Patent Grant
9051656
The present invention describes a method for the manufacture of aryl-alkyl surfactant precursors from inexpensive starting materials. The invention utilizes an electrolytic decarboxylation process (EDP) to perform the reaction at low temperature without the use of catalysts. The general surfactants manufactured will potentially be used by companies involved with Enhanced Oil Recovery (EOR), synthetic motor oil, flocculation, mining, paints, coatings, adhesives, industrial applications under extreme conditions of pH and temperature just to mention a few.
More than 50 million pounds of aryl-alkyl sulfonic acid surfactants are widely used for Enhanced Oil Recovery (EOR) and other industrial applications, but they are expensive to manufacture by a traditional process shown below:
As shown above, the current process involves using long chain alpha-alkenes that are expensive, currently ˜$6/gallon, to react with benzene ring in the presence of a catalyst. In the above process, the beta carbon of the long chain alpha-alkene is reactive, resulting is a product having an undesirable methyl side chain.
It would be an advancement in the art to prepare aryl-alkyl surfactant precursors using lower cost starting materials compared to alpha-alkenes. It would also be an advancement in the art to prepare aryl-alkyl surfactant precursors in a process that avoids the producing products having undesirable side chains.
The present invention describes a method for the manufacture of aryl-alkyl surfactant precursor from inexpensive starting materials. According to the presently discussed method, aryl-alkyl surfactant precursors are manufactured using lower cost ($1.50/gallon) fatty acids instead of alpha-alkenes. Also the invention describes an electrolytic decarboxylation process (EDP) to perform the reaction at low temperature and low pressure without the use of catalysts. The EDP process using a divided or undivided cell may offer a way to reduce their cost of manufacture. The general surfactants manufactured will potentially be used by companies involved with EOR, synthetic motor oil, flocculation, mining, paints, coatings, adhesives, industrial applications under extreme conditions of pH and temperature just to mention a few.
One Electrolytic Decarboxylation Process is disclosed in U.S. Patent Application Publication No. 20110024288, which is incorporated herein by reference.
The invention relates to the conversion of mixture of arenes (aromatic or aryl hydrocarbons) or alkali aryl carboxylates and fatty acid alkali salt starting materials into aryl-alkyl hydrocarbons by electrolytic method. The starting materials can be of plant, algal, or animal origin. The electrolysis cell deployed for this reaction utilizes a selective alkali ion transport membrane technology.
In a first disclosed method, a mixture of aryl carboxylic acid and alkyl carboxylic acids are converted to their respective alkali salts via an acid neutralization process. These alkali salts are then mixed with one or more appropriate solvents to yield a reacting mixture. The mixture is then converted to an aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of both the aryl carboxylate and the alkyl carboxylate and subsequent aryl-alkyl carbon-carbon coupling. The alkyl carboxylic acid is preferably a fatty acid.
In a second disclosed method, an arene and alkyl acid alkali salts are mixed with one or more appropriate solvents to yield a reacting mixture. Non-limiting examples of arene hydrocarbons include benzene, ethyl benzene, and naphthalene. The mixture is then converted to aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of the fatty acid carboxylate and subsequent aryl-alkyl carbon-carbon coupling.
In a third disclosed method, an arene hydrocarbon is reacted with an alkali metal to form an alkali metal-arene adduct (Ar−M+). The adduct is mixed with a fatty acid alkali salt in one or more appropriate solvents to yield a reacting mixture. The mixture is then converted to aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of fatty carboxylate and subsequent aryl-alkyl carbon-carbon coupling.
Embodiments of the present invention will be best understood by reference to the enclosed drawings. It will be readily understood that the components of the present invention, as generally described and illustrated in the figures herein, could be arranged and designed in a wide variety of different configurations. Thus, the following more detailed description of the embodiments of the methods and cells of the present invention, as represented in
Reference throughout this specification to “one embodiment,” “an embodiment,” or similar language means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present invention. Thus, appearances of the phrases “in one embodiment,” “in an embodiment,” and similar language throughout this specification may, but do not necessarily, all refer to the same embodiment. Additionally, while the following description refers to several embodiments and examples of the various components and aspects of the described invention, all of the described embodiments and examples are to be considered, in all respects, as illustrative only and not as being limiting in any manner.
Furthermore, the described features, structures, or characteristics of the invention may be combined in any suitable manner in one or more embodiments. In the following description, numerous specific details are disclosed to provide a thorough understanding of embodiments of the invention. One having ordinary skill in the relevant art will recognize, however, that the invention may be practiced without one or more of the specific details, or with other methods, components, materials, and so forth. In other instances, well-known structures, materials, or operations are not shown or described in detail to avoid obscuring aspects of the invention.
Referring now to
The alkali ion conductive membrane 110 can comprise virtually any suitable alkali ion conductive membrane that selectively conducts alkali ions and prevents the passage of water, hydroxide ions, or other reaction products. The alkali ion conducting membrane may comprise a ceramic, a polymer, or combinations thereof. In one non-limiting embodiment, the alkali ion conducting membrane comprises an alkali ion super ion conducting (MSICON) membrane. Some non-limiting examples of such membranes include, but are not limited to, a NaSICON (sodium super ionic conductor membrane) and a NaSICON-type membrane. The alkali ion conductive membrane may be any of a number of sodium super ion conducting materials, including, without limitation, those disclosed in United States Patent Application Publications Nos. 2010/0331170 and 2008/0245671 and in U.S. Pat. No. 5,580,430. The foregoing applications and patent are hereby incorporated by reference. Where other non-sodium alkali compounds are used within the scope of the present invention, it is to be understood that similar alkali ion conductive membranes such as a LiSICON membrane, a LiSICON-type membrane, a KSICON membrane, a KSICON-type membrane may be used. In some embodiments, an alkali ion conducting ion-exchange polymeric membrane may be used. In some embodiments, the alkali ion conducting membrane may comprise an alkali ion conductive glass or beta alumina.
In one embodiment, the alkali ion conductive membrane is between about 200 microns and about 2000 microns thick. In other embodiment, the membrane is between about 400 and 1000 microns thick. In one embodiment 3 inch diameter MSICON wafers are assembled in a scaffold.
The electrochemical cell 100 may be of standard parallel plate configuration where flat plate electrodes and membranes are used, such as shown in
The anode 116 can comprise any suitable anode material that allows oxidation (decarboxylation) reaction and subsequent free radical carbon-carbon coupling in the anolyte compartment when electrical potential passes between the anode and the cathode. Some non-limiting examples of suitable anode materials include, but are not limited to, smooth platinum, titanium, nickel, cobalt, iron, stainless steel, lead dioxide, metal alloys, combinations thereof, and other known or novel anode materials. In one embodiment, the anode 116 may comprise iron-nickel alloys such as KOVAR® or INVAR®. In other embodiments, the anode 116 may comprise carbon based electrodes such as boron doped diamond, glassy carbon, and synthetic carbon. Additionally, in some embodiments the anode 116 comprises a dimensionally stable anode (DSA), which may include, but is not limited to, rhenium dioxide and titanium dioxide on a titanium substrate, and rhenium dioxide and tantalum pentoxide on a titanium substrate.
The cathode 118 may also be fabricated of any suitable cathode that allows the cell to reduce water or methanol in the catholyte compartment to produce hydroxide ions or methoxide ions and hydrogen gas. The cathode 118 may comprise the materials used in the anode 116. Some non-limiting examples of suitable cathode materials include, without limitation, nickel, stainless steel, graphite, and any other suitable cathode material that is known or novel.
The electrolytic cell 100 is operated by feeding an anolyte solution 124 into the anolyte compartment 112. The anolyte solution 124 comprises a solvent 126, an alkali metal salt of an alkyl carboxylic acid 128, and an aryl compound 130. In some embodiments, the aryl compound may comprise an alkali metal salt of an aryl carboxylic acid. In some embodiments, the aryl compound may comprise an arene hydrocarbon. In some embodiments, the aryl compound may comprise an alkali metal-arene adduct (Ar−M+). The alkali metal-arene adduct is obtained by reacting an arene hydrocarbon with an alkali metal.
The anolyte solution 124 may comprise a mixture of solvents. The anolyte solution solvent may comprise a two-phase solvent system, wherein one phase is capable of dissolving ionic materials and the other phase is capable of dissolving non-ionic materials. For example, the solvent may comprise an organic phase solvent such as a non-ionic, non-aqueous solvent. Inorganic or other solvents may also be used. An example of such a solvent would be a long chain fatty acid alcohol, or other similar organic solvent. Mixed with this organic phase solvent is an ionic solvent or aqueous solvent, such as water or an ionic liquid. This water/ionic liquid dissolves the alkali metal salt of the fatty acid. Using this type of “two-phase” system, the aryl-alkyl hydrocarbon, when formed, will readily dissolve in the organic phase, and will be repelled by the aqueous/ionic phase. This means that the formed hydrocarbon(s) will readily separate from the aqueous/ionic phase.
In one embodiment, the anolyte comprises G-type solvents, H-Type solvents, and/or mixtures thereof. G-type solvents are di-hydroxyl compounds. In one embodiment the G-type compound comprises two hydroxyl groups in contiguous position. H-type solvents are hydrocarbon compounds or solvent which can dissolve hydrocarbons. For example, H-type solvents include, hydrocarbons, chlorinated hydrocarbons, alcohols, ketones, mono alcohols, and petroleum fractions such as hexane, gasoline, kerosene, dodecane, tetrolene, and the like. The H-type solvent can also be a product of the decarboxylation process recycled as a fraction of the hydrocarbon product. This will obviate the need of procuring additional solvents and hence improve overall economics of the process.
By way of further description, G-type of solvents solvate a —COONa group of a alkali metal salt of carboxylic acid by hydrogen bonding with two different oxygen atoms, whereas the hydrocarbon end of the alkali metal salt of carboxylic acid is solvated by an H-type of solvent. For a given G-type solvent, the solvency increases with increase of hydrocarbons in the H-type solvent.
Table 1, below, shows some non-limiting examples of G-type and H-type solvents:
The solubility of various sodium salts of carboxylic acids were tested at room temperature in a magnetically stirred glass beaker using G-type solvents, H-type solvents, and combinations of G- and H-type solvents. The following tables show solubility test results for various salts.
The anolyte solution may optionally contain a supporting electrolyte which is soluble in the solvent and which provides high electrolyte conductivity in the anolyte solution. One non-limiting example of a supporting electrolyte includes an alkali metal tetrafluoroborate. Another example may include tetramethylammonium hexafluorophosphate. Other ionic solids may also be used.
Certain alkali ion conductive membranes, such as ceramic NaSICON and NaSICON-type membranes, have a high temperature tolerance and thus the anolyte solution may be heated to a higher temperature without substantially affecting the temperature of the catholyte solution (or vice versa). NaSICON and NaSICON-type ceramic membranes can be heated and still function effectively at higher temperatures. This means that polar solvents (or non-polar solvents) that dissolve fatty acids and sodium salts at high temperatures may be used in the anolyte solution. For example, palmitic acid may be heated to form a liquid and this liquid is an excellent solvent for sodium palmitate. At the same time, the catholyte solution is unaffected by temperature. In fact, a different solvent system could simultaneously be used in the catholyte compartment. Alternatively, other molten salts or acids may be used to dissolve ionic sodium carboxylic acids and salts in the anolyte. Long chain hydrocarbons, ethers, triglycerides, esters, alcohols, or other solvents may dissolve carboxylic acids and sodium salts. Such compounds could be used as the anolyte solvent without affecting the catholyte. Ionic liquids could also be used as the anolyte solvent. These materials not only would dissolve large quantities of fatty acid sodium salts, but also, may operate to facilitate the decarboxylation reaction at higher temperatures. Ionic liquids are a class of chemicals with very low vapor pressure and excellent dissolving abilities/dissolving properties. A variety of different ionic liquids may be used.
Under the influence of electric potential 122, electrochemical (anodic) decarboxylation reactions take place at the anode 116 resulting in the formation of carbon dioxide 132 and alkyl radicals (R•). The alkyl radicals react with the aryl compound under conditions that permit aryl-alkyl carbon-carbon coupling, thereby forming the aryl-alkyl surfactant precursor, and optionally other reaction products which may be removed from the anolyte compartment 112 in product stream 134.
In some disclosed embodiments, a catholyte solution feed stream 136 is fed into the catholyte compartment 114. The catholyte solution may comprise a solvent that is the same or different than the anolyte solvent. The anolyte and catholyte solvents may be different because the alkali conductive membrane isolates the compartments 112 and 114 from each other. Thus, the anolyte and catholyte solvents may be each separately selected for the reactions in each particular compartment (and/or to adjust the solubility of the chemicals in each particular compartment). Thus, the designer of the cell 100 may tailor the anolyte and catholyte solvents for the reaction occurring in the specific compartment, without having to worry about the solvents mixing and/or the reactions occurring in the other compartment. The catholyte solvent may comprise a mixture of solvents.
In one disclosed embodiment, the catholyte solution comprises water. At least initially, the catholyte solution feed stream 136 preferably includes alkali ions, which may be in the form of an unsaturated alkali hydroxide solution. The concentration of alkali hydroxide is between about 0.1% by weight and about 50% by weight of the solution. In one embodiment, the catholyte solution feed stream 136 includes a dilute solution of alkali hydroxide. During operation, the source of alkali ions may be provided by alkali ions 120 transporting across the alkali ion conductive membrane 110 from the anolyte compartment 112 to the catholyte compartment 114. While alkali hydroxide is used in the following discussion, persons skilled in the art will appreciate that methanol may substitute alkali hydroxide in the apparatus for preparing alkali methylate instead. Thus, feed stream 136 may comprise methanol.
At the cathode 118, reduction of water to form hydrogen gas 138 and hydroxide ions takes place (Reaction 1). The hydroxide ions react with available alkali ions (M+) 120 (transported from anode compartment 112 via the alkali conductive membrane 110) to form alkali hydroxide as shown in Reaction (2). The alkali hydroxide may be recovered in catholyte product stream 140.
2H2O+2e−→H2+2OH− (1)
M++2H2O+2e−→2MOH+H2 (2)
In the case of catholyte solution feed stream 136 comprising methanol, methoxide ions will react with available alkali ions to form alkali methoxide as shown in Reaction (3).
2M++2CH3OH+2e−→2MOCH3+H2 (3)
The alkali methoxide may be recovered in catholyte product stream 140.
It will be appreciated that the catholyte product stream 140 comprises a base which may be used to neutralize the alkyl carboxylic acid to produce the alkali metal salt of an alkyl carboxylic acid 128. Thus, the base consumed in the acid neutralization step may be produced in the catholyte compartment, recovered, and re-used in future acid neutralization reactions or other chemical processes.
In one embodiment of the processes and apparatus of the present invention, the electrolytic cell 100 may be operated in a continuous mode. In a continuous mode, the cell is initially filled with anolyte solution and catholyte solution and then, during operation, additional solutions are fed into the cell and products, by-products, and/or diluted solutions are removed from the cell without ceasing operation of the cell. The feeding of the anolyte solution and catholyte solution may be done continuously or it may be done intermittently, meaning that the flow of a given solution is initiated or stopped according to the need for the solution and/or to maintain desired concentrations of solutions in the cell compartments, without emptying any one individual compartment or any combination of the two compartments. Similarly, the removal of solutions from the anolyte compartment and the catholyte compartment may also be continuous or intermittent. Control of the addition and/or removal of solutions from the cell may be done by any suitable means. Such means include manual operation, such as by one or more human operators, and automated operation, such as by using sensors, electronic valves, laboratory robots, etc. operating under computer or analog control. In automated operation, a valve or stopcock may be opened or closed according to a signal received from a computer or electronic controller on the basis of a timer, the output of a sensor, or other means. Examples of automated systems are well known in the art. Some combination of manual and automated operation may also be used. Alternatively, the amount of each solution that is to be added or removed per unit time to maintain a steady state may be experimentally determined for a given cell, and the flow of solutions into and out of the system set accordingly to achieve the steady state flow conditions.
In another embodiment, the electrolytic cell 100 is operated in batch mode. In batch mode, the anolyte solution and catholyte solution are fed initially into the cell and then the cell is operated until the desired concentration of product is produced in the anolyte and catholyte. The cell is then emptied, the products collected, and the cell refilled to start the process again. Alternatively, combinations of continuous mode and batch mode production may be used. Also, in either mode, the feeding of solutions may be done using a pre-prepared solution or using components that form the solution in situ.
It should be noted that both continuous and batch mode have dynamic flow of solutions. In one embodiment of continuous mode operation, the anolyte solution is added to the anolyte compartment so that the sodium concentration is maintained at a certain concentration or concentration range during operation of the electrolytic cell 100. In one embodiment of batch mode operation, a certain quantity of alkali ions are transferred through the alkali ion conductive membrane to the catholyte compartment and are not replenished, with the cell operation is stopped when the alkali ion concentration in the anolyte compartment reduces to a certain amount or when the appropriate product concentration is reached in the catholyte compartment.
As disclosed above, the anolyte solution 124 comprises a solvent 126, an alkali metal salt of an alkyl carboxylic acid 128, and an aryl compound 130. The aryl compound may take different forms, and the choice of aryl compound will determine the method for preparing the desired aryl-alkyl surfactant precursor. Method 1 applies where the aryl compound comprises an alkali metal salt of an aryl carboxylic acid. Method 2 applies where the aryl compound comprises an arene hydrocarbon. Method 3 applies where the aryl compound comprises an alkali metal-arene adduct (Ar−M+).
Method 1: The first step is conversion of the aryl carboxylic acid (ArCOOH) and the alkyl carboxylic acid (RCOOH) to alkali metal salts via an acid neutralization process using a base such as alkali methoxide (Reactions 4A and 4C) or alkali hydroxide (Reactions 4B and 4D).
RCOOH+CH3OM→RCOOM+CH3OH (4A)
RCOOH+MOH→RCOOM+H2O (4B)
ArCOOH+CH3OM→ArCOOM+CH3OH (4C)
ArCOOH+MOH→ArCOOM+H2O (4D)
Wherein M is an alkali metal such as lithium, sodium or potassium; RCOOH is a carboxylic acid and R is an alkyl hydrocarbon having a C8 to C24 hydrocarbon chain, Ar is an arene (also known as an aromatic or aryl)hydrocarbon. In some embodiments R is derived from a fatty acid. It is within the scope of the invention to obtain the alkyl carboxylate salts by saponification (alkaline hydrolysis) of certain fats and oils (triglycerides).
The RCOOM and ArCOOM are combined with a suitable solvent to prepare an anolyte solution. The anolyte solution may optionally include a supporting electrolyte which is soluble in the solvent and provides high electrolyte conductivity in the anolyte solution. The anolyte solution is fed into an electrochemical cell, such as cell 100 shown in
In this disclosed method, under the influence of electric potential, electrochemical (anodic) decarboxylation reactions take place at the anode resulting in the formation of carbon dioxide, alkyl radicals (R•), and aryl radicals (Ar•) according to Reactions 5 and 6, below.
R—COOM→R•+CO2+e−+M+ (5)
Ar—COOM→Ar•+CO2+e−+M+ (6)
The alkyl radicals react with the aryl radicals under conditions that permit aryl-alkyl carbon-carbon coupling, thereby forming the aryl-alkyl surfactant precursor, and optionally other reaction products. Non-limiting examples of the free radical reaction steps are shown below.
R•+Ar•→R—Ar (cross dimerization) (7)
R•+R•→R—R (alkyl hydrocarbon dimerization) (8)
Ar•+Ar•→Ar—Ar (arene dimerization) (9)
Note that the radical in the case of Ar• is a radical present on the aromatic carbon (i.e. associated with the aromatic ring). Alternatively radicals can also be formed on alkyl groups attached to the aromatic ring in which case different products than from above can be formed. For example, if the alkali salt of the alkyl caroxylic acid is Ar—CH2—COOM, non-limiting examples of possible free radical reactions are shown below:
Ar—CH2—COOM→Ar—CH2•+CO2+e−+M+ (10)
Ar—CH3+R•→Ar—CH2•+R—H (hydrogen abstraction) (11)
R•+Ar—CH2→R—Ar (cross dimerization) (12)
R•+R•→R—R (alkyl hydrocarbon dimerization) (8)
Ar—CH2•+Ar→Ar—CH2—Ar (arene dimerization) (13)
Ar•+Ar•→Ar—Ar (arene dimerization) (9)
The above decarboxylation and radical formation reactions are typically conducted in aqueous or non-aqueous solutions at high current densities. Once the R—Ar surfactant precursor is formed, the product may be recovered for further processing. For instance, the aromatic ring may be sulfonated, preferably at the para site, to form the surfactant product (R—Ar—HSO4).
Some advantages of this embodiment, using alkali metal salt of the alkyl carboxylic acid instead of carboxylic acid itself in the above mentioned two compartment electrolytic cell are:
1. R—COOM is more polar than R—COOH and so more probable to decarboxylate at lower voltages.
2. The electrolyte conductivity may be higher for alkali metal salts of fatty acids than fatty acids themselves.
3. The anolyte and catholyte solutions can be completely different allowing favorable reactions to take place at either electrode.
The alkali ion conductive solid electrolyte membrane selectively transfers alkali ions (M+) from the anolyte compartment to the catholyte compartment under the influence of an electrical potential while preventing anolyte solution and catholyte solution mixing.
Non-limiting examples of suitable the catholyte solutions include aqueous alkali hydroxide and non aqueous methanol/alkali methoxide solution. An electrochemically active cathode is housed in the catholyte compartment, where reduction reactions take place according to Reactions 1, 2, or 3. The base used in the acid neutralization reaction may be regenerated in the catholyte compartment.
Method 2: The first step is conversion of the alkyl carboxylic acid (RCOOH) to alkali metal salts via an acid neutralization process using a base such as alkali methoxide (Reaction 4A) or alkali hydroxide (Reaction 4B).
RCOOH+CH3OM→RCOOM+CH3OH (4A)
RCOOH+MOH→RCOOM+H2O (4B)
Wherein R and M are as defined above. The next step is to mix RCOOM and an arene hydrocarbon (Ar) with a suitable solvent to prepare an anolyte solution. The anolyte solution may optionally include a supporting electrolyte.
The anolyte solution is fed into an electrolytic cell as described in Method 1, where oxidation (decarboxylation) reaction and subsequent free radical carbon-carbon coupling takes place. The free radical reaction steps are shown below with the arene hydrocarbon being benzene as an example:
R—COOM→R•+CO2+e−+M+ (5)
The alkali ion (M+) transfers through the alkali ion conductive membrane from the anolyte compartment to the catholyte compartment. The alkyl radical (R•) reacts with the benzene (Ar) to form an intermediate according to Reaction (14). The alkyl radical can react with itself according to Reaction (8):
R•+C6H6→[R—C6H6•] intermediate (14)
R•+R•→R—R (alkyl hydrocarbon dimerization) (8)
The intermediate may undergo any of the following non-limiting reactions:
[R—C6H6•]+R•→R—C6H5+RH (hydrogen abstraction by the second R•) (15)
[R—C6H6•]+[R—C6H6•]→R—C6H5+R—C6H7 (disproportionation) (16)
[R—C6H6•]+[R—C6H6•]→2R—C6H6 (arene dimerization) (17)
In the case of C6H6• the radical is present on the aromatic carbon (i.e. associated with the aromatic ring). Alternatively radicals can also be formed on alkyl groups attached to the aromatic ring in which case different products can be formed, non-limiting examples of which are shown below:
C6H6—CH3+R•→C6H6—CH2•R—H (hydrogen abstraction by the second R•) (18)
R•+C6H6—CH2•→R—CH2—C6H6 (cross dimerization) (19)
R•+R•→R—R (alkyl hydrocarbon dimerization) (8)
C6H6—CH2•+C6H6•→C6H6—CH2—C6H6 (arene dimerization) (20)
C6H6—CH2•+C6H6—CH2•→C6H6—CH2—CH2—C6H6 (arene dimerization) (21)
Once the desired R—Ar surfactant precursor is formed, the product may be recovered for further processing. For instance, the aromatic ring may be sulfonated, preferably at the para site, to form the surfactant product (R—Ar—HSO4).
Method 3: The first step is conversion of the alkyl carboxylic acid (RCOOH) to alkali metal salts via an acid neutralization process using a base such as alkali methoxide (Reaction 4A) or alkali hydroxide (Reaction 4B).
RCOOH+CH3OM→RCOOM+CH3OH (4A)
RCOOH+MOH→RCOOM+H2O (4B)
Wherein R and M are as defined above. The next step is to mix an arene hydrocarbon with an equimolar amount of alkali metal to form an Ar−M+ adduct as described in the following reference: Donald E. Paul, David Lipkin, S. I. Weissman “Reaction of Sodium Metal with Aromatic Hydrocarbons” J. Am. Chem. Soc., 1956, 78 (1), pp 116-120.
The next step is to mix RCOOM and the Ar−M+ adduct to prepare an anolyte solution. The anolyte solution may optionally include a supporting electrolyte.
The anolyte solution is fed into an electrolytic cell as described in Method 1, where oxidation (decarboxylation) reaction and subsequent free radical carbon-carbon coupling takes place. The free radical reaction steps are shown below with the arene hydrocarbon being benzene as an example:
R—COOM→R•+CO2+e−+M+ (5)
The alkyl radical will lose an electron to form a carbocation (R+) as follows:
R•→R++e− (21)
Reaction (21) may occur at a high current density. In one embodiment reaction (21) occurs at a current density greater than about 100 mA/cm2 of anode area.
The carbocation (R+) then reacts with the alkali metal aryl Ar−M+ adduct to form the aryl-alkyl product as follows:
R++Ar−M+→R—Ar+M+ (22)
The alkali ion (M+) transfers through the alkali ion conductive membrane from the anolyte compartment to the catholyte compartment. Once the R—Ar surfactant precursor is formed, the product may be recovered for further processing. For instance, the aromatic ring may be sulfonated, preferably at the para site, to form the surfactant product (R—Ar—HSO4).
The decarboxylation and radical formation reactions as depicted above in relation to all three methods are believed to be stoichiometric. However, by changing the stoichiometric ratio of the reactants, it is possible to change the product compositions. For example, if excess of Ar—COOM is used in the above reaction, it is probable to increase the formation of Ar—Ar and R—Ar compared to R—R. Thus it is possible to tailor the process to maximize the desirable products and reduce the formation of undesirable products.
The product ratio may also be varied by changing the current density at which the decarboxylation takes place. As an example, it may be possible to vary the formation of one type of radicals predominantly compared to a different type (radicals of the type Ar—CH2• where the radical is associated with alkyl group associated with aromatic carbon compared to •Ar—CH2 where the radical is associated with the aromatic ring carbon) changing the product selection and composition.
The anolyte solution 212 comprises an anolyte solvent 216, an alkali metal salt of an alkyl carboxylic acid 218, and an aromatic or aryl compound 220. In some embodiments, the aromatic compound 220 may comprise an alkali metal salt of an aromatic carboxylic acid 222. In some embodiments, the aromatic compound may comprise an aromatic (arene) hydrocarbon 224. In some embodiments, the aromatic compound 220 may comprise an alkali metal-arene adduct (Ar−M+) 226. In some embodiments, the alkali metal salt of an alkyl carboxylic acid 218 may be obtained by saponification of an oil or fat triglyceride 228. In some embodiments the alkali metal salt of an alkyl carboxylic acid 218 may be obtained by acid neutralization 230 of an alkyl carboxylic acid, such as a fatty acid. In such cases, the alkyl carboxylic acid may comprise an alkyl hydrocarbon having a C8 to C24 hydrocarbon chain.
The catholyte solution 214 may comprise a solvent that is the same or different than the anolyte solvent. In one disclosed embodiment, the catholyte solution comprises methanol or water 232. Under the influence of an electric potential, the catholyte solution reacts to form a base 234 comprising an alkali methylate (methoxide) or an alkali hydroxide, depending upon the composition of the catholyte solution. The base 234 may be recovered and used to prepare the alkali salt of the alkyl carboxylic acid 218.
Under the influence of an electric potential, the anolyte solution undergoes electrochemical (anodic) decarboxylation reactions resulting in the formation of carbon dioxide 236 and alkyl radicals (R•). The alkyl radicals react with the aromatic compound 220 under conditions that permit aryl-alkyl carbon-carbon coupling, thereby forming aryl-alkyl hydrocarbons 238. Other hydrocarbon products may also be produced, including but not limited to, alkyl-alkyl and aryl-aryl hydrocarbons.
The following examples are given to illustrate various embodiments within the scope of the present invention. These are given by way of example only, and it is understood that the following examples are not comprehensive or exhaustive of the many types of embodiments of the present invention that can be prepared in accordance with the present invention.
Several experiments were performed to demonstrate technical feasibility of the electrolytic decarboxylation process (EDP) described herein for manufacturing aryl-alkyl precursors from inexpensive starting materials and to perform the synthesis reaction at low temperature and low pressure without the use of catalysts. The experiments demonstrated the decarboxylation of sodium salts of aromatic and aliphatic carboxylic acids in electrolytic cells utilizing a NaSelect® NaSICON membrane manufactured by Ceramatec, Inc., Salt Lake City, Utah, to make mixed aromatic-aliphatic hydrocarbon products.
A mixture comprising an aryl carboxylic acid salt and an alkyl carboxylic acid salt was converted to an aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of both the aryl carboxylate and the alkyl carboxylate and subsequent aryl-alkyl carbon-carbon coupling. An equimolar mixture of sodium benzoate and sodium acetate was dissolved in a solvent comprising 20% water and 80% methanol to form an anolyte solution.
Approximately 300 mL of the anolyte solution was introduced into a two-compartment micro electrolysis reactor with minimal membrane-anode gap. The anolyte solution flow rate ranged from 60-100 ml/min. The electrolysis reactor contained a 1 mm thick NaSelect® NaSICON membrane having a 1 inch diameter. A smooth platinum anode and a nickel cathode were used in the electrolysis reactor. A 15 wt. % NaOH catholyte solution was used in the catholyte compartment. The electrolysis reactor was operated at a current density of 200-300 mA per cm2 of membrane area. The operating temperature was approximately 40° C.
The electrolysis reactor was operated in batch mode, i.e. the anolyte and catholyte solutions are re-circulated until ˜40-50% of the sodium salts are converted to hydrocarbons in the anolyte compartment and form sodium hydroxide in the catholyte compartment.
It is within the scope of the invention to operate the electrolysis reactor in a semi-continuous mode, i.e. the anolyte and catholyte solutions are re-circulated until a pre-determined amount of sodium salt starting material (e.g. 10%) is converted to hydrocarbons in the anolyte compartment. A continuous process is preferred for processing hydrocarbons at large scale in which the starting salt concentration is always maintained and the hydrocarbon product is continuously removed.
The electrolytic decarboxylation reactions are shown below:
CH3COONa→CH3•+CO2+e−+Na+
C6H5COONa→C6H5•+CO2+e−+Na+
The evolved carbon dioxide was detected using an IR sensor and by lime-water analysis.
CH3•+C6H5•→C6H5—CH3 (cross dimerization)
CH3•+CH3•→CH3—CH3 (alkyl hydrocarbon dimerization)
C6H5•+C6H5•→C6H5—C6H5 (arene dimerization)
The reaction products were extracted with dodecane. The reaction products were analyzed by gas chromatography (GC). The following products were observed:
Benzene: 70 mg/kg
Ethyl benzene: 270 mg/kg
Toluene: <50 mg/kg
Other peaks in the GC pattern were left unidentified. The formation of ethyl benzene was not expected. Without being bound by theory, the ethyl benzene may have formed from toluene by the following mechanism:
A mixture comprising an alkyl carboxylic acid salt and an arene hydrocarbon (benzene in this example) was converted to an aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of the alkyl carboxylate and subsequent aryl-alkyl carbon-carbon coupling. An equimolar mixture of benzene and sodium acetate was dissolved in methanol to form an anolyte solution.
The anolyte solution was introduced into a two-compartment micro electrolysis reactor and operated as described in Example 1. The electrolytic decarboxylation reaction is shown below:
CH3COONa→CH3•+CO2+e−+Na+
The evolved carbon dioxide was detected using an IR sensor and by lime-water analysis.
[CH3—C6H6•]+CH3•→CH3—C6H5+CH4 (hydrogen abstraction by CH3•)
[CH3—C6H6•]+[CH3—C6H6•]→CH3—C6H5+CH3—C6H7 (disproportionation)
[CH3—C6H6•]+[CH3—C6H6•]→2CH3—C6H6 (arene dimerization)
The reaction products were extracted with non polar extractants such as dodecane. The reaction products were analyzed by gas chromatography (GC). The following products were observed:
Ethyl benzene: 250 mg/kg
Methyl acetate: 220 mg/kg
Toluene: 150 mg/kg
Toluene was produced, proving aryl-alkyl coupling. Without being bound by theory, it is believe the ethyl benzene was formed from toluene as described in Example 1. The methyl acetate was formed by reaction of methanol and sodium acetate. Other peaks in the GC pattern were left unidentified.
A mixture comprising an alkyl carboxylic acid salt and an arene hydrocarbon (ethyl benzene in this example) was converted to an aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of the alkyl carboxylate and subsequent aryl-alkyl carbon-carbon coupling. An equimolar mixture of ethyl benzene and sodium propionate was dissolved in methanol to form an anolyte solution.
The anolyte solution was introduced into a two-compartment micro electrolysis reactor and operated as described in Example 1. The electrolytic decarboxylation reaction is shown below:
CH3CH2COONa→C2H5•+CO2+e−+Na+
The evolved carbon dioxide was detected using an IR sensor and by lime-water analysis.
[(C2H5)2—C6H6•]+C2H5•→(C2H5)2—C6H5+C2H6 (hydrogen abstraction by C2H5•)
[(C2H5)2—C6H6•]+[(C2H5)2—C6H6•]→(C2H5)2—C6H5+(C2H5)2—C6H7 (disproportionation)
[(C2H5)2—C6H6•]+[(C2H5)2—C6H6•]→2C2H5—C6H5+H2 (arene dimerization)
The reaction products were extracted with non polar extractants such as dodecane. The reaction products were analyzed by gas chromatography (GC). The following products were observed:
Butane: 120 mg/kg
1,2-diethylbenzene: 438 mg/kg
1,2,3-Trimethylbenzene: 120 mg/kg
Benzene: 360 mg/kg
Sec-butylbenzene: 57 mg/kg
Toluene: 190 mg/kg
Diethyl benzene was produced, proving aryl-alkyl coupling. 1,2,3-trimethyl benzene, benzene, sec-butylbenzene, toluene were also formed. Without being bound by theory, it is believed these products were formed due to complex rearrangements and bond cleavages. Other peaks in the GC pattern were left unidentified.
A mixture comprising an alkyl carboxylic acid salt and an arene hydrocarbon (methyl naphthalene in this example) was converted to an aryl-alkyl hydrocarbon by electrolytic (anodic) decarboxylation of the alkyl carboxylate and subsequent aryl-alkyl carbon-carbon coupling. An equimolar mixture of methyl naphthalene and sodium acetate was dissolved in methanol to form an anolyte solution.
The anolyte solution was introduced into a two-compartment micro electrolysis reactor and operated as described in Example 1. The electrolytic decarboxylation reaction is shown below:
CH3COONa→CH3•+CO2+e−+Na+
The evolved carbon dioxide was detected using an IR sensor and by lime-water analysis.
[(CH3)2—C10H7•]+CH3•→(CH3)2—C10H6+CH4 (hydrogen abstraction by CH3•)
[(CH3)2—C10H7•]+[(CH3)2—C10H7•]→(CH3)2—C10H6+(CH3)2—C10H8 (disproportionation)
[(CH3)2—C10H7•]+[(CH3)2—C10H7•]→2(CH3)2—C10H6+H2 (arene dimerization)
The reaction products were extracted with non polar extractants such as dodecane. The reaction products were analyzed by gas chromatography (GC). The following products were observed:
C11-C13 alkyl naphthalenes: 170 g/kg
2-benzylidenecyclopentanone: 261 mg/kg
2-methyl-1-naphthalenol: 5.4 g/kg
Many other peaks in the GC pattern were left unidentified.
While specific embodiments and examples of the present invention have been illustrated and described, numerous modifications come to mind without significantly departing from the spirit of the invention, and the scope of protection is only limited by the scope of the accompanying claims.
This application claims the benefit of U.S. Provisional Application No. 61/327,477, filed Apr. 23, 2010 and U.S. Provisional Application No. 61/353,724, filed Jun. 11, 2010. This application is a continuation-in-part of U.S. application Ser. No. 12/840,401, filed Jul. 21, 2010, which application claims the benefit of U.S. Provisional Application No. 61/228,078, filed Jul. 23, 2009, U.S. Provisional Application No. 61/258,557, filed Nov. 5, 2009, and U.S. Provisional Application No. 61/260,961, filed on Nov. 13, 2009. These non-provisional and provisional patent applications are expressly incorporated herein by reference.
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| Number | Date | Country | |
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| 20110226633 A1 | Sep 2011 | US |
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| 61353724 | Jun 2010 | US | |
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| Number | Date | Country | |
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| Parent | 12840401 | Jul 2010 | US |
| Child | 13092685 | US |
