JP2017075398A - Electrochemical hydroxide systems and methods using metal oxidation - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide methods and systems for an electrochemical cell including an anode and a cathode, where the anode is contacted with a metal ion so as to convert the metal ion from a lower oxidation state to a higher oxidation state.SOLUTION: The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon so as to form products. A method of present invention further includes re-circulating an aqueous medium containing the metal ion in the lower oxidation state back to the anode electrolyte.SELECTED DRAWING: None

Description

CROSS REFERENCE TO RELATED APPLICATIONS This application is a continuation-in-part of U.S. Patent Application No. 13 / 474,598, filed May 17, 2012, which is incorporated herein by reference. US Provisional Patent Application No. 61 / 488,079, filed May 19, 2011, US Provisional Patent Application No. 61 / 499,499, filed June 21, 2011, August 5, 2011 US Provisional Patent Application No. 61 / 515,474 filed on the same day, US Provisional Patent Application No. 61 / 546,461 filed on October 12, 2011, US application filed on October 28, 2011 Provisional Patent Application No. 61 / 552,701, U.S. Provisional Patent Application No. 61 / 597,404 filed on Feb. 10, 2012, and U.S. Provisional Patent Application No. 61 filed on Mar. 29, 2012. / 617, Claim priority to 390. In the present disclosure, all of these are hereby incorporated by reference in their entirety.

Background In many chemical processes, caustic soda is necessary to achieve a chemical reaction, for example, to neutralize the acid, buffer the pH of the solution, or precipitate insoluble hydroxides from the solution. obtain. One method that can produce caustic soda is by an electrochemical system. Large amounts of energy, salt, and water may be used in the electrochemical production of caustic soda, such as by a chloroalkali process.

  Polyvinyl chloride, commonly known as PVC, can be the third most widely produced plastic after polyethylene and polypropylene. PVC is widely used in construction because it is durable, inexpensive and easily processed. PVC can be made by polymerization of vinyl chloride monomer, which can be made from ethylene dichloride. Ethylene dichloride can be made by direct chlorination of ethylene using chlorine gas made from a chloroalkali process.

  The production of chlorine and caustic soda by electrolysis of an aqueous solution of sodium chloride or brine is one of the electrochemical processes that require high energy consumption. The total energy requirement to maintain this process by the chloroalkali industry is, for example, about 2% of the total power generated in the United States and about 1% in Japan. High energy consumption may be associated with high carbon dioxide emissions from fossil fuel combustion. Therefore, it is necessary to cope with a reduction in power demand in order to suppress environmental pollution and global warming.

In one aspect, contacting an anode and an anode electrolyte, the anode electrolyte comprising metal ions, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode Contacting the cathode electrolyte with a cathode electrolyte, and reacting an unsaturated hydrocarbon or saturated hydrocarbon with the anode electrolyte containing the higher oxidation state metal ion in the aqueous medium to halogenate in the aqueous medium. Forming one or more organic compounds comprising a hydrocarbon and the lower oxidation state metal ions, and separating the one or more organic compounds from the aqueous medium comprising the lower oxidation state metal ions Providing a method.

  In some embodiments of the above aspects, the method further comprises forming alkali, water or hydrogen gas at the cathode. In some embodiments of the above aspects, the method further comprises forming alkali at the cathode. In some embodiments of the above aspects, the method further comprises forming hydrogen gas at the cathode. In some embodiments of the above aspects, the method further comprises forming water at the cathode. In some embodiments of the above aspects, the cathode is an oxygen depolarized cathode that reduces oxygen and water to hydroxide ions. In some embodiments of the above aspects, the cathode is a hydrogen gas generating cathode that reduces water to hydrogen gas and hydroxide ions. In some embodiments of the above aspects, the cathode is a hydrogen gas generating cathode that reduces hydrochloric acid to hydrogen gas. In some embodiments of the above aspects, the cathode is an oxygen depolarized cathode that reacts with hydrochloric acid and oxygen gas to form water.

  In some embodiments of the above aspects and embodiments, the method further comprises recycling an aqueous medium comprising lower oxidation state metal ions back to the anode electrolyte. In some embodiments of the above aspects and embodiments, the aqueous medium recycled back to the anode electrolyte contains less than 100 ppm, or less than 50 ppm, or less than 10 ppm, or less than 1 ppm organic compound (s). Including.

  In some embodiments of the above aspects and embodiments, the aqueous medium comprises between 5 and 95 wt% water, or between 5 and 90 wt% water, or between 5 and 99 wt% water. Including.

In some embodiments of the above aspects and embodiments, the metal ions include, but are not limited to, iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium. , Osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, metal ions include, but are not limited to, iron, chromium, copper, and tin. In some embodiments, the metal ion is copper. In some embodiments, the lower oxidation state of the metal ion is 1+, 2+, 3+, 4+, or 5+. In some embodiments, the higher oxidation state of the metal ion is 2+, 3+, 4+, 5+, or 6+. In some embodiments, the metal ion is copper that is converted from Cu ⁺ to Cu ²⁺ , the metal ion is iron that is converted from Fe ²⁺ to Fe ³⁺ , and the metal ion is from Sn ^2+. Tin that is converted to Sn ⁴⁺ , the metal ion is chromium that is converted from Cr ²⁺ to Cr ³⁺ , the metal ion is platinum that is converted from Pt ²⁺ to Pt ⁴⁺ , or these It is a combination.

  In some embodiments of the above aspects and embodiments, no gas is used or formed at the anode.

  In some embodiments of the above aspects and embodiments, the method further comprises adding a ligand to the anode electrolyte, wherein the ligand interacts with a metal ion.

  In some embodiments of the above aspects and embodiments, the method comprises reacting an anode electrolyte comprising a higher oxidation state metal ion and a ligand with an unsaturated hydrocarbon or saturated hydrocarbon. Further comprising a step in an aqueous medium.

  In some embodiments of the above aspects and embodiments, the reaction of the anode electrolyte comprising a higher oxidation state metal ion with an unsaturated hydrocarbon or saturated hydrocarbon comprises a higher oxidation state metal halide or metal. Sulfates (which lead to halohydrocarbons or sulfohydrocarbons, respectively) and halogenation or sulfonation using lower oxidation state metal halides or metal sulfates. In some embodiments, the lower oxidation state metal halide or metal sulfate is recycled back to the anode electrolyte.

  In some embodiments of the above aspects and embodiments, the anode electrolyte comprising a higher oxidation state metal ion further comprises a lower oxidation state metal ion.

In some embodiments of the above aspects and embodiments, the unsaturated hydrocarbon is a compound of formula I that provides a compound of formula II after halogenation;

In the formula, n is 2 to 10, m is 0 to 5, q is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), R ′ and R ″ are independently selected from hydrogen, alkyl, and substituted alkyl;
X is a halogen selected from chloro, bromo, and iodo.

  In some embodiments, m is 0, n is 2, q is 2, and X is chloro. In some embodiments, the compound of formula I is ethylene, propylene, or butylene, respectively, and the compound of formula II is ethylene dichloride, propylene dichloride, or 1,4-dichlorobutane. In some embodiments, the method further comprises forming a vinyl chloride monomer from ethylene dichloride and forming poly (vinyl chloride) from the vinyl chloride monomer.

In some embodiments of the above aspects and embodiments, the saturated hydrocarbon is a compound of formula III that results in a compound of formula IV after halogenation;

In the formula, n is 2 to 10, k is 0 to 5, s is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), R ′ and R ″ are independently selected from hydrogen, alkyl, and substituted alkyl;
X is a halogen selected from chloro, bromo, and iodo.

  In some embodiments, the compound of formula III is methane, ethane, or propane.

  In some embodiments of the above aspects and embodiments, the one or more organic compounds further comprises chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, or a combination thereof.

  In some embodiments of the above aspects and embodiments, separating the one or more organic compounds from the aqueous medium containing the lower oxidation state metal ions includes using an adsorbent.

  In some embodiments of the above aspects and embodiments, the adsorbent is selected from activated carbon, alumina, activated silica, polymers, and combinations thereof. In some embodiments of the above aspects and embodiments, the adsorbent is polyethylene, polypropylene, polystyrene, polymethylpentene, polybutene-1, polyolefin elastomer, polyisobutylene, ethylene propylene rubber, polymethyl acrylate, poly (methyl methacrylate). ), Poly (isobutylmethacrylate), and combinations thereof. In some embodiments of the above aspects and embodiments, the adsorbent is activated carbon. In some embodiments of the above aspects and embodiments, the adsorbent is polystyrene.

  In some embodiments of the above aspects and embodiments, the adsorbent adsorbs greater than 95% w / w organic compound.

  In some embodiments of the above aspects and embodiments, the method includes purging with an inert fluid, changing chemical conditions, increasing temperature, decreasing partial pressure, decreasing concentration, inert gas or steam. The method further includes regenerating the adsorbent using a technique selected from purging and combinations thereof. In some embodiments of the above aspects and embodiments, the method further comprises regenerating the adsorbent by purging with an inert fluid. In some embodiments of the above aspects and embodiments, the method further comprises regenerating the adsorbent by purging with an inert gas or vapor at an elevated temperature.

  In some embodiments of the above aspects and embodiments, the method further comprises the step of providing turbulence in the anode electrolyte to improve mass transfer at the anode. Methods for providing turbulence are described herein.

  In some embodiments of the above aspects and embodiments, the method further comprises contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with the anode electrolyte. This diffusion enhanced anode (eg, but not limited to a porous anode) is described herein.

  In one aspect, an anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize metal ions from a lower oxidation state to a higher oxidation state, and in contact with the cathode electrolyte. An anode electrolyte operably connected to the anode chamber and containing the higher oxidation state metal ions in an aqueous medium and reacted with an unsaturated hydrocarbon or a saturated hydrocarbon to form an aqueous solution. A reactor configured to form one or more organic compounds, including halogenated hydrocarbons, and metal ions of a lower oxidation state in the medium; and operably connected to the reactor and the anode And is configured to separate one or more organic compounds from an aqueous medium containing metal ions in the lower oxidation state Providing a system including a Pareta.

  In some embodiments of the above aspects and embodiments, the separator further includes a recirculation system operably connected to the anode to recycle the aqueous medium containing lower oxidation state metal ions to the anode electrolyte. .

  In some embodiments of the above aspects and embodiments, the anode is a diffusion enhanced anode, such as but not limited to a porous anode. The porous anode may be flat or corrugated, as described herein.

  In some embodiments of the above aspects and embodiments, the separator comprises an adsorbent selected from activated carbon, alumina, activated silica, polymers, and combinations thereof.

  In some embodiments of the above aspects and embodiments, the system further comprises a ligand in the anode electrolyte, wherein the ligand is configured to interact with the metal ion.

  In some embodiments of the above system aspects and embodiments, the cathode is a gas diffusion cathode configured to react oxygen gas with water to form hydroxide ions. In some embodiments of the above system aspects and embodiments, the cathode is a hydrogen gas generating cathode configured to form hydrogen gas and hydroxide ions by reducing water. In some embodiments of the above system aspects and embodiments, the cathode is a hydrogen gas generating cathode configured to reduce an acid, such as hydrochloric acid, to hydrogen gas. In some embodiments of the system aspects and embodiments described above, the cathode is a gas diffusion cathode configured to react hydrochloric acid and oxygen to form water.

  In some embodiments of the above system aspects and embodiments, the anode is configured not to form a gas.

  In some embodiments of the above aspects and embodiments, the system is configured to contact a cathode electrolyte and a divalent cation to form a carbonate and / or bicarbonate product. Further included.

  In some embodiments of the above aspects and embodiments, the metal ion is copper. In some embodiments of the above aspects and embodiments, the unsaturated hydrocarbon is ethylene. In some embodiments of the above aspects and embodiments, the one or more organic compounds are selected from ethylene dichloride, chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, and combinations thereof.

  In some embodiments of the above aspects and embodiments, the separator is one or more of a packed bed column comprising polystyrene.

In some embodiments, the treatment of the higher oxidation state metal ions with the unsaturated hydrocarbon is inside the anode chamber. In some embodiments, the treatment of the higher oxidation state metal ions with the unsaturated hydrocarbon is outside the anode chamber. In some embodiments, treatment of higher oxidation state metal ions with unsaturated hydrocarbons results in chlorohydrocarbons. In some embodiments, the chlorohydrocarbon is ethylene dichloride. In some embodiments, the method further comprises treating Cu ²⁺ ions with ethylene to form ethylene dichloride. In some embodiments, the method further comprises the step of treating ethylene dichloride to form vinyl chloride monomer. In some embodiments, the method further comprises treating the vinyl chloride monomer to form polychlorinated (vinyl).
In a preferred embodiment of the present invention, for example, the following items are provided.
(Item 1)
Contacting an anode with an anode electrolyte, the anode electrolyte comprising metal ions;
Oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
One or more comprising a halogenated hydrocarbon in the aqueous medium by reacting an unsaturated hydrocarbon or saturated hydrocarbon in the aqueous medium with the anode electrolyte comprising the metal ions in the higher oxidation state. Forming said organic compound and said lower oxidation state metal ion;
Separating the one or more organic compounds from the aqueous medium comprising the lower oxidation state metal ions.
(Item 2)
The method of claim 1, further comprising recycling the aqueous medium comprising the lower oxidation state metal ions back to the anode electrolyte.
(Item 3)
Item 3. The method according to item 1 or 2, wherein the aqueous medium comprises between 5 and 95% by weight of water.
(Item 4)
The method according to any one of the preceding items, further comprising forming alkali, water or hydrogen gas at the cathode.
(Item 5)
The metal ions are iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium. A method according to any one of the preceding items selected from the group consisting of manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof.
(Item 6)
The method according to any one of the preceding items, wherein the metal ions are selected from the group consisting of iron, chromium, copper, and tin.
(Item 7)
Whether the metal ion is copper that is converted from Cu ⁺ to Cu ²⁺ , the metal ion is iron that is converted from Fe ²⁺ to Fe ³⁺ , or the metal ion is Sn ²⁺ to Sn ⁴⁺ Whether the metal ions are tin that is converted from Cr ²⁺ to Cr ³⁺ , or the metal ions are platinum that is converted from Pt ²⁺ to Pt ⁴⁺ , Or a method according to any one of the preceding items, which is a combination thereof.
(Item 8)
The unsaturated hydrocarbon is a compound of formula I resulting in a compound of formula II after halogenation;

In the formula, n is 2 to 10, m is 0 to 5, q is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), where R ′ and R ″ are independently from hydrogen, alkyl, and substituted alkyl. Selected
X is a halogen selected from chloro, bromo, and iodo,
A method according to any one of the preceding items.
(Item 9)
Item 9. The method according to Item 8, wherein the compound of the formula I is ethylene, propylene, or butylene, and the compound of the formula II is ethylene dichloride, propylene dichloride, or 1,4-dichlorobutane, respectively.
(Item 10)
The method of any one of the preceding items, wherein the one or more organic compounds further comprises chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, or a combination thereof.
(Item 11)
The method of any one of the preceding items, wherein the step of separating the one or more organic compounds from the aqueous medium comprising the lower oxidation state metal ions comprises using an adsorbent. Method.
(Item 12)
Item 12. The method of item 11, wherein the adsorbent is selected from activated carbon, alumina, activated silica, polymer, and combinations thereof.
(Item 13)
The adsorbent is from polyethylene, polypropylene, polystyrene, polymethylpentene, polybutene-1, polyolefin elastomer, polyisobutylene, ethylene propylene rubber, polymethyl acrylate, poly (methyl methacrylate), poly (isobutyl methacrylate), and combinations thereof. 13. The method according to item 11 or 12, which is a selected polyolefin.
(Item 14)
14. The method according to any one of items 11 to 13, wherein the adsorbent is polystyrene. (Item 15)
15. A method according to any one of items 11 to 14, wherein the adsorbent adsorbs more than 95% w / w organic compound.
(Item 16)
The adsorbent using a technique selected from purging with an inert fluid, changing chemical conditions, increasing temperature, decreasing partial pressure, decreasing concentration, purging with an inert gas or vapor, and combinations thereof 16. The method according to any one of items 11 to 15, further comprising the step of regenerating.
(Item 17)
The method of any preceding item, further comprising providing turbulence in the anode electrolyte to improve mass transfer at the anode.
(Item 18)
The method of any one of the preceding items, further comprising contacting a diffusion enhanced anode with the anode electrolyte.
(Item 19)
An anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize the metal ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
Reacting the anode electrolyte containing the metal ions in the higher oxidation state with an unsaturated hydrocarbon or saturated hydrocarbon in an aqueous medium operatively connected to the anode chamber and in the aqueous medium. A reactor configured to form one or more organic compounds comprising a halogenated hydrocarbon and the lower oxidation state metal ions;
A separator operatively connected to the reactor and the anode and configured to separate the one or more organic compounds from the aqueous medium comprising the lower oxidation state metal ions; Including system.
(Item 20)
20. The system of item 19, wherein the separator further comprises a recirculation system that is operably connected to the anode and recirculates the aqueous medium containing the lower oxidation state metal ions to the anode electrolyte.
(Item 21)
21. A system according to item 19 or 20, wherein the anode is a diffusion enhanced anode.
(Item 22)
22. The system according to any one of items 19 to 21, wherein the separator comprises an adsorbent selected from activated carbon, alumina, activated silica, polymer, and combinations thereof.
(Item 23)
23. A system according to any one of items 19 to 22, wherein the metal ion is copper.
(Item 24)
24. Any one of items 19 to 23, wherein the unsaturated hydrocarbon is ethylene and the one or more organic compounds are selected from ethylene dichloride, chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, and combinations thereof. The system described in.
(Item 25)
25. A system according to any one of items 19 to 24, wherein the separator is one or more of a packed bed column comprising polystyrene.

  The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention may be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings of which:

FIG. 1A is a diagram illustrating an embodiment of the present invention.

FIG. 1B is a diagram illustrating an embodiment of the present invention.

FIG. 2 is a diagram illustrating an embodiment of the present invention.

3A and 3B are diagrams illustrating an embodiment of the present invention.

FIG. 4A is a diagram illustrating an embodiment of the present invention.

FIG. 4B is a diagram illustrating an embodiment of the present invention.

FIG. 5A is a diagram illustrating an embodiment of the present invention.

FIG. 5B is a diagram illustrating an embodiment of the present invention.

FIG. 5C is a diagram illustrating an embodiment of the present invention.

FIG. 6 is a diagram illustrating an embodiment of the present invention.

FIG. 7A is a diagram illustrating an embodiment of the present invention.

FIG. 7B is a diagram illustrating an embodiment of the present invention.

FIG. 7C is a diagram illustrating an embodiment of the present invention.

FIG. 8A is a diagram illustrating an embodiment of the present invention.

FIG. 8B is a diagram illustrating an embodiment of the present invention.

FIG. 8C is a diagram illustrating an embodiment of the present invention.

FIG. 9 is a diagram illustrating an embodiment of the present invention.

FIG. 10A is a diagram illustrating an embodiment of the present invention.

FIG. 10B is a diagram illustrating an embodiment of the present invention.

FIG. 11 is a diagram illustrating an embodiment of the present invention.

FIG. 12 is a diagram illustrating an embodiment of the present invention.

FIG. 13 is a diagram illustrating an embodiment of the present invention.

FIG. 14 is an exemplary graph described in Example 2 herein.

FIG. 15 is an exemplary graph described in Example 3 herein.

FIG. 16 is a diagram illustrating some illustrative examples of diffusion enhanced anodes (eg, but not limited to porous anodes) as described herein.

FIG. 17 is an exemplary graph for different adsorbents described in Example 5 herein.

FIG. 18 is an exemplary graph for adsorption and regeneration as described in Example 5 herein.

FIG. 19 is an exemplary dynamic adsorption column described in Example 5 herein.

FIG. 20 is an exemplary graph described in Example 5 herein.

DETAILED DESCRIPTION Disclosed herein are systems and methods related to the oxidation of metal ions by an anode in an anode chamber, wherein the metal ions are oxidized from a lower oxidation state to a higher oxidation state.

  As one skilled in the art can appreciate, the electrochemical systems and methods are alternative equivalent salt solutions such as potassium chloride solution or sodium chloride solution or magnesium chloride solution or sodium sulfate solution or With the ammonium chloride solution, an equivalent alkaline solution in the cathode electrolyte, such as potassium hydroxide and / or potassium carbonate and / or potassium bicarbonate, or sodium hydroxide and / or sodium carbonate and / or sodium bicarbonate, or hydroxide It can be configured to produce magnesium and / or magnesium carbonate. Accordingly, as long as such equivalents are based on or suggested by the present systems and methods, these equivalents are within the scope of the application.

  Before describing the present invention in more detail, it is to be understood that the invention is not limited to the specific embodiments described (since these can, of course, vary). The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting, since the scope of the present invention is limited only by the appended claims. Should also be understood.

  Where a range of values is provided, each value between the upper and lower limits of the range (up to one-tenth of the lower limit unit, unless the context clearly indicates otherwise) It is understood that any other stated value within that stated range or values therebetween are encompassed within the invention. The upper and lower limits of these smaller ranges may independently be included within that smaller range and are also encompassed within the invention (including any specifically excluded limits within the stated ranges). Suppose). Where the stated range includes one or both of the limits, ranges excluding either or both of those included limits are also included in the invention.

  Certain ranges presented herein with numbers may be interpreted as “about” numbers. “About” provides literal support for the exact number preceded by about, and for numbers that are close to or approximately the number that the term is preceded. In determining whether a number is close to or approximately that of a specifically stated number, a near or approximate requested number is specific in the context in which it is presented. It may be a number that provides a substantially equivalent number to the stated number.

  Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although any methods and materials similar or equivalent to those described herein can also be used in the practice or testing of the present invention, representative exemplary methods and materials are now described.

  All publications and patents cited herein are hereby incorporated by reference as if each individual publication or patent was specifically and individually indicated to be incorporated by reference. Incorporated herein by reference for the purpose of disclosing and describing methods and / or materials (public materials cited in connection with these methods and / or materials). . The citation of any published material is for its disclosure prior to the filing date and should not be construed as an admission that the present invention is not eligible to precede such published material based on the prior invention. Further, the dates of publications provided may be different from the actual publication dates that may need to be individually verified.

  As used herein and in the appended claims, the singular forms “a”, “an”, and “the” refer to the plural unless the context clearly dictates otherwise. Note that it includes. It should also be noted that the claims may be drafted to exclude any optional element. Accordingly, this description is intended to serve as a preliminary basis for the use of exclusive terms such as “alone”, “only”, or the use of “reactive” restrictions in connection with the description of claim elements. .

  As will be apparent to those skilled in the art upon reading this disclosure, each of the individual embodiments described and illustrated herein is capable of several other implementations without departing from the scope or spirit of the invention. It has individual components and features that may be easily separated from, or combined with, any feature of the form. Any recited method can be carried out in the order of events recited or in any other order which is logically possible.

Compositions, Methods, and Systems In one aspect, methods and systems are provided for the oxidation of metal ions from a lower oxidation state to a higher oxidation state in an anode chamber of an electrochemical cell. Metal ions formed with higher oxidation states may be used as such or used for commercial purposes such as, but not limited to, chemical synthesis reactions, reduction reactions. In one aspect, the electrochemical cells described herein provide a system that is efficient and low voltage where a metal compound, such as a metal halide, having a higher oxidation state produced by the anode. For example, metal chloride or metal sulfate, but is not limited to the generation of hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid, or sulfuric acid from hydrogen gas, And / or other purposes such as the generation of halohydrocarbons or sulfohydrocarbons from hydrocarbons.

  “Halohydrocarbon” or “halogenated hydrocarbon”, as used herein, includes halo-substituted hydrocarbons, where halo is any that can be attached to a hydrocarbon based on the valence allowed. Any number of halogens may be used. Halogen includes fluoro, chloro, bromo, and iodo. Examples of halohydrocarbons include chlorohydrocarbons, bromohydrocarbons, and iodohydrocarbons. Chloro hydrocarbons include, but are not limited to, monochloro hydrocarbons, dichloro hydrocarbons, trichloro hydrocarbons, and the like. For metal halides such as, but not limited to, metal bromide and metal iodide, the metal bromide or metal iodide having a higher oxidation state produced by the anode chamber includes, but is not limited to, hydrogen bromide or iodide. Generation of hydrides and / or other such as, but not limited to, generation of bromo or iodo hydrocarbons such as monobromo hydrocarbons, dibromo hydrocarbons, tribromo hydrocarbons, monoiodo hydrocarbons, diiodo hydrocarbons, triiodo hydrocarbons Can be used for purposes. In some embodiments, higher oxidation state metal ions may be sold as such in a commercial market.

“Sulfohydrocarbon” as used herein includes hydrocarbons substituted with one or more of —SO ₃ H or —OSO ₂ OH, based on the allowed valence.

  The electrochemical cell of the present invention may be any electrochemical cell in which lower oxidation state metal ions are converted to higher oxidation state metal ions in the anode chamber. In such an electrochemical cell, the cathode reaction may be any reaction that forms or does not form alkali in the cathode chamber. Such a cathode consumes electrons and includes, but is not limited to, a reaction of water that forms hydroxide ions and hydrogen gas, or a reaction of oxygen gas and water that forms hydroxide ions, or hydrogen gas. Any reaction is carried out, including the reduction of protons from acids forming, for example hydrochloric acid, or the reaction of protons and oxygen gas from hydrochloric acid forming water.

  In some embodiments, an electrochemical cell can include the production of alkali in the cathode chamber of the cell. The alkali generated in the cathode chamber may be used as is for commercial purposes or may be treated with a divalent cation to form a divalent cation-containing carbonate / bicarbonate. In some embodiments, alkali generated in the cathode chamber may be used to capture or capture carbon dioxide. Carbon dioxide can be present in the flue gas emitted by various industrial plants. Carbon dioxide can be captured in the form of carbonate and / or bicarbonate products. In some embodiments, a metal compound having a higher oxidation state metal may be removed from the anode chamber and used for any commercial process known to those skilled in the art. Thus, both anode and cathode electrolytes can be used to generate products that can be used for commercial purposes, thereby providing a more economical, efficient and less energy intensive process.

  In some embodiments, the metal compound produced by the anode chamber is hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, or hydroiodic acid, sulfuric acid, and / or halohydrocarbon or For the generation of sulfohydrocarbons, they may be used as is or purified before reacting with hydrogen gas, unsaturated hydrocarbons, or saturated hydrocarbons, respectively. In some embodiments, the metal compound may be used in-situ where hydrogen gas is generated, and / or in some embodiments, the metal compound removed from the anode chamber generates hydrogen gas and hydrogen The gas may be moved to a location where hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, or hydroiodic acid is formed. In some embodiments, the metal compound may be used in the field where an unsaturated hydrocarbon such as, but not limited to, ethylene gas is generated or moved in an electrochemical system and In some embodiments, the metal compound removed from the anode chamber may be moved to a location where unsaturated hydrocarbons such as, but not limited to, ethylene gas are generated or moved, such as halohydrocarbons. For example, chlorohydrocarbons are formed therefrom. In some embodiments, an ethylene gas generation facility is integrated with the electrochemical system of the present invention to simultaneously produce a higher oxidation state metal compound and ethylene gas, treat them together, and produce a product, for example, Form ethylene dichloride (EDC). Ethylene dichloride may also be 1,2-dichloroethane, dichloroethane, 1,2-ethylene dichloride, glycol dichloride, freon 150, borer sol, brocide, destruxol borer-sol, dichlor-mulsion, Dutch oil, or granosan Can be known as In some embodiments, the electrochemical system of the present invention is a vinyl chloride monomer (VCM) production facility, or an EDC formed by the systems and methods of the present invention is used in VCM and / or PVC production. Integrated with polyvinyl chloride (PVC) production facility.

  The electrochemical systems and methods described herein do not require, but are not limited to, a gas diffusion anode; higher cell efficiency; lower voltage; platinum-free anode; carbon dioxide capture; One or more advantages over conventional electrochemical systems known in the art, including the formation of environmentally friendly and environmentally friendly chemicals; and / or various commercially feasible products. Realize.

  The systems and methods of the present invention include, but are not limited to, metal salts formed at the anode, metal salts used to form various other chemicals, alkalis formed at the cathode, various other An electrochemical cell is provided that produces a variety of products such as the alkali used to form the product and / or hydrogen gas formed at the cathode. All such products have been defined herein and such chemicals are formed using electrochemical cells that operate at low voltage or energy and high efficiency, so they are “environmentally friendly. May be referred to as “chemical substances”. The low voltage or less energy intensive processes described herein result in less emissions of carbon dioxide compared to conventional methods of making similar chemicals or products. In some embodiments, but not limited to, chemicals or products such as carbonate and bicarbonate products are formed by the capture of carbon dioxide from flue gas in the alkali generated at the cathode. Such carbonate and bicarbonate products are “environmentally friendly chemicals” because they reduce pollution and provide a cleaner environment.

Metal “Metal ion” or “metal” as used herein includes any metal ion that can be converted from a lower oxidation state to a higher oxidation state. Examples of metal ions include, but are not limited to, iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel Palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, the metal ion includes, but is not limited to, iron, copper, tin, chromium, or combinations thereof. In some embodiments, the metal ion is copper. In some embodiments, the metal ion is tin. In some embodiments, the metal ion is iron. In some embodiments, the metal ion is chromium. In some embodiments, the metal ion is platinum. “Oxidation state” as used herein includes the degree of oxidation of atoms in a substance. For example, in some embodiments, the oxidation state is a net charge on the ions. Some examples of reaction of metal ions at the anode are as shown in Table I below (SHE is a standard hydrogen electrode). The theoretical value of the anode potential is also shown. It should be understood that some variation from these voltages may occur depending on electrolyte conditions, pH, concentration, etc., and such variations are well within the scope of the present invention.

  The metal ions may be present as metal compounds or metal alloys or combinations thereof. In some embodiments, the anion bound to the metal is the same as the anion of the electrolyte. For example, for sodium chloride or potassium chloride used as the electrolyte, metal chlorides such as, but not limited to, iron chloride, copper chloride, tin chloride, chromium chloride are used as the metal compound. For example, metal sulfates such as, but not limited to, iron sulfate, copper sulfate, tin sulfate, and chromium sulfate are used as the metal compound for sodium sulfate or potassium sulfate used as the electrolyte. For example, for sodium bromide or potassium bromide used as the electrolyte, metal bromides such as, but not limited to, iron bromide, copper bromide, tin bromide are used as the metal compound.

  In some embodiments, the electrolyte anion may be partially or completely different from the metal anion. For example, in some embodiments, the electrolyte anion may be sulfuric acid, while the metal anion may be chloride. In such embodiments, it may be desirable to have a lower concentration of chloride ions in the electrochemical cell. For example, in some embodiments, higher concentrations of chloride ions in the anode electrolyte due to electrolyte chloride and metal chloride may result in undesirable ionic species in the anode electrolyte. This can be avoided by utilizing an electrolyte containing ions other than chloride. In some embodiments, the anode electrolyte may be a combination of ions similar to the metal anion and a different anion than the metal ion. For example, when the metal anion is chloride, the anode electrolyte can be a mix of sulfate and chloride ions. In such embodiments, it may be desirable to have a sufficient concentration of chloride ions in the electrolyte to dissolve the metal salt, but not so high as to result in undesirable ionic species formation.

  In some embodiments, the electrolyte and / or metal compound is selected based on the desired end product. For example, if HCl is desired from the reaction between hydrogen gas and a metal compound, metal chloride is used as the metal compound and sodium chloride is used as the electrolyte. For example, if a brominated hydrocarbon is desired from a reaction between a metal compound and a hydrocarbon, metal bromide is used as the metal compound and sodium bromide or potassium bromide is used as the electrolyte.

In some embodiments, the metal ions used in the electrochemical systems described herein are soluble in the anode electrolyte and / or from a lower oxidation state to a higher oxidation state. It can be selected based on the cell voltage desired for metal oxidation. For example, the voltage required to oxidize Cr ²⁺ to Cr ³⁺ may be lower than that required for Sn ²⁺ to Sn ⁴⁺ but formed by the reaction of hydrogen gas with Cr ³⁺ The amount of HCl formed may be lower than the HCl formed with Sn ⁴⁺ by two chlorine atoms obtained per tin molecule. Thus, in some embodiments, if a lower cell voltage may be desirable, metal ion oxidation that results in a lower cell voltage, such as but not limited to Cr ²⁺ , may be used. For example, a lower voltage may be desirable for reactions where carbon dioxide is captured by alkali generated by the cathode electrolyte. In some embodiments, if higher amounts of product, such as hydrochloric acid, may be desired, metal ions (but not limited to Sn) that result in higher amounts of product despite relatively higher voltages. ²⁺ ) may be used. For example, the cell voltage may be higher for the tin system compared to the chromium system, but the concentration of acid formed with Sn ⁴⁺ may offset the higher voltage of the system. Products formed by the systems and methods described herein, such as acids, halohydrocarbons, sulfohydrocarbons, carbonates, bicarbonates, etc., are required for previously known methods of making the same products It is understood that it is still an “environmentally friendly” chemical because it is made by a less energy intensive process compared to the energy input considered.

  In some embodiments, both lower oxidation state metal ions and higher oxidation state metal ions are present in the anode electrolyte. In some embodiments, it may be desirable to have both lower and higher oxidation state metal ions in the anode electrolyte. Appropriate ratios of lower and higher oxidation state metal ions in the anode electrolyte have been described herein. Lower oxidation state metal ions mixed with higher oxidation state metal ions help lower voltages in electrochemical systems and higher yields and selectivity in corresponding catalytic reactions with hydrogen gas or hydrocarbons Can do.

  In some embodiments, the metal ions in the anode electrolyte are mixed metal ions. For example, an anode electrolyte containing lower oxidation state copper ions and higher oxidation state copper ions may also contain another metal ion such as, but not limited to, iron. In some embodiments, the presence of the second metal ion in the anode electrolyte can be beneficial in reducing the total energy of the electrochemical reaction in combination with the catalytic reaction.

  Some examples of metal compounds that can be used in the systems and methods of the present invention include, but are not limited to, copper (II) sulfate, copper (II) nitrate, copper (I) chloride, copper (I) bromide. , Copper (I) iodide, iron (III) sulfate, iron (III) nitrate, iron (II) chloride, iron (II) bromide, iron (II) iodide, tin (II) sulfate, tin (II) nitrate ), Tin (II) chloride, tin (II) bromide, tin (II) iodide, chromium (III) sulfate, chromium (III) nitrate, chromium (II) chloride, chromium (II) bromide, chromium iodide (II), zinc chloride (II), zinc bromide (II) and the like are included.

Ligand In some embodiments, an additive, eg, a ligand, is used in conjunction with a metal ion to improve the efficiency of metal ion oxidation inside the anode chamber and / or the metal ion inside / outside of the anode chamber. Improve catalytic reactions such as, but not limited to, reaction with hydrogen gas, with unsaturated hydrocarbons, and / or with saturated hydrocarbons. In some embodiments, the ligand is added to the anode electrolyte along with the metal. In some embodiments, the ligand is bound to a metal ion. In some embodiments, the ligand is bound to the metal ion by a covalent bond, an ionic bond and / or a coordinate bond. In some embodiments, the ligand is bound to the metal ion by van der Waals attraction.

  Accordingly, in some embodiments, contacting the anode with the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, and adding a ligand to the anode electrolyte. A method in which a ligand interacts with a metal ion and contacting the cathode and the cathode electrolyte. In some embodiments, contacting the anode with the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, and adding a ligand to the anode electrolyte, comprising: A method in which a ligand interacts with a metal ion and contacting the cathode and the cathode electrolyte, wherein the cathode generates hydroxide ions, water, and / or hydrogen gas. provide. In some embodiments, contacting the anode with the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, and adding a ligand to the anode electrolyte, comprising: A ligand interacting with a metal ion, contacting the cathode with a cathode electrolyte, wherein the cathode generates hydroxide ions, water, and / or hydrogen gas, the ligand and higher Contacting an anode electrolyte containing oxidized metal ions with an unsaturated hydrocarbon, hydrogen gas, saturated hydrocarbon, or a combination thereof is provided.

In some embodiments, contacting the anode with the anode electrolyte, oxidizing the metal halide from a lower oxidation state to a higher oxidation state at the anode, and adding a ligand to the metal halide. The ligand interacting with the metal ion, contacting the cathode and the cathode electrolyte, wherein the cathode generates hydroxide ions, water, and / or hydrogen gas, and unsaturated. And / or halogenating the saturated hydrocarbon with a higher oxidation state metal halide. In some embodiments, the metal halide is a metal chloride and the halogenation reaction is chlorination. In some embodiments, such methods contain a hydrogen gas generating cathode. In some embodiments, such methods contain an oxygen depolarized cathode. In some embodiments, the unsaturated hydrocarbon in such a method is a substituted alkene or an unsubstituted alkene as C _n H _2n (where n is 2-20) (or an alkyne, or as further described herein). Formula I) as described, for example ethylene, propylene, butene and the like. In some embodiments, the saturated hydrocarbon in such methods is a substituted alkane or an unsubstituted alkane as C _n H _{2n + 2} (where n is 2-20) (or as further described herein). Formula III) such as methane, ethane, propane and the like. In some embodiments, the metal in such a method is a metal chloride, such as copper chloride. In some embodiments, such a method results in a net energy reduction of greater than 100 kJ / mol or greater than 150 kJ / mol or greater than 200 kJ / mol or greater than 100-250 kJ / mol; Provides voltage reduction (described below and in FIG. 8C). In some embodiments, unsaturated hydrocarbons in such methods include, but are not limited to, C ₂ -C ₅ alkenes such as ethylene, propylene, isobutylene, 2-butene (cis and / or trans), pentene, and the like. or, but not limited to, but include ethylene, propylene, isobutylene, a _C 2 -C ₄ alkene, such as 2-butene (cis and / or trans). In some embodiments, the unsaturated hydrocarbon in such a method is ethylene, and the metal ion in such a method is a metal chloride, such as copper chloride. In such a process, EDC is formed by halogenation of ethylene. In some embodiments, the saturated hydrocarbon in such a method is ethane, and the metal ion in such a method is a metal chloride, such as platinum chloride or copper chloride. In such a process, chloroethane or EDC is formed by halogenation of ethane.

In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; configured to interact with the metal ions A system comprising: a ligand in an anode electrolyte; and a cathode in contact with the cathode electrolyte. In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; configured to interact with the metal ions A system comprising: a ligand in an anode electrolyte; and a cathode in contact with the cathode electrolyte configured to produce hydroxide ions, water, and / or hydrogen gas. In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; configured to interact with the metal ions A ligand in the anode electrolyte; a cathode in contact with the cathode electrolyte configured to form hydroxide ions, water, and / or hydrogen gas; a ligand and a higher oxidation state metal A system is provided that includes an anode electrolyte containing ions and a reactor configured to react an unsaturated hydrocarbon, hydrogen gas, saturated hydrocarbon, or a combination thereof. In some embodiments, such a system contains an oxygen depolarized cathode. In some embodiments, such a system contains a hydrogen gas generating cathode. In some embodiments, such a system provides a net energy reduction of greater than 100 kJ / mol or greater than 150 kJ / mol or greater than 200 kJ / mol or greater than 100-250 kJ / mol, or the system has a voltage greater than 1V. There is a reduction (described below and in FIG. 8C). In some embodiments, unsaturated hydrocarbons in such systems include, but are not limited to, C ₂ -C ₅ alkenes such as ethylene, propylene, isobutylene, 2-butene (cis and / or trans), pentene, and the like. or, but not limited to, but include ethylene, propylene, isobutylene, a _C 2 -C ₄ alkene, such as 2-butene (cis and / or trans). In some embodiments, the unsaturated hydrocarbon in such a system is ethylene. In some embodiments, the metal in such a system is a metal chloride, such as copper chloride. In some embodiments, the unsaturated hydrocarbon in such a system is ethylene and the metal ion in such a system is a metal chloride, such as copper chloride. In such a system, EDC is formed by halogenation of ethylene. In some embodiments, the saturated hydrocarbon in such a system is ethane, and the metal ion in such a system is a metal chloride, such as platinum chloride, copper chloride, and the like. In such systems, ethane halogenation forms chloroethane and / or EDC.

  In some embodiments, the ligand provides one or more of the following: Increased reactivity of metal ions to unsaturated hydrocarbons, saturated hydrocarbons, or hydrogen gas, enhanced selectivity of metal ions to halogenation of unsaturated or saturated hydrocarbons, metal ions to unsaturated hydrocarbons, saturated hydrocarbons , Or enhanced transfer of halogen to hydrogen gas, reduced redox potential of electrochemical cell, enhanced solubility of metal ions in aqueous medium, reduced cross-membrane of metal ions to cathode electrolyte in electrochemical cell, Reduce corrosion of electrochemical cells and / or reactors, enhanced separation of metal ions from acidic solutions after reaction with hydrogen gas (eg, size exclusion membrane), separation of metal ions from halogenated hydrocarbon solutions Enhancement (eg, size exclusion membrane), as well as combinations thereof.

In some embodiments, binding of the ligand to the metal ion increases the size of the metal ion sufficiently larger to prevent migration of the metal ion through the ion exchange membrane in the cell. In some embodiments, an anion exchange membrane in an electrochemical cell is used in conjunction with a size exclusion membrane to prevent migration of metal ions bound to the ligand from the anode electrolyte to the cathode electrolyte. obtain. Such membranes are described herein below. In some embodiments, binding of the ligand to the metal ion increases the solubility of the metal ion in an aqueous medium. In some embodiments, the binding of ligands to metal ions reduces metal corrosion in electrochemical cells and reactors. In some embodiments, the binding of the ligand to the metal ion increases the size of the metal ion sufficiently larger to facilitate the separation of the metal ion from the acid or from the halogenated hydrocarbon after the reaction. In some embodiments, the presence of the ligand and / or binding of the ligand to the metal ion may prevent the formation of various halogenated species of the metal ion in solution and may favor the formation of only the desired species. For example, the presence of a ligand in a copper ion solution may limit the formation of various halogenated species of copper ions, such as, but not limited to, [CuCl ₃ ] ²⁻ or CuCl ₂ ^O, but Cu ^2+. The formation of / Cu ⁺ ions may be advantageous. In some embodiments, the presence and / or binding of the ligand in the metal ion solution reduces the overall voltage of the cell by providing one or more of the above advantages.

  “Ligand” as used herein includes any ligand capable of enhancing the properties of a metal ion. In some embodiments, ligands include, but are not limited to, substituted or unsubstituted aliphatic phosphines, substituted or unsubstituted aromatic phosphines, substituted or unsubstituted aminophosphines, substituted or unsubstituted crown ethers, substituted or unsubstituted Substituted aliphatic nitrogen, substituted or unsubstituted cyclic nitrogen, substituted or unsubstituted aliphatic sulfur, substituted or unsubstituted cyclic sulfur, substituted or unsubstituted heterocyclic rings, and substituted or unsubstituted heterocyclic aromatic compounds are included.

Substituted or unsubstituted aliphatic nitrogen In some embodiments, the ligand is a substituted or unsubstituted aliphatic nitrogen of formula A;

In the formula, n and m are independently 0 to 2, and R and R ¹ are independently H, alkyl, or substituted alkyl. In some embodiments, alkyl is methyl, ethyl, propyl, i-propyl, butyl, i-butyl, or pentyl. In some embodiments, a substituted alkyl is an alkyl that is substituted with one or more of the groups including alkenyl, halogen, amine, substituted amine, and combinations thereof. In some embodiments, the substituted amine is substituted with a group selected from hydrogen and / or alkyl.

In some embodiments, the ligand is a substituted or unsubstituted aliphatic nitrogen of formula B;

Wherein R and R ¹ are independently H, alkyl, or substituted alkyl. In some embodiments, alkyl is methyl, ethyl, propyl, i-propyl, butyl, i-butyl, or pentyl. In some embodiments, a substituted alkyl is an alkyl that is substituted with one or more of the groups including alkenyl, halogen, amine, substituted amine, and combinations thereof. In some embodiments, the substituted amine is substituted with a group selected from hydrogen and / or alkyl.

In some embodiments, the ligand is a substituted or unsubstituted aliphatic nitrogen donor of formula B, and R and R ¹ are independently H, C ₁ -C ₄ alkyl, or substituted C ₁ -C ₄ alkyl. It is. In some _embodiments, C 1 -C ₄ alkyl are methyl, ethyl, propyl, i- propyl, butyl or i- butyl. In some embodiments, substituted C ₁ -C ₄ alkyl, alkenyl, halogen, amine, is C ₁ -C ₄ alkyl substituted with one or more groups including substituted amines, and combinations thereof . In some embodiments, the substituted amine is substituted with a group selected from hydrogen and / or C ₁ -C ₃ alkyl.

  The concentration of the ligand can be selected based on various parameters including, but not limited to, metal ion concentration, ligand solubility, and the like.

Substituted or unsubstituted crown ether having O, S, P or N heteroatoms In some embodiments, the ligand is a substituted or unsubstituted crown ether of formula C;

In the formula, R is independently O, S, P, or N, and n is 0 or 1.

  In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is O, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is S, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is N, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is P, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is O or S, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is O or N, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is N or S, and n is 0 or 1. In some embodiments, the ligand is a substituted or unsubstituted crown ether of Formula C, R is N or P, and n is 0 or 1.

Substituted or unsubstituted phosphine In some embodiments, the ligand is a substituted or unsubstituted phosphine of formula D, or an oxide thereof,

Wherein R ¹ , R ² , and R ³ are independently H, alkyl, substituted alkyl, alkoxy, substituted alkoxy, aryl, substituted aryl, heteroaryl, substituted heteroaryl, amine, substituted amine, cycloalkyl, substituted Cycloalkyl, heterocycloalkyl, and substituted heterocycloalkyl.

An example of an oxide of formula D is

Where R ¹ , R ² , and R ³ are independently H, alkyl, substituted alkyl, alkoxy, substituted alkoxy, aryl, substituted aryl, heteroaryl, substituted heteroaryl, amine, substituted amine, cyclo Alkyl, substituted cycloalkyl, heterocycloalkyl, and substituted heterocycloalkyl.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkyl and substituted alkyl. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkyl and substituted alkyl, where substituted alkyl is alkoxy, substituted alkoxy, amine, and substituted amine Substituted with a group selected from In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkyl and substituted alkyl, wherein the substituted alkyl is a group selected from alkoxy and amine Has been replaced.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkoxy and substituted alkoxy. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkoxy and substituted alkoxy, where substituted alkoxy is alkyl, substituted alkyl, amine, and substituted Substituted with a group selected from amines. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently alkoxy and substituted alkoxy, wherein the substituted alkoxy is a group selected from alkyl and amine Has been replaced.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently aryl and substituted aryl. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently aryl and substituted aryl, where substituted aryl is alkyl, substituted alkyl, alkoxy, substituted alkoxy , An amine, and a group selected from substituted amines. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently aryl and substituted aryl, wherein the substituted aryl is selected from alkyl, alkoxy, and amine Substituted with a group. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently aryl and substituted aryl, wherein the substituted aryl is a group selected from alkyl and alkoxy Has been replaced.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heteroaryl and substituted heteroaryl. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heteroaryl and substituted heteroaryl, where substituted heteroaryl is alkyl, substituted alkyl, alkoxy Substituted with a group selected from: substituted alkoxy, amine and substituted amine. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heteroaryl and substituted heteroaryl, wherein the substituted heteroaryl is from alkyl, alkoxy, and amine. Substituted with a selected group.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently cycloalkyl and substituted cycloalkyl. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently cycloalkyl and substituted cycloalkyl, where substituted cycloalkyl is alkyl, substituted alkyl, alkoxy Substituted with a group selected from: substituted alkoxy, amine and substituted amine. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently cycloalkyl and substituted cycloalkyl, wherein the substituted cycloalkyl is from alkyl, alkoxy, and amine. Substituted with a selected group.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heterocycloalkyl and substituted heterocycloalkyl. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heterocycloalkyl and substituted heterocycloalkyl, wherein the substituted heterocycloalkyl is alkyl, substituted Substituted with a group selected from alkyl, alkoxy, substituted alkoxy, amine and substituted amine. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently heterocycloalkyl and substituted heterocycloalkyl, wherein the substituted heterocycloalkyl is alkyl, alkoxy And substituted with a group selected from amines.

In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently an amine and a substituted amine. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently an amine and a substituted amine, wherein the substituted amine is an alkyl, substituted alkyl, alkoxy, and substituted Substituted with a group selected from alkoxy. In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently an amine and a substituted amine, wherein the substituted amine is a group selected from alkyl and alkoxy Has been replaced by In some embodiments of the compound of Formula D or oxide thereof, R ¹ , R ² , and R ³ are independently an amine and a substituted amine, and the substituted amine is substituted with an alkyl.

In some embodiments, the ligand is a substituted or unsubstituted phosphine of formula D or an oxide thereof;

Wherein R ¹ , R ² , and R ³ are independently H, alkyl; substituted alkyl substituted with a group selected from alkoxy, substituted alkoxy, amine, and substituted amine; aryl; alkyl, substituted alkyl Substituted aryl substituted with a group selected from alkoxy, substituted alkoxy, amine, and substituted amine; heteroaryl; substituted with a group selected from alkyl, substituted alkyl, alkoxy, substituted alkoxy, amine, and substituted amine A substituted heteroaryl; an amine; a substituted amine substituted with a group selected from alkyl, substituted alkyl, alkoxy, and substituted alkoxy; cycloalkyl; from alkyl, substituted alkyl, alkoxy, substituted alkoxy, amine, and substituted amine A position substituted with a selected group Cycloalkyl; heterocycloalkyl; and alkyl, substituted alkyl, alkoxy, substituted heterocycloalkyl substituted with a group selected from substituted alkoxy, amines, and substituted amines.

In some embodiments, the ligand is a substituted or unsubstituted phosphine of formula D or an oxide thereof;

Wherein R ¹ , R ² , and R ³ are independently H, alkyl; a substituted alkyl substituted with a group selected from alkoxy and amine; aryl; a group selected from alkyl, alkoxy, and amine A substituted aryl substituted with a group selected from alkyl, alkoxy and amine; an amine; a substituted amine substituted with a group selected from alkyl and alkoxy; Cycloalkyl; substituted cycloalkyl substituted with a group selected from alkyl, alkoxy, and amine; heterocycloalkyl; and substituted heterocycloalkyl substituted with a group selected from alkyl, alkoxy, and amine .

Substituted or unsubstituted pyridine In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E;

Wherein R ¹ and R ² are independently H, alkyl, substituted alkyl, aryl, substituted aryl, heteroaryl, substituted heteroaryl, amine, substituted amine, cycloalkyl, substituted cycloalkyl, heterocycloalkyl, and substituted Heterocycloalkyl.

In some embodiments, the ligand is a substituted or unsubstituted pyridine of formula E;

Wherein R ¹ and R ² are independently H, alkyl, substituted alkyl, heteroaryl, substituted heteroaryl, amine, and substituted amine.

In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, R ¹ and R ² are independently H, alkyl, and substituted alkyl, where substituted alkyl is alkoxy, substituted alkoxy, Substituted with a group selected from amines and substituted amines. In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, R ¹ and R ² are independently H, alkyl, and substituted alkyl, wherein the substituted alkyl is from an amine and a substituted amine. Substituted with a selected group, the substituted amine is substituted with alkyl, heteroaryl or substituted heteroaryl.

In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, and R ¹ and R ² are independently heteroaryl and substituted heteroaryl. In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, and R ¹ and R ² are independently heteroaryl, and substituted heteroaryl substituted with alkyl, alkoxy, or amine. .

In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, and R ¹ and R ² are independently an amine and a substituted amine. In some embodiments, the ligand is a substituted or unsubstituted pyridine of Formula E, R ¹ and R ² are independently an amine and a substituted amine, and the substituted amine is an alkyl, heteroaryl, or substituted heteroaryl Has been replaced by

In some embodiments, the ligand is a substituted or unsubstituted pyridine of formula E;

Wherein R ¹ and R ² are independently H; alkyl; substituted alkyl substituted with a group selected from amine and substituted amine; heteroaryl; substituted heteroaryl substituted with alkyl, alkoxy or amine Amines; and substituted amines substituted with alkyl, heteroaryl or substituted heteroaryl.

Substituted or unsubstituted dinitriles In some embodiments, the ligand is a substituted or unsubstituted dinitrile of Formula F;

In the formula, R is hydrogen, alkyl, or substituted alkyl, n is 0 to 2, m is 0 to 3, and k is 1 to 3.

  In some embodiments, the ligand is a substituted or unsubstituted dinitrile of Formula F, R is a substituted alkyl substituted with hydrogen, alkyl, or alkoxy or amine, and n is 0-1 , M is 0-3, and k is 1-3.

  In some embodiments, the ligand is a substituted or unsubstituted dinitrile of Formula F, R is hydrogen or alkyl, n is 0 to 1, m is 0 to 3, and k is 1-3.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphines, substituted or unsubstituted crown ethers, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitriles, and combinations thereof; and metal ions A composition comprising an aqueous medium comprising is provided.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; and iron, Chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, Compositions comprising an aqueous medium comprising a metal ion selected from molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof are provided.

  In one embodiment, a ligand, metal ion selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; And a composition comprising an aqueous medium comprising a salt.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; iron, chromium , Copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum And a metal ion selected from tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof; and an aqueous medium comprising a salt.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; iron, chromium , Copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum Metal ions selected from tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof; and sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or combinations thereof Providing a composition comprising an aqueous medium containing.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; metal ions; And an aqueous medium comprising a salt comprising sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or combinations thereof.

  In one embodiment, a ligand, metal ion selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; A composition comprising an aqueous medium comprising a salt; and an unsaturated or saturated hydrocarbon is provided.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; iron, chromium , Copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum There is provided a composition comprising an aqueous medium comprising: a metal ion selected from tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof; a salt; and an unsaturated or saturated hydrocarbon.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; iron, chromium , Copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum Metal ions selected from tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof; sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or a salt comprising a combination thereof; To provide a composition comprising an aqueous medium containing an unsaturated or saturated hydrocarbon.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; metal ions; Provided is a composition comprising a salt comprising sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or a combination thereof; and an aqueous medium comprising an unsaturated or saturated hydrocarbon.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; metal ions; A salt comprising sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or combinations thereof; and an unsaturated or saturated hydrocarbon selected from ethylene, propylene, butylene, ethane, propane, butane, and combinations thereof A composition comprising an aqueous medium is provided.

  In one embodiment, a ligand selected from substituted or unsubstituted phosphine, substituted or unsubstituted crown ether, substituted or unsubstituted aliphatic nitrogen, substituted or unsubstituted pyridine, substituted or unsubstituted dinitrile, and combinations thereof; iron, chromium , Copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold, nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum Metal ions selected from tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof; sodium chloride, ammonium chloride, sodium sulfate, ammonium sulfate, calcium chloride, or a salt comprising a combination thereof; Providing ethylene, propylene, butylene, ethane, propane, butane, and a composition comprising an aqueous medium containing an unsaturated or saturated hydrocarbon is selected from those combinations.

In some embodiments of the methods and systems provided herein, the ligand is
Sulfonated bathocuproine;
Pyridine;
Tris (2-pyridylmethyl) amine;
Glutaronitrile;
Iminodiacetonitrile;
Malononitrile;
Succinonitrile;
Tris (diethylamino) phosphine;
Tris (dimethylamino) phosphine;
Tri (2-furyl) phosphine;
Tris (4-methoxyphenyl) phosphine;
Bis (diethylamino) phenylphosphine;
Tris (N, N-tetramethylene) phosphoric triamide;
Di-tert-butyl N, N-diisopropylphosphoramidite;
Diethyl phosphoramidate;
Hexamethylphosphoramide;
Diethylenetriamine;
Tris (2-aminoethyl) amine;
N, N, N ′, N ′, N ″ -pentamethyldiethylenetriamine;
15-crown-5;
1,4,8,11-tetrathiacyclotetradecane; and salts or stereoisomers thereof.

  In some embodiments, adding a ligand to an anode electrolyte comprising a metal ion solution and, without limitation, enhancing the reactivity of the metal ion to unsaturated hydrocarbons, saturated hydrocarbons, or hydrogen gas, unsaturated Alternatively, enhanced selectivity of metal ions for halogenation of saturated hydrocarbons, enhanced halogen transfer from metal ions to unsaturated hydrocarbons, saturated hydrocarbons, or hydrogen gas, reduced redox potential of electrochemical cells, aqueous Enhanced solubility of metal ions in the medium, reduced membrane crossing of metal ions to the cathode electrolyte in the electrochemical cell, reduced corrosion of the electrochemical cell and / or reactor, acidic solution after reaction with hydrogen gas Enhanced separation of metal ions from halogen, enhanced separation of metal ions from halogenated hydrocarbon solutions, and combinations thereof Including and a step resulting in one or more properties, a method of using the ligand.

  In some embodiments, a method is provided that includes improving the efficiency of an electrochemical cell, the electrochemical cell comprising an anode in contact with an anode electrolyte comprising metal ions, the anode comprising metal ions. Oxidation from lower oxidation state to higher oxidation state. In some embodiments, efficiency is related to the voltage applied to the electrochemical cell.

  As used herein, “alkenyl” has 2 to 10 carbon atoms, in some embodiments 2 to 6 carbon atoms or 2 to 4 carbon atoms, and has at least one Refers to straight or branched chain hydrocarbyl with vinyl unsaturation (> C = C <) sites. For example, ethenyl, propenyl, and 1,3-butadienyl.

  As used herein, “alkoxy” refers to —O-alkyl, where alkyl is defined herein. Alkoxy includes, by way of example, methoxy, ethoxy, n-propoxy, isopropoxy, n-butoxy, t-butoxy, sec-butoxy, and n-pentoxy.

As used herein, “alkyl” refers to a monovalent saturated aliphatic hydrocarbyl group having 1 to 10 carbon atoms, and in some embodiments, 1 to 6 carbon atoms. “C _x -C _y alkyl” refers to an alkyl group having _{x to y} carbon atoms. This term includes, by way of example, straight chain and branched hydrocarbyl groups such as methyl (CH ₃ —), ethyl (CH ₃ CH ₂ —), n-propyl (CH ₃ CH ₂ CH ₂ —), isopropyl ( _{(CH 3) 2 CH -)} , n- butyl _{(CH 3 CH 2 CH 2 CH} 2 -), isobutyl _{((CH 3) 2 CHCH 2} -), sec- butyl _{((CH 3) (CH 3} CH 2) CH -), t-butyl _{((CH 3) 3 C -} ), n- pentyl _{(CH 3 CH 2 CH 2 CH} 2 CH 2 -), and neopentyl _{((CH 3) 3 CCH 2} - containing).

As used herein, “amino” or “amine” refers to the group —NH ₂ .

  As used herein, “aryl” refers to an aromatic group of 6 to 14 carbon atoms (having no ring heteroatoms), where the aromatic group is a single ring (eg, Phenyl) or multiple condensed (fused) rings (eg, naphthyl or anthryl).

  As used herein, “cycloalkyl” refers to a saturated or partially saturated cyclic group of 3 to 14 carbon atoms (without ring heteroatoms), which saturated or partially saturated cyclic group. Have a single ring or multiple rings including fused, bridged, and spiro ring systems. Examples of cycloalkyl groups include, for example, cyclopropyl, cyclobutyl, cyclopentyl, cyclooctyl, and cyclohexenyl.

  As used herein, “halo” or “halogen” refers to fluoro, chloro, bromo, and iodo.

  As used herein, “heteroaryl” refers to an aromatic group of 1-6 heteroatoms selected from the group consisting of oxygen, nitrogen, and sulfur, and is a single ring (eg, furanyl). As well as multiple ring systems such as benzimidazol-2-yl and benzimidazol-6-yl. Heteroaryl includes, but is not limited to, pyridyl, furanyl, thienyl, thiazolyl, isothiazolyl, triazolyl, imidazolyl, isoxazolyl, pyrrolyl, pyrazolyl, pyridazinyl, pyrimidinyl, benzofuranyl, tetrahydrobenzofuranyl, isobenzofuranyl, benzothiazolyl, benzo Isothiazolyl, benzotriazolyl, indolyl, isoindolyl, benzoxazolyl, quinolyl, tetrahydroquinolinyl, isoquinolyl, quinazolinonyl, benzimidazolyl, benzoisoxazolyl, or benzothienyl.

  As used herein, “heterocycloalkyl” refers to a saturated or partially saturated cyclic group having 1 to 5 heteroatoms selected from the group consisting of nitrogen, sulfur, or oxygen, As well as multiple ring systems, including fused, bridged, and spiro ring systems. Heterocyclyl includes, but is not limited to, tetrahydropyranyl, piperidinyl, N-methylpiperidin-3-yl, piperazinyl, N-methylpyrrolidin-3-yl, 3-pyrrolidinyl, 2-pyrrolidin-1-yl, morpholinyl, And pyrrolidinyl.

  As used herein, “substituted alkoxy” refers to —O-substituted alkyl, where substituted alkyl is as defined herein.

  As used herein, “substituted alkyl” refers to 1 to 5 selected from the group consisting of alkenyl, halogen, —OH, —COOH, amino, substituted amino, and in some embodiments, 1 to 3 Refers to an alkyl group having one or two or more substituents, the substituents being as defined herein.

As used herein, “substituted amino” or “substituted amine” refers to the group —NR ¹⁰ R ¹¹ , where R ¹⁰ and R ¹¹ are hydrogen, alkyl, substituted alkyl, aryl, substituted aryl, heteroaryl, And independently selected from the group consisting of substituted heteroaryl.

  As used herein, “substituted aryl” is 1-8 selected from the group consisting of alkyl, substituted alkyl, alkoxy, substituted alkoxy, amine, substituted amine, alkenyl, halogen, —OH, and —COOH. , In some embodiments, refers to an aryl group that is substituted with 1-5, 1-3, or 1-2 substituents, wherein the substituents are as defined herein. It is.

  As used herein, “substituted cycloalkyl” is 1-8 selected from the group consisting of alkyl, substituted alkyl, alkoxy, substituted alkoxy, amine, substituted amine, alkenyl, halogen, —OH, and —COOH. Or, in some embodiments, or in some embodiments, refers to a cycloalkyl group, as defined herein, having 1-3 substituents, the substituents defined herein As defined in.

  As used herein, “substituted heteroaryl” is substituted with 1 to 5, or 1 to 3, or 1 to 2 substituents selected from the group consisting of substituents as defined for substituted aryl. Refers to a heteroaryl group that is present.

  As used herein, a “substituted heterocycloalkyl” is substituted with 1 to 5 substituents as defined for substituted cycloalkyl, or in some embodiments with 1 to 3, Refers to a heterocyclic group as defined herein.

  For all substituted groups as defined above, polymers obtained by defining substituents with additional substituents themselves (eg substituted as substituents, which are themselves substituted with substituted aryl groups) It is understood that substituted aryl having an aryl group, etc.) are not intended to be included herein. In such cases, the maximum number of such substitutions is three. Similarly, it is understood that the above definitions are not intended to include impermissible substitution patterns (eg, methyl substituted with 5 chloro groups). Such unacceptable substitution patterns are well known to those skilled in the art.

  In some embodiments, the concentration of the ligand in the electrochemical cell depends on the concentration of lower and / or higher oxidation state metal ions. In some embodiments, the ligand concentration is between 0.25M and 5M; or between 0.25M and 4M; or between 0.25M and 3M; or between 0.5M and 5M; Between 5M and 4M; or between 0.5M and 3M; or between 0.5M and 2.5M; or between 0.5M and 2M; or between 0.5M and 1.5M; or 0.5M Between ˜1M; or between 1M and 2M; or between 1.5M and 2.5M; or between 1.5M and 2M.

  In some embodiments, the ratio of the concentration of ligand to the concentration of Cu (I) ions is between 1: 1 to 4: 1; or between 1: 1 to 3: 1; or 1: 1 to 2: 1 or 1: 1, or 2: 1, or 3: 1 or 4: 1.

  In some embodiments, the solution used in the catalytic reaction, i.e., the reaction of the higher oxidation state metal ion with the unsaturated or saturated hydrocarbon, and the solution used in the electrochemical reaction is 4.5M to Higher oxidation state metal ions between 7M, e.g. concentration of Cu (II), lower oxidation state metal ions between 0.25M and 1.5M, e.g. concentration of Cu (I), and 0 Contains a concentration of ligand between 25M and 6M. In some embodiments, the concentration of sodium chloride in the solution can affect the solubility of the ligand and / or metal ions; the yield and selectivity of the catalytic reaction; and / or the efficiency of the electrochemical cell. Thus, in some embodiments, the concentration of sodium chloride in the solution is 1M-3M. In some embodiments, the solution used in the catalytic reaction, i.e., the reaction of the higher oxidation state metal ion with the unsaturated or saturated hydrocarbon, and the solution used in the electrochemical reaction is 4.5M to Higher oxidation state metal ions, such as Cu (II) concentration between 7M, lower oxidation state metal ions, such as Cu (I) concentration, between 0.25M and 1.5M; Contains a concentration of ligand between 25M-6M and a concentration of sodium chloride between 1M-3M.

Electrochemical Method and System In one aspect, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state in the anode chamber; Contacting the cathode electrolyte in the cathode chamber with the cathode. In one aspect, contacting the metal ions in the anode electrolyte in the anode chamber with the anode, converting the metal ions from a lower oxidation state to a higher oxidation state in the anode chamber, and the cathode electrolyte in the cathode chamber A method is provided that includes contacting the cathode and forming alkali, water, and / or hydrogen gas in the cathode chamber. In one aspect, contacting the anode with metal ions in the anode electrolyte in the anode chamber, converting the metal ions from a lower oxidation state to a higher oxidation state in the anode chamber, and an unsaturated or saturated hydrocarbon Treating a higher oxidation state metal ion. In some embodiments, treatment of higher oxidation state metal ions with unsaturated or saturated hydrocarbons results in the formation of halohydrocarbons. In some embodiments, treatment of higher oxidation state metal ions with unsaturated or saturated hydrocarbons is inside the anode chamber. In some embodiments, treatment of higher oxidation state metal ions with unsaturated or saturated hydrocarbons is outside the anode chamber. In some embodiments, the cathode is an oxygen depolarized cathode.

  Several embodiments of electrochemical cells are illustrated in the figures and described herein. It should be understood that the figures are for illustrative purposes only and that variations in reagents and equipment are well within the scope of the present invention. All electrochemical methods and systems described herein do not produce chlorine gas, as found in chloroalkali systems. All systems and methods related to halogenation or sulfonation of unsaturated or saturated hydrocarbons do not use oxygen gas in the catalytic reactor.

  In some embodiments, contacting the metal ions in the anode electrolyte in the anode chamber with the anode; converting or oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode; A method is provided that includes contacting a cathode electrolyte with a cathode in a cathode chamber and forming alkali, water, and / or hydrogen gas at the cathode. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting the electrolyte with the cathode; forming alkali, water, and / or hydrogen gas at the cathode; and an anode electrolyte comprising the higher oxidation state metal ions and unsaturated and / or saturated hydrocarbons. Contacting to form a halogenated hydrocarbon, or contacting a hydrogen gas with an anode electrolyte comprising a higher oxidation state metal ion to form an acid, or a combination of both. provide.

  In some embodiments, an anode chamber comprising an anode in contact with a metal ion in the anode electrolyte and configured to convert the metal ion from a lower oxidation state to a higher oxidation state; And a cathode chamber that includes a cathode in contact with the system. In another aspect, an anode chamber containing an anode in contact with metal ions in an anode electrolyte and configured to convert metal ions from a lower oxidation state to a higher oxidation state; and a cathode electrolyte; And a cathode chamber configured to produce alkali, water, and / or hydrogen gas. In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber comprising a cathode in contact with the cathode electrolyte, wherein the cathode is configured to form alkali, water, and / or hydrogen gas in the cathode electrolyte; Contacting an anode electrolyte operatively connected to the anode chamber and containing metal ions in a higher oxidation state with unsaturated and / or saturated hydrocarbons and / or hydrogen gas, respectively, halogenated hydrocarbons; Or a reactor comprising a reactor configured to form acid. In another aspect, an anode chamber comprising an anode in contact with metal ions in the anode electrolyte and configured to convert metal ions from a lower oxidation state to a higher oxidation state; Or an unsaturated and / or saturated hydrocarbon delivery system configured to deliver saturated hydrocarbons to the anode chamber, wherein the anode chamber also converts the unsaturated and / or saturated hydrocarbons to halogenated hydrocarbons And an unsaturated and / or saturated hydrocarbon delivery system configured to provide a system.

As illustrated in FIG. 1A, the electrochemical system 100A includes an anode chamber having an anode in contact with an anode electrolyte that is converted to a higher oxidation state metal ion (denoted ^{MH +} ) by the anode. Contains the lower oxidation state metal ions (denoted ^{ML +} ) to be converted. The metal ion may be in the form of sulfate, chloride, bromide, or iodide.

As used herein, “lower oxidation state” represented as ^{L +} in ML + includes the lower oxidation state of the metal. For example, the lower oxidation state of the metal ion may be 1+, 2+, 3+, 4+, or 5+. As used herein, “higher oxidation state” expressed as ^{H +} in MH + includes the higher oxidation state of the metal. For example, the higher oxidation state of the metal ion may be 2+, 3+, 4+, 5+, or 6+.

  The electron (s) generated at the anode are used to drive the reaction at the cathode. The cathodic reaction can be any reaction known in the art. Where the anode electrolyte is sodium chloride, or sodium sulfate containing a metal halide, the anode chamber and cathode chamber are in some embodiments, such as but not limited to sodium ions, to the cathode electrolyte. It can be separated by an ion exchange membrane (IEM) that can allow the passage of ions. Some reactions that can occur at the cathode include, but are not limited to, water reactions to form hydroxide ions and hydrogen gas, oxygen and water reactions to form hydroxide ions, and hydrogen gas to form. Reduction of HCl; or reaction of HCl and oxygen gas to form water.

As illustrated in FIG. 1B, electrochemical system 100B includes a cathode chamber having a cathode in contact with a cathode electrolyte that forms hydroxide ions in the cathode electrolyte. Electrochemical system 100B also includes an anode chamber having an anode in contact with the anode electrolyte, the anode electrolyte containing lower oxidation state metal ions (denoted ^{ML +} ), which is higher by the anode. Converted to oxidized metal ions (denoted ^{MH +} ). The electron (s) generated at the anode are used to drive the reaction at the cathode. When the anode electrolyte is sodium chloride, sodium bromide, sodium iodide, sodium sulfate, ammonium chloride, or the like, or an equivalent solution containing a metal halide, the anode and cathode chambers are filled with sodium ions to the cathode electrolyte. They are separated by an ion exchange membrane (IEM) that allows passage. In some embodiments, if the cathode electrolyte is, for example, sodium chloride, sodium bromide, sodium iodide, or sodium sulfate, or an equivalent solution, the ion exchange membrane is not limited to the anode electrolyte. Allows passage of anions such as chloride, bromide, iodide, or sulfate ions. In the cathode electrolyte, sodium ions combine with hydroxide ions to form sodium hydroxide. Anions combine with metal ions to form metal halides or metal sulfates. The hydroxide-forming cathode as illustrated in FIG. 1B is for illustrative purposes only, other cathodes such as cathodes that reduce HCl to form hydrogen gas, or react both HCl and oxygen gas to produce water. It should be understood that the cathodes that form are equally applicable to the above system. Such cathodes have been described herein.

  In some embodiments, the electrochemical system of the present invention includes one or more ion exchange membranes. Accordingly, in some embodiments, contacting the metal ions in the anode electrolyte with the anode in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and the cathode chamber Providing a method comprising: contacting a cathode electrolyte with a cathode in the substrate; forming alkali, water, and / or hydrogen gas at the cathode; and separating the cathode and anode by at least one ion exchange membrane. To do. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting the electrolyte with the cathode; forming alkali, water, and / or hydrogen gas at the cathode; separating the cathode and anode with at least one ion exchange membrane; and higher oxidation state metal ions Contacting an anode electrolyte containing hydrogen with an unsaturated and / or saturated hydrocarbon to form a halogenated hydrocarbon, or contacting an anode electrolyte containing higher oxidation state metal ions with hydrogen gas to form an acid Step to do, or And a combination of both these, a method. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber comprising a cathode in contact with a cathode electrolyte, the cathode chamber being configured to produce alkali, water, and / or hydrogen gas; a cathode and an anode At least one ion exchange membrane. In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber comprising a cathode in contact with a cathode electrolyte, the cathode chamber being configured to produce alkali, water, and / or hydrogen gas; a cathode and an anode At least one ion exchange membrane that separates the anode electrolyte; an anode electrolyte operably connected to the anode chamber and comprising metal ions in a higher oxidation state; and unsaturated and / or saturated hydrocarbons and / or hydrogen gas A reactor configured to contact and form a halogenated hydrocarbon and an acid, respectively Including, to provide a system. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

As illustrated in FIG. 2, the electrochemical system 200 includes a cathode in contact with the cathode electrolyte and an anode in contact with the anode electrolyte. The cathode forms hydroxide ions in the cathode electrolyte, and the anode converts metal ions from a lower oxidation state (M ^{L +} ) to a higher oxidation state (M ^{H +} ). The anode and cathode are separated by an anion exchange membrane (AEM) and a cation exchange membrane (CEM). A third electrolyte (eg, sodium chloride, sodium bromide, sodium iodide, sodium sulfate, ammonium chloride, or a combination thereof, or an equivalent solution) is disposed between the AEM and CEM. Sodium ions from the third electrolyte pass through the CEM to form sodium hydroxide in the cathode chamber, and halide anions from the third electrolyte, such as chloride ions, bromide ions or iodide ions, or The sulfate anion passes through the AEM and forms a solution for the metal halide or metal sulfate in the anode chamber. The metal halide or metal sulfate formed in the anode electrolyte is then delivered to a reactor for reaction with hydrogen gas or unsaturated or saturated hydrocarbons, hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrogen bromide. Acid, hydrogen iodide, or hydroiodic acid and / or halohydrocarbon are generated, respectively. The third electrolyte can be removed from the central chamber as a depleted ion solution after ion migration. For example, in some embodiments, when the third electrolyte is a sodium chloride solution, after the transfer of sodium ions to the cathode electrolyte and the transfer of chloride ions to the anode electrolyte, the depleted sodium chloride solution is Can be removed from the central chamber. The depleted salt solution may be used for commercial purposes, or may be transferred as an electrolyte to the anode and / or cathode chamber, or concentrated for reuse as a third electrolyte. In some embodiments, the depleted salt solution can be useful for preparing demineralized water. The hydroxide-forming cathode as illustrated in FIG. 2 is for illustrative purposes only, other cathodes such as cathodes that reduce HCl to form hydrogen gas, or react both HCl and oxygen gas to produce water. It should be understood that the cathodes that form are equally applicable to the above system and have been further described herein.

  In some embodiments, the two ion exchange membranes may be replaced with a single ion exchange membrane as illustrated in FIG. 1A or 1B, as illustrated in FIG. In some embodiments, the ion exchange membrane is an anion exchange membrane, as illustrated in FIG. 3A. In such embodiments, the cathode electrolyte can be sodium halide, sodium sulfate or an equivalent solution, and the AEM allows the passage of anions to the anode electrolyte, but metal ions from the anode electrolyte to the cathode electrolyte. Is to prevent the passage of. In some embodiments, the ion exchange membrane is a cation exchange membrane as illustrated in FIG. 3B. In such embodiments, the anode electrolyte can be an equivalent solution containing sodium halide, sodium sulfate, or a metal halide solution, or an equivalent solution, and the CEM can pass the sodium cation through the cathode electrolyte. While allowing, it is such that the passage of metal ions from the anode electrolyte to the cathode electrolyte is prevented. In some embodiments, using one ion exchange membrane instead of two ion exchange membranes can reduce the resistance provided by multiple IEMs and promote lower voltages for performing electrochemical reactions Can do. Some examples of suitable anion exchange membranes are provided herein.

  In some embodiments, the cathode used in the electrochemical system of the present invention is a hydrogen gas generating cathode. Accordingly, in some embodiments, contacting the metal ions in the anode electrolyte with the anode in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and the cathode chamber Contacting the cathode electrolyte with the cathode and forming alkali and hydrogen gas at the cathode. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting the electrolyte with the cathode; forming alkali and hydrogen gas at the cathode; and contacting the anode electrolyte containing higher oxidation state metal ions with an unsaturated or saturated hydrocarbon to form the halogenated hydrocarbon. A method is provided comprising the step of forming, or contacting an anode electrolyte comprising a higher oxidation state metal ion with hydrogen gas to form an acid, or a combination of both. In some embodiments, the method further comprises separating the cathode and anode by at least one ion exchange membrane. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof. In some embodiments, the above method includes an anode that does not form a gas. In some embodiments, the method includes an anode that does not use a gas.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. And a cathode chamber comprising a cathode in contact with the cathode electrolyte, wherein the cathode is configured to produce alkali and hydrogen gas. In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber including a cathode in contact with the cathode electrolyte, wherein the cathode is configured to generate alkali and hydrogen gas; operably connected to the anode chamber; And an anode electrolyte containing higher oxidation state metal ions and an unsaturated or saturated hydrocarbon and / or hydrogen gas in contact with each other to form a halogenated hydrocarbon and an acid, respectively. A system including a container. In some embodiments, the system is configured not to produce gas at the anode. In some embodiments, the system is configured to use no gas at the anode. In some embodiments, the system further comprises at least one ion exchange membrane that separates the cathode and anode. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

For example, as illustrated in FIG. 4A, the electrochemical system 400 includes a cathode in contact with a cathode electrolyte 401 where hydroxide is formed in the cathode electrolyte. System 400 also includes an anode in contact with anode electrolyte 402 that converts lower oxidation state metal ions (M ^{L +} ) to higher oxidation state metal ions (M ^{H +} ). The following are the reactions that occur at the cathode and anode.
H ₂ O + e ⁻ → 1 / 2H ₂ + OH ⁻ (cathode)
M ^{L +} → M ^{H +} + xe ⁻ (anode, x = 1 to 3)
For example, Fe ²⁺ → Fe ³⁺ + e ⁻ (anode)
Cr ²⁺ → Cr ³⁺ + e ⁻ (anode)
Sn ²⁺ → Sn ⁴⁺ + 2e ⁻ (anode)
Cu ⁺ → Cu ²⁺ + e ⁻ (anode)

As illustrated in FIG. 4A, the electrochemical system 400 includes a cathode that forms hydroxide ions and hydrogen gas at the cathode. Hydrogen gas may exit or be captured and stored for commercial purposes. In some embodiments, the hydrogen released at the cathode is subjected to halogenation or sulfonation (including sulfation) with a metal halide or metal sulfate formed in the anode electrolyte, hydrogen chloride, hydrochloric acid, Hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid, or sulfuric acid may be formed. Such reactions are described in detail herein. The ^{MH +} formed at the anode combines with chloride ions to form higher oxidation state metal chlorides such as, but not limited to, FeCl ₃ , CrCl ₃ , SnCl ₄ , or CuCl ₂ . The hydroxide ions formed at the cathode combine with sodium ions to form sodium hydroxide.

Chloride ions in this application are for illustrative purposes only, and other equivalent ions such as, but not limited to, sulfate, bromide or iodide are also well within the scope of the invention and correspond in the anode electrolyte. It should be understood that this results in a metal halide or metal sulfate. It should also be understood that the MCn _n shown in the figures exemplified herein is a mixture of lower oxidation state metal ions and higher oxidation state metal ions. The integer _n in MCl _n merely represents the lower and higher oxidation state metal ions and may be from 1 to 5 or more depending on the metal ion. For example, in some embodiments, when copper is a metal ion, MCl _n can be a mixture of CuCl and CuCl ₂ . This mixture of copper ions in the anode electrolyte can then be contacted with hydrogen gas, unsaturated hydrocarbons, and / or saturated hydrocarbons to form the respective products.

  In some embodiments, the cathode used in the electrochemical system of the present invention is a hydrogen gas generating cathode that does not form alkali. Accordingly, in some embodiments, contacting the metal ions in the anode electrolyte with the anode in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and the cathode chamber Contacting the cathode electrolyte with the cathode and forming hydrogen gas at the cathode. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting the electrolyte with the cathode, forming hydrogen gas at the cathode, and contacting the anode electrolyte containing higher oxidation state metal ions with an unsaturated or saturated hydrocarbon to form a halogenated hydrocarbon. There is provided a method comprising: contacting a hydrogen gas with an anode electrolyte comprising a metal oxide of a higher oxidation state, or forming an acid, or a combination of both. In some embodiments, the method further comprises separating the cathode and anode by at least one ion exchange membrane. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof. In some embodiments, the above method includes an anode that does not form a gas. In some embodiments, the method includes an anode that does not use a gas.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. And a cathode chamber comprising a cathode in contact with the cathode electrolyte, wherein the cathode is configured to generate hydrogen gas. In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber including a cathode in contact with the cathode electrolyte, the cathode chamber configured to generate hydrogen gas; and operably connected to the anode chamber And a reactor configured to contact an anode electrolyte comprising higher oxidation state metal ions with an unsaturated or saturated hydrocarbon and / or hydrogen gas to form a halogenated hydrocarbon and an acid, respectively. A system including the above is provided. In some embodiments, the system is configured not to produce gas at the anode. In some embodiments, the system is configured to use no gas at the anode. In some embodiments, the system further comprises at least one ion exchange membrane that separates the cathode and anode. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

For example, as illustrated in FIG. 4B, the electrochemical system 400 includes a cathode in contact with a cathode electrolyte 401, where hydrochloric acid delivered to the cathode electrolyte is converted to hydrogen gas in the cathode electrolyte. . System 400 also includes an anode in contact with anode electrolyte 402 that converts lower oxidation state metal ions (M ^{L +} ) to higher oxidation state metal ions (M ^{H +} ). The following are the reactions that occur at the cathode and anode.
2H ⁺ + 2e ⁻ → H ₂ (cathode)
M ^{L +} → M ^{H +} + xe ⁻ (anode, x = 1 to 3)
For example, Fe ²⁺ → Fe ³⁺ + e ⁻ (anode)
Cr ²⁺ → Cr ³⁺ + e ⁻ (anode)
Sn ²⁺ → Sn ⁴⁺ + 2e ⁻ (anode)
Cu ⁺ → Cu ²⁺ + e ⁻ (anode)

As illustrated in FIG. 4B, the electrochemical system 400 includes a cathode that forms hydrogen gas at the cathode. Hydrogen gas may exit or be captured and stored for commercial purposes. In some embodiments, the hydrogen released at the cathode is subjected to halogenation or sulfonation (including sulfation) with a metal halide or metal sulfate formed in the anode electrolyte, hydrogen chloride, hydrochloric acid, Hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid, or sulfuric acid may be formed. Such reactions are described in detail herein. The ^{MH +} formed at the anode combines with chloride ions to form higher oxidation state metal chlorides such as, but not limited to, FeCl ₃ , CrCl ₃ , SnCl ₄ , or CuCl ₂ . The hydroxide ions formed at the cathode combine with sodium ions to form sodium hydroxide.

One AEM in FIG. 4B is for illustrative purposes only, the system has a CEM, HCl is delivered into the anode electrolyte, and hydrogen ions are delivered through the CEM to the cathode electrolyte. Should be understood. In some embodiments, the system illustrated in FIG. 4B may contain both AEM and CEM, and the central chamber contains a chloride salt. It should also be understood that the MCn _n shown in the figures exemplified herein is a mixture of lower oxidation state metal ions and higher oxidation state metal ions. The integer _n in MCl _n merely represents the lower and higher oxidation state metal ions and may be from 1 to 5 or more depending on the metal ion. For example, in some embodiments, when copper is a metal ion, MCl _n can be a mixture of CuCl and CuCl ₂ . This mixture of copper ions in the anode electrolyte can then be contacted with hydrogen gas, unsaturated hydrocarbons, and / or saturated hydrocarbons to form the respective products.

  In some embodiments, the cathode in the electrochemical system of the present invention may be a gas diffusion cathode. In some embodiments, the cathode in the electrochemical system of the present invention may be a gas diffusion cathode that forms alkali at the cathode. In some embodiments, contacting the metal ions in the anode electrolyte with the anode, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, a gas diffusion cathode and the cathode electrolyte Contacting the method. In some embodiments, the gas diffusion cathode is an oxygen depolarized cathode (ODC). In some embodiments, the method includes forming an alkali in the ODC. In some embodiments, contacting the anode and the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, and contacting the cathode and the cathode electrolyte. The cathode is an oxygen depolarized cathode that reduces oxygen and water to hydroxide ions. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting an electrolyte with a gas diffusion cathode, forming an alkali at the cathode, contacting an anode electrolyte comprising a higher oxidation state metal ion with an unsaturated and / or saturated hydrocarbon, to form a halogenated hydrocarbon; Or contacting an anode electrolyte containing higher oxidation state metal ions with hydrogen gas to form an acid, or a combination of both. In some embodiments, the gas diffusion cathode does not form a gas. In some embodiments, the method includes an anode that does not form a gas. In some embodiments, the method includes an anode that does not use a gas. In some embodiments, the method further comprises separating the cathode and anode by at least one ion exchange membrane. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, wherein the anode converts or oxidizes metal ions from a lower oxidation state to a higher oxidation state. And a cathode chamber comprising a gas diffusion cathode in contact with the cathode electrolyte, wherein the cathode is configured to generate alkali. To do. In some embodiments, the gas diffusion cathode is an oxygen depolarized cathode (ODC). In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber including a gas diffusion cathode in contact with the cathode electrolyte, the cathode chamber being configured to generate alkali; operably connected to the anode chamber; And an anode electrolyte comprising a higher oxidation state metal ion and an unsaturated and / or saturated hydrocarbon and / or hydrogen gas in contact to form a halogenated hydrocarbon and an acid, respectively. And a reactor including the reactor. In some embodiments, the system is configured not to produce gas at the gas diffusion cathode. In some embodiments, the system is configured not to produce gas at the anode. In some embodiments, the system is configured to use no gas at the anode. In some embodiments, the system further comprises at least one ion exchange membrane that separates the cathode and anode. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

  As used herein, a “gas diffusion cathode”, or “gas diffusion electrode”, or other equivalent includes any electrode that can react with a gas to form an ionic species. In some embodiments, the gas diffusion cathode, as used herein, is an oxygen depolarized cathode (ODC). Such a gas diffusion cathode may be referred to as a gas diffusion electrode, an oxygen consumption cathode, an oxygen reduction cathode, an oxygen inlet cathode, an oxygen depolarized cathode, and the like.

In some embodiments, as illustrated in FIG. 5A, the combination of a gas diffusion cathode (eg, ODC) and anode in an electrochemical cell can result in the generation of alkali in the cathode chamber. In some embodiments, electrochemical system 500 includes a gas diffusion cathode in contact with cathode electrolyte 501 and an anode in contact with anode electrolyte 502. The anode and cathode are separated by an anion exchange membrane (AEM) and a cation exchange membrane (CEM). A third electrolyte (eg, sodium halide or sodium sulfate) is placed between the AEM and CEM. The following are possible reactions at the anode and cathode.
H ₂ O + 1 / 2O ₂ + 2e ⁻ → 2OH ⁻ (cathode)
M ^{L +} → M ^{H +} + xe ⁻ (anode, x = 1 to 3)
For example, 2Fe ²⁺ → 2Fe ³⁺ + 2e ⁻ (anode)
2Cr ²⁺ → 2Cr ³⁺ + 2e ⁻ (anode)
Sn ²⁺ → Sn ⁴⁺ + 2e ⁻ (anode)
2Cu ⁺ → 2Cu ²⁺ + 2e ⁻ (anode)

^{M H +} is formed at the anode, mate with chloride ions, but are not limited _{to, FeCl 3, CrCl 3, SnCl} 4 or metal chlorides such as CuCl _2, MCl _n is formed. The hydroxide ions formed at the cathode react with sodium ions to form sodium hydroxide. The oxygen at the cathode can be the atmosphere, or any commercially available source of oxygen.

  Methods and systems containing a gas diffusion cathode or ODC as described herein and illustrated in FIG. 5A are compared to methods and systems that include a hydrogen gas generating cathode (as illustrated in FIG. 4A) Can result in voltage reduction. Voltage reduction can result in less electricity consumption and less carbon dioxide emissions due to electricity generation. This can result in the generation of environmentally friendly chemicals such as sodium hydroxide, halogenated hydrocarbons and / or acids formed by the efficient and energy-saving methods and systems of the present invention. In some embodiments, an electrochemical cell with ODC is greater than 0.5 V, or 1 V compared to an electrochemical cell without ODC or compared to an electrochemical cell with a hydrogen gas generating cathode. Has a theoretical voltage reduction above, or above 1.5V, or between 0.5-1.5V. In some embodiments, this voltage reduction is at a cathode electrolyte pH between 7-15, or 7-14, or 6-12, or 7-12, or 7-10. Achieved.

The overall cell potential can be determined by a Nernst combination for each half-cell reaction.
E = E ⁰ −RT ln (Q) / nF
Where E ⁰ is the standard reduction potential, R is the general gas constant (8.314 J / mol K), T is the absolute temperature, and n is the number of electrons involved in the half-cell reaction. Yes, F is the Faraday constant (96485 J / V mol), and Q is the reaction quotient. Therefore,
E _overall = E _anode- E _cathode
It is.

When a lower oxidation state metal is oxidized to a higher oxidation state metal at the anode as described below,
Cu ⁺ → Cu ²⁺ + 2e ⁻
E _anodes based on various concentrations of copper II species can be between 0.159 and 0.75V.

When water is reduced to hydroxide ions and hydrogen gas at the cathode (as illustrated in FIG. 4A) as follows:
2H ₂ O + 2e ⁻ = H ₂ + 2OH ⁻ ,
E _cathode = −0.059 pH _c (where pH _c is the pH of the cathode electrolyte (= 14))
E _cathode = -0.83

The _total E is between 0.989 and 1.53 depending on the concentration of copper ions in the anode electrolyte.

When water is reduced to hydroxide ions in the ODC (as illustrated in FIG. 5A) as follows:
2H ₂ O + O ₂ + 4e ⁻ → 4OH ⁻
E _cathode = 1.224−0.059 pH _c (where pH _c = 14)
E _cathode = 0.4V

The _total E is between -0.241 and 0.3 V depending on the concentration of copper ions in the anode electrolyte.

  Therefore, the use of ODC in the cathode chamber is between about 1.5V or 0.5-2V compared to an electrochemical cell without ODC or compared to an electrochemical cell with a hydrogen gas generating cathode. Or a theoretical voltage reduction in the cathode chamber or between 0.5 and 1.5V or between 1 and 1.5V, or a theoretical voltage reduction in the cell.

  Accordingly, in some embodiments, contacting the metal ions in the anode electrolyte with the anode, contacting the oxygen depolarized cathode with the cathode electrolyte, applying a voltage to the anode and the cathode, and the cathode Forming an alkali at the anode, converting metal ions from a lower oxidation state to a higher oxidation state at the anode, as compared to a hydrogen gas generating cathode or as compared to a cell without ODC, Reducing the voltage above 0.5V or between 0.5-1.5V. In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. And a cathode chamber comprising an oxygen depolarizing cathode in contact with the cathode electrolyte, wherein the cathode is configured to generate alkali, the system comprising: The system provides a voltage reduction above 0.5V or between 0.5-1.5V compared to a system with a hydrogen gas generating cathode or compared to a system without an ODC. In some embodiments, the voltage reduction is a theoretical voltage reduction that can vary depending on the ohmic resistance in the cell.

  While the method and system containing a gas diffusion cathode or ODC provides a voltage reduction compared to the method and system containing a hydrogen gas generating cathode, both systems, i.e., the system and hydrogen containing the ODC of the present invention. A system containing a gas generating cathode exhibits significant voltage reduction compared to chloroalkali systems previously known in the art. Voltage reduction can result in less electricity consumption and less carbon dioxide emissions due to the generation of electricity. This can result in the generation of environmentally friendly chemicals such as sodium hydroxide, halogenated hydrocarbons and / or acids formed by the efficient and energy-saving methods and systems of the present invention. For example, voltage reduction is beneficial in the production of EDC that is typically formed by reacting a halogenated hydrocarbon, such as ethylene, with chlorine gas generated by a chloroalkali process that consumes high voltage. In some embodiments, the electrochemical system of the present invention (two or three compartment cells with a hydrogen gas generating cathode or ODC) is greater than 0.5 V, or greater than 1 V compared to a chloroalkali process. Or have a theoretical voltage reduction of more than 1.5V, or 0.5-3V. In some embodiments, this voltage reduction is achieved by a cathode electrolyte pH between 7-15, or between 7-14, or 6-12, or 7-12, or 7-10.

For example, a theoretical E _anode in a chloroalkali process is about 1.36 V, subject to the following reaction.
2Cl ⁻ → Cl ₂ + 2e ⁻

The theoretical E _cathode in the chloroalkali process is about −0.83 V (at pH> 14), subject to the following reaction.
2H ₂ O + 2e ⁻ = H ₂ + 2OH ⁻

The _overall theoretical E for the chloroalkali process is then 2.19V. The _total theoretical E for the hydrogen gas producing cathode in the system of the present invention is between 0.989 and 1.53 V, and then the _total E for the ODC in the system of the present invention is the copper ion in the anode electrolyte. Depending on the concentration, it is between -0.241 and 0.3V. Thus, the electrochemical system of the present invention is more than 3V or more than 2V or between 0.5 and 2.5V or between 0.5 and 2.0V or between 0.5 and 1 compared to a chloroalkali system. . Cathode chamber between 5V or between 0.5 and 1.0V or between 1 and 1.5V or between 1 and 2V or between 1 and 2.5V or between 1.5 and 2.5V Results in a theoretical voltage reduction in the cell, or a theoretical voltage reduction in the cell.

  In some embodiments, the electrochemical cell may be conditioned with a first electrolyte and may be operated with a second electrolyte. For example, in some embodiments, the electrochemical cell and AEM, CEM or combinations thereof are conditioned with sodium sulfate as the electrolyte, and after stabilization of the voltage with sodium sulfate, the cell is with sodium chloride as the electrolyte. Can work. An illustrative example of such stabilization of an electrochemical cell is described in Example 13 herein. Thus, in some embodiments, contacting the first anode electrolyte and anode in the anode chamber, contacting the cathode electrolyte and cathode in the cathode chamber, and the cathode and anode by at least one ion exchange membrane. Separating the ion exchange membrane with a first anode electrolyte in the anode chamber, contacting the anode with a second anode electrolyte containing metal ions, and lower oxidation of metal ions at the anode A method is provided that includes oxidizing from a state to a higher oxidation state and forming alkali, water, and / or hydrogen gas at the cathode. In some embodiments, the first anode electrolyte is sodium sulfate and the second anode electrolyte is sodium chloride. In some embodiments, the method includes contacting a second anode electrolyte comprising a higher oxidation state metal ion with an unsaturated and / or saturated hydrocarbon to form a halogenated hydrocarbon, or The method further includes contacting the second anode electrolyte containing high oxidation state metal ions with hydrogen gas to form an acid, or a combination of both. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

  In some embodiments, the cathode in the electrochemical system of the present invention may be a gas diffusion cathode that reacts HCl and oxygen gas to form water. In some embodiments, contacting the metal ions in the anode electrolyte with the anode, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, a gas diffusion cathode and the cathode electrolyte Contacting the method. In some embodiments, the gas diffusion cathode is an oxygen depolarized cathode (ODC). In some embodiments, the method includes reacting HCl and oxygen gas in the ODC to form water. In some embodiments, contacting the anode and the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, and contacting the cathode and the cathode electrolyte. The cathode is an oxygen depolarized cathode that reacts oxygen and HCl to form water. In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode, and a cathode in the cathode chamber Contacting an electrolyte with a gas diffusion cathode, forming water from HCl and oxygen gas at the cathode, and contacting an anode electrolyte containing higher oxidation state metal ions with an unsaturated and / or saturated hydrocarbon. Providing a process comprising: forming a halogenated hydrocarbon, or contacting an anode electrolyte comprising a higher oxidation state metal ion with hydrogen gas to form an acid, or a combination of both . In some embodiments, the gas diffusion cathode does not form a gas. In some embodiments, the method includes an anode that does not form a gas. In some embodiments, the method includes an anode that does not use a gas. In some embodiments, the method further comprises separating the cathode and anode by at least one ion exchange membrane. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, wherein the anode converts or oxidizes metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber comprising a gas diffusion cathode in contact with a cathode electrolyte, wherein the cathode is configured to produce water from HCl. I will provide a. In some embodiments, the gas diffusion cathode is an oxygen depolarized cathode (ODC). In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A cathode chamber comprising a gas diffusion cathode in contact with the cathode electrolyte, wherein the cathode is configured to produce water from HCl; operably connected to the anode chamber And an anode electrolyte comprising higher oxidation state metal ions and configured to contact unsaturated and / or saturated hydrocarbons and / or hydrogen gas to form halogenated hydrocarbons and acids, respectively. And a reactor. In some embodiments, the system is configured not to produce gas at the gas diffusion cathode. In some embodiments, the system is configured not to produce gas at the anode. In some embodiments, the system is configured to use no gas at the anode. In some embodiments, the system further comprises at least one ion exchange membrane that separates the cathode and anode. In some embodiments, the ion exchange membrane is a cation exchange membrane (CEM), an anion exchange membrane (AEM), or a combination thereof.

In some embodiments, as illustrated in FIG. 5B, the combination of a gas diffusion cathode (eg, ODC) and anode in an electrochemical cell can result in the generation of water in the cathode chamber. In some embodiments, electrochemical system 500 includes a gas diffusion cathode in contact with cathode electrolyte 501 and an anode in contact with anode electrolyte 502. The following are possible reactions at the anode and cathode.
2H ⁺ + 1 / 2O ₂ + 2e ⁻ → H ₂ O (cathode)
M ^{L +} → M ^{H +} + xe ⁻ (anode, x = 1 to 3)
For example, 2Fe ²⁺ → 2Fe ³⁺ + 2e ⁻ (anode)
2Cr ²⁺ → 2Cr ³⁺ + 2e ⁻ (anode)
Sn ²⁺ → Sn ⁴⁺ + 2e ⁻ (anode)
2Cu ⁺ → 2Cu ²⁺ + 2e ⁻ (anode)

^{M H +} is formed at the anode, mate with chloride ions, but are not limited _{to, FeCl 3, CrCl 3, SnCl} 4 or metal chlorides such as CuCl _2, MCl _n is formed. The oxygen at the cathode can be air or any commercially available source of oxygen. One AEM in FIG. 5B is for illustrative purposes only, the system has a CEM, HCl is delivered into the anode electrolyte, and hydrogen ions are delivered through the CEM to the cathode electrolyte. Should be understood. In some embodiments, the system illustrated in FIG. 5B contains both AEM and CEM, and the central chamber may contain chloride salts.

  In some embodiments, the electrochemical system of the present invention may be combined with other electrochemical cells for efficient and low energy intensive systems. For example, in some embodiments, as illustrated in FIG. 5C, the electrochemical system 400 of FIG. 4B may be different so that hydrochloric acid formed in other electrochemical cells is provided to the cathode electrolyte of the system 400. You may combine with the electrochemical cell of. Except for changing the cathode compartment, receiving HCl from another electrochemical cell, oxidizing it, and forming hydrogen gas, the electrochemical system 400 is a system 100A (FIG. 1A), 100B (FIG. 1B), 200 (FIG. 2), 400 (FIG. 4A), 500 (FIGS. 5A and 5B). Chloride ions migrate through the AEM from the cathode electrolyte to the anode electrolyte. This can lead to an overall improvement in the voltage of the system. For example, the theoretical cell voltage of the system may be between 0.1 and 0.7V. In some embodiments, when the cathode is ODC, the theoretical cell voltage can be between -0.5 and -1V. An electrochemical cell that produces HCl in the anode electrolyte is described in US patent application Ser. No. 12 / 503,557, filed Jul. 15, 2009, which is hereby incorporated by reference in its entirety. ). Other sources of HCl are well known in the art. An example of the HCl source from the VCM generation process and its integration into the electrochemical system of the present invention is illustrated in FIG. 8B below.

  In some embodiments of the methods and systems described herein, a size exclusion membrane (SEM) is used in conjunction with or in place of an anion exchange membrane (AEM). Is done. In some embodiments, the AEM is surface coated with a layer of SEM. In some embodiments, the SEM is coupled to or pressed against the AEM. By using SEM with or instead of AEM, metal ions, or ligands, from the anolyte to the catholyte are reduced due to the large size of the metal ions alone or the large size of the metal ions bound to the ligand. Migration of bound metal ions can be prevented. This can further prevent CEM fouling or catholyte contamination by metal ions. It should be understood that this use of a SEM in combination with or in place of AEM still facilitates the transfer of chloride ions from the third electrolyte to the anolyte. In some embodiments, contacting the anode and the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, contacting the cathode and the cathode electrolyte, Using a size exclusion membrane to prevent the migration of metal ions from the anode electrolyte to the cathode electrolyte. In some embodiments, the method comprises a cathode that produces alkali in the cathode electrolyte, or an oxygen depolarized cathode that produces alkali in the cathode electrolyte, or an oxygen depolarized cathode that produces water in the cathode electrolyte. Or a cathode for generating hydrogen gas. In some embodiments, the method comprises contacting an anode electrolyte comprising a higher oxidation state metal ion with an unsaturated or saturated hydrocarbon to form a halogenated hydrocarbon, or a higher oxidation state metal. The method further includes contacting the anode electrolyte containing ions with hydrogen gas to form an acid, or a combination of both. In some embodiments, the unsaturated hydrocarbon in such a process is ethylene. In some embodiments, the metal ion in such a method is copper chloride. In some embodiments, the unsaturated hydrocarbon in such a method is ethylene and the metal ion is copper chloride. An example of a halogenated hydrocarbon that can be formed from ethylene is ethylene dichloride (EDC).

  In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; a cathode in contact with the cathode electrolyte; A system including a size exclusion membrane disposed between the anode and the cathode and configured to prevent migration of metal ions from the anode electrolyte to the cathode electrolyte. In some embodiments, the system further includes a cathode configured to generate alkali in the cathode electrolyte, generate water in the cathode electrolyte, or generate hydrogen gas. In some embodiments, the system further includes an oxygen depolarized cathode configured to generate alkali and / or water in the cathode electrolyte. In some embodiments, the system further includes a hydrogen gas generating cathode. In some embodiments, the system is in contact with an unsaturated or saturated hydrocarbon in contact with an anode electrolyte that is operatively connected to the anode chamber and that includes a metal oxide in a higher oxidation state. Or a reactor configured to contact hydrogen gas with an anode electrolyte containing higher oxidation state metal ions to form an acid, or a combination of both. . In some embodiments, the unsaturated hydrocarbon in such a system is ethylene. In some embodiments, the metal ion in such a system is copper chloride. In some embodiments, the unsaturated hydrocarbon in such a system is ethylene and the metal ion is copper chloride. One example of a halogenated hydrocarbon that can be formed from ethylene is EDC.

  In some embodiments, the size exclusion membrane completely prevents migration of metal ions to the cathode chamber or the central chamber with the third electrolyte, as defined herein above and herein. 100%; or 99%; or 95% or 75%; or 50%; or 25%; or 25 to 50%; or 50 to 75%; or 50 to 95%. Reduce between.

  In some embodiments, the AEM used in the methods and systems of the present invention is an organic compound (e.g., such that the AEM does not interact with organic matter and / or does not react or absorb metal ions) , Ligands or hydrocarbons). This can be achieved, by way of example only, by using a polymer that does not contain free radicals or anions that are available for reaction with organics or with metal ions. By way of example only, a polymer containing a fully quaternized amine can be used as an AEM. Other examples of AEM have been described herein.

  In some embodiments of the methods and systems described herein, a turbulent promoter is used in the anode compartment to improve mass transfer at the anode. For example, as the current density increases in the electrochemical cell, a mass transfer limited reaction rate is achieved at the anode. Laminar flow of the anolyte can cause resistance and diffusion problems. A turbulent promoter can be used in the anode compartment in order to improve mass transfer at the anode and thereby reduce the cell voltage. As used herein, a “turbulent promoter” includes components in the anode compartment of an electrochemical cell that provide turbulent flow. In some embodiments, a turbulent promoter can be provided behind the anode, i.e., between the anode and the wall of the electrochemical cell, and / or in some embodiments, the turbulent promoter is It can be provided between the anode and the anion exchange membrane. By way of example only, the electrochemical systems shown in FIGS. 1A, 1B, 2, 4A, 4B, 5A, 5B, 5C, 6, 8A, 9 and 12 are: A turbulent promoter may be present between the anode and an ion exchange membrane, such as an anion exchange membrane, and / or a turbulent promoter may be present between the anode and the outer wall of the cell.

  An example of a turbulent promoter is gas bubbling in the anode compartment. The gas may be any inert gas that does not react with the components of the anolyte. For example, the gas includes, but is not limited to, air, nitrogen, and argon. Gas bubbling at the anode can stir the anode electrolyte and improve mass transfer at the anode. Improved mass transfer can lead to a reduction in cell voltage. Other examples of turbulent promoters include, but are not limited to, the incorporation of carbon cloth adjacent to the anode, the incorporation of carbon / graphite felt adjacent to the anode, expanded plastic adjacent to the anode, adjacent to the anode. Includes fishing nets, combinations of the above.

  In some embodiments, contacting the anode and the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, contacting the cathode and the cathode electrolyte, Providing a turbulent flow in the anode electrolyte using a turbulent promoter. In some embodiments, the method further comprises reducing the cell voltage by 50-200 mV or 100-200 mV by providing turbulence. In some embodiments, contacting the anode and the anode electrolyte, oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode, contacting the cathode and the cathode electrolyte, Providing a turbulent flow in the anode electrolyte by passing air bubbles through the anode. Examples of gases include, but are not limited to air, nitrogen, and argon. In some embodiments, the method further comprises reducing the cell voltage by 50-200 mV or 100-200 mV by providing turbulence (see Example 3).

  In some embodiments, the method includes a cathode that produces alkali in the cathode electrolyte, an oxygen depolarized cathode that produces alkali in the cathode electrolyte, or an oxygen depolarized cathode that produces water in the cathode electrolyte. Or a cathode for generating hydrogen gas. In some embodiments, the method includes contacting an anode electrolyte comprising a higher oxidation state metal ion with an unsaturated or saturated hydrocarbon to form a halogenated hydrocarbon, or a higher oxidation state. The method further includes contacting the anode electrolyte containing metal ions with hydrogen gas to form an acid, or a combination of both. In some embodiments, the unsaturated hydrocarbon in such a process is ethylene. In some embodiments, the metal ion in such a method is copper chloride. In some embodiments, the unsaturated hydrocarbon in such a process is ethylene and the metal ion is copper chloride. An example of a halogenated hydrocarbon that can be formed from ethylene is ethylene dichloride, EDC. In some embodiments, a ligand as described herein can be used in the method.

  In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state, and a cathode in contact with the cathode electrolyte A turbulent promoter disposed about the anode and configured to provide turbulence in the anode electrolyte. In some embodiments, an anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state, and a cathode in contact with the cathode electrolyte A gas bubbler disposed about the anode and configured to bubble gas in the anode electrolyte and provide turbulence. Examples of gases include, but are not limited to air, nitrogen, and argon. A gas bubbler may be any means known in the art for bubbling gas into the anode compartment.

  In some embodiments, the system further includes a cathode configured to generate alkali in the cathode electrolyte, generate water in the cathode electrolyte, or generate hydrogen gas. In some embodiments, the system further includes an oxygen depolarized cathode configured to generate alkali and / or water in the cathode electrolyte. In some embodiments, the system further includes a hydrogen gas generating cathode. In some embodiments, the system described above is halocarbonized by contacting an anode electrolyte that is operably connected to the anode chamber and that includes a higher oxidation state metal ion with an unsaturated or saturated hydrocarbon. Further comprising a reactor configured to form hydrogen, or contact an anode electrolyte containing higher oxidation state metal ions with hydrogen gas to form an acid, or a combination of both. . In some embodiments, the unsaturated hydrocarbon in such a system is ethylene. In some embodiments, the metal ion in such a system is copper chloride. In some embodiments, the unsaturated hydrocarbon in such a system is ethylene and the metal ion is copper chloride. An example of a halogenated hydrocarbon that can be formed from ethylene is EDC.

In some embodiments, the metal formed in the anode electrolyte with a higher oxidation state is the corresponding oxidized product (halogenated hydrocarbon and / or acid), and the reduced lower oxidation state. It is subjected to reactions that can lead to metals. The lower oxidation state metal ions may then be recycled back to the electrochemical system for generation of higher oxidation state metal ions. Such reactions that regenerate lower oxidation state metal ions from higher oxidation state metal ions include, but are not limited to, reaction with hydrogen gas or hydrocarbon as described herein. .
Reaction with hydrogen gas, unsaturated hydrocarbons, and saturated hydrocarbons

  In some embodiments, contacting the metal ions in the anode electrolyte in the anode chamber with the anode; converting or oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode; Treating higher oxidation state metal ions with hydrogen gas. In some embodiments of the above method, the method includes contacting the cathode and the cathode electrolyte and forming alkali in the cathode electrolyte. In some embodiments of the above methods, the method includes contacting the cathode with a cathode electrolyte and forming alkali and / or hydrogen gas at the cathode. In some embodiments of the above methods, the method includes contacting the cathode with a cathode electrolyte and forming alkali, water, and / or hydrogen gas at the cathode. In some embodiments of the above method, the method includes contacting the gas diffusion cathode with a cathode electrolyte and forming alkali at the cathode. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and the cathode and cathode electrolyte And a step of forming alkali, water or hydrogen gas at the cathode, and treating higher oxidation state metal ions in the anode electrolyte with hydrogen gas from the cathode. . In some embodiments, contacting the anode with metal ions in the anode electrolyte in the anode chamber, converting the metal ions from a lower oxidation state to a higher oxidation state at the anode, and oxygen depolarization A method is provided that includes contacting a cathode with a cathode electrolyte, forming alkali or water at the cathode, and treating higher oxidation state metal ions in the anode electrolyte with hydrogen gas. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and the cathode and cathode electrolyte And a step of forming water or hydrogen gas at the cathode and treating the higher oxidation state metal ions in the anode electrolyte with hydrogen gas. In some embodiments, treatment of hydrogen gas with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, the above method comprises treating hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid by treating higher oxidation state metal ions with hydrogen gas. And / or forming sulfuric acid. In some embodiments, treatment of higher oxidation state metal ions with hydrogen gas comprises hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid and / or sulfuric acid, and more This results in the formation of low oxidation state metal ions. In some embodiments, lower oxidation state metal ions are recycled back to the anode chamber. In some embodiments, the lower oxidation state metal ion and acid mixture is subjected to an acid retardation technique, before the lower oxidation state metal ions are recycled back to the anode chamber. The lower oxidation state metal ions are separated from the acid.

  In some embodiments of the method described above, the method does not produce chlorine gas at the anode.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. An anode chamber; and a reactor operably connected to the anode chamber and configured to react hydrogen gas with an anode electrolyte containing metal ions in a higher oxidation state. provide. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali in the cathode electrolyte. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form hydrogen gas in the cathode electrolyte. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali and hydrogen gas in the cathode electrolyte. In some embodiments of the above system, the system includes a gas diffusion cathode having a cathode electrolyte, the cathode configured to form alkali in the cathode electrolyte. In some embodiments of the system, the system includes a gas diffusion cathode having a cathode electrolyte, the cathode configured to form water in the cathode electrolyte. In some embodiments, an anode chamber comprising an anode having metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. A cathode chamber comprising a cathode having a cathode electrolyte, wherein the cathode is configured to form alkali and / or hydrogen gas in the cathode electrolyte; operable in the anode chamber And a reactor configured to react hydrogen gas from the cathode with an anode electrolyte comprising higher oxidation state metal ions. In some embodiments, the reactor is operatively connected to the anode chamber and comprises an anode electrolyte comprising higher oxidation state metal ions and hydrogen gas from the cathode of the same electrochemical cell, or It is configured to react with hydrogen gas from an external source. In some embodiments, treatment of hydrogen gas with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, the system described above can react with or treat a higher oxidation state metal ion with hydrogen gas to produce hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide. Forming hydroiodic acid, and / or sulfuric acid. In some embodiments, treatment of higher oxidation state metal ions with hydrogen gas comprises hydrogen chloride, hydrochloric acid, hydrogen bromide, hydrobromic acid, hydrogen iodide, hydroiodic acid, and / or sulfuric acid, and This results in the formation of lower oxidation state metal ions. In some embodiments, the system is configured to form lower oxidation state metal ions from higher oxidation state metal ions with hydrogen gas and recirculate lower oxidation state metal ions back to the anode chamber. It is configured. In some embodiments, the system uses, but is not limited to, ion exchange resins, size exclusion membranes, and acid retardation techniques such as acid dialysis to separate lower oxidation state metal ions from the acid. Is configured to do.

  In some embodiments of the system described above, the anode in the system is configured not to produce chlorine gas.

  In some embodiments, the metal formed with a higher oxidation state in the anode electrolyte of the electrochemical system of FIGS. 1A, 1B, 2, 3A, 3B, 4A, 4B, 5A and 5B is Based on the bound anion, it can react with hydrogen gas to form the corresponding product. For example, a metal chloride, metal bromide, metal iodide, or metal sulfate can be reacted with the corresponding hydrogen chloride, hydrochloric acid, hydrogen bromide, bromide, respectively, after reaction of hydrogen gas with a metal halide or metal sulfate, respectively. May result in hydroacid, hydrogen iodide, hydroiodic acid, or sulfuric acid. In some embodiments, the hydrogen gas is from an external source. In some embodiments, such as those illustrated in FIGS. 4A or 4B, the hydrogen gas that reacts with the metal halide or metal sulfate is the hydrogen gas formed at the cathode. In some embodiments, the hydrogen gas is obtained from a combination of an external source and hydrogen gas formed at the cathode. In some embodiments, the reaction of the metal halide or metal sulfate with hydrogen gas results in the generation of the above products, and the lower oxidation state metal halide or metal sulfate. The lower oxidation state metal ions may then be recycled back to the electrochemical system for generation of higher oxidation state metal ions.

An example of the electrochemical system of FIG. 5A is as illustrated in FIG. The system 600 of FIG. 6 is for exemplary purposes only, other metal ions having different oxidation states (eg, chromium, tin, etc.) and products other than alkali in the cathode chamber, eg, water (as in FIG. 5B). ) Or other electrochemical systems that form hydrogen gas (as in FIGS. 4A or 4B) should be understood to be equally applicable to the systems described above. In some embodiments, as illustrated in FIG. 6, electrochemical system 600 includes an oxygen depolarized cathode that generates hydroxide ions from water and oxygen. The system 600 also includes an anode that converts metal ions from a 2+ oxidation state to a 3+ oxidation state (or from a 2+ oxidation state to a 4+ oxidation state, eg, Sn). M ³⁺ ions combine with chloride ions to form MCl ₃ . The metal chloride MCl ₃ then reacts with hydrogen gas and undergoes metal ion reduction to a lower oxidation state to form MCl ₂ . MCl ₂ is then recycled back to the anode chamber for conversion to MCl ₃ . Hydrochloric acid is generated in the process, which may be used for commercial purposes, or may be utilized in other processes as described herein. In some embodiments, the HCl produced by this method can be used for mineral dissolution to generate a divalent cation, wherein the divalent cation is as described herein. Can be used in a simple carbonate precipitation process. In some embodiments, the metal halide or metal sulfate in FIG. 6 may react with an unsaturated or saturated hydrocarbon to form a halohydrocarbon or sulfohydrocarbon as described herein ( Not shown). In some embodiments, the cathode is not a gas diffusion cathode, but is a cathode as described in FIGS. 4A or 4B. In some embodiments, the system 600 can be applied to any electrochemical system that produces alkali.

Some examples of reactors in which a reaction between a metal compound and hydrogen gas takes place are provided herein. As an example, a reactor, for example a reaction column for the reaction of higher oxidation state metal ions (formed as shown) with hydrogen gas, is illustrated in FIG. 7A. In some embodiments, the anolyte is passed through a reaction column, as illustrated in FIG. 7A. A gas containing hydrogen is also delivered to the reaction column. Excess hydrogen gas may exit the reaction tower, which may be collected and transferred back to the reaction tower. Inside the reaction tower, an anolyte containing higher oxidation state metal ions (exemplified as FeCl ₃ ) reacts with hydrogen gas and is exemplified as HCl and lower oxidation state metal ions, ie FeCl _2. A reduced form of the metal ion. The reaction tower may optionally contain activated carbon or activated carbon, or alternatively the activated carbon may be present outside the reaction tower. The reaction between the metal ions and hydrogen gas may occur on the activated carbon (from which the reduced anolyte may be regenerated) or the activated carbon simply removes impurities from the gas. It may act as a filter. Reduced anolytes containing HCl and lower oxidation state metal ions include, but are not limited to, separation techniques or acid letters known in the art, including ion exchange resins, size exclusion membranes, and acid dialysis. It can be subjected to acid recovery using a foundation technology to separate HCl from the anolyte. In some embodiments, the ligands described herein can facilitate the separation of metal ions from acidic solutions due to the large size of the ligand bound to the metal ions. An anolyte containing lower oxidation state metal ions may be recycled back to the electrochemical cell and HCl may be collected.

As another example of a reactor, the reaction of higher oxidation state metal ions (formed as shown in the figure) with hydrogen gas is also illustrated in FIG. 7B. As illustrated in FIG. 7B, the anolyte from the anode chamber containing higher oxidation state metal ions such as, but not limited to, Fe ³⁺ , Sn ⁴⁺ , Cr ³⁺ is used to react with hydrogen gas, HCl may be formed or used to purify the SO ₂ containing gas to form a clean gas or sulfuric acid. In some embodiments, it is contemplated that NOx gas may react with higher oxidation state metal ions to form nitric acid. In some embodiments, the anolyte is passed through a reaction tower, as illustrated in FIG. 7B. A gas containing hydrogen, SO ₂ and / or NOx is also delivered to the reaction column. Excess hydrogen gas may be discharged from the reaction tower, which may be collected and moved back to the reaction tower. Excess SO ₂ may be passed through the scrubber before releasing the cleaner gas to the atmosphere. An anolyte containing higher oxidation state metal ions inside the reaction column reacts with hydrogen gas and / or SO _2, and HCl and / or H ₂ SO ₄ and lower oxidation state metal ions, ie reduction Can form the metal ions in the formed form. The reaction tower may optionally contain activated carbon or activated carbon, or alternatively the activated carbon may be present outside the reaction tower. The reaction of the metal ions with hydrogen gas or SO ₂ gas may take place on the activated carbon (from which the reduced anolyte may be regenerated) or the activated carbon can simply be an impurity from the gas. It may act as a filter for removing. Reduced anolytes containing HCl and / or H ₂ SO ₄ and lower oxidation state metal ions are known in the art including, but not limited to, ion exchange resins, size exclusion membranes, acid dialysis, and the like. It can be subjected to acid recovery using known separation techniques to separate HCl and / or H ₂ SO ₄ from the anolyte. In some embodiments, the ligands described herein can facilitate the separation of metal ions from acidic solutions due to the large size of the ligand bound to the metal ions. The anolyte containing the lower oxidation state metal ions may be recycled back to the electrochemical cell and HCl and / or H ₂ SO ₄ may be collected. In some embodiments, the reaction inside the reaction column can occur at a temperature of 50-100 ° C. for 1-10 hours.

An example of an ion exchange resin for separating HCl from a metal-containing anolyte is as illustrated in FIG. 7C. As illustrated in FIG. 7C, the separation process may include preferential adsorption / absorption of mineral acid on the anion exchange resin. In a first step, the anolyte containing HCl and / or _H 2 SO _4, to adsorb HCl and / or _H 2 SO _4, then passed through an ion exchange resin to separate the anolyte. HCl and / or H ₂ SO ₄ can be regenerated from the resin by washing the resin with water. Diffusion dialysis may be another method for separating the acid from the anolyte. In some embodiments, the ligands described herein can facilitate the separation of metal ions from acidic solutions due to the large size of the ligand bound to the metal ions.

In some embodiments, the hydrochloric acid generated in the process is used partially or completely to dissolve the scrap iron and form FeCl ₂ and hydrogen gas. FeCl ₂ generated in the process may be recycled back to the anode chamber for conversion to FeCl ₃ . In some embodiments, hydrogen gas may be used in a hydrogen fuel cell. A fuel cell can also be used to generate electricity that powers the electrochemical articles described herein. In some embodiments, hydrogen gas is fed into the electrochemical system described in US Provisional Patent Application No. 61 / 477,097, which is hereby incorporated by reference in its entirety. Move.

  In some embodiments, hydrochloric acid with or without lower oxidation state metal ions is subjected to another electrochemical process to generate hydrogen gas and higher oxidation state metal ions. Such a system is as illustrated in FIG.

In some embodiments, hydrochloric acid generated in the process is used to generate ethylene dichloride as exemplified below.
2CuCl (aq) + 2HCl (aq) + 1 / 2O ₂ (g) → 2CuCl ₂ (aq) + H ₂ O (l)
C ₂ H ₄ (g) + 2CuCl ₂ (aq) → 2CuCl (aq) + C ₂ H ₄ Cl ₂ (l)

  In some embodiments, the metal formed with a higher oxidation state in the anode electrolyte of the electrochemical system of FIGS. 1A, 1B, 2, 3A, 3B, 4A, 4B, 5A, 5B, and 5C is Can react with unsaturated hydrocarbons to form the corresponding halo or sulfo hydrocarbons based on the anion bound to the metal. For example, metal chlorides, metal bromides, metal iodides, metal sulfates, etc. may be reacted with the corresponding chlorohydrocarbons, bromohydrocarbons, iodocarbons after the reaction of unsaturated hydrocarbons with metal halides or metal sulfates. Hydrogen, or sulfohydrocarbon may be provided. In some embodiments, the reaction of a metal halide or metal sulfate with an unsaturated hydrocarbon results in the generation of the above product, and a lower oxidation state metal halide or metal sulfate. The lower oxidation state metal ions may then be recycled back to the electrochemical system to generate higher oxidation state metal ions.

"Unsaturated hydrocarbon", as used herein, is a hydrocarbon having an unsaturated carbon, or a hydrocarbon having at least one double bond and / or at least one triple bond between adjacent carbon atoms. including. The unsaturated hydrocarbon may be linear, branched, or cyclic (aromatic or non-aromatic). For example, the hydrocarbon may be olefinic, acetylenic, non-aromatic, such as cyclohexene, aromatic groups or substituted unsaturated hydrocarbons (including but not limited to, halogenated unsaturated hydrocarbons). A hydrocarbon having at least one double bond may be referred to as an olefin or alkene, and may have the general formula of unsubstituted alkene as C _n H _2n , where n is 2 to 20, or 2 to 2 10, or 2-8, or 2-5. In some embodiments, the one or more hydrogens on the alkene include, but are not limited to, halogen (including chloro, bromo, iodo, and fluoro), carboxylic acid (—COOH), hydroxyl (—OH) , May be further substituted with other functional groups such as amines. Unsaturated hydrocarbons include, but are not limited to, all unsaturated isomeric forms such as cis and trans isomers, E and Z isomers, positional isomers.

In some embodiments, the unsaturated hydrocarbon in the methods and systems provided herein is of Formula I that results in a compound of Formula II after halogenation or sulfonation (including sulfation);

In the formula, n is 2 to 10, m is 0 to 5, q is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), where R ′ and R ″ are independently from hydrogen, alkyl, and substituted alkyl. Selected
X is a halogen selected from fluoro, chloro, bromo, and iodo; —SO ₃ H; or —OSO ₂ OH.

  It should be understood that the R substituent (s) can be on one carbon atom or on more than one carbon atom, depending on the number of R and carbon atoms. By way of example only, when n is 3 and m is 2, the substituent R may be on the same carbon atom or on two different carbon atoms.

  In some embodiments, the unsaturated hydrocarbon in the methods and systems provided herein is of Formula I, which results in a compound of Formula II after halogenation, wherein n is 2-10. M is 0-5, q is 1-5, R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), wherein Wherein R ′ and R ″ are independently selected from hydrogen, alkyl, and substituted alkyl, and X is a halogen selected from chloro, bromo, and iodo.

  In some embodiments, the unsaturated hydrocarbon in the methods and systems provided herein is of Formula I, which results in a compound of Formula II after halogenation, wherein n is from 2 to 5 M is 0-3, q is 1-4, R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), wherein Wherein R ′ and R ″ are independently selected from hydrogen and alkyl, and X is a halogen selected from chloro and bromo.

  In some embodiments, the unsaturated hydrocarbon in the methods and systems provided herein is of Formula I, which results in a compound of Formula II after halogenation, wherein n is from 2 to 5 Yes, m is 0-3, q is 1-4, R is independently selected from hydrogen, halogen, and -OH, and X is a halogen selected from chloro and bromo.

  It should be understood that when m is greater than 1, the substituents R may be on the same carbon atom or on different carbon atoms. Similarly, when q is greater than 1, it should be understood that the substituents X may be on the same carbon atom or on different carbon atoms.

  In some embodiments for the above embodiments of Formula I, m is 0 and q is 1-2. In such embodiments, X is chloro.

Examples of substituted or unsubstituted alkenes comprising Formula I include, but are not limited to, ethylene, chloroethylene, bromoethylene, iodoethylene, propylene, chloropropylene, hydroxylpropylene, 1-butylene, 2-butylene (cis or trans ), Isobutylene, 1,3-butadiene, pentylene, hexene, cyclopropylene, cyclobutylene, cyclohexene and the like. Hydrocarbons having at least one triple bond may be referred to as alkynes and may have the general formula of unsubstituted alkynes as C _n H _2n-2 , where n is 2-10, or 2 -8, or 2-5. In some embodiments, one or more hydrogens on the alkyne may be further substituted with other functional groups such as, but not limited to, halogen, carboxylic acid, hydroxyl.

In some embodiments, the unsaturated hydrocarbon in the methods and systems provided herein is of Formula IA that results in a compound of Formula IIA after halogenation or sulfonation (including sulfation);

In the formula, n is 2 to 10, m is 0 to 5, q is 1 to 5, and R is hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″) Independently selected from where R ′ and R ″ are independently selected from hydrogen, alkyl, and substituted alkyl;
X is a halogen selected from fluoro, chloro, bromo, and iodo; —SO ₃ H; or —OSO ₂ OH.

  Examples of substituted or unsubstituted alkynes include, but are not limited to, acetylene, propyne, chloropropyne, bromopropyne, butyne, pentyne, hexyne and the like.

  It should be understood that the R substituent (s) can be on one carbon atom or on more than one carbon atom, depending on the number of R and carbon atoms. By way of example only, when n is 3 and m is 2, the substituent R may be on the same carbon atom or on two different carbon atoms.

  In some embodiments, contacting the metal ions in the anode electrolyte in the anode chamber with the anode; converting or oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode; Treating an anode electrolyte comprising a higher oxidation state metal ion with an unsaturated hydrocarbon. In some embodiments of the above method, the method includes contacting the cathode with a cathode electrolyte and forming alkali at the cathode. In some embodiments of the above methods, the method includes contacting the cathode with a cathode electrolyte and forming alkali, water, and / or hydrogen gas at the cathode. In some embodiments of the above method, the method includes contacting the gas diffusion cathode and the cathode electrolyte and forming alkali or water at the cathode. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and the cathode and cathode electrolyte A step of forming an alkali, water and / or hydrogen gas at the cathode, and treating an anode electrolyte comprising higher oxidation state metal ions with an unsaturated hydrocarbon. provide. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and a gas diffusion cathode; A method is provided that includes contacting a cathode electrolyte, forming alkali or water at the cathode, and treating an anode electrolyte comprising higher oxidation state metal ions with an unsaturated hydrocarbon. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and a gas diffusion cathode; A method is provided that includes contacting a cathode electrolyte, forming alkali at the cathode, and treating an anode electrolyte comprising higher oxidation state metal ions with an unsaturated hydrocarbon. In some embodiments, treatment of unsaturated hydrocarbons with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, treatment of higher oxidation state metal ions with unsaturated hydrocarbons results in chloro, bromo, iodo, or sulfohydrocarbons and lower oxidation state metal ions. In some embodiments, lower oxidation state metal ions may be recycled back to the anode chamber.

  In some embodiments of the above method, the anode does not produce chlorine gas. In some embodiments of the above method, treatment of unsaturated hydrocarbons with higher oxidation state metal ions does not require oxygen gas and / or chlorine gas. In some embodiments of the above method, the anode does not produce chlorine gas, and treatment of unsaturated hydrocarbons with higher oxidation state metal ions does not require oxygen gas and / or chlorine gas.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. An anode chamber; and a reactor operatively connected to the anode chamber and configured to react the unsaturated hydrocarbon with an anode electrolyte comprising metal ions in a higher oxidation state; Provide a system. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali, water, and / or hydrogen gas in the cathode electrolyte. . In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali and / or hydrogen gas in the cathode electrolyte. In some embodiments of the above system, the system includes a gas diffusion cathode with a cathode electrolyte, the cathode configured to form alkali or water in the cathode electrolyte. In some embodiments, an anode chamber comprising an anode having metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. A cathode chamber comprising a cathode having a cathode electrolyte, wherein the cathode is configured to form alkali, water or hydrogen gas in the cathode electrolyte; operable in the anode chamber And a reactor configured to react the unsaturated hydrocarbon with an anode electrolyte that is connected to and comprising a higher oxidation state metal ion. In some embodiments, an anode chamber comprising an anode having metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. A cathode chamber comprising a gas diffusion cathode having a cathode electrolyte, the cathode chamber being configured to form alkali in the cathode electrolyte; operably connected to the anode chamber And a reactor configured to react the unsaturated hydrocarbon with an anode electrolyte containing higher oxidation state metal ions. In some embodiments, treatment of unsaturated hydrocarbons with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, treatment of higher oxidation state metal ions with unsaturated hydrocarbons results in chloro, bromo, iodo, or sulfohydrocarbons and lower oxidation state metal ions. In some embodiments, the system forms a lower oxidation state metal ion from a higher oxidation state metal ion with an unsaturated hydrocarbon and recirculates the lower oxidation state metal ion back to the anode chamber. It is configured to let you.

  In some embodiments, the unsaturated hydrocarbon in the method and system embodiments described above and as described herein is of Formula I or a C2-C10 alkene or C2-C5 alkene. It is. In some embodiments of the methods and systems as described above, the unsaturated hydrocarbon in the above embodiments and as described herein is ethylene. Halohydrocarbons formed from such unsaturated hydrocarbons are those of formula II (described herein), such as ethylene dichloride, chloroethanol, butyl chloride, dichlorobutane, chlorobutanol, and the like. In some embodiments of the methods and systems as described above, the metal ion is a metal ion described herein such as, but not limited to, copper, iron, tin, or chromium.

  In some embodiments of the above system, the anode is configured not to produce chlorine gas. In some embodiments of the above system, the reactor configured to react unsaturated hydrocarbons with higher oxidation state metal ions does not require oxygen gas and / or chlorine gas. It is configured. In some embodiments of the above method, the anode is configured not to produce chlorine gas and the reactor is configured not to require oxygen gas and / or chlorine gas.

An example of the electrochemical system of FIG. 5A is as illustrated in FIG. 8A. The system 800 of FIG. 8A is for exemplary purposes only and forms other metal ions having different oxidation states, other unsaturated hydrocarbons, and non-alkali products such as water or hydrogen gas in the cathode chamber. It should be understood that other electrochemical systems are equally applicable to the above system. The cathode of FIG. 4A or 4B can also be replaced in FIG. 8A. In some embodiments, as illustrated in FIG. 8A, electrochemical system 800 includes an oxygen depolarized cathode that generates hydroxide ions from water and oxygen. System 800 also includes an anode that converts metal ions from a 1+ oxidation state to a 2+ oxidation state. Cu ²⁺ ions combine with chloride ions to form CuCl ₂ . The metal chloride CuCl ₂ then reacts with an unsaturated hydrocarbon such as, but not limited to, ethylene, to reduce the metal ion to a lower oxidation state, CuCl, and without limitation, ethylene dichloride. A dichlorohydrocarbon such as can be formed. Then, CuCl is recirculated back to the anode chamber for conversion to CuCl _2.

  The ethylene dichloride formed by the method and system of the present invention can be used for any commercial purpose. In some embodiments, ethylene dichloride is subjected to vinyl chloride monomer (VCM) formation by a process such as cracking / purification. Vinyl chloride monomer can be used in the production of polyvinyl chloride. In some embodiments, the hydrochloric acid formed during the conversion of EDC to VCM can be separated and reacted with acetylene to further form VCM.

In some embodiments, HCl generated in the process of VCM formation may be circulated to one or more of the electrochemical systems described herein, where HCl is the cathode or anode electrolyte. Used to form hydrogen gas or water at the cathode. As in FIG. 8B, the integrated electrochemical system of the present invention is illustrated in combination with VCM / PVC synthesis. The electrochemical system of the present invention, such as any of the systems illustrated in FIGS. 1B, 2, 4A or 5A, may be used to form CuCl ₂ , which results in EDC when reacted with ethylene . EDC cracking and subsequent treatment of VCM produce HCl, which can be circulated to either the electrochemical system of FIG. 4B or 5B to further form CuCl ₂ . It should be understood that the entire process can be performed only with the system of FIG. 4B or 5B (ie, does not incorporate the system of FIG. 1B, 2, 4A or 5A).

  In some embodiments, chlorination of ethylene in an aqueous medium having a higher oxidation state metal chloride results in ethylene dichloride, chloroethanol, or a combination thereof. In some embodiments of the methods and systems described herein, more than 10% by weight from ethylene; or more than 20%, or more than 30%, or more than 40%, or more than 50% by weight. Or more than 60 wt%, or more than 70 wt%, or more than 80 wt%, or more than 90 wt%, or more than 95 wt%, or about 99 wt%, or between about 10 to 99 wt%, or about 10 Between ˜95 wt%, or between about 15 and 95 wt%, or between about 25 and 95 wt%, or between about 50 and 95 wt%, or between about 50 and 99 wt% Or about 50 to 99.9% by weight of ethylene dichloride, or about 50 to 99.99% by weight of ethylene dichloride. In some embodiments, the remaining weight percent is chloroethanol. In some embodiments, no chloroethanol is formed in the reaction. In some embodiments, less than 0.001 wt% or less than 0.01 wt% or less than 0.1 wt% or less than 0.5 wt% or less than 1 wt% or less than 5 wt% or less than 10 wt% or Less than 20% by weight of chloroethanol is formed with the rest of the EDC in the reaction. In some embodiments, less than 0.001 wt%, or less than 0.01 wt%, or less than 0.1 wt%, or less than 0.5 wt%, or less than 1 wt%, or less than 5 wt% of metal ions are EDC Present in the product. In some embodiments, less than 0.001 wt% or less than 0.01 wt% or less than 0.1 wt% chloroethanol and / or metal ions are present in the EDC product.

In some embodiments, the EDC product containing metal ions may be subjected to a washing step that may include rinsing with an organic solvent or passing the EDC product through a column to remove metal ions. In some embodiments, the EDC product may be purified by distillation, wherein by-products such as chloral (CCl ₃ CHO) and / or chloral hydrate (2,2,2-trichloroethane-1 , 1-diol) can be separated if formed.

In some embodiments, the unsaturated hydrocarbon is propene. In some embodiments, a higher oxidation state metal ion, eg, CuCl ₂ , is treated with propene to provide propane dichloride (C ₃ H ₆ Cl ₂ ) or dichloropropane (DCP), which is chlorinated. Can be used to make allyl (C ₃ H ₅ Cl). In some embodiments, the unsaturated hydrocarbon is butane or butylene. In some embodiments, higher oxidation state metal ions such as CuCl ₂ are treated with butene, resulting in butane dichloride (C ₄ H ₈ Cl ₂ ) or dichlorobutene (C ₄ H ₆ Cl ₂ ). This can be used to make chloroprene (C ₄ H ₅ Cl). In some embodiments, the unsaturated hydrocarbon is benzene. In some embodiments, a higher oxidation state metal ion, eg, CuCl ₂ , is treated with benzene to provide chlorobenzene. In some embodiments, the higher oxidation state metal ions, for example, the CuCl ₂ is treated with acetylene, chloro acetylene, dichloroacetylene, vinyl chloride, dichloroethene, tetrachloroethene, or a combination thereof is brought. In some embodiments, the unsaturated hydrocarbon is treated with a higher oxidation state metal chloride, including but not limited to ethylene dichloride, chloroethanol, chloropropene, propylene oxide (and further dehydrochlorinated). Allyl chloride, methyl chloride, trichloroethylene, tetrachloroethene, chlorobenzene, 1,2-dichloroethane, 1,1,2-trichloroethane, 1,1,2,2-tetrachloroethane, pentachloroethane, 1,1-dichloroethene, Form a product containing chlorophenol, chlorinated toluene and the like.

  In some embodiments, the yield of halogenated hydrocarbons from unsaturated hydrocarbons using metal ions, such as the yield of EDC from ethylene, or the yield of DCP from propylene, or from butene Dichlorobutene is more than 90% or more than 95% or between 90 and 95% or between 90 and 99% or between 90 and 99.9%. In some embodiments, the selectivity of halogenated hydrocarbons from unsaturated hydrocarbons using metal ions, such as the yield of EDC from ethylene, or the yield of DCP from propylene, or from butene. Dichlorobutene is greater than 80% or 90% or between 80 and 99% by weight. In some embodiments, STY (space time yield) of halogenated hydrocarbons from unsaturated hydrocarbons using metal ions, eg, yield of EDC from ethylene, or yield of DCP from propylene Or dichlorobutene from butene is greater than 3, or greater than 4, or greater than 5, or between 3 and 5 or between 3 and 6 or between 3 and 8.

  In some embodiments, the metal formed with a higher oxidation state in the anode electrolyte of the electrochemical system of FIGS. 1A, 1B, 2, 3A, 3B, 4A, 4B, 5A, and 5B is saturated. Based on the anion bound to the metal reacting with the hydrocarbon, the corresponding halohydrocarbon or sulfohydrocarbon can be formed. For example, metal chlorides, metal bromides, metal iodides, metal sulfates, etc., after the reaction of saturated hydrocarbons with metal halides or metal sulfates, the corresponding chlorohydrocarbons, bromohydrocarbons, iodohydrocarbons Or may result in a sulfohydrocarbon. In some embodiments, the reaction of a metal halide or metal sulfate with a saturated hydrocarbon results in the generation of the above product, and a lower oxidation state metal halide or metal sulfate. The lower oxidation state metal ions may then be recycled back to the electrochemical system in order to generate higher oxidation state metal ions.

“Saturated hydrocarbon”, as used herein, includes hydrocarbons that have neither unsaturated carbons nor unsaturated hydrocarbons. The hydrocarbon may be linear, branched or cyclic. For example, the hydrocarbon may be a substituted or unsubstituted alkane and / or a substituted or unsubstituted cycloalkane. The hydrocarbon may have the general formula of unsubstituted alkanes as C _n H _{2n + 2} , where n is 2-20 or 2-10 or 2-8, or 2-5. In some embodiments, the one or more hydrogens on the alkane or cycloalkane include, but are not limited to, halogen (including chloro, bromo, iodo, and fluoro), carboxylic acid (—COOH), hydroxyl ( -OH), may be further substituted with other functional groups such as amines.

In some embodiments, the saturated hydrocarbon in the methods and systems provided herein is of formula III that results in a compound of formula IV after halogenation or sulfonation (including sulfation);

In the formula, n is 2 to 10, k is 0 to 5, s is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), R ′ and R ″ are independently selected from hydrogen, alkyl, and substituted alkyl;
X is a halogen selected from fluoro, chloro, bromo, and iodo; —SO ₃ H; or —OSO ₂ OH.

  It should be understood that the R substituent (s) can be on one carbon atom or on more than one carbon atom, depending on the number of R and carbon atoms. By way of example only, when n is 3 and k is 2, the substituents R may be on the same carbon atom or on two different carbon atoms.

In some embodiments, the saturated hydrocarbon in the methods and systems provided herein is of formula III, which results in a compound of formula IV after halogenation;
In the formula, n is 2 to 10, k is 0 to 5, s is 1 to 5,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), where R ′ and R ″ are independently from hydrogen, alkyl, and substituted alkyl. Selected
X is a halogen selected from chloro, bromo, and iodo.

In some embodiments, the saturated hydrocarbon in the methods and systems provided herein is of formula III, which results in a compound of formula IV after halogenation;
In the formula, n is 2 to 5, k is 0 to 3, s is 1 to 4,
R is independently selected from hydrogen, halogen, —COOR ′, —OH, and —NR ′ (R ″), wherein R ′ and R ″ are independently selected from hydrogen and alkyl;
X is a halogen selected from chloro and bromo.

In some embodiments, the saturated hydrocarbon in the methods and systems provided herein is of formula III, which results in a compound of formula IV after halogenation;
In the formula, n is 2 to 5, k is 0 to 3, s is 1 to 4,
R is independently selected from hydrogen, halogen, and -OH;
X is a halogen selected from chloro and bromo.

  It should be understood that when k is greater than 1, the substituents R may be on the same carbon atom or on different carbon atoms. Similarly, it should be understood that when s is greater than 1, the substituents X may be on the same carbon atom or on different carbon atoms.

  In some embodiments for the above embodiments of Formula III, k is 0 and s is 1-2. In such embodiments, X is chloro.

  For example, examples of substituted or unsubstituted alkanes of formula III include, but are not limited to, methane, ethane, chloroethane, bromoethane, iodoethane, propane, chloropropane, hydroxypropane, butane, chlorobutane, hydroxybutane, pentane, hexane, cyclohexane , Cyclopentane, chlorocyclopentane, and the like.

  In some embodiments, contacting the metal ions in the anode electrolyte in the anode chamber with the anode; converting or oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode; Treating an anode electrolyte comprising higher oxidation state metal ions with saturated hydrocarbons. In some embodiments of the above method, the method includes contacting the cathode with a cathode electrolyte and forming alkali at the cathode. In some embodiments of the above methods, the method includes contacting the cathode with a cathode electrolyte and forming alkali and hydrogen gas at the cathode. In some embodiments of the above method, the method includes contacting the cathode with a cathode electrolyte and forming hydrogen gas at the cathode. In some embodiments of the above method, the method includes contacting the gas diffusion cathode with a cathode electrolyte and forming alkali at the cathode. In some embodiments of the above method, the method includes contacting the gas diffusion cathode and the cathode electrolyte and forming water at the cathode. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and the cathode and cathode electrolyte A step of forming an alkali, water, and / or hydrogen gas at the cathode, and treating an anode electrolyte comprising higher oxidation state metal ions with saturated hydrocarbons. To do. In some embodiments, contacting the anode with a metal ion in the anode electrolyte in the anode chamber, converting the metal ion from a lower oxidation state to a higher oxidation state at the anode, and a gas diffusion cathode; A method is provided comprising: contacting a cathode electrolyte; forming alkali or water at the cathode; and treating an anode electrolyte comprising higher oxidation state metal ions with a saturated hydrocarbon. In some embodiments, treatment of saturated hydrocarbons with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, treatment of higher oxidation state metal ions with saturated hydrocarbons may include halogenated hydrocarbons or sulfohydrocarbons, such as chloro, bromo, iodo, or sulfohydrocarbons, and lower oxidation state. Brings metal ions. In some embodiments, lower oxidation state metal ions may be recycled back to the anode chamber. In some embodiments, the saturated hydrocarbon in the above embodiments and as described herein is of formula III (described herein) or a C2-C10 alkane or C2-C5. It is an alkane. In some embodiments, the saturated hydrocarbon in the above embodiments and as described herein is methane. In some embodiments, the saturated hydrocarbon in the above embodiments and as described herein is ethane. In some embodiments, the saturated hydrocarbon in the above embodiments and as described herein is propane. Halohydrocarbons formed from such saturated hydrocarbons are those of formula IV (described herein), such as chloromethane, dichloromethane, chloroethane, dichloroethane, chloropropane, dichloropropane, and the like.

  In some embodiments of the above method, the metal ions used are platinum, palladium, copper, iron, tin, and chromium. In some embodiments of the above method, the anode does not produce chlorine gas. In some embodiments of the above method, treatment of saturated hydrocarbons with higher oxidation state metal ions does not require oxygen gas and / or chlorine gas. In some embodiments of the above method, the anode does not produce chlorine gas, and the treatment of saturated hydrocarbons with higher oxidation state metal ions does not require oxygen gas and / or chlorine gas.

  In some embodiments, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state. A system comprising: an anode chamber; and a reactor operably connected to the anode chamber and configured to react a saturated hydrocarbon with an anode electrolyte containing metal ions in a higher oxidation state I will provide a. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali at the cathode. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form hydrogen gas at the cathode. In some embodiments of the system, the system includes a cathode chamber that includes a cathode having a cathode electrolyte, the cathode configured to form alkali and hydrogen gas at the cathode. In some embodiments of the system, the system includes a gas diffusion cathode with a cathode electrolyte, the cathode configured to form alkali at the cathode. In some embodiments of the system, the system includes a gas diffusion cathode with a cathode electrolyte, the cathode configured to form water at the cathode. In some embodiments, an anode chamber comprising an anode having metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. A cathode chamber comprising a cathode having a cathode electrolyte, the cathode chamber being configured to form alkali, water, and hydrogen gas in the cathode electrolyte; operating in the anode chamber A system is provided that includes an anode electrolyte that is operatively connected and that is configured to react a saturated hydrocarbon with an anode electrolyte that includes higher oxidation state metal ions. In some embodiments, an anode chamber comprising an anode having metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. A cathode chamber comprising a gas diffusion cathode having a cathode electrolyte, wherein the cathode is configured to form alkali or water in the cathode electrolyte; operably in the anode chamber A system is provided that includes an anode electrolyte that is connected and includes a metal oxide in a higher oxidation state and a reactor configured to react a saturated hydrocarbon. In some embodiments, treatment of saturated hydrocarbons with higher oxidation state metal ions may be inside the cathode chamber or outside the cathode chamber. In some embodiments, treatment of higher oxidation state metal ions with saturated hydrocarbons results in chloro, bromo, iodo, or sulfohydrocarbons and lower oxidation state metal ions. In some embodiments, the system forms a lower oxidation state metal ion from a higher oxidation state metal ion with saturated hydrocarbons and recirculates the lower oxidation state metal ion back to the anode chamber. It is configured as follows.

  In some embodiments of the methods and systems as described above, the metal ion is a metal ion described herein, such as, but not limited to, platinum, palladium, copper, iron, tin, or chromium. It is.

  In some embodiments of the above system, the anode is configured not to produce chlorine gas. In some embodiments of the above system, the reactor configured to react saturated hydrocarbons with higher oxidation state metal ions is configured to not require oxygen gas and / or chlorine gas. Has been. In some embodiments of the above method, the anode is configured not to produce chlorine gas and the reactor is configured not to require oxygen gas and / or chlorine gas.

  It should be understood that the example electrochemical system illustrated in FIG. 8A can be configured for saturated hydrocarbons by replacing unsaturated hydrocarbons with saturated hydrocarbons. Thus, suitable metal ions such as platinum chloride, palladium chloride, copper chloride and the like can be used.

  In some embodiments, chlorination of ethane in an aqueous medium having a higher oxidation state metal chloride results in ethane chloride, ethane dichloride, or combinations thereof. In some embodiments of the methods and systems described herein, more than 10% by weight from ethane; or more than 20%, or more than 30%, or more than 40%, or more than 50% by weight. Or more than 60 wt%, or more than 70 wt%, or more than 80 wt%, or more than 90 wt%, or more than 95 wt%, or about 99 wt%, or between about 10 to 99 wt%, or about 10 Between -95 wt%, or between about 15-95 wt%, or between about 25-95 wt%, or between about 50-95 wt%, or between about 50-99 wt%, or about 50 There is a formation of chloroethane between ˜99.9 wt%, or between about 50-99.99 wt%. In some embodiments, the remaining weight percent is chloroethanol and / or ethylene dichloride. In some embodiments, no chloroethanol is formed in the reaction. In some embodiments, less than 0.001 wt% or less than 0.01 wt% or less than 0.1 wt% or less than 0.5 wt% or less than 1 wt% or less than 5 wt% or less than 10 wt% or Less than 20% by weight of chloroethanol is formed with the remaining product in the reaction. In some embodiments, less than 0.001 wt% or less than 0.01 wt% or less than 0.1 wt% or less than 0.5 wt% or less than 1 wt% or less than 5 wt% metal ions are produced It exists in things. In some embodiments, less than 0.001 wt% or less than 0.01 wt% or less than 0.1 wt% chloroethanol and / or metal ions are present in the product.

  In some embodiments, the yield of halogenated hydrocarbons from saturated hydrocarbons using metal ions, for example, the yield of chloroethane or EDC from ethane is greater than 90% or 95% or 90% Between -95 wt% or between 90-99 wt% or between 90-99.9 wt%. In some embodiments, the selectivity of halogenated hydrocarbons from saturated hydrocarbons using metal ions, such as chloroethane or EDC yield from ethane, is greater than 80% or 90% or 80% by weight. Between ˜99% by weight. In some embodiments, the STY (space time yield) of the halogenated hydrocarbon from the saturated hydrocarbon is greater than 3, or greater than 4, or greater than 5, or between 3 and 5, or 3 to 6. Or between 3-8.

  Products such as, but not limited to, halogenated hydrocarbons, acids, carbonates, and / or bicarbonates formed by the methods and systems of the present invention are formed by methods and systems previously known in the art. It is more environmentally conscious than the same products that are produced. Contacting the anode with the anode electrolyte, oxidizing the metal chloride from a lower oxidation state to a higher oxidation state at the anode, contacting the cathode with the cathode electrolyte, unsaturated or saturated hydrocarbons; And halogenating with a metal oxide in a higher oxidation state to produce an environmentally friendly halogenated hydrocarbon. A method for producing an environmentally friendly halogenated hydrocarbon is provided. In some embodiments, environmentally friendly halogenated hydrocarbons formed by the methods described herein are provided. An anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; a cathode in contact with the cathode electrolyte; operably connected to the anode chamber And a reactor that is configured to react higher-oxidation state metal ions with unsaturated or saturated hydrocarbons to form halogenated hydrocarbons that are environmentally friendly. To do.

  The terms “environmentally friendly” or “environmentally friendly”, or grammatical equivalents thereof, as used herein, refer to the same chemical or product formed by methods known in the art. By comparison, it includes any chemical or product formed by the method and system of the present invention with higher energy or voltage reduction. For example, chloroalkali is a process typically used to make chlorine gas, which is then used to chlorinate ethylene to form EDC. The amount of energy required to make EDC from the chloroalkali process is higher than the amount of energy required to make EDC from the metal oxidation process of the present invention. Thus, the EDC produced by the method and system of the present invention is more environmentally friendly than the EDC produced by the chloroalkali process. Such a reduction in energy is illustrated in FIG. 8C illustrating the activation barrier for performing the method of the present invention compared to the activation barrier for the chloroalkali process.

As illustrated in FIG. 8C, a comparison is made between the energy required to make EDC from the chloroalkali process and the energy required to make EDC from the methods and systems of the present invention. . The process of making EDC is illustrated in two parts. Electrochemical part (compared with the generation of chlorine occurring in the chloroalkali process, copper oxidation occurs in the system 1 and system 2 of the present invention). Catalytic part (in systems 1 and 2) (copper (II) chloride (generated by electrochemistry) chlorinates ethylene, chlorine gas (generated by chloroalkali process) chlorinates ethylene (known previously), Form EDC). In the system 1, the electrochemical reaction is performed in the absence of the ligand, and in the system 2, the electrochemical reaction is performed in the presence of the ligand. In System 1, System 2, and the chloroalkali process, the cathode is a hydrogen gas generating cathode and the current density for the electrochemical reaction is 300 mA / cm ² . As illustrated in FIG. 8C, for the electrochemical reaction, there is an energy reduction of over 125 kJ / mol for the chloroalkali process for system 1 and an energy reduction of over 225 kJ / mol for the chloroalkali process for system 2 . Thus, the method and system of the present invention can be used to produce environmentally friendly halogenated hydrocarbons such as, but not limited to, EDC, as compared to conventional processes, such as the chloroalkali process for making EDC. Up to 300 kJ / mol; or up to 250 kJ / mol; or between 50 and 300 kJ / mol; or between 50 and 250 kJ / mol; or between 100 and 250 kJ / mol; or between 100 and 200 kJ / mol Reductions can be made. This translates to a reduction in EDC of over 1 megawatt hour / ton or between 1 and 21 megawatt hours / ton for systems 1 and 2 compared to the chloroalkali process. This also correlates with a voltage reduction of more than 1V or between 1-2V (1V x 2 electrons is approximately 200 kJ / mol) compared to the chloroalkali process.

  As also illustrated in FIG. 8C, the catalytic part of the reaction has a theoretical low barrier for systems 1 and 2, respectively, and a high barrier for the two systems 1 and 2, respectively. Catalytic reactions in System 1 and System 2 are not limited to these, depending on conditions such as concentration, reactor size, flow rate, etc., at a low barrier point, or at a high barrier point, or somewhere in between. I can get up. Even if there is some energy input to the catalytic reaction in systems 1 and 2, this is offset by significant energy reduction in the electrochemical reaction, up to 100 kJ / mol; or more than 100 kJ / mol; or 50-100 kJ There is a net energy reduction between / mol; or between 0 and 100 kJ / mol. This translates to an EDC of up to 1 megawatt hour / ton or greater than 1 megawatt hour / ton, or a voltage reduction between 0-1 V or over 1 V; or 1-2 V compared to the chloroalkali process. It should be understood that the chloroalkali process, system 1 and system 2 are all performed in an aqueous medium. Electrochemical cells or catalysis systems that run on organic solvents (eg, having some or all of the water from the electrochemical cells removed by azeotropic distillation) require even higher energy than conventional methods, Do not give environment-friendly halogenated hydrocarbons.

  Still further illustrated in FIG. 8C is the reduction of energy in system 2 with the use of ligand compared to system 1 without the use of ligand.

  Thus, contacting the anode with the anode electrolyte, oxidizing the metal chloride from a lower oxidation state to a higher oxidation state at the anode, contacting the cathode with the cathode electrolyte, unsaturated or saturated And halogenating the hydrocarbon with a metal oxide in a higher oxidation state to produce an environmentally friendly halogenated hydrocarbon. Result in a net energy reduction of more than 100 kJ / mol or more than 150 kJ / mol or more than 200 kJ / mol or between 100 and 250 kJ / mol or between 50 and 100 kJ / mol or between 0 and 100 kJ / mol; Is more than 1V or 0-1V or 1-2V It results in a voltage reduction of 0~2V. An anode in contact with the anode electrolyte and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; a cathode in contact with the cathode electrolyte; operably connected to the anode chamber And a reactor that is configured to react higher-oxidation state metal ions with unsaturated or saturated hydrocarbons to form halogenated hydrocarbons that are environmentally friendly. However, the system provides a net energy reduction of more than 100 kJ / mol or more than 150 kJ / mol or more than 200 kJ / mol or between 100 and 250 kJ / mol or between 50 and 100 kJ / mol or between 0 and 100 kJ / mol. Or the system is above 1V or between 0-1V or 1-2V Results in a voltage reduction of between 0~2V.

  All the electrochemical systems and methods described herein are performed in greater than 5% water or greater than 6% water or aqueous media. In one aspect, the method and system provide the advantage of conducting a metal oxidation reaction and a reduction reaction outside the cell (all in aqueous medium) in an electrochemical cell. Applicants have shown that the use of aqueous media in halogenation or sulfonation of unsaturated or saturated hydrocarbons or hydrogen gas not only resulted in high product yields and selectivities (Examples herein). Surprisingly, it resulted in the generation of reduced metal ions having a lower oxidation state in aqueous media (which can be recycled back to the electrochemical system) I found it. In some embodiments, the electrochemical cell operates efficiently in an aqueous medium, so that the anode contains higher oxidation state metal ions that react with unsaturated or saturated hydrocarbons or hydrogen gas in the aqueous medium. It is not necessary to remove water (eg, by azeotropic distillation) from the electrolyte, and minimal removal is not required. Thus, the use of aqueous media in both electrochemical cells and catalysis systems provides an efficient and less energy intensive integrated system and method of the present invention.

  Thus, in some embodiments, contacting the anode with the anode electrolyte, the anode electrolyte comprising metal ions and oxidizing the metal ions from a lower oxidation state to a higher oxidation state at the anode. Contacting the cathode with the cathode electrolyte, and reacting the anode electrolyte containing the higher oxidation state metal ions with an unsaturated or saturated hydrocarbon in an aqueous medium, the aqueous medium comprising: More than 5% by weight water or more than 5.5% by weight or more than 6% by weight or between 5 and 90% by weight or between 5 and 95% by weight or between 5 and 99% by weight water or 5.5 Between ~ 90% or 5.5-95% or 5.5-99% water or 6-90% by weight Or comprising a step of including water during 6 to 95 wt% during or 6-99 wt%, to provide a method. In some embodiments, contacting the anode with an anode electrolyte, the anode electrolyte comprising metal ions, and the metal halide or metal sulfate at the anode from a lower oxidation state to a higher oxidation state. Oxidizing the cathode to the cathode electrolyte, and halogenating or sulfonating the unsaturated or saturated hydrocarbon with a higher oxidation state metal halide or metal sulfate in an aqueous medium. Wherein the aqueous medium is more than 5% or 5.5% or 6% or 5 to 90% or 5 to 95% or 5 to 99% water or Water between 5.5 and 90 wt% or between 5.5 and 95 wt% or between 5.5 and 99 wt% Other comprises the step of including water during or between 6-99 wt% or between 6-95 wt% of 6 to 90 wt%, to provide a method. Unsaturated hydrocarbons (eg, formula I), saturated hydrocarbons (eg, formula III), halogenated hydrocarbons (eg, formulas II and IV), metal ions, and the like have all been described in detail herein.

  In some embodiments, contacting the anode with the anode electrolyte, oxidizing the metal halide or metal sulfate from a lower oxidation state to a higher oxidation state at the anode, and the cathode and cathode electrolyte. Contacting a higher oxidation state metal halide or metal sulfate with hydrogen gas in an aqueous medium to form an acid, such as hydrochloric acid or sulfuric acid, wherein the aqueous medium is 5 More than 5.5% water or more than 5.5% or more than 6% or between 5 and 90% or between 5 and 95% or between 5 and 99% water or between 5.5 and 90% % Or 5.5 to 95% by weight or 5.5 to 99% by weight water or 6 to 90% by weight or 6 to 95% by weight And a step including water during or between 6-99 wt%, to provide a method. In some embodiments, the cathode generates hydroxide ions.

  In some embodiments of the above method, the cathode produces water, alkali, and / or hydrogen gas. In some embodiments of the above method, the cathode is an ODC that produces water. In some embodiments of the above method, the cathode is an ODC that produces alkali. In some embodiments of the above method, the cathode produces hydrogen gas. In some embodiments of the above method, the cathode is an oxygen depolarizing cathode that reduces oxygen and water to hydroxide ions, and the cathode generates hydrogen gas that reduces water to hydrogen gas and hydroxide ions. The cathode is a hydrogen gas generating cathode that reduces hydrochloric acid to hydrogen gas, or the cathode is an oxygen depolarized cathode that reacts hydrochloric acid and oxygen gas to form water.

  In some embodiments of the above method, the metal ion is any metal ion described herein. In some embodiments of the above method, the metal ions are iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold , Nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, the metal ion is selected from the group consisting of iron, chromium, copper, and tin. In some embodiments, the metal ion is copper. In some embodiments, the lower oxidation state of the metal ion is 1+, 2+, 3+, 4+, or 5+. In some embodiments, the higher oxidation state of the metal ion is 2+, 3+, 4+, 5+, or 6+.

  In some embodiments, the method further comprises recycling at least a portion of the lower oxidation state metal ions back to the electrochemical cell. In some embodiments, the method does not perform azeotropic distillation of water prior to reacting the higher oxidation state metal ions with unsaturated or saturated hydrocarbons. In some embodiments, the above method does not produce chlorine gas at the anode. In some embodiments, the above method does not require oxygen gas and / or chlorine gas for chlorination of unsaturated or saturated hydrocarbons to halogenated hydrocarbons.

  In some embodiments, an anode in contact with an anode electrolyte comprising metal ions and configured to oxidize metal ions from a lower oxidation state to a higher oxidation state; in contact with a cathode electrolyte A cathode that is operatively connected to the anode chamber and configured to react an unsaturated electrolyte or a saturated hydrocarbon with an anode electrolyte that includes metal ions in a higher oxidation state in an aqueous medium. Reactor wherein the aqueous medium is greater than 5 wt% water or greater than 5.5 wt% or greater than 6 wt% or between 5 and 90 wt% or between 5 and 95 wt% or between 5 and 99 wt% Between water or between 5.5 and 90% by weight or between 5.5 and 95% by weight or between 5.5 and 99% by weight or between 6 and 90% by weight or 6 And a reactor containing water during or between 6-99 wt% of 95 wt%, to provide a system. In some embodiments, an anode in contact with an anode electrolyte and configured to oxidize a metal halide or metal sulfate from a lower oxidation state to a higher oxidation state at the anode, and a cathode electrolyte Halogenated or sulphonated unsaturated or saturated hydrocarbons with a higher oxidation state metal halide or metal sulfate in an aqueous medium and operably connected to the anode chamber in contact with the anode chamber A reactor configured so that the aqueous medium is more than 5 wt% water or more than 5.5 wt% or 6 wt% or 5 to 90 wt% or 5 to 95 wt% Or between 5 and 99 wt% water or between 5.5 and 90 wt% or between 5.5 and 95 wt% or between 5.5 and 99 wt% And a reactor containing water or 6 to 90 wt.% Or between 6-95 wt% or between 6-99% by weight of water during, provides a system.

  In some embodiments, an anode in contact with an anode electrolyte and configured to oxidize a metal halide or metal sulfate from a lower oxidation state to a higher oxidation state at the anode, and a cathode electrolyte Contacting a cathode in contact with the anode chamber, a metal halide or metal sulfate in a higher oxidation state and hydrogen gas in an aqueous medium, and contacting an acid such as hydrochloric acid Or a reactor configured to form sulfuric acid, wherein the aqueous medium is greater than 5 wt% water or greater than 5.5 wt% or greater than 6 wt% or between 5 and 90 wt% or between 5 and 5 wt% Between 95% by weight or between 5 and 99% by weight water or between 5.5 and 90% by weight or between 5.5 and 95% by weight or between 5.5 and 99% by weight And a reactor containing water during or between 6-99 wt% or between 6-95% by weight of water or 6 to 90% by weight between, providing system.

  In some embodiments of the above system, the cathode is configured to generate hydroxide ions. In some embodiments of the above system, the cathode is configured to produce hydrogen gas. In some embodiments of the above system, the cathode is configured to produce water. In some embodiments of the above system, the cathode is an ODC. In some embodiments of such methods and systems, azeotropic distillation of water is not required to reduce the amount of water in the anode electrolyte. In some embodiments, the system further includes a separator operably connected to the reactor that separates products, eg, acids or halogenated hydrocarbons, from lower oxidation state metal ions. In some embodiments, the system further includes a recirculation system operably connected to the separator and anode chamber of the electrochemical system, the recirculation system comprising at least a lower oxidation state metal ion. A portion is configured to be recycled from the separator back to the electrochemical cell. Such a recirculation system may be a conduit, pipe, tube, etc. that may be used to move the solution. Appropriate control valves and computer control systems may be associated with such recirculation systems.

  In some embodiments, the system is configured not to produce chlorine gas at the anode. In some embodiments, the system is configured such that oxygen gas and / or chlorine gas is not required for chlorination of unsaturated or saturated hydrocarbons to halogenated hydrocarbons.

  In some embodiments, the methods and systems described herein can be used to halogenated hydrocarbons and / or other organic products (herein) before circulating the metal ion solution back to the electrochemical cell. Separating the saturated or unsaturated hydrocarbons (which are formed after the reaction of the saturated or unsaturated hydrocarbons with higher oxidation state metal ions) from the metal ions, as described. In some embodiments, it may be desirable to remove organics from the metal ion solution prior to circulating the metal ion solution back to the electrochemical cell to prevent membrane fouling in the electrochemical cell. . As described hereinabove, after reaction with the unsaturated or saturated hydrocarbon, the aqueous medium containing the metal ions is free of organic products (eg, halogenated hydrocarbons and other by-products (in trace amounts)). May be present), but is not limited to. For example, a metal ion solution containing higher oxidation state metal ions reacts with ethylene to form lower oxidation state metal ions and ethylene dichloride. Other by-products may be formed, including but not limited to chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde (chloral), and the like. A method and system for separating organic products from metal ions in an aqueous medium prior to circulating the aqueous medium containing metal ions back to the electrochemical cell. The aqueous medium may be a mixture of both lower oxidation state metal ions and higher oxidation state metal ions, the ratio of lower oxidation state metal ions to higher oxidation state metal ions being determined by the electrochemical cell. Aqueous medium from which the lower oxidation state is converted to a higher oxidation state, and the aqueous medium after reaction with hydrocarbons (where the higher oxidation state is converted to a lower oxidation state) ).

  In some embodiments, separation of organic products from metal ions in an aqueous medium is performed using an adsorbent. As used herein, “adsorbent” includes compounds that have a high affinity for organic compounds and have no or very low affinity for metal ions. In some embodiments, the adsorbent has no or very low affinity for water in addition to having low or low affinity for metal ions. Have sex. Thus, the adsorbent adsorbs organic matter but may be a hydrophobic compound that repels metal ions and water. As used herein, “organic”, or “organic compound” or “organic product” includes any compound having carbon therein.

  In some embodiments, the method comprises the step of removing organic products from the metal ion solution using an adsorbent (eg, but not limited to activated carbon, alumina, activated silica, polymer, etc.). Including. These adsorbents are commercially available. Examples of activated carbon that can be used in this method include, but are not limited to, powdered activated carbon, granular activated carbon, extruded activated carbon, bead activated carbon, impregnated carbon, polymer coated carbon, carbon cloth, and the like. An “adsorbent polymer” or “polymer” as used herein in the context of an adsorbent has a high affinity for organic compounds, but no or low affinity for metal ions and water. Including polymers with affinity. Examples of polymers that can be used as adsorbents include, but are not limited to, polyolefins. As used herein, “polyolefin” or “polyalkene” includes polymers produced from olefins (or alkenes) as monomers. The olefin or alkene may be an aliphatic compound or an aromatic compound. Examples include polyethylene, polypropylene, polystyrene, polymethylpentene, polybutene-1, polyolefin elastomer, polyisobutylene, ethylene propylene rubber, polymethyl acrylate, poly (methyl methacrylate), and poly (isobutyl methacrylate). However, it is not limited to these.

  In some embodiments, the adsorbent as used herein is from an aqueous medium containing metal ions, organic compounds and water, from more than 90 wt.% Organic compounds, or more than 95 wt.% Organic compounds. Or adsorb more than 99 wt / wt% or more than 99.99 wt / wt% organic compound, or more than 99.999 wt / wt% organic compound. In some embodiments, the adsorbent used herein comprises less than 2 wt / wt% metal ions or less than 1 wt / wt% metal ions from an aqueous medium containing metal ions, organic compounds and water. Or less than 0.1 wt / wt% metal ions, or less than 0.01 wt / wt% metal ions, or less than 0.001 wt / wt% metal ions. In some embodiments, the adsorbent used herein does not adsorb metal ions from aqueous media. In some embodiments, the aqueous medium obtained after passing the adsorbent (and recycled back to the electrochemical cell) is less than 100 ppm, or less than 50 ppm, or less than 10 ppm, or less than 1 ppm organic. Contains compounds.

  The adsorbent can be used in any shape and form that is commercially available. For example, in some method and system embodiments, the adsorbent is in the form of a powder, plate, mesh, bead, cloth, fiber, pill, flake, block, etc. . In some method and system embodiments, the adsorbent is in the form of a bed, packed column, and the like. In some method and system embodiments, the adsorbent may be in the form of a series of beds or columns of packed adsorbent material. For example, in some method and system embodiments, the adsorbent is one or more of packed columns (arranged in parallel or in series) containing activated carbon powder, polystyrene beads or polystyrene powder.

In some method and system embodiments, after adsorption of organic products, various desorption techniques (purging with an inert fluid (eg, water), changing chemical conditions such as pH, increasing temperature, partial pressure, etc. Such as, but not limited to, purge with high temperature inert gas (such as, but not limited to, purge with> 100 ^° C vapor, nitrogen gas, argon gas or air), etc. The adsorbent is regenerated by using (but not limited to).

  In some method and system embodiments, the adsorbent can be disposed of, incinerated, or discarded after the desorption process. In some method and system embodiments, the adsorbent is reused in the adsorption process after desorption. In some method and system embodiments, the adsorbent is reused in multiple adsorption and regeneration cycles prior to disposal. In some method and system embodiments, the adsorbent is reused for 1, 2, 3, 4, 5 or more adsorption and regeneration cycles prior to disposal.

In some embodiments,
Contacting the anode with an anode electrolyte, the anode electrolyte comprising metal ions;
Oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
In an aqueous medium, an unsaturated or saturated hydrocarbon is reacted with an anolyte containing the higher oxidation state metal ion to form one or more organic compounds comprising a halogenated hydrocarbon and the above in an aqueous medium. Forming metal ions in a lower oxidation state;
Separating the one or more organic compounds from an aqueous medium comprising the lower oxidation state metal ions.

  In some embodiments of the above method, the method further comprises recycling an aqueous medium comprising lower oxidation state metal ions back to the anode electrolyte.

  In some embodiments of the above methods, unsaturated hydrocarbons (such as Formula I), saturated hydrocarbons (such as Formula III), halogenated hydrocarbons (such as Formulas II and IV), metal ions, and the like are all herein. Is described in detail.

In some embodiments,
Contacting the anode with an anode electrolyte, the anode electrolyte comprising metal ions;
Oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
One or more organic compounds comprising ethylene dichloride and the lower oxidation state metal ion in aqueous medium by reacting ethylene with an anode electrolyte comprising the higher oxidation state metal ion in an aqueous medium. Forming a step;
Separating the one or more organic compounds from an aqueous medium comprising the lower oxidation state metal ions;
Recycling the aqueous medium containing the lower oxidation state metal ions back to the anode electrolyte.

In some embodiments of the above methods, the aqueous medium is greater than 5 wt% water, or greater than 5.5 wt%, or greater than 6 wt%, or between 5-90 wt%, or 5-95 wt% %, Or 5 to 99% by weight of water, or 5.5 to 90% by weight, or 5.5 to 95% by weight, or 5.5 to 99% by weight of water, Or between 6 and 90 wt%, or between 6 and 95 wt%, or between 6 and 99 wt%. In some embodiments of the above methods, the organic compound further comprises one or more of chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, or combinations thereof. In some embodiments of the above method, the metal ion is copper. The lower oxidation state metal ion is Cu (I) and the higher oxidation state metal ion is Cu (II). In some embodiments of the above method, the metal salt is copper halide. The lower oxidation state metal ion is Cu (I) Cl and the higher oxidation state metal ion is Cu (II) Cl ₂ .

  In some embodiments of the above methods, the step of separating the one or more organic compounds from the aqueous medium that includes lower oxidation state metal ions includes using one or more adsorbents. . In some embodiments of the above method, the adsorbent is activated carbon. In some embodiments of the above method, the adsorbent is not limited to: polyethylene, polypropylene, polystyrene, polymethylpentene, polybutene-1, polyolefin elastomer, polyisobutylene, ethylene propylene rubber, polymethyl acrylate. , Polymers such as polyolefins selected from poly (methyl methacrylate), poly (isobutyl methacrylate) and combinations thereof. In some embodiments of the above method, the adsorbent is polystyrene.

In some embodiments,
Contacting the anode with an anode electrolyte, the anode electrolyte comprising metal ions;
Oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
In an aqueous medium, an unsaturated or saturated hydrocarbon is reacted with an anode electrolyte containing a metal ion in the higher oxidation state, and in the aqueous medium, one or more organic compounds containing a halogenated hydrocarbon and the above Forming metal ions in a low oxidation state;
Separating the one or more organic compounds from an aqueous medium comprising metal ions in a lower oxidation state by using an adsorbent;
Recycling the aqueous medium containing the lower oxidation state metal ions to the anode electrolyte.

In some embodiments,
Contacting the anode with an anode electrolyte, the anode electrolyte comprising metal ions;
Oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
One or more organic compounds comprising ethylene dichloride and the lower oxidation state metal ion in aqueous medium by reacting ethylene with an anode electrolyte comprising the higher oxidation state metal ion in an aqueous medium. Forming a step;
Separating the one or more organic compounds from an aqueous medium comprising metal ions in a lower oxidation state by using an adsorbent;
Recycling the aqueous medium containing the lower oxidation state metal ions to the anode electrolyte.

  In some embodiments, in the above method, the adsorbent is activated carbon. In some embodiments, in the above method, the adsorbent is a polyolefin such as polystyrene.

  In some embodiments of the above methods, the adsorbent is from an aqueous medium, greater than 90% w / w organic compound, or greater than 95% w / w organic compound, or greater than 99% w / w, or 99% Adsorb more than .99 wt / wt% or more than 99.999 wt / wt% organic compounds. In some embodiments of the above method, the aqueous medium obtained after passing the adsorbent (which is recycled back to the anode electrolyte) is less than 100 ppm, or less than 50 ppm, or less than 10 ppm, Alternatively, it contains less than 1 ppm organic compound.

  In some embodiments of the above method, the cathode produces water, alkali and / or hydrogen gas. In some embodiments of the above method, the cathode is an ODC that produces water. In some embodiments of the above method, the cathode is an ODC that produces alkali. In some embodiments of the above method, the cathode produces hydrogen gas. In some embodiments of the above method, the cathode is an oxygen depolarizing cathode that reduces oxygen and water to hydroxide ions, or the cathode is a hydrogen gas generating cathode that reduces water to hydrogen gas and hydroxide ions. The cathode is a hydrogen gas generating cathode that reduces hydrochloric acid to hydrogen gas, or the cathode is an oxygen depolarized cathode that reacts hydrochloric acid and oxygen gas to form water.

  In some embodiments of the above method, the metal ion is any metal ion described herein. In some embodiments of the above method, the metal ions are iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold , Nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, the metal ion is selected from the group consisting of iron, chromium, copper and tin. In some embodiments, the metal ion is copper. In some embodiments, the lower oxidation state of the metal ion is 1+, 2+, 3+, 4+ or 5+. In some embodiments, the higher oxidation state of the metal ion is 2+, 3+, 4+, 5+ or 6+.

In some embodiments,
Contacting the anode with an anode electrolyte, the anode electrolyte comprising copper ions;
Oxidizing copper ions from a lower oxidation state to a higher oxidation state at the anode;
Contacting the cathode with the cathode electrolyte;
One or more organic compounds comprising ethylene dichloride and the lower oxidation state copper ions in aqueous medium by reacting ethylene with an anode electrolyte comprising the higher oxidation state copper ions in aqueous medium. Forming a step;
Using one or more adsorbents selected from activated carbon, polyolefin, activated silica, and combinations thereof, the one or more organic compounds are separated from the aqueous medium containing the lower oxidation state copper ions to 100 ppm. Producing an aqueous medium comprising less than, or less than 50 ppm, or less than 10 ppm, or less than 1 ppm organic compound and copper ions in the lower oxidation state;
Recycling the aqueous medium containing the lower oxidation state copper ions to the anode electrolyte.

  In some embodiments, the methods provided above can further include providing turbulence in the anode electrolyte to improve mass transfer at the anode. Such turbulence at the anode, using a turbulent promoter, is described herein above. In some embodiments, the provided method can further include contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte. Such diffusion enhanced anodes (eg, but not limited to porous anodes) are described herein below.

In some embodiments,
An anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize metal ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
Halogenation is carried out in an aqueous medium by reacting an anode electrolyte operatively connected to the anode chamber and containing the higher oxidation state metal ions with an unsaturated hydrocarbon or saturated hydrocarbon in an aqueous medium. A reactor configured to form one or more organic compounds including hydrocarbons and metal ions of a lower oxidation state;
The one or more organic compounds are operatively connected to a reactor and an anode and separate from the lower oxidation state metal ions and include the lower oxidation state metal ions And a separator configured to recycle the aqueous medium to the anode electrolyte.

  In some embodiments of the above system, unsaturated hydrocarbons (such as Formula I), saturated hydrocarbons (such as Formula III), halogenated hydrocarbons (such as Formulas II and IV), metal ions, and the like are all herein. Is described in detail.

In some embodiments,
An anode in contact with an anode electrolyte comprising a metal halide or metal sulfate, wherein the anode is configured to oxidize the metal halide or metal sulfate from a lower oxidation state to a higher oxidation state; ,
A cathode in contact with the cathode electrolyte;
Operatively connected to the anode chamber and halogenated or sulfonated with a metal halide or metal sulfate in an aqueous medium with an unsaturated or saturated hydrocarbon to form a halogenated hydrocarbon or sulfone in an aqueous medium A reactor configured to form one or more organic compounds comprising a fluorinated hydrocarbon and metal ions of a lower oxidation state;
Separating said one or more organic compounds from said lower oxidation state metal halide or metal sulfate aqueous medium, wherein said lower oxidation state is operatively connected to a reactor and an anode And a separator configured to recycle an aqueous medium comprising a metal halide or metal sulfate to the anode electrolyte.

In some embodiments,
An anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize metal ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
One or more organic compounds comprising ethylene dichloride in an aqueous medium by reacting ethylene with the higher oxidation state metal ions in an aqueous medium and operatively connected to the anode chamber; A reactor configured to form metal ions in a lower oxidation state than the above;
The one or more organic compounds are operatively connected to a reactor and an anode and separate from the lower oxidation state metal ions and include the lower oxidation state metal ions And a separator configured to recycle the aqueous medium to the anode electrolyte.

  In some embodiments of the above system, the aqueous medium is greater than 5 wt% water, or greater than 5.5 wt%, or greater than 6 wt%, or between 5-90 wt%, or 5-95 wt% %, Or 5 to 99% by weight of water, or 5.5 to 90% by weight, or 5.5 to 95% by weight, or 5.5 to 99% by weight of water, Or between 6 and 90 wt%, or between 6 and 95 wt%, or between 6 and 99 wt%.

  In some embodiments of the above system, the separator further comprises a recirculation system for recycling an aqueous medium comprising lower oxidation state metal ions to the anode electrolyte.

  In some embodiments of the above system, the one or more organic compounds include one or more of chloroethanol, dichloroacetaldehyde, trichloroacetaldehyde, or combinations thereof. In some embodiments of the above system, the metal ion is copper. The lower oxidation state metal ion is Cu (I) and the higher oxidation state metal ion is Cu (II). In some embodiments of the above system, the metal halide is copper halide and the metal sulfate is copper sulfate.

  In some embodiments of the above system, the separator that separates one or more organic compounds from an aqueous medium that includes lower oxidation state metal ions includes one or more adsorbents. In some embodiments of the above system, the separator is activated carbon. In some embodiments of the above system, the separator is not limited to: polyethylene, polypropylene, polystyrene, polymethylpentene, polybutene-1, polyolefin elastomer, polyisobutylene, ethylene propylene rubber, polymethyl acrylate, Polymers such as polyolefins selected from poly (methyl methacrylate), poly (isobutyl methacrylate) and combinations thereof. In some embodiments of the above system, the separator is polystyrene.

In some embodiments,
An anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize metal ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
Halogenation is carried out in an aqueous medium by reacting an anode electrolyte operatively connected to the anode chamber and containing the higher oxidation state metal ions with an unsaturated hydrocarbon or saturated hydrocarbon in an aqueous medium. A reactor configured to form one or more organic compounds including hydrocarbons and metal ions of a lower oxidation state;
An aqueous solution operably connected to the reactor and the anode and separating the one or more organic compounds from the lower oxidation state metal ions and comprising the lower oxidation state metal ions And a separator comprising one or more adsorbents configured to recirculate the medium to the anode electrolyte.

In some embodiments,
An anode in contact with an anode electrolyte comprising metal ions, the anode configured to oxidize metal ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
One or more organic compounds comprising ethylene dichloride in an aqueous medium by reacting ethylene with the higher oxidation state metal ions in an aqueous medium and operatively connected to the anode chamber; A reactor configured to form metal ions in a lower oxidation state than the above;
An aqueous solution operably connected to the reactor and the anode and separating the one or more organic compounds from the lower oxidation state metal ions and comprising the lower oxidation state metal ions And a separator comprising one or more adsorbents configured to recirculate the medium to the anode electrolyte.

  In some embodiments, in the above system, the adsorbent is activated carbon. In some embodiments, in the above system, the adsorbent is a polyolefin such as polystyrene.

  In some embodiments of the above system, the adsorbent is from an aqueous medium, greater than 90 wt / wt% organic compound, or greater than 95 wt / wt% organic compound, or greater than 99 wt / wt%, or 99 Adsorb more than .99 wt / wt% or more than 99.999 wt / wt% organic compounds. In some embodiments of the above system, the aqueous medium obtained after passing through the adsorbent (which is recycled back to the anode electrolyte) is less than 100 ppm, or less than 50 ppm, or less than 10 ppm, Alternatively, it contains less than 1 ppm organic compound.

  In some embodiments of the above system, the cathode is configured to produce water, alkali and / or hydrogen gas. In some embodiments of the above system, the cathode is an ODC configured to produce water. In some embodiments of the above system, the cathode is an ODC configured to generate alkali. In some embodiments of the above system, the cathode is configured to produce hydrogen gas. In some embodiments of the above system, the cathode is an oxygen depolarized cathode configured to reduce oxygen and water to hydroxide ions, or the cathode converts water to hydrogen gas and hydroxide ions. A hydrogen gas generating cathode configured to reduce, the cathode is a hydrogen gas generating cathode configured to reduce hydrochloric acid to hydrogen gas, or the cathode reacts hydrochloric acid and oxygen gas. An oxygen depolarizing cathode configured to form water.

  In some embodiments of the above system, the metal ion is any metal ion described herein. In some embodiments of the above system, the metal ions are iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold , Nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, the metal ion is selected from the group consisting of iron, chromium, copper and tin. In some embodiments, the metal ion is copper. In some embodiments, the lower oxidation state of the metal ion is 1+, 2+, 3+, 4+ or 5+. In some embodiments, the higher oxidation state of the metal ion is 2+, 3+, 4+, 5+ or 6+.

In some embodiments,
An anode in contact with an anode electrolyte comprising copper ions, the anode configured to oxidize copper ions from a lower oxidation state to a higher oxidation state;
A cathode in contact with the cathode electrolyte;
One or more organic compounds including ethylene dichloride in an aqueous medium by reacting ethylene with the higher oxidation state copper ions in an aqueous medium operatively connected to the anode chamber; A reactor configured to form copper ions in a lower oxidation state than the above;
Separating the one or more organic compounds from the aqueous medium that is operatively connected to the reactor and the anode and that includes the lower oxidation state metal ions, less than 100 ppm, or less than 50 ppm, or less than 10 ppm; Or one or more adsorbents selected from activated carbon, polyolefins, activated silica, and combinations thereof, configured to produce an aqueous medium comprising less than 1 ppm organic compound and lower oxidation copper ions Including a separator,
And a recycling system for recycling a portion of the aqueous medium containing the lower oxidation state metal ions to the anode electrolyte.

  In some embodiments of the systems described herein, the separator is a series of beds or packed columns of adsorbents linked together.

  In some embodiments of the above system, the recirculation system may be a conduit, pipe, tube, etc. that may be used to move the solution. Appropriate control valves and computer control systems may be associated with such recirculation systems.

  In some embodiments, the system is configured not to produce chlorine gas at the anode. In some embodiments, the system is configured such that oxygen gas and / or chlorine gas is not required for chlorination of unsaturated or saturated hydrocarbons to halogenated hydrocarbons.

In some system embodiments, the system may employ various desorption techniques (purging with an inert fluid (eg, water), changing chemical conditions such as pH, increasing temperature, partial pressure after organic product adsorption. Such as, but not limited to, purge with high temperature inert gas (such as, but not limited to, purge with> 100 ^° C vapor, nitrogen gas, argon gas or air), etc. A regenerator that regenerates the adsorbent by using (but not limited to).

  In some embodiments, the components of the reactor and / or separator in the system of the present invention comprise the amount of hydrocarbon introduced into the reactor, the amount of anode electrolyte introduced into the reactor, the amount into the separator. Amount of aqueous medium containing organic matter and metal ions, adsorption time by adsorbent, temperature and pressure conditions in reactor and separator, flow rate in and out of reactor and separator, regeneration time of adsorbent in separator, return to electrochemical cell A control station configured to control the time, flow rate, etc. of the aqueous medium may be included.

  The control station may include a series of valves or a multi-valve system that is controlled manually, mechanically or digitally, or may use any other convenient flow regulator protocol. In some cases, the control station provides input and output parameters to the user and a computer interface configured to control the quantities and conditions as described above (where the adjustment is computer assisted, or Completely controlled by a computer).

  The methods and systems of the present invention can also include one or more detectors configured to monitor ethylene gas flow, metal ion concentration in an aqueous medium or organic matter concentration in an aqueous medium, and the like. . Monitoring can include, but is not limited to, collecting data about the pressure, temperature and composition of aqueous media and gases. The detector can be any convenient device configured to monitor, such as a pressure sensor (eg, electromagnetic pressure sensor, potentiometric pressure sensor, etc.), temperature sensor (resistance temperature detector, thermocouple, gas thermometer, sensor Misters, pyrometers, infrared sensors, etc.), volume sensors (eg, geophysical diffraction tomography, X-ray tomography, hydroacoustic surveyors, etc.), as well as the chemical structure of aqueous media or gases Apparatus (for example, IR spectrometer, NMR spectrometer, UV-vis spectrophotometer, high-performance liquid chromatograph, inductively coupled plasma emission spectrometer, inductively coupled plasma mass spectrometer, ion chromatograph, X-ray diffractometer, Gas chromatograph, gas chromatograph mass spectrometer, flow indicator Transfection analysis, scintillation counters, may be acid titration and flame emission spectrometer, etc.).

  In some embodiments, the detector may also include a computer interface configured to provide the user with collected data about aqueous media, metal ions and / or organics. For example, the detector can measure the concentration of aqueous media, metal ions and / or organics, and the computer interface can provide an overview of compositional changes over time in aqueous media, metal ions and / or organics. Can do. In some embodiments, the summary may be saved as a computer readable data file or printed out as a user readable document.

  In some embodiments, the detector may be a monitoring device that can collect real-time data (eg, internal pressure, temperature, etc.) about aqueous media, metal ions and / or organics. In other embodiments, the detector measures the parameters of the aqueous medium, metal ions and / or organic matter at regular intervals (eg, its composition is determined every minute, every 5 minutes, every 10 minutes, every 30 minutes, One or more detectors configured to measure every 60 minutes, every 100 minutes, every 200 minutes, every 500 minutes, or at some other interval.

  In some embodiments, the electrochemical systems and methods described herein include an aqueous medium that contains greater than 5% water by weight. In some embodiments, the aqueous medium is greater than 5% water; or greater than 6% water; or greater than 8% water; or greater than 10% water; or greater than 15% water; Or more than 20% water; or more than 25% water; or more than 50% water; or more than 60% water; or more than 70% water; or more than 80% water; or 90 Greater than wt% water; or about 99 wt% water; or between 5 and 100 wt% water; or between 5 and 99 wt% water; or between 5 and 90 wt% water; or 5 Between 80% water; or between 5 and 70% water; or between 5 and 60% water; or between 5 and 50% water; or between 5 and 40% by weight. Water; or between 5-30% by weight water; or between 5-20% by weight water; or between 5-10% by weight Water; or 6 to 100% by weight water; or 6 to 99% by weight water; or 6 to 90% by weight water; or 6 to 80% by weight water; or 6 to 70 Water between 6% by weight; or between 6% and 50% by weight of water; or between 6% and 40% by weight of water; or between 6% and 30% by weight of water. Or 6 to 20% by weight water; or 6 to 10% by weight water; or 8 to 100% by weight water; or 8 to 99% by weight water; or 8 to 90% by weight. Between 8% and 80% water; or between 8 and 70% water; or between 8 and 60% water; or between 8 and 50% water; Or between 8 and 40 wt% water; or between 8 and 30 wt% water; or between 8 and 20 wt% water; or between 8 and 10 wt% Or between 10 and 100 wt% water; or between 10 and 75 wt% water; or between 10 and 50 wt% water; or between 20 and 100 wt% water; or between 20 and 50 wt% % Water; or 50-100% water; or 50-75% water; or 50-60% water; or 70-100% water; Or between 70 and 90% by weight of water; or between 80 and 100% by weight of water. In some embodiments, the aqueous medium can include a water-soluble organic solvent.

  In some embodiments of the methods and systems described herein, the amount of total metal ions in the anode electrolyte, or the amount of copper in the anode electrolyte, or the amount of iron in the anode electrolyte, or the anode electrolyte The amount of chromium in, or the amount of tin in the anode electrolyte, or the amount of platinum, or the amount of metal ions in contact with the unsaturated or saturated hydrocarbon, between 1-12M; or between 1-11M; or Between 1-10M; or between 1-9M; or between 1-8M; or between 1-7M; or between 1-6M; or between 1-5M; or between 1-4M; or 1 Between -3M; or between 1-2M; or between 2-12M; or between 2-11M; or between 2-10M; or between 2-9M; or between 2-8M; Between 7M; Between 2-6M; or between 2-5M; or between 2-4M; or between 2-3M; or between 3-12M; or between 3-11M; or between 3-10M; or Between 3-9M; or between 3-8M; or between 3-7M; or between 3-6M; or between 3-5M; or between 3-4M; or between 4-12M; or 4 Between ˜11M; or between 4-10M; or between 4-9M; or between 4-8M; or between 4-7M; or between 4-6M; or between 4-5M; Between 12M; or between 5-11M; or between 5-10M; or between 5-9M; or between 5-8M; or between 5-7M; or between 5-6M; or 6-12M Between; or between 6-11M; or between 6-10M; or between 6-9M; Between 6-8M; or between 6-7M; or between 7-12M; or between 7-11M; or between 7-10M; or between 7-9M; or between 7-8M; or 8 Between -12M; or between 8-11M; or between 8-10M; or between 8-9M; or between 9-12M; or between 9-11M; or between 9-10M; Between 12M; or between 10-11M; or between 11-12M. In some embodiments, the amount of total ions in the anode electrolyte as described above is the amount of lower oxidation state metal ions plus the amount of higher oxidation state metal ions; or of higher oxidation state metal ions. Total amount; or the total amount of metal ions in the lower oxidation state.

  In some embodiments of the methods and systems described herein, an anode electrolyte containing metal ions may contain a mixture of lower oxidation state metal ions and higher oxidation state metal ions. In some embodiments, it may be desirable to have a mix of lower oxidation state metal ions and higher oxidation state metal ions in the anode electrolyte. In some embodiments, the anode electrolyte in contact with the unsaturated or saturated hydrocarbon contains lower oxidation state metal ions and higher oxidation state metal ions. In some embodiments, the lower oxidation state metal ion and the higher oxidation state metal ion are such that the reaction of the metal ion with an unsaturated or saturated hydrocarbon occurs to form a halo or sulfohydrocarbon. Exist in ratio. In some embodiments, the ratio of the higher oxidation state metal ions to the lower oxidation state metal ions is between 20: 1 and 1:20, or between 14: 1 and 1: 2; or 14: Between 1-8: 1; or between 14: 1 and 7: 1; or between 2: 1 and 1: 2; or between 1: 1 and 1: 2; or between 4: 1 and 1: 2. Between; or 7: 1 to 1: 2.

  In some embodiments of the methods and systems described herein, the anode electrolyte in the electrochemical systems and methods of the present invention is a higher oxidation state metal ion in the range of 4-7M, 0.1 Contains lower oxidation state metal ions in the range of ~ 2M and sodium chloride in the range of 1-3M. The anode electrolyte can optionally contain 0.01-0.1M hydrochloric acid. In some embodiments of the methods and systems described herein, an anode electrolyte that reacts with hydrogen gas or an unsaturated or saturated hydrocarbon is a higher oxidation state metal ion in the range of 4-7M, 0 Contains lower oxidation state metal ions in the range of 1-2 M and sodium chloride in the range of 1-3 M. The anode electrolyte can optionally contain 0.01-0.1M hydrochloric acid.

  In some embodiments of the methods and systems described herein, the anode electrolyte may contain other cations in addition to the metal ions. Other cations include, but are not limited to, alkali metal ions and / or alkaline earth metal ions (eg, but not limited to lithium, sodium, calcium, magnesium, etc.). The amount of other cations added to the anode electrolyte is between 0.01 and 5M; or between 0.01 and 1M; or between 0.05 and 1M; or between 0.5 and 2M; May be between 5M.

  In some embodiments of the methods and systems described herein, the anode electrolyte may contain an acid. Acid may be added to the anolyte to bring the pH of the anolyte to 1 or 2 or less. The acid can be hydrochloric acid or sulfuric acid.

  The system provided herein includes a reactor operably connected to the anode chamber. The reactor is configured to contact the metal chloride in the anode electrolyte with hydrogen gas or an unsaturated or saturated hydrocarbon. The reactor may be any means for contacting the metal chloride in the anode electrolyte with hydrogen gas or an unsaturated or saturated hydrocarbon. Such means or such reactors are well known in the art and include, but are not limited to, pipes, ducts, tanks, series of tanks, containers, towers, conduits, and the like. Some examples of such reactors are described herein in FIGS. 7A, 7B, 10A, and 10B. The reactor may include one or more controllers that control temperature sensors, pressure sensors, control mechanisms, inert gas injectors, etc. to monitor, control, and / or accelerate the reaction. In some embodiments, the reaction between a metal chloride having a higher oxidation state metal ion and an unsaturated or saturated hydrocarbon is between 100-200 ° C or between 100-175 ° C or between 150-175. Performed in the reactor at a temperature between 0C and a pressure between 100 and 500 psig or between 100 and 400 psig or between 100 and 300 psig or between 150 and 350 psig. In some embodiments, the reactor components are lined with Teflon® to prevent corrosion of the components. Some examples of reactors for carrying out the reaction of higher oxidation state metal ions with hydrogen gas are illustrated in FIGS. 7A and 7B.

  In some embodiments, unsaturated or saturated hydrocarbons may be provided to the anode chamber, where metal halides or metal sulfates with higher oxidation state metals react with unsaturated or saturated hydrocarbons. And the respective products are formed inside the anode chamber. In some embodiments, unsaturated or saturated hydrocarbons may be provided to the anode chamber, where the metal chloride with the higher oxidation state metal reacts with the unsaturated or saturated hydrocarbons to produce chlorocarbons. Hydrogen is formed. Such a system includes an unsaturated or saturated hydrocarbon delivery system operably connected to the anode chamber and configured to deliver unsaturated or saturated hydrocarbons to the anode chamber. The unsaturated or saturated hydrocarbon can be a solid, liquid, or gas. Unsaturated or saturated hydrocarbons can be fed to the anode using any means for directing unsaturated or saturated hydrocarbons from an external source to the anode chamber. Such means for directing unsaturated or saturated hydrocarbons from an external source to the anode chamber, or unsaturated or saturated hydrocarbon delivery systems are well known in the art, including but not limited to pipes, Includes tanks, ducts, and conduits. In some embodiments, the system, or an unsaturated or saturated hydrocarbon delivery system, includes a duct that directs the unsaturated or saturated hydrocarbon from an external source to the anode. It should be understood that unsaturated or saturated hydrocarbons may be directed from the bottom of the cell, the top or side of the cell to the anode. In some embodiments, the unsaturated or saturated hydrocarbon gas is directed to the anode so that the unsaturated or saturated hydrocarbon gas is not in direct contact with the anolyte. In some embodiments, unsaturated or saturated hydrocarbons may be directed to the anode through multiple inlets. The sources of unsaturated or saturated hydrocarbons that provide unsaturated or saturated hydrocarbons to the anode chamber in the methods and systems provided herein include any source of unsaturated or saturated hydrocarbons known in the art. . Such sources include, but are not limited to, commercial grade unsaturated or saturated hydrocarbons and / or unsaturated or saturated hydrocarbon generation plants such as the petrochemical refining industry.

  In some embodiments, the electrochemical cell of the present invention is used in the field where unsaturated or saturated hydrocarbons are generated, for example, in a refinery for performing halogenation (eg, chlorination) of unsaturated or saturated hydrocarbons. Provide a method and system to be installed. In some embodiments, a metal ion-containing anolyte from an electrochemical system is formed for unsaturated or saturated hydrocarbons to undergo halogenation (eg, chlorination) of unsaturated or saturated hydrocarbons. Transported to refinery. In some embodiments, the methods and systems of the present invention can utilize ethylene gas from a refinery without requiring ethylene gas filtration or cleaning. Typically, an ethylene gas generation plant purifies gas and removes impurities. In some embodiments of the methods and systems of the present invention, such pre-purification of gas is not required and can be avoided.

In some embodiments, metal generation and halogenation, eg, chlorination reactions, are performed in the same anode chamber. An illustrative example of such an embodiment is shown in FIG. The system 900 of FIG. 9 is for exemplary purposes only and includes other metal ions having different oxidation states, other unsaturated or saturated hydrocarbons, and non-alkali products such as water or hydrogen gas in the cathode chamber. It should be understood that other electrochemical systems that form and other unsaturated or saturated hydrocarbon gases are equally applicable to the system. In some embodiments, as illustrated in FIG. 9, the electrochemical system 900 includes an anode located near the AEM. The system 900 also includes a gas diffusion layer (GDL). The anode electrolyte is in contact with the anode on one side and in contact with the GDL on the other side. In some embodiments, the anode may be located to minimize resistance from the anolyte, for example, the anode may be located near or coupled to the AEM. In some embodiments, the anode converts metal ions from a lower oxidation state to a higher oxidation state metal ions. For example, the anode converts metal ions from a 1+ oxidation state to a 2+ oxidation state. Cu ²⁺ ions combine with chloride ions to form CuCl ₂ . Ethylene gas is compressed into the gas containing chamber on one side of the GDL. The ethylene gas then diffuses through the gas diffusion layer and reacts with the higher oxidation state metal chloride to form chlorohydrocarbons such as ethylene dichloride. The metal chloride CuCl ₂ undergoes reduction to a lower oxidation state and forms CuCl. In some embodiments, the anode electrolyte may be removed, using, but not limited to, separation techniques well known in the art including, but not limited to, filtration, vacuum distillation, fractional distillation, fractional crystallization, ion exchange resin, and the like. The ethylene dichloride may be separated from the anode electrolyte. In some embodiments, ethylene dichloride may be at a higher concentration than the anode electrolyte and may form a separate layer inside the anode chamber. In such embodiments, ethylene dichloride can be removed from the bottom surface of the cell. In some embodiments, the gas may be removed by piercing the gas containing chamber on one side of the GDL. In some embodiments, the anode chamber may be pierced to remove ethylene gas or gaseous byproducts. System 900 also includes an oxygen depolarized cathode that generates hydroxide ions from water and oxygen. The hydroxide ions can be subjected to any of the carbonate precipitation processes described herein. In some embodiments, the cathode is not a gas diffusion cathode, but is a cathode as described in FIGS. 4A or 4B. In some embodiments, the system 900 can be utilized for any electrochemical system that produces alkali.

  In some embodiments of the systems and methods described herein, no gas is formed at the cathode. In some embodiments of the systems and methods described herein, hydrogen gas is formed at the cathode. In some embodiments of the systems and methods described herein, no gas is formed at the anode. In some embodiments of the systems and methods described herein, no gases other than gaseous unsaturated hydrocarbons and saturated hydrocarbons are used at the anode.

Another illustrative example of a reactor connected to an electrochemical system is illustrated in FIG. 10A. As illustrated in FIG. 10A, the anode chamber of the electrochemical system (the electrochemical system can be any electrochemical system described herein) is connected to a reactor, The reactor is also connected to a source of unsaturated or saturated hydrocarbon (example illustrated as ethylene (C ₂ H ₄ ) in FIG. 10A). In some embodiments, the electrochemical system and the reactor are inside the same unit and connected inside the unit. Anode electrolyte containing higher oxidation state metal ions, optionally with lower oxidation state metal ions, along with ethylene, is fed to a prestressed (eg, brick lined) reactor. The chlorination of ethylene takes place inside the reactor and forms ethylene dichloride (EDC or dichloroethane (DCE)) and lower oxidation state metal ions. The reactor can operate in the range of 340-360 ° F. and 200-300 psig. While not limited to these, other reactor conditions such as metal ion concentration, ratio of lower and higher oxidation state metal ions, DCE and water vapor partial pressure can be set to increase the selectivity. It can be assured that it works with it. The heat of reaction can be removed by evaporating the water. In some embodiments, a cooling surface may not be required in the reactor and thus may not require a temperature gradient or close temperature control. The reactor effluent gas can be quenched with water in a prestressed (eg brick lined) packed tower (shown as a “quenched” reactor in FIG. 10A). The liquid exiting the tower can be further cooled and separated into an aqueous phase and a DCE phase. The aqueous phase may be split, some recycled to the tower as quench water and the rest recycled to the reactor or electrochemical system. The DCE product can be further cooled and flushed to separate additional water and dissolved ethylene. This dissolved ethylene can be recycled as shown in FIG. 10A. Uncondensed gas from the quench tower can be recycled to the reactor except for a purge stream that removes inerts. The purge stream passes through the ethylene recovery system and can keep the overall utilization of ethylene high, for example as high as 95%. Experimental decisions can be made at actual process temperatures, pressures, and flammability limits for ethylene gas at the composition. Plant construction materials include prestressed brick lining, Hasteloys B and C, inconel, dopant grade titanium (eg, AKOT, grade II), tantalum, Kynar, Teflon®, PEEK, glass, or other polymers or Can include plastic. The reactor can also be designed such that the anode electrolyte flows continuously in and out of the reactor.

  Another illustrative example of a reactor connected to an electrochemical system is as illustrated in FIG. 10B. As illustrated in FIG. 10B, the reactor system 1000 is a glass vessel A suspended from an upper portion of a metal flange B connected to an outlet line C by a metal ball socket welded to the flange head. The glass reactor is placed in an electrically heated metal shell D. Heat input and temperature can be controlled by an automatic temperature regulator. Hydrocarbons may be introduced through openings E and through glass tube F into a metal shell to which a frit glass foot may be attached. This arrangement can result in pressure equalization on both sides of the glass reactor. The hydrocarbon may be contacted with the metal solution (higher oxidation state metal) at the bottom of the reactor or the medium may be bubbled. Volatile products, water vapor, and / or unreacted hydrocarbons may exit via line C, optionally with a valve H that can reduce the pressure to atmospheric pressure. The exhaust gas can be passed through a suitable trap system to remove the product. A bypass arrangement G that allows the passage of gas in the pressure zone without passing an aqueous metal medium may also be attached to the instrument. In some embodiments, the lower oxidation state reduced metal ions left in the vessel are subjected to electrolysis as described herein to regenerate the higher oxidation state metal ions.

An exemplary embodiment of the invention is as shown in FIG. As illustrated in FIG. 11, the electrochemical system 600 of FIG. 6 (or alternatively, the system 400 of FIG. 4A) is integrated with a CuCl—HCl electrochemical system 1100 (also illustrated as a system in FIG. 4B). obtain. In the CuCl-HCl electrochemical system 1100, the inputs at the anode are CuCl and HCl, which results in CuCl ₂ and hydrogen ions. The hydrogen ions pass through the proton exchange membrane and go to the cathode, where hydrogen gas is formed. In some embodiments, a chloride conductive membrane may also be used. In some embodiments, it is contemplated that the CuCl-HCl cell can operate at 0.5V or lower and the system 600 can operate at 0V or lower. Some deviation from the intended voltage can be caused by resistive losses.

In one aspect, in the systems and methods provided herein, CuCl ₂ formed in the anode electrolyte can be used for copper production. For example, CuCl ₂ formed in the systems and methods of the present invention can be used for leaching processes that extract copper from copper minerals. By way of example only, chalcopyrite is a copper mineral that can be leached into the chloride environment with the aid of the oxidant Cu ²⁺ . Bivalent copper can leach copper and other sulfides of chalcopyrite. When copper is leached, other minerals such as iron, sulfur, gold, silver, etc. can be recovered. In some embodiments, CuCl ₂ produced by the electrochemical cells described herein may be added to the copper mineral concentrate. Cu ²⁺ ions can oxidize copper minerals to form CuCl. CuCl solution from the concentrate may be fed back to the anode compartment of an electrochemical cell as described herein capable of converting the CuCl to CuCl _2. CuCl ₂ can then be fed back to the mineral concentrate to further oxidize the copper mineral. As copper leaches, it can agglomerate silver with further precipitation of zinc, lead and the like. The copper may then be precipitated as copper oxide by treatment with alkali (this alkali may be generated by the cathode chamber of the electrochemical cell). After precipitation of copper as an oxide, the filtrate NaCl may be returned to the electrochemical cell. Hydrogen gas generated at the cathode can be used for copper oxide reduction to form metallic copper (at high temperature). Molten copper can be molded into copper products such as copper wire rods. This method can be used for low grade or various types of copper minerals. The electrochemical plant may be installed near the quarry or near the concentrator, eliminating the transportation costs for waste and allowing the transportation of valuable metal products only.

  The processes and systems described herein can be batch processes or systems or continuous flow processes or systems.

  The reaction of hydrogen gas or unsaturated or saturated hydrocarbon with higher oxidation state metal ions as described in aspects and embodiments herein is performed in an aqueous medium. In some embodiments, such reactions may be in a non-aqueous liquid medium that may be a solvent for a hydrocarbon or hydrogen gas feed. The liquid medium or solvent may be aqueous or non-aqueous. Suitable non-aqueous solvents are polar and non-polar aprotic solvents such as dimethylformamide (DMF), dimethyl sulfoxide (DMSO), halogenated hydrocarbons, by way of example only, dichloromethane, carbon tetrachloride, and 1,2 Dichloroethane, as well as organic nitriles, for example acetonitrile. The organic solvent may contain nitrogen atoms that can form chemical bonds with lower oxidation state metals, thereby providing enhanced stability to lower oxidation state metal ions. In some embodiments, acetonitrile is the organic solvent.

  In some embodiments, when an organic solvent is used for the reaction between a higher oxidation state metal ion and hydrogen gas or hydrocarbon, water may need to be removed from the metal-containing medium. Thus, metal ions obtained from the electrochemical systems described herein can contain water. In some embodiments, water can be removed from the metal ion-containing medium by azeotropic distillation of the mixture. In some embodiments, higher oxidation state metal ions and hydrogen gas or solvents containing unsaturated or saturated hydrocarbons are 5 to 90% in the reaction medium; or 5 to 80%; or 5 to 70%. Or 5-60%; or 5-50%; or 5-40%; or 5-30%; or 5-20%; or 5-10% by weight water. The amount of water that can be tolerated in the reaction medium can depend on the particular halide support in the medium, and the amount of water that can be tolerated is, for example, more for copper chloride than for ferric chloride. Many. Such an azeotropic distillation can be avoided when an aqueous medium is used in the reaction.

  In some embodiments, the reaction of higher oxidation state metal ions with hydrogen gas or unsaturated or saturated hydrocarbons can occur when the reaction temperature is greater than 50 ° C. and up to 350 ° C. In an aqueous medium, the reaction is carried out under superatmospheric pressure up to a value of 1000 psi or less, and the reaction medium in the liquid phase is brought to a temperature of 50 ° C to 200 ° C, typically about 120 ° C to about 180 ° C. Can be maintained.

  In some embodiments, the reaction of the higher oxidation state metal ion with the unsaturated or saturated hydrocarbon may comprise a halide support. In some embodiments, the ratio of halide ions to higher oxidation state total metal ions is 1: 1; or a ratio greater than 1: 1; or 1.5: 1; or a ratio greater than 2: 1; And / or at least 3: 1. Thus, for example, the ratio in a cupric halide solution in concentrated hydrochloric acid can be about 2: 1 or 3: 1. In some embodiments, it may be desirable to use a high concentration of metal halide and a saturated or nearly saturated solution of metal halide due to high utilization of the halide support. If necessary, the solution can be buffered to maintain the pH at the desired level during the halogenation reaction.

  In some embodiments, non-halogenated salts of metals may be added to a solution containing higher oxidation state metal ions. The added metal salt can be soluble in the metal halide solution. Examples of suitable salts suitable for incorporation into a cupric chloride solution include, but are not limited to, copper sulfate, copper nitrate, and copper tetrafluoroborate. In some embodiments, a metal halide that is different from the metal halide used in the methods and systems may be added. For example, ferric chloride may be added to the cupric chloride system at the time of halogenation of the unsaturated hydrocarbon.

  The unsaturated or saturated hydrocarbon feed can be fed continuously or intermittently to the halogenation vessel. Efficient halogenation can depend on the achievement of intimate contact between the feedstock in solution and metal ions, and the halogenation reaction can be achieved by techniques designed to improve or maximize such contact. Can be done. The metal ion solution may be agitated by stirring or shaking or any desired technique. For example, the reaction may be performed in a column, such as a packed column, or trickle bed reactor or a reactor described herein. For example, if the unsaturated or saturated hydrocarbon is gaseous, a reverse current technique may be used, where the unsaturated or saturated hydrocarbon goes up through the column or reactor and the metal ion solution is Go down through the column or reactor. In addition to enhancing the contact of unsaturated or saturated hydrocarbons with metal ions in solution, the techniques described herein also provide that the solution is aqueous and the aqueous solution of unsaturated or saturated hydrocarbons. The dissolution rate of unsaturated or saturated hydrocarbons in solution may be enhanced, as it may be desirable if the properties are low. Feedstock dissolution can also be assisted by higher pressures.

  Mixtures of saturated, unsaturated hydrocarbons and / or partially halogenated hydrocarbons may be used. In some embodiments, the partially halogenated product of the process of the present invention capable of further halogenation is passed to the reaction vessel through a product recovery stage, and, if appropriate, a lower oxidation state metal ion regeneration stage. It can be recycled back. In some embodiments, the halogenation reaction may be continued outside the halogenation reaction vessel, for example, in a separate regeneration vessel, to avoid overhalogenation of unsaturated or saturated hydrocarbons. Care may need to be taken in the control of.

  In some embodiments, the electrochemical system described herein is installed near a plant that produces unsaturated or saturated hydrocarbons or produces hydrogen gas. In some embodiments, the electrochemical system described herein is installed near a PVC plant. For example, in some embodiments, the electrochemical system is within a 100 mile radius of an ethylene gas, hydrogen gas, vinyl chloride monomer, and / or PVC plant. In some embodiments, the electrochemical system described herein is installed inside or outside an ethylene plant for the reaction of ethylene and metal ions. In some embodiments, the plant described above is retrofitted with an electrochemical system as described herein. In some embodiments, an anode electrolyte containing higher oxidation state metal ions is transported to the plant location described above. In some embodiments, anode electrolytes containing higher oxidation state metal ions are transported within 100 miles of the plant location. In some embodiments, the electrochemical system described herein is such that the alkali generated in the cathode electrolyte reacts with a divalent cation to form a carbonate / bicarbonate product. Installed near the plant as described above, and near the source of divalent cations. In some embodiments, the electrochemical systems described herein allow the alkali generated in the cathode electrolyte to capture carbon dioxide and form a carbonate / bicarbonate product. Installed near a plant as described above, near a source of divalent cations and / or a source of carbon dioxide. In some embodiments, carbon dioxide generated by a refinery that forms unsaturated or saturated hydrocarbons is used in an electrochemical system or used in the precipitation of a carbonate / bicarbonate product. Thus, in some embodiments, the electrochemical systems described herein allow the alkali generated in the cathode electrolyte to capture carbon dioxide and form a carbonate / bicarbonate product. Thus, it is installed near a plant as described above, near a source of divalent cations and / or a source of carbon dioxide, for example a refinery producing unsaturated or saturated hydrocarbons.

  Any number of halo or sulfohydrocarbons can be generated from the reaction of higher oxidation state metal chlorides with unsaturated or saturated hydrocarbons as described herein. Chlorohydrocarbons can be used in the chemical and / or manufacturing industries. Chlorohydrocarbons can be used as chemical intermediates or solvents. The use of solvents includes a wide variety of applications including reaction media for metal and fabric cleaning, oil extraction, and chemical synthesis.

  In some embodiments, an unsaturated hydrocarbon, such as ethylene, reacts with a higher oxidation state metal chloride to form ethylene dichloride. Ethylene dichloride includes, but is not limited to, vinyl chloride, trichlorethylene and tetrachloroethylene, vinylidene chloride, trichloroethane, ethylene glycol, diaminoethylene, polyvinyl chloride, nylon, viscose rayon, styrene-butadiene rubber, and various plastics. Production of chemicals related to plastics, rubber and synthetic textile fibers; as solvents used as grease remover and paint remover; resin, asphalt, bitumen, rubber, fat, oil, wax, gum, photo, photocopy, As a solvent for cosmetics, leather cleaning, and drugs; fumigants for cereals, orchards, fungi, upholstery, and carpets; as pickling agents; for various organic compounds such as ethylenediamine As a building block reagent as an intermediate in synthesis; As a source of chlorine with removal of ethene and chloride; As a precursor of 1,1,1-trichloroethane used in dry cleaning; Antiknock additive in leaded fuel As a use in the extraction of spices, for example Beninoki, paprika and turmeric; as an excipient for pesticides; in paints, coatings and adhesives; and for various purposes including but not limited to combinations thereof Can be used.

  In the methods and systems described herein, in some embodiments, no hydrochloric acid is formed in the anode chamber. In the methods and systems described herein, in some embodiments, no gas is formed at the anode. In the methods and systems described herein, in some embodiments, no gas is used at the anode. In the methods and systems described herein, in some embodiments, hydrogen gas is formed at the cathode. In the methods and systems described herein, in some embodiments, no hydrogen gas is formed at the cathode.

  In some embodiments, a wire is connected between the cathode and anode so that current passes through the cell. In such embodiments, the cell may act as a battery, and the current generated by the cell may be used to generate alkali (which is removed from the cell). In some embodiments, the resistance of the cell may increase and the current may decrease. In such an embodiment, a voltage may be applied to the electrochemical cell. Cell resistance can increase for a variety of reasons including, but not limited to, electrode erosion, liquid resistance, film fouling, and the like. In some embodiments, current can be drawn from the cell using an ampere load.

  In some embodiments, the systems provided herein can be any chloroalkali process, or chloroalkali process with ODC, or any oxidizer that oxidizes metal ions from a lower oxidation state to a higher oxidation state in the anode chamber. Compared to other processes, it results in a low to zero voltage system that produces alkali. In some embodiments, a system described herein is less than 2V; or less than 1.2V; or less than 1.1V; or less than 1V; or less than 0.9V; or less than 0.8V; or Or less than 0.7V; or less than 0.5V; or less than 0.4V; or less than 0.3V; or less than 0.2V; or less than 0.1V; or 0 volts; Between 2V; or between 0 and 1V; or between 0 and 0.5V; or between 0.5 and 1V; or between 0.5 and 2V; or between 0 and 0.1V; Between 1 and 1 V; or between 0.1 and 2 V; or between 0.01 and 0.5 V; or between 0.01 and 1.2 V; or between 1 and 1.2 V; or 0.2 ~ 1V; or between 0V; or 0.5V; or 0.6V; Others 0.7 V; operating at or 1V voltage; or 0.8 V; or 0.9V.

  As used herein, “voltage” refers to the voltage or bias applied to or taken from an electrochemical cell that drives the desired reaction between the anode and cathode in the electrochemical cell. Including. In some embodiments, the desired reaction can be electron transfer between the anode and cathode such that an alkaline solution, water, or hydrogen gas is formed in the cathode electrolyte and metal ions are oxidized at the anode. . In some embodiments, the desired reaction can be electron transfer between the anode and the cathode so that higher oxidation state metal ions are formed from lower oxidation state metal ions in the anode electrolyte. To apply a current across the anode and cathode of the electrochemical cell, a voltage can be applied to the electrochemical cell by any means. Such means are well known in the art and include, but are not limited to, devices such as power sources, fuel cells, devices powered by sunlight, devices powered by wind, and the like. Is included. The type of power source that provides the current may be any power source known to those skilled in the art. For example, in some embodiments, the voltage may be applied by connecting the cell's anode and cathode to an external direct current (DC) power source. The power source may be an alternating current (AC) rectified to DC. The DC power source may have adjustable voltage and current that apply the required amount of voltage to the electrochemical cell.

In some embodiments, the current applied to the electrochemical cell is at least 50 mA / cm ² ; or at least 100 mA / cm ² ; or at least 150 mA / cm ² ; or at least 200 mA / cm ² ; or at least 500 mA / cm ² ; or at least 1000 mA / cm ^2;, or at least 1500 mA / cm ^2;, or at least 2000 mA / cm ^2;, or at least 2500 mA / cm ^2; or between 100~2500mA / cm ^2; or between 100~2000mA / cm ^2; or 100 ～1500MA / between cm ^2; or between 100~1000mA / cm ^2; or between 100~500mA / cm ^2; or between 200~2500mA / cm ^2; or 200~2000mA / c Between ^2; or between 200~1500mA / cm ^2; or between 200~1000mA / cm ^2; or between 200~500mA / cm ^2; or between 500~2500mA / cm ^2; or 500~2000mA / cm between ^2; or between 500~1500mA / cm ^2; or between 500~1000mA / cm ^2; or between 1000~2500mA / cm ^2; or between 1000~2000mA / cm ^2; or 1000~1500mA / cm or between 1500~2500mA / cm ^2;; between ² or between 1500~2000mA / cm ^2; or between 2000~2500mA / cm ^2.

In some embodiments, the current applied is 100~250mA / cm ² or 100~150mA / cm ² or 100~200mA / cm ² or 100~300mA / cm ² or 100~400mA / cm ² or 100～500MA / cm ² or 150～200MA / cm ² or 200～150MA / cm ² or 200～300MA / cm ² or 200～400MA / cm ² or 200～500MA / cm ² or 150 mA / cm ² or 200 mA / cm ² or 300 mA / when a cm ² or 400 mA / cm ² or 500mA / cm ² or 600 mA / cm ^2, the cell operates at a voltage between 0 V to 3 V. In some embodiments, the cell operates between 0-1V. In some embodiments, when the current applied is 100~250mA / cm ² or 100~150mA / cm ² or 150~200mA / cm ² or 150 mA / cm ² or 200 mA / cm ^2, the cell is 0 Operates at 1.5V. In some embodiments, the cell during the 0~1V in ampere load 100~250mA / cm ² or 100~150mA / cm ² or 150~200mA / cm ² or 150 mA / cm ² or 200 mA / cm ² Operates with. In some embodiments, the cell, 0.5V at 100~250mA / cm ² or 100~150mA / cm ² or 150~200mA / cm ² or 150 mA / cm ² or 200 mA / cm ² current or ampere load Operates with.

  In some embodiments, the systems and methods provided herein further include a percolator and / or spacer between the anode and the ion exchange membrane and / or between the cathode and the ion exchange membrane. An electrochemical system containing a percolator and / or spacer is described in US Provisional Application No. 61 / 442,573, filed Feb. 14, 2011, which is hereby incorporated by reference in its entirety. (Incorporated in the book).

  The systems provided herein can be applied to or used for any one or more of the methods described herein. In some embodiments, the systems provided herein further include an oxygen gas supply or delivery system operably connected to the cathode chamber. The oxygen gas delivery system is configured to provide oxygen gas to the gas diffusion cathode. In some embodiments, the oxygen gas delivery system is configured to deliver gas to the gas diffusion cathode, where the reduction of the gas is catalyzed to provide hydroxide ions. In some embodiments, oxygen gas and water are reduced to hydroxide ions, and unreacted oxygen gas in the system is recovered and recycled to the cathode. Oxygen gas can be supplied to the cathode using any means for directing oxygen gas from an external source to the cathode. Such means for directing oxygen gas from an external source to the cathode, or oxygen gas delivery systems are well known in the art and include, but are not limited to, pipes, ducts, conduits, and the like. In some embodiments, the system or oxygen gas delivery system includes a duct that directs oxygen gas from an external source to the cathode. It should be understood that oxygen gas may be directed from the bottom of the cell, the top or side of the cell to the cathode. In some embodiments, oxygen gas is directed to the backside of the cathode, where the oxygen gas is not in direct contact with the catholyte. In some embodiments, oxygen gas may be directed to the cathode through multiple inlets. Sources of oxygen that provide oxygen gas to the gas diffusion cathode in the methods and systems provided herein include any source of oxygen known in the art. Such sources include, but are not limited to, ambient air, commercial grade oxygen gas from cylinders, oxygen gas obtained by fractionating liquid air, oxygen gas obtained by passing air through a bed of zeolite, Oxygen gas obtained from electrolysis of water, oxygen obtained by pushing air through a ceramic membrane based on zirconium dioxide either by high pressure or current, chemical oxygen generator, oxygen as a liquid in an adiabatic tanker Gas or a combination of these is included. In some embodiments, the source of oxygen may also provide carbon dioxide gas. In some embodiments, oxygen from a source of oxygen gas can be purified before being provided to the cathode chamber. In some embodiments, oxygen from a source of oxygen gas is used as is in the cathode chamber.

Cathode electrolyte containing alkali in the cathode chamber can be withdrawn from the cathode chamber. The alkali can be separated from the cathode electrolyte using techniques known in the art including, but not limited to, diffusion dialysis. In some embodiments, the alkali produced by the methods and systems provided herein is used commercially as is or in commercial processes known in the art. The purity of the alkali produced by the method and system can vary depending on end use requirements. For example, the methods and systems provided herein using an electrochemical cell with a membrane can produce a membrane quality alkali that may be substantially free of impurities. In some embodiments, less pure alkali can be produced by avoiding the use of membranes or by adding carbon to the cathode electrolyte. In some embodiments, the alkali produced in the cathode electrolyte is greater than 2 wt / wt% or greater than 5 wt / wt% or between 5 and 50 wt / wt%.

  In some embodiments, the alkali produced in the cathode chamber can be used in various commercial processes as described herein. In some embodiments, a system suitable for such an application can be operably coupled to the electrochemical unit, or the alkali can be transported to the appropriate site for use. In some embodiments, the system collects alkali from the cathode chamber and a tank capable of collecting, processing and / or transporting the alkali produced in the cathode chamber for use in various commercial processes. A collector configured to be coupled to a suitable process, which may be any means for collecting and treating alkali, including but not limited to collectors, pipes and the like.

  In some embodiments, the alkali, such as sodium hydroxide, produced with the cathode electrolyte is used as is for commercial purposes or treated in various ways well known in the art. For example, sodium hydroxide produced in the catholyte is used as a base in the chemical industry, household and / or as a base in the manufacture of pulp, paper, textiles, drinking water, soap, synthetic detergents and drainage cleaners. obtain. In some embodiments, sodium hydroxide can be used to make paper. Along with sodium sulfide, sodium hydroxide can be a component of white liquor used to separate lignin from cellulose fibers in the kraft process. This can also be useful in some of the later stages of the process of bleaching brown pulp obtained from the pulping process. These stages can include oxygen delignification, oxidative extraction and simple extraction, all of which may require a strong alkaline environment with a pH> 10.5 at the end of the stage. In some embodiments, sodium hydroxide can be used to digest the tissue. This process involves placing the carcass in a sealed chamber and then placing the carcass in a mixture of sodium hydroxide and water that can break the chemical bonds that keep the body intact. Can be included. In some embodiments, sodium hydroxide can be used in a Bayer process that uses sodium hydroxide in the purification of alumina-containing raw ore (bauxite) to produce alumina (aluminum oxide). Alumina is a raw material that can be used to produce aluminum metal by the Hall-Herault process. Alumina can be dissolved in sodium hydroxide, and impurities that are difficult to dissolve at high pH, such as iron oxide, can be left behind in the form of highly alkaline red mud. In some embodiments, sodium hydroxide can be used in the soap manufacturing process. In some embodiments, sodium hydroxide can be used in the production of biodiesel where sodium hydroxide can be used as a catalyst for transesterification of methanol and triglycerides. In some embodiments, sodium hydroxide can be used as a cleaning agent, such as, but not limited to, a degreasing agent in stainless steel and glass bakeware.

  In some embodiments, sodium hydroxide can be used in food preparation. Sodium hydroxide food applications include, but are not limited to, fruit or vegetable cleaning or chemical peeling, chocolate and cocoa processing, caramel coloring production, poultry boiling, soft drink processing and ice cream thickening. It is. Olives can be soaked in sodium hydroxide to soften it, and pretzel or German lye rolls can be polished with sodium hydroxide solution before baking to crisp. In some embodiments, sodium hydroxide can be used at home as a drain cleaner for cleaning clogged drains. In some embodiments, sodium hydroxide can be used as a relaxer that straightens the hair. In some embodiments, sodium hydroxide can be used in oil refining and oil drilling because it can increase viscosity and prevent heavy material from precipitating. In the chemical industry, sodium hydroxide can provide functions for acid neutralization, hydrolysis, condensation, saponification, and replacement of other groups in organic compounds with hydroxyl ions. In some embodiments, sodium hydroxide can be used in the textile industry. The mercerization of the fiber with sodium hydroxide solution can allow greater tensile strength and firm gloss. This can also remove wax and oil from the fiber, making the fiber more amenable to bleaching and dyeing. Sodium hydroxide can be used in the production of viscose rayon. In some embodiments, sodium hydroxide can be used to produce sodium hypochlorite that can be used as a home bleach and disinfectant, and in preservatives, and can also be used for the production of aspirin. It can be used to produce sodium phenolate.

Contacting Carbon Dioxide with Cathode Electrolyte In one aspect, a method and system as described herein is provided that includes contacting carbon dioxide with a cathode electrolyte either inside the cathode chamber or outside the cathode chamber. In one aspect, contacting the metal ion with the anode in the anode electrolyte of the anode chamber; converting or oxidizing the metal ion from a lower oxidation state to a higher oxidation state in the anode chamber; and cathode in the cathode chamber Contacting the electrolyte with the cathode; generating alkali in the cathode electrolyte; and contacting the alkali in the cathode electrolyte with carbon from a carbon source, such as carbon dioxide from a carbon dioxide source. I will provide a. In some embodiments, the method includes using the higher oxidation state metal produced in the anode chamber as is (as described herein), or reacting with hydrogen gas or not. Further included is a step (as described herein) used for reaction with saturated or saturated hydrocarbons. In some embodiments, contacting the anode with the anode electrolyte; oxidizing metal ions from a lower oxidation state to a higher oxidation state at the anode; contacting the cathode with the cathode electrolyte; in the cathode electrolyte A method is provided comprising: generating hydroxide ions; and contacting the cathode electrolyte with an industrial exhaust gas containing carbon dioxide or a solution of carbon dioxide containing bicarbonate ions.

  In another aspect, an anode chamber comprising an anode in contact with metal ions in an anode electrolyte, wherein the anode is configured to convert metal ions from a lower oxidation state to a higher oxidation state; the cathode generates alkali A cathode chamber that includes a cathode in contact with the cathode electrolyte, and is operably coupled to the cathode chamber and carbon from a carbon source, such as carbon dioxide from a carbon dioxide source, in the cathode electrolyte. A system is provided that includes a contactor configured to contact an alkali. In some embodiments, the system is operably coupled to the anode chamber, and the higher oxidation state metal ions are combined with hydrogen gas or unsaturated or saturated hydrocarbons (as described herein). It further includes a reactor configured to react.

  In some embodiments, carbon from a carbon source is treated with a cathode electrolyte to produce a solution of dissolved carbon dioxide in the alkali of the cathode electrolyte. The alkali present in the cathode electrolyte can facilitate the dissolution of carbon dioxide in the solution. The solution containing dissolved carbon dioxide includes carbonic acid, bicarbonate, carbonate or any combination thereof. In such methods and systems, carbon from a carbon source includes gaseous carbon dioxide from an industrial process or a solution of carbon dioxide from a gas / liquid contactor in contact with gaseous carbon dioxide from an industrial process. . Such contactors are further defined herein. In some embodiments of systems including contactors, the cathode chamber includes bicarbonate and carbonate ions in addition to hydroxide ions.

  An illustrative example of an electrochemical system integrated with carbon from a carbon source is illustrated in FIG. The system 1200 of FIG. 12 is for exemplary purposes only and other metal ions having different oxidation states (eg, chromium, tin, etc.); Other electrochemical systems described herein, such as the 8A, 8B, 9 and 11 electrochemical systems; and a third electrolyte other than sodium chloride, such as sodium sulfate, is a modification that is equally applicable to this system. It should be understood. The electrochemical system 1200 of FIG. 12 includes an anode and a cathode separated by an anion exchange membrane and a cation exchange membrane, creating a third chamber containing a third electrolyte, NaCl. The metal ions are oxidized from a lower oxidation state to a higher oxidation state in the anode chamber, and then the higher oxidation state of the metal is reacted with hydrogen gas or with unsaturated or saturated hydrocarbons, etc. Used for reaction in reactor. The products produced by such reactions are described herein. Although the cathode is illustrated in FIG. 12 as a cathode that forms hydrogen gas, ODC is equally applicable to this system. The cathode chamber is connected to a gas / liquid contactor in contact with gaseous carbon dioxide. A cathode electrolyte comprising an alkali such as hydroxide and / or sodium carbonate is circulated to a gas / liquid contactor that contacts the cathode electrolyte with gaseous carbon dioxide resulting in the formation of a sodium bicarbonate / sodium carbonate solution. This solution of dissolved carbon dioxide is then circulated to the cathode chamber where the alkali produced at the cathode converts bicarbonate ions to carbonate ions, bringing the pH of the cathode electrolyte below 12. This in turn reduces the cell voltage to less than 2V. The sodium carbonate solution thus produced can be recycled back to the gas / liquid contactor for further contact with gaseous carbon dioxide or to carry out a calcium carbonate precipitation process as described herein. It can be taken out. In some embodiments, gaseous carbon dioxide is fed directly into the cathode chamber without use in the middle of the gas / liquid contactor. In some embodiments, the bicarbonate solution from the gas / liquid contactor is not fed to the cathode chamber, but instead is used to precipitate the bicarbonate product.

  Methods and systems relating to contacting carbon from a carbon source with a cathode electrolyte (when the cathode is either an ODC or a hydrogen gas generating cathode), as described herein and illustrated in FIG. Voltage savings can be provided as compared to methods and systems where carbon from the source is not contacted with the cathode electrolyte. The voltage savings can result in less power consumption for electricity generation and less carbon dioxide emissions. This is because sodium carbonate, sodium bicarbonate, calcium / magnesium bicarbonate or calcium / magnesium carbonate, halogenated hydrocarbons and / or produced by the methods and systems of the present invention that are efficient and energy saving. It can lead to the production of more environmentally friendly chemicals such as acids. In some embodiments, the electrochemical cell that contacts carbon from a carbon source (such as carbon dioxide gas from a gas / liquid contactor or a carbonic acid / sodium bicarbonate solution) with the alkali generated at the cathode comprises: More than 0.1V, more than 0.2V, more than 0.5V, more than 1V or more than 1.5V or 0.1 to 0.1% compared to an electrochemical cell that does not come into contact with alkali from a cathode such as an ODC or hydrogen gas generating cathode Between 1.5V, 0.1-1V, 0.2-1.5V, 0.2-1V, 0.5-1.5V or 0.5-1V Has theoretical cathode half-cell voltage savings or theoretical total cell voltage savings. In some embodiments, this voltage saving is achieved at a cathode electrolyte pH between 7-13, 6-12, 7-12, 7-10, or 6-13.

Based on the Nernst equation described above, the lower oxidation state metal is oxidized at the anode as follows:
Cu ⁺ → Cu ²⁺ + 2e ⁻
The E _anode based on the concentration of the copper (II) species is between 0.159 and 0.75V.

Water is reduced at the cathode to hydroxide ions and hydrogen gas (as shown in FIG. 4A or FIG. 12), and the hydroxide ions are converted to bicarbonate ions (carbon dioxide gas or cathode dissolved directly in the cathode electrolyte). When contacted with a carbon / sodium bicarbonate solution from a gas / liquid contactor circulated in the electrolyte to form carbonate, the pH of the cathode electrolyte drops from 14 to less than 14 as follows:
E _cathode = −0.059 pH _c (where pH _c is the pH of the cathode electrolyte = 10)
E _cathode = -0.59

The _total E is then between 0.749 and 1.29 depending on the concentration of copper ions in the anode electrolyte. E _cathode = -0.59 is greater than 200 mV or between 200 mV and 500 mV or between 100 and 500 mV, compared to E _cathode = -0.83 for hydrogen gas generating cathodes not in contact with bicarbonate / carbonate ions Savings. E _total = 0.748-1.29 is greater than 200 mV or 200 mV-1.2 V versus E _total = 0.899-1.53 for hydrogen gas generating cathodes not in contact with bicarbonate / carbonate ions Or between 100 mV and 1.5V.

Similarly, water is reduced to hydroxide ions with ODC (as illustrated in FIG. 5A), and the hydroxide ions are converted into bicarbonate ions (carbon dioxide gas dissolved directly in the cathode electrolyte or in the cathode electrolyte). When contacted with carbonated / sodium bicarbonate solution (such as from a circulating gas / liquid contactor) to form carbonate, the pH of the cathode electrolyte drops from 14 to less than 14 as follows:
E _cathode = 1.224−0.059 pH _c (pH _c = 10)
E _cathode = 0.636V

The _total E is then between -0.477 and 0.064 V depending on the concentration of copper ions in the anode electrolyte. E _cathode = 0.636 is greater than 100 mV or between 100 mV and 200 mV, between 100 and 500 mV, or between 200 and 500 mV for E _cathode = 0.4 for ODC not in contact with bicarbonate / carbonate ions. It is a savings in between. E _total = −0.477 to 0.064V is greater than 200 mV or 200 mV to 1.2V vs. E _total = −0.241 to 0.3 for ODC not in contact with bicarbonate / carbonate ions. Or between 100 mV and 1.5V.

As mentioned above, increasing the cathode electrolyte to a pH of 14 or higher increases the difference between the anode half cell potential and the cathode half cell potential. CO ₂ addition also other interventions (e.g., dilution with water) by extending the period of without also cell operation, the cell potential required will continue to increase. Operation of the electrochemical cell with a cathode pH between 7-13 or 7-12 provides significant energy savings.

  Thus, due to the different pH values in the cathode electrolyte, the voltage applied between the anode and cathode is less than 2.9V, less than 2.5V, less than 2.1V or 2.0V, less than 1.5V. Less than 0V or less than 0.5V or between 0.5-1.5V, while the pH at the cathode electrolyte is between 7-13, 7-12, 6-12 or 7-10, Hydroxide ions, carbonate ions and / or bicarbonate ions are generated in the electrolyte.

  In some embodiments, the carbon source is any gaseous source of carbon dioxide and / or any source that provides a dissolved form of carbon dioxide or a solution of carbon dioxide. The dissolved form of carbon dioxide or a solution of carbon dioxide comprises carbonic acid, bicarbonate ions, carbonate ions or combinations thereof. In some embodiments, the oxygen gas and / or carbon dioxide gas supplied to the cathode is from any oxygen source and carbon dioxide gas source known in the art. The oxygen gas supply source and the carbon dioxide gas supply source may be the same or different. Some examples of oxygen gas sources and carbon dioxide gas sources are as described herein.

  In some embodiments, the alkali produced in the cathode chamber is treated with a gaseous stream of carbon dioxide and / or dissolved carbon dioxide to produce a carbonate / bicarbonate product that can be used as such for commercial purposes. Or can be treated with a divalent cation such as, but not limited to, alkaline earth metal ions to produce alkaline earth metal carbonates and / or bicarbonates.

As used herein, “carbon from a carbon source” includes gas form of carbon dioxide or dissolved form of carbon dioxide or a solution of carbon dioxide. The carbon from the carbon source includes CO ₂ , carbonic acid, bicarbonate ion, carbonate ion or combinations thereof. As used herein, “carbon source” includes any source that provides a gaseous and / or dissolved form of carbon dioxide. Sources of carbon, but are not limited to, the discharge stream, or industrial process to provide a gaseous stream CO _2; willing to provide CO _2, carbonate, bicarbonate ions, the solution containing carbonate ions, or a combination thereof / Liquid contactor; and / or bicarbonate brine solution.

In some embodiments, the gaseous CO ₂ is an exhaust stream or product from an industrial plant. The characteristics of the industrial plant can vary in these embodiments. Industrial plants include, but are not limited to, refineries, power plants that produce unsaturated or saturated hydrocarbons (eg, International Application No. PCT entitled “Methods of sequencing CO ₂ ” filed on Dec. 24, 2008). / US08 / 88318 (the disclosure of which is as described in detail in its entirety herein incorporated by reference), chemical processing plants, steel mills, paper mills, cement plants (e.g. , US Provisional Application No. 61 / 088,340 (the disclosure of which is incorporated in its entirety herein by reference in its entirety) and CO ₂ as a by-product Other industrial plants to be produced are included. An exhaust stream means a gas stream (or similar stream) produced as a by-product of an industrial plant production process. The gaseous stream may be substantially pure CO ₂ or a multi-component gaseous stream comprising CO ₂ and one or more additional gases. Multi-component gaseous streams (including CO ₂ ) that can be used as the CO ₂ source in embodiments of the method include reduced state streams such as synthesis gas, shift reaction synthesis gas, natural gas and hydrogen, and oxidation state stream. For example, both flue gas from combustion such as methane combustion. Exhaust gas containing NOx, SOx, VOC, particulate matter and Hg will incorporate these compounds along with the carbonate in the precipitation product. Specific multi-component gaseous streams of interest that can be processed according to the present invention include, but are not limited to, oxygen-containing combustion power plant flue gas, turbocharged boiler product gas, coal gasification product gas, Shifted coal gasification product gas, anaerobic digester product gas, oil well natural gas stream, and reformed natural gas or methane hydrate are included. If the gas contains both carbon dioxide and oxygen gas, the gas can be used both as a carbon dioxide source and as a source of oxygen. For example, flue gas obtained by combustion of oxygen and methane can contain oxygen gas and can provide a source of both carbon dioxide gas and oxygen gas.

  Thus, the exhaust stream is produced from a variety of different types of industrial plants. Exhaust streams suitable for the present invention include exhaust streams such as flue gas produced in industrial plants that combust fossil fuels (eg, coal, oil, natural gas) or naturally derived organic fuel deposits (eg, tar sands). , Heavy oil, oil shale, etc.). In some embodiments, an exhaust stream suitable for the systems and methods of the present invention is a coal combustion such as a pulverized coal power plant, a supercritical coal power plant, a mass combustion coal power plant, a fluidized bed coal power plant, etc. Supplied from a power plant. In some embodiments, the exhaust stream is supplied from a gas or oil fired boiler and steam turbine power plant, a gas or oil fired boiler simple cycle gas turbine power plant, or a gas or oil fired boiler combined cycle gas turbine power plant Is done. In some embodiments, an exhaust stream produced by a power plant that burns synthesis gas (ie, gas produced by gasification of organic matter such as coal, biomass, etc.) is used. In some embodiments, an exhaust stream from an integrated gasification combined cycle (IGCC) plant is used. In some embodiments, an exhaust stream produced from a Heat Recovery Steam Generator (HRSG) plant is used to produce a composition according to the systems and methods provided herein.

  The exhaust stream produced at the cement plant is also suitable for the systems and methods provided herein. Cement plant exhaust streams include exhaust streams from both wet and dry process plants, which can use shaft kilns or rotary kilns and can include pre-calcining furnaces. Each of these industrial plants may burn a single fuel or may burn two or more fuels sequentially or simultaneously.

  Carbon dioxide may be present in normal ambient air, but considering its very low concentration, ambient carbon dioxide is a bicarbonate such as that obtained when carbon from a carbon source is contacted with the cathode electrolyte and It is not possible to provide enough carbon dioxide to achieve carbonate production. In some embodiments of the system and method, the pressure in the electrochemical system may be higher than the ambient atmospheric pressure in the ambient air, thus generally preventing ambient carbon dioxide from penetrating into the cathode electrolyte. Can do.

  The contact system or contactor includes any means for contacting carbon from a carbon source with the cathode electrolyte inside or outside the cathode chamber. Such means for contacting carbon with the cathode electrolyte, or contactors configured to contact carbon from a carbon source with the cathode chamber are well known in the art and include, but are not limited to, Includes injections, pipes, ducts, and conduits. In some embodiments, the system includes a duct that directs carbon to the cathode electrolyte in the cathode chamber. When carbon from a carbon source is contacted with the cathode electrolyte in the cathode chamber, the carbon is from the bottom of the cell, from the top of the cell, from the side inlet in the cell, and / or depending on the amount of carbon desired in the cathode chamber. Alternatively, it should be understood that the cathode electrolyte can be injected from all inlet ports. The amount of carbon from the carbon source in the cathode chamber may depend on the flow rate of the solution, the desired pH of the cathode electrolyte, and / or the cell size. Such optimization of the amount of carbon from the carbon source is well within the scope of the present invention. In some embodiments, carbon from a carbon source is from gaseous carbon dioxide from an industrial process or a solution of carbon dioxide from a gas / liquid contactor in contact with gaseous carbon dioxide from an industrial process. Selected.

  In some embodiments, the cathode compartment includes a partition that facilitates delivery of carbon dioxide gas and / or a solution of carbon dioxide in the cathode compartment. In some embodiments, the septum can help prevent mixing of carbon dioxide gas and oxygen gas and / or mixing of carbon dioxide gas in the cathode chamber and hydrogen gas in the anode chamber. In some embodiments, the septum provides a catholyte comprising carbon dioxide in gas form as well as carbon dioxide in dissolved form. In some embodiments, a system provided herein is a partition that divides a cathode electrolyte into a first cathode electrolyte portion and a second cathode electrolyte portion, the second cathode electrolyte comprising dissolved carbon dioxide. A portion in contact with the cathode; a first cathode electrolyte portion comprising dissolved carbon dioxide and gaseous carbon dioxide includes a septum contacting the second cathode electrolyte portion under the septum. In this system, the septum is placed in the cathode electrolyte such that gas in the first cathode electrolyte portion, such as carbon dioxide, is separated from the cathode electrolyte in the second cathode electrolyte portion. Thus, the septum can serve as a means to prevent mixing of gas at the cathode and / or gas and / or vapor from the anode. Such septa are described in US Patent Publication No. 2010/0084280, filed Nov. 12, 2009, which is hereby incorporated by reference in its entirety.

In some embodiments, the carbon source is a gas / liquid contactor that provides a dissolved form of carbon dioxide or a solution of carbon dioxide comprising CO ₂ , carbonate, bicarbonate ion, carbonate ion, or combinations thereof. . In some embodiments, the partially or fully dissolved CO ₂ saturated solution is injected with a CO ₂ gaseous stream through the slurry or solution to create CO ₂ charged water, or It is produced by diffusing. In some embodiments, the CO ₂ saturated slurry or solution comprises a proton scavenger obtained from the cathode electrolyte of an electrochemical cell as described herein. In some embodiments, the gas / liquid contactor can include a bubble chamber in which CO ₂ gas is bubbled through a slurry or solution that includes a proton scavenger. In some embodiments, the contactor can include a spray tower that sprays or circulates a slurry or solution comprising a proton scavenger through CO ₂ gas. In some embodiments, the contactor can include a packed bed to increase the contact surface area between the solution containing the proton scavenger and the CO ₂ gas. For example, the gas / liquid contactor or absorber may include a sodium carbonate slurry or solution or a packed bed. CO ₂ is injected through this slurry or solution or packed bed, where the alkaline medium facilitates dissolution of CO ₂ into the solution. After dissolution of CO ₂ , the solution can contain bicarbonate, carbonate, or combinations thereof. In some embodiments, the fluid temperature of a typical absorber or contactor is 32-37 ° C. An absorber or contactor that absorbs CO ₂ into solution is described in US patent application Ser. No. 12 / 721,549, filed Mar. 10, 2010 (in this disclosure, which is hereby incorporated by reference in its entirety. Incorporated herein by reference). A solution containing a carbonate / bicarbonate species can be withdrawn from the gas / liquid contactor to produce a bicarbonate / carbonate product. In some embodiments, the carbonate / bicarbonate solution can be transferred to a cathode electrolyte containing alkali. This alkali can convert the bicarbonate substantially or completely to carbonate to form a carbonate solution. The carbonate solution can be recycled back to the gas / liquid contactor or withdrawn from the cathode chamber and treated with divalent cations to produce a bicarbonate / carbonate product.

  In some embodiments, the alkali generated in the cathode electrolyte may be sent to a gas / liquid contactor where carbon dioxide gas is contacted with the alkali. After contact with the alkali, the carbon dioxide gas can result in the production of carbonic acid, bicarbonate ions, carbonate ions or combinations thereof. The dissolved form of carbon dioxide can then be returned to the cathode chamber where the alkali can convert the bicarbonate to carbonate. The carbonate / bicarbonate mixture can then be used as such for commercial purposes or is treated with a divalent cation such as an alkaline earth metal ion to produce an alkaline earth metal carbonate / bicarbonate.

  The system in some embodiments includes a cathode electrolyte circulation system adapted to extract and circulate the cathode electrolyte in the system. In some embodiments, the cathode electrolyte circulation system includes a gas / liquid contactor adapted to contact carbon with a cathode electrolyte that circulates carbon from a carbon source and to recycle the electrolyte. Included outside the cathode chamber. Since the pH of the cathode electrolyte can be adjusted by extracting and / or circulating carbon from the cathode electrolyte / carbon source from the system, the pH of the cathode electrolyte compartment is removed from the system and the gas / liquid Control is possible by controlling the amount of cathode electrolyte that is passed through the contactor and / or recycled back to the cathode chamber.

In some embodiments, the carbon source is a bicarbonate brine solution. Bicarbonate brine solutions are available from US Provisional Application No. 61 / 433,641 filed Jan. 18, 2011 and 61 / 408,325 filed Oct. 29, 2010 (both in the present disclosure these are both The entirety of which is incorporated herein by reference). As used herein, a “bicarbonate brine solution” includes any brine containing bicarbonate ions. In some embodiments, the brine is a synthetic brine, such as a solution of a bicarbonate comprising, for example, sodium bicarbonate, potassium bicarbonate, lithium bicarbonate, and the like. In some embodiments, the brine is a naturally occurring bicarbonate brine, eg, a subterranean brine such as a naturally occurring lake. In some embodiments, the bicarbonate brine is made from underground brines such as, but not limited to, carbonate brine, alkaline brine, hard brine and / or alkaline hard brine. In some embodiments, the bicarbonate brine is made from a mineral that has been crushed and dissolved in the brine, and optionally further processed. Mineral substances can be found below, above or below the surface of the lake. Bicarbonate brine can also be made from evaporation residual rocks. Bicarbonate brine includes, in addition to bicarbonate (HCO ₃ ⁻ ), other oxyanions of carbon such as, but not limited to, carbonate (H ₂ CO ₃ ) and / or carbonate (CO ₃ ²⁻ ). be able to.

In some embodiments of the electrochemical cells described herein, the system includes carbon such as CO ₂ , carbonic acid, bicarbonate ions, carbonate ions or combinations thereof from a carbon source, and from a cathode electrolyte. It is comprised so that carbonate ion may be produced | generated by reaction with alkalis, such as sodium hydroxide. In some embodiments (not shown in the figure), carbon from a carbon source, such as gas form of carbon dioxide, can be contacted with the catholyte in the cathodic chamber and the hydroxide / carbonate / bicarbonate can be contacted. Catholyte containing carbonate can be withdrawn from the cathode chamber and contacted with a gas / liquid contactor outside the cathode chamber. In such embodiments, the catholyte from the gas / liquid contactor can be contacted again with the catholyte in the cathode chamber.

For systems where carbon from a carbon source contacts the cathode electrolyte outside the cathode chamber, the alkali-containing cathode electrolyte can be withdrawn from the cathode chamber and added to a container configured to contain carbon from the carbon source. be able to. The container may have a piping system in communication with the solution and / or bicarbonate brine containing the inlet or CO ₂ for carbon source, such as a pipe or conduit gaseous stream, the CO ₂ in the dissolved form. The vessel may be in fluid communication with a reactor capable of producing, modifying and / or storing a carbon source such as a bicarbonate brine solution.

  For systems in which carbon from a carbon source is contacted with a cathode electrolyte in a cathode chamber, a cathode electrolyte comprising alkali, bicarbonate and / or carbonate is withdrawn from the cathode chamber and an alkaline earth metal ion as described herein. To produce a bicarbonate / carbonate product.

Electrochemical Cell Components The methods and systems provided herein include one or more of the following components.

In some embodiments, the anode can include a conductive base support that is corrosion stable. For example, but not limited to, amorphous carbon, such as carbon black, specifically fluorinated as described in US Pat. No. 4,908,198 and marketed under the trade name SFC ™ Carbons. Fluorinated carbon like carbon. Other examples of electrically conductive base materials include, but are not limited to, substoichiometric titanium oxide, such as magnesium having the formula TiO _{x, where} x ranges from about 1.67 to about 1.9. Phase-stoichiometric titanium oxide is included. For example, titanium oxide Ti ₄ O ₇ . In some embodiments, the carbon-based material provides a mechanical support for GDE or as a blend material to increase electrical conductivity, but uses it as a catalyst support to prevent corrosion I can't do it.

In some embodiments, a gas diffusion electrode or a generic electrode described herein is an electrocatalyst (eg, to assist in electrochemical dissociation, for example, reduction of oxygen at the cathode or oxidation of metal ions at the anode). electrocatalyst). Examples of electrocatalysts include highly dispersed platinum group metal metals or alloys such as platinum, palladium, ruthenium, rhodium, iridium, or combinations thereof (eg, platinum-rhodium, platinum-ruthenium, PtIr mixed metal oxides). Metal-coated titanium mesh or galvanized platinum-coated titanium, etc.); electrocatalytic metal oxides (eg, but not limited to IrO ₂ ); gold, tantalum, carbon, graphite, organometallic large Examples include, but are not limited to, cyclic compounds and other electrocatalysts known in the art for electrochemical reduction of oxygen or oxidation of metals.

  In some embodiments, the electrodes described herein include porous uniform composite structures and physical and compositional configurations in which each layer is clearly distinguishable, such as electrical conductivity to prevent porosity and flooding. It relates to a non-uniform layered type composite structure that can have a conductive base and loss of the three-phase interface and the resulting electrode performance.

  In some embodiments, the electrode provided herein can be a porous polymer on or adjacent to the anodic or cathodic solution side of the electrode that can help reduce penetration and electrode fouling. An anode having a layer and a cathode can be included. A stable polymeric resin or film may be included in the composite electrode layer adjacent to the anolyte, which may be a nonionic polymer such as polystyrene, polyvinyl chloride, polysulfone, or polystyrene sulfonic acid, styrene and vinyl. Formed from ionically charged polymers such as those formed from sulfonated copolymers of benzene, carboxylated polymer derivatives, sulfonated or carboxylated polymers with partially or fully fluorinated hydrocarbon chains and aminated polymers such as polyvinylpyridine Contains resin. A stable microporous polymer film can be included on the dry side to prevent electrolyte penetration. In some embodiments, the gas diffusion cathode includes such cathodes known in the art that are coated with a high surface area coating such as noble metals such as gold and / or silver, noble metal alloys, and nickel.

  In some embodiments, the methods and systems provided herein include an anode that allows for increased diffusion of electrolyte in or around the anode. Applicants have found that the anode shape and / or geometry can affect the flow or velocity of the anode electrolyte around the anode in the anode chamber, thus improving mass transfer, It has been discovered that the voltage of the cell may be reduced. In some embodiments, the methods and systems provided herein include an anode that is a “diffusion enhanced” anode. As used herein, a “diffusion enhanced” anode includes an anode that enhances diffusion of electrolyte in and / or around the anode, thereby enhancing reaction at the anode. In some embodiments, the diffusion enhanced anode is a porous anode. As used herein, “porous anode” includes an anode having pores therein. Applicants have unexpectedly and surprisingly realized that diffusion enhanced anodes (eg, but not limited to porous anodes) used in the methods and systems provided herein are electrochemical systems. In some advantages over non-diffusive or non-porous anodes (this advantage is greater surface area, increased active sites, reduced voltage, reduced or eliminated resistance due to anode electrolyte, increased current density, anode electrolyte Including, but not limited to, increased turbulence in the medium and / or improved mass transfer.

  A diffusion enhanced anode (eg, but not limited to a porous anode) may be flat or non-flat. For example, in some embodiments, a diffusion-enhanced anode (eg, but not limited to a porous anode) has a flat form (the flat form is a flattened flat form, a perforated plate, a network structure, etc. Including, but not limited to). In some embodiments, the diffusion enhanced anode (eg, but not limited to a porous anode) comprises a stretched mesh or is a flat stretched mesh anode.

  In some embodiments, a diffusion enhanced anode (eg, but not limited to a porous anode) is non-flat or has a corrugated geometry. In some embodiments, the corrugated geometry of the anode can provide additional benefits of turbulence to the anode electrolyte and improve mass transfer at the anode. As used herein, “corrugated” or “corrugated geometry” or “corrugated anode” includes an anode that is not flat, ie, non-flat. The corrugated geometric structure of the anode includes non-flat shape, stretched non-flat shape, stepped shape, undulating shape, wavy shape, 3D shape, crimp shape, groove shape, pleat shape, pucker shape, ridge Shapes, frills, ripples, wrinkles, woven mesh, punched tab style, etc., but are not limited thereto.

  Some examples of flat and corrugated geometry of diffusion enhanced anodes (eg, but not limited to porous anodes) are illustrated in FIG. These examples are for illustrative purposes only, and any other variations from these geometric structures are well within the scope of the present invention. FIG. 16A is an example of a flat stretched anode, and FIG. 16B is an example of a corrugated anode.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and And generating the method.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with a cathode electrolyte, and unsaturated hydrocarbon or saturated carbonization. Reacting hydrogen with an anode electrolyte containing higher oxidation state metal ions to produce a halogenated hydrocarbon.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode ( For example, but not limited to, a porous anode), oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and greater than 5 wt% water. Reacting an unsaturated hydrocarbon or saturated hydrocarbon with an anode electrolyte containing a metal ion in the higher oxidation state in an aqueous medium comprising: a halogenated hydrocarbon.

  In some embodiments of the above methods, unsaturated hydrocarbons (such as Formula I), saturated hydrocarbons (such as Formula III), halogenated hydrocarbons (such as Formulas II and IV), metal ions, and the like are all herein. Is described in detail.

  In some embodiments of the above method, the aqueous medium is greater than 5 wt% water, or greater than 5.5 wt%, or greater than 6 wt%, or between 5-90 wt%, or 5-95 wt% %, Or 5 to 99% by weight of water, or 5.5 to 90% by weight, or 5.5 to 95% by weight, or 5.5 to 99% by weight of water, Or between 6 and 90 wt%, or between 6 and 95 wt%, or between 6 and 99 wt%.

  In some embodiments of the above method, the cathode produces water, alkali and / or hydrogen gas. In some embodiments of the above method, the cathode is an ODC that produces water. In some embodiments of the above method, the cathode is an ODC that produces alkali. In some embodiments of the above method, the cathode produces hydrogen gas. In some embodiments of the above method, the cathode is an oxygen depolarized cathode that reduces oxygen and water to hydroxide ions, or the cathode generates hydrogen gas that reduces water to hydrogen gas and hydroxide ions. Either the cathode, the cathode is a hydrogen gas generating cathode that reduces hydrochloric acid to hydrogen gas, or the cathode is an oxygen depolarized cathode that reacts hydrochloric acid and oxygen gas to form water.

  In some embodiments of the above method, the metal ion is any metal ion described herein. In some embodiments of the above method, the metal ions are iron, chromium, copper, tin, silver, cobalt, uranium, lead, mercury, vanadium, bismuth, titanium, ruthenium, osmium, europium, zinc, cadmium, gold , Nickel, palladium, platinum, rhodium, iridium, manganese, technetium, rhenium, molybdenum, tungsten, niobium, tantalum, zirconium, hafnium, and combinations thereof. In some embodiments, the metal ion is selected from the group consisting of iron, chromium, copper and tin. In some embodiments, the metal ion is copper. In some embodiments, the lower oxidation state of the metal ion is 1+, 2+, 3+, 4+ or 5+. In some embodiments, the higher oxidation state of the metal ion is 2+, 3+, 4+, 5+ or 6+.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising copper ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing copper ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and forming hydroxide at the cathode. And generating the method.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising copper ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing copper ions from a lower oxidation state to a higher oxidation state, contacting the cathode with a cathode electrolyte, unsaturated hydrocarbon or saturated carbon Reacting hydrogen with an anode electrolyte comprising higher oxidation copper ions to produce a halogenated hydrocarbon.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising copper ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing copper ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and greater than 5 wt% water. Reacting an unsaturated hydrocarbon or saturated hydrocarbon with an anode electrolyte comprising the higher oxidation state copper ions in an aqueous medium comprising the production of a halogenated hydrocarbon.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising copper ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing copper ions from a lower oxidation state to a higher oxidation state, contacting the cathode with a cathode electrolyte, and ethylene in the higher oxidation state. Reacting with an anode electrolyte comprising copper ions to produce ethylene dichloride.

  In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising copper ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing copper ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and greater than 5 wt% water. Reacting ethylene with an anode electrolyte containing higher oxidation copper ions in an aqueous medium containing to produce ethylene dichloride.

  In some embodiments of the above methods and embodiments, the use of a diffusion enhanced anode (eg, but not limited to a porous anode) is 10 to 10 compared to a non-diffusing or non-porous anode. Provides voltage savings between 500 mV, or 50-250 mV, or 100-200 mV, or 200-400 mV, or 25-450 mV, or 250-350 mV, or 100-500 mV .

  In some embodiments of the above methods and embodiments, the use of a corrugated anode is between 10-500 mV, or between 50-250 mV, or between 100-200 mV, or compared to a flat porous anode, or It provides a voltage saving between 200-400 mV, or between 25-450 mV, or between 250-350 mV, or between 100-500 mV.

  Diffusion-enhanced anodes (eg, but not limited to porous anodes) have various parameters (number of mesh lines per inch, mesh size, pore size, wire thickness or wire diameter, open area) Including, but not limited to, percentage, waveform amplitude, waveform repetition period, etc.). These characteristics of diffusion enhanced anodes (eg, but not limited to porous anodes) are characteristic of porous anodes (eg, increased surface area for anodic reaction, reduced solution resistance, between anode and cathode) Such as, but not limited to, a decrease in the voltage applied to the anode, an increase in electrolyte turbulence across the anode, and / or improved mass transfer at the anode.

  In some embodiments of the methods and embodiments described above, the diffusion enhanced anode (eg, but not limited to a porous anode) is between 2 × 1 mm and 20 × 10 mm, or 2 × 1 mm to 10 ×. Between 5 mm, or between 2 × 1 mm and 5 × 5 mm, or between 1 × 1 mm and 20 × 10 mm, or between 1 × 1 mm and 10 × 5 mm, or between 1 × 1 mm and 5 × 5 mm, or 5 Having a pore opening size (as illustrated in FIG. 16) in a range such as between x1 mm and 10 x5 mm, or between 5 x1 mm and 20 x10 mm, or between 10 x5 mm and 20 x10 mm. Can do. It should be understood that the pore size of the porous anode may also depend on the pore geometry. For example, the geometric structure of the pores may be rhombus or square. For the rhombus geometry, the pore size may be, for example, 3 × 10 mm (3 mm is the width of the rhombus and 10 mm is its length), or vice versa. For a square geometry, the pore size is, for example, 3 mm on each side. The woven mesh may be a mesh having square pores, and the stretched mesh may be a mesh having rhombic pores.

  In some embodiments of the above methods and embodiments, the diffusion enhanced anode (e.g., but not limited to a porous anode) is between 0.5 mm and 5 mm, or between 0.5 mm and 4 mm, Or between 0.5 mm and 3 mm, or between 0.5 mm and 2 mm, or between 0.5 mm and 1 mm, or between 1 mm and 5 mm, or between 1 mm and 4 mm, or between 1 mm and 3 mm, or 1 mm Between ˜2 mm, or between 2 mm and 5 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 0.5 mm and 2.5 mm, or between 0.5 mm and 1.5 mm, or 1 mm Between -1.5 mm, or between 1 mm-2.5 mm, or between 2.5 mm-3 mm, or 0.5 mm, or 1 mm, or 2 mm, and It may have thickness or mesh thickness of 3mm pores wire (such as illustrated in FIG. 16).

  In some embodiments of the above methods and embodiments, if the diffusion enhanced anode (eg, but not limited to a porous anode) is a corrugated anode, the corrugated anode is between 1 mm and 8 mm, or 1 mm. Between -7 mm, or between 1 mm and 6 mm, or between 1 mm and 5 mm, or between 1 mm and 4 mm, or between 1 mm and 4.5 mm, or between 1 mm and 3 mm, or between 1 mm and 2 mm, or Between 2 mm and 8 mm, or between 2 mm and 6 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 3 mm and 8 mm, or between 3 mm and 7 mm, or between 3 mm and 5 mm, or 3 mm Between -4 mm, or between 4 mm and 8 mm, or between 4 mm and 5 mm, or between 5 mm and 7 mm, or 5 m It can have a range of wave amplitude between ～8Mm (as illustrated in FIG. 16).

  In some embodiments of the above methods and embodiments, when the diffusion enhanced anode (eg, but not limited to a porous anode) is a corrugated anode, the corrugated anode is between 2 mm and 35 mm, or 2 mm. Between 32 mm, or between 2 mm and 30 mm, or between 2 mm and 25 mm, or between 2 mm and 20 mm, or between 2 mm and 16 mm, or between 2 mm and 10 mm, or between 5 mm and 35 mm, or between 5 mm and Between 30 mm, or between 5 mm and 25 mm, or between 5 mm and 20 mm, or between 5 mm and 16 mm, or between 5 mm and 10 mm, or between 15 mm and 35 mm, or between 15 mm and 30 mm, or between 15 mm and 25 mm Between, or between 15 mm and 20 mm, or between 20 mm and 35 mm It may have between, or between 25Mm～30mm or between 25mm~35mm or scope waveform period of between 25Mm～30mm (not shown),,.

In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and The anode is between 2 × 1 mm and 20 × 10 mm, or between 2 × 1 mm and 10 × 5 mm, or between 2 × 1 mm and 5 × 5 mm, or between 1 × 1 mm and 20 × 10 mm, or 1 × 1 mm to 10 × 5 mm, or 1 × 1 mm to 5 × 5 mm. Or a pore opening size in the range between 5 × 1 mm and 10 × 5 mm, or between 5 × 1 mm and 20 × 10 mm, or between 10 × 5 mm and 20 × 10 mm;
Between 0.5 mm and 5 mm, or between 0.5 mm and 4 mm, or between 0.5 mm and 3 mm, or between 0.5 mm and 2 mm, or between 0.5 mm and 1 mm, or between 1 mm and 5 mm Or between 1 mm and 4 mm, or between 1 mm and 3 mm, or between 1 mm and 2 mm, or between 2 mm and 5 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 0.5 mm and 2. Between 5 mm, or between 0.5 mm and 1.5 mm, or between 1 mm and 1.5 mm, or between 1 mm and 2.5 mm or between 2.5 mm and 3 mm, or 0.5 mm, or 1 mm , Or 2 mm or 3 mm pore wire thickness or mesh thickness;
Between 1 mm and 8 mm, or between 1 mm and 7 mm, or between 1 mm and 6 mm, or between 1 mm and 5 mm, or between 1 mm and 4 mm, or between 1 mm and 4.5 mm, or between 1 mm and 3 mm, Or between 1 mm and 2 mm, or between 2 mm and 8 mm, or between 2 mm and 6 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 3 mm and 8 mm, or between 3 mm and 7 mm, or Waveform amplitude in the range between 3 mm and 5 mm, or between 3 mm and 4 mm, or between 4 mm and 8 mm, or between 4 mm and 5 mm, or between 5 mm and 7 mm, or between 5 mm and 8 mm; and 2 mm and 35 mm , Or between 2 mm and 32 mm, or between 2 mm and 30 mm, or between 2 mm and 25 mm, or between 2 mm and 20 m m, or 2 mm to 16 mm, or 2 mm to 10 mm, or 5 mm to 35 mm, or 5 mm to 30 mm, or 5 mm to 25 mm, or 5 mm to 20 mm, or 5 mm to 16 mm. Between, or between 5 mm and 10 mm, or between 15 mm and 35 mm, or between 15 mm and 30 mm, or between 15 mm and 25 mm, or between 15 mm and 20 mm, or between 20 mm and 35 mm, or between 25 mm and 30 mm Or including one or more of the waveform periods in the range between 25 mm and 35 mm, or between 25 mm and 30 mm.

In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with a cathode electrolyte, and unsaturated hydrocarbon or saturated carbonization. Reacting hydrogen with an anode electrolyte containing metal ions in a higher oxidation state to produce a halogenated hydrocarbon, wherein the anode is between 2 × 1 mm and 20 × 10 mm, or 2 × 1 mm Between 10 × 5 mm, or between 2 × 1 mm and 5 × 5 mm, or 1 × 1 mm Between 20 × 10 mm, or between 1 × 1 mm and 10 × 5 mm, or between 1 × 1 mm and 5 × 5 mm, or between 5 × 1 mm and 10 × 5 mm, or between 5 × 1 mm and 20 × 10 mm, Or a pore opening size in the range between 10 × 5 mm and 20 × 10 mm;
Between 0.5 mm and 5 mm, or between 0.5 mm and 4 mm, or between 0.5 mm and 3 mm, or between 0.5 mm and 2 mm, or between 0.5 mm and 1 mm, or between 1 mm and 5 mm Or between 1 mm and 4 mm, or between 1 mm and 3 mm, or between 1 mm and 2 mm, or between 2 mm and 5 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 0.5 mm and 2. Between 5 mm, or between 0.5 mm and 1.5 mm, or between 1 mm and 1.5 mm, or between 1 mm and 2.5 mm or between 2.5 mm and 3 mm, or 0.5 mm, or 1 mm , Or 2 mm or 3 mm pore wire thickness or mesh thickness;
Between 1 mm and 8 mm, or between 1 mm and 7 mm, or between 1 mm and 6 mm, or between 1 mm and 5 mm, or between 1 mm and 4 mm, or between 1 mm and 4.5 mm, or between 1 mm and 3 mm, Or between 1 mm and 2 mm, or between 2 mm and 8 mm, or between 2 mm and 6 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 3 mm and 8 mm, or between 3 mm and 7 mm, or Waveform amplitude in the range between 3 mm and 5 mm, or between 3 mm and 4 mm, or between 4 mm and 8 mm, or between 4 mm and 5 mm, or between 5 mm and 7 mm, or between 5 mm and 8 mm; and 2 mm and 35 mm , Or between 2 mm and 32 mm, or between 2 mm and 30 mm, or between 2 mm and 25 mm, or between 2 mm and 20 m m, or 2 mm to 16 mm, or 2 mm to 10 mm, or 5 mm to 35 mm, or 5 mm to 30 mm, or 5 mm to 25 mm, or 5 mm to 20 mm, or 5 mm to 16 mm. Between, or between 5 mm and 10 mm, or between 15 mm and 35 mm, or between 15 mm and 30 mm, or between 15 mm and 25 mm, or between 15 mm and 20 mm, or between 20 mm and 35 mm, or between 25 mm and 30 mm Or including one or more of the waveform periods in the range between 25 mm and 35 mm, or between 25 mm and 30 mm.

In some embodiments, contacting a diffusion enhanced anode (eg, but not limited to a porous anode) with an anode electrolyte, the anode electrolyte comprising metal ions, and a diffusion enhanced anode (eg, A porous anode, but not limited to) oxidizing metal ions from a lower oxidation state to a higher oxidation state, contacting the cathode with the cathode electrolyte, and greater than 5 wt% water. Reacting an unsaturated hydrocarbon or saturated hydrocarbon with an anode electrolyte containing a metal oxide in a higher oxidation state in an aqueous medium comprising the halogenated hydrocarbon, wherein the anode comprises the following 2 Between x1mm and 20x10mm, or between 2x1mm and 10x5mm, or 2x1m Between -5 x 5 mm, or between 1 x 1 mm and 20 x 10 mm, or between 1 x 1 mm and 10 x 5 mm, or between 1 x 1 mm and 5 x 5 mm, or between 5 x 1 mm and 10 x 5 mm. Or pore opening size in the range between 5 × 1 mm and 20 × 10 mm, or between 10 × 5 mm and 20 × 10 mm;
Between 0.5 mm and 5 mm, or between 0.5 mm and 4 mm, or between 0.5 mm and 3 mm, or between 0.5 mm and 2 mm, or between 0.5 mm and 1 mm, or between 1 mm and 5 mm Or between 1 mm and 4 mm, or between 1 mm and 3 mm, or between 1 mm and 2 mm, or between 2 mm and 5 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 0.5 mm and 2. Between 5 mm, or between 0.5 mm and 1.5 mm, or between 1 mm and 1.5 mm, or between 1 mm and 2.5 mm or between 2.5 mm and 3 mm, or 0.5 mm, or 1 mm , Or 2 mm or 3 mm pore wire thickness or mesh thickness;
Between 1 mm and 8 mm, or between 1 mm and 7 mm, or between 1 mm and 6 mm, or between 1 mm and 5 mm, or between 1 mm and 4 mm, or between 1 mm and 4.5 mm, or between 1 mm and 3 mm, Or between 1 mm and 2 mm, or between 2 mm and 8 mm, or between 2 mm and 6 mm, or between 2 mm and 4 mm, or between 2 mm and 3 mm, or between 3 mm and 8 mm, or between 3 mm and 7 mm, or Waveform amplitude in the range between 3 mm and 5 mm, or between 3 mm and 4 mm, or between 4 mm and 8 mm, or between 4 mm and 5 mm, or between 5 mm and 7 mm, or between 5 mm and 8 mm; and 2 mm and 35 mm , Or between 2 mm and 32 mm, or between 2 mm and 30 mm, or between 2 mm and 25 mm, or between 2 mm and 20 m m, or 2 mm to 16 mm, or 2 mm to 10 mm, or 5 mm to 35 mm, or 5 mm to 30 mm, or 5 mm to 25 mm, or 5 mm to 20 mm, or 5 mm to 16 mm. Between, or between 5 mm and 10 mm, or between 15 mm and 35 mm, or between 15 mm and 30 mm, or between 15 mm and 25 mm, or between 15 mm and 20 mm, or between 20 mm and 35 mm, or between 25 mm and 30 mm Or including one or more of the waveform periods in the range between 25 mm and 35 mm, or between 25 mm and 30 mm.

In some embodiments, the diffusion enhanced anode (eg, but not limited to a porous anode) is made from an electrocatalyst coated metal (eg, titanium, etc.). Examples of electrocatalysts are described above, and examples of electrocatalysts include highly dispersed platinum group metal metals or alloys such as platinum, palladium, ruthenium, rhodium, iridium, or combinations thereof (eg, platinum -Rhodium, platinum-ruthenium, titanium mesh coated with PtIr mixed metal oxides or titanium coated with galvanized platinum, etc .; electrocatalytic metal oxides (eg but not limited to IrO ₂ ); Examples include, but are not limited to, gold, tantalum, carbon, graphite, organometallic macrocycles, and other electrocatalysts known in the art. Diffusion enhanced anodes (eg, but not limited to porous anodes) may be commercially available or made of a suitable metal. The electrode may be coated with an electrocatalyst using processes well known in the art. For example, the metal may be immersed in a coating catalyst solution and subjected to processes such as heating, sandblasting, and the like. Such methods of fabricating the anode and coating with a catalyst are well known in the art.

  In some embodiments, in the systems and methods provided herein, an electrolyte comprising a catholyte or catholyte and / or an anolyte or anolyte or a third electrolyte disposed between an AEM and a CEM Including, but not limited to, salt water or fresh water. Salt water includes, but is not limited to, sea water, brine and / or black water. In some embodiments, the cathode electrolyte in the systems and methods provided herein includes, but is not limited to, seawater, fresh water, brine, hemihydrate, hydroxides such as sodium hydroxide or combinations thereof. included. “Salt water” is used in its conventional sense to refer to several different types of aqueous fluids other than fresh water, and the term “salt water” includes, but is not limited to, half salt water, sea water and brine (naturally occurring). Underground brines or artificial underground brines and artificial brines (including, for example, geothermal plant wastewater, desalination wastewater, etc.) and other saline solutions that contain more salt than freshwater salinity. Brine is water that is saturated or nearly saturated in salt and has a salinity of 50 ppt (parts per thousand) or more. Half-saline is water having a salinity in the range of 0.5 to 35 ppt, which contains more salt than fresh water but not as much as seawater. Seawater is water from the sea or ocean and has a salinity in the range of 35-50 ppt. The salt water source may be a natural source such as the sea, ocean, lake, marsh, estuary, lagoon, or an artificial source. In some embodiments, the systems provided herein include brine from terrestrial brine. In some embodiments, the depleted brine drawn from the electrochemical cell is replenished with salt and recycled back to the electrochemical cell.

  In some embodiments, the electrolyte comprising a cathode electrolyte and / or an anode electrolyte and / or a third electrolyte, such as brine, has a chloride content of greater than 1%, such as NaCl; or greater than 10% NaCl; or 20% Greater than NaCl; or greater than 40% NaCl; or greater than 50% NaCl; or greater than 60% NaCl; or greater than 70% NaCl; or greater than 80% NaCl; or greater than 90% Or between 1 and 99% NaCl; or between 1 and 95% NaCl; or between 1 and 90% NaCl; or between 1 and 80% NaCl; or between 1 and 70% NaCl; or between 1-60% NaCl; or between 1-50% NaCl; or between 1-40% NaCl; or between 1-30% aCl; or 1-20% NaCl; or 1-10% NaCl; or 10-99% NaCl; or 10-95% NaCl; or 10-90% NaCl; or 10-80% NaCl; or 10-70% NaCl; or 10-60% NaCl; or 10-50% NaCl; or 10-40% NaCl; or between 10-30% NaCl; or between 10-20% NaCl; or between 20-99% NaCl; or between 20-95% NaCl; or between 20-90% NaCl; or 20 to 80% NaCl; or 20 to 70% NaCl; or 20 to 60% NaCl; or 20 to 50% NaCl; or 20 to 4 % NaCl; or 20-30% NaCl; or 30-99% NaCl; or 30-95% NaCl; or 30-90% NaCl; or 30-80 % NaCl; or 30-70% NaCl; or 30-60% NaCl; or 30-50% NaCl; or 30-40% NaCl; or 40-99. % NaCl; or 40-95% NaCl; or 40-90% NaCl; or 40-80% NaCl; or 40-70% NaCl; or 40-60 % NaCl; or 40-50% NaCl; or 50-99% NaCl; or 50-95% NaCl; or 50-90% NaCl; Or 50 to 80% NaCl; or 50 to 70% NaCl; or 50 to 60% NaCl; or 60 to 99% NaCl; or 60 to 95% NaCl. Or 60-90% NaCl; or 60-80% NaCl; or 60-70% NaCl; or 70-99% NaCl; or 70-95% NaCl; Or 70-90% NaCl; or 70-80% NaCl; or 80-99% NaCl; or 80-95% NaCl; or 80-90% NaCl; Or water containing 90-99% NaCl; or 90-95% NaCl. In some embodiments, the above ratios apply to ammonium chloride, ferric chloride, sodium bromide, sodium iodide or sodium sulfate as the electrolyte. Ratios noted herein include weight percent, weight / weight percent or weight / volume percent. All electrochemical systems described herein, including sodium chloride, should be replaced with other suitable electrolytes such as, but not limited to, ammonium chloride, sodium bromide, sodium iodide, sodium sulfate, or combinations thereof. It should be understood that

  In some embodiments, the cathode electrolyte, such as saline, fresh water and / or sodium hydroxide, does not contain alkaline earth metal ions or divalent cations. As used herein, divalent cations include, but are not limited to, alkaline earth metal ions such as calcium, magnesium, barium, strontium, radium. In some embodiments, the cathode electrolyte, such as brine, fresh water and / or sodium hydroxide, contains less than 1% w / w divalent cation. In some embodiments, the cathode electrolyte, such as sea water, fresh water, brine, half salt water, and / or sodium hydroxide, contains less than 1% w / w divalent cation. In some embodiments, the cathode electrolyte, such as seawater, fresh water, brine, half salt water, and / or sodium hydroxide, includes divalent cations including, but not limited to, calcium, magnesium, and combinations thereof. In some embodiments, the cathode electrolyte, such as seawater, fresh water, brine, half salt water, and / or sodium hydroxide, includes but is not limited to less than 1% w / w% including calcium, magnesium, and combinations thereof. Contains a valent cation.

  In some embodiments, the cathode electrolyte, such as sea water, fresh water, brine, hemihydrate and / or sodium hydroxide, is less than 1% w / w; or less than 5% w / w; or less than 10% w / w; Or less than 15 wt / wt%; or less than 20 wt / wt%; or less than 25 wt / wt%; or less than 30 wt / wt%; or less than 40 wt / wt%; or less than 50 wt / wt%; or 60 Less than 70% w / w; or less than 80% w / w; or less than 90% w / w; or less than 95% w / w; or between 0.05 and 1% w / w Or between 0.5 and 1 wt / wt%; or between 0.5 and 5 wt / wt%; or between 0.5 and 10 wt / wt%; or between 0.5 and 20 wt / wt% Between; Between 0.5 and 30 wt / wt%; or between 0.5 and 40 wt / wt%; or between 0.5 and 50 wt / wt%; or between 0.5 and 60 wt / wt% Between; or between 0.5 and 70 wt / wt%; or between 0.5 and 80 wt / wt%; or between 0.5 and 90 wt / wt%; or between 5 and 8 wt / wt% Between; or between 5-10 wt / wt%; or between 5-20 wt / wt%; or between 5-30 wt / wt%; or between 5-40 wt / wt%; or 5-50 Between wt / wt%; or between 5-60 wt / wt%; or between 5-70 wt / wt%; or between 5-80 wt / wt%; or between 5-90 wt / wt% Or between 10 and 20 wt / wt%; or between 10 and 30 wt / wt%; or between 10 and 40 wt / wt% Or between 10 and 50 wt / wt%; or between 10 and 60 wt / wt%; or between 10 and 70 wt / wt%; or between 10 and 80 wt / wt%; or between 10 and 90 wt% Between / wt%; or between 30-40 wt / wt%; or between 30-50 wt / wt%; or between 30-60 wt / wt%; or between 30-70 wt / wt%; Or between 30 and 80 wt / wt%; or between 30 and 90 wt / wt%; or between 50 and 60 wt / wt%; or between 50 and 70 wt / wt%; or between 50 and 80 wt /% Or between 50 and 90 wt / wt%; or between 75 and 80 wt / wt%; or between 75 and 90 wt / wt%; or between 80 and 90 wt / wt%; or Divalent cations between 90-95 wt / wt% (divalent Cations include, but are not limited to, calcium, magnesium and combinations thereof.

  In some embodiments, the cathode electrolyte includes, but is not limited to, sodium hydroxide, sodium bicarbonate, sodium carbonate, or combinations thereof. In some embodiments, the cathode electrolyte includes, but is not limited to, sodium hydroxide or potassium hydroxide. In some embodiments, the cathode electrolyte includes, but is not limited to, sodium hydroxide, divalent cations, or combinations thereof. In some embodiments, the cathode electrolyte includes, but is not limited to, sodium hydroxide, sodium bicarbonate, sodium carbonate, divalent cations or combinations thereof. In some embodiments, the cathode electrolyte includes, but is not limited to, sodium hydroxide, calcium bicarbonate, calcium carbonate, magnesium bicarbonate, magnesium carbonate, calcium magnesium carbonate, or combinations thereof. In some embodiments, the cathode electrolyte includes, but is not limited to, brine, sodium hydroxide, bicarbonate brine solution, or combinations thereof. In some embodiments, the cathode electrolyte includes, but is not limited to, brine and sodium hydroxide. In some embodiments, the cathode electrolyte includes, but is not limited to, fresh water and sodium hydroxide. In some embodiments, the cathode electrolyte comprises fresh water that has neither alkalinity nor divalent cations. In some embodiments, the cathode electrolyte includes, but is not limited to, fresh water, sodium hydroxide, sodium bicarbonate, sodium carbonate, divalent cations, or combinations thereof.

  In some embodiments, the anode electrolyte includes, but is not limited to, fresh water and metal ions. In some embodiments, the anode electrolyte includes, but is not limited to, brine and metal ions. In some embodiments, the anolyte comprises a metal ion solution.

  In some embodiments, the depleted salt water from the cell can be circulated back to the cell. In some embodiments, the cathode electrolyte is 1-90%; 1-50%; or 1-40%; or 1-30%; or 1-15%; or 1-20%; or 1-10%. Or 5 to 90%; or 5 to 50%; or 5 to 40%; or 5 to 30%; or 5 to 20%; or 5 to 10%; or 10 to 90%; or 10 to 50%; 10-40%; or 10-30%; or 10-20%; or 15-20%; or 15-30%; or 20-30% sodium hydroxide solution. In some embodiments, the anode electrolyte is 0-5M; or 0-4.5M; or 0-4M; or 0-3.5M; or 0-3M; or 0-2.5M; or 0-2M. Or 0 to 1.5M; or 0 to 1M; or 1 to 5M; or 1 to 4.5M; or 1 to 4M; or 1 to 3.5M; or 1 to 3M; or 1 to 2.5M; 1 to 2M; or 1 to 1.5M; or 2 to 5M; or 2 to 4.5M; or 2 to 4M; or 2 to 3.5M; or 2 to 3M; or 2 to 2.5M; 5M; or 3-4.5M; or 3-4M; or 3-3.5M; or 4-5M; or 4.5-5M. In some embodiments, the anode does not produce oxygen gas. In some embodiments, the anode does not produce chlorine gas.

In some embodiments, the cathode and anode electrolytes are partially or completely separated by an ion exchange membrane. In some embodiments, the ion exchange membrane is an anion exchange membrane or a cation exchange membrane. In some embodiments, the cation exchange membrane in an electrochemical cell as disclosed herein is conventional, such as Asahi Kasei in Japan (Tokyo); or Membrane International (Glen Rock, NJ) in the United States. Alternatively, it can be obtained from DuPont. Examples of CEM include, but are not limited to, N2030WX (Dupont), F8020 / F8080 (Flemion) and F6801 (Aciplex). The desired CEM in the method and system of the present invention has minimal resistance loss, selectivity greater than 90% and high stability in dense caustic. In the method and system of the present invention, AEM is exposed to a concentrated metal salt anolyte and a saturated brine stream. AEM allows the passage of salt ions, such as chloride ions, to the anolyte, but desirably rejects metal ionic species from the anolyte. In some embodiments, the metal salt comprises a variety of ionic species (cations, anions and / or neutrals) including, but not limited to, MCl ⁺ , MCl ₂ ⁻ , MCl ₂ ⁰ , M ^{2+ and the} like. Although it can be formed, it is desirable that such complexes do not pass through the AEM or foul the membrane. Provided in the examples are some of the membranes tested for the methods and systems of the present invention that have been found to prevent metal crossover.

Thus, contacting the metal ion with the anode in the anode electrolyte of the anode chamber; converting the metal ion from a lower oxidation state to a higher oxidation state at the anode; contacting the cathode electrolyte with the cathode in the cathode chamber; Generating an alkali, water or hydrogen gas at the cathode; and preventing migration of metal ions from the anode electrolyte to the cathode electrolyte by using an anion exchange membrane, the anion exchange membrane There is provided below 3Omucm ^2, the method having the ohmic resistance of less than ² or 1Ωcm than ² 2Omucm herein. In some embodiments, the anion exchange membrane has an ohmic resistance of 1-3 Ωcm ² . In some embodiments, contacting the metal ions with the anode in the anode electrolyte of the anode chamber; converting the metal ions from a lower oxidation state to a higher oxidation state at the anode; and the cathode electrolyte and cathode in the cathode chamber A step of generating alkali, water or hydrogen gas at the cathode; and preventing the migration of metal ions from the anode electrolyte to the cathode electrolyte by using an anion exchange membrane comprising: The anion exchange membrane provides a method for rejecting more than 80%, 90% or 99% or about 99.9% of all metal ions from the anode electrolyte.

An anode in contact with metal ions in the anode electrolyte of the anode chamber, the anode configured to convert the metal ions from a lower oxidation state to a higher oxidation state in the anode chamber; a cathode electrolyte in the cathode chamber; anion exchange with less than 3Omucm ^2, the ohmic resistance of less than ² or 1Ωcm than ² 2Omucm; a cathode in contact, the alkali in the cathode compartment, water or a cathode and configured to produce hydrogen gas and A system comprising a membrane is also provided. In some embodiments, the anion exchange membrane has an ohmic resistance between 1 and 3 Ωcm ² . In some embodiments, an anode in contact with metal ions in the anode electrolyte of the anode chamber, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber A cathode in contact with the cathode electrolyte in the cathode chamber, the cathode configured to produce alkali, water or hydrogen gas in the cathode chamber; and all metal ions from the anode electrolyte And an anion exchange membrane that rejects greater than 80%, greater than 90% or greater than 99%, or about 99.9%.

Contacting the metal ion with the anode in the anode electrolyte of the anode chamber; converting the metal ion from a lower oxidation state to a higher oxidation state at the anode; contacting the cathode electrolyte with the cathode in the cathode chamber; and separating the anode electrolyte from the brine compartments in an anion exchange membrane; step and to produce an alkali in the step and be separated from the brine compartments of the cathode electrolyte by a cation exchange membrane; less than 3Ωcm ^2, 2Ωcm ² or less than 1 .OMEGA.cm ² Also provided herein is a method comprising preventing migration of metal ions from the anode electrolyte to the brine compartment by using an anion exchange membrane having an ohmic resistance of less than. In some embodiments, the anion exchange membrane has an ohmic resistance between 1 and 3 Ωcm ² . In some embodiments, contacting the metal ions with the anode in the anode electrolyte of the anode chamber; converting the metal ions from a lower oxidation state to a higher oxidation state at the anode; and the cathode electrolyte and cathode in the cathode chamber Contacting the cathode; generating the alkali at the cathode; separating the anode electrolyte from the brine compartment with an anion exchange membrane; separating the cathode electrolyte from the brine compartment with a cation exchange membrane; from the anode electrolyte; Preventing migration of metal ions from the anode electrolyte to the brine compartment by using an anion exchange membrane that rejects more than 80%, more than 90% or more than 99% or about 99.9% of all metal ions of Including methods, including To.

An anode in contact with metal ions in the anode electrolyte of the anode chamber, the anode configured to convert the metal ions from a lower oxidation state to a higher oxidation state in the anode chamber; a cathode electrolyte in the cathode chamber; A cathode in contact with the cathode configured to generate alkali in the cathode chamber; an anion exchange membrane that separates the anode electrolyte from the brine compartment; and a cation that separates the cathode electrolyte from the brine compartment a system comprising an interchangeable membrane, the anion exchange membrane is less than 3Omucm ^2, also provides a system with an ohmic resistance of less than ² or 1Ωcm than ² 2Omucm. In some embodiments, the anion exchange membrane has an ohmic resistance between 1 and 3 Ωcm ² . In some embodiments, an anode in contact with metal ions in the anode electrolyte of the anode chamber, the anode configured to convert metal ions from a lower oxidation state to a higher oxidation state in the anode chamber A cathode in contact with the cathode electrolyte in the cathode chamber, the cathode configured to generate alkali in the cathode chamber; an anion exchange membrane separating the anode electrolyte from the brine compartment; and the cathode electrolyte A cation exchange membrane that separates from the brine compartment, wherein the anion exchange membrane comprises greater than 80%, greater than 90% or greater than 99% or about 99.9% of all metal ions from the anode electrolyte. Provide a system to reject.

  The above methods and systems involving AEM further include treating the anode electrolyte containing higher oxidation state metal ions with hydrogen gas, unsaturated hydrocarbon or saturated hydrocarbon as described herein.

  Examples of cation exchange membranes include, but are not limited to, cation membranes made of perfluorinated polymers containing anionic groups, such as sulfonic acid and / or carboxylic acid groups. However, in some embodiments, depending on the need to limit or tolerate the transfer of certain cationic or anionic species between electrolytes, for example, sodium ions from the anode electrolyte into the cathode electrolyte It is more restrictive so that a cation exchange membrane can be used that allows migration but limits the migration of other ions from the anode electrolyte into the cathode electrolyte, thus allowing the transfer of one species of cation. It will be appreciated that cation exchange membranes can be used to limit the migration of other species of cations. Similarly, in some embodiments, depending on the need to limit or allow the migration of certain anionic species between electrolytes, for example, the migration of chloride ions from the cathode electrolyte into the anode electrolyte is It is more restrictive so that an anion exchange membrane that allows but limits the migration of hydroxide ions from the cathode electrolyte into the anode electrolyte may be used, thus allowing the transfer of one species of anion. Anion exchange membranes that limit the migration of other types of anions can be used. Such limiting cation and / or anion exchange membranes are commercially available and can be selected by those skilled in the art.

  In some embodiments, a system is provided that includes one or more anion exchange membranes and cation exchange membranes located between an anode and a cathode. In some embodiments, these membranes should be selected so that they can function in acidic and / or basic electrolyte solutions as required. Other desirable characteristics of the membrane are high ion selectivity, low ionic resistance, high burst strength, and in acidic electrolytic solutions in the temperature range of 0 ° C. to 100 ° C. or higher or in alkaline solutions in similar temperature ranges that can be used. Including high stability. In some embodiments, it is desirable that the ion exchange membrane prevent the transport of metal ions from the anolyte to the catholyte. In some embodiments, 0C to 90C, 0C to 80C, 0C to 70C, 0C to 60C, 0C to 50C, 0C to 40C, 0C to 30C, 0 A stable membrane can be used in the range of -20 ° C to 20 ° C or 0 ° C to 10 ° C or higher. In some embodiments, it is stable in the range of 0 ° C to 90 ° C, 0 ° C to 80 ° C, 0 ° C to 70 ° C, 0 ° C to 60 ° C, 0 ° C to 50 ° C, or 0 ° C to 40 ° C, At higher temperatures, unstable membranes can be used. For other embodiments, an ion-specific that allows one type of cation transfer but does not allow another transfer; or allows one type of anion transfer but does not allow other transfers. It may be useful to utilize an ion exchange membrane to achieve one or more desired products in the electrolyte. In some embodiments, the membrane is 0C-90C, 0C-80C, 0C-70C, 0C-60C, 0C-50C, 0C-40C, 0C- Stable for the desired length of time in the system, for example, days, weeks or months or years, at 30 ° C, 0 ° C-20 ° C or 0 ° C-10 ° C and higher and / or lower temperature ranges And may be functional. In some embodiments, for example, the membrane has an electrolyte temperature of 100 ° C., 90 ° C., 80 ° C., 70 ° C., 60 ° C., 50 ° C., 40 ° C., 30 ° C., 20 ° C., 10 ° C., 5 ° C. and higher Alternatively, it may be stable and functional at lower electrolyte temperatures for at least 1 day, at least 5 days, 10 days, 15 days, 20 days, 100 days, 1000 days, 5-10 years or more.

  The ohmic resistance of the membrane can affect the voltage drop between the anode and the cathode. For example, as the membrane's ohmic resistance increases, the voltage between the anode and cathode can increase, and vice versa. Membranes that can be used include, but are not limited to, membranes with relatively low ohmic resistance and relatively high ion mobility; membranes with relatively high hydration properties that increase with temperature and thus reduce ohmic resistance. It is. By selecting a membrane with a lower ohmic resistance known in the art, the voltage drop between the anode and cathode at a particular temperature can be reduced.

  What is scattered through the membrane may be an ion channel containing acidic groups. These ion channels may extend from the inner surface to the outer surface of the matrix, and the acidic group can easily bind water by a reversible reaction as hydrated water. This binding of water as hydration water can follow first order kinetics, so that the reaction rate is proportional to temperature. Thus, the membrane can be selected to provide relatively low ohmic and ionic resistance, while at the same time providing improved strength and resistance for the operating temperature range in the system.

  In some embodiments, carbon from the carbon source reacts with hydroxide ions when contacted with the cathode electrolyte in the cathode chamber, producing water and carbonate ions depending on the pH of the cathode electrolyte. Adding carbon from a carbon source to the cathode electrolyte can lower the pH of the cathode electrolyte. Thus, depending on the degree of alkalinity desired for the cathode electrolyte, the pH of the cathode electrolyte can be adjusted, in some embodiments it is between 6-12; between 7-14 or greater; or Between 7 and 13; or between 7 and 12; or between 7 and 11; or between 7 and 10; or between 7 and 9; or between 7 and 8; or between 8 and 14 or greater Or between 8 and 13; or between 8 and 12; or between 8 and 11; or between 8 and 10; or between 8 and 9; or between 9 and 14 or higher values; Or between 9 and 13; or between 9 and 12; or between 9 and 11; or between 9 and 10; or between 10 and 14 or greater; or between 10 and 13; Between 12; or 10-1 Or between 11 and 14 or greater; or between 11 and 13; or between 11 and 12; or between 12 and 14 or greater; or between 12 and 13; or 13 Maintained between ˜14 or greater values. In some embodiments, the pH of the cathode electrolyte is any value between 7 and 14 or greater, pH less than 12, pH 7.0, 7.5, 8.0, 8.5, 9 0.0, 9.5, 10.0, 10.5, 11.0, 11.5, 12.0, 12.5, 13.0, 13.5, 14.0 and / or higher be able to.

  Similarly, in some embodiments of the system, the pH of the anode electrolyte is adjusted to be between 0-7, 0-6, 0-5, 0-4, 0-3, Maintain between 0-2 or between 0-1. Since the voltage between the anode and cathode can depend on several factors including the pH difference between the anode and cathode electrolytes (which can be determined by the Nernst equation well known in the art) In some embodiments, the pH of the anode electrolyte is adjusted to 0, 0.5, 1.0, 1.5, 2.0, 2.5, 3 depending on the desired operating voltage between the anode and cathode. 0.0, 3.5, 4.0, 4.5, 5.0, 5.5, 6.0, 6.5 and 7 can be adjusted to values between 0-7. Thus, in an equivalent system where it is desirable to reduce energy usage and / or reduce the voltage between the anode and cathode, such as in the case of a chlor-alkali process, carbon from a carbon source is described herein. In addition to the cathode electrolyte as disclosed in, a desired pH difference between the anode and cathode electrolytes can be achieved.

  The system can be from an anode electrolyte pH, cathode electrolyte pH, hydroxide concentration in the cathode electrolyte, anode electrolyte withdrawal and replenishment, cathode electrolyte withdrawal and replenishment, and / or a carbon source added to the cathode electrolyte. By adjusting the amount of carbon, it can be configured to create any desired pH difference between the anode and cathode electrolytes. By adjusting the pH difference between the anode and cathode electrolytes, the voltage between the anode and cathode can be adjusted. In some embodiments, the system comprises at least 4 pH units; at least 5 pH units; at least 6 pH units; at least 7 pH units; at least 8 pH units; at least 9 pH units; at least 10 pH units; at least 11 pH between the anode electrolyte and the cathode electrolyte. At least 12 pH units; at least 14 pH units; or between 4-12 pH units; or between 4-11 pH units; or between 4-10 pH units; or between 4-9 pH units; or 4-8 pH Between units; or between 4 and 7 pH units; or between 4 and 6 pH units; or between 4 and 5 pH units; or between 3 and 12 pH units; or between 3 and 11 pH units; or between 3 and 10 pH units Between; or between 3-9 pH units; or 3-8 Between H units; or between 3 and 7 pH units; or between 3 and 6 pH units; or between 3 and 5 pH units; or between 3 and 4 pH units; or between 5 and 12 pH units; or between 5 and 11 pH units Between; 5-10 pH units; or 5-9 pH units; or 5-8 pH units; or 5-7 pH units; or 5-6 pH units; or 6-12 pH units. Or between 6-11 pH units; or between 6-10 pH units; or between 6-9 pH units; or between 6-8 pH units; or between 6-7 pH units; or between 7-12 pH units; Between 7 and 11 pH units; or between 7 and 10 pH units; or between 7 and 9 pH units; or between 7 and 8 pH units; or between 8 and 12 pH units; or between 8 and 11 pH units; or Between -10 pH units; or between 8-9 pH units; or between 9-12 pH units; or between 9-11 pH units; or between 9-10 pH units; or between 10-12 pH units; It can be configured to produce a pH difference between units; or between 11-12 pH units. In some embodiments, the system is configured to generate a pH difference of at least 4 pH units between the anode electrolyte and the cathode electrolyte.

  In some embodiments, in the methods and systems provided herein, the anode and cathode electrolytes in the electrochemical cell are at room temperature, such as greater than 40 ° C, greater than 50 ° C, greater than 60 ° C, greater than 70 ° C, or 80 ° C. Operate at high temperature, such as above + 30 ° C or between 30-70 ° C.

Production of Bicarbonate and / or Carbonate Product In some embodiments, the methods and systems provided herein include a carbonate / bicarbonate solution obtained after the cathode electrolyte has contacted carbon from a carbon source. Configured to process. In some embodiments, a solution comprising carbonate and / or bicarbonate is treated with a divalent cation such as, but not limited to, calcium and / or magnesium to produce a carbonate and / or magnesium and / or magnesium. Bicarbonate is produced. An exemplary embodiment for such a process is shown in FIG.

As illustrated in FIG. 13, process 1300 illustrates a method and system for treating a carbonate / bicarbonate solution obtained after contacting a cathode electrolyte with carbon from a carbon source. In some embodiments, the solution is subjected to precipitation in a sedimentation separator 1301. In some embodiments, the solution comprises sodium hydroxide, sodium carbonate and / or sodium bicarbonate. In some embodiments, the system treats bicarbonate and / or carbonate ions in the cathode electrolyte with alkaline earth metal ions or divalent cations, including but not limited to calcium, magnesium, and combinations thereof. Configured to do. As used herein, “divalent cation” includes any solid or solution containing a divalent cation, such as an alkaline earth metal ion, or any aqueous medium containing an alkaline earth metal. Alkaline earth metals include calcium, magnesium, strontium, barium and the like or combinations thereof. Divalent cations (eg, alkaline earth metal cations such as Ca ²⁺ and Mg ²⁺ ) can be found in factory effluents, seawater, brine, hard water, minerals and many other suitable sources. Alkaline earth metal-containing water includes fresh water or salt water depending on the method of using water. In some embodiments, the water used in this process includes one or more alkaline earth metals, such as magnesium, calcium, and the like. In some embodiments, the alkaline earth metal ions are 1% to 99% by weight of the solution comprising alkaline earth metal ions; or 1% to 95% by weight; or 1% to 90% by weight; or 1% to 80%; or 1% to 70%; or 1% to 60%; or 1% to 50%; or 1% to 40%; or 1% to 30% Or 1 wt% to 20 wt%; or 1 wt% to 10 wt%; or 20 wt% to 95 wt%; or 20 wt% to 80 wt%; or 20 wt% to 50 wt%; or 50 50% to 80%; or 50% to 75%; or 75% to 90%; or 75% to 80%; or 80% to 90% % Present . In some embodiments, the alkaline earth metal ions are present in salt water such as sea water. In some embodiments, the source of divalent cations is hard water or naturally derived hard brine. In some embodiments, calcium rich water can be mixed with a magnesium silicate mineral such as olivine or serpentine.

  In some embodiments, gypsum (eg, by the Solvay method) provides a source of divalent cations such as, but not limited to, calcium ions. After the carbonate / bicarbonate solution from the cathode chamber and calcium from the gypsum are precipitated, the supernatant containing sodium sulfate is circulated to the electrochemical system described herein. be able to. This sodium sulfate solution is used in conjunction with a metal sulfate such as copper sulfate to oxidize such Cu (I) ions to Cu (II) ions in the anode chamber and to sulphonate hydrogen gas or hydrogen gas. It can be further used for sulfonation of unsaturated or saturated hydrocarbons. In such embodiments, the electrochemical system is fully integrated with the sedimentation process. Such use of gypsum as a source of calcium is described in US Provisional Application No. 61 / 514,879 filed Aug. 3, 2011, which is hereby incorporated by reference in its entirety. Have been described.

  Depending on the location, industrial effluent streams from various industrial processes provide a convenient source of cations (and in some cases other materials useful in the process, such as metal hydroxides). Such exhaust streams include, but are not limited to, mining waste; fossil fuel incineration ash (eg, fly ash, bottom ash, boiler slag); slag (eg, iron slag, phosphorus slag); cement kiln waste (eg, , Cement kiln dust); petroleum refining / petrochemical refining waste (eg oil fields and methane seam brine); coal seam waste (eg gas production brine and coal seam brine); paper processing waste; water softening waste brine (E.g., ion exchange waste); silicon processing waste; agricultural waste; metal finishing waste; high pH fiber industrial waste and caustic sludge. In some embodiments, the aqueous solution of the cation is 10 to 50,000 ppm; or 10 to 10,000 ppm; or 10 to 5,000 ppm; or 10 to 1,000 ppm; or 10 to 100 ppm; or 50 to 50 Or 50 to 10,000 ppm; or 50 to 100 ppm; or 100 to 50,000 ppm; or 100 to 10,000 ppm; or 100 to 1,000 ppm; or 100 to 500 ppm; or 1 5,000 to 50,000 ppm; or 1,000 to 10,000 ppm; or 5,000 to 50,000 ppm; or 5,000 to 10,000 ppm; or 10,000 to 50,000 ppm in amounts ranging from 10,000 to 50,000 ppm; Or ma Including the Neshiumu.

Fresh water is a convenient source of cations (eg, alkaline earth metal cations such as Ca ²⁺ and Mg ²⁺ ). Any suitable number of fresh water sources can be used, including fresh water sources ranging from sources that are relatively free of mineral matter to sources that are relatively rich in mineral matter. Mineral-rich fresh water sources may be naturally derived, including many hard water sources, either lakes or inland seas. Some mineral-rich freshwater sources such as alkaline lakes or inland seas (eg Lake Van in Turkey) also provide sources of pH modifiers. Mineral-rich freshwater sources can be artificial. For example, the method described herein in which mineral-soft (soft) water is contacted with a source of a cation such as an alkaline earth metal cation (eg, Ca ²⁺ , Mg ^2+, etc.) and Can produce water rich in minerals suitable for the system. Cations or their precursors (eg, salts, minerals) can be converted into fresh water (or other described herein using any convenient protocol (eg, addition of solids, suspensions or solutions)) Can be added to any type of water). In some embodiments, a divalent cation selected from Ca ²⁺ and Mg ²⁺ is added to fresh water. In some embodiments, fresh water containing Ca ²⁺ is mixed with magnesium silicate (eg, olivine or serpentine) or a product or processed form thereof to obtain a solution comprising calcium and magnesium cations. .

  Precipitates obtained after contacting carbon from a carbon source with the cathode electrolyte and divalent cation include, but are not limited to, calcium carbonate, magnesium carbonate, calcium bicarbonate, magnesium bicarbonate, calcium magnesium carbonate or Combinations of these are included. In some embodiments, the precipitate may be, but is not limited to, mixing, stirring, temperature, pH, sedimentation, sediment residence time, sediment dehydration, washing the precipitate with water, ionic ratio, additive The carbonate composition of the present invention can be made by subjecting to one or more of the steps including concentration, drying, milling, crushing, storage, aging and curing. In some embodiments, the precipitation conditions are such that the carbonate product is in a metastable form such as, but not limited to, vaterite, aragonite, amorphous calcium carbonate, or combinations thereof.

  The sedimentation separator 1301 can be a tank or a series of tanks. Contact protocols include, but are not limited to, direct contact protocols, such as flowing a volume of water containing cations, such as alkaline earth metal ions, through a volume of sodium hydroxide-containing cathode electrolyte; Contact between directional flowing liquid phase streams; and countercurrent means such as contact between opposing flowing liquid phase streams. Thus, contact can be achieved through the use of injectors, bubblers, fluid venturi reactors, spargers, gas filters, sprays, trays or packed column reactors, etc., where convenient. In some embodiments, contact is by spray. In some embodiments, the contact is by passing through a packed tower. In some embodiments, carbon from a carbon source is added to a cathode source containing a source of cations and a hydroxide. In some embodiments, a cathode source containing a cation source and an alkali is added to the carbon from the carbon source. In some embodiments, both the cation source and the carbon from the carbon source are added simultaneously to the alkali-containing cathode electrolyte in a settling separator for settling.

  In some embodiments, when carbon from a carbon source is added to the cathode electrolyte in the cathode chamber, the extracted cathode electrolyte comprising hydroxide, bicarbonate and / or carbonate is further combined with a divalent cation and Feed to settling separator for reaction. In some embodiments, when carbon and divalent cations from a carbon source are added to the cathode electrolyte in the cathode chamber, sodium hydroxide, calcium carbonate, magnesium carbonate, calcium bicarbonate, magnesium bicarbonate, carbonate The extracted cathode electrolyte containing calcium magnesium or a combination thereof is fed to a sedimentation separator for further processing.

  A sedimentation separator 1301 containing a solution of calcium carbonate, magnesium carbonate, calcium bicarbonate, magnesium bicarbonate, calcium magnesium carbonate or a combination thereof is subjected to sedimentation conditions. In the precipitation step, the carbonate compound, which may be amorphous or crystalline, precipitates. These carbonate compounds can form reaction products comprising carbonic acid, bicarbonate, carbonate or mixtures thereof. The carbonate precipitate can be a self-cementing composition and can be stored as such in the mother liquor or can be further processed to make a cement product. Alternatively, the precipitate can be subjected to further processing to obtain a hydraulic cement or supplementary cementitious material (SCM) composition. Self-cementing compositions, hydraulic cements and SCM are described in US patent application Ser. No. 12 / 857,248 filed Aug. 16, 2010 (in this disclosure, which is hereby incorporated by reference in its entirety. Incorporated).

  The one or more conditions of interest or the one or more settling conditions include conditions that alter the physical environment of the water to produce the desired precipitated product. Such one or more conditions or settling conditions include, but are not limited to, one or more of temperature, pH, precipitation, dehydration or separation of the precipitate, drying, milling and storage. For example, the temperature of the water may be in a range suitable for sedimentation of the desired composition to occur. For example, the temperature of the water can be raised to an appropriate temperature for precipitation of the desired carbonate compound. In such embodiments, the temperature of the water may be 5 to 70 ° C, such as 20 to 50 ° C, including 25 to 45 ° C. Thus, a given set of sedimentation conditions may be at a temperature in the range of 0-100 ° C., but in certain embodiments, the temperature can be increased to produce the desired precipitate. In certain embodiments, the temperature is increased using energy generated by a low or zero carbon dioxide emission source, such as a solar energy source, wind energy source, hydropower energy source, and the like.

  The residence time of the precipitate in the settling separator until the precipitate is removed from the solution can vary. In some embodiments, the residence time of the precipitate in the solution is greater than 5 seconds, between 5 seconds and 1 hour, between 5 seconds and 1 minute, between 5 seconds and 20 seconds, and between 5 seconds and 30 seconds. Or between 5 seconds and 40 seconds. Without being limited by theory, it is believed that the residence time of the precipitate may affect the particle size. For example, shorter residence times can result in smaller or more dispersed particles, while longer residence times can result in agglomerated or larger size particles. In some embodiments, the residence time in the process of the present invention may be separated or mixed for subsequent steps in the process, single or multiple batches of small size particles and large sizes. Particles can also be used.

  The nature of the precipitate can also be influenced by the selection of an appropriate main ion ratio. The major ion ratio can affect polymorph formation, so the carbonate product is in a metastable form such as, but not limited to, vaterite, aragonite, amorphous calcium carbonate, or combinations thereof It is. In some embodiments, the carbonate product can also include calcite. Such polymorphic precipitates are described in US patent application Ser. No. 12 / 857,248 filed Aug. 16, 2010, which is hereby incorporated by reference in its entirety. Has been. For example, magnesium can stabilize vaterite and / or amorphous calcium carbonate in the precipitate. The settling rate can also affect the polymorphic phase formation of the compound and can be controlled in a manner sufficient to produce the desired precipitated product. The fastest settling can be achieved by seeding the solution with the desired polymorphic form. In the absence of seed crystals, rapid sedimentation can be achieved by rapidly increasing the pH of the seawater. The higher the pH, the faster the settling.

  In some embodiments, the set of conditions for producing the desired precipitate from water includes, but is not limited to, the temperature and pH of the water, and optionally the concentration of additives and ionic species in the water. Sedimentation conditions can also include factors such as mixing speed, agitation form such as ultrasound, seed crystals, catalyst, membrane or substrate presence. In some embodiments, sedimentation conditions include supersaturation conditions, temperature, pH and / or concentration gradients, or circulation or modification of any of these parameters. The protocol used to prepare the carbonate compound precipitate according to the present invention may be a batch protocol or a continuous protocol. It will be appreciated that the settling conditions may be different compared to a batch system to produce a given precipitate in a continuous flow system.

  Following the formation of carbonate precipitate from water, the resulting precipitated carbonate composition can be separated from the mother liquor or dehydrated to obtain a precipitated product, as illustrated in step 1302 of FIG. Alternatively, the precipitate is left in the mother liquor or mother supernate and used as a cementing composition. Separation of sediment, for example, when bulk excess water flows out of sediment, either by gravity alone or by vacuum, mechanical pressing, or filtering the sediment from the mother liquor to obtain a filtrate, etc. Can be achieved using any convenient approach, including a mechanical approach. Separation of bulk water produces a wet dehydrated precipitate. The dewatering station may be any number of dewatering stations coupled together (eg, in parallel or in series or a combination thereof) to dewater the slurry.

  The above protocol results in the formation of a precipitate and mother liquor slurry. This precipitate in the mother liquor and / or slurry can provide a self-cementing composition. In some embodiments, some or all of the dehydrated precipitate or slurry is further processed to make a hydraulic cement or SCM composition.

  If desired, the composition composed of the precipitate and mother liquor can be stored for a period of time following settling and prior to further processing. For example, the composition may be stored at a temperature range of 1-40 ° C., such as 20-25 ° C. for a period of 1 day to 1000 days or longer, such as a range of 1 day to 10 days or longer. it can.

  The slurry component is then separated. Embodiments can include treatment of the mother liquor, where the mother liquor may or may not be present in the same composition as the product. The resulting reaction mother liquor can be disposed of using any convenient protocol. In certain embodiments, this can be sent to a tailings pond 1307 for disposal. In certain embodiments, it can be disposed of in naturally occurring waters such as oceans, seas, lakes or rivers. In certain embodiments, the mother liquor is returned to the source of feed water for the method of the invention, such as the ocean or sea. Alternatively, the mother liquor can be further processed. For example, as further described in US patent application Ser. No. 12 / 163,205, filed Jun. 27, 2008, which is hereby incorporated by reference in its entirety. It can be subjected to a desalting protocol.

  The resulting dehydrated precipitate is then dried to produce the carbonate composition of the present invention, as illustrated in step 1304 of FIG. Drying can be achieved by air drying the precipitate. When the precipitate is air dried, the air drying may be at a temperature in the range of -70 to 120 ° C as desired. In certain embodiments, drying is accomplished by freezing and drying (ie, lyophilization), where the precipitate is frozen, the ambient pressure is reduced, and fully heated to freeze in the material Water is sublimated directly from the frozen precipitate phase to the gas. In still other embodiments, the precipitate is spray dried to dry the precipitate, wherein the liquid containing the precipitate is supplied and dried by a hot gas (such as a gaseous exhaust stream from a power plant). For example, the feed liquid is pumped through the atomizer and into the main drying chamber, allowing the hot gas to pass in the direction of the atomizer as cocurrent or countercurrent. Depending on the specific drying protocol of the system, the drying station can include filtration elements, freeze-drying structures, spray-drying structures, and the like. In the drying step, air and fine powder can be released (1306).

  In some embodiments, the spray drying step can include separation of different sized precipitate particles. If desired, the dehydrated precipitation product from 1302 can be washed prior to drying, as illustrated in step 1303 of FIG. The precipitate can be washed with fresh water to remove, for example, salts (such as NaCl) from the dehydrated precipitate. The used washing water can be disposed of appropriately, for example, by discarding it in a reservoir. The water used for cleaning may contain metals such as iron and nickel.

  In some embodiments, the dried precipitate is refined, milled, aged, and / or cured (as shown in purification step 1305) to achieve desired physical properties such as particle size, surface area, zeta potential, etc. Or one or more ingredients are added to a precipitate, such as a mixture, agglomerate, auxiliary cementitious material, to form a carbonate composition. The purification process can include a variety of different protocols. In certain embodiments, the product is subjected to mechanical purification, such as grinding, to obtain a product having the desired physical properties, such as particle size. The dried precipitate can be milled or ground to obtain the desired particle size.

  In some embodiments, the calcium carbonate precipitate produced by the methods and systems of the present invention is in a metastable form including, but not limited to, vaterite, aragonite, amorphous calcium carbonate, or combinations thereof. is there. In some embodiments, the calcium carbonate precipitate produced by the methods and systems of the present invention is in a metastable form including, but not limited to, vaterite, amorphous calcium carbonate, or combinations thereof. . Vaterite containing a composition of calcium carbonate is converted into a stable polymorphic form such as aragonite, calcite or combinations thereof having high compressive strength after contact with water.

  The resulting carbonate or cementitious composition has carbon derived elements or markers from the carbon source used in the process. The carbonate composition after setting and curing is at least 14 MPa; or at least 16 MPa; or at least 18 MPa; or at least 20 MPa; or at least 25 MPa; or at least 30 MPa; or at least 35 MPa; or at least 40 MPa; or at least 45 MPa; Or at least 55 MPa; or at least 65 MPa; or at least 75 MPa; or at least 80 MPa; or at least 85 MPa; or at least 90 MPa; or at least 95 MPa; or at least 100 MPa; or 14-100 MPa; ;Also 14-75 MPa; or 14-65 MPa; or 14-60 MPa; or 14-55 MPa; or 14-50 MPa; or 14-45 MPa; or 14-40 MPa; or 14-35 MPa; or 14-30 MPa; or 14-25 MPa; or 14-20 MPa; or 14-16 MPa; or 17-35 MPa; or 17-30 MPa; or 17-25 MPa; or 17-20 MPa; or 17-18 MPa; or 20-100 MPa; 20-90 MPa; or 20-80 MPa; or 20-75 MPa; or 20-70 MPa; or 20-65 MPa; or 20-60 MPa; or 20-55 MPa; or 20-50 MP Or 20 to 45 MPa; or 20 to 35 MPa; or 20 to 30 MPa; or 20 to 25 MPa; or 30 to 100 MPa; or 30 to 90 MPa; or 30 to 80 MPa; or 30 to 75 MPa; or 30 to 70 MPa; Or 30 to 65 MPa; or 30 to 55 MPa; or 30 to 50 MPa; or 30 to 45 MPa; or 30 to 40 MPa; or 30 to 35 MPa; or 40 to 100 MPa; or 40 to 90 MPa; or 40 to 80 MPa; Or 40 to 75 MPa; or 40 to 65 MPa; or 40 to 60 MPa; or 40 to 55 MPa; or 40 to 50 MPa; or 40 to 45 MPa; or 50 to 100 MPa; or 50-90 MPa; or 50-80 MPa; or 50-75 MPa; or 50-70 MPa; or 50-65 MPa; or 50-60 MPa; or 50-55 MPa; or 60-100 MPa; or 60-90 MPa; 80 MPa; or 60-75 MPa; or 60-70 MPa; or 60-65 MPa; or 70-100 MPa; or 70-90 MPa; or 70-80 MPa; or 70-75 MPa; or 80-100 MPa; or 80-90 MPa; 85 MPa; or 90-100 MPa; or 90-95 MPa; or 14 MPa, 16 MPa, 18 MPa, 20 MPa, 25 MPa, 30 MPa, 35 MPa, 40 MPa or 45 MP It has a compressive strength. For example, in some embodiments of the above aspects and embodiments, the composition after setting and curing has a compressive strength of 14 MPa to 40 MPa, 17 MPa to 40 MPa, 20 MPa to 40 MPa, 30 MPa to 40 MPa, or 35 MPa to 40 MPa. In some embodiments, the compressive strength described herein is compressive strength after 1, 3, 7, or 28 days.

  In some embodiments, a precipitate comprising, for example, calcium and magnesium carbonates and bicarbonates is a building material, such as US patent application Ser. No. 12 / 126,776 filed May 23, 2008 by the same applicant. In the present disclosure, it can be used as a cement and aggregate as described in (incorporated herein by reference in its entirety).

  The following examples are presented in order to provide those skilled in the art with a complete disclosure and description of how to make and use the present invention, which are within the scope of what the inventors regard as their invention. It is not intended to be limiting, nor is it intended to represent that the following experiment is all or the only experiment performed. In addition to those described herein, various modifications of the present invention will become apparent to those skilled in the art from the foregoing description and accompanying drawings. Such modifications are encompassed by the appended claims. Efforts have been made to ensure accuracy with respect to numbers used (eg amounts, temperature, etc.) but it should be admitted that there are some experimental errors and deviations. Unless indicated otherwise, parts are parts by weight, molecular weight is weight average molecular weight, temperature is in degrees Centigrade, and pressure is at or near atmospheric.

In the examples and others, the abbreviations have the following meanings.

Example 1
Formation of halohydrocarbons from unsaturated hydrocarbons Formation of EDC from ethylene using copper chloride This experiment is directed to the production of ethylene dichloride (EDC) from ethylene using cupric chloride. The experiment was performed in a pressure vessel. The pressure vessel was equipped with an outer jacket containing a catalyst, a cupric chloride solution, and an inlet for bubbling ethylene gas into the cupric chloride solution. The concentration of the reaction product was as shown in Table 1 below. The pressure vessel was heated to 160 ° C. and during the experiment ethylene gas was passed through the vessel containing 200 mL of solution at 300 psi for 30 minutes to 1 hour. The vessel was cooled to 4 ° C and then drained and opened. The product formed in solution was extracted with ethyl acetate and then separated with a separatory funnel. The ethyl acetate extract containing EDC was subjected to gas chromatography (GC).

Production of dichloropropane from propylene using copper chloride This experiment is directed to the production of 1,2-dichloropropane (DCP) from propylene using cupric chloride. The experiment was performed in a pressure vessel. The pressure vessel was equipped with an outer jacket containing the catalyst, ie cupric chloride solution, and an inlet for bubbling propylene gas into the cupric chloride solution. A 150 mL solution of 5M CuCl ₂ , 0.5M CuCl, 1M NaCl and 0.03M HCl was placed in a 450 mL stirred glass lining pressure vessel. The closed vessel was purged with N ₂ and then heated to 160 ° C. After reaching this temperature, propylene was added to the vessel and the pressure was increased, mostly from autogenous due to water vapor, to a pressure of 130 psig. After 15 minutes, additional propylene was added to increase the pressure from 120 psig to 140 psig. After an additional 15 minutes, the pressure was 135 psig. At this point, the reactor was cooled to 14 ° C. and opened under reduced pressure. Ethyl acetate was used to rinse the reactor parts and then used as the extraction solvent. The product was analyzed by gas chromatography. This showed 0.203 g of 1,2-dichloropropane recovered in the ethyl acetate phase.

(Example 2)
Recirculation of the aqueous phase from the catalytic reactor to the electrochemical system This example illustrates the recycling of the Cu (I) solution produced in the catalytic reactor to the electrochemical cell containing the PtIr wire mesh electrode. A solution containing 4.5M Cu (II), 0.1M Cu (I) and 1.0M NaCl was charged to a Parr bomb type reactor over 60 minutes and reacted at 160 ° C. and 330 psi. To see the effect of organic residues such as EDC or residual extractant on anode performance, the same solution was tested by anodic cyclic voltammetry (CV) before and after the catalysis run. Each CV experiment was performed at 70 ° C., 10 mVs ⁻¹ scan rate for 5 cycles, 0.3-0.8 V against a saturated calomel electrode (SCE).

FIG. 14 illustrates the resulting V / I response of a PtIr wire mesh electrode (6 cm ² ) in solution before and after catalysis (labeled pre and post, respectively). As illustrated in FIG. 14, the redox potential (voltage at zero current) shifted to a lower voltage after catalysis, as predicted from the Nernst equation for increasing Cu (I) concentration. The increase in Cu (I) concentration was due to EDC formation associated with Cu (I) regeneration during the catalytic reaction. The pre-catalytic CV curve reached a limiting current in the vicinity of 0.5 A due to the mass transfer limit at low Cu (I) concentrations. Cu (I) production during the catalysis run is shown by a marked improvement in the kinetic behavior after catalysis, and FIG. 14 shows a steep and linear I not reaching the limit current. Illustrated as / V gradient. It was clear that there was no adverse effect of residual EDC or other organics, as shown by a typical reversible I / V curve obtained with CV after catalysis.
(Example 3)
Air bubbling in the anode compartment

  This example illustrates the cell voltage drop when air is bubbled around the anode. As described herein, air circulation in the anode compartment improves mass transfer at the anode, thereby reducing cell voltage.

The solutions introduced in the full cell were 0.9 M Cu (I), 4.5 M Cu (II) and 2.5 M NaCl anolyte and 10 wt% NaOH catholyte. The anion exchange membrane was FAS-PK-130. The flow rate in the anolyte was 1.7 l / min, and the distance between the anode and the rear wall was 3 mm. A fishing net was used on one side of the anode to separate the anode from the anion exchange membrane. As illustrated in FIG. 15, the voltage dropped by 100-200 mV each time the bubble passed through the anode compartment.
Example 4
Effect of anode geometry on cell voltage

  This example illustrates the cell voltage drop when a corrugated anode is used in a cell versus a flat stretched anode.

The solutions introduced in the full cell were 0.9 M Cu (I), 4.5 M Cu (II) and 2.5 M NaCl anolyte and 10 wt% NaOH catholyte. The anion exchange membrane was a FAS-130 separator and the temperature was 70 ^° C. As shown in FIG. 16A, the flat stretched anode showed cell voltages of 3.30V and 3.32V, whereas the corrugated anode showed 3.05V and 2.30V as shown in FIG. A cell voltage of 95V was shown. There was a voltage saving between 250 mV and 370 mV.
(Example 5)
Adsorption of organic matter on adsorbent

In this experiment, adsorption of organic substances from an aqueous metal solution was tested using different adsorbents. The adsorbents tested were activated carbon (Aldrich, 20-60 mesh), pelleted PMMA ((average Mw of about 120,000 by poly (methyl methacrylate) GPC, Aldrich) and pelleted PBMA ((poly (isobutyl methacrylate) Average Mw about 130,000, Aldrich) (PMMA and PBMA are both shown in Figure 17 as PXMA) as well as cross-linked PS (Dowex Optipore® L-493, Aldrich) PS (Dowex Optipore) (Registered trademark) L-493, Aldrich) were 20-50 mesh beads having a surface area of 1100 m ² / g, an average pore diameter of 4.6 nm and an average breaking strength of 500 g / bead.

Electrostatic adsorption experiments were performed in 20 mL screw cap vials. Stock aqueous solution containing 4M CuCl ₂ (H ₂ O) ₂ , 1M CuCl and 2M NaCl was doped with a small amount of ethylene dichloride (EDC), chloroethanol (CE), dichloroacetaldehyde (DCA) and trichloroacetaldehyde (TCA). . The organic content of the solution was analyzed by extracting the aqueous solution with 1 mL of EtOAc and analyzing the organic concentration of the EtOAc extraction solvent. As shown in the graph illustrated in FIG. 17, 6 mL of the stock solution was stirred at 90 ^° C. with different amounts of adsorbent material for a specified time. After filtration, the organic content of the treated aqueous solution was analyzed by extraction and GCMS analysis of the organic phase. It has been observed that increasing the amount of adsorbent material achieves an increased decrease in organic content. The most significant decrease was observed with cross-linked PS.

  In this experiment, repeatedly, adsorb organics from a Cu-containing solution on a given adsorbent material (Dowex Optipore® 495-L), wash the material with cold and hot water, dry the material, The washed material was then used again for adsorption to test the regeneration capacity of the adsorbent. The result of the experiment is illustrated in FIG. It was observed that the adsorption performance was very close to that of the unused material even after the second regeneration. It was also observed that ultraviolet (UV) measurement of Cu concentration after organics adsorption on Dowex material showed no significant change. In the unused material, an approximately 10% decrease in the overall Cu concentration was observed, and in the recycled material, only a 1-2% decrease in the Cu concentration was observed. These findings point to the advantage of repeated use of the polymer adsorbing material that the polymer adsorbing material adsorbs organics from the copper ion-containing solution without retaining the majority of Cu ions even after multiple use cycles. . Thus, the adsorbent material can be regenerated after its adsorption capacity is exhausted, and after regeneration, the adsorbent material can be reused for adsorption.

The Dowex Optipore® 495-L material was then evaluated on a dynamic adsorption column (illustrated in FIG. 19) to establish a breakthrough time under flow conditions. A stock solution containing 511 g CuCl ₂ (H ₂ O) ₂ , 49 g CuCl, 117 g NaCl and 500 g water was added to EDC (1.8 mg / mL), CE (0.387 mg / mL), TCA (0.654 mg / mL). ) And DCA (0.241 mg / mL). The initial organic concentration was analyzed by extraction and GCMS analysis. The 91-94 ^° C heat stock solution was pumped through a column (1.25 cm diameter, 15.2 cm length) packed with 13.5 g Dowex Optipore® V495L. The temperature measured at the outlet was 78-81 ^° C. The flow rate was 18 mL / min. After 60 minutes, the feed was switched from the stock solution to hot DI water and a regeneration cycle was started. Samples were taken at intervals shown in the graph illustrated in FIG. Samples were analyzed for their organic content by extraction and GCMS analysis of the organic phase. The CE immediately followed by DCA had the earliest breakthrough time, followed by TCA. The slowest breakthrough time was observed with EDC.

The regeneration profile of organic matter followed the same order as adsorption. First, the adsorbed CE was washed out with hot water, and DCA was washed out immediately thereafter. The next organic compound washed out from the adsorbent was TCA and finally EDC. It has been observed that the adsorption and desorption profiles and times can be affected by flow rate, temperature, column dimensions and other parameters. These parameters can be used to optimize techniques for removal of organics from the exit stream before entering the electrochemical cell.

Claims (1)

Invention described in the specification.