• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    1484612 Laminates E I DU PONT DE NEMOURS & CO 20 May 1975 [21 June 1974] 21578/75 Heading B5N [Also in Division C7] A composite ion-exchange polymer film comprises pendant sulphonyl groups in ionexchangeable form, each attached to a C atom to which at least one F atom is also attached, not more than 1/3 of the thickness thereof comprising polymer (i) which has an EW at least 250 greater than polymer (ii) comprising the remainder of the film. The film is used with polymer (i) facing the cathode in conventional diaphragmcell chlor-alkali production. Polymer (i) may have an EW no more than 2000 and polymer (ii) an EW of 1000-1500. The membrane may comprise a copolymer of an ethylenically unsaturated fluorocarbon, e.g. TFE with an unsaturated fluoro-sulphonyl compound of formula CF 2 =CFORfSO 2 F where the ether link is optional and Rf is a bivalent C 2-8 perfluoro radical with or without ether linkages, e.g. CF 2 = CFOCF 2 CF(CF 3 )OCF 2 CF 2 SO 2 F, and wherein the SO 2 F groups are subsequently converted to ion-exchange form such as a sulphonamide or sulphonic acid or salt group. The ion-exchange groups of polymers (i) and (ii) may be the same or different. A reinforcement of fabric of fluorinated resin, glass or quartz may be embedded in the polymer (ii). A laminate with a PTFE cloth is disclosed.
    公开号:SU710519A3
    申请号:SU752145943
    申请日:1975-06-20
    公开日:1980-01-15
    发明作者:Ньютон Волмсли Питер
    申请人:Е.И.Дюпон Де Немур Энд Компани (Фирма)；
    IPC主号:
    专利说明:

    (54) COMBINED BY MEMBRANE electrical resistance is a small part of the thickness of the membrane and, therefore, the increase in the total resistivity caused by this layer is relatively small. The advantages of using a barrier LAYER are superior to the disadvantage associated with a high equivalent weight of a polymer having a high electrical resistance. resistivity Although a polymer with a high equivalent weight can be no more than one third of the thickness of the membrane, it is most desirable that this polymer should be no more than hydrochloric fifth or one-tenth of its thickness. Since a high equivalent weight polymer has barrier properties for anions passing from the cathode of an electrolytic cell to the anode, the polymer must form a continuous layer. Three buoys are 0.5 mm thick. The thickness of the layer may vary depending on the equivalent weight of the polymer used, the higher the equilibrium weight, the stronger the barrier properties for the pro. the course of ishh anions. For example, we take an equivalent weight of 2000 or more. Since the electric specific. if the resistance increases with an increase in the equivalent weight, then with a view to both the livers the minimum power consumed is the most. It is desirable to use a thinner barrier layer. The difference in equivalent weights of polymers forming two parts of a composite membrane must be at least 250. The main part of a composite membrane has a low equivalent weight of eg IOOO or more. Although a low equivalent weight is desirable, polymers with too low equivalent weights absorb too much water, which reduces their mechanical properties. From a production point of view, it is desirable that an equivalent weight of 1000-1500. The total thickness of the membrane varies with, depending on the ion-exchange groups used, equivalent polymer weights, the required membrane strength, and the operating conditions of the electrolytic cells, etc. Usually, the lower limit of the thickness of the composite membrane is 3 mm, and preferably 4. mm. There is no upper limit for film thickness (except for practical reasons). For example, an increase in electrical resistance leads to an excessive film thickness. In addition, the increased weight of the polymer leads to increased cost. “As already mentioned, the composite membrane is especially useful in the production of halogens and metal hydroxides from alkali or alkaline earth metals. Example. In this and subsequent, uifix examples, membranes with specific specific equivalent weights are obtained from the original copolymer obtained from ethylene tetrafluoride and tPj CFO (iF2 t, FO (iFjClF2 OiP) The copolymer is converted into ionic form with a sulfide group of the form SOg during chlorine-alkali process element. A composite membrane consisting of a film with a thickness of 1/2 mm with an equivalent weight of 1700 and a film with a thickness of 4 mm with an equivalent weight of 1100 applied in layers on a film of T-12 fabric is placed in a laboratory chlorine-alkali element between two flat metal electrodes used. The electrodes used are a stainless steel mesh cathode and a stable titanium mesh anode coated with an oxide of a noble metafield. The distance between the film and each of the electrodes is approximately 1/8 inch. On the anode side in a circulating element. It emits hot (80 ° C) aqueous sodium chloride solution, the weight concentration of which is maintained at 12–15%. The concentration of hot caustic () catalyst is maintained at 5–7 n., which is achieved by continuous addition of water to the catholyte. After the element temperature reaches 80 ° C, a current is passed through the element, the value of which is 2 A per 1 square meter. inch of membrane. After three days of continuous operation, the efficiency of the galvanic cell was found by determining the amount of caustic produced as a function of the amount of electricity passed through the cell. The efficiency found was 85.6%. The voltage on the galvanic cell is 4.43 V, and the caustic concentration of catholyte is 7.1 and. Energy consumption 1,775 kWh per lb {454 g) of chlorine. PRI me R 2 (comparative). A composite membrane consisting of a 5 mm thick film with an equivalent weight of 1200 applied in layers on a layer of T-12 fabric is installed in the laboratory chlor-alkaline electroplating element described in Example 1. After two days of continuous operation, the effectiveness of the galvanic cell is determined. amounted to 47.2%. The voltage is 3.34 in, and the concentration of caustic is 6 n.
    After an additional five days of continuous operation, the efficiency of the element was 46.4%. The voltage is 3.32 volts and the caustic concentration is 6.8 n.
    This last example shows that energy consumption was 2,427 kWh per 1 pound of chlorine.
    Primerz (comparative). A composite membrane consisting of a 5 mm thick film with an equivalent weight of 1100, applied in layers on the T-12 LAYER, is placed in the laboratory chlor-alkali electroplating element described in Example 1. After three days of continuous operation, the effectiveness of the galvanic cell is determined. amounted to 38.6%. The voltage on the galvanic cell is 3.32 V, and the concentration of caustic in catholyte is 5.4 n.
    Energy consumption is 2.950 kWh per lb. of chlorine.
    权利要求:
    Claims (1)
    [1]
    1. US patent 3784399, 0 cl. From 25 to 13/08, published 1973.
    类似技术:
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    同族专利:
    公开号 | 公开日
    JPS5418994B2|1979-07-11|
    FR2275298A1|1976-01-16|
    US3909378A|1975-09-30|
    JPS5114184A|1976-02-04|
    AU8225475A|1976-12-23|
    DE2509868B2|1976-12-09|
    ZA753961B|1976-05-26|
    IL47528A|1978-04-30|
    DE2509868A1|1976-01-02|
    EG11807A|1977-11-30|
    GB1484612A|1977-09-01|
    SU1075986A3|1984-02-23|
    IL47528D0|1975-08-31|
    CA1052322A|1979-04-10|
    IT1039190B|1979-12-10|
    FR2275298B1|1979-10-19|
    NL7507405A|1975-12-23|
    BR7503908A|1976-07-06|
    BE830500A|1975-10-16|
    AU499236B2|1979-04-12|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3692569A|1970-02-12|1972-09-19|Du Pont|Surface-activated fluorocarbon objects|
    US3784399A|1971-09-08|1974-01-08|Du Pont|Films of fluorinated polymer containing sulfonyl groups with one surface in the sulfonamide or sulfonamide salt form and a process for preparing such|DE2437395C3|1973-10-15|1979-02-08|E.I. Du Pont De Nemours And Co., Wilmington, Del. |Film made from fluorine-containing polymers with side chains containing sulfonyl groups|
    US4113585A|1975-10-20|1978-09-12|E. I. Du Pont De Nemours And Company|Method and apparatus for electrolysis of alkali or alkaline earth metal halide|
    US4056447A|1975-03-06|1977-11-01|Oronzio De Nora Impianti Elettrochimici S.P.A.|Electrolyzing alkali metal chlorides using resin bonded asbestos diaphragm|
    US4021327A|1975-04-29|1977-05-03|E. I. Du Pont De Nemours And Company|Reinforced cation permeable separator|
    JPS526374A|1975-07-07|1977-01-18|Tokuyama Soda Co Ltd|Anode structure for electrolysis|
    JPS5833312B2|1975-10-28|1983-07-19|Asahi Chemical Ind|
    JPS6125793B2|1975-12-15|1986-06-17|Tokuyama Soda Kk|
    JPS52145397A|1976-03-31|1977-12-03|Asahi Chem Ind Co Ltd|Electrolysis|
    GB1581348A|1976-08-04|1980-12-10|Ici Ltd|Bipolar unit for electrolytic cell|
    US4110265A|1977-03-01|1978-08-29|Ionics Inc.|Ion exchange membranes based upon polyphenylene sulfide|
    US4217198A|1979-03-23|1980-08-12|Olin Corporation|Coated perfluorosulfonic acid resin membranes and a method for their preparation|
    US4250126A|1979-03-30|1981-02-10|Dow Yates|Chlorine generator and method|
    US4243508A|1979-04-26|1981-01-06|Dankese Joseph P|Electrochemical apparatus|
    US4384937A|1979-05-29|1983-05-24|Diamond Shamrock Corporation|Production of chromic acid in a three-compartment cell|
    US4273628A|1979-05-29|1981-06-16|Diamond Shamrock Corp.|Production of chromic acid using two-compartment and three-compartment cells|
    JPH0118156B2|1979-10-06|1989-04-04|Tosoh Corp|
    CA1172919A|1980-04-09|1984-08-21|Walther G. Grot|Protective clothing of fabric containing a layer ofhighly fluorinated ion exchange polymer|
    CA1172920A|1980-04-09|1984-08-21|Walther G. Grot|Protective clothing of fabric containing a layer ofhighly fluorinated ion exchange polymer|
    US4804727A|1980-06-11|1989-02-14|The Dow Chemical Company|Process to produce novel fluorocarbon vinyl ethers and resulting polymers|
    US4337137A|1980-06-11|1982-06-29|The Dow Chemical Company|Composite ion exchange membranes|
    US4470889A|1980-06-11|1984-09-11|The Dow Chemical Company|Electrolytic cell having an improved ion exchange membrane and process for operating|
    US4330654A|1980-06-11|1982-05-18|The Dow Chemical Company|Novel polymers having acid functionality|
    US4337211A|1980-06-11|1982-06-29|The Dow Chemical Company|Fluorocarbon ethers having substituted halogen site and process to prepare|
    US4358545A|1980-06-11|1982-11-09|The Dow Chemical Company|Sulfonic acid electrolytic cell having flourinated polymer membrane with hydration product less than 22,000|
    US4515989A|1980-06-11|1985-05-07|The Dow Chemical Company|Preparation decarboxylation and polymerization of novel acid flourides and resulting monomers|
    US4358412A|1980-06-11|1982-11-09|The Dow Chemical Company|Preparation of vinyl ethers|
    CA1214433A|1980-11-05|1986-11-25|Toyo Soda Manufacturing Co., Ltd.|Method for manufacturing cation exchange membrane|
    US4401711A|1981-01-16|1983-08-30|E. I. Du Pont De Nemours And Company|Cation exchange membrane with high equivalent weight component|
    AT26471T|1982-06-09|1987-04-15|Ici Plc|POROESES DIAPHRAGMA FOR AN ELECTROLYSIS CELL.|
    US4871703A|1983-05-31|1989-10-03|The Dow Chemical Company|Process for preparation of an electrocatalyst|
    US4610764A|1984-02-07|1986-09-09|Asahi Glass Company Ltd.|Electrolytic cation exchange membrane|
    DE3650465T2|1985-02-09|1996-09-12|Asahi Chemical Ind|Permeable polymer membrane for gas drying|
    US4784900A|1985-05-31|1988-11-15|University Of Bath|Method for sizing polytretrafluoroethylene fabrics|
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    US4668372A|1985-12-16|1987-05-26|The Dow Chemical Company|Method for making an electrolytic unit from a plastic material|
    US4668371A|1985-12-16|1987-05-26|The Dow Chemical Company|Structural frame for an electrochemical cell|
    US4670123A|1985-12-16|1987-06-02|The Dow Chemical Company|Structural frame for an electrochemical cell|
    US4778723A|1986-06-20|1988-10-18|The Dow Chemical Company|Method for sizing polytetrafluoroethylene fibers, yarn, or threads|
    US4698243A|1986-06-20|1987-10-06|The Dow Chemical Company|Method for sizing and hydrolyzing polytetrafluoroethylene fabrics, fibers, yarns, or threads|
    US4731263A|1986-09-26|1988-03-15|The Dow Chemical Company|Method for the preparation of ionomer films|
    US4738741A|1986-12-19|1988-04-19|The Dow Chemical Company|Method for forming an improved membrane/electrode combination having interconnected roadways of catalytically active particles|
    US4752370A|1986-12-19|1988-06-21|The Dow Chemical Company|Supported membrane/electrode structure combination wherein catalytically active particles are coated onto the membrane|
    US5039389A|1986-12-19|1991-08-13|The Dow Chemical Company|Membrane/electrode combination having interconnected roadways of catalytically active particles|
    US4889577A|1986-12-19|1989-12-26|The Dow Chemical Company|Method for making an improved supported membrane/electrode structure combination wherein catalytically active particles are coated onto the membrane|
    US4940525A|1987-05-08|1990-07-10|The Dow Chemical Company|Low equivalent weight sulfonic fluoropolymers|
    US4859745A|1987-12-22|1989-08-22|The Dow Chemical Company|Stratified fibrous fluoropolymer compositions and process for forming such fluoropolymers|
    US5013414A|1989-04-19|1991-05-07|The Dow Chemical Company|Electrode structure for an electrolytic cell and electrolytic process used therein|
    US5427658A|1993-10-21|1995-06-27|Electrosci Incorporated|Electrolytic cell and method for producing a mixed oxidant gas|
    US5716504A|1995-07-10|1998-02-10|Asahi Glass Company Ltd.|Cation exchange membrane for electrolysis and process for producing potassium hydroxide of high purity|
    US6375825B1|1999-10-28|2002-04-23|Chemical Products Corporation|Process for the production of alkaline earth hydroxide|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US481751A|US3909378A|1974-06-21|1974-06-21|Composite cation exchange membrane and use thereof in electrolysis of an alkali metal halide|
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