Field of the Invention

The present invention relates to electrochemical processing generally and, more particularly, to a method and/or apparatus for implementing a heterocycle catalyzed electrochemical process . Background of the Invention

Alcohols and organic chemicals with hydroxyl and carbonyl functional groups are important to industrial processes and the production of light alcohol fuels. At present, several different processes are used for production of alcohols. Most alcohols are produced from oil or natural gas, while some including ethanol and pentanol are produced biologically. Hydroxyl groups are often introduced to organic molecules via catalytic hydrogenation of aldehydes or acid catalyzed hydration of alkenes. Some specific examples include methanol, which is produced by catalytic conversion of synthesis gas at high temperature and pressure. Ethanol is produced by acid catalyzed hydration of ethylene or by various microorganisms via fermentation of sugars.

Two major processes exist for propanol production. Acid catalyzed hydration of propylene is performed, resulting in a mixture of both isopropanol and n-propanol. Another process to make n-propanol is hydroformylation of ethylene to propionaldehyde followed by catalytic hydrogenation of propionaldehyde to n-propanol. N-butanol is produced in a manner similar to that of n-propanol. Propylene is converted to butyraldehyde via hydroformylation. The butyraldehyde is then catalytically hydrogenated to n-butanol. Sec-butanol is produced in a manner similar to ethanol, by the acid catalyzed hydration of 1-butene or 2-butene. Isomers of pentanol are primarily produced by the distillation of fusel oil. Fusel oil is a product of some biological fermentation processes. Hexanol and higher order alcohols are commonly produced by oligomerization of ethylene, which results in a mix of different products separated via distillation.

At present, many different techniques are currently used to create other organic products. Biological processes, such as fermentation of sugars, produce ethanol or fusel oil. The Fischer-Tropsch process is used for conversion of synthesis gases to organic molecules. Hyoroformylation of alkenes is followed by catalytic hydrogenation to alcohols or alkanes. Polymerization of alkenes results in organic products. Electrochemical hydrodimerization of alkenes, notably the Monsanto process, produces adiponitrile.

Existing electrochemical and photochemical processes/ systems have one or more of the following problems that prevent commercialization on a large scale. Selectively producing some alcohols, notably isopropanol, butanol, pentanol, and higher order alcohols is difficult. Selectively reducing carboxyl or carbonyl groups is also difficult without undesirable side reactions such as hydrogenation of aromatic molecules or heterocycles . Many existing processes, notably the Fischer-Tropsch process, make multiple products that are subsequently separated. Production of some aldehydes and alcohols use multi-step reactions that collectively have low energy efficiency. Likewise, hydrodimerization without a catalyst can be very inefficient. Existing reaction pathways use high heat, high temperature and/or highly acid environments. The heat conditions result in the use of expensive materials for the reactors. Many existing processes, both thermally and electrochemically driven, also use alkenes as a starting material. Summary of the Invention

The present invention concerns a method for heterocycle catalyzed electrochemical reduction of a carbonyl compound. The method generally includes steps (A) to (C) . Step (A) may introduce the carbonyl compound into a solution of an electrolyte and a heterocycle catalyst in a divided electrochemical cell. The divided electrochemical cell may include an anode in a first cell compartment and a cathode in a second cell compartment. The cathode generally reduces the carbonyl compound to at least one aldehyde compound. Step (B) may vary which of the aldehyde compounds is produced by adjusting one or more of (i) a cathode material, (ii) the electrolyte, (iii) the heterocycle catalyst, (iv) a pH level and (v) an electrical potential. Step (C) may separate the aldehyde compounds from the solution.

The objects, features and advantages of the present invention include providing a method and/or apparatus for implementing a heterocycle catalyzed electrochemical process that may (i) reduce carbonyl groups to aldehydes, (ii) reduce aldehydes to alcohols, (iii) reduce keto groups to hydroxyl groups, (iv) support heterocycle catalyzed electrochemical processing at a commercial level, (v) operate at atmospheric pressure, (vi) operate at ambient temperature, (vii) use water as a solvent, (viii) process at a mild pH( (ix) selectively electrohydrodimerize carbonyl-containing compounds to a variety of organic chemicals and/or (x) provide stable processing over time.

Brief Description of the Drawings

These and other objects, features and advantages of the present invention will be apparent from the following detailed description and the appended claims and drawings in which:

FIG. 1 is a block diagram of a system in accordance with a preferred embodiment of the present invention;

FIG. 2 is a diagram illustrating reductions of two-carbon and higher starting materials;

FIG. 3 are formulae of example hydrodimerization reactions;

FIG. 4 is a table illustrating relative product yields for different cathode material, catalyst and cathode potential combinations ;

FIG. 5 is a formula of an aromatic heterocyclic amine catalyst ;

FIGS. 6-8 are formulae of substituted or unsubstituted aromatic 5-member heterocyclic amines or 6-member heterocyclic amines ;

FIG. 9 is a flow diagram of an example method used in electrochemical examples; and

FIG. 10 is a flow diagram of an example method used in photochemical examples. Detailed Description of the Preferred Embodiments

Some embodiments of the present invention relate to heterocycle catalyzed reduction of keto groups to hydroxy1 groups, carboxylic acids to more reduced carboxylic acids, carboxylic acids to aldehydes and/or aldehydes to alcohols. Some embodiments ^' generally relate to hydrodimerize of carbonyl compounds. The methods generally include electrochemically and/or photoelectrochemically reducing in an aqueous, electrolyte-supported divided electrochemical cell that includes an anode (e.g., an inert conductive counter electrode) in a cell compartment and a conductive or p-type semiconductor working cathode electrode in another cell compartment. A catalyst may be included to help produce a reduced product. The reactants may be continuously introduced into the cathode electrolyte solution to saturate the solution.

For electrochemical reductions, the electrode may be a suitable conductive electrode, such as Al, Au, Ag, C, Cd, Co, Cr, Cu, Cu alloys (e.g., brass and bronze) , Ga, Hg, In, Mo, Nb, Ni, Ni alloys, Ni-Fe alloys, Sn, Sn alloys, Ti, V, W, Zn, stainless steel (SS) , austenitic steel, ferritic steel, duplex steel martensitic steel, Nichrome, elgiloy (e.g., Co-Ni-Cr) , degenerately doped p-Si, degenerately doped p-Si:As and degenerately doped p-Si:B. Other conductive electrodes may be implemented to meet the criteria of a particular application. For photoelectrochemical reductions, the electrode may be a p-type semiconductor, such as p-GaAs, p-GaP, p-InN, p-InP, p-CdTe, p-GaInP ₂ and p-Si. Other semiconductor electrodes may be implemented to meet the criteria of a particular application.

Before any embodiments of the invention are explained in detail, it is to be understood that the embodiments may not be limited in application per the details of the structure or the function as set forth in the following descriptions or illustrated in the figures of the drawing. Different embodiments may be capable of being practiced or carried out in various ways. Also, it is to be understood that the phraseology and terminology used herein is for the purpose of description and should not be regarded as limiting. The use of terms such as "including," "comprising," or "having" and variations thereof herein are generally ir.eant to encompass the item listed thereafter and equivalents thereof as well as additional items. Further, unless otherwise noted, technical terms may be used according to conventional usage.

In the following description of methods, process steps may be carried out over a range of temperatures (e.g., approximately 10°C (Celsius) to 50°C) and a range of pressures (e.g., approximately 1 to 10 atmospheres) unless otherwise specified. Numerical ranges recited herein generally include all values from the lower value to the upper value (e.g., all possible combinations of numerical values between the lowest value and the highest value enumerated are considered expressly stated) . For example, if a concentration range or beneficial effect range is stated as 1% to 50%, it is intended that values such as 2% to 40%, 10% to 30%, or 1% to 3%, etc., are expressly enumerated. The above may be simple examples of what is specifically intended.

Referring to FIG. 1, a block diagram of a system 100 is shown in accordance with a preferred embodiment of the present invention. The system (or apparatus) 100 generally comprises a cell (or container) 102, a liquid source 104, a power source 106, a reactant source 108, an extractor 110 and an extractor 112, A product may be presented from the extractor 110. An output gas may be presented from the extractor 112. Another output gas may be presented from the cell 102.

The cell 102 may be implemented as a divided cell. The divided cell may be a divided electrochemical cell and/or a divided photochemical cell. The cell 102 is generally operational to reduce carbonyl compounds and/or carboxyl group compounds {e.g., reactants) to aldehyde, alcohols, hydroxyl groups and/or organic products containing keto groups. The reactants may also be reduced to methanol, ethanol, propanol, pentanol, hexanol and septanol. The cell 102 may also be operational to hydrodimerize carbonyl compounds to butanone (methyl ethyl ketone) , butanol, octanone and/or octanol. The carbonyl compounds may include, but are not limited to, aldehydes and carboxylic acids. The reactions generally takes place by introducing the reactants into an aqueous solution of an electrolyte in the cell 102. A cathode in the cell 102 may hydrodimerize and/or reduce the reactants into one or more organic compounds.

The cell 102 generally comprises two or more compartments (or chambers) 114a-114b, a separator (or membrane) 116, an anode 118 and a cathode 120. The anode 118 may be disposed in a given compartment (e.g., 114a). The cathode 120 may be disposed in another compartment (e.g., 114b) on an opposite side of the separator 116 as the anode 118. An aqueous solution 122 may fill both compartments 114a-114b. A catalyst 124 may be added to the compartment 114b containing the cathode 120.

The liquid source 104 may implement a water source. The liquid source 104 may be operational to provide pure water to the cell 102.

The power source 106 may implement a variable voltage source. The source 106 may be operational to generate an electrical potential between the anode 118 and the cathode 120. The electrical potential my be a DC voltage.

The reactant source 108 may implement a keto group, carbonyl compound, carboxyl group compound and/or aldehyde source. The source 108 is generally operational to provide the reactants to the cell 102. In some embodiments, the reactants are introduced directly into the compartment 114b containing the cathode 120.

The extractor 110 may implement an organic product extractor. The extractor 110 is generally operational to extract (separate) organic products (e.g., acetaldehyde, acetone, butanone, 2-butanol, n-butanol, ethanol, glyoxal, glyoxylic acid, methanol, octanone, octanol, oxalic acid, propanol, propioin and the like) from the electrolyte 122. The extracted organic products may be presented through a port 126 of the system 100 for subsequent storage and/or consumption by other devices and/or processes.

The extractor 112 may implement an oxygen extractor. The extractor 112 is generally operational to extract oxygen (e.g., 0 ₂ ) byproducts created by the reactions. The extracted oxygen may be presented through a port 128 of the system 100 for subsequent storage and/or consumption by other devices and/or processes. Any other excess gases (e.g. , hydrogen) created by the reactions may be vented from the cell 102 via a port 130.

In the process described, water may be oxidized (or split) to protons and oxygen at the anode 118 while organic molecules containing a carbonyl or carboxyl group are hydrodimerized and sometimes reduced at the cathode 120. The electrolyte 122 in the cell 102 may use water as a solvent with any salts that are water soluble and with a heterocycle catalyst 124. The catalysts 124 may include, but are not limited to, azoles, imidazoles, indoles, pyridine, pyrrole, thiazole and furan. Examples of the heterocyclic compounds catalysts 124 may be pyridine, imidazole, pyrrole, thiazole, furan, thiophene and the substituted heterocycles such as amino-thiazole and benzimidazole . Cathode materials generally include any conductor. Any anode material may be used. The overall process is generally driven by the power source 106. Combinations of cathodes 120, electrolytes 122, introduction of the carbonyl or carboxyl group to the cell 102, pH levels and electric potential from the power source 106 may be used to control the reaction products of the cell 102. Organic products resulting from the reactions may include, but are not limited to, alcohols, aldehydes, organic molecules containing hydroxy1 groups and/or organic products containing keto groups.

In some nonaqueous embodiments, the solvent may include methanol, acetonitrile, and/or other nonaqueous solvents. The electrolytes generally include tetraalkyl ammonium salts and a heterocyclic catalyst. In a system containing nonaqueous catholyte and aqueous anolyte, the products generally include all of the products seen in aqueous systems with higher yields .

Experiments were conducted in one, two and three- compartment electrochemical cells 102 with a platinum anode 118 and Saturated Calomel Electrode (SCE) as the reference electrode. The experiments were generally conducted at ambient temperature and pressure. Reactants were introduced into the cells during the experiments. A potentiostat or DC power supply 106 provides the electrical energy to drive the process. Cell potentials ranged from 1.5 volts to 4 volts, depending on the cathode material. Half cell potentials at the cathode ranged from -1 volt to -2 volts relative to the SCE, depending on the cathode material used. Products from the experiments were analyzed using gas chromatography and a spectrometer. Referring to FIG. 2, a diagram illustrating reductions of two-carbon and higher starting materials is shown. Complex molecules, such as oxalic acid (a carboxylic acid) may be reduced to a simpler glyoxylic acid {a C2 carboxylic acid) . The glyoxylic acid may be further reduced to glyoxal (a dialdehyde) . Furthermore, the glyoxal may be reduced to acetaldehyde (an aldehyde) . The acetaldehyde is generally reducible to ethanol (a primary alcohol) . Other aldehydes may include, but are not limited to, formaldehyde, butanal and benzaldehyde. Other alcohols may include, but are not limited to, methanol, 2-butanol, n-butanol, propanol, and propioin. The process is controlled to get a desired product by using combinations of specific conductive cathodes, catalysts, electrolytes, surface morphology of the electrodes, pH levels and/or introduction of reactants relative to the cathode. Faradaic yields for the products generally range from less than 1% to more than 90% with the remainder generally being hydrogen.

Referring to FIG. 3, formulae of example hydrodimerization reactions are shown. Formula (!) generally illustrates a hydrodimerization of two acetaldehyde molecules (e.g., C ₂ H ₄ O) into a butanone molecule (e.g., C ₄ H ₈ O) and half of an oxygen (e.g., O ₂ ) molecule. Formula (2) may illustrate a hydrodimerization of two acetaldehyde molecules and two hydrogen ions (e.g., H ⁺ ) into a butanol molecule (e.g., C ₄ H ₉ OH) and half of an oxygen molecule. Formula (3) may show a hydrodimerization of two butyric acid molecules (e.g., C ₄ H ₈ O ₂ ) and two hydrogen ions into an octanol molecule (e.g., C ₈ H ₁₈ O) and one and a half oxygen molecules. Formula (4) generally illustrates a hydrodimerization of two butyric acid molecules into a 2-octanone molecule (e.g., C ₈ H ₁₆ O) and one and a half oxygen molecules. Referring to FIG. 4, a table illustrating relative product yields for different cathode material, catalyst and cathode potential combinations are shown. Lower pH generally favors reduction of a carbonyl group without dimerization, for instance, the reduction of formic acid to methanol. Aldehydes may be more likely to reduce to alcohols without dimerization. Carboxylic acids and dialdehydes may be more likely to dimerize, with the exception of formic acid. Faradaic yields generally improve with more negative cathodic potential, particularly for dimerization. Any N-containing heterocycle may be used as a catalyst. 4,4' bipyridine was generally found to be an effective catalyst. Conversion rates generally improve with catalyst concentrations in excess of 50 millimolar (mM) .

Referring to FIG. 5, a formula of an aromatic heterocyclic amine catalyst is shown. The ring structure may be an aromatic 5-member heterocyclic ring or 6-member heterocyclic ring with at least one ring nitrogen and is optionally substituted at one or more ring positions other than nitrogen with R. L may be C or N. Rl may be H. R2 may be H if L is N or R2 is R if L is C. R is an optional substitutent on any ring carbon and may be independently selected from H, a straight chain or branched chain lower alkyl, hydroxyl, amino, pyridyl, or two R's taken together with the ring carbons bonded thereto are a fused six-member aryl ring and n = 0 to 4.

Referring to FIGS. 6-8, formulae of substituted or unsubstituted aromatic 5-member heterocyclic amines or 6-member heterocyclic amines are shown. Referring to FIG. 6, R3 may be H. R4, R5, R7 and R8 are generally independently H, straight chain or branched chain lower alkyl, hydroxyl, amino, or taken together are a fused six-member aryl ring. R6 may be H, straight chain or branched chain lower alkyl, hydroxyl, amino or pyridyl.

Referring to FIG. 7, one of LI, L2 and L3 may be N, while the other L's may be C. R9 may be H. If Ll is N, R10 may be H. If L2 is N, Rll may be H. If L3 is N, R12 may be H. If Ll, L2 or L3 is C, then R10, Rll, R12, R13 and R14 may be independently selected from straight chain or branched chain lower alkyl, hydroxyl, amino, or pyridyl.

Referring to FIG. 8, R15 and R16 may be H. R17, R18 and R19 are generally independently selected from straight chain or branched chain lower alkyl, hydroxyl, amino, or pyridyl.

Suitably, the concentration of aromatic heterocyclic amine catalysts is about 10 mM to 1 M. Concentrations of the electrolyte may be about 0.1 M to 1 M. The electrolyte may be suitably a salt, such as KCl, NaNO ₃ , Na ₂ SO ₄ , NaCl, NaF, NaClO ₄ , KClO ₄ , K ₂ SiO ₃ , or CaCl ₂ at a concentration of about 0.5 M. Other electrolytes may include, but are not limited to, all group 1 cations (e.g., H, Li, Na, K, Rb and Cs) except Francium (Fr) , Ca, ammonium cations, alkylammonium cations and alkyl amines. Additional electrolytes may include, but are not limited to, all group 17 anions (e.g., F, Cl, Br, I and At), borates, carbonates, nitrates, nitrites, perchlorates, phosphates, polyphosphates, silicates and sulfates. Na generally performs as well as K with regard to best practices, so NaCl may be exchanged with KCl. NaF may perform about as well as NaCl, so NaF may be exchanged for NaCl or KCl in many cases. Larger anions tend to change the chemistry and favor different products. For instance, sulfate may favor polymer or methanol production while Cl may favor products such as acetone. The pH of the solution is generally maintained at about pH 3 to 8, suitably about 4.7 to 5.6. Some embodiments of the present invention may be further explained by the following examples, which should not be construed by way of limiting the scope of the invention.

Example 1: General Electrochemical Methods.

Chemicals and materials. All chemicals used were > 98% purity and used as received from the vendor {e.g., Aldrich) , without further purification. Either deionized or high purity water (Nanopure, Barnstead) was used to prepare the aqueous electrolyte solutions.

Electrochemical system. The electrochemical system was composed of a standard two-compartment electrolysis cell 102 to separate the anode 118 and cathode 120 reactions. The compartments were separated by a porous glass frit or other ion conducting bridge 116. A 0.5 M KC1 (Electro Migration Dispersion (EMD) > 99%) was generally used as the supporting electrolyte 122. A concentration of the desired aromatic heterocyclic amine, such as pyridine, pyridine derivatives, bipyridine, imidazole and imidazole derivatives, of between about 1 mM to 1 M was used.

Referring to FIG. 9, a flow diagram of an example method 140 used in the electrochemical examples is shown. The method (or process) 140 generally comprises a step (or block) 142, a step (or block) 144, a step (or block) 146, a step (or block) 148 and a step (or block) 150. The method 140 may be implemented using the system 100.

In the step 142, the electrodes 118 and 120 may be activated where appropriate. Introduction of the reactants into the cell 102 may be performed in the step 144. Electrolysis of the reactants into organic products may occur during step 146. In the step 148, the organic products may be separated from the electrolyte. Analysis of the reduction products may be performed in the step 150.

The working electrode was a steel electrode of a known area. Before and during all electrolysis, the reactants were continuously introduced into the electrolyte to saturate the solution. The resulting pH of the solution was maintained at about pH 3 to pH 8.

Example 2: General Photoelectrochemical Methods.

Chemicals and materials. All chemicals used were analytical grade or higher. Either deionized or high purity water (Nanopure, Barnstead) was used to prepare the aqueous electrolyte solutions .

Fhotoelectrochemical system. The photoelectrochemical system was composed of a Pyrex three-necked flask containing 0.5 M KCl as supporting electrolyte and a 1 mM to 1 M catalyst (e.g., 10 mM pyridine or pyridine derivative) . The photocathode was a single crystal p-type semiconductor etched for approximately 1 to 2 minutes in a bath of concentrated HNO ₃ :HC1, 2:1 v/v prior to use. An ohmic contact was made to the back of the freshly etched crystal ^' using an indium/zinc (2 wt. % Zn) solder. The contact was connected to an external lead with conducting silver epoxy (Epoxy Technology H31) covered in glass tubing and insulated using an epoxy cement {Loctite 0151 Hysol) to expose only the front face of the semiconductor to solution. All potentials were referenced against a saturated calomel electrode (Accumet) . During all electrolysis, the reactants were continuously introduced to the electrolyte to saturate the solution. The resulting pH of the solution was maintained at about pH 3 to 8 {e.g., pH 5.2) .

Referring to FIG. 10, a flow diagram of an example method 160 used in the photochemical examples is shown. The method (or process) 160 generally comprises a step (or block) 162, a step {or block) 164, a step (or block) 166, a step (or block) 168 and a step (or block) 170. The method 160 may be implemented using the system 100.

In the step 162, the photoelectrode may be activated.

Introduction of the reactants into the cell 102 may be performed in the step 164. Electrolysis of the reactants into organic products may occur during step 166. In the step 168, the organic products may be separated from the electrolyte. Analysis of the reduction products may be performed in the step 170.

Light sources. Four different light sources were used for the illumination of the p-type semiconductor electrode. For initial electrolysis experiments, a Hg-Xe arc lamp (USHIO UXM 200H) was used in a lamp housing (PTI Model A-1010) and powered by a PTI LTS-200 power supply. Similarly, a Xe arc lamp (USHIO UXL 151H) was used in the same housing in conjunction with a PTI monochromator to illuminate the electrode at various specific wavelengths .

A fiber optic spectrometer (Ocean Optics S2000) or a silicon photodetector (Newport 818-SL silicon detector) was used to measure the relative resulting power emitted through the monochromator. The flatband potential was obtained by measurements of the open circuit photovoltage during various irradiation intensities using the 200 watt (W) Hg-Xe lamp (3 W/cm ² - 23 W/cm ² ) . The photovoltage was observed to saturate at intensities above approximately 6 W/cm ² .

For quantum yield determinations, electrolysis was performed under illumination by two different light-emitting diodes (LEDs) . A blue LED (Luxeon V Dental Blue, Future Electronics) with a luminous output of 500 milliwatt (mW) +/- 50 nW at 465 nanometers (nra) and a 20 nm full width at half maximum (FWHM) was driven at to a maximum rated current of 700 mA using a Xitanium Driver (Advance Transformer Company) . A Fraen collimating lens (Future Electronics) was used to direct the output light. The resultant power density that reached the window of the photoelectrochemical cell was determined to be 42 mW/cm ² , measured using a Scientech 364 thermopile power meter and silicon photodetector. The measured power density was assumed to be greater than the actual power density observed at the semiconductor face due to luminous intensity loss through the solution layer between the wall of the photoelectrochemical cell and the electrode.

Example 3: Analysis of Products of Electrolysis.

Electrochemical experiments were generally performed using a CH Instruments potentiostat or a DC power supply with current logger to run bulk electrolysis experiments. The CH Instruments potentiostat was generally used for cyclic voltammetry. Electrolysis was run under potentiostatic conditions from approximately 6 hours to 30 hours until a relatively similar amount of charge was passed for each run.

Gas Chromatography. The electrolysis samples were analyzed using a gas chromatograph (HP 5890 GC) equipped with a FID detector. Removal of the supporting electrolyte salt was first achieved with an Amberlite IRN-150 ion exchange resin (cleaned prior to use to ensure no organic artifacts by stirring in a 0.1% v/v aqueous solution of Triton X-100, reduced (Aldrich) , filtered and rinsed with a copious amount of water, and vacuum dried below the maximum temperature of the resin (approximately 60°C) before the sample was directly injected into the GC which housed a DB-Wax column (Agilent Technologies, 60 m, 1 micrometer (μm) film thickness) . Approximately 1 gram of resin was used to remove the salt from 1 milliliter (mL) of the sample. The injector temperature was held at 200°C, the oven temperature maintained at 120°C, and the detector temperature at 200°C.

Spectrophotometry. The presence of formaldehyde was also determined by the chromotropic acid assay. Briefly, a solution of 0.3 g of 4, 5-dihydroxynaphthalene- 2 , 7-disulfonic acid, disodium salt dihydrate (Aldrich) was dissolved in 10 mL deionized water before diluting to 100 mL with concentrated sulfuric acid. For formaldehyde, an aliquot of 1.5 mL was then added to 0.5 mL of the sample. The presence of formaldehyde (absorbency at 577 nm) was detected against a standard curve using an HP 8453 UV-Vis spectrometer. For formic acid, a 0.5 mL aliquot of sample was first reduced with an approximately 100 mg piece of Mg wire and 0.5 mL concentrated hydrochloric acid (added slowly in aliquots over a 10 minute period) to convert to formaldehyde before following the chromotropic acid assay as described above.

Nuclear Magnetic Resonance. NMR spectra of electrolyte volumes after bulk electrolysis were also obtained using an automated Bruker UltrashieldTM 500 Plus spectrometer with an excitation sculpting pulse technique for water suppression. Data processing was achieved using MestReNova software.

Selective hydrodimerization of carbonyl-containing organic molecules, such as aldehydes and carboxylic acids, may be performed in the cell 102. For instance, some two-carbon molecules such as an acetaldehyde may be hydrodimerized into butanone (methyl ethyl ketone) or butanol. Similarly, a carboxylic acid such as butyric acid may be hydrodimerized to octanone or octanol.

Selective reduction of carboxylic acids to aldehydes and/or alcohols and the reduction of aldehydes to alcohols may also be performed in the cell 102. other carbonyl groups, such as ketones, may also be reduced to hydroxy! groups. The selectivity of the process generally maximizes efficiency and ease of product extraction relative to existing processes used for organic chemical production. Some embodiments do not operate at high temperatures, high pressures or high acidity. Biologically-produced chemicals with carbonyl groups may be converted to environmentally-friendly alcohol fuels, thereby reducing greenhouse gas emissions. Conversion of small molecules to longer-chain molecules, generally reduces the costs of upgrading small molecules into high value products. A variety of C2, C4, C6, C8 organic molecules may be produced.

Some embodiments of the present invention generally provide for new cathode materials and new electrolyte materials. Specific combinations of the cathode materials, the electrolytes and the catalysts may be used to get a desired organic product. Process conditions may be controlled to maximize conversion efficiency and selectivity. Cell parameters may be selected to minimize unproductive side reactions like H ₂ evolution from water electrolysis. Choice of specific configurations of heterocyclic amine catalysts with engineered functional groups may be utilized in the system 100 to achieve high faradaic rates. Process conditions described above may facilitate long life (e.g. , improved stability) , electrode and cell cycling and product recovery.

Cathode, catalyst and electrolyte combinations may be used to selectively electrohydrodimerize carbonyl-containing compounds to a variety of valuable organic chemicals . The cathode, catalyst and electrolyte combinations may also be used to selectively reduce carbonyl groups, including aldehydes, to alcohols and carboxylic acids to aldehydes and/or alcohols. The relative low cost and abundance of the combinations disclosed above generally opens the possibility of commercialization. The processes described my operate at atmospheric pressure, ambient temperature, uses water as a solvent and features mild pH (e.g., generally greater than pH 4) . The features generally mean that abundant, low-cost materials may be used to build plants incorporating some embodiments of the present invention. Furthermore, the process may be stable over time.

In an electrochemical system with fixed cathodes, the electrolyte and/or catalyst may be altered to change the organic product mix. The cathodes may be swapped out in a modular electrochemical system to change the organic product mix. In a hybrid photoelectrochemical system, the cathode or anode may ^' be a photovoltaic material. Plant operating in conjunction with biological production of simple carbonyl-containing chemicals such as acetaldehyde, lactic acid, citric acid, etc. may include the system 100 to covert the chemicals into other useful organic compounds. Biologically produced chemicals may be converted into longer chain chemicals and products such fuels, solvents and the like.

While the invention has been particularly shown and described with reference to the preferred embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made without departing from the scope of the invention.