• 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:
    1509051 Vinyl chloride HOECHST AG 7 April 1975 [6 April 1974] 14219/75 Heading C2C A process for the manufacture of vinyl chloride by pyrolysis of 1,2-dichloroethane, which comprises passing liquid 1,2-dichloroethane downwardly through a coiled pyrolysis tube having an internal diameter in the range of from 12 to 16 cm and being heated in a furnace by means of two sets of burners, one st being arranged above the other set and the upper set being supplied with from 1À7 to 2À3 times the quantity of fuel supplied to the lower set, the 1,2-dichloroethane being completely vaporized without any substantial pyrolysis thereof in a part of the pyrolysis tube above the burners which is heated substantially wholly by convection from the burners, the vapour then passing through a part of the tube heated directly by the upper and lower set of burners at which part of the vapour is further heated and pyrolysed to form a pyrolysis product from which hydrogen chloride and vinyl chloride are separated, any unreacted 1,2-dichloroethane being recovered fom the remaining pyrolysis product after reacting the remaining pyrolysis product with chlorine by an uncatalysed reaction, and the recovered 1,2-dichloroethane being recirculated through the pyrolysis tube as a liquid.
    公开号:SU736870A3
    申请号:SU752120193
    申请日:1975-04-04
    公开日:1980-05-25
    发明作者:Ридль Иозеф；Фрелих Вальтер；Миттермайер Эрих
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a process for the preparation of vinyl chloride, which is widely used as a monomer for the preparation of polymeric materials. A known method of producing vinyl chloride by splitting 1,2-dichloroethane at a temperature of 480-510 ° C in a tubular reactor with a pipe diameter of 2-8 cm, with an even supply of heat to the upper and lower rows burned by thermally splitting zones during the movement of 1,2-dichloroethane . The resulting reaction mass is rectified, the desired product is isolated, unreacted 1,2-dichloroethane, hydrogen chloride and the residue of thermal decomposition are separated. The residue is rectified with unprotected 1,2-dichloroethane, 1,2-dichloroethane is separated and returned to the START process 1, In the thermal cleavage zone, the pressure is maintained at 15-40 at. The conversion of 1,2-dichloroethane is 50-70%. At the same time, a significant amount of niobokip by-products, such as unsaturated hydrocarbons, butadiene-1, 3, is formed; 2-chlorobutadiene-1,3j 1,1-dichloroethylene, as well as up to 0.06% of aromatic hydrocarbons (benzene). A significant amount of resinous products are also formed, which causes fast clogging of the pyrolysis tubes, the need for their cleaning. The overhaul mileage of the reaction furnace will not exceed 6-8 weeks. The aim of the invention is to reduce the formation of by-products of the process. This is achieved by the proposed method of obtaining vinyl chloride, which consists in that 1,2-dichloroethane is thermally spattered at a temperature of 486-510 ° C in a tubular reactor e with an internal diameter of 12-16 cm, with a supply (heat to the upper and lower p dies of the burners of the thermal decomposition zone in the course of movement of 1,2-1 chloroethane, with the ratio of the amount of heat supplied to the upper and lower rows of the burners (1.8-2, 2): 1. The resulting reaction mass is rectified, hydrogen chloride is released, target product that has reacted 1,2-dichloro en and the residue thermal cleavage, the cleavage residue terkmcheskogo neprorragirovavshim rectified with 1,2-dichloro-
    ethane when fed to the zone of the joint rectification of chlorine.
    The distinctive features of the spraying tank are pyrolysis, and the supply of chlorine in the co-distillation of the residue of thermal cleavage and unreacted 1,2-dichloroethane,
    When carrying out the method, if honestly chlorine is supplied to the co-distillation zone, it is 20-80% by weight, based on the amount of 2-chlorobutadiene-1,3, which is contained in the product fed to the rectifier,
    Figures 1 and 2 illustrate the cleavage zones of dichloroethane;
    1 - convection zone. Zone heating: VA dichloroethane introduced into the furnace in liquid form. 2 - Evaporation zone. Dichloroethane evaporation zone, 3 - Dichloroethane vapor heating zone. 4- Splitting zone.
     It is advisable to carry out the evaporation of dichloroethane at temperatures of pipes close to the boiling point of dichloroethane in order to limit the coke emission in the corresponding zones of the furnace.
    In furnaces of known design, the evaporation zone 2 lies in the region of the upper rows of burners (see FIG. 1). In reaction furnaces (see, FIG. 2) according to the invention, the evaporation zone 2 is over- located from the region of the upper rows of burners to the colder one. The upper part of the furnace is located closer to the convection zone 1, where heat is transferred to the pipe walls only as a result of convection. This results in a 30-40% reduction in the formation of coke and degradation by-products. In addition, the supply of chlorine to the zone of joint rectification: the pyrolysis cell and unreacted 1,2-dichloroethane allowed to reduce the level of 5poroprene (2-chlorobutadiene) in recirculated dichloroethane to 1.РО-200 million without using a catalyst.
    FIG. 3 shows a scheme for the preparation of vinyl chloride.
    Dichloroethane flows1; and 1 and 2 in the decontamination zone 3 are freed from the wet azeotrope (dichloroethane) water, m.p. 7 l 6 ° С at 760 mmHg); Dry dichloroethane is fed through a Tpifi bbc 4k column 5, where it, together with the dichloroethane recycle, is freed from high-grade materials removed from the bottom of the column through line 6. Purified 1,2-dichloroethane is fed through line 7 to reactor 8, where splitting occurs. The cleavage products through the pipe 9 lead to the ring 10, where through the pipe 11
    hydrogen chloride is separated. Through conduit 12, the mixture released from hydrogen chloride is supplied to the column 13, where vinyl chloride is separated through conduit 14. Unreacted dichloroethane is taken from the bottom of the column 13 and recycled through conduit 15 to the column 5, from which it is partially separated during the splitting process. high-boiling substances — returning again for splitting; In order to better remove low-boiling substances through pipelines 15 and 16, chlorine is supplied to the inlet of the column 5, which does not detect in the distillate of the column 5 is chlorine. Due to the supply of chlorine, low boiling point substances are converted into chlorinated compounds boiling above dichloroethane and which, through conduit 6, are taken from the bottom of the column 5 along with other high boiling substances.
    Example 1, In a pyrolysis furnace {cm, FIG. 2) (the pipes of which have an internal diameter of 13.24 cm) load 1087, 8 tons of 1, 2-dichloroethane per day, of which 549.2 tons / day (50.49%) are split. The furnace has 4 p yes g; eagle. 45 100 nm day of gaseous methane are supplied to these rows of burners in a ratio,%: upper range of 27.3, average closest range of 40, average nearest range of 18, lower range of 13.8. The fuel supply in both the upper rows in relation to both the lower rows of the ladies is 2.1: 1. The pyrolysis temperature is 510 ° C. After the rapid cooling of the combustible pyrolysis in the distillation column 10, hydrogen chloride is first separated off as head products, followed by vinyl chloride in the distillation column. column 12. Obtained 346.7 tons (97.2%) of vinyl chloride per day relative to the dichloroethane used. The residue from the column contains unreacted dichloroethane. The residue is separated and fed to a distillation column for separating dichloroethane from high boilers, dosing 570 kg per day of chlorine.
    权利要求:
    Claims (2)
    [1]
    As dichloroethane is added, fresh dichloroethane is fed to the distillation column 4 along with the return unconverted dichloroethane. The head product of the column serves as raw material, pyrolKza, and has the following composition, wt.% 0.007 vinyl chloride, 0.005 ethyl chloride, 0.016 1.1 dichloroylane, 0.024. chloroprene, 0.055 1,1-dichloroethane, 0.010 carbon tetrachloride,. 0.551. benzene, 0.042 chloroform, 0.083 1,1,2-trichloroane, 99.141 1, g-dihvoretan, 0.005 tetrachloroethylene, 0.002 ethylene chlorohydrin, the rest 0.059. Without chlorine supply, the chloroprene (2-chlorobutane diene) content is set to 0.043% by weight. The addition of chlorine causes a decrease in the chloroprene content to 0.019% by weight 190. The service life of the pyrolysis furnace is four months. After this period, the furnace is turned off to remove the coke. Furnace designs with a pipe diameter of 6.25 cm have a service life of only up to two months. Example
    [2]
    2. A pyrolysis furnace with an inner diameter of pipes of 13.24 cm is loaded with 1094.5 tons of di sloretan c. per day, from which 559.3 t were split per day (51.1%). Furnace. Pyrolysis designed analog. according to FIG. 2, however, in the pyrolysis zone, it is increased by 6 pipes and a number of burners. 4 out of 5 rows of burners are supplied with 45,700 gaseous methane in the following quantitative ratios, i: upper row - not used, closest to the upper row 42.4, average row 22, Qf average row 17.8 , lower p d 17,8. The fuel supply to both upper rows with respect to both lower rows is 1.8: 1. The pyrolysis temperature is 510 s. The temperature is measured using thermocouples at a distance of 15 cm from the outlet of the burner gas. Further processing and return of unreacted dichloroethane is carried out as described in the example. 1. Get 351,7 t / day (97%) of vinyl chloride relative to the used dichloroethane. 610 kg / day of chlorine is added to the residue discharged from the bottom of the vinyl chloride stripping column. The head product of the column serves as a raw material for pyrolysis, and has the following composition, wt.%: 0.073 vinyl chloride, 0.005 Ethyl chloride, 0.011 1,1-dichloroethylene, 0.03 chloroprene, O, O76 1,1-dichloroethane, 0.003 carbon tetrachloride, 0.131 benzene, 0.019 chloroform, O., 017 1,1,2-trichporethylene, 99.567 1,2-dichloroethane 0.005 tetrachloro ethylene, 0.005 1,1,2-trichloroethane, 9 mpn ethylene chlorohydrin, 0.022 impurities. . Without chlorine supply, the chloroprene (2-chlorobutad ene) content is set to 0.046% by weight. The addition of chlorine causes a decrease in the chloroprene content to 0.012 wt.% (120 ppm). The service life of the pyrolysis furnace is 4-5 months. , After regeneration, no material change is established .: Example 3 (comparative). The same device as used in Example 1 is used. For pyrolysis, 1044.6 tons / day of ethane dyspore are loaded, of which 575.6 tons per day (55.1%) are cleaved. Rows of burner for splitting furnace load 47,300 norms. mV of gaseous methane in the following quantitative ratios,% j. the top row 25, the closest row 25, the closest row 25, the bottom row 25. The fuel supply to both the top rows in relation to the bottom row holders is 1; 1. The pyrolysis temperature is. Processing A combustible pyrolysis gas and the return of unreacted dichloroethane to the pyrolysis furnace are carried out as in Example 1. No chlorine is added to the residue from the bottom of the column to distill the vinyl chloride. The head product of the column is for separating high boiling parts that are loaded into an oven for. decomposition, has the following composition, wt.%: 0.032 vinyl chloride 0.007 chloride, ethyl, 0.015 1.1g-dichporethylene, 0.056 chloroprene, 0.055 1.1-da1xporethane, O., 004 carbon tetrachloride, 1., 090 benzene, 0.041 chloroform, 1,1,2-trichloroethyl, 98,607 1,2-dichloroethane 0.005 tetrachloroethylene, 0.005 1,1,2-trichporethane, 0.005 dichloroethyl ether. The service life of the pyrolysis furnace is 2 months 10 days. After this period, the furnace is stopped to remove the coke. The invention method of obtaining vinyl chloride by thermal decomposition of 1,2-dichloroethane at a temperature of 480-510 ° C in a tubular reactor with heat supply in the upper and lower row of the thermal splitting zone in the course of movement of 1,2-dichloroethane followed by rectification of the reaction mixture . and the release of hydrogen chloride, the desired product and. the remainder of thermal splitting, which is returned to the beginning of the process and rectification of the RU.YUT together with. unreacted 1,2-dichloroethane, which is characterized by the fact that, in order to reduce the formation of by-products of the process, thermal splitting is carried out in a tubular reactor with an inner diameter of tubes of 12–16 cm when correlating the amount of heat supplied to the upper and lower rows burners (1.8-2.2): while in the zone of joint distillation of the residue of thermal cleavage and unreacted i, 2-dichloroethane, chlorine gas is supplied. .Sources of information received in BHHMaHHis during examination 1. Patent of England No. 938824, cl. 2/3 / s, pub. 9.10.63 (prototype)
    .
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    同族专利:
    公开号 | 公开日
    DK145975A|1975-10-07|
    IT1034854B|1979-10-10|
    LU72208A1|1977-02-02|
    NO142575C|1980-09-17|
    NL7503850A|1975-10-08|
    JPS50135005A|1975-10-25|
    CH610289A5|1979-04-12|
    DE2416786B1|1975-10-16|
    GB1509051A|1978-04-26|
    SE7503891L|1975-10-07|
    FR2266680B1|1980-02-08|
    JPS598245B2|1984-02-23|
    IE41227B1|1979-11-21|
    NO142575B|1980-06-02|
    RO72435A|1981-06-26|
    DE2416786C2|1984-09-13|
    PL111015B1|1980-08-30|
    NL178681C|1986-05-01|
    SE418079B|1981-05-04|
    AT340883B|1978-01-10|
    ZA751911B|1976-03-31|
    CS189703B2|1979-04-30|
    FR2266680A1|1975-10-31|
    IE41227L|1975-10-06|
    NL178681B|1985-12-02|
    BE827635A|1975-10-07|
    NO751170L|1975-10-07|
    US4225520A|1980-09-30|
    DD119202A5|1976-04-12|
    HU178928B|1982-07-28|
    ATA256175A|1977-05-15|
    CA1050050A|1979-03-06|
    ES436166A1|1977-01-01|
    AU7984175A|1976-10-07|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    CA586326A|1959-11-03|Columbia-Southern Chemical Corporation|Process for the preparation of trichloroethylene|
    NL31269C|1930-10-08|
    US2748176A|1952-08-23|1956-05-29|Monsanto Chemicals|Purification of dichloroethane|
    NL271082A|1960-11-10|
    DE1568310A1|1966-07-23|1970-03-05|Huels Chemische Werke Ag|Process for the production of 1,2-dichloroethane|
    DE1910854C3|1969-03-04|1978-08-31|Hoechst Ag, 6000 Frankfurt|Process for the production of vinyl chloride|DE2754891C3|1977-12-09|1981-02-26|Wacker-Chemie Gmbh, 8000 Muenchen|Process for the purification of unreacted 1,2-dichloroethane from vinyl chloride production|
    DE2903640A1|1979-01-31|1980-08-14|Hoechst Ag|METHOD FOR PURIFYING 1,2-DICHLORAETHANE WHICH HAS BEEN RECOVERED TO VINYL CHLORIDE IN THE COMPLETE THERMAL CLEAVING|
    JP3804690B2|1996-03-11|2006-08-02|鹿島塩ビモノマー株式会社|Heat recovery method and heat recovery apparatus in thermal decomposition process of 1,2-dichloroethane|
    NO319656B1|2003-11-03|2005-09-05|Polymers Holding As|Process for the production of vinyl chloride|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2416786A|DE2416786C2|1974-04-06|1974-04-06|Process for the production of vinyl chloride|
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