• 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:
    An improved process is provided for the production of chlorine dioxide and chlorine wherein an alkali metal chlorate and a strong acid selected from the group sulfuric acid, hydrochloric acid, phosphoric acid, and mixtures thereof are circulated and reacted in an integral forced circulation crystallizing reaction evaporator comprising in vertical disposition:
    公开号:SU973002A3
    申请号:SU772566297
    申请日:1977-12-30
    公开日:1982-11-07
    发明作者:А.Фуллер Виллард；А.Шилт Эрл
    申请人:Хукер Кемикалз Энд Пластикс Корп.(Фирма)；
    IPC主号:
    专利说明:

    The invention relates to chemical reactor designs and can be used to produce chlorine dioxide. A known reactor for the production of chlorine dioxide, containing a vertical cylindrical body with an expanded separation section, a suction tube placed in it, and fittings for input and output of reagents Cl. The disadvantage of the known reactor is the low efficiency of the processes caused by the absence of circulation and heating of the reactants. The purpose of the invention is to intensify the process by circulating and heating the reaction agents. The goal is achieved by the fact that the reactor for chlorine dioxide production, containing a vertical cylindrical body with an expanded upper separation part, a droplet-bomber housed in it, and reagent inlet and outlet nozzles, is provided with a pipe with outlet funnel-shaped, installed coaxially inside the separation part of the body under droplet separator and connected to the fitting of the reagent inlet, the distribution element, made in the form of a funnel and located along the axis of the housing in the funnel-shaped end of the pipe, are tubular a heat exchanger disposed in the casing below the lower end of the pipe, an injection chamber located at the bottom of the housing under the heat exchanger, and a vane pump, fixed in the side wall of the pump chamber. The drawing shows the proposed reactor, a longitudinal section. The chlorine dioxide reactor contains a vertical cylindrical body 1 with an expanded upper separation part. 2, a drop separator 3 placed in it, fittings 4-7 for input and output of reagents, a pipe 8 with an output pile-like face 9 installed coaxially inside the separation part 2 of the housing 1 under the drop separator 3 and connected to the fitting 4 input of reagents, distribution element 1О, retracted in the form of a funnel and located along the axis of the housing in the funnel-shaped end 9 of the pipe 8, a tubular heat exchanger 11 placed in the housing under the lower end of the pipe 8, a pressure chamber 12 placed in the lower part of the housing under the heat exchanger 11, and. a vane pump 13 fixed in the side wall of the injection chamber 12. The pump 13 directs the flow of fluid from the inlet section 14 into the chamber 12 of the effective continuous circulation of the reaction mixture through the heat exchanger 11 to the reaction crystallization evaporation and separation part 2, into which pipe 3 and the distribution element 10 serves to direct the flow of heated reacting liquid to a level near the liquid-vapor interface, where water evaporates and chlorine and chlorine are released into separation space 15 vapor is liquid. Preferably, the upper part 9 of the pipe, 8 has the shape of a funnel, expanding upwards, and the distribution element 10 preferably has a funnel shape and is located centrally and concentrically with respect to the funnel part 9 of the pipe 8. Water, chlorine dioxide and chloroform are discharged through fitting 7 release from the separation space 15 pairs - liquid. The liquid reaction mixture flows from the interface of the steam-5-flow through the upper part of the pipe 8 and further down through the outer cylindrical section 16, the outer part 17 of the tubular elements of the heat exchanger 11 and into the section 14 of the inlet of the discharge chamber 12. The alkali metal chlorate solution is fed into the discharge chamber 12 through the inlet nozzle 5 and the pump 13 is forced to circulate and with a pen (to be used as described above. A strong acid is fed into the rising fluid flow through the nozzle 4 so that the main mixing and interaction Disconnected during the circulation of the reaction mixture to the upper part of the pipe 8. A fitting 4 of the inlet system was made (or protected) from a material resistant to strong CPS, such as Teflon. It is preferable to introduce strong acid through fitting 4 into the rising flow of liquid directly above the pipes elements of the heat exchange chamber, since the turbulent flow that occurs at the liquid outlet from the tubular elements into the reaction crystallization evaporation separation part 2 increases the rate of mixing of the reactants. As part 2 reacts to release chlorine and chlorine dioxide, a strong acid salt and an alkali metal salt is formed, and crystallizes in the evaporated liquid. Alkali metal crystals can be removed in the form of a water suspension through the outlet 6 of the exhaust system. Then the aqueous suspension is treated as described above, and the mother liquor is returned to the reaction mixture. The pump 13 may be of a mechanical type, for example, a rotor or propeller. In another embodiment, the flow of air or inert gas can be used as a pressure device either alone or in combination with a mechanical pressure device. In the preferred embodiment, the separator 3 is placed in the separation space 15 vapor-liquid in the upper part 2 in order to remove any liquid involved in the vapor flow from the vapor that is discharged through fitting 7. The drip tray 3 may be of any of the known types, for example the mesh type. It is desirable that the reaction crystallization evaporation chamber was equipped with an anti-explosion valve 18 to prevent the accidental release of gases in the event of an unexpected increase in pressure. Although the reactions in the proposed device are carried out at atmospheric pressure, it is preferable to carry them out at a reduced pressure 50 to 5OO mm Hg A vacuum device (not shown) can be any conventional device, for example, a mechanical vacuum pump, an air jet pump, a steam siphon, and so on. Heat exchanger 11 includes a heat transfer fluid inlet system 19 and an exhaust system 20 to create a heat flow fluid, for example steam, through the surrounding tubes space. In addition, it is preferable that in the space surrounding the tubes there are a plurality of horizontally arranged screens 21, adapted SH1X, in order to direct the flow of the heat transfer fluid in a horizontal direction to create maximum heat exchange efficiency. The flow of heat-transfer fluid is controlled in such a way as to provide the desired reaction temperature. To bring the reaction mixture to the desired temperature, the degree of dilution in the evaporation chamber is changed - j until the reaction solution reaches the boiling point at the desired temperature, and the teyya feed rate into the heat exchange chamber is set to such. ; to raise the reaction temperature to 10 boiling point and to ensure the evaporation of water at a rate sufficient to maintain an almost constant volume of liquid. Evaporation of water at the indicated rate causes. the formation in the reaction is a crystalline product solution in the reaction crystallized evaporation-separation part 1. The rate of energy supply to the system from all sources after the sta- tionary conditions have been reached is such that all the water added to the system and forms c in the course of the reactions occurring in this system, with the exception of crystallized water in all crystalline 25
    Salts of alkali metal and water from aqueous suspension, removed from the system, evaporated from the reaction mixture in the reaction crystallization evaporation chamber and removed from the system in the form of water vapor. The energy feed rate is related to the selected temperature,
    appropriate vacuum, the rate at which water is added to the system after steady conditions have been established, and the rate at which water is removed in the form of water of crystallization and water suspension.
    The temperature of the reaction mixture may vary considerably depending on the desired evaporation rate and operating pressure.
    Polyester resins of the above type satisfy the requirements of temperature resistance, resistance to mechanical stress and resistance to corrosion. However, such materials: corrode upon contact with alkali metal springs. Therefore, it is preferable to construct one. a forced-circulation circulating crystallizer-evaporator from combining materials, where that part of the evaporator that is in contact with the liquid reaction mixture is made of titanium, and that part of the evaporator that is in contact with the vapors of the above liquid is made from a suitable polyester resin.
    The solution works as follows. A full solution of sodium chlorate (3.2 M) sodium chloride (3.36 M) is fed to the outlet of the discharge chamber 12 through the clamp 5 of the inlet system 24 and forced to circulate upward through the inside of the 21 tubular elements of the heat exchanger 11. When the solution enters the inner part 22, through the inlet 4 of the inlet system, serves a 50% aqueous solution of sulfuric acid, which moves with the lifting solution. The pressure in the system is below 200 mmHg. Steam is passed through heat exchanger 11, through intake system 19 and exhaust system 2O at a rate and at a temperature sufficient to maintain the circulation of the reaction mixture at a temperature of about 78 ° C. The input rate of the reactants is maintained so that the reaction volume is at a constant level, higher than the top of the pipe 8 and the distribution element 1O, as the excess water added to the feed solution boils away, the output in the form of steam through the exhaust system 7 chlorine dioxide and chlorine formed in the reaction mixture. Using pump 13, the reaction mixture is circulated through the chambers of the reaction evaporator in the manner shown in the drawing. As the reaction proceeds, chlorine dioxide and chlorine are formed and removed along with the water vapor. The anhydrous sodium sulfate is crystallized from the solution and removed from the reaction mixture through the spout 6 of the discharge chamber 12.
    Although the preferred method of circulating the reaction mixture, which is necessary to achieve maximum efficiency. Moving and flowing through the interface of the liquid-vapor interface is circulated in the direction indicated by the arrows in the drawing, the direction of flow can be OPT.
    Invention Formula
    A chlorine dioxide reactor containing a vertical cylindrical body with an expanded upper separation part, a droplet separator placed in it, and an input to the output of reagents, characterized in that, in order to intensify the process by circulating and heating the reagent
    权利要求:
    Claims (1)
    [1]
    The claims
    A reactor for producing chlorine dioxide, comprising a vertical cylindrical body with an expanded upper separation part, a droplet eliminator located in it, and reagent inlet and outlet fittings, characterized in that, in order to intensify the process due to circulation and heating of the reagent, 973002
    Otov, it is equipped with a pipe with an outlet funnel-shaped end installed coaxially inside the separation part of the housing under the drop collector and connected to the reagent inlet fitting, a distributing element made in the form of a funnel and located along the axis of the housing In the funnel-shaped end of the pipe, a tubular heat exchanger, placed in box
    8 pus under the lower end of the pipe, an injection chamber, placed in the lower part of the housing under the heat exchanger, and a vane pump mounted in the side wall of the discharge chamber.
    类似技术:
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    同族专利:
    公开号 | 公开日
    NO148410B|1983-06-27|
    DE2759134C3|1981-05-27|
    AU3204477A|1979-07-05|
    NZ186064A|1979-10-25|
    NO148410C|1983-10-05|
    NO774495L|1978-07-03|
    SE7714881L|1978-07-01|
    MX149045A|1983-08-11|
    SE432583B|1984-04-09|
    JPS602242B2|1985-01-21|
    FI65977C|1984-08-10|
    FR2376066B1|1981-12-11|
    BR7708725A|1978-09-05|
    DE2759134A1|1978-07-20|
    PT67476A|1978-01-01|
    JPS5387995A|1978-08-02|
    ES465644A1|1978-09-16|
    AU513443B2|1980-12-04|
    FI65977B|1984-04-30|
    FR2376066A1|1978-07-28|
    US4079123A|1978-03-14|
    PT67476B|1979-05-28|
    FI773944A|1978-07-01|
    DE2759134B2|1980-08-07|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO2012166021A2|2011-05-31|2012-12-06|Открытое Акционерное Общество "Уральский Научно-Исследовательский Химический Институт С Опытным Заводом"|Method and apparatus for producing a solution of chlorine dioxide and chlorine in water|NL250214A|1959-04-06|
    GB1077306A|1964-08-13|1967-07-26|Electric Reduction Co|Improvements in the manufacture of chlorine dioxide|
    US3864456A|1964-08-13|1975-02-04|Electric Reduction Co|Manufacture of chlorine dioxide, chlorine and anhydrous sodium sulphate|
    US3933987A|1966-10-24|1976-01-20|Hooker Chemicals & Plastics Corporation|Simultaneous production of chlorine dioxide and a salt of a strong acid|
    US3563702A|1968-03-05|1971-02-16|Hooker Chemical Corp|Production of chlorine dioxide|
    US3816077A|1971-05-21|1974-06-11|Hooker Chemical Corp|Chlorine dioxide generating system|
    US3975506A|1973-07-05|1976-08-17|Erco Industries Limited|Production of chlorine dioxide|
    US3895100A|1973-07-05|1975-07-15|Erco Ind Ltd|Production of chlorine dioxide|
    US3976430A|1974-08-05|1976-08-24|Hooker Chemicals & Plastics Corporation|Forced circulation cooling crystallizer|
    US3974266A|1975-03-07|1976-08-10|Hooker Chemicals & Plastics Corporation|Production of chlorine dioxide|CA1223715A|1976-10-26|1987-07-07|David N. Glew|Production of chlorine dioxide|
    NZ190344A|1978-05-18|1981-02-11|Hooker Chemicals Plastics Corp|Continuous production of a mixture of chlorine dioxide, chlorine and a neutral alkali metal salt|
    CA1125989A|1978-06-28|1982-06-22|Erco Industries Limited|Modular chlorine dioxide generation systems|
    US4362707A|1981-04-23|1982-12-07|Diamond Shamrock Corporation|Preparation of chlorine dioxide with platinum group metal oxide catalysts|
    US4451444A|1981-10-21|1984-05-29|Lamb-Weston, Inc.|Method and apparatus for producing chlorine dioxide|
    CA1163420A|1982-09-09|1984-03-13|Gerald Cowley|Production of chlorine dioxide on a small scale|
    US4839152A|1988-03-25|1989-06-13|Olin Corporation|Process for producing an aqueous solution containing chlorine dioxide and chlorine|
    US4886653A|1988-03-25|1989-12-12|Olin Corporation|Process and apparatus for producing an aqueous solution containing chlorine dioxide and chlorine|
    US5770171A|1990-03-05|1998-06-23|Eka Nobel Inc.|Process for production of chlorine dioxide|
    US5858246A|1997-01-14|1999-01-12|Fountainhead Technologies, Inc.|Method of water purification with oxides of chlorine|
    US6322768B1|1998-09-29|2001-11-27|International Paper Company|Recovery of chlorine dioxide from gas streams|
    FI122623B|2009-10-30|2012-04-30|Kemira Oyj|Process for the preparation of chlorine dioxide|
    CN106219491B|2016-07-27|2018-02-27|广西博世科环保科技股份有限公司|The synthesis chlorine dioxide preparing process recycled based on heat energy and byproduct|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/755,925|US4079123A|1976-12-30|1976-12-30|Process for the production of chlorine dioxide|
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