therefore acts as an accumulator for inorganics, which were present in the original waste stream, and the large volume of electrolyte provides a thermal buffer for the energy released during oxidation of the organics.
• the generation of secondary waste is minimal, as the process needs no additional reagents.
• the entire process can be shut down by simply turning off the power, affording a level of control unavailable in many other techniques.
• Iron powder is dissolved in commercially available 70% methane sulfonic acid.
• the ferrous ion solution is diluted with water to produce 1.5 molar ferrous methane sulfonate in excess methane sulfonic acid.
• the solution is treated in a divided electrochemical cell fitted with an indium oxide or platinum coated titanium electrode. Current is applied until the ferrous iron is converted to ferric ion.
• Wood flour is added to form a suspension.
• the mixture is heated to SO 0 C and stirred for one hour or until all the iron is converted to the ferrous state.
• the mixture is filtered to remove any unreacted wood flour.
• the solution is then treated by liquid/liquid extraction to remove organic materials formed, and regenerated in the electrochemical cell to form ferric ion for treatment with more wood flour.
• powdered coal (100 mesh) is treated in a reactor with ferric methane sulfonic acid in excess methane sulfonic acid at 180 0 C.
• the solution after reaction is fed to the anode compartment of an electrochemical cell.
• the cell has an ion exchange membrane made from NAFIONTM.
• the cathode is made from stainless titanium, the anode is iridium oxide coated titanium.
• the product from the cathode is hydrogen and the anodic products are oxidized coal, carbon dioxide, and a small amount of sulfuric acid.
• Oxidized coal can be further oxidized by repeated cycling of the process, or the solution is mixed with further quantities of coal to top up the available fuel. At even higher temperatures (e.g., 300 0 C and higher) complete oxidation of the coal to carbon dioxide is possible.
• feedstocks include switchgrass, lignocellulosic materials, paper products, cotton products, agricultural waste products, and other plant-derived polysaccharides that are ordinarily not fermentable by microorganisms. Suitable feedstocks are described in EP 0091221 and WO 02/12529, which are incorporated by reference herein.
• additional and/or alternative oxidating species may be employed, and particularly suitable alternative oxidizing species include aluminum ions and manganese ions in various oxidation states.
• the hydrogen evolved in such systems can be used as fuel component to regenerate the oxidizing species (e.g., using electrochemical regeneration of Fe +3 from Fe +2 in a hydrogen powered fuel cell). Therefore, it should be particularly noted that the partial oxidation of the feedstock will not only provide fermentable materials for ethanol production, but also reduce overall energy consumption by energetic coupling of the hydrogen byproduct with the regeneration of the oxidant. Moreover, as the MSA significantly increases solubility of the oxidant and, reaction time and temperature can be further reduced. Additional configurations, contemplations and details suitable for use herein are described in U.S. Pat. No. 3,939,286, which is incorporated by reference herein.

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