• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:

    公开号:SU878202A3
    申请号:SU752114572
    申请日:1975-03-07
    公开日:1981-10-30
    发明作者:Секо Маоми；Огава Синсаку；Есида Мунео；Емияма Акира；Такемура Рейдзи；Оно Хироси
    申请人:Асахи Касеи Когио Кабусики Кайся (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to electrochemical production, in particular to the electrolysis of a sodium chloride solution using ion-exchange membranes, and can be used in the electrolytic production of chlorine, hydrogen and caustic soda with a low content of impurities.
    There is a method of electrolysis of an aqueous solution of sodium chloride in an electrolyzer separated by a cation exchange membrane into anode and cathode spaces, while the pressures in the gas phase of the anode and the wafer are equal to fl].
    cathode sorry
    The disadvantage of this method is the relatively high voltage on the cell, which leads to increased energy consumption for electrolysis.
    The purpose of the invention is to reduce the voltage on the cell.
    This goal is achieved by the fact that in the method of electrolysis of water.
    solution of sodium chloride in the electrolyzer, separated by a cation exchange membrane into the anode and cathode spaces, the pressure in the gas phase of the cathode space is maintained at 0.2-5 m 30 water.article. higher than in the gas phase of the anode space.
    In this case, the membrane approaches the anode, and the bubbles of released chlorine do not allow the membrane to snuggle against it.
    The proposed method is illustrated in the drawing.
    The electrolysis of an aqueous solution of sodium chloride is carried out in a bipolar cell. In the electrolyzer, a cation exchange membrane 1 of a perfluorinated copolymer is used. Anode 2 consists of a 1.5 mm thick titanium sheet with stamped holes (porosity 60%) coated with a mixture of 55 mol.% Ruthenium oxide, 40 mol.% Titanium oxide and 5 mol.% Zirconium oxide. Cathode 3 consists of a perforated steel sheet with a porosity of 60% and a thickness of 1.6 mm. The anode 2 and cathode 3 are 1.2x2.4 m in size and are arranged vertically parallel to each other at a distance of 2 mm. The dividing wall 4 is made of a steel sheet 9 mm thick clad with a titanium sheet 1 mm thick. The space between the anode 2 and the titanium side 5 of the dividing wall is electrically connected by welding 878202 ki to the titanium sheet of the fins 4 mm thick, 25 mm wide and length
    1.2 m and an anode chamber 7 is formed behind the anode. The rib 6 is positioned vertically and is provided with ten MI holes with a diameter of 10 mm to improve horizontal mixing of gases or anolyte. The space between the cathode 3 and the iron side 8 of the anode is electrically connected by welding to the iron sheet. Ribs 9 are 6 mm thick, 45 mm wide and 1.2 m long, and a cathode chamber 10 is obtained in part of the space behind the cathode 45 mm wide. The rib 9 is arranged vertically and equipped with ten holes with a diameter of 10 mm to improve horizontal mixing of gases or catholyte. The periphery of the anode chamber 7 and the cathode chamber 10 is surrounded by an iron frame 11 with a thickness of 16 mm. Parts of the iron frame in contact with the anolyte. Q6-2Q is faced with a titanium sheet 2 mm thick. The iron frame 11 is provided with inlet 12 and outlet 13 nozzles of anolyte T inlet 14 and outlet 15 nozzles for catholyte. 74 such cells are collected in a filter press type electrolyzer. A packing 16 is placed on the working iron frame 11 to maintain a distance between the electrodes of 2 mm and prevent leakage.
    Catholyte and anolyte are supplied at a rate of 600 l / h to each cell. The concentration of caustic soda at the output of 5 N. The electrolysis temperature is 90 ° C, the load on the electrolyzer is 14.2 kA, the current density is 5 kA / mt. The chlorine released at the anode and hydrogen released at the cathode, for the most part, pass to the side of the electrodes opposite to the membrane.
    The difference between the pressure in the gas phase of the cathode and anode space is regulated by changing the pressure in the anolyte and catholyte collectors and measured with a mercury manometer, and the voltage on the cells of the electrolyzer is simultaneously determined.
    The measurement results are shown in the table.
    Note e. Enak + suggests that the pressure in the gas phase of the cathode space is greater than in the gas phase of the anode space.
    After disassembling the electrolyzer, no visible membrane changes were detected.
    From the data given in the table, it follows that when the pressure difference in the gas phase of the cathode and anode space is less than 0.2 m water column, the voltage across the cell increases. The increase in pressure difference above 5 : m water causes a risk of mechanical destruction of the membrane and the elements of the cell.
    When implementing the proposed method, it is desirable to acidify the anolyte with hydrochloric acid to a pH of 3.5 or lower, which provides a high current output of chlorine. At pH 2.0 £ 0.2, after 120 hours of electrolysis of chloric acid ions was not detected, and the oxygen content in the chlorine gas was 0.39%.
    Thus, the proposed method allows to reduce the voltage on the cell to 0.05-0.25 V and, thereby, reduce the cost of electricity for electrolysis.
    The pressure difference in the gas phase of the cathode and anode space, m water The voltage on the cell of the cell, In -1 4.11 0 3.7-3.9 +0.2 3.72 +1.0 3.65 +2.0 3.65 +5.0 3.65
    权利要求:
    Claims (1)
    [1]
    The invention relates to electrochemical production, in particular to the electrolysis of sodium chloride solution using ion-exchange membranes, and can be applied in the electrolytic production of chlorine, hydrogen and caustic soda with a low content of impurities. The known method of electrolysis of an aqueous solution of sodium chloride in an electrolyzer, separated by a cation-exchange membrane into the anode and cathode spaces, while the pressure in the gas phase of the anodic and cathodic space is equal to Tl. The disadvantage of this method is the relatively high voltage on the cell, which leads to increased energy consumption for electrolysis. The purpose of the invention is to reduce the voltage on the electrolyzer. This goal is achieved by the fact that in the method of electrolysis of an aqueous solution of sodium chloride in an electrolytic cell divided by an ion exchange membrane into the anode and cathode spaces, the pressure in the gas phase of the cathode space is maintained at 0.2–5 m water line. higher than in the gas phase of the anode space. In this case, the membrane approaches the anode, and the bubbles of released chlorine do not allow the membrane to closely adhere to it. The proposed method is illustrated in the drawing. The electrolysis of an aqueous solution of sodium chloride is carried out in a bipolar cell. A cation-exchange membrane 1 made from perfluorinated copolymer is used in the electrolyzer. Anode 2 consists of a 1.5 mm thick sheet of titanium with stamped holes (porosity 60%), coated with a mixture of 55 mol.% Ruthenium oxide, 40 mol.% Titanium oxide and 5 mol.% Zirconium oxide. Cathode 3 consists of a perforated steel sheet with a porosity of 60% and a thickness of 1.6 mm. The anode 2 and cathode 3 have dimensions of 1.2x2.4 m and are located vertically parallel to each other at a distance of 2 mm. The separating wall 4 is made of a steel sheet 9 mm thick, clad with a titanium sheet 1 mm thick. The space between the anode 2 and the titanium side 5 of the separation wall is electrically connected by welding to the titanium sheet rib b 4 mm thick, 25 mm wide and 1.2 m long and anode Kcwiepa 7 is formed behind the anode. Rib 6 is positioned vertically and supplied with ten tfH holes with a 10 mm di-dilet to improve horizontal mixing of gases or anlitolite. The space between the cathode 3 and the iron side 8 of the anode is electrically connected by welding to the iron sheet ribs 9 with a thickness of 6 mm, a width of 45 mm and a length of 1.2 m and receive the cathode chamber 10 in the clean space behind the cathode with a width of 45 mm. and provide ten holes with a diameter of 10 mm to improve the horizon; 1 or 6 mixing of the gases or catholyte. the periphery of the anode chamber 7 and the cathode chamber 10 is surrounded by an iron frame 11 with a thickness of 16 mm. Parts of the iron frame that are in contact with the anolyte ,. They are faced with a titanium sheet 2 mm thick. The iron frame 11 is provided with inlet 12 and outlet 13 anolyte pipes and inlet 14 and outlet 15 catholyte pipes. 74 such cells are collected in a filter press type electrolyzer. A gasket 16 is laid on the working iron frame 11 to maintain the distance between the electrodes of 2 mm and prevent leakage. Catholyte and anolyte are fed at a rate of 600 l / h to each well. The concentration of caustic soda at the outlet is 5 n. The electrolysis temperature is 90 ° C, the load on the electrolyzer is 14.2 kA, the current density is 5 kA / mt The chlorine released at the anode is chlorine and the hydrogen released at the cathode is reversed relative to membrane side of the electrodes. The difference between the pressure in the gas phase of the cathode and anode spaces is regulated by changing the pressure in the anolyte and catholyte collectors and measured with a mercury manometer, while simultaneously determining the voltage across the cells of the electrolyzer. The measurement results are shown in the table. NOTE e. The + sign indicates that the pressure in the gas phase of the cathode space is higher than in the gas phase of the anode space. After disassembling the electrolyzer, no visible membrane changes were detected. From the data given in the table, it follows that when the pressure difference in the gas phase of the cathode and anode space is less than 0.2 mW, the voltage across the electrolyzer increases. The increase in the pressure difference above the 5th water column causes the danger of mechanical destruction of the membrane and elements of the electrolyzer. In the implementation of the proposed method, it is desirable to acidify the anolyte with hydrochloric acid to a pH of 3.5 or below, which provides a high yield of chlorine current. At pH 2, OiO, 2, after 120 hours of electrolysis of chloric acid ions was not detected, and the oxygen content in chlorine gas was 0.39%. Thus, the proposed method allows to reduce the voltage on the cell of the electrolyzer to 0.05-0.25 V and, thereby, reduce the cost of electricity for electrolysis. The pressure difference in the voltage on the gas phase of the cathode cell of an electron and anode lyser, In space, m water. 3.7-3.9. Formula of the invention. A method of electrolysis of an aqueous solution of sodium chloride in an electrolytic cell divided by a cation-exchange membrane into an anode and cathode space, characterized in that in order to reduce the voltage on the electrolyzer, the pressure in the gas phase of the cathode space is maintained at 0 2-5 m water column higher than in the gas phase of the anode space. Information sources,. taken into account during the examination 1. The patent of Germany 2260771, cl. C 25 V 13/08, 12.07.73 (prototype) 1
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    同族专利:
    公开号 | 公开日
    JPS5168477A|1976-06-14|
    JPS5232865B2|1977-08-24|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE2503652A1|1974-02-04|1975-08-07|Diamond Shamrock Corp|CELL FOR CHLORAL CALCIUM ELECTROLYSIS|JPS5643116B2|1976-07-05|1981-10-09|
    JPS5927389B2|1978-02-15|1984-07-05|Asahi Chemical Ind|
    JPS5858433B2|1978-10-20|1983-12-24|Tokuyama Soda Kk|
    JPS6135277B2|1985-01-10|1986-08-12|Kanegafuchi Chemical Ind|
    JPS63101276U|1986-12-23|1988-07-01|
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    JP6499151B2|2016-12-26|2019-04-10|株式会社イープラン|Electrolytic cell|
    EP3575439A4|2017-01-26|2020-04-08|Asahi Kasei Kabushiki Kaisha|Electrolytic bath, electrolysis device, electrolysis method, and method for producing hydrogen|
    WO2018139613A1|2017-01-26|2018-08-02|旭化成株式会社|Bipolar element, bipolar electrolytic cell, and hydrogen manufacturing method|
    JP6294991B1|2017-04-14|2018-03-14|株式会社イープラン|Bipolar electrolytic cell|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP49141745A|JPS5232865B2|1974-12-10|1974-12-10|
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