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    • 专利摘要:
    METHOD FOR PREPARING 1,2-DICHLORETHANE by the interaction of ethylene and chlorine at elevated temperature at atmospheric pressure or under pressure of 1.3-5.5 atm in the presence of a catalyst based on iron salt and an inhibitor — oxygen in an environment of 1,2-dichloroethane and in a medium The desired product from the reaction mass by distillation, characterized in that, with the aim of reducing the amount of by-products and the corrosivity of the medium, anhydrous alkali or alkaline earth metal tetrachloroferrate or ammonium or a mixture is used as a catalyst ferric chloride (III) and alkali or alkaline earth metal or ammonium salts with a concentration of catalyst in the used solvent, 1, 2-dichloroethane, 0.0020, 35 wt.% (based on gelochloride chloride) for (III) and the process conducted at a temperature of 40-150C.
    公开号:SU1277887A3
    申请号:SU833673517
    申请日:1983-12-06
    公开日:1986-12-15
    发明作者:Хундек Йоахим；Шольц Харальд；Хеннен Ханс
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

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    The invention relates to a method for producing 1,2-dichloroethane (DCE) one of one of the most important in organic chemistry, which is found to be 1-1 tons, for example, used as a solvent.
    The purpose of the invention is to reduce the amount of by-products and the corrosivity of the medium.
    In the preparation of I, 2-dichloroethane by the reaction of ethylene with chlorine in 1,2-dichloroethane (as solvent and reaction medium) 1,1,2-trichloroethane is formed as the main by-product.
    To suppress the substitution reaction, elements of Group IV-VI of the Periodic System, such as anhydrous iron (III) chloride, are used as a catalyst along with chlorides. The resulting impure catalyst-containing dichloroethane is usually discharged from the reaction vessel and, to remove the catalyst and the hydrogen chloride contained in the crude product, is treated with aqueous alkaline solutions and then distilled. The application of the resSC. as a catalyst for the coupling chlorination of ethylene is associated with a number of disadvantages. Thus, EeCl and the presence of water act in a corrosive manner with respect to the metallic material of the reactor, the columns and the heat exchangers, as it contacts the catalyst. Technical grade chlorine, which is used for chlorination, always contains traces of moisture, moreover, hydrogen chloride is always formed as an undesirable by-product. Since the thermal energy released during the chlorination of ethylene is to be used, the reaction should be carried out at temperatures above the boiling point of dichloroethane at atmospheric pressure. When the temperature rises, the corrosion correction significantly decreases. Therefore, the apparatus for chlorination reactions must be made of corrosion-resistant materials, which affects the efficiency of the proposed method.
    It has been established that the corrosion caused by the action of Fed as a catalytic agent upon obtaining 1, 2 br; lordtan can be substantially suppressed in a non-corrosive-resistant, 1 reactor, as well as anhydrous tetrachloroferrates as a catalyst. Compounds are preferred because the formation of by-products is reduced.
    The following compounds of ammonium tetrachloride (I) ammonium (NH PeCl tetrafchloroferrate (I) sodium (NaFeCl); potassium tetrachloroferrate (D) potassium (KFeC); bis- / tetrachloroferrate (I -) / magnesium (MpjFeCl) can be used as tetrachloroferrates.
    The preparation of catalysts can be produced by a limestone method. Anhydrous ag-gmonium tetrachloroferrate is obtained by fusing a mixture of stoichiometric amounts of ammonium chloride and anhydrous iron (III) chloride.
    The catalyst according to the proposed method is usually dissolved or suspended in a solvent loaded into the reactor (it can be prepared outside the reaction solution and introduced into the reactor). Also, anhydrous Fed and another anhydrous component, which is capable of processing, is added to the solvent loaded into the reactor. zovan1-by tetrachloroferrate.
    These catalysts are technically progressive, since they are suppressed by a significant degree of corrosion, which appears and has a negative effect on the preparation of 1,2-dichloroethane by known methods when using corrosion-resistant metal reactors.
    It has been established that with the exception of a small amount of the first A11 Substitution I, 1, 2-three: x: lorethan and hydrogen chloride under the conditions of the proposed method, it is not about any other by-products.
    The reaction solution during the long reaction time remains bright, if ammonium tetrachloride (I) is present in the reaction solution. The reaction mixture, which during the course of the reaction may become a thermo-dye, becomes light again by adding yK, 33aHHFjix compounds during the further course of the reaction.
    According to the proposed method, the degree of conversion at a high volume-time code is almost quantitative. The proposed method can be carried out, for example, in a loop reactor or in any other reactor suitable for carrying out the method. Examples 1-4. A 1-liter glass loop reactor with a capacity of about 2 liters is loaded with kg of 1,2-dichloroethane, containing 0.1-0.3 wt.% Of one of the catalysts listed in the table in dissolved form. The rising loop of the reactor loop contains a layer of filler, inside which feed lines for ethylene, chlorine and air are located, through which about 60 l / h of chlorine and ethylene and 15 l / h of air are fed into the reactor in each case. The reaction liquid in the reaction system is kept in circulation according to the principle of the mammut pump. During the reaction, the temperature of the reaction mixture is set at about 17 ° C. In water fridge
    And the concentration of catalyst in the calculation of FeCl.
    PRI me R 5. Proceed analogously to example 1, however, 2072 g of 1,2-dchloroethane, in which 1, 6 g of FeCl, is dissolved, is charged to the reactor. According to the colorimetric determination of the content of FeCl, in a solution of 0.076 wt.%. During the reaction, quantities of ethylene and chlorine introduced into the reactor in the presence of air give crude dichloroethane containing 0.18% by weight of 1,1,2-trichloroethane.
    Then 0.5 g of MgCl 2 was added to the reaction solution. In the course of further experimentation, for 4 weeks with uninterrupted production, about 265 g of crude product is obtained. Iron content in
    I
    the reaction mixture, despite the steel element embedded in the reactor, remains unchanged.
    Analysis of 1, 2-dichloroethane product A) condensed in a condenser, (a product B), the remaining liquid, the B reactor, gives the following values:
    Product A, wt.% Product B, wt.%
    From 0.002
    0.002 1.2 DCE 99.97 99.84 1,1,2-TCE 0.021 0.089 NCE ..: 0.001 Other 0.007
    0.07. PRI me R 6.
    Proceed as in Example 5, while 2155 g of 1,2-dichloroethane, in which 7.4 pre-dissolved above the reactor, is pre-dissolved, dichloroethane vapor from the reactor is condensed, then the part of the condensate corresponding to the quantity produced is drained and taken away using a condensation separator, while excess condensate is fed back to the reaction zone. With the aid of a cooling trap, another part of dichloroethane is separated from flue gases, consisting mainly of inert gases. The resulting crude dichloroethane has the composition shown in the table. The yield of crude dichloroethane is an average of 267 g / h, with the indicated amounts of gas being determined only by instruments for measuring the flow rate. Despite the steel element built into the reactor, the iron content in the reaction mixture remains unchanged. 1.7 g of iron (III) chloride. According to the colorimetric determination of iron, the Fed content in the solution is 0.083% by weight. In the course of the reaction, the amounts of ethylene and chlorine introduced into the reactor in the presence of air are given crude crude dichloroethane with a content of 1,1,2-trichloroethane O, 12 wt.%. Then, 0.6 g of NaCl is added to the reaction solution, and additional amounts of 1, 2-dichloroethane are obtained. Analysis of 1,2-di: chloroethane (product A) in the condenser gives the following values: Product A, wt.%, 002 1,2-LHE99.97 I, 1,2-TCE. 0.025., 001 Others 0.004 After the experiment, which lasted 10 days in an uninterrupted manner, 1.7 Fed and 0.6 g Nad are added to the reaction liquid so that the content of iron (III) chloride in solution is 0.164% by weight. Analysis of product A, released in a condenser, gives the following values: Product A, wt.%, 002 1,2-DCE .99.98 1, 2-TCE0.0122 HCf-0.001 Others0.004 Experience continues for 7 days with a failure ryvnoy production. Another 1.7 g of Fed and 0.6 g of Nad are added to the reaction mixture so that the content of iron (III) chloride in the solution is 0.248 wt.%. Product A, having been condensed in the condenser, the reaction liquid B has the following composition: Product A, m s.% Product B, mA with 0.002; 0.002 CjH.-Cl 1.2-DCE 99.97 99.8 1.1.2 - THC 0,018 0,068 NS G CO, 001 0,004 0,12 Other Example7. A mixture with 4341 g of 1,2-dichloroethane and 3.3 g of FeC is loaded into the apparatus with a bag with a capacity of 5 l. The colorimetrically determined content Fed is 0.076 wt.% Then a magnet-mixed solution of 1.1 Na CO is added. The mixture is loaded through a feed tube under 60 l / h of chlorine gas and 15 l / h of air through another tube with a fused glass plate — 60 l / h of ethylene. In a water reservoir (ike located above the reactor, napi, i dichloroethane is condensed out of the reactor, then a condensation separator is removed and a part of the condensate is taken out, corresponding to the amount of dichloroethane being produced, while the excess condensate is returned to the zone reactions. With the aid of a cooling trap, a further part of the condensate is separated from the off-gas, preferably consisting of inert gases. Analysis of product A, which is in the condenser, gives the following values: Product A, m p.%, 0.002 .sg, 2-LH :). 99.96, 1,2-TCE 0.031 her 0.002 Others 0.005 After a 60-hour test period, the bulk solution is diluted with 1,2-dichloroethane, so that the colorimetrically determined content of ferric (III) chloride is 0.028% by weight. After another 40 hours, analysis of product A, released in a condenser, gives the following value; Product A, May /: 0.002 99.96 1,2-DCE 0.03 1,1.2-TCE HCt 0.001 0.003 Other PRI me R 8, E steel reactor, 2-dichloroethane, pe to obtain volume which is about 25 m and which is loaded with about 20 m of dCE, about 1.0 kg of ferric chloride are dissolved. In a reactor at a pressure of 2.5 at and a temperature of 100-110 ° C, 500 n.m. ethylene and chlorine, as well as 5 Nm. of air. In the reactor, corrosion samples were placed at 4 locations, which were collected after 20 days. It turned out that in the case of non-alloyed steel, corrosion was on average 0.43 mm per year. FeC concentration. in the reaction mixture rose from 0.04 to about 0.2 wt.%. In the course of further preparation, 71X) is introduced over 90 hours 0-, 1 n, x. / h ammonia. Since 1, 2, trichloroethane and hydrogen chloride were contained in the reaction mixture due to the side reaction of DCE with chlorine, the reaction mixture formed NHC1, which in turn reacts with FeCl further to tetrachloroferrate (1) ammonium NHv (FeCl ..). Won-CH catalyst concentration of 0.25 wt.%. Thereafter, corrosion crusts are marked in the reactor, and under these conditions, corrosion is found to be less than 0.05 mm per year. To convert the resulting corrosion equipment, the FeCl apparatus was daily injected into the reaction mixture of about 50 ml of NH. The concentration of the catalyst increased to 0.35%. The crude raw EDC is removed as a vapor along with the reaction gas, condensed and purified by distillation. 11 example9. About 0.5 kg of iron (III) chloride concentration of about 0.002% by weight is dissolved in the reactor according to Example 8, filled with approximately 20 m of DCE. In addition, about 70 L of ammonia (gas) is added to this solution. At a pressure in the upper part of about 1.3 at and a temperature of about 40 ° C, the reactor is introduced hourly in K 800 Nm of ethylene and chlorine 78 and 8 Nm. of air. With the aid of the EDC formed on chlorination with DCE, hydrogen chloride is formed in the reaction mixture ammonium tetrachloroferrate (I). About 3.5 t / h of raw DCE are removed from the reactor and about 10 l / h of ammonia (gas} are injected. The required amount of FeCl is formed as a result of corrosion of the nozzles placed in the reaction zone of iron. The reaction product is sent to the bottom of the distillation column from which the 99.99% DCE product was obtained, the catalyst was removed from the bottom of the distillation column together with high-boiling by-products. Example 10. In the installation according to Example 8, about 2.5 t / h of DCE are obtained. reactor of approximately 150 ° C at a pressure of 5.5 at. Product beats l dissolved .From the reactor in the vapor state. The heat which is not used for vaporizing the reaction product, is carried out in a special heat exchanger to obtain about 1 t / h of steam can be used kotorsh m for heating purposes.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR PRODUCING 1,2-DICHLOROETHANE by the interaction of ethylene and chlorine at elevated temperature at atmospheric pressure or under a pressure of 1.3-5.5 atm in the presence of a catalyst based on an iron salt and an inhibitor - atmospheric oxygen in 1,2-dichloroethane and isolating the target product from the reaction mass by distillation, characterized in that, in order to reduce the amount of by-products and the corrosivity of the medium, anhydrous alkali or alkaline earth metal tetrachloroferrate, or ammonium or a mixture of chloride is used as a catalyst iron (III) and salts of an alkali or alkaline earth metal, or ammonium at a concentration of the catalyst in the used solvent, 1,2-dichloroethane, 0.0020.35 wt.% calculated on iron (III) chloride and the process is carried out at a temperature of 40 -150 ° C.
    SU "> 1277887 AZ
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE1042558B|1957-01-11|1958-11-06|Basf Ag|Process for the production of saturated, chlorinated hydrocarbons|
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    JP4883974B2|2005-10-03|2012-02-22|株式会社トクヤマ|Process for producing 1,2-dichloroethane|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
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