• 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:
    A METHOD FOR CLEANING NON-PROTECTIVE DURING PYROLYSIS OF 1,2-DICHLORETHANE by chlorination with chlorine, characterized in that, in order to increase the degree of purification of 1,2-dichloroethane, cleaning is carried out at a temperature of 1550 ° C and a pressure of 1-5 atm in the presence o- or m-cresol or a mixture thereof, or a monochlorine derivative of cresol containing chlorine in the o position to the OH group, in an amount of 10-100 / weight. ppm, based on unreacted 1,2-dichloroethane, chlorination is carried out with a quantity of chlorine that provides a chlorine content in the outgoing 1,2-dichloroethane 300-600 wt. ppm followed by removal of excess chlorine by reaction with ethylene 1 phi equimolar ratio of ethylene and excess chlorine. WITH S
    公开号:SU1110379A3
    申请号:SU782694553
    申请日:1978-12-08
    公开日:1984-08-23
    发明作者:Шмидхаммер Людвиг；Фрей Хелльмут
    申请人:Вакер-Хеми,Гмбх (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for purifying unreacted 1,2-dichloroethane during the pyrolysis process, as a result of which 1,2-dichloro ethane is used to produce vinyl chloride and as a solvent. The pyrolysis of dichloroethane is carried out with the aim of creeping vinyl chloride. The dichloroethane unreacted during pyrolysis contains 2-chlorobutadiene-1,3; 1-chlorobutadiene-1,3 and a friend of admixed. A known method of purification of unreacted 1,2-dichloroztan, according to which chlorine gas is fed to the column after separation of hydrogen chloride and vinyl chloride. The disadvantages of this method are the incomplete separation of butadiene-1,3-1,3 and the flow with a noticeable chlorination rate of 1.2 -dichloroethane to form high boiling 1,1,2-trichlorozan. The closest to the invention to the technical essence and the achieved result is the method according to which 0.02-1% (200-10000 ppm) of chlorine is added to the pyrolysis products containing 1,2-dichloro ethane, and after adding chlorine the mixture remains for some time in the reactor at. The purified product contains 100 ppm of chloroprene, 600 ppm of trichloroethane and 1620 ppm of non-susceptible 1 chlorination products 2. The disadvantages of this method are insufficient purification and a significant amount of impurities after purification. In addition, as a result of the prolonged stay of chlorine in the reactor, significant equipment corrosion is possible. The aim of the invention is to increase the purity of the unreacted. 1,2-dichloroethane. This goal is achieved in that according to the purification method of 1,2-dichloroethane unreacted during pyrolysis, the purification is carried out at 15-50 ° C and a pressure of 1.5 atm by chlorinating with such an amount of chlorine that provides a chlorine content in the output of 1.2 -dichloroethane-300 600 wt. ppm in the presence of o- or m-cresol, or a mixture of them, or monochloroproduct cresol containing chlorine in the o-position to the OH group in an amount of 10-100 weight.р per non-regrouping 1,2-dichloroethane, and removing excess chlorine is carried out by reaction with ethylene, at an equimolar ratio of ethylene and excess chlorine. Cleaning is carried out as follows. The mixture containing 1,2-dichloroethane leaves the pyrolysis reactor at and dramatically creeps up to 150 ° C. Then the mixture is fed to the column, where HC1 is separated along with other gaseous components. The mixture containing dichloroethane, vinyl chloride and chlorohydrocarbons from the settling tank is fed to the next column, where vinyl chloride, methyl chloride, butadiene, vinyl acetylene and water are separated. Dichloroethane with an admixture of ethyl chloride, chlorbutadiene and 1,1,2-trichloroethane remains in the column. In order to avoid polymerization during the distillation, chlorbutadiene is chlorinated. Side reactions, in particular the chlorination of dichloroethane to 1,1,2-trichloroethane, are suppressed by additions of cresols, their chlorine derivatives, or mixtures thereof. An additional advantage of the process is that it is easy to dechlorinate the mixture with ethylene, since cresols catalyze the reaction of chlorine with ethylene. Best results are obtained when chlorine contains up to 1% by volume of oxygen. Selective chlorination of chlorobutarpenes contained in unreacted 1,2-dichloroethane is carried out in the presence of 10-100 ppm of cresol or their mixture in the reaction tube without packing or filled with packing elements. Chlorine is used, which is obtained by evaporation of liquid chlorine or electrolysis, preferably with an oxygen content of up to 1%. The dechlorination reactor is made in the form of a pipe filled with packing elements — Raishg steel rings. When working on the proposed method, reaction tubes from ordinary carbon steel are used. The use of expensive special steels unnecessarily. The invention is illustrated by examples 1, 3, 5-9. Comparative examples 2 and 4 illustrate the need to use cresols when purifying 1,2-dichloroethane in accordance with the invention. Example 1. 30 t / h of the bottom of the column exiting without the separation of 1,2-dichloro-ethane vinyl chloride containing, by weight, 1, 2, 1-1 xlichloroethane, 10% by weight ppm ethyl chloride, 1000 ppm pm i 2-chlorobutadiene 1.3 and 150 weight. ppm 1-chlorobutadiene-1,3, at 152 ° С and pressure of 5 atm with a continuous pressure of 10 wt. ppm o-cresol in the form of a solution in 1,2-dichloroethane is cooled in a refrigerator to, after which the chlorine gas obtained by evaporating liquid is passed through it in the reaction tube without a nozzle (diameter, 250 mm and 5000 mm long) at a speed of 0.843 kmol / h. chlorine. In pesjoibTETe, at the exit from the chlorination zone, the retention of isomeric chlorobutadienes in unreacted 1,2-dichloroethane is reduced to less than 1 weight. ppm At the same time, the concentration of 1,1,2-trichloroethane with an excess in the mixture of free chlorine 460 weight. The ppm rises only to 176 ppm. Immediately after leaving the chlorination zone, the unreacted 1,2-dichloroethane is directed to a 220 mm diameter pipe filled with Rashig steel rings and 3800 mm long in which stenylene is passed through it at a speed of 0.1944 kmol / h. . The conditions (temperature, pressure) of the dechlorinated treatment are not identical to the conditions of the chlorination stage. In this case, free chlorine quantitatively reacts with ethylene, resulting in the formation of 1,2-dichloroethane. The content of ethyl chloride in unreacted 1,2-dichloroethane does not increase. After dechlorinated, the content of free chlorine in unreacted 1,2-dichloroethane is only 2 wt. ppm, which corresponded to the degree of conversion of ethylene to 99.6%.
    In accordance with example 1, the following material balance occurs.
    Add:
    0.843 kmol per hour of chlorine, which is equivalent to 69.85 kg / h of chlorine;
    1500 ppm 2-chlorobutadiene at 30 tons per hour, which is equivalent to 45 kg / h, which consumes 36.10 kg / h of chlorine;
    150 pm 1-chlorobutadiene at 30 tons per hour, this is equivalent to 4.5 kg / h; consuming 7.22 kg / h of chlorine;
    176 ppm 1,1,2-trichloroethane at 30 tons per hour, this is equivalent to 5.1 kg / h.
    Thus, 13.82 kg / h of chlorine is consumed, and 0.195 kmol / h of excess chlorine remains in the reactor.
    Adding an equivalent amount of ethylene (0.1944 kmol / h) provides almost complete conversion to 1,2-dichloroethane.
    PRI me R 2 (comparative). As in the case of example 1, unreacted 1,2-dichloroethane (at a flow rate of 30 t / h) with the same initial content of impurities, but without the addition of o-cresol, passes 1,247 kmol / h of chlorine, obtained by evaporation of liquid chlorine, and 0.1944 kmol / h of ethylene under the same reaction conditions. Although in this case the excess of free juiopa in the mixture after the chlorination zone is 460 weight ppm, the content of 2-chloro utadiene in unreacted 1,2 dichloroethane is 20 weight ppm. In addition, it contains 2000 ppm of 1,1,2 trichlesratan, formed by the reaction of chlorine with 1,2-dichloroethane.
    After dechlorination, the content of 1,1,2-trichloroethane increases to 2140 ppm by weight. The unreacted 1,2-dichloroethane released from the dechlorination zone contains, in addition, 30% by weight of ethyl chloride formed by the reaction of ethylene with hydrogen chloride, 200% by weight of free chlorine and about 110% by weight. ppm of ethylene (which corresponded to the degree of conversion of ethylene
    0 40%), most of which is released in the buffer tank, operating at atomic pressure, into the gas phase and thus lost. The content of the remaining in the mixture of free chlorine is reduced due to
    5 slowly reacting it with 1,2-dichloroethane and chlorinating a residual amount of 2-chlorobutadiene-1,3 to about 100 weight. ppm, resulting in the content in unreacted 1.20-dichloroethane 1,1,2-trichloroethane in the buffer tank increases to about 2300 weight. ppm In addition, due to the presence in buffer gases of buffer capacity of free chlorine and large quantities of chloride
    5 hydrogen produced by the interaction of chlorine with 1,2-dichloroethane, problems arise due to environmental pollution and equipment corrosion. Rinse of the gas becomes necessary in the cut-out.
    0 of this capacity.
    In accordance with Example 2 (comparative), the following balance is achieved: Add:
    1,247 kmol / h of chlorine, equivalent to
    J 88,537 kg / h of chlorine;
    1500 ppm 2-chlorobutadiene at 30 tons per hour (only 1480 ppm react), consume 36.62 kg / h of chlorine;
    1994 ppm 1,1,2-trichloroethane at 30 tons per hour;
    0, this amounts to 59.82 kg / h, resulting from the consumption of 31.81 kg / h of chlorine.
    Thus, an excess amount of unreacted chlorine is 13.887 kg / h, which corresponds to 460 ppm.
    5 In this case, it was necessary to add approximately 28.7 kg / h of chlorine as compared with Example 1, with chlorine actually being used to form the valueless 1,1,2-trichloroethane.
    g In a dechlorination operation, 0.1944 kmol / h of ethylene is added. , Detected:
    140 ppm of trichloroethane at 30 tons per hour is equivalent to 4.2 kg / h of an additional amount of trichloroethane of no value, for the formation of which 2.23 kg / h of chlorine is consumed;
    110 ppm of unreacted ethylene at 30 tons per hour - this is equivalent to 3.3 kg / h, which corresponds to an ethylene conversion of 40%); 200 ppm and reprocessed chlorine at 30 tons per hour, equivalent to 6 kg / h. These data show that in order to remove the amount of chlorine that is still found in the mixture after the dechlorination operation, it is necessary to introduce into the system almost 50% excess of ethylene instead of the equivalent amount of ethylene used to remove all chlorine, as happens in accordance with the invention. Example 3. To 20 t / h of 1,2-dichloroethane, unreacted during thermal splitting it with the formation of vinyl chloride and hydrogen chloride, and containing 5 weight. ppm 1,1,2-1chloroethane, 7 wt. ppm of ethyl chloride, 1000 ppm of 2-chlorobut-diena-1, 3 and 120 ppm of 1-chlorobutadiene-1,3, as in Example 1, m-cresol is continuously added to a content of 15 ppm and cooled its up to 32 ° C. Then, through unreacted 1,2-dichloroethane, electrolysis chlorine is passed in the same reaction tube without a batch as in example I, at a rate of 0.404 kmol / h, containing about 0.6% oxygen by volume. As a result, at the exit from the chlorination zone, the content of isomeric chlorobtadienes in unreacted 1,2-dichloroethane is reduced to less than 1 ppm. The content of 1,1,2-trichloroethane (T | Re with an excess of free chlorine of 350 weight ppm) rises only to 165 weight ppm. Immediately after chlorination, unreacted 1,2-dichloroethane is sent to the same reaction tube as in the case of Example 1, in which ethylene is passed through it at a speed of 0.099 kmol / h. With this, free chlorine almost quantitatively reacts with ethylene 1, resulting in the formation of 1,2-dichloroethane, while the content of ethyl chloride remains the same. The amount of chlorinated 1,2-dichloroethane products does not increase with. The chlorination of the unreacted 1,2-dichloroethane contained only 1 ppm of free chlorine, which corresponds to the degree of ethylene conversion of 99 ,. Example 4 (comparative). As in the case of Example 3, but without the dog can of m-cresol through Henpopeai-1,2-dichloroet supplied at a rate of 20 t / h with the same content of the mixture is passed in succession to 0.565 kmol / h of electrolytic chlorine and 0.384 kmol / h of euchene. In unreconstituted 1,2-dichloroethane. after the chlorination zone, in addition to 550 ppm of free bodily chlorine, it was 900 wt. ppm of 1,1,2-trichloroethane and 40 ppm of 2-chlorobutadiene-1, 3, which remains in the mixture after the dechlorinated stage, since at this stage chlorine reacts with ethylene, which is supplied in the cootBeicTBemio pain, above stoichiometric amount. At the exit from the dechlorination zone in unreacted 2-dichloroethane, along with 5 ppm of free chlorine, contains 25 ppm of ethyl chloride, 960 ppm of ppm: 1,1,2-dichloroethane and 0.238 kmol / h of ethylene (which corresponds to an ethylene conversion of 37.6%), most of which is emitted in a buffer tank operating at and atmospheric pressure, the gas phase and thus is lost. Example 5. As in the case of example I, through unreacted 1,2-dichloroethane, supplied at a speed of 30 t / h. -f of the same composition at 20 C and a pressure of 3 atm is passed in the presence of 5 wt. o-cresol and 5 wt. ppm m-cresol successively 0.927 kmol / h of chlorine, obtained by evaporation of liquid chlorine, pa, and 0.302 kmol / h of ethylene. The following compounds are contained in the unreacted 1,2-dichloroethane leaving the dechlorination zone: 10 ppm of ethyl chloride; 1 ppm 2-chlorobut-1,3; 1 ppm of 1-chlorobutadiene-1,3; 74 ppm of 1,1,2-trichlorethylene; 1 weight. ppm free chlorine. Ethylene was not found in the mixture. : Example 6 A flow of 30 t / h of unreacted 1,2-dichloroethane containing 14 ppm 1,1,2 trichloroethane, 5 ppm ethyl chloride, 1800 ppm 2-chlorobutadiene-1, 3 and 250 ppm 1 -chlorobutadiene-1,3, which is collected at the bottom of a vinyl chloride column at a pressure of 5 atm and 152 ° C, is cooled to 15 ° C. A stream of 15 ppm of o-cresol and m-cresol (weight ratio 1: 1) is continuously added diluted with 1,2-dichloroethane. Next, dichloroethane is treated with 1046 kmol / h of chlorine vapor, as a result of which, at the exit from the chlorination zone, the amount of isomers of chlorobutadiene in unreacted 1,2-dichloroethane decreases to less than 1 ppm, whereas the concentration of 1,1,2-trichloroethane with an excess of free chlorine is 550 ppm rises only to 165 ppm. Immediately after this, the mixture is removed from the chlorination zone, unreacted 1,2-dichloroethane is fed to pipes filled with iron .- / Raschig rings, in which it is treated with 0.232 kmol / h of ethylene, as a result of which free chlorine is almost quantitatively converted into 1,2-dichloroethane, which is not accompanied by a decrease in the amount of ethyl chloride in
    权利要求:
    Claims (1)
    [1]
    METHOD FOR CLEANING OF 1,2-Dichloroethane unreacted during pyrolysis by chlorination with chlorine, characterized in that, in order to increase the degree of purification of 1,2-dichloroethane, the purification is carried out at a temperature of 1550 ° C and a pressure of 1-5 atm in the presence of o- or m-cresol, or a mixture thereof, or a monochloro-derivative of cresol containing chlorine in the o-position to the OH group, in an amount of 10-100 'weight. ppm calculated on unreacted 1,2-dichloroethane, chlorination is carried out with such a quantity of chlorine that provides a chlorine content in the resulting 1,2-dichloroethane of 300-600 weight. rrm. followed by removal of excess chlorine by reaction with ethylene at an equimolar ratio of ethylene and excess chlorine. g cl s
    类似技术:
    公开号 | 公开日 | 专利标题
    US5969195A|1999-10-19|Hydrolysis of alkyl monohalides
    KR20130062235A|2013-06-12|Process for the preparation of isocyanates
    SU1110379A3|1984-08-23|Process for purifying 1,2-dichloroethane unreacted in pyrolysis process
    US20100036180A1|2010-02-11|Method of obtaining 1,2-dichloroethane by direct chlorination with a step of separation from the catalyst by direct evaporation, and facility for the implementation thereof
    US4754088A|1988-06-28|Process for oxychlorination of ethylene
    US4851597A|1989-07-25|Process for the thermal cleavage of 1,2-dichloroethane
    Hirschkind1949|Chlorination of saturated hydrocarbons
    US3140244A|1964-07-07|Removal of volatile organic materials from aqueous hydrochloric acid
    US3065280A|1962-11-20|Production of methyl chloroform
    US4060460A|1977-11-29|Removal of chloroprenes from ethylene dichloride
    RU2010789C1|1994-04-15|Continuous method of 1,1-dichlorotetrafluoroethane synthesis
    US4018880A|1977-04-19|Method of purifying hydrogen chloride gas
    JPH0819015B2|1996-02-28|Recovery of ethylene, chlorine and hydrogen chloride from vent waste gas of direct chlorination reactor
    US5068475A|1991-11-26|Process for purifying unreacted 1,2-dichloroethane from a 1,2-dichloroethane pyrolysis process
    US4065513A|1977-12-27|Process for removing acetylene from hydrogen chloride gas
    US4028426A|1977-06-07|Removal of monochloroacetylene from chlorinated hydrocarbons
    US3998706A|1976-12-21|Process for the separation of chlorohydrocarbons from lower boiling impurities
    US4028427A|1977-06-07|Aqueous stream treatment in chlorinated hydrocarbon production
    US5198121A|1993-03-30|Drying of hydrocarbon/hydrochloric acid/water admixtures
    SU1277887A3|1986-12-15|Method of producing 1,2-dichlorethane
    CA1117984A|1982-02-09|Vapor phase chlorination of1,1-dichloroethane
    US6103945A|2000-08-15|Process for converting the low-boiling by-products formed during the thermal cracking of 1,2-dichloroethane
    KR920005051B1|1992-06-26|Process for drying hydrocarbons and its use in the preparation of chloro methanes
    KR810001007B1|1981-08-29|Process for treating unreacted 1,2-dichloroethane from 1,2-dichloroethane cracking
    JP3800683B2|2006-07-26|Method for producing chlorinated aromatic hydrocarbons
    同族专利:
    公开号 | 公开日
    DE2754891A1|1979-06-13|
    EP0002501B1|1981-08-12|
    NO150637C|1984-11-21|
    CA1112671A|1981-11-17|
    DD139839A5|1980-01-23|
    DE2754891B2|1980-05-08|
    EP0002501A1|1979-06-27|
    NO784135L|1979-06-12|
    NO150637B|1984-08-13|
    US4188347A|1980-02-12|
    GR78335B|1984-09-26|
    IN150703B|1982-11-20|
    JPS5761331B2|1982-12-23|
    JPS54117409A|1979-09-12|
    YU39853B|1985-04-30|
    BR7808028A|1979-08-07|
    DE2754891C3|1981-02-26|
    CS203024B2|1981-02-27|
    ES475831A1|1979-04-16|
    YU285778A|1982-06-30|
    MX150772A|1984-07-13|
    PT68873A|1979-01-01|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE1902843C3|1969-01-21|1974-04-25|Wacker-Chemie Gmbh, 8000 Muenchen|Process for the addition of chlorine to olefins|
    CA946416A|1969-04-09|1974-04-30|Armin Jacobowsky|Process for reducing the concentration of 2-chlorobutadiene , carbon tetrachloride and benzene in 1,2-dichloroethane recovered in the incomplete thermal cracking into vinyl chloride|
    BE746270A|1970-02-20|1970-08-20|Solvay|PROCESS FOR THE TREATMENT OF THE GASEOUS PRODUCT FROM THE PYROLYSIS OF 1,2-DICHLORETHANE AND VINYL CHLORIDE,|
    BE787606A|1971-08-18|1973-02-16|Knapsack Ag|PROCESS FOR PREPARING 3,4-DICHLOROBUTENE-1|
    US3898294A|1972-11-06|1975-08-05|Petro Tex Chem Corp|Chloroprene process improvement|
    IT1007120B|1973-02-15|1976-10-30|Basf Ag|PROCESS FOR THE PREPARATION OF VINYLCHLORIDE|
    DE2416786C2|1974-04-06|1984-09-13|Hoechst Ag, 6230 Frankfurt|Process for the production of vinyl chloride|
    US4060460A|1975-05-22|1977-11-29|Allied Chemical Corporation|Removal of chloroprenes from ethylene dichloride|
    US4125564A|1977-11-02|1978-11-14|Denki Kagaku Kogyo Kabushiki Kaisha, Chuo-Kenkyusho|Process for producing chloroprene|DE3441045A1|1984-11-09|1986-05-15|Wacker-Chemie GmbH, 8000 München|METHOD FOR TREATING 1.2-DICHLORETHANE FOR PYROLYSIS|
    JP2716520B2|1989-04-28|1998-02-18|三井東圧化学株式会社|1.2 Method for removing chloroprene from dichloroethane|
    DE4012538A1|1990-04-19|1991-10-24|Wacker Chemie Gmbh|METHOD FOR PURIFYING UNreacted 1,2-DICHLORETHANE FROM A 1,2-DICHLORETHANE PYROLYSIS PROCESS|
    NO319656B1|2003-11-03|2005-09-05|Polymers Holding As|Process for the production of vinyl chloride|
    DE102012021236A1|2012-10-27|2014-04-30|Daimler Ag|Device for isolating small particles, has slider unit that moves coordinated slider in defined distance from edge of support surface such that small particles are provided in proper orientation at center of gravity of support surface|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2754891A|DE2754891C3|1977-12-09|1977-12-09|Process for the purification of unreacted 1,2-dichloroethane from vinyl chloride production|
    [返回顶部]