• 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:
    1. A method for purifying saline acid from organic impurities, including treating the starting acid with an inert carrier gas in the column in bubbling mode and discharging the purified acid from the bottom and an inert carrier gas stream containing organic impurities from the top of the column, characterized in that In order to increase the degree of purification from C-hydrocarbons, hydrogen chloride gas emitted from the hydrochloric acid being purified is used as an inert carrier gas, and the process is carried out while boiling points, 2. The method of claim 1, wherein: the process is carried out under a pressure of 1-4 bar.
    公开号:SU1181528A3
    申请号:SU823441468
    申请日:1982-05-21
    公开日:1985-09-23
    发明作者:Штиккен Герхард
    申请人:Хемише Верке Хюльс Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for the purification of hydrochloric acid, in particular to a method for the purification of hydrochloric acid from organic impurities. The aim of the invention is to increase the degree of purification of Cj-chlorohydrocarbons. Example 1. A glass column with a diameter of 200 mm containing Raschig rings with dimensions of 25x25 mm (nozzle layer height of 3000 mm) is fed with 425 kg / h 35 weight,% hydrochloric acid at a pressure of 1 bar (abs.). The content of the impurity in the starting hydrochloric acid is 5000 mg of organic bound chlorine per liter. The impurity is C) -hlouhydrocarbons of the following composition:,; GSN.S; : CHCl,: CC1F 1: 3: 1: 0.03 (weight, h,). The initial hydrochloric acid has a temperature of 20 ° C and is fed to the upper part of the column, which operates as a brewing column. The cube is maintained at the boiling point of the acid (approximately) using a heat exchanger operating on a low pressure steam. The purified hydrochloric acid is withdrawn from the bottom of the column. It contains 20 mg of organically bound chlorine per liter. Thus, the purification rate is 99.6%. To achieve this purification degree, 1.5% hydrochloric acid fed to the column, i.e., hydrochloric gas containing C ( chlorohydrocarbons, diverted in the amount of 4.5 m / m of purified hydrochloric acid. Example 2 In a glass column with a diameter of 100 mm, containing a Raschig ring measuring 4x4 mm (height of the nozzle layer 3000 mm), 45 kg / 35 wt.% Hydrochloric acid at a pressure of 1 bar (abs.). The impurity content in the initial acid is 1200 mg o. chlorine-bound per liter. The impurity has the same characteristic as in Example 1. The starting acid, having a temperature of 20 ° C, is fed to the top of the column, working as a bubble column. The cube is maintained at the boiling point of the acid ( approximately 65 ° C) using a thermostatically controlled heat exchanger. Purified hydrochloric acid is withdrawn from a cubic column. It contains 10 mg of organically bound chlorine per liter, which corresponds to a purity level of 99.2%. of the upper portion of the column in the form of hydrogen chloride gas of about 1% hydrochloric acid fed to the column, ie, hydrochloric gas containing Cj-chlorinated hydrocarbons is withdrawn in an amount of 3.0 cleaned with hydrochloric acid. Example 3 Example 2 is repeated with the difference that the process is carried out at a pressure of 4 bar (abs) and the temperature of the bottom of the bubble column rises to about 100 ° C. The purified hydrochloric acid is removed from the bottom of the column, the residual impurity concentration 10 mg of organically bound chlorine per liter. This corresponds to a purity of 99.2%. To achieve this purity, about 1% of the hydrochloric acid fed to the column is withdrawn from the top of the column as hydrochloric acid, i. Hydrochloric gas, containing C-hydrocarbons, is removed in an amount of 0.8 hydrochloric acid to be purified. A gaseous stream containing Cj-chlorohydrocarbons, discharged at a pressure of 4 bar (abs.), Can be directly fed into the operations under a pressure of 3 bar (abs.) Absorber of the methane chlorination unit. Example 4 A glass column with a diameter of 50 mm, containing Raschig Rings with dimensions of 4x4 mm (nozzle layer height 2000 mm), is supplied with 13 kg / h 35 weight,% hydrochloric acid at a pressure of 4 bar (abs), of which the C-chlorohydrocarbons of composition specified in example 1 are dissolved at a concentration of 3000 mg of organically bound chlorine per liter. The starting hydrochloric acid having a temperature of 50 ° C is fed to the top of the column, which functions as a bubble column. The cube of the column is maintained at the boiling point of the acid (about 100 ° C) using a heat exchanger operating on thermostatically controlled oil. The purified hydrochloric acid is withdrawn from the bottom of the column. It contains 25 mg of organically bound chlorine per liter, which corresponds to a purity of 99.2%. Heating regulate
    权利要求:
    Claims (2)
    [1]
    1. A METHOD FOR CLEANING HYDROCHLORIC ACID FROM ORGANIC IMPURITIES, comprising treating the initial acid with an inert carrier gas in a column not in the bubbling mode and withdrawing purified acid from the cube and an inert carrier gas stream containing organic impurities from the top of the column, characterized in that , in order to increase the degree of purification from C ^ chlorohydrocarbons, gaseous hydrogen chloride released from the hydrochloric acid to be purified is used as an inert carrier gas, and the processing is carried out while maintaining the column in the cube Boiling Temperature.
    [2]
    2. The method according to p. ^ Characterized in that the process is carried out under a pressure of 1-4 bar.
    eo ςπ y
    QD>
    类似技术:
    公开号 | 公开日 | 专利标题
    US2540905A|1951-02-06|Recovery of chlorine
    US4470959A|1984-09-11|Continuous production of silicon tetrafluoride gas in a vertical column
    SU1181528A3|1985-09-23|Method of removing organic admixtures from hydrochloric acid
    US3597167A|1971-08-03|Removal of chlorine and organic impurities from hydrochloric acid
    JPH0741302A|1995-02-10|Method of separating hf from mixture of hf and hydrochlorofluorocarbon 123 and/or 124
    US3140244A|1964-07-07|Removal of volatile organic materials from aqueous hydrochloric acid
    SU546276A3|1977-02-05|Vinyl chloride cleaning method
    SU1447267A3|1988-12-23|Method of cleaning gases of acid admixtures
    AU709531B2|1999-09-02|Process for the purification of pentafluoroethane
    AU697583B2|1998-10-08|Process for the preparation of 1,1-difluoroethane
    EP0773915A1|1997-05-21|Purification of allyl chloride
    US4358348A|1982-11-09|Process for the preparation of pure hexafluoropropylene oxide
    KR100488229B1|2005-05-10|Process for producing difluoromethane
    RU2004136121A|2006-05-20|METHOD FOR PRODUCING TRICHLOROSILANE
    US4018880A|1977-04-19|Method of purifying hydrogen chloride gas
    JP2009539772A|2009-11-19|Separation and / or recovery of propyl bromide
    KR100281797B1|2001-02-15|Method of producing dichlorohydrin
    JP2710262B2|1998-02-10|Method for producing chlorinated methane
    US4251457A|1981-02-17|Process for purification of the off-gases resulting from the production of benzoyl chloride from phosgene
    JP2003001048A|2003-01-07|Method of drying wet gas, method of removing sulfuric acid mist, and method of producing chlorine using these methods
    EP0326054B1|1992-04-15|Process for purification of 2,2,3,3-tetrafluorooxetane
    JP3265589B2|2002-03-11|How to remove carbon disulfide
    US3076043A|1963-01-29|Method of recovering high purity chloroform and carbon tetrachloride
    US3445533A|1969-05-20|Removal of chlorine from nitrogen or hydrogen chloride by reaction with a hydrocarbon
    US4372924A|1983-02-08|Purification of alkali metal hydroxides
    同族专利:
    公开号 | 公开日
    ES8307659A1|1983-08-01|
    DD202127A5|1983-08-31|
    ES511466A0|1983-08-01|
    EP0088145B1|1986-07-09|
    EP0088145A2|1983-09-14|
    JPS58156506A|1983-09-17|
    AT20662T|1986-07-15|
    US4786488A|1988-11-22|
    DE3207887A1|1983-09-15|
    DE3271918D1|1986-08-14|
    NO821056L|1983-09-06|
    EP0088145A3|1984-03-07|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    NL280802A|1961-07-11|
    US3597167A|1968-03-29|1971-08-03|Velsicol Chemical Corp|Removal of chlorine and organic impurities from hydrochloric acid|
    DE2413043A1|1974-03-19|1975-09-25|Bayer Ag|METHOD FOR PURIFYING HYDROLINE ACID|
    US4010017A|1975-04-15|1977-03-01|Vulcan Materials Company|Recovery of hydrogen chloride from chlorinated hydrocarbons such as chloromethanes|
    JPS5436999A|1977-08-30|1979-03-19|Oki Electric Ind Co Ltd|Automatic money receiving and paying apparatus|
    US4263269A|1978-11-13|1981-04-21|The Dow Chemical Company|Removal of organic contaminants from aqueous hydrochloric acid|
    JPS5929521B2|1980-02-20|1984-07-21|Chisso Corp|AU772772B2|1999-11-08|2004-05-06|I.B.E. Co., Ltd.|Defoaming and air-water treating device|
    CN1130246C|2000-03-03|2003-12-10|北京清华紫光英力化工技术有限责任公司|Refining and recovering process for industrial by-product halogen hydride gas|
    CN100460312C|2006-09-20|2009-02-11|河北沧州大化集团有限责任公司|Method of preparing hydrochloric acid using TDI byproduct hydrogen chloride gas and its device|
    CN108218666B|2017-12-25|2021-03-26|山东东岳氟硅材料有限公司|Method and device for recovering methyl chloride from byproduct hydrochloric acid|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19823207887|DE3207887A1|1982-03-05|1982-03-05|METHOD FOR PURIFYING SALT ACIDS|
    [返回顶部]