WO1996034998A1 - Conversion electrochimique d'halogenure d'hydrogene anhydre en gaz halogene au moyen d'une membrane a transport cationique - Google Patents

Conversion electrochimique d'halogenure d'hydrogene anhydre en gaz halogene au moyen d'une membrane a transport cationique Download PDF

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Publication number
WO1996034998A1
WO1996034998A1 PCT/US1995/016032 US9516032W WO9634998A1 WO 1996034998 A1 WO1996034998 A1 WO 1996034998A1 US 9516032 W US9516032 W US 9516032W WO 9634998 A1 WO9634998 A1 WO 9634998A1
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Prior art keywords
membrane
water
hydrogen halide
cathode
hydrogen
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PCT/US1995/016032
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English (en)
Inventor
Francisco Jose Freire
William H. Zimmerman
Pallav Tatapudi
James Arthur Trainham, Iii
Clarence Garlan Law, Jr.
John Scott Newman
Douglas John Eames
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E.I. Du Pont De Nemours And Company
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Application filed by E.I. Du Pont De Nemours And Company filed Critical E.I. Du Pont De Nemours And Company
Priority to EP95944322A priority Critical patent/EP0828865B1/fr
Priority to DE69523077T priority patent/DE69523077T2/de
Priority to JP53327296A priority patent/JP3827019B2/ja
Priority to AU46398/96A priority patent/AU4639896A/en
Priority to MX9708397A priority patent/MX9708397A/es
Publication of WO1996034998A1 publication Critical patent/WO1996034998A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/24—Halogens or compounds thereof
    • C25B1/26—Chlorine; Compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/24—Halogens or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded

Definitions

  • the present invention relates to an electro ⁇ chemical cell, system and process for converting essentially anhydrous hydrogen halide to essentially dry halogen gas.
  • the process of the present invention is useful for converting anhydrous hydrogen halide, in particular, hydrogen chloride, hydrogen fluoride, hydrogen bromide and hydrogen iodide, to a halogen gas, such as chlorine, fluorine, bromine, or iodine.
  • Hydrogen chloride (HC1) or hydrochloric acid is a reaction by-product of many manufacturing processes which use chlorine.
  • chlorine is used to manufacture polyvinyl chloride, isocyanates, and chlorinated hydrocarbons/fluorinated hydrocarbons, with hydrogen chloride as a by-product of these processes.
  • supply so exceeds demand hydrogen chloride or the acid produced often cannot be sold or used, even after careful purification. Shipment over long distances is not economically feasible. Discharge of the acid or chloride ions into waste water streams is environmentally unsound. Recovery and feedback of the chlorine to the manufacturing process is the most desirable route for handling the HCl by-product.
  • the current electrochemical commercial process is known as the Uhde process.
  • aqueous HCl solution of approximately 22% is fed at 65° to 80° C to both compartments of an electrochemical cell, where exposure to a direct current in the cell results in an electrochemical reaction and a decrease in HCl concentration to 17% with the production of chlorine gas and hydrogen gas.
  • a polymeric separator divides the two compartments.
  • the process requires recycling of dilute (17%) HCl solution produced during the electrolysis step and regenerating an HCl solution of 22% for feed to the electrochemical cell.
  • the overall reaction of the Uhde process is expressed by the equation:
  • the chlorine gas produced by the Uhde process is wet, usually containing about 1% to 2% water. This wet chlorine gas must then be further processed to produce a dry, usable gas. If the concentration of HCl in the water becomes too low, it is possible for oxygen to be generated from the water present in the Uhde process. This possible side reaction of the Uhde process due to the presence of water, is expressed by the equation:
  • the presence of water in the Uhde system limits the current densities at which the cells can perform to less than 500 amps./ft. 2 , because of this side reaction.
  • the side reaction results in reduced electrical efficiency and corrosion of the cell components.
  • Balko employs an electrolytic cell having a solid polymer electrolyte membrane.
  • Hydrogen chloride in the form of hydrogen ions and chloride ions in aqueous solution, is introduced into an electrolytic cell.
  • the solid polymer electrolyte membrane is bonded to the anode to permit transport from the anode surface into the membrane.
  • controlling and minimizing the oxygen evolution side reaction is an important consideration. Evolution of oxygen decreases cell efficiency and leads to rapid corrosion of components of the cell.
  • the design and configuration of the anode pore size and electrode thickness employed by Balko maximizes transport of the chloride ions. This results in effective chlorine evolution while minimizing the evolution of oxygen, since oxygen evolution tends to increase under conditions of chloride ion depletion near the anode surface. In Balko, although oxygen evolution may be minimized, it is not eliminated.
  • Balko As can be seen from Figs. 3 to 5 of Balko, as the overall current density is increased, the rate of oxygen evolution increases, as evidenced by the increase in the concentration of oxygen found in the chlorine produced. Balko can run at higher current densities, but is limited by the deleterious effects of oxygen evolution. If the Balko cell were to be run at high current densities, the anode would be destroyed.
  • the conductivity of a membrane is directly related to the water content in the membrane and decreases at low water content. Limiting current density occurs when the concentration of water within the membrane reaches a value that will no longer support additional proton conduction. Therefore, limiting current density can develop when the conductivity decreases due to low water concentrations.
  • the existing electrochemical processes for converting hydrogen halides as discussed above are aqueous processes which require first dissolving the hydrogen halide in water. Since these electrochemical cells have water in their anolytes and catholytes, the membranes of such cells are normally kept hydrated. There exists a need for directly producing essentially dry halogen gas without having to first dissolve the hydrogen halide in water, and for keeping the membrane hydrated during such a process. This would allow the limiting current density of the cell to be increased and/or controlled, so that the cell components would not be destroyed.
  • the present invention solves the problems of the prior art by providing an electrochemical cell, system and process for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide.
  • This cell, system and process allow for direct processing of anhydrous hydrogen halide which is a by-product of manufacturing processes, without first dissolving the hydrogen halide in water.
  • This direct production of essentially dry halogen gas when done, for example, for chlorine gas, is less capital intensive than processes of the prior art, which require separation of water from the chlorine gas.
  • This direct production of essentially dry halogen gas also requires lower investment costs than the electrochemical conversions of hydrogen chloride of the prior art.
  • the membrane is kept hydrated.
  • This enables the limiting current density of the cell to be increased, as well as controlled.
  • this allows an electrochemical cell to be designed in which a valuable component, such as the cation-exchange membrane, is protected from prolonged exposure to excessive current, which could deteriorate the membrane, and thus impact the membrane's and the cell's long-term performance.
  • control of limiting current is especially desirable where it is necessary to compensate for changes in manufacturing rates of suppliers of the anhydrous hydrogen halide, such as hydrogen chloride.
  • the membrane of an electrochemical cell used to convert essentially anhydrous hydrogen halide to essentially dry halogen gas is kept hydrated in a variety of ways.
  • the membrane is kept hydrated by a supply of oxygen, which provides an excess of oxygen to the cell. This increases the conversion rate of protons transported across the membrane and the supplied oxygen to water, which allows the limiting current density to be increased. In addition, with this supply of oxygen, it is possible to take advantage of this excess of oxygen without the economic penalty of discarding products from the cell associated with other ways of hydrating the membrane.
  • an electrochemical cell for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide.
  • the electrochemical cell comprises means for oxidizing molecules of essentially anhydrous hydrogen halide to produce essentially dry halogen gas and protons, cation-transporting means for transporting the protons therethrough, where the oxidizing means is disposed in contact with one side of the cation-transporting means, means for reducing the transported protons, wherein the reducing means is disposed in contact with the other side of the cation- transporting means, and means for supplying water to the cation-transporting means at the other side of the cation-transporting means.
  • the electrochemical cell comprises means for oxidizing molecules of essentially anhydrous hydrogen halide to produce essentially dry halogen gas and protons; cation-transporting means for transporting the protons therethrough, where the oxidizing means is disposed in contact with one side of the cation-transporting means; means for reducing the transported protons, wherein the reducing means is disposed in contact with the other side of the cation- transporting means, and inlet means for supplying water to the cation-transporting means at the other side of the reducing means; inlet means for supplying water to the cation-transporting means at the other side of the cation-transporting means; outlet means for releasing a fluid from reducing means at the other side of the cation-transporting means; and means for recycling the fluid back to the cation-transporting means at the other side of the cation-
  • a process for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide wherein molecules of essentially anhydrous hydrogen halide are fed to an inlet of the electrochemical cell and are transported to an anode of the cell; the molecules of the essentially anhydrous hydrogen halide are oxidized at the anode to produce essentially dry halogen gas and protons; the protons are transported through a cation- transporting membrane of the cell; the transported protons are reduced at a cathode, of the electrochemical cell; and a humidified gas stream is supplied to the membrane.
  • the process of the present invention may be described as a process for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide, wherein current is supplied to an electrochemical cell; molecules of essentially anhydrous hydrogen halide are fed to an inlet of the electrochemical cell and are transported to an anode of the cell; the molecules of the essentially anhydrous hydrogen halide are oxidized at the anode to produce essentially dry halogen gas and protons; the protons are transported through a cation-transporting membrane of the cell; the transported protons are reduced at a cathode of the electrochemical cell; water is supplied to the membrane at the cathode and the and water is transported by diffusion towards the anode; the transported protons drag the water present in the membrane towards the cathode; and the amount of current required to achieve a balance between the water transported by diffusion toward the anode and dragged by the proton transport toward the cathode is controlled by adjusting the amount of water supplied to the membrane at the cathode
  • Fig. 1 is a cross-sectional view of an electro- chemical cell for producing halogen gas from anhydrous hydrogen halide according to any of the first, second, third or fourth embodiments of the present invention.
  • Fig. 1A is a cut-away, top cross-sectional view of the anode and cathode mass flow fields as shown in Fig. 1.
  • Fig. 2 is a schematic diagram of a system for producing essentially dry halogen gas from anhydrous hydrogen halide using the electrochemical cell of Fig. 1 and for recycling a fluid released from the cell back to the membrane, where liquid water is added to the cathode-side inlet of the cell.
  • Fig. 3 is a schematic diagram of a system for producing essentially dry halogen gas from anhydrous hydrogen halide using the electrochemical cell of Fig. 1 and for recycling a fluid released from the cell back to the membrane, where a humidified gas stream comprising hydrogen is added to the cathode- side inlet of the cell.
  • Fig. 4 is a schematic diagram of a system for producing essentially dry halogen gas from anhydrous hydrogen halide using the electrochemical cell of Fig. 1 and for recycling a fluid released from the cell back to the membrane, where a humidified gas stream comprising oxygen is added to the cathode-side inlet of the cell.
  • Fig. 5 is a schematic diagram of a system for producing essentially dry halogen gas from anhydrous hydrogen halide using the electrochemical cell of Fig. 1 and for recycling a fluid released from the cell back to the membrane, where a humidified gas stream comprising oxygen is added to the cathode-side inlet of the cell.
  • an electrochemical cell for the direct production of essentially dry halogen gas from anhydrous hydrogen halide.
  • a cell is shown generally at 10 in Fig. 1.
  • the cell of the present invention will be described with respect to a preferred embodiment of the present invention, which directly produces essentially dry chlorine gas from anhydrous hydrogen chloride.
  • This cell may alternatively be used to produce other halogen gases, such as bromine, fluorine and iodine from a respective anhydrous hydrogen halide, such as hydrogen bromide, hydrogen fluoride and hydrogen iodide.
  • the term "direct” means that the electrochemical cell obviates the need to remove water from the halogen gas produced or the need to convert essentially anhydrous hydrogen halide to aqueous hydrogen halide before electro ⁇ chemical treatment.
  • chlorine gas, as well as hydrogen is produced in this cell.
  • water, as well as chlorine gas is produced by this cell, as will be explained more fully below.
  • the electrochemical cell of the first through fourth embodiments comprises means for oxidizing molecules of essentially anhydrous hydrogen halide to produce essentially dry halogen gas and protons.
  • the oxidizing means is an electrode, or more specifically, an anode 12 as shown in Fig. 1..
  • electrochemical cell 10 On the anode side, electrochemical cell 10 has an anode-side inlet 14 and an anode-side outlet 16. Since in the preferred embodiment, anhydrous HCl is carried through the inlet, and chlorine gas is carried through the outlet, the inlet and the outlet may be lined with a perfluoropolymer, sold as TEFLON* PFA (hereinafter referred to as "TEFLON* PFA”) by E. I. du Pont de Nemours and Company of Wilmington, Delaware (hereinafter referred to as "DuPont”) .
  • TEFLON* PFA perfluoropolymer
  • the electrochemical cell of the first through fourth embodiments also comprises cation-transporting means for transporting the protons therethrough, where one side of the oxidizing means is disposed in contact with one side of the cation-transporting means.
  • the cation-transporting means is a cation- transporting membrane 18 as shown in Fig. 1. More specifically, membrane 18 may be a proton-conducting membrane.
  • Membrane 18 may be a commercial cationic membrane made of a fluoro- or perfluoropolymer, preferably a copolymer of two or more fluoro or perfluoromonomers,- at least one of which has pendant sulfonic acid groups.
  • carboxylic groups are not desirable, because those groups tend to decrease the conductivity of the membrane when they are protonated.
  • Suitable resin materials are available commercially or can be made according to patent literature. They include fluorinated polymers with side chains of the type -CF 2 CFRS0 3 H and -OCF 2 CF 2 CF 2 S0 3 H, where R is a F, Cl, CF 2 C1, or a C ⁇ to C 10 perfluoroalkyl radical.
  • those resins may be in the form that has pendant -S0 2 F groups, rather than -S0 3 H groups.
  • the sulfonyl fluoride groups can be hydrolyzed with potassium hydroxide to -S0 3 K groups, which then are exchanged with an acid to -S0 3 H groups.
  • Suitable cationic membranes which are made of hydrated, copolymers of polytetrafluoroethylene and poly-sulfonyl fluoride vinyl ether-containing pendant sulfonic acid groups, are offered by DuPont under the trademark "NAFION" (hereinafter referred to as NAFION ® ) .
  • NATION ® membranes containing pendant sulfonic acid groups include NAFION ® 117, NAFION ® 324 and NAFION ® 417.
  • the first type of NAFION® is unsupported and has an equivalent weight of 1100 g., equivalent weight being defined as the amount of resin required to neutralize one liter of a 1M sodium hydroxide solution.
  • the other two types of NAFION ® are both supported on a fluorocarbon fabric, the equivalent weight of NAFION ® 417 also being 1100 g.
  • NAFION ® 324 has a two-layer structure, a 125 ⁇ jn-thick membrane having an equivalent weight of 1100 g., and a 25 ⁇ m-thick membrane having an equivalent weight of 1500 g.
  • NAFION ® 117F grade is a precursor membrane having pendant -S0 2 F groups that can be converted to sulfonic acid groups.
  • NAFION ® 117F grade is a precursor membrane having pendant -S0 2 F groups that can be converted to sulfonic acid groups.
  • the present invention describes the use of a solid polymer electrolyte membrane, it is well within the scope of the invention to use other cation- transporting membranes which are not polymeric.
  • proton-conducting ceramics such as beta- alumina may be used.
  • Beta-alumina is a class of nonstoichiometric crystalline compounds having the general structure Na 2 0 x -Al 0 3 , in which x ranges from 5 ( ⁇ "-alumina) to 11 ( ⁇ -alumina) .
  • the electrochemical cell of the first through fourth embodiments also comprises an electrode, or more specifically, cathode 20, where the cathode is disposed in contact with the other side (as opposed to the side which is in contact with the anode) of membrane 18 as illustrated in Fig. 1.
  • Cathode 20 has a cathode-side inlet 2 * 4 and a cathode-side outlet 26 as shown in Fig. 1. Since in the preferred embodiment, anhydrous HCl is processed, and since some chlorides pass through the membrane and consequently, HCl is present on the cathode-side of the cell, the cathode inlet and the outlet may be lined with TEFLON ® PFA.
  • cationic charges are transported through the membrane from anode to cathode, while each electrode carries out a half-cell reaction.
  • molecules of anhydrous hydrogen chloride are transported to the surface of the anode through anode- side inlet 14.
  • the molecules of the anhydrous hydrogen chloride are oxidized to produce essentially dry chlorine gas and protons.
  • the essentially dry chlorine gas exits through anode-side outlet 16 as shown in Fig. 1.
  • the protons, H + are transported through the membrane and reduced at the cathode. This is explained in more detail below.
  • the anode and the cathode may comprise porous, gas-diffusion electrodes. Such electrodes provide the advantage of high specific surface area, as known to one skilled in the art.
  • the anode and the cathode comprise an electrochemically active material disposed adjacent, meaning at or under, the surface of the cation-transporting membrane. A thin film of the electrochemically active material may be applied directly to the membrane. Alternatively, the electrochemically active material may be hot-pressed to the membrane, as shown in A. J. Appleby and E. B. Yeager, Energy, Vol. 11, 137 (1986). Alternatively, the electrochemically active material may be deposited into the membrane, as shown in U.S. Patent No.
  • the electrochemically active material may comprise any type of catalytic or metallic material or metallic oxide, as long as the material can support charge transfer.
  • the electrochemically active material may comprise a catalyst material such as platinum, ruthenium, osmium, rhenium, rhodium, iridium, palladium, gold, titanium or zirconium and the oxides, alloys or mixtures thereof.
  • the oxides of these materials are not used for the cathode.
  • Other catalyst materials suitable for use with the present invention may include, but are not limited to, transition metal macro cycles in monomeric and polymeric forms and transition metal oxides, including perovskites and pyrochores.
  • the electrochemically active material may comprise a catalyst material on a support material.
  • the support material may comprise particles of carbon and particles of polytetrafluoro- ethylene, which is sold under the trademark "TEFLON"
  • TEFLON ® commercially available from DuPont.
  • the electrochemically active material may be bonded by virtue of the TEFLON ® to a support structure, or gas diffusion layer, of carbon paper or graphite cloth and hot-pressed to the cation- transporting membrane.
  • the hydrophobic nature of TEFLON ® does not allow a film of water to form at the anode. A water barrier in the electrode would hamper the diffusion of HCl to the reaction sites.
  • the electrodes are preferably hot-pressed into the membrane in order to have good contact between the catalyst and the membrane.
  • the loadings of electrochemically active material may vary based on the method of application to the membrane.
  • Hot-pressed, gas-diffusion electrodes typically have loadings of 0.10 to 0.50 mg/cm 2 .
  • Lower loadings are possible with other available methods of deposition, such as distributing them as thin films from inks onto the membranes, as described in Wilson and Gottesfeld, "High Performance Catalyzed Membranes of Ultra-low Pt Loadings for Polymer Electrolyte Fuel Cells", Los Alamos National Laboratory, J. Electrd- chem. Soc, Vol. 139, No. 2 L28-30, 1992, where the inks contain solubilized NAFION ® ionomer to enhance the catalyst-ionomer surface contact and to act as a binder to the NAFION ® membrane sheet. With such a system, loadings as low as 0.017 mg active material per cm 2 have been achieved.
  • the membrane of the present invention serves as the electrolyte in which the protons constitute the current.
  • the membrane must be in a sufficient state of hydration in order to act as a proton conductor. Electro-osmotic drag occurs in the membrane, where protons drag water in the direction of current flow. This leads to the development of a concentration gradient of water within the membrane.
  • the conductivity of a membrane is directly related to the water content in the membrane and decreases at low water content. Limiting current occurs when the concentration of water within the membrane reaches a value that will no longer support additional proton conduction. Thus, limiting current density can develop when the conductivity decreases due to low water concentrations.
  • water in the form of a humidified gas stream or liquid water, is supplied to the membrane at the cathode. This is necessary in order to achieve efficient proton transport.
  • the hydration of the membrane is accomplished by the introduction of either liquid water in the first embodiment, or a gas stream comprising hydrogen or nitrogen, respectively, in the second and third embodiments, to the membrane at the cathode-side of the membrane.
  • membrane hydration is accomplished by the production of water at the cathode, as well as the introduction of a humidified gas stream comprising oxygen at the cathode-side of the membrane, which produces water.
  • hydrogen, nitrogen and oxygen are described herein, it is within the scope of the present invention to humidified gas streams comprising other gases.
  • the water at the cathode side of the membrane is transported by diffusion towards the anode.
  • the transported protons drag the water in the membrane, which includes water already present in the membrane to begin with, towards the cathode.
  • the amount of current required to achieve a balance between the water transported by diffusion toward the anode and dragged by the proton transport toward the cathode, at which point limiting current occurs may be controlled by adjusting the amount of water supplied to the membrane at the cathode. Consequently, with the present invention, limiting current may be controlled. This is especially desirable where it is necessary to lower or raise limiting current in order to compensate for changes in the amount of anhydrous hydrogen halide which needs to be processed. This may change in response to changes in manufacturing rates of manufacturers which produce hydrogen chloride.
  • the electrochemical cell of the first through fourth embodiments also comprises inlet means for supplying water to the cation-transporting means at the other side of the cation-transporting means.
  • the inlet means comprises a cathode-side inlet 24 as shown in Fig. 1 which supplies water, in various forms as will be explained below, to the side of the membrane which is disposed in contact with the cathode.
  • the electrochemical cell also comprises outlet means for releasing a fluid from the reducing means at the other side of the cation-transporting means.
  • the outlet means comprises a cathode-side outlet 26 as shown in.Fig.-1, which releases a fluid from the cathode at the side of the membrane which is disposed in contact with the cathode.
  • a cathode-side outlet 26 as shown in.Fig.-1, which releases a fluid from the cathode at the side of the membrane which is disposed in contact with the cathode.
  • the cathode-side inlet and outlet are preferably lined with TEFLON ® PFA.
  • the electrochemical cell of the first through fourth embodiments further comprises an anode flow field 28 disposed in contact with the anode and a cathode flow field 30 disposed in contact with the cathode.
  • the flow fields are electrically conductive, and act as both mass and current flow fields. More specifically, the mass flow fields may include a plurality of anode flow channels 29 and a plurality of cathode flow channels 31 as shown in Fig. 1A.
  • Anode flow field and channels 29 direct reactants, such as anhydrous HCl, and products, such as essentially dry chlorine gas, from the anode.
  • Cathode flow field 30 and channels 31 direct catholyte, such as liquid water in the first embodiment, or a humidified gas stream in the second through fourth embodiments to the cathode and products, such as hydrogen vapor, liquid water and HCl dissolved in the water in the first embodiment, hydrogen and hydrogen halide, in the form of vapor, in the second embodiment, hydrogen, nitrogen, water and hydrogen halide, all in the form of vapor, in the third embodiment, and oxygen, water and hydrogen halide. all in the form of vapor, in the fourth embodiment.
  • the anode and the cathode mass flow fields may comprise grooved porous graphite paper.
  • the flow fields may also be made of a porous carbon in the form of a foam, cloth or matte. The.
  • electrochemical cell of the first through fourth embodiments may also comprise an anode mass flow manifold 32 and a cathode mass flow field manifold 34 as shown in Fig. 1.
  • the purpose of such manifolds is to bring anolyte to and products from the anode, and catholyte to and products from the cathode.
  • the manifolds form a frame around the anode mass flow field and the anode, and the cathode mass flow field and the cathode, respectively.
  • These manifolds are preferably made of a corrosion resistant material, such TEFLON ® PFA.
  • a gasket 36, 38 also contributes to forming a frame around the respective anode and cathode mass flow fields.
  • These gaskets are preferably also made of a corrosion resistant material, such as polytetrafluoroethylene, sold under the trademark TEFLON ® PTFE by DuPont.
  • the electrochemical cell of the first through fourth embodiments also comprises an anode current bus 46 and a cathode current bus 48 as shown in Fig. 1.
  • the current buses conduct current to and from a voltage source (not shown) .
  • anode current bus 46 is connected to the positive terminal of a voltage source
  • cathode current bus 48 is connected to the negative terminal of the voltage source, so that when voltage is supplied to the cell, current flows through all of the cell components to the right of current bus 46 as shown in Fig. 1, including current bus 48, from which it returns to the voltage source.
  • the current buses are made of a conductor material, such as copper.
  • the electrochemical cell of the first and second embodiments further comprises a respective current distributor disposed in contact with a respective flow field.
  • An anode current distributor 40 is disposed in contact with anode flow field 28, and a cathode current distributor 42 is disposed in contact with cathode flow field 30.
  • the anode current distributor collects current from the anode bus and distributes it to the anode by electronic conduction.
  • the cathode current distributor collects current from the cathode and distributes it to the cathode bus.
  • the anode and the cathode current distributors preferably each comprise a non-porous layer.
  • the anode current distributor provides a barrier between the anode current bus and the anode, as well as between the current bus and the anhydrous hydrogen halide, such as hydrogen chloride, and the halogen gas, such as chlorine.
  • the cathode current distributor provides a barrier between the cathode current bus and the cathode, as well as between the cathode current bus and the hydrogen halide. This barrier is desirable, as there is some migration of hydrogen halide through the membrane.
  • the current distributors of the present invention may be made of a variety of materials, and the material used for the anode current distributor need not be the same as the material used for the cathode current distributor. In one instance, the anode current distributor is made of platinized tantalum, and the cathode current distributor is made of a nickel-based alloy, such as UNS10665, sold as HASTELLOY ® B-2, by Haynes, International.
  • the electrochemical cell also comprises a conductive structural support 44 disposed in contact with anode current distributor 40.
  • the support on the anode side is preferably made of UNS31603 (316L stainless steel) .
  • a seal 45 preferably in the form of an O-ring made from a perfluoroelastomer, sold under the trademark KALREZ ® by DuPont, is disposed between structural support 44 on the anode side and anode current distributor 40.
  • the cathode current distributor acts as a corrosion-resistant structural backer on the cathode side. This piece can be drilled and tapped to accept the TEFLON ® PFA fitting, which is used for the inlet and outlet.
  • a bipolar arrangement as familiar to one skilled in the art, is preferred.
  • the electrochemical cell of the present invention may be used in a bipolar stack.
  • current distributors 40 and 42 and all the elements disposed in between as shown in Fig. 1 are repeated along the length of the cell, and current buses are placed on the outside of the stack.
  • the electrochemical cell can be operated over a wide range of temperatures. Room temperature operation is an advantage, due to the ease of use. of the cell. However, operation at elevated temperatures provides the advantages of improved kinetics and increased electrolyte conductivity.
  • one is not restricted to operate the electrochemical cell of any of the first through fourth embodiments at atmospheric pressure. The cell could be run at differential pressure gradients, which change the transport characteristics of water or other components in the cell, including the membrane.
  • the electrochemical cell of any of the embodiments of the present invention can be operated at higher temperatures at a given pressure than electrochemical cells operated with aqueous hydrogen chloride of the prior art. This affects the kinetics of the reactions and the conductivity of the NAFION ® . Higher temperatures result in lower cell voltages. However, limits on temperature occur because of the properties of the materials used for elements of the cell. For example, the properties of a NAFION ® membrane change when the cell is operated above 120° C. The properties of a polymer electrolyte membrane make it difficult to operate a cell at temperatures above 150° C. With a membrane made of other materials, such as a ceramic material like beta- alumina, it is possible to operate a cell at temperatures above 200° C.
  • a system and a process for recycling a fluid released from an electrochemical cell used for the direct production of essentially dry halogen gas from essentially anhydrous hydrogen halide is shown in Fig. 2 and comprises an electrochemical cell 10, which is the same as electrochemical cell 10 as described above.
  • electrochemical cell 10 which is the same as electrochemical cell 10 as described above.
  • liquid water is fed to cathode-side inlet 24 as shown in Fig. 1, and subsequently to the cathode-side of the membrane.
  • Cathode-side outlet 26 releases a fluid, which in the first embodiment comprises water (H 2 0) in the form of a liquid, hydrogen (H 2 ) in the form of vapor, and hydrogen halide, such as hydrogen chloride, which is dissolved in the water.
  • a fluid which in the first embodiment comprises water (H 2 0) in the form of a liquid, hydrogen (H 2 ) in the form of vapor, and hydrogen halide, such as hydrogen chloride, which is dissolved in the water.
  • the system for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide further comprises means for recycling the released fluid back to the cation-transporting means. More specifically, the recycling means comprises a recycling loop which recycles the released fluid back to the membrane at the cathode-side of the membrane.
  • the recycling means may comprise a cooler for cooling the released fluid. As shown in Fig. 2, hydrogen (H 2 ) in the form of a vapor, water (H 2 0) in the form of a liquid, and a hydrogen halide, such as hydrogen chloride, which is dissolved in the water, which have been released from the cell, are carried through a line 50 to a' cooler 52 which cools the released fluid.
  • the recycling means may also comprise a separator for removing a portion of the hydrogen halide from the released fluid. As shown in Fig. 2, after the released fluid is cooled, it is carried through a line 54 to a separator 56, which removes a portion of the hydrogen chloride dissolved in water (H 2 0) through a line 70 as shown in Fig. .2.
  • the recycling means may further comprise a scrubber for removing another portion of the hydrogen halide. Specifically, hydrogen (H 2 ) , hydrogen chloride (HCl) and water (H2O) , all in the form of vapor, are carried through a line 60 to a scrubber 62.
  • the recycling means may also comprise a pump for pumping the. released fluid through the recycling loop back to the membrane.
  • liquid water (H 2 0) and hydrogen chloride (HCl) dissolved in the water, are carried through line 70 to a pump 72.
  • the water and hydrogen chloride are then carried out of pump 72 through a line 74.
  • the recycling means of the first embodiment may also comprise a' temperer, shown as a heater/cooler 80 in Fig. 2, which tempers the released fluid. Temperer 80 may either heat or cool the released fluid, depending on the desired temperature for the electrochemical cell.
  • the recycling means of the first embodiment may further comprise a conditioner 78 for conditioning the released fluid.
  • Conditioner 78 supplies heat and water through a line 77 to the released fluid.
  • Liquid water (H2O) with a small amount of residual hydrochloric acid, is carried through a line 82 back to electrochemical cell 10, where it is used to continuously supply liquid water to the membrane.
  • a system and a process for recycling a gas stream from an electrochemical cell used for the direct production of essentially dry halogen gas from essentially anhydrous hydrogen halide is shown in Fig. 3 and comprises an electrochemical cell 10', which is the same as electrochemical cell 10 as described above.
  • a humidified gas stream comprising hydrogen is fed to cathode-side inlet 24 of the cell as shown in Fig. 1.
  • the humidified gas stream comprises primarily hydrogen. However, in practice, traces of other gases, except oxygen, may be included in the gas stream .of the second embodiment.
  • Cathode-side outlet 26 as shown in Fig. 1 releases a fluid from the cathode, which in the second embodiment comprises water (H 2 0) , hydrogen (H 2 ) , and' hydrogen halide, such as HCl, all in the form of vapor.
  • the system for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide of the second embodiment further comprises means for recycling the released fluid back to the cation- transporting means. More specifically, the recycling means comprises a recycling loop which recycles the released fluid back to the membrane at the cathode- side of the membrane.
  • the recycling means of the second embodiment may comprise a cooler for cooling the released fluid. As shown in Fig. 3, the water (H 2 0) , hydrogen (H 2 ) and hydrogen halide, all in the form of vapor, are carried through a line 50' to a cooler 52' which cools the released fluid.
  • the released fluid comprises hydrogen halide, specifically hydrogen chloride in a preferred embodiment
  • the recycling means may also comprise a separator for removing a portion of the hydrogen halide from the released fluid.
  • a separator for removing a portion of the hydrogen halide from the released fluid.
  • the recycling means may further comprise a scrubber for removing another portion of the hydrogen halide.
  • hydrogen (H 2 ) , hydrogen chloride (HCl) and water (H 2 0) are carried through a line 60' to a scrubber 62'.
  • An alkali solution is added to scrubber 62' through a line 64', so that the scrubber removes another portion of the hydrogen chloride through a line 68', as a halide alkali salt.
  • Hydrogen vapor (H 2 ) and water vapor (H 2 0) which may be discarded or used in another process, are vented from scrubber 62' through a line 66'.
  • Hydrogen vapor (H 2 ) and water vapor (H 2 0) are carried away from scrubber 62' by a line 67'.
  • the recycling means may also comprise a humidifier for humidifying the released fluid.
  • a humidifier 65' humidifies the released fluid, which is hydrogen vapor and water vapor, with water, in either liquid or vapor form, through a line 69' .
  • the humidified hydrogen and water vapor is carried away from line 69' by a line 71'.
  • the recycling means may also comprise a compressor 72' for compressing the released fluid. The water and hydrogen are then carried out of compressor 72' through a line 74'.
  • the recycling means of the second embodiment may also comprise a temperer, shown as a heater/cooler 80' in Fig. 2, which tempers the released fluid. Temperer 80' may either heat or cool the released fluid, depending on the desired temperature of the cell.
  • the water and hydrogen vapor are then carried through a line 76'.
  • the recycling means of the second embodiment may further comprise a conditioner 78' for conditioning, or supplying heat and water, to the released fluid, which is still hydrogen vapor and water vapor, through a line 77''.
  • a humidifier or a conditioner are used, but not both.
  • the hydrogen and water vapor are carried through a line 82' back to electrochemical cell 10', where they are used to continuously suppiy a humidified gas stream, which includes hydrogen, to the membrane.
  • a system and a process for recycling a gas stream from an electrochemical cell used for the direct production of essentially dry halogen gas from essentially anhydrous hydrogen halide is shown in Fig. 4 and comprises an electrochemical cell 10'', which is the same as electrochemical cell 10 as described above.
  • a humidified gas stream comprising nitrogen is fed to cathode-side inlet 24 as shown in Fig. 1.
  • the humidified gas comprises primarily nitrogen. However, in practice, traces of other gases other than oxygen may be included in the gas stream.
  • Cathode-side outlet 26 as shown in Fig.
  • the system for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide of the third embodiment further comprises means for recycling the released fluid back to the cation- transporting means. More specifically, the recycling means comprises a recycling loop which recycles the released fluid back to the membrane at the cathode- side of the membrane.
  • the recycling means of the third embodiment may comprise a cooler for cooling the released fluid. As shown in Fig.
  • the water (H 2 0) , nitrogen (N 2 ) , hydrogen (H 2 ) and hydrogen halide, such as HCl, all in the form of a vapor, are carried through line 50'' to a cooler 52'' which cools the released fluid.
  • the released fluid comprises hydrogen halide, specifically hydrogen chloride in a preferred embodiment, and the recycling means may also comprise a separator for removing a portion of the hydrogen halide from the released fluid.
  • the released fluid is carried through a line 54'' to a separator 56'', which removes a portion of the hydrogen chloride and the water (H 2 0) in the form of liquid through a line 70''.
  • the recycling means may further comprise a scrubber for removing another portion of the hydrogen halide.
  • a scrubber for removing another portion of the hydrogen halide.
  • hydrogen (H 2 ) , nitrogen (N 2 ) f hydrogen chloride (HCl) and water (H 2 0) are carried through a line 60'' to a scrubber 62' '.
  • An alkali solution is added to scrubber 62'' through a line
  • the recycling means may also comprise a humidifier for humidifying the released fluid.
  • a humidifier 65'' humidifies the released fluid, which is hydrogen vapor, nitrogen vapor and water vapor, with water, in either liquid or vapor form through a line 69''.
  • the recycling means may also comprise a compressor 72'' for compressing the released fluid. The water, hydrogen and nitrogen, all in the form of vapor, are then carried out of compressor 72*' through a line 74'*.
  • the humidified fluid is carried away from line 69'' by a line 71''.
  • the recycling means of the third embodiment may also comprise a temperer, shown as heater/cooler 80'' in Fig. 4, which tempers the released fluid.
  • the water, hydrogen and nitrogen are then carried through a line 74'' to temperer 80''.
  • Temperer 80'' may either heat or cool the released fluid, depending on the desired temperature of the cell.
  • the recycling means of the second embodiment may further comprise a conditioner 78'' for supplying heat and water to the released fluid through a line 77''.
  • a humidifier or a conditioner is used in the recycle loop of the third embodiment, but not both.
  • additional nitrogen is supplied from a source 84' ' to the cell through a line 83' ', since nitrogen is being lost in the loop through line 66.
  • the nitrogen may be added anywhere in the recycle loop.
  • Nitrogen (N ,) and water vapor. (H 2 0 (vapor) ) are carried through a line 82' ' back to electrochemical cell 10*', where they are used to continuously supply a humidified gas stream, which includes nitrogen, to the membrane at the cathode-side of the membrane.
  • a system and a process for recycling a gas stream from an electrochemical cell used for the direct production of essentially dry halogen gas from essentially anhydrous hydrogen halide is shown in Fig. 5 and comprises an electrochemical cell 10"'', which is the same as electrochemical cell 10 as described above.
  • a humidified gas stream comprising oxygen is fed to cathode-side inlet 24 as shown in Fig. 1.
  • the humidified gas comprises primarily oxygen. However, in practice, traces of other gases, not including hydrogen, but including nitrogen, may be in the gas stream.
  • Cathode-side outlet 26 as shown in Fig.
  • a fluid from the cathode through a line 50' 1 ', which in the fourth embodiment comprises oxygen (0 2 ) , water (H 2 0) and hydrogen halide, such as hydrogen chloride (HCl) , all in the form of vapor, as shown in Fig. 5.
  • oxygen (0 2 )
  • water H 2 0
  • hydrogen halide such as hydrogen chloride (HCl)
  • the system for directly producing essentially dry halogen gas from essentially anhydrous hydrogen halide of the fourth embodiment further comprises means for recycling the released fluid back to the cation- transporting means. More specifically, the recycling means comprises a recycling loop which recycles the released fluid back to the membrane at the cathode- side of the membrane.
  • the recycling means of the third embodiment may comprise a cooler for cooling the released fluid. As shown in Fig. 5, water, (H 2 0) , oxygen (0 2 ) and hydrogen chloride (HCl) , all in the form of vapor, are carried through a line 50''' to a cooler 52' ' ' which cools the released fluid.
  • the released fluid comprises hydrogen halide, and preferably, hydrogen chloride
  • the recycling means may also comprise a separator for removing a portion of the hydrogen halide from the released fluid.
  • a separator for removing a portion of the hydrogen halide from the released fluid.
  • the recycling means may further comprise a scrubber for removing another portion of the hydrogen halide.
  • oxygen (0 2 ) , hydrogen chloride (HCl) and water (H 2 0) are carried through a line 60''' to a scrubber 62'''.
  • An alkali solution is added to scrubber 62''' through a line 64'*', so that the scrubber removes another portion of the hydrogen chloride through a line 68'*', as a halide alkali salt.
  • a portion of the oxygen vapor (0 2 ) and the water vapor (H 0) is not vented, but rather all of the oxygen and water vapor are carried away from scrubber 62' ' ' by a line 67*'*.
  • the recycling means may also comprise a humidifier 65'*' for humidifying the released fluid with water, in either liquid or vapor form, through a line 69'*'.
  • the humidified fluid is carried away from line 69 ' ' ' by a line 71'**.
  • the recycling means may also comprise a compressor 72''' for compressing the released fluid.
  • the water vapor and oxygen vapor are then carried out of compressor 72' ' ' through a line 74' ' ' .
  • the recycling means of the fourth embodiment may also comprise an oxygen supply for supplying additional oxygen to the released fluid.
  • An oxygen supply supplies additional oxygen to the released fluid through a line 77''' as shown in Fig. 5, although this line could be placed anywhere in the recycling loop.
  • a line 79' " carries the oxygenated released fluid away from oxygen supply line 83' ' ' .
  • the recycling means of the fourth embodiment may also comprise a temperer, shown as heater/cooler 80' ' ' in Fig. 5, which tempers the released fluid. Temperer 80''' may either heat or cool the released fluid, depending on the desired temperature of the cell.
  • a line 76' '' carries the tempered fluid away from temperer 80'''.
  • the recycling means of the fourth embodiment may further comprise a conditioner 78''' for supplying heat and water to the released fluid through a line 77'''.
  • Oxygen (0 2 ) and water vapor (H 2 0 (vapor) ) are carried through a line 82' ' ' back to electrochemical cell 10''', where the oxygen they are used to continuously supply a humidified gas stream, which includes oxygen to the membrane.
  • the anhydrous hydrogen halide may comprise hydrogen chloride, hydrogen bromide, hydrogen fluoride or hydrogen iodide. It should be noted that the production of bromine gas and iodine gas can be accomplished when the electrochemical cell is run at elevated temperatures (i.e., about 60° C and above for bromine and about 190° C and above for iodine) . In the case of iodine, a membrane made of a material other than NAFION ® should be used.
  • anhydrous hydrogen halide is hydrogen chloride.
  • anode current distributor 40 collects current from the anode bus and distributes it to the anode by electronic conduction.
  • Molecules of essentially anhydrous hydrogen chloride gas are fed to an inlet, specifically anode inlet 14 of electrochemical cell 10, and are transported to the surface of anode 12 and through the gas channels in the mass flow fields.
  • liquid water as shown in Fig. 2 is added to the cell at the cathode.
  • the water is delivered to the cathode through cathode inlet 24 and through flow channels 31 formed in cathode flow field 30.
  • a humidified gas stream comprising hydrogen is delivered to the cathode through cathode inlet 24, and in the third embodiment, a humidified gas stream comprising nitrogen in delivered through inlet 2 .
  • This hydrates the membrane and thereby increase the efficiency of proton transport through the membrane.
  • Molecules of the anhydrous hydrogen chloride are oxidized at the anode under the potential created by the voltage source to produce essentially dry chlorine gas at the anode, and protons (H + ) . This reaction is given by the equation:
  • the chlorine gas exits through anode outlet 16 as shown in Fig. 1.
  • the protons are transported through the membrane, which acts as an electrolyte.
  • the transported protons are reduced at the cathode. This reaction is given by the equation:
  • a fluid is released from the, cell and is recycled back to the membrane through the respective recycle loops as described above with respect to Figs. 2 - 4.
  • Hydrogen which is evolved at the interface between the cathode and the membrane exits via cathode-side outlet 26. The hydrogen bubbles through the water and is not affected by the TEFLON ® in the electrode.
  • Cathode current distributor 42 collects current from cathode 20 and distributes- it to cathode bus 48.
  • the amount of current required to achieve a balance between the water transported by diffusion toward the anode and dragged by proton transport toward the cathode is controlled by adjusting the amount of water supplied to the membrane.
  • the water supplied to the membrane is adjusted by controlling the feed rate of the humidified gas stream.
  • the water supplied to the membrane is adjusted by controlling the water content of the humidified gas stream.
  • humidified gas streams comprising either hydrogen or nitrogen are described for the first embodiment, it is within the scope of the present invention to humidified gas streams comprising other gases.
  • the electrochemical cell operates as described above, except that a humidified gas stream comprising oxygen is supplied to the cell at the cathode. Oxygen and the transported protons are reduced at the cathode to water, which is expressed by the equation:
  • the water formed exits via cathode-side outlet 26 as shown in Fig. 1, along with any nitrogen and unreacted oxygen.
  • the water also helps to maintain hydration of the membrane.
  • the cathode-side outlet releases a fluid from the cathode, which comprises oxygen (0 2 ) , water (H 2 0) and hydrogen halide, such as hydrogen chloride (HCl) , as described above with respect to
  • Fig. 5 This fluid released from the cell is recycled back to the membrane through the recycle loop as described above with respect to Fig. 5.
  • the amount of current required to achieve a balance between the water transported by diffusion toward the anode and dragged by proton transport toward the cathode is controlled by adjusting the amount of water supplied to the membrane.
  • the water supplied to the membrane is adjusted by controlling the feed rate of the humidified gas stream.
  • the water supplied to the membrane is adjusted by controlling the water content of the humidified gas stream.
  • a humidified gas stream comprising oxygen is described for the second embodiment, it is within the scope of the present invention to humidified gas streams comprising other gases.
  • the cathode reaction is the formation of water.
  • This cathode reaction has the advantage of more favorable thermodynamics relative to H 2 production at the cathode as in the first embodiment. This is because the overall reaction in this embodiment, which is expressed by the following equation:
  • the amount of voltage or energy required as input to the cell is reduced in the fourth embodiment.
  • there is always an excess of oxygen in the cell This means that almost all the protons transported across the membrane react with oxygen to form water. This provides a higher conversion to water.
  • the higher the excess of oxygen the faster the cathode reaction proceeds.
  • the recycle loop of the fourth embodiment in particular provides a faster cathode reaction.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

L'invention porte sur une cellule, un système et un procédé électrochimiques servant à convertir de l'halogénure d'hydrogène quasiment anhydre en gaz halogène quasiment sec. Le procédé de l'invention s'avère utile pour convertir de l'halogénure d'hydrogène anhydre, en particulier, du chlorure d'hydrogène, du fluorure d'hydrogène, du bromure d'hydrogène et du iodure d'hydrogène en gaz halogène, tel que du chlore, du fluor, du brome ou de l'iode. Dans cette invention, en particulier, on approvisionne en eau la membrane à transport cationique au niveau de la cathode de différentes manières. L'invention permet de récupérer un fluide libéré côté cathode et de retourner après recyclage le fluide récupéré au côté cathode de la membrane. On peut ainsi recycler le fluide récupéré qui a été libéré pour alimenter la membrane en eau, ce qui permet d'augmenter et/ou de réguler la densité de courant limite de la cellule.
PCT/US1995/016032 1995-05-01 1995-12-13 Conversion electrochimique d'halogenure d'hydrogene anhydre en gaz halogene au moyen d'une membrane a transport cationique WO1996034998A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP95944322A EP0828865B1 (fr) 1995-05-01 1995-12-13 Conversion electrochimique d'halogenure d'hydrogene anhydre en gaz halogene au moyen d'une membrane a transport cationique
DE69523077T DE69523077T2 (de) 1995-05-01 1995-12-13 Elektrochemische umwandlung von wasserfreiem halogenwasserstoff in halogengas mittels einer kationenaustauschermembran
JP53327296A JP3827019B2 (ja) 1995-05-01 1995-12-13 カチオン−輸送膜を使用する無水ハロゲン化水素のハロゲンガスへの電気化学的転化
AU46398/96A AU4639896A (en) 1995-05-01 1995-12-13 Electrochemical conversion of anhydrous hydrogen halide to h alogen gas using a cation-transporting membrane
MX9708397A MX9708397A (es) 1995-05-01 1995-12-13 Conversion electroquimica del haluro de hidrogeno anhidro a gas halogeno usando una membrana de transporte cationica.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US43241095A 1995-05-01 1995-05-01
US08/432,410 1995-05-01

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WO1996034998A1 true WO1996034998A1 (fr) 1996-11-07

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JP (1) JP3827019B2 (fr)
AU (1) AU4639896A (fr)
CA (1) CA2219922A1 (fr)
DE (1) DE69523077T2 (fr)
MX (1) MX9708397A (fr)
WO (1) WO1996034998A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19755636A1 (de) * 1997-12-15 1999-06-17 Bayer Ag Verfahren zur elektrochemischen Aufarbeitung von HCl-Gas zu hochreinem Chlor
GB2403166A (en) * 2003-06-25 2004-12-29 Accentus Plc Electrodeionisation process
WO2007131700A1 (fr) * 2006-05-16 2007-11-22 Bayer Materialscience Ag Procédé de fabrication d'isocyanates
EP2148942A2 (fr) * 2007-05-14 2010-02-03 GRT, Inc. Procédé de conversion de matières premières d'hydrocarbures avec récupération électrolytique d'halogène

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2488448A1 (fr) * 2009-10-16 2012-08-22 Solvay Fluor und Derivate GmbH Fluor gazeux de grande pureté, sa fabrication et son utilisation, et procédé de surveillance des impuretés dans un fluor gazeux

Citations (4)

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Publication number Priority date Publication date Assignee Title
GB959846A (en) * 1960-11-01 1964-06-03 Ionics An electrolytic process for producing halogen gases and the apparatus therefor
WO1979000688A1 (fr) * 1978-03-02 1979-09-20 Lindstroem Ab Olle Cellule a electrolyse specialement concue pour l'electrolyse chloroalcaline avec electrode a air
US4221644A (en) * 1979-08-14 1980-09-09 Diamond Shamrock Corporation Air-depolarized chlor-alkali cell operation methods
WO1995014797A1 (fr) * 1993-11-22 1995-06-01 E.I. Du Pont De Nemours And Company Anode utile pour la conversion electrochimique d'un halogenure d'hydrogene anhydre en halogene gazeux

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB959846A (en) * 1960-11-01 1964-06-03 Ionics An electrolytic process for producing halogen gases and the apparatus therefor
WO1979000688A1 (fr) * 1978-03-02 1979-09-20 Lindstroem Ab Olle Cellule a electrolyse specialement concue pour l'electrolyse chloroalcaline avec electrode a air
US4221644A (en) * 1979-08-14 1980-09-09 Diamond Shamrock Corporation Air-depolarized chlor-alkali cell operation methods
WO1995014797A1 (fr) * 1993-11-22 1995-06-01 E.I. Du Pont De Nemours And Company Anode utile pour la conversion electrochimique d'un halogenure d'hydrogene anhydre en halogene gazeux

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19755636A1 (de) * 1997-12-15 1999-06-17 Bayer Ag Verfahren zur elektrochemischen Aufarbeitung von HCl-Gas zu hochreinem Chlor
US6368490B1 (en) 1997-12-15 2002-04-09 Bayer Aktiengesellschaft Method for electrochemically processing HCL gas into highly pure chlorine
GB2403166A (en) * 2003-06-25 2004-12-29 Accentus Plc Electrodeionisation process
GB2403166B (en) * 2003-06-25 2006-11-01 Ipsolutions Electrodeionisation process
WO2007131700A1 (fr) * 2006-05-16 2007-11-22 Bayer Materialscience Ag Procédé de fabrication d'isocyanates
EP2148942A2 (fr) * 2007-05-14 2010-02-03 GRT, Inc. Procédé de conversion de matières premières d'hydrocarbures avec récupération électrolytique d'halogène
EP2148942A4 (fr) * 2007-05-14 2011-11-09 Grt Inc Procédé de conversion de matières premières d'hydrocarbures avec récupération électrolytique d'halogène

Also Published As

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JP3827019B2 (ja) 2006-09-27
DE69523077T2 (de) 2002-06-06
EP0828865A1 (fr) 1998-03-18
MX9708397A (es) 1998-02-28
DE69523077D1 (de) 2001-11-08
CA2219922A1 (fr) 1996-11-07
AU4639896A (en) 1996-11-21
JPH11504390A (ja) 1999-04-20
EP0828865B1 (fr) 2001-10-04

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