Method for producing vinyl chloride from ethane and ethylene (variants)

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer from ethane and ethylene. Method involves generating the outlet flow from reactor by catalytic interaction in common of ethane, ethylene, oxygen and at least one chlorine source taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At the indicated stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst doesn't comprise iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more rare-earth material but not cerium. Indicated outlet flow from reactor is cooled and condensed to form flow of crude product comprising the first part of hydrogen chloride and flow of crude cooled hydrogen chloride comprising the second part of indicated hydrogen chloride. Then method involves separation of indicated flow of crude product for vinyl chloride monomer as the flow product and flow of light fractions comprising the indicated first part of indicated hydrogen chloride. Then indicated flow of light fractions is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at indicated generating stage. Also, invention proposes variants of a method for producing vinyl chloride from ethane and ethylene. Invention provides preparing vinyl (chloride) from ethane and ethylene by the complete extraction of hydrogen chloride from the reactor outlet flow.

EFFECT: improved producing method.

40, 9 tbl, 3 dwg, 31 ex

 

The present invention is directed to a device and method for the production of vinyl chloride monomer (VCM) of ethane and ethylene. In particular, the present invention is directed to methods of production of vinyl chloride monomer, where (1) in the input streams into the appropriate reactor contains significant amounts of both ethane and ethylene, (2) hydrogen chloride in the stream exiting the reactor, only partially extracted from the output stream when the first node after the stage or stages of reaction conversion of ethane/ethylene vinyl and (3) the portion of the remainder of the hydrogen chloride is recycled to the reactor in the flow of gas being recycled.

The vinyl chloride is the most important material in modern trade, and most of the methods used at the present time, a vinyl chloride from 1,2-dichloroethane (EDC), where EDC is first derived from ethylene; thus, according to known literature data, the system is used only at least three operations (obtaining ethylene from primary hydrocarbons, mainly by thermal cracking; the conversion of ethylene to EDC, and then the conversion of EDC to VCM). Industry inherent long-term need to move to such decisions, in which the vinyl chloride is obtained from the primary hydrocarbon in a more direct way and more economically, without the need and in pre-production and purification of ethylene, and inherent in this approach, the economic benefit stimulated a significant number of developments.

As the first General areas for development the production of vinyl ethane is of interest for a number of firms involved in the production of vinyl chloride, and is currently available is a significant amount of literature on this topic. The following sections give an overview of the main works related to the embodiments presented in new developments under this description.

Patent UK 1039369, entitled "CATALYTIC CONVERSION OF ETHANE TO VINYL CHLORIDE", which issued on August 17, 1966, describes the use of polyvalent metals, including metals from the series of lanthanides, in the production of vinyl chloride from ethane. This patent describes the use of certain catalysts, provided that "pairs available chlorine and oxygen are used in specific controlled relationship. The described system operates at temperatures in the range between 500 and 750°C. Available chlorine in the described technologies optionally includes 1,2-dichloroethane. However, this patent does not mention that together with ethane need to make ethylene. It also does not mention that in the process must be set to a specific molar ratio of ethane to ethylene, does not describe the recycling of ethylene, and instead indicated that ethyl is n reacts with the formation of polymers or ethylene dichloride, or ethylchloride.

Patent UK 1492945, entitled "PROCESS FOR PRODUCING VINYL CHLORIDE", which issued on November 23, 1977 in the name of John Lynn Barclay, describes a method for the production of vinyl chloride with the use of lanthanum in the catalyst for the conversion of ethane to vinyl on the basis of copper. As the authors describe, lanthanum is present to the favorable changes in the volatility of copper at elevated temperatures, need to work. The examples demonstrate the advantages of an excess of hydrogen chloride in an appropriate reaction.

Patent UK 2095242, entitled "PREPARATION OF MONOCHLORO-OLEFINS BY OXYCHLORINATION OF ALKANES", which issued on September 29, 1982 in the name of David Roger Pyke and Robert Reid, describes how to obtain monochloropropane olefins, which comprises bringing into interaction at elevated temperature gaseous mixture containing alkane, a source of chlorine and molecular oxygen, in the presence of a catalyst containing metallic silver and/or its connection, and one or more compounds of manganese, cobalt or Nickel. As the authors state, the catalyst can be fed a mixture of ethane and ethylene. No examples are not given, and the specific advantages of mixtures of ethane/ethylene are not described.

Patent UK 2101596 entitled "OXYCHLORINATION OF ALKANES TO MONOCHLORINATED OLEFINS", which issued on January 19, 1983 in the name of Robert Reid and David Pyke, describes ways is to produce monochloramine olefins, which includes bringing in the interaction at a high temperature gaseous mixture containing alkane, a source of chlorine and molecular oxygen, in the presence of a catalyst containing compounds of copper, manganese and titanium, and is suitable for use in the production of vinyl chloride from ethane. In addition, as the authors describe, the reaction products, in one of the embodiments, the isolated and used as is, or in one of the embodiments, recyclart in the reactor to increase the output monochloropropane of olefin. As the authors state, the catalyst can pogatsa mixture of ethane and ethylene. No examples are not given, and the specific advantages of mixtures of ethane/ethylene are not described.

U.S. patent 3629354 entitled "HALOGENATED HYDROCARBONS", which issued on December 21, 1971 in the name of William Q. Beard, Jr. describes a method for the production of vinyl chloride and joint production of ethylene from ethane in the presence of hydrogen chloride and oxygen. The preferred catalyst is copper or iron on the substrate. One of the examples in this patent shows an excess of hydrogen chloride (HCl) relative to ethane in the reaction mixture. The ratio of ethane to chlorine hydrogen one to four is used to obtain a stream containing 38.4% of ethylene (which does not require HCl to obtain) and 27.9% of vinyl chloride (which requires to acquire the Oia only 1 mol HCl 1 mol of vinyl chloride).

U.S. patent 3658933, entitled "ETHYLENE FROM ETHANE, HALOGEN AND HYDROGEN HALIDE THROUGH FLUIDIZED CATALYST", which issued on April 25, 1972 in the name of William Q. Beard, Jr., describes the method of production of vinylchloride in the system of the three reactors, uniting the reactor for oxidisation, the reactor for oxyhalogenation and reactor for dehydrohalogenation. The authors show that (hydroxy)halogenation ethane, in some cases, amplified by adding a halogen and hydrogen halide. As in the U.S. patent 3629354 obtained ethylene gives VCM by conventional oxyhalogenation (oxychlorination process) and cracking. HCl produced during the cracking operation, is returned to the reactor halogenation.

U.S. patent 3658934, entitled "ETHYLENE FROM ETHANE AND HALOGEN THROUGH FLUIDIZED RARE EARTH CATALYST", which issued on April 25, 1972 in the name of William Q. Beard, Jr., and U.S. patent 3702311 entitled "HALODEHYDROGENATION CATALYST", which issued November 7, 1972 in the name of William Q. Beard, Jr., describe both methods for the production of vinylchloride in the system of the three reactors, uniting the reactor halogenation, the reactor oxyhalogenation and the reactor dehydrohalogenation. The authors describe halogenation ethane with obtaining ethylene for subsequent transformation into EDC by oxyhalogenation (oxychlorination process) with the subsequent receipt of VCM by conventional thermal cracking. HCl, produces the range of operation of the cracking, return to the reactor oxyhalogenation in '934 and the reactor halogenation in the '311. As shown in the latter patent, the advantages of excess chlorine in the form of HCl and Cl2increases the yield of desired products.

U.S. patent 3644561 entitled "OXYDEHYDROGENATION OF ETHANE", which issued on February 22, 1972 in the name of William Q. Beard, Jr., and U.S. patent 3769362 entitled "OXYDEHYDROGENATION OF ETHANE", which issued on October 30, 1973 in the name of William Q. Beard, Jr., closely connected with the above patents describe methods of oxidisation of ethane to ethylene in the presence of excess amounts of hydrogen halide. The patent describes a catalyst from a halide or copper, or iron, optionally stabilized with rare earth halide element, where the ratio of the halide of rare earth element to the halide of copper or iron is higher than 1:1. The patent describes the use of a significant excess of HCl relative to the molar amount of ethane, HCl and is not consumed in the reaction.

U.S. patent 4046823, entitled "PROCESS FOR PRODUCING 1,2-DICHLOROETHANE", issued September 6, 1977 in the name Ronnie D. Gordon and Charles M. Starks, describes a method for the production of EDC, where the ethane and chlorine react in the gas phase over a catalyst containing copper.

U.S. patent 4100211, entitled "PROCESS FOR PREPARATION OF ETHYLENE AND VINYL CHLORIDE FROM ETHANE, which you is an 11 July 1978 in the name of Angelo Joseph's magistro, describes the regeneration of a catalyst based on iron for a method where the ethane is converted as in ethylene and VCM in the mixture. This patent describes that the source of chlorine is present in an amount of from 0.1 to 10 mol per 1 mol of ethane. As a rule, with increasing ratio of hydrogen chloride to ethane yield of vinyl chloride and other chlorinated products also increased, even when the reduction of yield of ethylene.

U.S. patent 4300005, entitled "PREPARATION OF VINYL CHLORIDE", issued November 10, 1981 in the name of Tao, R. Li, provides a catalyst based on copper for the production of VCM in the presence of excess HCl.

U.S. patent 5097083, entitled "PROCESS FOR THE CHLORINATION OF ETHANE", which issued on March 17, 1992 in the name of John E. Stauffer, describes chloropeta as a source of chlorine for the conversion of ethane to VCM. This patent describes the ways in which the chlorohydrocarbons can be used to capture HCl for later use in obtaining vinyl.

EVC Corporation is very active in the field of the technologies of converting ethane to vinyl, and the following four patents are a consequence of their development efforts.

European patent EP 667845 entitled "OXYCHLORINATION CATALYST", which issued on January 14, 1998 in the name of Ray Hardman and lan Michael Clegg, describes a catalyst based on copper with a stabilizing package designed for the catalysis of Pribram is of ethane to vinyl. This catalyst, obviously, applies to the subsequent technology, described in the following three U.S. patents.

U.S. patent 5663465, entitled "BY-PRODUCT RECYCLING IN OXYCHLORINATION PROCESS", issued September 2, 1997 in the name of Ian Michael Clegg and Ray Hardman, describes a method of catalytic conversion of ethane to VCM, which combine the ethane and chlorine source in the reactor for the oxychlorination process with an appropriate catalyst; recyclery by-products in the reactor for the oxychlorination process; process the by-products of unsaturated chlorinated hydrocarbons on stage hydrogenation to convert them to their saturated analogs and send them back to the reactor; glorious by - product of ethylene to 1,2-dichloroethane for recycling.

U.S. patent 5728905, entitled "VINYL CHLORIDE PRODUCTION PROCESS", issued March 17, 1998 in the name of Ian Michael Clegg and Ray Hardman, describes the production of vinyl from ethane in the presence of excess HCl using a catalyst based on copper. This patent describes a method for the catalytic oxychlorination process ethane in the presence of ethane, oxygen source and a source of chlorine, in the presence of a catalyst containing copper and alkali metal. HCl fed into the reactor for the oxychlorination process in excess relative to the stoichiometric requirements based on chlorine.

U.S. patent 5763710 entitled "OXYCHLORINATION PROCESS", which issued on 9 June 1998 on the two Ian Michael Clegg and Ray Hardman, discusses the catalytic oxychloination ethane to VCM by combining ethane and chlorine source in the reactor for the oxychlorination process in the presence of the catalyst for oxychlorination process (reaction conditions are selected to maintain an excess of HCl); Department of VCM products and recycling of by-products in the reactor.

Turning now to the field of production of vinyl chloride from ethylene, in most commercial methods for the production of VCM using ethylene and chlorine as a key source of nutrients. Ethylene is brought into contact with chlorine in the liquid 1,2-dichloroethane containing the catalyst in the reactor direct chlorination. 1,2-Dichloroethane are then subjected to cracking at elevated temperatures with getting VCM and hydrogen chloride (HCl). Get HCl, in turn, is introduced into the reactor for the oxychlorination process, where it interacts with ethylene and oxygen to obtain additional quantities of 1,2-dichloroethane. This 1,2-dichloroethane also served on thermal cracking with the aim of obtaining VCM. This method is described in U.S. patent 5210358, entitled "CATALYST COMPOSITION AND PROCESS FOR THE PREPARATION OF ETHYLENE FROM ETHANE, which issued may 11, 1993 in the name of Angelo J.'s magistro.

Three separate process (direct chlorination process, oxychlorination process, and thermal cracking) in most of the currently used commercial methods are often referred to in combination as "sblanc the line" for EDC, although additional sources of chlorine (HCl), in one of the embodiments, also included in these advanced systems. The overall stoichiometry "balanced" setup is as follows:

4C2H4+2Cl2+O2->4C2H3Cl+2H2About

The cost of ethylene represents a significant share of the total value of production of VCM and requires significant production costs. Ethane is less expensive than ethylene and VCM production of ethane should, therefore, significantly reduce the cost of production of VCM in comparison with the cost of production of VCM, when it is produced primarily from purified and dedicated ethylene.

Commonly called the conversion of ethylene, oxygen and hydrogen chloride in 1,2-dichloroethane oxychloination. Catalysts for the production of 1,2-dichloroethane by oxychlorination process of ethylene have many common to all such catalysts characteristics. Catalysts capable of this chemical reaction are classified as modified catalysts of the deacon (Deacon) [Olah, G. A., Molnar, A., Hydrocarbon Chemistry, John Wiley & Sons (New York, 1995), p. 226]. The chemical mechanism of the process of the deacon comes to the reaction of deacon - oxidation of HCl with obtaining elemental chlorine and water. Other authors proposed that this oxychloination applied with a view to use HCl is La chlorination and HCl to oxidative turned into Cl 2through a process of deacon [Selective Oxychlorination hydrocarbons: A Critical Analysis, Catalytica Associates, Inc., Study 4164A, October 1982, page 1]. Thus, the catalysts for the oxychlorination process defined by their ability to produce free chlorine (Cl2). In fact, process, oxychlorination process alkanes associated with the production of free chlorine in the system [Selective Oxychlorination hydrocarbons: A Critical Analysis, Catalytical Associates, Inc., Study 4164A, October 1982, page 21, and references therein]. These catalysts are used, the metals on the carrier capable of receiving more than one stable oxidation state, such as copper and iron. In the conventional technology oxychloination is an oxidative addition of two atoms of chlorine to ethylene from HCl or other source of the recovered chlorine.

Production of vinyl ethane can be done by oxychlorination process with the proviso that there are catalysts that are capable of producing free chlorine. Such catalysts will convert ethylene into 1,2-dichloroethane at low temperatures. At higher temperatures 1,2-dichloroethane will be subjected to thermal cracking with getting hydrochloric acid and vinyl chloride. Catalysts for oxychlorination process hairout olefinic substances to chloropeta with a higher degree of chlorination. Thus, just as the ethylene is converted to 1,2-dichloroethane, vinyl chloride is converted to 1,2-trichloroethane. Processes using catalysts for oxychlorination process inherent in the formation of by-products with a higher degree of chlorination. This is explored in great detail in the patents company EVC (European patent EP 667845, U.S. patent 5663465, U.S. patent 5728905 and U.S. patent 5763710), in which it is shown, that are produced when using the catalyst for oxychlorination process high levels repeatedly chlorinated by-products. Considering the above, we can conclude that many of the concepts concerning the use of ethane for the production of VCM, were clearly described previously. Used catalysts are often modified catalysts of the deacon, operating at temperatures significantly higher (>400° (C)than those required for the implementation of the ethylene oxychlorination process (<275°). The catalysts used for the production of VCM from ethane, often stabilized against migration of transition metals of the first row, as described and reviewed in the United Kingdom patent 1492945; patent UK 2101596; U.S. patent 3644561; U.S. patent 4300005 and U.S. patent 5728905.

Using chloropeta as sources of chlorine in the way of the conversion of ethane to VCM described in the patent UK 1039369; patent UK 2101596; U.S. patent 5097083; U.S. patent 5663465 and U.S. patent 5763710. The large patent is of ritani 1039369 requires to the reactor system was introduced water. In the United Kingdom patent 2101596 use of specific catalysts based on copper. U.S. patent 5663465 describes a method that uses the phase of direct chlorination for the conversion of ethylene to EDC before its introduction into the reactor VCM.

The source of the prior art EP 0162457 describes a method of producing vinyl chloride by dehydrochlorination of ethylene dichloride (EDC->Ministry of amelioration+HCl). This source refers to a different process, different from the claimed here chemical process "oxidehydrogenation".

New approaches to methods of manufacture of vinyl chloride would consist in the development and use of catalysts suitable for the conversion of significant amounts of ethane and ethylene in the monomer vinyl chloride. However, among the reaction products formed hydrogen chloride. In this regard, the management of flows of hydrogen chloride (and related hydrochloric acid) in the process is a major task that must be solved when using the system catalysts, able to turn as ethane and ethylene in the monomer vinyl chloride. When constructing a plant for producing vinyl chloride there is also a need to give the opportunity to the maximum extent possible to use the previously used equipment,despite the fact that some existing equipment may have the opportunity to work with hydrogen chloride, and the other part of the available equipment does not have the ability to work with hydrogen chloride. The present invention provides embodiments to meet these needs due to the fact that offers the device and how to work with hydrogen chloride produced by the reactor for the production of vinyl from the ethane/ethylene, by almost completely removed from the output stream of the reactor in the process of the first node following stage or stages of the reaction of obtaining vinyl ethane/ethylene.

The present invention provides a method for the production of vinyl chloride using the following stages:

generating the output stream from the first reactor through catalytic interaction together ethane, ethylene, oxygen and at least one source of chlorine from among hydrogen chloride, chlorine or a busy chloropetalum, where the molar ratio of ethane to ethylene is in the range from 0.02 to 50;

cooling and condensation of the output stream from the first reactor to generate a crude product stream containing the first part of the hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the hydrogen chloride;

split stream of raw product stream, a product of vinyl chloride monomer and the flow of light fractions provided the first part of the hydrogen chloride, and

recycling flow of light fractions to catalytic interaction together with ethane, ethylene, oxygen and a source of chlorine being generated.

The present invention also provides a method for the production of vinyl chloride, comprising the following stages:

generating the output stream from the first reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or a busy chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the first reactor to generate a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product stream, a product of vinyl chloride monomer and the flow of light fractions containing the specified first part of the hydrogen chloride, and

recycling the specified stream of light fractions to catalytic interaction together with the specified ethane, specified ethylene specified by the oxygen and the specified source of chlorine being generated.

the Present invention additionally provides a method for the production of vinyl chloride, includes the following stages:

generating the output stream from the first reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or a busy chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the first reactor to generate a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow of water and flow of product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified chilled raw stream of hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent hydrogen chloride and

recycling the specified stream of light fractions indicated in the p reactor.

The present invention further provides a method for the production of vinyl chloride, comprising the following stages:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and/ at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor to generate a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent hydrogen chloride;

the division specified stream of light fractions in the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

absorption and recycling in the specified reactor stream S2 from the specified purge flow and

recycling specified being recycled gas flow in the specified reactor.

The present invention further provides a method for the production of vinyl chloride, comprising the stage of:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor for the formation of a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-,2-dichloroethylene and TRANS-1,2-dichlorethylene, the stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent - hydrogen chloride;

split the specified stream of light fractions in the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

hydrogenation of the specified mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene with education being recycled flow to enter into the specified reactor;

absorption and recycling in the specified reactor stream S2 from the specified purge flow and

recycling the specified stream being recycled gas in the specified reactor.

The present invention further provides a device for the production of vinyl chloride, containing

a reactor for generating the output stream from the reactor through catalytic interaction compatible with the local ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

means for cooling and condensing the specified output stream from the reactor, for the formation of a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

means for dividing the specified stream of raw product stream, a product of vinyl chloride monomer and the flow of light fractions containing the specified first part of the said hydrogen chloride, and

means for recycling the specified stream of light fractions in the specified reactor.

The present invention further provides a device for the production of vinyl chloride, including

a reactor for generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

means for cooling and condensing the specified output the second stream from the reactor for the formation of the stream of raw product, contains the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

means for dividing the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the first part of the said hydrogen chloride;

means for extracting a stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

means for recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent hydrogen chloride and

means for recycling the specified stream of light fractions in the specified reactor.

The present invention further provides a device for the production of vinyl chloride, containing

a reactor for generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0,to 50;

means for cooling and condensing the specified output stream from the reactor for the formation of a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

means for dividing the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

means for extracting a stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

means for recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent - hydrogen chloride;

means for dividing the specified stream of light fractions in the purge stream and the stream is being recycled gas;

means for absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

means for combining the specified water flow of hydrogen chloride with the specified stream raw chilled chloride is th hydrogen;

means for absorption and recycling in the specified reactor stream S2 from the specified purge flow and

means for recycling the specified stream being recycled gas in the specified reactor.

The present invention further provides a device for the production of vinyl chloride, containing

a reactor for generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

means for cooling and condensing the specified output stream from the reactor, for the formation of a crude product stream containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

means for dividing the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

tools to extract the deposits of a stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

means for recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent - hydrogen chloride;

means for dividing the specified stream of light fractions in the purge stream and the stream is being recycled gas;

means for absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

means for combining the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

means for hydrogenation specified mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene to create a being recycled feed stream into the specified reactor;

means for absorption and recycling in the specified reactor stream S2 from the specified purge flow and

means for recycling the specified stream being recycled gas in the specified reactor.

The present invention further provides a vinyl chloride produced using a method comprising the following stages:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where mol is the amount specified ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product stream, a product of vinyl chloride monomer and a stream of light fractions containing the specified first part of the said hydrogen chloride, and

recycling the specified stream of light fractions to catalytic interaction together with the specified ethane, specified ethylene specified by the oxygen and the specified source of chlorine at this stage of generation.

The present invention further provides a vinyl chloride produced using a method comprising the following stages:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the specified x is aristovo hydrogen, and flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent hydrogen chloride and

recycling the specified stream of light fractions in the specified reactor.

The present invention further provides a vinyl chloride produced using a method comprising steps:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor formed with the eating of the stream of raw product, contains the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent - hydrogen chloride;

split the specified stream of light fractions in the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

absorption and recycling in the specified reactor stream S2 from the specified purge flow and

recycling specified being recycled gas flow in the specified reactor.

On toadie the invention further provides a vinyl chloride, produced using a method comprising the following stages:

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the said hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the said hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the said hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor in the form specified reagent hydrogen chloride;

split the specified stream light FR the capabilities of on the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

hydrogenation of the specified mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene to create stream being recycled to the specified reactor;

absorption and recycling in the specified reactor stream S2 from the specified purge flow and

recycling the specified stream being recycled gas in the specified reactor.

Additional features and advantages of the present invention become more apparent when reading the detailed description of the preferred embodiments and the accompanying drawings.

Figure 1 shows a schematic description, to the maximum possible extent that it can be represented on the basis of earlier publications, the proposed method of conversion of ethane to vinyl chloride using a catalyst capable of converting ethane to VCM.

Figure 2 shows how the conversion of ethane/ethylene to vinyl chloride using a catalyst capable of converting ethane and ethylene to VCM by oxidehydrogenation.

Figure 3 shows a modified process oxidehydrogenation according to the SNO 2, where demonstrated additional hydrogenation flows CIS-dichloroethylene and TRANS-dichlorethylene to 1,2-dichloroethane.

As noted in the discussion section of the BACKGROUND of the present description process, oxychlorination process is usually considered as oxidative addition of two atoms of chlorine to ethylene from HCl or other source of the recovered chlorine. Catalysts capable of implementing this chemical process, are classified as modified catalysts of deacon [Olah, G. A., Molnar, A., Hydrocarbon Chemistry, John Wiley & Sons (New York, 1995), p. 226]. The chemical mechanism of the process of deacon associated with the deacon reaction is the oxidation of HCl with obtaining elemental chlorine and water.

In contrast to oxychloination in the preferred method described here, it is preferable to use oxidehydrogenation when prevrawenie acanadarhh and atlantageorgia flow in the VCM with high selectivity. Oxidehydrogenation represents the conversion of the hydrocarbon with oxygen and a source of chlorine, chlorinated hydrocarbons, where the carbon atoms or retain their original valence or valency is reduced (i.e. sp3the carbon atoms remain sp3or converted to sp2a sp2the carbon atoms remain sp2or converted to sp). This differs from the usual on the determining the oxychlorination process, where ethylene is converted to 1,2-dichloroethane, using oxygen and a source of chlorine, with a General increase in the valency of carbon atoms (i.e. sp2the carbon atoms are converted to sp3carbon atoms). When the ability of the catalyst to prevrawenie ethylene in the vinyl chloride is advantageous to recycle the ethylene produced in the reaction of oxidehydrogenation, back into the reactor. By-products produced in the reactor oxidehydrogenation include ethylchloride, 1,2-dichloroethane, CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene. Catalyst oxidehydrogenation is also an active catalyst for the elimination of HCl from saturated chlorohydrocarbons. Recycling ethylchloride and 1,2-dichloroethane in some cases, the benefit is used in the production of vinyl chloride.

Other significant chlorinated organic by-products are dichlorethylene. These substances, in one of the embodiments, hydronauts obtaining 1,2-dichloroethane. 1,2-Dichloroethane (EDC) is a chemical produced in large quantities, and either sold or recycled. In an alternative embodiment EDC fully hydronaut obtaining ethane and HCl. Hydrogenation under conditions of intermediate stringency gives a mixture of 1,2-dichloroethane, ethane, ethylchloride and HCl; such mixtures are also is suitable for recycling to the reactor oxidehydrogenation.

Let us now turn to figure 1. In relation to the conversion of ethane to vinyl, to the extent that it may best be understood from the earlier publications, the method 100 of the conversion of ethane to VCM shows a scheme of the proposed method of conversion of ethane to vinyl chloride using a catalyst capable of prevrawenie ethane to VCM; in this regard, the method does not involve input of significant amounts of ethylene or of recyclorama threads, any of the input streams into the reactor for the conversion of ethane to VCM (Ethane Reactor 102). It should also be noted that, because the system of production of vinyl ethane in the corresponding normal scale production, to the authors ' knowledge, not yet constructed, the proposed solution for the method are the only sources for the development of incarnations that were previously formulated in the form of concepts. In this regard, the method 100 represents a unified and simplified approach to methods, jointly reviewed in several publications related to research and development EVC Corporation: Vinyl Chloride/Ethylene Bichloride 94/95-5 (August, 1996; Chemical Systems, Inc.; Tarrytown, New York); European patent EP 667845; U.S. patent 5663465; U.S. patent 5728905 and U.S. patent 5763710.

When considering the details presented on figure 1, you can see that Ethane Reactor 102 provides an output fluid flow in the Column is Alenia 106, where HCl is extinguished in the output stream from the reactor. Column Blanking 106 directs the flow of highly concentrated aqueous solution of the crude HCl in the Phase Separation Subsystem 108. The Phase Separation subsystem 108 provides an output fluid flow in the Subsystem Extract Anhydrous HCl 110, where an aqueous solution of hydrogen chloride (hydrochloric acid), anhydrous HCl and water extracted from the stream of highly concentrated aqueous solution of the crude HCl.

Subsystem Extract Anhydrous HCl 110 provides the output Stream 130 for recycling anhydrous hydrogen chloride to Ethane Reactor 102 and Subsystem Extract Anhydrous HCl 110 provides output water (for future use and for disposal as waste). Subsystem Extract Anhydrous HCl 110 returns relatively dilute stream of an aqueous solution of HCl (hydrochloric acid) using a Stream 128 in the Column of Damping 106. Column Blanking 106 also provides an output fluid flow in the Column Selection Light Fractions 114, where the flow of light fractions containing ethylene, optionally removed from the product stream leaving the reactor.

Column Selection Light Fractions 114 produces a stream of light fractions in the Reactor Direct Chlorination 112, where chlorine (Stream 126) add to the direct chlorination of ethylene in the stream of light fractions to EDC (1,2-dichloroethane). EDC extract in which Olonne to Extract EDC 116 for recycling in Ethane Reactor 102 and a number of remaining gaseous light ends recyclery in Ethane Reactor 102 in the form of a Stream 134, and device for the determination of CO (carbon monoxide) in the composition provide measurement (not shown) for use in determining a control system (not shown) corresponding portion of the remaining gaseous light ends processing using Node Oxidation Waste 118, with the generation of the waste stream to remove CO, CO2and other impurities from the system.

The output from the Column Selection Light Fractions 114, which does not enter the Reactor Direct Chlorination 112 is sent (a) a first Subsystem Drying 120 to remove water; (b) then in the Column Purification VCM 122, to highlight product - VCM (vinyl chloride monomer), and then (C) optionally, in the Column Removal of Heavy Fractions 124 for the removal of heavy fractions and generation of Stream 132. Stream 132 is a mixed fluid CIS-1,2-dichloroethylene and TRANS-1,2-dichloroethylene, 1,2-dichloroethane, ethylchloride and other chlorinated organics. In the alternative the proposed embodiment, based on the literature review, the Subsystem Drying 120 removes the water in front of the Column Selection Light Fractions 114, while carrying VCM output from the Column Selection Light Fractions 114 is directed (a) in the Column for Purification of the VCM 122, to highlight product - VCM (vinyl chloride monomer), and then (b) in addition to the Column removal of Heavy Tails is s 124 for the removal of heavy fractions and generation of Stream 132.

Finally, the Thread 132 is sent to the Hydrogenation Reactor RCl (chlorinated organics) 104, where the addition of hydrogen produces recyclery stream to the Ethane Reactor 102.

We now turn to a consideration of figure 2, in accordance with the preferred embodiments according to the present description. The method 200 Oxidehydrogenation ethane to VCM demonstrates a method of producing vinyl chloride from ethane/ethylene using a catalyst capable of prevrawenie ethane and ethylene to VCM by oxidehydrogenation; in this regard, the method requires the input of significant quantities of ethane and ethylene, or from recyclorama flows, either from the input flow in reactor (Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM). At the reactor inlet 202 Oxidehydrogenation Ethane/Ethylene to VCM receives (a) an input stream - the Input Stream of Ethane 222, an Input Stream of HCl 224, an Input Stream of Oxygen 226 and the Input Stream of Chlorine 228 and (b) recyclorama streams - Stream Ethylchloride 230, the Flow of Hydrogen Chloride (HCl) 266 and the Flow recyclorama Light Fractions 248, and part of the Flow EDC 262, when the EDC is advantageously used for recycling in accordance with market conditions and work conditions at a specific point in production.

As reflected in the application Dow No. 44649 from Mark E. Jones, Michael M. Olken, and Daniel A. Hickman, entitled "A PROCESS FOR CONVERSION OF THYLENE TO VINYL CHLORIDE, AND NOVEL CATALYST COMPOSITIONS USEFUL FOR SUCH PROCESS", filed October 3, 2000, United States Receiving Office, Express Mail Mailing Number EL636832801US, the catalyst used in the Reactor 202 to Oxidehydrogenation Ethane/Ethylene to VCM, contains at least one rare earth material. Rare earth elements are a group of 17 elements consisting of scandium (atomic number 21)and yttrium (atomic number 39) and lanthanoids (atomic numbers 57-71) [James C. Hedrick, U.S. Geological Survey - Minerals Information - 1997, "Rare-Earth Metals"]. The catalyst may be present either in the form of a porous bulk material, or it can be deposited on an appropriate substrate. The preferred rare earth materials are those, which are based on lanthanum, cerium, neodymium, praseodymium, dysprosium, samarium, yttrium, gadolinium, erbium, ytterbium, holmium, terbium, europium, thulium and lutetium. The most preferred rare earth materials for use in the above method of obtaining VCM are those that have as the basis of such rare earth elements, which are usually considered as materials with only one constant valency. Catalytic properties of materials with variable valency is less than gelaterie than those who have the same constant value. For example, cerium is known to be a catalyst for okelani the-recovery having the opportunity to be in the 3+and 4+stable oxidation States. This is one of the reasons why, if rare earth material has as a basis the cerium, the catalyst additionally contains at least one rare earth element other than cerium. Preferably, if one of rare earth elements used in the catalyst is a cerium, cerium is present in a molar ratio that is less than the total number of other rare earth materials present in the catalyst. More preferably, however, to cerium in essence was not in the catalyst. The phrase "essentially no cerium" means that the cerium is in the amount of less than 33 at.% of the rare earth components, preferably less than 20 at.%, and most preferably less than 10 at.%.

Rare earth material for the catalyst preferably has as the basis of lanthanum, neodymium, praseodymium, or a mixture thereof. Most preferably, at least one of rare earth elements used in the catalyst, is a lanthanum. In addition, for atlantabased input stream in the method of obtaining a VCM according to the present invention, the catalyst essentially does not contain iron and copper. Typically, p is OUTSTA materials, which are capable of oxidation-restoration (redox)is undesirable for the catalyst. Preferred catalyst is that it essentially does not contain other transition metals that have more than one stable oxidation state. For example, manganese is a transition metal, which is preferably stripped from the catalyst. Under the expression "not substantially contain" means that the atomic ratio of rare earth element to the redox metal in the catalyst is higher than 1, preferably higher than 10, more preferably higher than 15, and most preferably higher than 50.

As indicated above, the catalyst may be deposited on an inert substrate. Preferred inert substrates include alumina, silica gel, silica - alumina, silica - magnesia, bauxite, magnesium oxide, silicon carbide, titanium oxide, zirconium oxide, zirconium silicate, and combinations thereof. However, in the preferred embodiment the substrate is a zeolite. When used as an inert substrate, the rare earth component of the material of the catalyst generally ranges from 3 to 85 wt.% from the total mass of the catalyst and the substrate. The catalyst can be applied to the substrate using the Institute of economy and management methods, already known in this field.

It may also be advantageous to include other elements in the catalyst, in the form as a porous bulk material, and the material deposited on the substrate. For example, the preferred additive elements include rare earth elements, boron, phosphorus, sulfur, silicon, germanium, titanium, zirconium, hafnium, aluminum, and combinations thereof. These elements may be present to modify the catalytic characteristics of the composition or to improve the mechanical properties (e.g., resistance to friction) material.

Before combining atlantabased input stream, the source of oxygen and a source of chlorine in the reactor for a variant of the method of obtaining a VCM according to the present invention, for the composition of the catalyst is desirable that it contained salt, at least one rare earth element, provided that the catalyst essentially does not contain iron and copper, and with the additional condition that, when used cerium, the catalyst additionally contains at least one rare earth element other than cerium. Salt, at least one rare earth element is preferably selected from oxychloride rare earth elements, chlorides of rare earth elements, oxides of rare earth elements and combinations thereof, provided that the catalyst according to codestone contains iron and copper, and with the additional condition that, when used cerium, the catalyst additionally contains at least one rare earth element other than cerium. More preferably, the salt comprises oxychloride rare earth element of the formula MOCl, where M represents at least one rare earth element selected from lanthanum, cerium, neodymium, praseodymium, dysprosium, samarium, yttrium, gadolinium, erbium, ytterbium, holmium, terbium, europium, thulium, lutetium, or mixtures thereof, with the proviso that when cerium is present, then there is at least one rare earth element other than cerium. Most preferably, the salt is a porous, three-dimensional material of lanthanum oxychloride (LaOCl). As already mentioned, the best material that does not undergo large changes (e.g., fractures), when chlorinated in situ in this way, and provides an additional advantageous property of water solubility in the context of this method, after a period of use (LaOCl is initially insoluble in water), so if you need to remove spent catalyst from the reactor with the liquefied layer, the fixed layer or from other equipment or containers in this way, it can be done without hydroblasting or usual time-consuming mechanical is their methods, by simply draining the used catalyst from the reactor together with water.

Typically, when salt is an oxychloride of rare earth element (MOCl), it has a surface area according to BET of at least 12 m2/g, preferably at least 15 m2/g, more preferably at least 20 m2/g and most preferably at least 30 m2/, typically the surface area by the BET is less than 200 m2/year For these above measurements adsorption isotherm of nitrogen measured at 77 K and the surface area is calculated according to the isotherms using the BET method (Brunauer, S., Emmett, P.M., and Teller, E., J. Am. Chem. Soc., 60, 309 (1938)). In addition, it is seen that the phase MOCl have a characteristic diffraction pattern by x-ray on the powders (XRD), which differ from the phases MCl3.

It is also possible, as in some cases stated previously, obtaining mixtures of rare earth elements (M) in the composition MOCl. For example, M may be a mixture of at least two rare earth elements selected from lanthanum, cerium, neodymium, praseodymium, dysprosium, samarium, yttrium, gadolinium, erbium, ytterbium, holmium, terbium, europium, thulium and lutetium. Similarly it is also possible to obtain mixtures of various compositions MOCl, where M is different is for each song MOCl in the mixture.

As soon as atlantagay the input stream, the source of oxygen and a source of chlorine combined in the reactor, the catalyst is formed from a salt of at least one rare earth element in situ. In this respect it is assumed that formed in situ catalyst contains a rare earth chloride component. An example of such a chloride MCl is3where M represents a rare earth component selected from lanthanum, cerium, neodymium, praseodymium, dysprosium, samarium, yttrium, gadolinium, erbium, ytterbium, holmium, terbium, europium, thulium, lutetium and mixtures thereof, with the proviso that when cerium is present, the catalyst additionally contains at least one rare earth element other than cerium. Typically, when salt is a chloride rare earth element (MCl3), it has a surface area according to BET of at least 5 m2/g, preferably at least 10 m2/g, more preferably at least 15 m2/g, more preferably at least 20 m2/g and most preferably at least 30 m2/year

In the light of the present description, the person skilled in the art will undoubtedly provide alternative means of obtaining usable compositions of the catalysts. The method, which, as the authors suggest, is the preferred DL the formation of the composition, containing oxychloride rare earth element (MOCl), includes the following stages: (a) preparation of a solution of chloride salt of rare earth element or elements in a solvent containing either water or alcohol, or a mixture thereof; (b) adding a nitrogen-containing bases for the formation of a precipitate, and (C) collecting, drying and calcination of the precipitate to form material MOCl. Typically, nitrogen base selected from ammonium hydroxide, alkylamine, arylamine, arylalkylamine, hydroxide of alkylamine, hydroxide of arylamine, hydroxide of arylalkylamine and mixtures thereof. Nitrogen base can be represented as a mixture of nitrogen bases with other foundations that do not contain nitrogen. Preferably the nitrogen base is a hydroxide of tetraalkylammonium. The solvent at the stage of (a) preferably represents water. Drying suitable as catalyst composition can be produced by any method, including spray drying, drying in an oven with blowing and other known methods. For the currently favored mode in the liquefied layer is preferred catalyst is dried by atomization.

The method considered in the present preferred to form the catalyst composition containing chloride rarely is zemelnogo element (MCl 3), includes the following stages: (a) preparation of a solution of chloride salt of rare earth element or elements in a solvent containing either water or alcohol, or a mixture thereof; (b) adding a nitrogen-containing bases for the formation of a precipitate; (C) collecting, drying and calcination of the precipitate and (d) bringing into contact the calcined precipitate with a source of chlorine. For example, one application of this method (using La for illustration) may be the deposition of LaCl3from the solution with nitrogen bases, it is dried, add it to the reactor, heating it to 400°in the reactor to effect the calcination, and then bringing into contact the calcined precipitate with a source of chlorine, with the formation of the composition of the catalyst in situ in the reactor. The preferred catalysts for use will be further refined by consideration of the examples presented in the next section of the present description.

In the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM catalytically interact together ethane, ethylene, hydrogen chloride, oxygen and chlorine, along with at least one recycled stream, to obtain the Output 232 from the Reactor; it should specifically be noted that the molar ratio of ethane to ethylene, calculated for all input streams of the reactor 202 Oxidehydrogenation is of Ethane/Ethylene to VCM, is in the range from 0.02 to 50 (note that a particular working relationship at any time is determined by the requirements workflow status) without long-term degradation of functional properties of the catalyst. Depending on market conditions and working conditions at a specific point in the production of ethylene is added to the Reactor 202 in the Flow of Ethylene 289. In this regard, the preferred molar ratio of ethane to ethylene, calculated for all input streams to the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM, is in the range from 0.1 to 10. When working conditions and market conditions (in particular manufacturing) allow, the preferred mode for the flow of Ethylene 289 represents zero flow, and molar relationship of ethane to ethylene, calculated for all input streams to the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM, most preferably, it ranged from 0.3 to 4, in this variation depends on local conditions and the service life of the catalyst. Even if the output stream from the Reactor 202 (Stream 232) is generated by the catalytic interaction of ethane, ethylene, oxygen together and at least one chlorine source selected from hydrogen chloride, chlorine or a busy chloropetalum, it should be noted that the selectivity is utilizator when prevrawenie these threads in VCM wins primarily due to pre-conditioning catalysts based on lanthanides using elemental chlorine. The selectivity of the catalyst in prevrawenie these threads in the VCM using catalysts based on lanthanides also improves when elemental chlorine (Stream 228) included as part of the composition of the source of chlorine in the Reactor 202. It should also be noted that all other systems of catalysts that demonstrate the ability to prevrawenie as ethane and ethylene to VCM, can also be profitably used in alternative embodiments, together with the here described method and apparatus for producing VCM.

Sources of chlorine (selected from hydrogen chloride, chlorine and chloropetalum), the Input Stream HCl 224, an Input Stream of Chlorine 228, any part of the FLOW EDC 262 selected for recycling, and any other recycled or input streams of raw materials containing, without limitation, at least one substance selected from chlorinated methane, or the chlorinated ethane (for example, without limitation, carbon tetrachloride, 1,2-dichloroethane, ethylchloride, 1,1-dichloroethane and 1,1,2-trichloroethane) collectively put chlorine in the reaction oxidehydrogenation; these streams individually change from one moment time to another when working in real-time to ensure stekhiometricheskogo the amount of chlorine, necessary for the conversion of obtaining VCM. With regard to EDC from the Stream EDC 262, market conditions affecting the possibility of direct sale, determine the appropriate number or for recycling to the Reactor 202, either directly for sale. Additional opportunity to use part of the Flow EDC 262, depending on the specific features is the introduction of the raw material into the furnace conversion in VCM. In this regard, operation of the Method 200 alternative is carried out in such a way that (a) 1,2-dichloroethane, generated in the Reactor 202, clear for sale, (b) 1,2-dichloroethane, generated in the Reactor 202 is cleaned for recycling to the Reactor 202, and/or (C) 1,2-dichloroethane, generated in the Reactor 202, cleanse for cracking in the furnace to obtain the vinyl. It should also be noted that sometimes advantageous to buy EDC as a source of chlorine.

The reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM generates the output stream from the Reactor 232 input in Cooling the Condenser 204. Cooling the Condenser 204 processes the output from the Reactor 232 receive (a) flow of the crude product (pair), containing the first part of the hydrogen chloride, and (b) flow raw (chilled water) hydrogen chloride containing remaining hydrogen chloride, which leaves the Reactor 202; the stream of raw product (pair) is predstavljaet a Stream 240.

Stream 234 is transferred to the Subsystem 206 Phase Separation to remove any remaining organic compounds from raw chilled HCl. Subsystem 206 Phase Separation is, in alternative embodiments, sump, desorber or a combination sump and desorber. From Subsystem 206 Phase Separation deleted organic materials (mainly in the liquid phase) is transferred to the Column 210 Selection of Light Fractions using a Stream 242, and a dedicated chilled raw (mostly liquid aqueous solution) HCl is transferred in the form of a Stream 236 in the Subsystem 208 Extraction Anhydrous HCl. Subsystem 208 Extraction Anhydrous HCl takes (water) Stream 274 from Node 214 Oxidation of Waste (node thermal oxidation or other oxidation suitable for purification of the output stream to compositions acceptable for the environment), the Flow 278 (water) from a Node 276 adsorption of HCl from Light Fractions and (water) Stream 236 and generates the output stream Stream 266 in the form of recycling anhydrous HCl into the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM. Stream 268 removes water from engine Extraction Anhydrous HCl 208 for later use or to retrieve waste. In the end. Subsystem 208 Extraction Anhydrous HCl works by removing the stream of anhydrous hydrogen chloride from the stream of raw cooled hydrogen chloride and the other is their streams of aqueous solutions of HCl Method 200. Subsystem 208 Extraction Anhydrous HCl also recyclery stream of anhydrous hydrogen chloride (par) in the reactor. As should be clear to experts in this field, there are other methods to highlight anhydrous HCl from mixtures of water and HCl.

Cooling the Condenser 204 also generates a Stream 240 (par) in Column 210 Selection of Light Fractions, where the flow of light fractions (steam Flow 244)containing ethylene, optionally removed from the output stream of the product from the reactor. Note that, in contrast to the previously discussed system according to Figure 1, the ethylene from the Column 210 Selection of Light Fractions for the most part is returned as recycle to the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM without becoming EDC.

After separation of HCl and flow of light fractions (Flow 244) from the output stream from the reactor Column 210 Selection of Light Fractions directs the Flow 252 to separate the flow of the product - water flux product of vinyl chloride monomer (Stream 254), flow ethylchloride (Stream 230), mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene (Stream 260), flow 1,2-dichloroethane (Stream 262) and heavy fractions (Flow 264). The method of implementation of these end offices is obvious to the person skilled in the art, and a significant number used in the classical ways of nodes can be used in RA is personal configurations to achieve these divisions. Subsystem 216 Drying Column 218 for Cleaning VCM and the Column 220 Removal of Heavy Fractions is convenient to designate, therefore, as a General systems division (and, as such, they should have the term "column"is interpreted as "virtual column"representing at least one physical column, though, in one of the proposed embodiments, each column may be a separate physical column) for separation of the Water Flow 256, the flow of Product VCM 254, Flow Ethylchloride 230, the Flow of CIS/TRANS-1,2-dichlorethylene 260 and Flow EDC 262 with the Flow of Heavy Fractions 264 as organic material for destruction in the furnace for incineration of organic waste or for use in the corresponding product, where total Flow properties of Heavy Fractions 264 are acceptable. In the alternative the proposed embodiment of the Subsystem 216 Drying removes the water in front of the Column 210 Selection of Light Fractions, whereby the output stream from the Column 210 Selection of Light Fractions is sent to the Column 218 VCM Purification. Again note that in relation to EDC from the Stream EDC 262 market conditions affect the ability of its direct sales, determining the appropriate number or for recycling to the Reactor 202, or for direct sale. In this regard, the work of the Pillars 218 VCM Purification and Columns 220 Removal of Heavy Fractions made the reader alternately, so (a) 1,2-dichloroethane is cleared for sale, (b) 1,2-dichloroethane cleared for recycling to the Reactor 202 and/or (C) 1,2-dichloroethane cleared for cracking in the furnace to obtain the vinyl.

Let us turn now to Flow 244, as it emerges from the Column 210 Selection of Light Fractions. Stream 244 is divided into the first part of the stream which is sent directly in the Stream 248 in the Reactor 202 Oxidehydrogenation Ethane/Ethylene to VCM, and the second stream which is sent to first Node 276 HCl absorption of Light Fractions, and then in Column 212 Absorption and separation of C2. Node 276 HCl Absorption of Light Fractions provides a water solution of HCl in the form of a Stream 278 in the Subsystem 208 Extraction Anhydrous HCl. Columns 212 Absorption and separation of C2 absorb and separate the materials C2 (ethane and ethylene) sent from the second part of the flow from the Stream 244 and ensure the recycling of materials C2 in the Reactor 202 via Stream 246 Recycling C2, which, in combination with the first part flow of the Flow 244 forms a Stream 248. Columns 212 Absorption and separation of C2 also issue the purge stream to the NODE 214 OXIDATION of WASTE, which produces a STREAM 250 WASTE into the atmosphere, and (water) Stream 274 in the Subsystem 208 Extraction Anhydrous HCl. Device for control of CO (carbon monoxide) in the composition provide measurements (not shown) for use SystemControl (not shown) in determining the appropriate part of the residual gaseous light ends processing using Columns 212 Adsorption and separation of C2 and Node 214 Oxidation of Waste with the purpose of generating a Flow Of 250 Waste thus, to not accumulate to levels unacceptable in the process.

Model the relative velocities of the flows and compositions of the streams for Method 202 Oxidehydrogenation ETHANE TO VCM clear from consideration of table 1. The data in table 1 (unit mass/unit time) use is made in the laboratory measurement of the operating characteristics of the catalyst for lanthanum oxychloride at 400°C and at a pressure essentially, the environment; additional details of the preferred catalyst is clear from the study "A PROCESS FOR THE CONVERSION OF ETHYLENE TO VINYL CHLORIDE, AND NOVEL CATALYST COMPOSITIONS USEFUL FOR SUCH PROCESS". Table 1 shows some of the threads as zero, in the context of data generation in the simulation, but this numerical value is not intended to indicate a complete lack of flow or lack of need in the stream. Table 1 shows the input Stream of Ethylene 289; in this respect, and, repeating the previous reasoning, when the market and working conditions at a specific point of production, the most preferred mode for the flow of Ethylene 289 is zero flow. However, under certain conditions, the Flow of Ethylene 289 provides a cost-effective stream.

Table 1
The MASS BALANCE conversion of ETHANE/TELENAV the vinyl CHLORIDE TO METHOD 200
StreamWith2H6C2H4O2HClCl2ArCOCO2EDCEtClVCMDCEH2AboutOnly
222573000000000000573
22400000000000000
226005390050000000545
228000063900000000639
2300000 000004500045
23289545632732042709129163451000954994798
23440120456001315731428874941709
23600045600000000494950
24085544432276042708126614572853089
242401200001315731428870 760
24489545632276042709129000002541
2461094300000000000152
2488893490241037618113000002247
2500000050183000013202
252000000001634510009501303
25400000000 001000001000
25600000000000055
2600000000000095095
262000000005340000534
26400000000000000
266000491000000000491
268000 000000000494494
278000350000000075111
28489535103042709129371000682568
2880003000000006870
2908953510004270912937100002498
294000000003710000371

Let us now turn to figure 3. The process 300 Oxidehydrogenation Ethane to VCM with CIS/TRANS-Recycling is a modification of the process 200 Oxidehydrogenation Ethane to VCM due to the inclusion of Site 280 Hydrogenation DCE (dichloroethylene) for (a) hydrogenation of CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene from the stream of CIS/TRANS-1,2-dichlorethylene 260 and (b) recycling of the output stream to the Reactor 202. In an alternative embodiment the Threads 230, 260, and 262 are separated in the form of a single mixed stream to the Column 220 for Removal of Heavy Fractions and this one mixed flow recyclery Node 280 Hydrogenation DCE.

Table 2 provides additional details regarding the components indicated on the drawings.

Specific features of the catalysts additionally explained by considering the following examples, which are purely explanatory.

Example 1

To demonstrate the production of vinyl chloride from a stream containing ethylene, prepare porous, refractory composition comprising lanthanum. The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride is (get from J.T. Baker Chemical Company) in 8 parts of deionized water. Add dropwise with stirring, ammonium hydroxide (get from Fisher Scientific, certified ACS specification) to obtain a neutral pH (universal indicator paper) causes the formation of gel. The mixture is centrifuged and the solution decanted from the solid product. Add approximately 150 ml of deionized water and gel vigorously stirred for dispersion of solid product. The resulting solution was centrifuged and the solution decanted. This stage wash is repeated two additional times. Assembled the washed gel is dried for two hours at 120°and then calcined at 550°C for four hours in air. The obtained solid product is ground and sieved to obtain particles suitable for further investigation. This method gives a solid product with x-ray diffraction pattern analysis of the powder corresponding to LaOCl.

Particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the ethylene, ethane, HCl, O2and inert gas (a mixture of No and Ar) can be typed into the reactor. The function of argon is to serve as an internal standard for analysis of the substances in the reactor and coming out of it, using gas chromatography. Contact time (volume) is calculated ka the volume of the catalyst divided by the volumetric flow rate at standard conditions. Feed speed correspond to the molar relationship. In the system of the reactor is fed directly athenagorase stream with a stoichiometry of one ethane, one of HCl and one oxygen. It provides a balanced stoichiometry for the production of VCM from ethylene.

Table 3 below presents the results of a research reactor using this composition.

Column 1 of table 3 shows a high selectivity to vinyl chloride, the catalyst is ethylene under oxidative conditions in the presence of HCl. The composition comprises helium to simulate reactor operating with air as the oxidizing gas.

Column 2 of table 3 shows high selectivity to vinyl chloride, the catalyst is ethylene under oxidative conditions in the presence of HCl. Now the composition of the enriched fuel to address the limitations imposed by flammable, and contains no helium.

Column 3 of table 3 shows high selectivity to vinyl chloride and ethylene, the catalyst serves ethane under oxidative conditions in the presence of HCl. Composition simulates the reactor using air as the oxidizing gas. Ethylene in the input stream is not prisutstvuet, present in the reactor is the product of partial oxidation of ethane.

Column 4 of table 3 shows the result for the case when administered as ethane and ethylene. The reactor operates in such a way that the amount of ethylene introduced into the reactor and leaving the reactor are equal. When working thus ethylene acts as an inert diluent, and becomes only the ethane. The results show a high yield of vinyl chloride and 1,2-dichloroethane. Argon is used as an internal standard to ensure that the flow of ethylene, part of the reactor, and the flow leaving the reactor were equal. The relationship of the areas under the chromatographic peaks of ethylene and argon are identical for input and output stream from the reactor. In this way the recycling of ethylene is modeled inside the reactor device.

Table 3
Molar relationship at the input
With2H423.703
C2H60012
HCl2212.5
O2111 1
Inert substances6,8040
401400401419
Contact time (sec)12,35,021,812,4
Conversion of O2(%)47,353,7of 54.893,9
Selectivity (%)
C2H4--44.7-
With2H4Cl210,714,00,112,8
VCM76,678,134,568,5

Example 2

To further demonstrate the use of a composition of the ethylene oxidation is converted into a vinyl chloride using a variety of sources of chlorine. The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Avocado Research Chemicals Ltd.) 6.6 parts of deionized water. Quick add with stirring 6M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of g is La. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 550°C for four hours in air. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor can enter ethylene, HCl, oxygen, 1,2-dichloroethane, carbon tetrachloride and helium. Contact time (volume) is calculated as the amount of catalyst divided by the volumetric flow rate at standard temperature and pressure. Speed input streams correspond to the molar relationship. The composition is heated to 400°and is treated with a mixture of 1:1:3 HCl:O2:Not within 2 hours before starting work.

The obtained composition in the production of vinyl chloride by feeding ethylene, source of chlorine and oxygen at 400°C. the Following table shows the data flow received between 82 and 163 hours using different sources of chlorine. Chlorine is served in the form of HCl, carbon tetrachloride and 1,2-dichloroethane. VCM denotes the vinyl chloride. Contact time (volume) is calculated as the amount of catalyst divided by the volumetric flow rate at standard temperature and pressure. The reactors operate at atmospheric pressure at the reactor outlet. As ethylene and 1,2-dichlo the ethane are referred to as particles With 2.

Table 4
Molar relationship at the input
With2H42,02,02,02,0
With2H60,00,00,00,0
CCl40,50,50,00,0
With2H4Cl20,00,01,80,0
HCl0,00,00,01,9
O21,01,01,01,0
Not+Ar8,99,08,96,7
400399401400
Contact time (sec)8,04,08,6a 4.9
The partial degree of conversion (%)
With2H440,427,018,720,1
With2H60,00,00,00,0
CCl4 94,878,40,00,0
With2H4Cl20,00,098,30,0
HCl0,00,00,044,7
O268,842,055,2of 37.8
Selectivity with respect to the moles converted With2
VCMto 59.6of 56.486,078,5
C2H4Cl214,830,70,02,2
With2H5Cl0,60,40,21,6

These data show that many sources of chlorine can be used in oxidative obtaining vinyl. When using carbon tetrachloride, 1,2-dichloroethane and HCl all they give a vinyl chloride as the dominant product.

Example 3

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Avocado Research Chemicals Ltd.) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified reagent CS, receive from Fisher Scientific) causes the formation of gel and gives the final value of pH cent to 8.85. The mixture is filtered to collect the solid product. The collected material is calcined in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas.

Table 5 shows the data where the input streams into the reactor should be installed so that the flow of ethylene (mol/min), which is in the reactor, and the flow of ethylene leaving the reactor are essentially the same. Similarly, the input streams into the reactor, similarly, are regulated so that the flow of HCl that is included in the reactor and leaving it, are essentially the same. The degree of conversion of oxygen is set slightly less than complete conversion to make it possible to monitor the activity of the catalyst. When working in this mode power consumption input substances are ethane, oxygen and chlorine. As ethylene, HCl and act as substances that are not produced and not consumed. The contact time is calculated as the amount of catalyst divided by the volumetric flow rate at standard temperature and dubliniensis example additionally illustrates the use of chlorine gas as a source of chlorine in the production of vinyl chloride.

Table 5
Molar relationship at the input
With2H42,1
With2H64,5
Cl20,5
HCl2,4
O21,0
Not+Ar7,4
T°)400
Contact time (sec)9,4
The partial degree of conversion (%)
With2H41,8
With2H627,3
Cl299,8
HClof-1.4
O296,4
Selectivity (%)
VCM79,0
C2H4Cl27,2
C2H5Cl1,7
COx5,1
C2H40,5

As in all the examples, VCM here refers to the vinyl chloride. With2H4Cl2is only 1,2-dichloroethane. COxis a combination of CO and CO2.

Examples 4 to 11 illustrate the generation of multiple rare earth compositions, each of which contains only one rare earth material. Data illustrating the performance characteristics of these compositions are presented in table 6.

Example 4

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Aldrich Chemical Company) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The gel is re-suspended in 6,66 parts deionized water. Centrifugation allows you to collect the gel. The collected gel dried at 120°before calcination at 550°C for four hours in air. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the ethylene, ethane, HCl, oxygen, and inert (a mixture of helium and argon gas can be introduced into the reactor. X-ray diffraction analysis of the powder shows that the material is a LaOCl. The measured surface area by BET is 42,06 m2/, Conques is to maintain data on the operating characteristics for this example are presented below in table 6.

Example 5

The solution NdCl3in water prepared by dissolving one part of commercially available hydrated neodymium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. X-ray diffraction analysis of the powder shows that the material is a NdOCl. The measured surface area by BET is 22,71 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 6

The solution PrCl3in water prepared by dissolving one part of commercially available hydrated praseodymium chloride (Alfa Aesar) in 6,67 parts deionized water. Repeat adding with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) call is for gel formation. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. X-ray diffraction analysis of the powder shows that the material is a PrOCl. The measured surface area by BET is 21,37 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 7

The solution SmCl3in water prepared by dissolving one part of commercially available hydrated samarium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 500°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could the introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. X-ray diffraction analysis of the powder shows that the material is a SmOCl. The measured surface area by BET is 30,09 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 8

A solution of HoCl3in water prepared by dissolving one part of commercially available hydrated holmium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 500°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 20,92 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 9

The solution ErCl3in water prepared by dissolving one part of commercially available hidradenoma the aqueous erbium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 500°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 19,80 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 10

The solution VbCl3in water prepared by dissolving one part of commercially available hydrated ytterbium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 500°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 20). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 2,23 m2/year Specific data on the performance specifications for this example are presented below in table 6.

Example 11

The solution YCl3in water prepared by dissolving one part of commercially available hydrated yttrium chloride (Alfa Aesar) in 6,67 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is filtered to collect the solid product. The collected gel dried at 120°before calcination at 500°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 29,72 m2/year Specific data on the performance specifications for this example are presented below in table 6.

These data demonstrate the suitability of bulk compositions containing rare earth the elements, for the conversion of atlantageorgia flows in the vinyl chloride.

Examples 12 to 16

Examples 12 to 16 illustrate various compositions based on rare earth elements, each of which contains a mixture of rare earth materials. Data illustrating the performance characteristics of these samples are presented in table 7.

Example 12

The solution LaCl3and NdCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) and 0.67 part of commercially available hydrated neodymium chloride (Alfa Aesar) in 13,33 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The final measured pH value is 8,96. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET of composition is employed, 21,40 m 2/year Specific data on the performance specifications for this example are presented below in table 7.

Example 13

The solution LaCl3and SmCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) and 0.67 part of commercially available hydrated samarium chloride (Alfa Aesar) in 13,33 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The final measured pH value is 8,96. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 21,01 m2/year Specific data on the performance specifications for this example are presented below in table 7.

Example 14

The solution LaCl3and YCl3in water prepared by dissolving one part of the commercial is available hydrated lanthanum chloride (purchased from Spectrum Quality Products) and 0.52 part of commercially available hydrated yttrium chloride (Alfa Aesar) in 13,33 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The final measured pH value is 8,96. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 20,98 m2/year Specific data on the performance specifications for this example are presented below in table 7.

Example 15

The solution LaCl3and HoCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) and one part of commercially available hydrated holmium chloride (Alfa Aesar) in 13,33 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The final measured pH value of the composition is yet 8,64. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 19,68 m2/year Specific data on the performance specifications for this example are presented below in table 7.

Example 16

The solution LaCl3and HoCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) and 0.75 part of commercially available hydrated ytterbium chloride (Alfa Aesar) in 13,33 parts deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The final measured pH value is 9,10. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°before calcination in air at 550°C for four hours. Receiving the hydrated solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 20,98 m2/year Specific data on the performance specifications for this example are presented below in table 7.

These data demonstrate the suitability of the volume containing rare earth elements compositions, which contain a mixture of rare earth materials, for turning atlantageorgia flows in the vinyl chloride.

Examples 17 - 24

Examples 17 to 24 are compositions containing rare earth materials in the presence of other additives.

Example 17

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Aldrich Chemical Company) in 6,67 parts deionized water. 0,48 parts ammonium hydroxide (Fisher Scientific) is added to 0.35 part powder CeO2received already prepared from commercial sources (Rhone-Poulenc). Containing lanthanum and cerium mixture is added together with stirring to form a gel. The resulting containing gel mixture is filtered and the collected solid product calcined in air at 550°C for 4 h the owls. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. Specific data on the performance specifications for this example are presented below in table 8.

Example 18

Composition comprising lanthanum, prepared using the method of example 5, ground using a mortar and pestle with the formation of fine powder. One part of the crushed powder combine from 0.43 parts of powder BaCl2and additionally crushed using a mortar and pestle to form a homogeneous mixture. Containing lanthanum and barium mixture is pressed for the formation of lumps. Pieces calcined at 800°C in air for 4 hours. The resulting material is placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. Specific data on the performance specifications for this example are presented below in table 8.

Example 19

The dried silica Grace Davison Grade 57 dried at 120°C for 2 hours. A saturated solution of LaCl3formed in the water using commercially available Hydra the new lanthanum chloride. The dried silica impregnated to the point of emergence of moisture by using a solution LaCl3. The impregnated silica leave to air dry for 2 days at ambient temperature. It further dried at 120°C for 1 hour. The resulting material is placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. Specific data on the performance specifications for this example are presented below in table 8.

Example 20

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) to 6.67 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The gel is re-suspended 12.5 parts of acetone (Fisher Scientific), centrifuged and the liquid is again decanted and discarded. Stage washing with acetone addition is repeated 4 times, with the use of 8.3 parts of acetone. The gel is re-suspended 12.5 parts of acetone, add 1,15 part of hexamethyldisilizane (p is bathed from Aldrich Chemical Company) and the solution stirred for one hour. The mixture is centrifuged to collect the gel. Collect the gel allow to dry in air at ambient temperature before calcination in air at 550°C for four hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. The measured surface area by BET is 58,82 m2/year Specific data on the performance specifications for this example are presented below in table 8.

Example 21

The solution LaCl2in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (Alfa Aesar) and 0,043 part of commercially available HfCl4(bought from Acros Organics) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°during the night before calcination at 550°C for 4 hours. Specific data on the performance specifications for this example are presented below in table 8.

P the emer 22

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (Alfa Aesar) and 0,086 part of commercially available HfCl4(bought from Acros Organics) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The collected gel dried at 80°during the night before calcination at 550°C for 4 hours. Specific data on the performance specifications for this example are presented below in table 8.

Example 23

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (Alfa Aesar) and 0,043 part of commercially available ZrOCl2(bought from Acros Organics) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. The gel is re-suspended in 6,67 parts of deionized water and subsequently centrifuged. The solution is decanted and discarded. SOBR the config gel prikalivajutsa 550° C for 4 hours. Specific data on the performance specifications for this example are presented below in table 8.

Example 24

The solution LaCl3in water prepared by dissolving commercially available hydrated lanthanum chloride in deionized water to obtain 2,16 M solution. Commercially produced zirconium oxide (get from Engelhard) dried at 350°With during the night. One part of zirconium oxide impregnated with 0.4 parts of a solution LaCl3. The sample is dried in air at room temperature, and then calcined in air at 550°C for 4 hours. The obtained solid product is ground and sieved. The sieved particles are placed in a reactor made of pure Nickel (alloy 200). The reactor is configured so that the reactor could be introduced ethylene, ethane, HCl, oxygen and inert (a mixture of helium and argon) gas. Specific data on the performance specifications for this example are presented below in table 8.

These data demonstrate vinyl chloride from Atlanterra flows using catalysts based on lanthanum, which contain other elements or deposited on a substrate.

Examples 25 to 30

Examples 25 to 30 illustrate some of the modifications that are possible to change the preparation of compositions of rare earth elements, th is-breaking for use.

Example 25

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The solution is decanted from the gel and drop. Prepare a saturated solution of 0.61 part of benzyltriethylammonium (purchased from Aldrich Chemical Company) in deionized water. The solution is added to the gel and mix. The collected gel calcined at 550°C for 4 hours. Specific data on the performance specifications for this example are presented below in table 9. This example illustrates the use of added ammonium salts to modify the preparation of compositions with rare earth elements.

Example 26

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid productdisplay one part glacial acetic acid to the gel, and the gel is re-dissolved. Adding a solution of 26 parts of acetone causes the formation of sludge. The solution is decanted and the solid product calcined at 550°C for 4 hours. Specific data on the performance specifications for this example are presented below in table 9. This example demonstrates the preparation of compositions with lanthanum, suitable for use by decomposition products of the addition of chlorine to carboxylic acids containing compounds of rare earth elements.

Example 27

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Spectrum Quality Products) in 10 parts of deionized water. Quick add with stirring 6 M ammonium hydroxide in water (diluted certified ACS reagent, Fisher Scientific) causes the formation of gel. The mixture is centrifuged to collect the solid product. The collected gel re-suspended at 3.33 parts of deionized water. Then add 0,0311 part of the reagent phosphoric acid (purchased from Fisher Scientific) does not produce visible changes in suspended gel. The mixture is again centrifuged and the solution decanted from the containing phosphorus gel. The collected gel calcined at 550°C for 4 hours. The calcined solid product has a surface area according to BET 33,05 m 2/year Specific data on the performance specifications for this example are presented below in table 9. This example demonstrates the preparation of compositions of rare earth elements, also containing phosphorus as phosphate.

Example 28

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Acros Organics) in 6,66 parts deionized water. The solution is formed by mixing of 0.95 parts of a commercially available DABCO, or 1,4-diazabicyclo[2,2,2]octane (purchased from ICN Pharmaceuticals), dissolved in 2.6 parts of deionized water. Rapid mixing of two solutions with stirring causes the formation of gel. The mixture is centrifuged to collect the solid product. The collected gel re-suspended in 6,67 parts deionized water. The mixture is again centrifuged and the solution decanted from the gel. The collected gel calcined for 4 hours at 550°C. the Calcined solid product has a surface area according to BET 38,77 m2/year Specific data on the performance specifications for this example are presented below in table 9. This example demonstrates the suitability of the alkylamine in the preparation of the composition of rare earth elements suitable for use.

Example 29

The solution LaCl3in water prepared by dissolving one part of the com the Cesky available hydrated lanthanum chloride (purchased from Acros Organics) in 10 parts of deionized water. To this solution is quickly added to 2.9 parts of a commercially available tetramethyldisiloxane (purchased from Aldrich Chemical Company) with stirring, causing the formation of a gel. The mixture is centrifuged and the solution decanted from the gel. The collected gel re-suspended in 6,67 parts deionized water. The mixture is again centrifuged and the solution decanted from the gel. The collected gel calcined for 4 hours at 550°C. the Calcined solid product has a surface area according to BET 80,35 m2/year Specific data on the performance specifications for this example are presented below in table 9. This example demonstrates the suitability of alkilammonievymi in the preparation of the composition of rare earth elements suitable for use.

Example 30

The solution LaCl3in water prepared by dissolving one part of commercially available hydrated lanthanum chloride (purchased from Avocado Research Chemicals Ltd.) in 6,67 parts deionized water. To this solution quickly and with stirring, add 1,63 part of commercially available 5 n NaOH solution (Fisher Scientific), causing the formation of a gel. The mixture is centrifuged and the solution decanted from the gel. The collected gel calcined for 4 hours at 550°C. the Calcined solid product has a surface area according to BET 16,23 m2/year Specific data on the performance for this is about the example presented below in table 9. This example demonstrates the suitability does not contain nitrogen bases for the formation of catalytically interesting materials. Although they are potentially functional, study materials, apparently, are inferior to those that are produced with the use of nitrogen-containing bases.

The present invention is described in an illustrative manner. In this regard, it is evident that the person skilled in the art, as only he will understand the advantages according to the preceding description, will be able to make modifications described herein specific embodiments, without deviating from the essence of the present invention. Such modifications should be considered within the framework of the present invention, which is limited only by the scope and essence of the attached claims.

1. Method for the production of vinyl chloride, including stage

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50, and where at this stage catalytic interaction using a catalyst containing co is ponent of rare earth material, provided that the catalyst contains almost no iron and copper, and with the additional proviso that when component rare earth material is cerium, the catalyst additionally contains at least one component of rare earth material other than cerium;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the hydrogen chloride;

split the specified stream of raw product stream, a product of vinyl chloride monomer and the flow of light fractions containing the specified first part of hydrogen chloride; and

recycling the specified stream of light fractions to catalytic interaction together with the specified ethane, specified ethylene specified by the oxygen and the specified source of chlorine at this stage of generation.

2. The method according to claim 1, characterized in that the rare earth material selected from lanthanum, neodymium, praseodymium and mixtures thereof.

3. The method according to claim 2, characterized in that the rare earth material is a lanthanum.

4. The method according to claim 1, characterized in that the molar ratio is in the range from 0.1 to 10.

5. The method according to claim 1, characterized in that the molar ratio is in the range from 0.3 to 4.

6. The method according to claim 1, characterized in that one of these sources of chlorine choose at least one substance from the group comprising chlorinated methane and chlorinated ethane.

7. The method according to claim 1, characterized in that one of these sources of chlorine select at least one of chlorinated organic compounds, including carbon tetrachloride, 1,2-dichloroethane, ethylchloride, 1,1-dichloroethane and 1,1,2-trichloroethane.

8. The method according to claim 1, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for sale.

9. The method according to claim 1, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for recycling in the specified reactor.

10. The method according to claim 1, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified to cracking in the furnace to obtain the vinyl.

11. Method for the production of vinyl chloride, including stage

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the limits of from 0.02 to 50, and where at this stage catalytic interaction using the catalyst, contains a rare earth material, provided that the catalyst contains almost no iron and copper, and with the additional proviso that when component rare earth material is cerium, the catalyst additionally contains at least one component of rare earth material other than cerium;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor as specified reagent hydrogen chloride and

recycling the specified stream of light fractions in the specified reactor.

12. The method according to claim 11, different is the present, what component of rare earth material selected from lanthanum, neodymium, praseodymium and mixtures thereof.

13. The method according to item 12, characterized in that the rare earth material is a lanthanum.

14. The method according to claim 11, characterized in that the molar ratio is in the range from 0.1 to 10.

15. The method according to claim 11, characterized in that the molar ratio is in the range from 0.3 to 4.

16. The method according to claim 11, characterized in that one of these sources of chlorine choose at least one substance from the group comprising chlorinated methane and chlorinated ethane.

17. The method according to claim 11, characterized in that one of these sources of chlorine select at least one of chlorinated organic compounds, including carbon tetrachloride, 1,2-dichloroethane, ethylchloride, 1,1-dichloroethane and 1,1,2-trichloroethane.

18. The method according to claim 11, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for sale.

19. The method according to claim 11, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for recycling in the specified reactor.

20. The method according to claim 11, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified to cracking in the furnace to obtain the vinyl.

21. Method for the production of vinyl chloride, including the tadji

generating the output stream from the reactor through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50, and where at this stage catalytic interaction using a catalyst containing a rare earth component of the material, provided that the catalyst contains almost no iron and copper, and with the additional proviso that when component rare earth material is cerium, the catalyst additionally contains at least one component rare earth material other than cerium;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first h is the terrain of hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor as specified reagent - hydrogen chloride;

split the specified stream of light fractions in the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

absorption and recycling in the specified reactor flow C2 containing ethane and ethylene from the specified purge flow and

recycling the specified stream being recycled gas in the specified reactor.

22. The method according to item 21, characterized in that the rare earth material selected from lanthanum, neodymium, praseodymium and mixtures thereof.

23. The method according to item 22, characterized in that the rare earth material is a lanthanum.

24. The method according to item 21, characterized in that the molar ratio is in the range from 0.1 to 10.

25. The method according to item 21, characterized in that the molar ratio is within about is 0.3 to 4.

26. The method according to item 21, wherein one of the specified sources of chlorine choose at least one substance from the group comprising chlorinated methane and chlorinated ethane.

27. The method according to item 21, wherein one of the specified sources of chlorine select at least one of chlorinated organic compounds, including carbon tetrachloride, 1,2-dichloroethane, ethylchloride, 1,1-dichloroethane and 1,1,2-trichloroethane.

28. The method according to item 21, wherein the 1,2-dichloroethane generated in this stage of the reaction, purified for sale.

29. The method according to item 21, wherein the 1,2-dichloroethane generated in this stage of the reaction, purified for recycling in the specified reactor.

30. The method according to item 21, wherein the 1,2-dichloroethane generated in this stage of the reaction, purified to cracking in the furnace to obtain the vinyl.

31. Method for the production of vinyl chloride, comprising the stage of:

generating the output stream from the reactor, through catalytic interaction together ethane, ethylene, oxygen and at least one chlorine source selected from hydrogen chloride, chlorine or chloropetalum, where the molar ratio of the indicated ethane to the specified ethylene is in the range from 0.02 to 50, and where at this stage catalytic interaction using utilizator, contains a rare earth material, provided that the catalyst contains almost no iron and copper, and with the additional proviso that when component rare earth material is cerium, the catalyst additionally contains at least one component of rare earth material, other than cerium;

cooling and condensing the specified output stream from the reactor with a stream of the crude product containing the first part of the hydrogen chloride, and the flow of raw cooled hydrogen chloride, containing the second part of the hydrogen chloride;

split the specified stream of raw product to product flow - water flow product of vinyl chloride monomer, the flow ethylchloride, mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene, a stream of 1,2-dichloroethane, the flow of heavy fractions and the flow of light fractions containing the specified first part of the hydrogen chloride;

retrieve stream of anhydrous hydrogen chloride from the specified stream raw cooled hydrogen chloride;

recycling the specified stream of anhydrous hydrogen chloride in the specified reactor as specified reagent - hydrogen chloride;

split the specified stream of light fractions in the purge stream and the stream is being recycled gas;

absorption of hydrogen chloride from the specified purge stream to separate the flow of an aqueous solution of hydrogen chloride;

joins the specified stream of an aqueous solution of hydrogen chloride with the specified stream raw cooled hydrogen chloride;

hydrogenation of the specified mixed flow CIS-1,2-dichloroethylene and TRANS-1,2-dichlorethylene with education being recycled stream to the specified reactor;

absorption and recycling in the specified reactor flow C2 containing ethane and ethylene from the specified purge stream; and

recycling the specified stream being recycled gas in the specified reactor.

32. The method according to p, characterized in that the rare earth material selected from lanthanum, neodymium, praseodymium and mixtures thereof.

33. The method according to p, characterized in that the rare earth material is a lanthanum.

34. The method according to p, characterized in that the molar ratio is in the range from 0.1 to 10.

35. The method according to p, characterized in that the molar ratio is in the range from 0.3 to 4.

36. The method according to p, characterized in that one of these sources of chlorine choose at least one substance from the group comprising chlorinated methane and chlorinated ethane.

37. The method according to p, characterized in that one of these sources of chlorine choose at least one of chlorinated organic compounds, including carbon tetrachloride, 1,2-dichloroethane, ethylchloride, 1,1-dichloroethane and 1,1,2-trichloroethane.

38. The method according to p, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for sale.

39. The method according to p, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purified for recycling in the specified reactor.

40. The method according to p, characterized in that the 1,2-dichloroethane generated in this stage of the reaction, purify, for cracking in the furnace to obtain the vinyl.

Priority signs:

Signs of paragraphs 1, 11, 21, 31, except signs separately below, as well as all the signs 2, 3, 6, 7, 9, 12, 13, 16, 17, 19, 22, 23, 26, 27, 29, 32, 33, 36, 37 and 39 have priority from 22.11.1999.

The following characteristics:

the ratio of ethane and ethylene are involved in the catalytic interaction (applies to claims 1 to, 4, 5, 11, 14, 15, 21, 24, 25, 31, 34, 35);

cooling and condensation of the output stream from the reactor (11, 21, 31);

the stage of recovery and recycling hydrogen chloride (11, 21, 31);

an additional indication of the destination options (future use) obtained in inventive ways 1,2-dichloroethane, namely the "for sale" and "for cracking in the furnace obtained for the vinyl I" (for PP, 10, 18, 20, 28, 30, 38, 40), have priority 06.10.2000.



 

Same patents:

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

FIELD: industrial organic synthesis.

SUBSTANCE: gas-phase thermal dehydrochlorination of 1,2-dichloroethane is conducted in presence of hydrogen chloride as promoter dissolved in feed in concentration between 50 and 10000 ppm.

EFFECT: increased conversion of raw material and reduced yield of by-products.

4 cl, 1 tbl, 8 ex

FIELD: chemical technology, in particular method for vinylchloride production.

SUBSTANCE: claimed method includes fast gas cooling in quenching column followed by separation of pyrolysis products. Quenching and separation are carried out by barbotage through the layer of liquid concentrated by-products of these gases in quenching column cube. Then steam/gas mixture is brought into contact with returning condensate in regular filling layer of rectification tower with simultaneous purification of steam/gas mixture in rectification zone upstream. Liquid concentrated by-products are additionally rectified in vacuum with isolating and recovery of products having boiling point higher than the same for dichloroethane and distillate recycling. Method of present invention also makes it possible to produce perchloroethylene and tricloroethylene.

EFFECT: vinylchloride of high quality; reduced effort and energy consumption.

2 tbl, 4 dwg, 2 ex

FIELD: chemical industry, in particular method for production of value monomer such as vinylchloride.

SUBSTANCE: claimed method includes passing of reaction mixture containing dichloroethane vapor trough catalytic layer providing dehydrochlorination of dichloroethane to vinylchloride. Catalyst has active centers having in IR-spectra of adsorbed ammonia absorption band with wave numbers in region of ν = 1410-1440 cm-1, and contains one platinum group metal as active component, and glass-fiber carrier. Carrier has in NMR29Si-specrum lines with chemical shifts of -100±3 ppm (Q3-line) and -110±3 ppm (Q4-line) in integral intensity ratio Q3/Q4 from 0.7 to 1.2; in IR-specrum it has absorption band of hydroxyls with wave number of ν = 3620-3650 cm-1 and half-width of 65-75 cm-1, and has density, measured by BET-method using argon thermal desorption, SAr = 0.5-30 m2/g, and specific surface, measured by alkali titration, SNa = 10-250 m2/g in ratio of SAr/SNa = 5-30.

EFFECT: method with high conversion ratio and selectivity.

3 cl, 2 ex

FIELD: chemical industry, in particular method for production of value products from lower alkanes.

SUBSTANCE: claimed method includes passing of gaseous reaction mixture containing at least one lower alkane and elementary chlorine through catalytic layer. Used catalyst represents geometrically structured system comprising microfiber with diameter of 5-20 mum. Catalyst has active centers having in IR-spectra of adsorbed ammonia absorption band with wave numbers in region of ν = 1410-1440 cm-1, and contains one platinum group metal as active component, and glass-fiber carrier. Carrier has in NMR29Si-specrum lines with chemical shifts of -100±3 ppm (Q3-line) and -110±3 ppm (Q4-line) in integral intensity ratio Q3/Q4 from 0.7 to 1.2; in IR-specrum it has absorption band of hydroxyls with wave number of ν = 3620-3650 cm-1 and half-width of 65-75 cm-1, and has density, measured by BET-method using argon thermal desorption, SAr = 0.5-30 m2/g, and specific surface, measured by alkali titration, SNa = 10-250 m2/g in ratio of SAr/SNa = 5-30.

EFFECT: method of increased yield.

3 cl, 4 ex

The invention relates to the production of parameningeal by alkylation of phenol, alpha-methylstyrene and the catalyst for this process
The invention relates to a technology for chlorohydrocarbons by the chlorination of olefins and subsequent separation of the products of chlorination on target and by-products, in particular to a method of rectification of a mixture of chlorinated propylene with obtaining allyl chloride of high purity
The invention relates to a technology for chlorohydrocarbons by the chlorination of olefins and subsequent separation of the products of chlorination on target and by-products, in particular to a method of rectification of a mixture of chlorinated propylene with obtaining allyl chloride of high purity

The invention relates to the processing of the products of oxidative pyrolysis gas metadatareader
The invention relates to the chemical industry and plastics

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

The invention relates to the industrial catalyst, its acquisition and its use, especially for the production of 1,2-dichloroethane (EDC) oxychloination of ethylene in the reactor with a fluidized bed or in a reactor with a fixed layer

The invention relates to a method for producing 1,2-dichloroethane by reacting Athena with hydrogen chloride and oxygen or oxygen-containing gas on copper-containing catalyst in the fluidized bed

The invention relates to methods for organochlorine products and can be used in the chemical industry for the improvement of the production of vinyl chloride from ethylene

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

The invention relates to the production of the monomer is vinyl chloride from ethane

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer from ethane and ethylene. Method involves generating the outlet flow from reactor by catalytic interaction in common of ethane, ethylene, oxygen and at least one chlorine source taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At the indicated stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst doesn't comprise iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more rare-earth material but not cerium. Indicated outlet flow from reactor is cooled and condensed to form flow of crude product comprising the first part of hydrogen chloride and flow of crude cooled hydrogen chloride comprising the second part of indicated hydrogen chloride. Then method involves separation of indicated flow of crude product for vinyl chloride monomer as the flow product and flow of light fractions comprising the indicated first part of indicated hydrogen chloride. Then indicated flow of light fractions is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at indicated generating stage. Also, invention proposes variants of a method for producing vinyl chloride from ethane and ethylene. Invention provides preparing vinyl (chloride) from ethane and ethylene by the complete extraction of hydrogen chloride from the reactor outlet flow.

EFFECT: improved producing method.

40, 9 tbl, 3 dwg, 31 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

Up!