TW201247595A - Manufacture of at least one ethylene derivative compound - Google Patents

Abstract

Ethylene-containing composition comprising (a) between 75 and 99.9 % by volume of hydrocarbon compounds containing 2 carbon atoms; and (b) a quantity of ethylene such that the ratio of this quantity to the total quantity of hydrocarbon compounds containing 2 carbon atoms is comprised between 97 and 99.5 %. Process for the manufacture of such ethylene-containing composition. Process for the manufacture of at least one ethylene derivative compound starting from such ethylene-containing composition. Process for the manufacture of ethylene dichloride according to which the ethylene-containing composition is subjected to a chlorination and/or an oxychlorination in order to produce ethylene dichloride, further pyrolyzed in order to produce vinyl chloride, further polymerized in order to produce polyvinyl chloride.

Description

201247595 VI. INSTRUCTIONS: This application claims the priority of the European Application No. 11154555.4, filed on Feb. 15, 2011, the entire content of TECHNICAL FIELD OF THE INVENTION The present invention relates to a composition containing B. In particular, the invention relates to an ethylene-containing composition suitable for the manufacture of at least one ethyl storage derivative, more particularly to the manufacture of ethylene dichloride (EDC). It also relates to a process for the manufacture of such an ethylene-containing composition and to a process for the manufacture of at least one ethylene derivative compound, preferably EDC/vinyl chloride (VC) and polyvinyl chloride (PVC). . [Prior Art] Olefins have traditionally been produced from petroleum feedstocks by catalytic or steam cracking processes. Such cracking processes, particularly steam cracking, produce basic olefins such as ethylene and/or propylene from a variety of hydrocarbon feedstocks. Ethylene and propylene are commodity commodity petrochemicals that are useful in many processes for making plastics and other compounds. Ethylene is used to make a variety of polyethylene plastics and is used in the manufacture of other chemicals such as EDC/VC/PVC 'ethylene oxide, ethylbenzene and alcohols. Propylene is used in the manufacture of a variety of polypropylene plastics and is used in the manufacture of other chemicals such as acrylonitrile and propylene oxide. It has been known for some time in the petrochemical industry that oxygenates, especially alcohols, can be converted to basic olefins such as ethylene and propylene. This process -5- 201247595 is known as the oxygenate to olefin process or OTO process. Preferred for the production of basic olefins is an oxygenate-based methanol. This methanol to olefin conversion process is known as the methanol to olefin process or the MTO process. This effluent stream from OTO (preferably an MTO reactor) contains desirable olefins, such as ethylene and propylene, together with undesirable high concentrations of by-products, the amount of which produces ethylene and propylene. They are unacceptable for their preferred disposal (e.g., polymerization) and should be removed thereafter to produce a stream of olefin product having high purity. The removal of by-products therefore means that some of the effluent stream exiting the OTO/MTO reactor is treated to produce very high purity olefins (called olefins of polymerization grade), in particular characterized by greater than 99.8% by volume, often It is a polymerization grade of ethylene having a purity of at least 99.9% by volume. An example of such a process for separating a polymerization grade of ethylene and propylene from an initial effluent stream from a methanol to olefins reaction system can be found in U.S. Patent No. 7,091,497. Equipment calculations and resources (materials and energy) necessary to provide polymerization grade olefins and, in particular, to provide a polymerization grade of ethylene, can substantially increase operating costs. Therefore, there is a need to provide an ethylene-containing composition at a low cost, such a composition may contain different types of impurities and be in a level that will not be inhibited for its future use. 201247595 [Invention] The object is in part to provide an ethylene-containing composition. Such a composition is preferably suitable for the manufacture of at least one ethylene derivative compound, in particular EDC, having a purity lower than the polymerization grade of ethylene. Such an ethylene-containing composition is preferably obtained from a mono-oxygen starting material by a process of a new oxygenate to olefin. To this end, the invention relates to an ethylene-containing composition 'comprising (a) between 75% and 99.9% by volume of a hydrocarbon compound having 2 carbon atoms; and (b) - measuring bismuth B The calcination is such that the ratio of the amount of rhodium to the total amount of the hydrocarbon compound having 2 carbon atoms is between 97% and 99.5%. The "ethylene-containing composition" is used in this specification to mean a composition comprising ethylene as a main component. The ethylene-containing composition according to the invention is comprised between 7 5 % and 9 9 % by volume, preferably between 7 7 % and 9 9.9%, more preferably 96% and 99.9 %. Between and preferably between 96.5% and 99.9% of a hydrocarbon compound having 2 carbon atoms. Most particularly preferred is an ethylene-containing composition comprising between 79% and 99.9% by volume of a hydrocarbon compound having 2 carbon atoms. The expression "hydrocarbon having 2 carbon atoms" is understood to mean, for the purposes of the present invention, any organic compound containing at least carbon and hydrogen atoms and containing 2 carbon atoms. Preferably, the hydrocarbon compound having 2 carbon atoms contained in the ethylene-containing composition according to the present invention is ethylene, ethane and acetylene. 201247595 The ethylene-containing composition according to the present invention comprises an amount of ruthenium ethylene such that the amount is 値 with the total amount of the hydrocarbon compound having 2 carbon atoms (preferably, ethylene, ethane and acetylene). The ratio is comprised between 9 7 and 99.5%, preferably between 97.5% and 99.5%, more preferably between 98% and 99.2%, and most preferably at 98.5%. Between 99.2%. The most preferred ethylene-containing composition comprising ethylene in an amount such that the amount is between hydrazine and a hydrocarbon compound having 2 carbon atoms (preferably ethylene, ethane and acetylene) The ratio of total 値 is between 98.8% and 99.2%. Accordingly, the ethylene-containing composition according to the invention comprises advantageously between 7.8% and 99.4% by volume, preferably between 75.1% and 99.4%, more preferably 94.1%. Between 99.1% and optimal is a quantity of ruthenium ethylene between 95.1% and 99.1%. Specifically, the most preferred is an ethylene-containing composition comprising ethylene in an amount of between 9 5 · 8 % and 99.1 % by volume. The ethylene-containing composition is therefore advantageously not a grade of ethylene, i.e. characterized by greater than 99.8% by volume, often a purity of up to 99.9% by volume. The ethylene-containing composition according to the present invention advantageously comprises less than 100 ppm by volume of a hydrocarbon compound containing at least 3 carbon atoms and less than 100 ppm by volume of oxygenate and water. The expression "hydrocarbon containing at least 3 carbon atoms" is understood to mean, for the purposes of the present invention, any organic compound containing at least carbon and hydrogen atoms and comprising at least 3 carbon atoms." Such a hydrocarbon comprising at least 3 carbon atoms Examples of the like -201247595 are propane, propylene, butane and their unsaturation together with all the more saturated or unsaturated compounds. The expression "oxygenate" is to be understood as meaning for the purposes of the present invention - The following organic compounds 'the compound includes at least carbon and hydrogen and at least one oxygen atom, such as an aliphatic alcohol, an ether, a carbonyl compound, a ketone, a carboxylic acid, a carbonate, an ester, and the like.) Limited to methanol, ethanol, n-propanol, isopropanol, C4-C20 methyl ether, diethyl ether, methyl ethyl ether, diisopropyl ether, dipropyl methyl ether, isopropyl methyl ether, C Ethyl ethyl ether, isopropylacetaldehyde, acetaldehyde, propionaldehyde, dimethyl carbonate, dimethyl ketone, methyl ester, acetic acid and ester thereof, propionic acid and ester thereof, and mixtures thereof, The oxygenate is selected from the following one or Species: methanol, diethyl ether, diethyl ether, formaldehyde, acetaldehyde, acetic acid and esters thereof or their products. More preferably, the oxygenates are selected from the group consisting of methanol, dimethyl ether, acetic acid and esters thereof or A mixture thereof. The ethylene-containing composition according to the invention advantageously comprises, by weight, preferably less than 50, more preferably less than 2 5, less than 10 and most preferably less than 5 ppm of a hydrocarbon compound containing at least 3. The ethylene-containing composition according to the present invention advantageously comprises an oxygen compound in an amount of 1 〇〇 ppm and water. The ethylene-containing composition according to the present invention is advantageous. The composition includes an oxygen compound and water in an amount of less than 50, more preferably less than 20', and less than 10 ppm. The derivative is at least atomic (the aldehyde is an alcohol, Diether, propyl ether, acid and its preferred alcohol, di-mixed, acetic acid product is a small carbon original product small sample and small best - 9 - 201247595 According to the inclusion of 20 packs of aliquots, the equenes 5 Preferably, the 00 is more than 10, most preferably less than 5 ppm and particularly preferably less than 2 ppm of the oxygenate. The ethylene-containing composition according to the present invention. Advantageously, comprising less than 100, preferably less than 50, more preferably less than 20, and most preferably less than 10 ppm water by volume. The ethylene-containing composition according to the invention further comprises Less than 2500 ppm by volume, preferably less than 1800, more preferably less than 100, and most preferably less than 50 ppm of water. Specifically, most particularly preferred is an ethylene-containing composition, including Less than 20 Ppm of acetylene by volume. The ethylene-containing composition according to the present invention advantageously comprises acetylene greater than 0.1, preferably greater than 0.3, and more preferably greater than 0.5 ppm by volume. The invention further relates to a process for the manufacture of an ethylene-containing composition according to the process: a) an effluent stream E which contains ethylene and other constituents from the process of the monooxygen to the olefin and which has been subjected to a conventional treatment Subject to a pre-treatment process to obtain a compressed effluent stream '; and b) the compressed effluent stream E' is separated in one to three distillation columns to obtain an ethylene-containing composition according to the present invention. The process according to the present invention is a process for the manufacture of an ethylene-containing -10-201247595 composition starting from the effluent stream E of ethylene and other constituents from a process from monooxygen to olefin. The expression "oxygen to olefins process (OTO process)" is understood to mean a process for starting from a mono-oxygen starting material for the purposes of the present invention and producing an effluent stream E containing bismuth and other constituents. "Oxygenate starting material" is understood to be a starting material for the purposes of the present invention. The starting material is one or more aliphatic alcohols or ethers. Examples of oxygenate starting materials include, but are not limited to, methanol, ethanol, n-propanol, and isopropyl. Alcohol, C4-C2 sterol 'dimethyl ether, diethyl ether, methyl ethyl ether, diisopropyl ether, dipropyl ether, propyl methyl ether 'isopropyl methyl ether, propyl ethyl acid Or isopropyl ethyl ether or a mixture thereof. Preferably, the oxygenate starting materials are selected from the group consisting of methanol, ethanol, dimethyl ether, methyl ethyl ether, diacetic acid or a mixture thereof. Preferably, the oxygenate starting material is selected from the group consisting of: methanol, dimethyl ether, or a mixture thereof. The method for making an ethylene-containing composition according to the present invention preferably comprises fgp containing B The effluent stream E of suspicion and other components is derived from a process from methanol to olefin. In the methanol to olefin process, the oxygenate materials are preferably: methanol, dimethyl ether, or a mixture thereof. The oxygenate starting material can be produced by any process known in the art, including Fermentation or reaction of synthesis gas (synthesis gas) derived from natural gas, petroleum liquids, carbonaceous materials (such as coal), recycled plastics, municipal waste or any other organic material. Preferably, such oxygenate materials are borrowed. Produced by the reaction of syngas. Syngas production processes are well known and include conventional steam reforming, autothermal conversion, or a combination thereof. -11 - 201247595 Preferably, 'syngas is produced by steam reforming of natural gas. In general, the production of syngas includes: natural gas (mostly a courtyard) and a combustion reaction of hydrogen, carbon monoxide and/or carbon dioxide from an oxygen source. Overall, then a heterogeneous catalyst (typically a copper based) Catalyst) is contacted with a stream of synthesis gas (typically carbon dioxide and carbon monoxide with hydrogen) to produce an oxygenate-containing stream. One or more diluents, such as nitrogen, argon, nitrogen, carbon monoxide, carbon dioxide, water, substantially unreacted alkanes (especially alkanes such as A, E, and B), substantially unreacted, A substantially unreacted aromatic compound and mixtures thereof are added to the oxygenate feedstock' typically used to reduce the concentration of active ingredient in the feed stream. The preferred diluent is water. It may also include hydrocarbons. A portion of the oxygenate feedstock, i.e., as a co-feed. Preferred hydrocarbons for co-feed include propylene, butene, pentene, C4 + hydrocarbon mixtures, cs + hydrocarbon mixtures, and mixtures thereof. More preferably, a Co hydrocarbon mixture, the most preferred of which is a mixture of c4 + hydrocarbons obtained from the separation and recycled to the reactor. Other oxygenates obtained from the subsequent separation (step b)) can be recycled to the reaction. In the device. According to the process for producing an ethylene-containing composition according to the present invention, it is preferred that the effluent stream E containing ethylene and other components is derived from the process of -oxygen to olefin, preferably methanol to olefin. Such production is preferably carried out in the presence of a catalyst, preferably a one-molecular catalyst or one molecule of catalyst composition. The molecular sieve -12-201247595 chemical composition advantageously comprises molecular sieves and binders and/or matrix materials 较佳 preferred molecular sieve catalysts of zeolite or zeolite type molecular sieves. Alternatively, the preferred molecular sieve is an aluminophosphate (AL Ρ Ο ) molecular sieve and/or a bismuth aluminophosphate (SAPO ) molecular sieve and a substituted, preferably metal-substituted ALPO and/or SAPO molecular sieve, A molecular sieve comprising a symbiotic material having two or more different phases or crystal structures in a molecular sieve composition. The binder material can include different types of hydrated alumina, vermiculite, and/or other inorganic oxide sols. The matrix material may comprise one or more rare earth metals, metal oxides and natural clays> The reactor used may be a fixed bed reactor, a fluidized bed reactor (continuous fluidized bed reactor or continuous high speed) a fluidized bed reactor), a mixed reactor having a plurality of dense or fixed bed zones and/or a fast fluidized bed reaction zone connected together, a circulating fluidized bed reactor, a riser reactor, and analog. The produced effluent stream E comprising ethylene and other constituents advantageously comprises the desired olefin product, such as ethylene and propylene together with by-products, such as hydrogen, aqua, carbon monoxide 'carbon dioxide, water, keyuan, propylene, propylene. Heavier components of propane and propylene, such as C4 + components (olefinic and aliphatic), multiple unsaturated components, such as acetylene, methyl acetylene, and propadiene, and oxygenates as defined above. The effluent stream E containing ethylene and other components from the oxygenate to olefin process (preferably methane to olefins) and having undergone a conventional treatment is subjected to a preconditioning treatment to obtain a preconditioning process prior to being subjected to separation. -13- 201247595 A compressed outflow stream E is obtained. Advantageously, the conventional treatment comprises cooling the effluent stream, and preferably comprises removing the produced condensate. The treatment includes cooling and quenching the effluent stream E and removing the resulting condensate. Advantageously, the preconditioning treatment comprises: i) reversing the simultaneous removal of the produced condensate; ii) removing the acid gas oxidized carbon and the like) and iii) performing the adsorption treatment of the oxygenate (which is understood to be for the present invention) The purpose is to refer to oxygen and hydrogen atoms and have a normal boiling point above 〇 ° C) as well as water. Removal of acid gases (which are carbon dioxide and similar to any known method (appropriate methods include absorption in an alkaline aqueous solution or methanol vapor). Adsorption treatment can use any known adsorbent admixture including alumina, activation Alumina, aluminosilicates such as 3A and 4A molecular sieves, lime, magnesium hydroxide, and the like. Preferably, the preconditioning process comprises i) using an interstage cooler for multistage compression of the effluent stream E, Condensate; ii) removing acid gases (wherein carbon dioxide and iii) for adsorption treatment to remove undesired oxygenates. Preferably, the preconditioning treatment comprises: multistage the effluent stream E at each cooler Compressing, removing the product and removing it by a city wash to remove the compressor from the penultimate and E cooling and/or it is preferred that it is preferred to include a spur stream E (which is two to remove unwanted, An organic compound comprising at least carbon can be passed through a solution, an aqueous amine (appropriate suction, molecular sieve, analog). The resulting cold and species are removed between each stage and water. Interstage condensate between stages: acid gas between the first and last steps of •14·201247595 and adsorption treatment on a suitable adsorbent to remove water and undesired oxygenates. The compressed effluent stream E' advantageously comprises up to PPm of oxygenate by volume and up to 10 ppm by volume of water by volume. The compressed effluent stream E' advantageously comprises up to ppm by volume, preferably up to 800 ppm, more preferably up to 6 Torr and most preferably up to 400 ppm of oxygenate. The compressed effluent stream E' advantageously comprises up to 1 Torr, preferably up to 50 ppm, more preferably up to 20 and most up to 10 ppm by volume of water. The compressed effluent stream E' advantageously comprises up to ppm of oxygenate by volume and up to 1% by volume of water by volume. As the composition of the effluent stream E changes, the maximum amount of enthalpy in the effluent stream E' and the maximum amount 水 of water can be independent of the above mentioned enthalpy of consideration as discussed above. After step a), the compressed effluent stream E' is separated in a to three distillation column to obtain an ethylene-containing composition according to the invention (i.e., as described above). The compressed outflow E' from a) can be subjected to a thermal conditioning step prior to introduction into the distillation column. The expression heat regulation step is understood to mean a series of heat exchanges that optimize energy usage, such as stepwise cooling of the effluent stream E' in a set of exchangers, first cooling with untreated water and then using ice-cold water, and then using The cold fluid plus the crossover recovers the sensible heat of the stream produced. The flow defined by the more steam than 1000 1000 and the most ppm of 1000 oxygen is internally paired, and the effluent stream E' can be exchanged as a single saturation or as several subfractions as described in -15-201247595. In the distillation column. It is preferably introduced as a single fraction. Each distillation column is advantageously a column comprising a stripping section and/or a rectifying section. If both segments are present, the rectifying section is preferably located above the stripping section. Each distillation column is advantageously selected from the group consisting of a distillation column comprising the above two stages and a column comprising only one of the two sections. Preferably, each distillation column comprises the two sections described above. Each distillation column is advantageously equipped with associated auxiliary equipment such as, for example, at least one reboiler and at least one condenser. A means for allowing intermediate withdrawal and an intermediate heat exchange can be added to the distillation column. When the distillation column is equipped with a condenser and as mentioned below, the composition or fraction is separated at the top of the distillation column, it is understood for the purposes of the present invention that such a composition or fraction is in the condenser. The exit is separated. According to a first embodiment of the process of the invention, after step a), the compressed effluent stream E' is separated in a distillation column T1 into an ethylene-containing composition C1 at the top of the distillation column T1 and separated A fraction H1 enriched in a compound containing at least 3 carbon atoms at the bottom of the distillation column T1. According to this first embodiment of the process according to the invention, the above step b) is advantageously carried out at a pressure of at least 8 bar, preferably at least 12 bar and at least 15 bar in a particularly preferred manner. Step b) Advantageously -16-201247595 is carried out at a pressure of at most 45 bar', preferably at most 4 bar, and at a maximum of 35 bar in a particularly preferred manner. The temperature at which the 'step b) according to this first embodiment is carried out is advantageously at least -60 ° C, preferably at least -55 ° C at the top of the distillation column T1 and at least - 5 0 in a particularly preferred manner. ° C. The top of the distillation column T 1 is advantageously at most 1 ° C, preferably at most 5 ° C and in a particularly preferred manner at most 0 ° C. According to this first embodiment, the temperature at which step b) is carried out is advantageously at least 〇 at the bottom of the distillation column T1, preferably at least 1 ° C and at least 20 ° C in a particularly preferred manner. The bottom of the distillation column T1 is advantageously at most 120 ° C, preferably at most 11 ° C and in a particularly preferred manner at most 1oooc. According to a second embodiment of the method of the invention, after step a), the compressed effluent stream E' is separated in two distillation columns by the following steps: b 1) - a first separation step, the step consisting in The compressed effluent stream E is separated into a fraction F2 at the top of the distillation column T2 in a first distillation column T2 and separated into fractions enriched with a compound having at least 4 carbon atoms at the bottom of the distillation column T2. 2; and b2) - a second separation step in which the fraction F2 is separated in a second distillation column T2' into an ethylene-containing composition C2 at the top of the distillation column T2' and separated into the distillation At the bottom of column T2' is a fraction η 2 enriched in a compound containing at least 3 carbon atoms. According to this second embodiment of the method of the invention, the above steps -17-201247595 bl) (first separation step) and step b2) (second separation step) are advantageously at least 8 bar, preferably at least 1 2 bar and carried out under a pressure of at least 15 bar in a particularly preferred manner. Step bl) is advantageously carried out at a maximum of 45 bar, preferably at most 40 bar and at a pressure of up to 35 bar in a particularly preferred manner. A compression can be applied between the two separation steps. According to this second embodiment, the temperature at which step b 1 ) is carried out is advantageously at least -20 ° C, preferably at least -15 ° C at the top of the distillation column T2 and at least - l in a particularly preferred manner 〇°C. Advantageously at the top of the distillation column T2 is at most 50 ° C, preferably at most 45 ° C and in a particularly preferred manner at most 40 ° C. According to this second embodiment, the temperature at which step bl) is carried out is advantageously at least 50 ° C at the bottom of the distillation column T2, preferably at least 60 ° C and in a particularly preferred manner at least 7 ° C. Advantageously at the bottom of the distillation column T2 is at most 160. (:, preferably at most l5 〇 ° C and in a particularly preferred manner is at most 140 ° C. According to this second embodiment, the temperature at which step b2) is carried out is advantageously at the top of the distillation column T2 ′ At least -7 ° C, preferably at least -60 ° C and in a particularly preferred manner at least _ 5 ° ° C. Advantageously at the top of the distillation column T2' is at most 0, preferably at most -5 °c and in a particularly preferred manner at most 10 °C. According to this second embodiment, the temperature at which step b2) is carried out is advantageously at least 〇 at the top of the distillation column T2' and at least 20 in a particularly preferred manner. C. In the distillation column T2, the bottom is advantageously at most 120 〇C, preferably at most 110 ° C compared to -18 - 201247595 and at most 100 ° C in a particularly preferred manner 〇 a third embodiment of the method according to the invention By way of step a), the compressed effluent stream E' is separated in three distillation columns by the following steps: bl) - a first separation step consisting in the compression of the effluent stream E' A distillation column T3 is separated into a fraction F3 at the top of the distillation column T3 and separated into a fraction F3'' b2) at the bottom of the distillation column T3 - a second separation step in which the fraction F3' is The second distillation column T3' is separated into a fraction F3" at the top of the distillation column T3' and separated into a fraction H3 enriched with a compound having at least 4 carbon atoms at the bottom of the distillation column T3'; and b3 a third separation step in which the fractions F3 and F3" are separated in a third distillation column T3" into an ethylene-containing composition C3 at the top of the distillation column T3" and separated into the distillation column. The bottom of T3" is enriched with a compound containing at least 3 carbon atoms. a fraction H3'. This third embodiment of the method according to the invention 'step bl) (first separation step), step b2) (second separation step) and step b3) (third separation step) are advantageously It is carried out at a pressure of at least 8 bar', preferably at least 12 bar, and at least 15 bar in a particularly preferred manner. Step bl) is advantageously at most 45 bar', preferably at most 40 bar and at In a particularly preferred manner, a pressure of up to 35 bar is carried out. A compression can be applied between each of the three separation steps. According to this third embodiment, the temperature at which step bl) is carried out is -19 - 201247595 The top of the distillation column T3 is advantageously at least -70 ° C ', preferably at least _ 60. (: and in a particularly preferred manner at least -50 ° C ° at the top of the distillation column T3 is advantageously at most 0 Preferably, it is at most -5 ° c and in a particularly preferred manner is at most -10 ° C. The temperature at which the 'step bl' is carried out according to this third embodiment is advantageously at least 0 at the bottom of the distillation column T3 'It is preferably at least i 〇 °c and at least 20 ° in a particularly preferred manner c. advantageously at the bottom of the distillation column T3 is at most 120 ° C, preferably at most 110 ° C and in a particularly preferred manner is at most 10 ° C. According to this third embodiment 'step b2) The temperature at the time of the distillation column T 3 is advantageously at least 〇, preferably at least 10 ° C and in a particularly preferred manner at least 20 ° C. advantageously at the top of the distillation column T 3 ' Up to 100 ° C, preferably up to 90 ° C and in a particularly preferred manner up to 80 ° C. According to this third embodiment, the temperature at which step b2) is carried out advantageously at the bottom of the distillation column T3' It is at least 20 ° C, preferably at least 3 ° C and in a particularly preferred manner at least 40 ° C. Advantageously at the bottom of the distillation column T3' is at most 160. (:, preferably at most 5 〇 c > C and in a particularly preferred manner is at most 140 ° C. The temperature at the time of proceeding according to this third embodiment 'step b3) is advantageous at the top of the distillation column T3" The ground is at least -7 ° C. Preferably, it is at least -60 ° C and in a particularly preferred manner at least -5 ° C. The top of the steaming tower T3" is advantageously at most 〇, preferably Is at most -5 ° C and in a particularly preferred manner is at most 10 ° C. -20- 201247595 According to this third embodiment, the temperature at which step b 3 ) is carried out is advantageously at the bottom of the distillation column T3" At least 〇, preferably at least 10 ° C and at least 20 in a particularly preferred manner. C» is advantageously at most 120 ° C at the bottom of the distillation column T3", preferably at most 110 ° C and in a particularly preferred manner at most 1 ° C. Enriched with at least 3 carbon atoms The fractions HI, H2' and H3' of the compound may be used as such or may be further purified into very high purity propylene (referred to as polymerization grade propylene) for use in the manufacture of propylene derivative compounds. The expression "containing at least 3 carbon atoms "Compound" is understood to mean a hydrocarbon compound having at least 3 carbon atoms as defined above for the purposes of the present invention. As an example of a propylene derivative compound, acrylonitrile and its derivatives may be mentioned, among others, together with a polymer produced therefrom, propylene oxide and its derivatives, and homopolymers and copolymers of propylene (hereinafter referred to as polypropylene). Polypropylene is a preferred propylene-derived compound. It is enriched with at least 4 carbons. The fractions H2 and H3 of the atomic compound can be used as such or can be further purified to a very high purity grade for use as a valuable hydrocarbon grade or as a fuel. "A compound having 4 carbon atoms" is understood to mean any organic compound containing at least carbon and hydrogen atoms and comprising at least 4 carbon atoms for the purposes of the present invention. Examples of such compounds containing at least 4 carbon atoms are Alkene, butene together with all saturated or unsaturated heavier compounds. -21 - 201247595 The process according to the invention is further characterized in that after step b), the ethylene-containing composition is subjected to an acetylene saturation. For the purposes of the invention, acetylene saturation is understood to be any operation which permits partial saturation of the triple bond of acetylene. In such operations, a series of hydrogenation (which is preferred) may be mentioned. The above acetylene hydrogenation step may By any known hydrogenation catalyst, such as a catalyst based on palladium, platinum, rhodium, ruthenium or iridium, the catalyst is placed on a support such as alumina, vermiculite, vermiculite/alumina, carbon, calcium carbonate or Barium sulphate, but also nickel-based catalysts and those based on cobalt-molybdenum complexes. Preferably, the hydrogenation step is carried out by a palladium-based or The catalyst is carried out. In a particularly preferred manner, it is carried out by means of a palladium-based catalyst. With regard to the support, the hydrogenation step is carried out in a particularly preferred manner by means of a compound based on the above, preferably palladium or platinum. The catalyst is palladium), preferably deposited on alumina, carbon, calcium carbonate or barium sulfate. The amount of palladium in the catalyst is advantageously at a level of 1% by weight. The temperature at which the step is carried out is advantageously at least 5, preferably at least 20.0, in a particularly preferred manner at least 25 ° C, in a most particularly preferred manner at least 40 ° C and in a true The most particularly preferred mode is at least 50 C. It is advantageously at most 150 C, preferably at most 120. (:, and in a particularly preferred manner at most ioo °c. With respect to this pressure, it is advantageously greater than or equal to 1 '. Preferably, the large -22-201247595 is at or equal to 5, in a particularly preferred manner is greater than or equal to 1 〇 and in a most particularly preferred manner Greater than or equal to 15 bar. It is advantageously less than or equal to 50, preferably less than or equal to 45' in a particularly preferred manner is less than or equal to 40 and in a most particularly preferred manner is less than or equal to 30 bar. Advantageously, the hydrogenation step of the acetylene is carried out using a large amount of hydrogen to complete the hydrogenation completely, that is, preferably at least 99%. The amount of hydrogen is advantageously such that the molar ratio of hydrogen:acetylene is equal to or greater than 1, preferably equal to or greater than 1.5, equal to or greater than 2 in a particularly preferred manner, and most preferably The mode is equal to or greater than 3 and is equal to or greater than 4 in a truly most particularly preferred manner. Drying can be optionally carried out after the acetylene is saturated. The process according to the invention is further characterized in that after step b), the ethylene-containing composition is more preferably subjected to a supplementary separation step (referred to as demethanization) to thereby separate the enriched specific ethylene A fraction of a light compound. Compounds lighter than ethylene are advantageously methane, hydrogen, carbon monoxide, nitrogen and other inert gases. This supplementary separation step is advantageously carried out at a pressure of at least 8 bar, preferably at least 12 bar and at a pressure of at least 15 bar in a particularly preferred manner. It is advantageously carried out at a pressure of at most 45 bar, preferably at most 40 bar and at a maximum of 35 bar in a particularly preferred manner. A compression can be applied before this step is fully removed. The temperature at which this additional separation step is carried out is advantageously at least _ 1 3 Μ at the top of the demethanization distillation column -23-201247595 D Μ. C, preferably at least _] 2 5 . C and at least -120 〇C in a particularly good way. The top of the demethanized distillation column DM is advantageously at most _50. €, preferably up to _60 cC and in a particularly good way up to -70. The temperature at which this supplementary separation step is carried out is advantageously at least _50 at the bottom of the demethanization distillation column DM. (:, preferably at least -47. <: and at least -45 in a particularly good manner. (:. at the top of the demethanized distillation column DM advantageously advantageously at most 0 ° C, preferably at most 5 ° C and in a particularly preferred manner at most 0 ° C. More preferably based on The method of the invention, together with the first, second and third embodiments of the method, is characterized in that after step b), the ethylene-containing composition is first subjected to an acetylene saturation and then subjected to a complementary separation. The step (referred to as demethanization) is thereby separated from a fraction enriched in a compound lighter than ethylene. The preferred first embodiment of the method according to the invention will now be described with reference to Figure 1 attached to the present description. The effluent stream E containing ethylene and other constituents from the process of the monooxygenate to the olefin (preferably MTO) and having undergone a conventional treatment (cooling, quenching and removal of the produced condensate) is carried out in one The compressor is compressed to undergo a preconditioning process PCT while removing the resulting condensate and subjected to a municipal wash to remove acid gases which are co2 and the like. The residual water and the undesired oxygenate are finally removed on a sorbent before the compressed effluent stream E' is fed to a distillation column T1 equipped with a reboiler and a condenser. An ethylene-containing composition C 1 is separated at the top of the distillation column T1 from -24 to 201247595 and a fraction 富1 enriched in a compound containing at least 3 carbon atoms is separated at the bottom of the distillation column. The ethylene-containing composition C 1 is then subjected to an acetylene-saturated AS 1 before being fed to a demethanized distillation column DM1 equipped with a reboiler and a condenser. A fraction L 1 enriched with a compound lighter than ethylene is separated at the top of the demethanized distillation column DM1 and the ethylene-containing composition C1" is separated at the bottom of the demethanized distillation column. According to the invention The preferred second embodiment of the method will now be described with reference to Figure 2 attached to the present description. Ethylene and other components containing the process from monooxygenate to olefin (preferably MTO) will have been subjected to one The effluent stream E of the conventional treatment (cooling, quenching and removal of the produced condensate) is subjected to a pre-conditioning treatment PCT by compression in a compressor while removing the produced condensate, and performing a city washing to remove CO 2 and the like therein. Acid gas of the product. The residual water and the undesired oxygenate are finally removed on a sorbent before the compressed effluent stream E' is fed to a distillation column T2 equipped with a reboiler and a condenser. A fraction F2 is separated at the top of the distillation column T2 and a fraction H2 enriched with a compound containing at least 4 carbon atoms is separated at the bottom of the distillation column T2. The fraction F2 is sent to the fraction a distillation column T2' having a reboiler and a condenser. The ethylene-containing composition C2 is separated at the top of the distillation column T2' and a fraction H2' rich in a compound containing at least 3 carbon atoms is The bottom of the distillation column T2' is separated. The ethylene-containing composition C2 is then subjected to a B-25-201247595 alkyne saturation AS2 before being fed to a demethanization distillation column DM2 equipped with a reboiler and a condenser. A fraction L2 enriched in a compound lighter than ethylene is separated at the top of the demethanized distillation column DM2 and the ethylene-containing composition C2" is separated at the bottom of the demethanized distillation column. A preferred third embodiment of the method according to the invention will now be described with reference to Figure 3 attached to the present description. The effluent stream E containing the ethylene and other components from the process of the monooxygenate to the olefin (preferably MTO) and which has been subjected to a conventional treatment (cooling, quenching and removal of the produced condensate) is subjected to a compression The compression in the machine is subjected to a preconditioning treatment PCT while removing the produced condensate, and performing a city washing to remove the acid gas which is C 02 and the like. The residual water and the undesired oxygenate are finally removed on a sorbent before the compressed effluent stream E' is fed to a distillation column T3 equipped with a reboiler and a condenser. A fraction F3 is separated at the top of the distillation column T3 and a fraction F3' is separated at the bottom of the distillation column T3. The fraction F3' is sent to a distillation column T3' equipped with a reboiler and a condenser. A fraction F3" is separated at the top of the distillation column T3' and a fraction H3 enriched with a compound containing at least 4 carbon atoms is separated at the bottom of the distillation column T3'. The fractions F3 and F3 are sent to the equilibration a distillation column T3" having a reboiler and a condenser. An ethylene-containing composition C3 is separated at the top of the distillation column T3" and a fraction H3' is enriched in a compound containing at least 3 carbon atoms. The bottom of the distillation column T3' is separated. The ethylene-containing composition C3 is then subjected to an acetylene-saturated AS3 before being fed to a demethanization distillation column DM3 equipped with a reboiler and a condenser. A fraction L3 enriched in a compound lighter than ethylene is separated at the top of the demethanization -26-201247595 distillation column DM3 and the ethylene-containing composition C3" is separated at the bottom of the demethanization distillation column. The invention further relates to a process for the production of at least one ethylene derivative compound starting from an ethylene-containing composition according to the invention. For the purposes of the present invention, the expression "at least one ethylene derivative compound" is understood to mean that one can be produced. Or more than one ethylene derivative compound: It is preferred to produce an ethylene derivative compound. The expression "ethylene derivative compound", used in the singular or plural form, is understood to mean, for the purposes of the present invention, Any ethylene derivative compound produced directly from ethylene together with any compound derived therefrom. The expression "ethylene derivative compound produced directly from ethylene", used herein in the singular or plural, is understood to mean For the purpose of the invention, any compound made directly from ethylene. The expression "a compound derived therefrom" As used herein, in the singular or plural, it is understood to mean any compound made from a compound made of ethylene itself for the purposes of the present invention, together with any compound derived therefrom. Examples of ethylene derivative compounds may, inter alia, mention: ethylene oxide, linear alpha olefins, homopolymers and copolymers of linear primary alcohols 'ethylene, ethylbenzene, vinyl acetate, acetaldehyde, ethanol Propionaldehyde and EDC. As examples of such compounds derived therefrom, mention may be made, inter alia, of -27-201247595 - ethylene glycols and ethers made from ethylene oxide - - made of ethylbenzene Styrene and styrene polymers derived from styrene, - VC manufactured by EDC, - vinylidene chloride derived from VC, fluorinated hydrocarbons, and PVC, and fluorinated polymers derived from fluorinated hydrocarbons, And - polyvinylidene chloride derived from vinylidene chloride and fluorinated hydrocarbons (and fluorinated polymers). Production of at least one ethylene derivative starting from the ethylene-containing composition according to the invention The method of the compound is preferably a process for producing ethylene oxide, ethylbenzene and/or EDC (as an ethylene derivative compound which is directly produced from ethylene) together with any compound derived therefrom. The expression "and/or" The method may be a method for producing only one of the above-mentioned derivative compounds or a method for producing a combination of two or three of the above ethylene derivative compounds. More preferably, according to the present invention The ethylene-containing composition begins to produce at least one ethylene derivative compound. Preferably, the method for producing ethylbenzene and/or EDC (as an ethylene derivative compound produced directly from ethylene) together with any compound derived therefrom Preferably, the method of producing at least one ethylene derivative compound from the ethylene-containing composition according to the present invention is preferably a process for producing EDC (as an ethylene derivative compound which is directly produced from ethylene). Along with the method of any compound derived therefrom, preferably VC and then PVC » 28-201247595 Accordingly, the present invention One object is a process for the manufacture of dichloroethane, according to which the ethylene-containing composition according to the invention (as defined above) is subjected to monochlorination and/or monooxychlorination to produce dichlorochloride. Ethane. The chlorination reaction (commonly referred to as direct chlorination) is advantageously carried out in a liquid phase (preferably predominantly EDC) containing a dissolved catalyst (e.g., FeCl3 or other Lewis acid). It is possible to advantageously combine this catalyst with a cocatalyst such as an alkali metal chloride. Good results have been given - a complex of FeCl3 and LiCl (lithium tetrachloroferrate - as described in patent application NL 690 1 3 98) ° The amount of FeCl3 used is advantageously per kg The liquid masterbatch is approximately g3 g to 30 g of FeCl3. The molar ratio of FeCl3 to LiCl is advantageously in the order of 0.5 to 2. Further, the chlorination reaction is preferably carried out in a chlorinated organic liquid medium. More preferably, the chlorinated organic liquid medium, also referred to as liquid masterbatch, consists essentially of EDC. The chlorination reaction according to the present invention is advantageously carried out at a temperature between 30 ° C and 150 ° C. Regardless of the pressure, good results have been obtained at temperatures below the boiling point (chlorination process under low temperature cooling conditions) and at the boiling point itself (the process of chlorination at the boiling point). When the chlorination process according to the invention is a chlorination process under supercooling conditions, good results are obtained by operating at a temperature below and at a pressure in the gas phase, which temperature is advantageously higher than or equal to 5 0 ° C and preferably -29 - 201247595 is higher than or equal to 60. (:, but advantageously lower than or equal to 8 〇〇 C and preferably lower than or equal to 7 〇. (:, and the pressure is advantageously higher than or equal to 1 and preferably higher or equal to absolute The pressure 'but advantageously less than or equal to 20, preferably less than or equal to 1 Torr and particularly preferably less than or equal to 6 bar absolute. The method of chlorination at the boiling point may preferably be effectively recovered. The heat of reaction. In this case, the reaction advantageously occurs at a temperature higher than or equal to 60 ° C. Preferably, it is higher than or equal to 7 〇. (: and particularly preferably higher than or equal to 85 〇C, but advantageously lower than or equal to i50 ° C and preferably lower than or equal to 135. (:, and the pressure in the gas phase is advantageously higher than or equal to 〇.2, preferably high Particularly preferred at or equal to 0.5' is greater than or equal to 1.1 and more particularly preferably greater than or equal to 1.3 bar absolute, but advantageously less than or equal to 1 〇 and preferably less than or equal to 6 Bar absolute pressure. The chlorination process can also be a hybrid loop-cooled process of chlorination at the boiling point. The expression "mixing loop cooling process of chlorination at boiling point" is understood to mean a process in which, for example, by immersing in the reaction medium An exchanger either cools the reaction medium by a circuit circulating in an exchanger while producing at least the amount of EDC formed in the gas phase. Advantageously, the reaction temperature and pressure are adjusted to produce The EDC exits in the gas phase and removes residual heat from the reaction medium by exchanging the surface area. The chlorinated ethylene-containing composition and also the molecular chlorine (either pure or diluted) can be used by any known equipment. The reaction medium is introduced -30-201247595 together or separately. It may be advantageous to separately introduce an ethylene-containing composition subjected to chlorination to increase its partial pressure and promote its dissolution' which usually constitutes a limiting step of the process. Ethylene is added in a sufficient amount to convert most of the chlorine 'and does not require the addition of excess chlorine. The ethylene/chlorine ratio used is preferably at 1 Between .2 mol/mol and 0.8 mo丨/mol, and particularly preferably between 1.05 mol/mol and 0.95 mol/mol. The chlorinated product obtained mainly contains EDC and also a small amount of by-products, for example 1,1,2-trichloroethane or a small amount of chlorinated product of ethane or methane. The EDC obtained by separating the product stream from the chlorination reactor is carried out according to known methods, and overall It is possible to utilize the heat of the chlorination reaction. It is then preferably carried out by condensation and gas/liquid separation. Then advantageously the unconverted product (methane, ethane, carbon monoxide, nitrogen, Oxygen and gas) are subjected to an easier separation than is necessary to separate pure ethylene starting from the initial mixture. The oxychlorination reaction is advantageously carried out in the presence of a catalyst comprising an active element comprising copper deposited on an inert support. The inert carrier is advantageously selected from the group consisting of alumina, silicone, mixed oxides, clays, and other carriers of natural origin. Alumina constitutes a preferred inert carrier. Preferred are catalysts comprising an active element, the number of active elements being advantageously at least two, one of which is copper. In the above -31 - 201247595 active elements other than copper, 'alkali metal, alkaline earth metal, rare earth metal and metals selected from the group consisting of nails, rhodium, palladium, starvation, rhodium, platinum may be mentioned. And gold. Catalysts comprising the following active elements are particularly advantageous: copper/magnesium/potassium, copper/magnesium/sodium; copper/magnesium/lithium, copper/magnesium/planing, copper/magnesium/sodium/lithium, copper/magnesium/potassium/lithium And copper / magnesium / planer / lithium, copper / magnesium / sodium / potassium, copper / magnesium / sodium / planing and copper / magnesium / potassium / planing. Most particularly preferred are the catalysts described in the patent applications EP-A 2 5 5 1 5 6 , ΕΡ Α 494 474, EP-A 657 212 and EP-A 657 213, the disclosures of which are incorporated by reference. The content of copper, calculated in the form of metal, is advantageously between 30 g/kg and 90 g/kg, preferably between 40 g/kg and 80 g/kg and particularly preferably Between 50 g/kg and 70 g/kg of catalyst. The magnesium content, calculated as metal, is advantageously between 1 〇g/kg and 30 g/kg, preferably between 12 g/kg and 25 g/kg and particularly preferably at 15 Between g/kg and 20 g/kg of catalyst. The content of alkali metal, calculated as metal' is advantageously between 0.1 g/kg and 30 g/kg, preferably between 〇5 g/kg and 20 g/kg and particularly preferably It is between 1 g/kg and 15 g/kg of catalyst. Copper: Magnesium: The atomic ratio of one or more metal is advantageously 1:0·1·2: 0.05-2, preferably 1:0.2-1.5: 0.1-1.5 and particularly good Is 1:0.5-1: 0.15-1° The catalyst has a specific surface area advantageously between 25 m2/g and 300 m2/g, preferably between 50 m2/s and 200 m2/g and It is particularly preferred to be between 75 m2/g and 175 m2/g (measured by nitrogen according to the BET method). -32-201247595 The catalyst can be selected in a fixed bed or a fluidized bed. of. The oxychlorination process operates within the scope of the reaction. The temperature is advantageously at 150 ° C, preferably between 200 ° C and 275 ° C and up to 25 5 ° C. The pressure is advantageously above atmospheric pressure. 1 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値 値This pressure is adjusted to obtain a constant pass rate in the reactor that is optimally maintained at different operating speeds. Typically from 1 second to 60 seconds, and preferably from 1 sec., the source of oxygen for oxychlorination may be air, a mixture, preferably pure oxygen. These reactants can be separated from other reactants by any known means of safety. These safety factors also require that the leaving or recirculating body mixture be maintained at the pressures and temperatures in question. It is preferred to maintain a so-called enriched mixture which contains too little oxygen for the fuel to be ignited. In the case where the compound has a wide range of flammability, the sufficient presence of hydrogen > 5 vol%) will constitute a deficiency in the ratio of hydrogen chloride/oxygen used advantageously between 6 mol/mol. The ethylene/hydrogen chloride ratio is between mol/mol and 0.6 mol/mol. The obtained chlorinated product mainly contains EDC and is used. The second usually recommended condition and between 300 ° C, preferably from 215 ° C at 2 bar absolute 値 , at 4 bar absolute 可以 force can be effectively timed and maintained for a residence time range of up to 40 seconds. Pure oxygen or one of them is introduced into the bed. It is generally advantageous to limit the flammability of the gas to the reactor, that is to say in this respect (> 2 vol%, compared to i. at 3 mol/mol and advantageously at 0.4) There is also a small amount of by-product -33-201247595, such as 1, 1,2-trichloroethane. EDC separated from the product stream from the chlorination reactor can be chlorinated from the oxychlorination before the EDC cracking step. The EDC separated in the product stream of the reactor is mixed or unmixed. When the two EDCs are mixed, they may be mixed completely or partially. Therefore, a method for producing dichloroethane (according to the method according to the method) The inventive ethylene-containing composition (as defined above) is subjected to monochlorination and/or monooxychlorination to produce dichloroethane. It is further characterized in that it preferably comprises heat of dichloroethane. The solution can be used to produce vinyl chloride. The EDC can then undergo an EDC pyrolysis (also known as cracking) to produce vinyl chloride (VC) and hydrogen chloride. The conditions under which the EDC cracking step can be carried out are known to those skilled in the art. EDC cracking May be in the presence or absence of a third compound It is possible to carry out the catalysts mentioned in the third compounds; EDC cleavage in this case is a catalytic EDC cleavage. However, EDC cleavage is preferably in the presence of a third compound and only in the action of heat. The EDC cracking is often referred to as pyrolysis in this case. The pyrolysis is advantageously obtained by a reaction in the gas phase in a tube furnace. The usual pyrolysis temperature is 400 ° C. And between 600 ° C, preferably between 480 ° C and 540 ° (range between 3). The residence time is advantageously between 1 second and 60 seconds, preferably from 5 seconds to 25 The range of seconds. In order to limit the formation of by-products and the contamination of the furnace tubes, the conversion of the EDC is advantageously limited to between 45% and 75%. Separation of VC and from the product stream obtained from pyrolysis Hydrogen chloride system - 34 - 201247595 is carried out according to known means using any known means to collect purified VC and hydrogen chloride. After purification, unconverted EDC is advantageously sent to the pyrolysis furnace. Method of dichloroethane (according to the method, the ethylene-containing combination according to the invention (as defined above) subjected to monochlorination and/or monooxychlorination to produce dichloroethane) is further characterized in that it preferably comprises pyrolysis of dichloroethane to produce vinyl chloride, more Preferably, it is characterized in that it further comprises a polymerization reaction of vinyl chloride to produce polyvinyl chloride. The manufacture of PVC may be a bulk 'solution or aqueous dispersion polymerization method, which is preferably an aqueous dispersion polymerization method. Aqueous dispersion polymerization is understood to mean free-radical polymerization in aqueous suspensions and free-radical polymerization in aqueous emulsions, as well as in aqueous microsuspensions. The expression of free-radical polymerization in aqueous suspensions is understood to mean Refers to any free radical polymerization process in an aqueous medium in the presence of a dispersant and an oil soluble free radical initiator. The expression of free radical polymerization in an aqueous emulsion is understood to mean any free radical polymerization process in the presence of an emulsifier and a water soluble free radical initiator in an aqueous medium. The expression of aqueous microsuspension polymerization (also referred to as polymerization in a homogenized aqueous dispersion) is understood to mean the use of oil-soluble initiators and the preparation of monomers in the presence of emulsifiers due to strong mechanical agitation and in the presence of emulsifiers. Any free hydrazine polymerization process under the conditions of droplets of the emulsion. -35- 201247595 An advantage of the present invention is that it allows an ethylene-containing composition to be obtained at a reduced cost. Another advantage of the present invention is that an ethylene-containing composition having a purity lower than that of the polymerization grade is obtained. It is of interest to obtain an ethylene-containing composition which can comprise different types of impurities and which is at a level which is not prohibited for its future use. Furthermore, for obtaining an ethylene-containing combination according to the invention The thermal power required for the material is significantly reduced compared to the ethylene obtained to achieve the polymerization grade. Finally, the total ethylene recovery obtained for the ethylene-containing composition according to the present invention is significantly higher than that obtained for the polymerization grade, if any of the patents, patent applications, and The disclosure of the disclosure conflicts with the description of the present application to the extent that it may make a term unclear, and the description should be preferred. [Embodiment] The following β examples are intended to illustrate the invention, but are not intended to limit the scope thereof.

These examples are based on the description of ASPEN PLUS® ASPENONE® V7.2 software from ASPEN TECHNOLOGY INC, Wheeler Road 200, Burlington, MA, USA. The ASPENONE® V7.2 database of pure components and mixtures is calculated. -36- 201247595 Example 1 (according to the invention) An effluent stream E having an ethylene and other constituents containing a process from methanol to olefin and having undergone a conventional treatment (cooling, quenching and removal of condensate produced) has The detailed composition given in Table 1 a below. The effluent stream E was subjected to the ASPEN PLUS® ASPENONE® V7.2 software analogy described below and graphically depicted in FIG. The molar flow rate is 29.1 56 kmol/h, of which 1 3.476 kmol ethylene/h. The temperature of the effluent stream E was 40 ° C at the inlet of the process and its absolute pressure was 2.5 bar. The effluent stream E is then cooled to a temperature of 40 ° C at the outlet by first compressing to an absolute pressure of 20 bar in a 3-stage compressor equipped with an interstage cooler between each stage. At the same time, the condensate produced is removed. A city washing liquid for removing acid gases in which CO 2 and the like are introduced is then introduced between the second and third stages of the compressor. The residual water and unwanted are added before the resulting compressed effluent stream E is fed to a distillation column T1 equipped with a reboiler and a condenser and comprising 20 theoretical stages including the reboiler and condenser. The oxygenate is finally removed on an adsorbent. The effluent stream E' is introduced to the 14th stage, the first stage is a condenser and the 20th stage is a reboiler. The ethylene-containing composition C1 having a mass reflux ratio fixed at 3.444.68 kg/h is separated at the top of the distillation column T1 (the outlet of the condenser) and is enriched with a compound having at least 3 carbon atoms. Fraction H1 is separated at the bottom of distillation column T1. The absolute pressure at the top and bottom of distillation column T1 is fixed at 20 bar. The temperature at the top of the steaming tower T1 (outlet of the condenser) at -37-201247595 is estimated to be _37.6 °C and the temperature at the bottom of the distillation column T1 is calculated to be 57.3 〇c. The mixture containing Cl was then heated to 50 ° C, mixed with q 474 kmol / h pure H 2 at 50 ° C and an absolute pressure of 20 bar and added to a deacetylation reactor ' It is subjected to an acetylene saturation AS 1 which is subjected to adiabatic action. The conversion rate of acetylene is estimated to be 99%, the selectivity of ethylene is estimated to be 6 0.1%, and the selectivity of hospital is estimated to be 39.9%. After deacetylation, the resulting ethylene-containing composition C1 is cooled to -30.7 ° C and added to a reboiler and a condenser and includes 20 theoretical stages (including the reboiler and condensation) - in the demethanization distillation column DM1. The ethylene-containing composition C1' was introduced to the 15th stage, the first stage was a condenser and the 20th stage was a reboiler. The mass reflux ratio of the demethanized distillation column was fixed at 10. A fraction L1 enriched in 63 kg/h of ethylene lighter compound is separated at the top of the demethanation distillation column DM1 (outlet of the condenser) and the ethylene-containing composition C1" is demethanized. The bottom of the distillation column is separated. The absolute pressure at the top and bottom of the demethanization distillation column is fixed at 20 bar. The temperature at the top of the demethanization distillation column (the outlet of the condenser) is estimated to be -1〇7.6°. C and the temperature at the bottom of the demethanization distillation column is calculated to be -29.2 ° C. The characteristics of the effluent streams E and E' of the ethylene-containing composition containing the compositions Cl, Cl' and Cl" along with the fractions HI and L1 are shown in the table. Given in la. The amount of inert gas, hydrogen, methane, CO 2 , acetylene, ethylene, ethane, propylene, other C 3 , C 4 , C 5 , H 20 , oxygenates and the total amount expressed as % by volume, except those in brackets, They are PPm by volume. -38- 201247595 rum 0.67 0.42 98.91 S 1—^ /-**V Ο r—N o /^-*S 'no /—V 〇/—»N 1—H rH /—N /·*—v T —H 100.00 3.921 63.00 -107.6 20.0 5 /*—V o /^S Ο /**~Ν Ο /—Ν Co" 〇\ 's—^ I 0.13 0.02 79.33 vq 14.07 4.60 /*—N 0.17 100.00 10.472 475.08 57.3 20.0 U /«—so χ—V ο 0.30 cK I 98.68 p /—N o /-vr—^ /*—v 100.00 13.617 381.79 -29.2 20.0 99.69 98.99 u 0.15 0.09 22.35 /*—S •o 76.62 0.79 / —N o /-V 1—H /-—S /—N 1—^ 100.00 17.538 444.79 -30.7 20.0 77.41 98.98 1—» 0.15 0.00 22.37 0.15 76.60 0.73 so /—VV 1— H /—*s 1—^ ιοο.οοΠ 17.522 444.68 -37.6 20.0 77.48 98.86 w 0.09 0.00 14.00 /—Ν 1—Η 0.10 47.99 0.46 29.68 0.62 5.27 1.72 V 0.06 100.00 27.994 919.76 40.0 20.0 w 0.09 0.00 13.45 0.03 0.09 46.22 0.45 28.80 0.61 5.22 1.66 2.87 0.50 100.00 29.156 947.29 40.0 in inert gas (calculated as N2) hydrogen methane C〇2 acetylene ethyleneethane propylene other C3 (calculated as propane) C4 (calculated as n-butene) C5 (calculated as n-pentene) H20 Oxygenate (calculated as methanol) Total i Molar flow rate (km〇l/h) Mass flow rate (kg/h) Temperature (°c) Absolute pressure (bar) Total ethylene, Ethane, acetylene (% by volume) capacity S N3 遁K] f loaded K1 ϋΐΐπ system i N3 -39- 201247595 The molar flow rate of the ethylene-containing composition Cl" reaches 13.617 kmol / h, of which 13.437 kmol ethylene / h. The total ethylene (ethylene in Cl / effluent E) recovery was 9 9.71%. The ethylene content of the ethylene-containing composition C1" reached 98.68% by volume and ethylene and total ethylene, The ratio of ethane to acetylene is 98.99%. The acetylene content in the ethylene-containing composition C1" reached 19.4 ppm by volume and the propylene content in the ethylene-containing composition C1" reached 0.3 ppm by volume. The calculated heat power in the reboiler of distillation column T1, and the power in the reboiler of the demethaniser DM1 are given in Table 2. The heat consumption rate in the ethylene-containing composition C1" reached 0.264 kWh/kg. Example 2 (Comparative Example) The same effluent stream E as in Example 1 was treated in the same manner as in Example 1. After that The ethylene-containing composition C1" was sent to an ethylene splitter S1 equipped with 40 theoretical stages including a reboiler and a condenser. The ethylene-containing composition C 1 " is introduced onto the first stage, the first stage is a condenser and the 40th stage is a reboiler. The mass reflux ratio of the column is fixed at 5. Ethylene-containing and enriched ratio The 36 〇〇〇kg/h fraction of the ethylene light compound is separated at the top of the ethylene splitter S1 (the outlet of the condenser) and still contains the saturated H1 of the B-boiled Fuyuan, in the B-disruptor The bottom of the si is separated. The absolute pressure at the top and bottom of the ethylene splitter S1 is fixed at 20 bar. The temperature at the top of the ethylene splitter s (the outlet of the condenser) is estimated to be -28.9. (: and the ethylene The temperature at the bottom of the splitter Si -40 - 201247595 is calculated as -25.4 〇C:. The fraction containing ethylene and enriched with lighter than ethylene is then sent to the tower DL 配备 equipped with 2 theoretical stages (to improve Separating a compound that is lighter than B) from the storage to produce a polymerization grade of B. The feed is introduced to the bottom of the column. The mass reflux ratio is fixed at 100. 4 kg/h of fraction L1. The top of the column (the outlet of the condenser) is separated and polymerized The graded ethylene C1" is separated at the bottom of the column. The absolute pressure at the top and bottom of the column is fixed at 2 bar. The temperature at the top of the distillation column DL1 (the outlet of the condenser) is estimated to be -37.5°. C and the temperature at the bottom of the distillation column DL1 is calculated to be _28.9 ° C. The characteristics of the polymerization grade of ethylene C 1 "' along with the fractions ' 1 ' and L 1 ' are given in Table 1 b. Inert gas, hydrogen, A hospital, C〇2 'acetylene, ethylene, ethane, propylene, other 匚3, 〇4'〇5, 仏0, the amount of oxan and the total amount expressed as % by volume 'except in brackets Those 'they are PPm by volume. -41 - 201247595 Table lb C1,,, ΗΓ L1, inert gas (calculated as N2) (<〇·!) (<〇·〇(<〇·!) Air (<〇·!) (<〇·〇(<〇·!) Methane 0.06 (<〇!) 21.48 C〇2 (<1) (<1) (<1) Acetylene (0.3) 0.03 (<〇·!) Ethylene 99.93 82.23 78.52 Ethane 0.02 17.73 (<〇·!) Propylene (<〇.1) (5.52) (<〇." Other C3 (as propane calculation ) (<0.1) (<〇·!) ( <〇.1) C4 (calculated as n-butene) (<1) (<1) (<1) C5 (calculated as n-pentene) (<1) (<1) (< 1) h2o (<1) (<1) (<1) Oxygenate (calculated as methanol) (<1) (<1) (<1) Total 100.00 100.00 100.00 Mohr flow rate (kmol /h) 12.693 0.767 0.157 Mass flow rate (kg/h) 356.00 21.79 4.00 Temperature (°C) -28.9 -25.4 -37.5 Absolute pressure (bar) 20.0 20.0 20.0 Total ethylene, ethane, acetylene (% by volume) 82.26 B Suspected/total ethylene, ethane, acetylene (%) 99.98 The molar flow rate of the polymerization grade of ethylene Cl"' reached 12.693 kmol/h, of which 1.684 kmolol ethylene/h. The total ethylene (E1 in ethylene / effluent E) recovery was 94.1 2%. The ethylene content of the polymerized anti-42-201247595 graded ethylene Cl"' reached 99 93 by volume. % and the ratio of ethylene to total ethylene, ethane, acetylene is 9 9 9 %. The acetylene content in the ethylene grade C1"' of the polymerization grade reached ο ppm by volume and the propylene content in C1"' was less than 〇 ppm by volume. Calculated thermal power in the reboiler of distillation column T1, and power in the reboiler of the demethanizer DM1, in the reboiler of the ethylene splitter Si and in the reboiler of the column DL1 The thermal power is given in Table 2. The heat rate of the polymerization grade of ethylene C1"' reached 0.855 kWh/kg. Table 2 Tower reboiler thermal power kW Example 1 Example 2 T1 77.309 77.309 DM1 23.628 23.628 S1 • 197.865 DLr 5.622 Total 100.937 304.424 From example 1 and According to the data of 2, the thermal power required to obtain the polymerization grade of ethylene C1"' seems to be greater than: 2. 2 times the heat power required to obtain the ethylene-containing composition ci". In addition, the total ethylene recovery from the above It appears that the ratio of ethylene to about 5.59% of ethylene is lost when the separation of ethylene from the effluent stream E is carried out on the polymerization grade of ethylene C1"' compared to the separation of the ethylene-containing composition C1". This lost ethylene can be recovered after spending more investment and energy. -43- 201247595 Example 3 (according to the invention) The same effluent stream E as in Example 1 (composition is given in Table 3a below) Subject to the ASPEN PLUS® ASPENONE® V7.2 software analogy described below and graphically in Figure 2. The Mohr flow rate is 29.156 kmol/h, of which 13.476 kmol is suspected/h. The temperature of the effluent stream E is in the process of The mouth is 40 ° C and its absolute pressure is 2.5 bar. After a pre-conditioning process PCT detailed in Example 1, the resulting compressed effluent stream E ' is added to a reboiler and a condenser and includes In a distillation column T2 of 20 theoretical grades (including the reboiler and condenser), the effluent stream E' is introduced to the first stage, the first stage is a condenser and the 20th stage is a reboiler. a fraction R2 of a mass reflux ratio fixed at 2.794.76 kg/h is separated at the top of the distillation column T2 (the outlet of the condenser) and a fraction H2 enriched with a compound having at least 4 carbon atoms in the distillation column T2 The bottom of the distillation column T2 is fixed at 20 bar. The temperature at the top of the distillation column τ 2 (the outlet of the condenser) is estimated to be - 8.5 ° C and the temperature at the bottom of the distillation column T2 Calculated as l 〇 7.5 ° C. Fraction F2 is sent to a replenishing column T2 ' equipped with a reboiler and a condenser and comprising 20 theoretical stages (including the reboiler and condenser). To level 10, the i-th system is condenser and the 20th a reboiler. The mass reflux ratio of the column is fixed at 3.445.00 kg / h of an ethylene-containing composition C2 separated at the top of the steaming tower T2' (the outlet of the condenser) and is enriched The fraction H2' of the compound - 44 - 201247595 of at least 3 carbon atoms is separated at the bottom of the distillation column T2'. The absolute pressure at the top and bottom of the distillation column T2 is fixed at 20 bar. The temperature at the top of the distillation column 2' (the outlet of the condenser) was estimated to be -37.6 °C and the temperature at the bottom of the distillation column T2' was calculated to be 48.6 °C. The ethylene-containing composition C2 is then heated to 50 ° C, mixed with 0.0528 kmol / h of pure H 2 at 50 ° C and an absolute pressure of 20 bar and added to a deacetylation reactor to Acetylene saturation AS2 undergoes adiabatic operation. The conversion of acetylene is estimated to be 99%, the selectivity of ethylene is estimated to be 60.1% and the selectivity of ethane is estimated to be 39.9%. After deacetylation, the resulting ethylene-containing composition C 2 is cooled to -30.7 ° C and added to a reboiler and a condenser and includes 20 theoretical stages (including the reboiler and condenser) ) in a demethanization distillation column DM2. The ethylene-containing composition C2' was introduced to the 15th stage, the first stage was a condenser and the 20th stage was a reboiler. The mass reflux ratio of the demethanized distillation column was fixed at 1 Torr. A fraction L2 enriched in 63 kg/h of ethylene lighter compound is separated at the top of the demethanized distillation column DM2 (outlet of the condenser) and the ethylene-containing composition C2" is demethanized The bottom of the distillation column is separated. The absolute pressure at the top and bottom of the demethanization distillation column is fixed at 20 bar. The temperature at the top of the demethanation distillation column (the outlet of the condenser) is estimated to be -107.6 °C and The temperature at the bottom of the demethanization distillation column was calculated to be -2 9.2 ° C. The characteristics of the ethylene-containing compositions C2, C2' and C2" along with the fractions F2, H2, H2' and L2 of the effluent streams E and E' are shown in Table 3a. Given in . Inert gas, hydrogen, methane, CO 2 , acetylene, ethylene, ethane, propylene, -45- 201247595 Others in terms of ppm C3, C4, % C5, H20, the amount of oxygenate and the total amount expressed as Except those in brackets, they are by volume -46- 201247595

Cj 0.67 0.41 98.91 /—N rH /-~N o /<—*so 、,〆—so \ o /-*s T—( /—Ν </^-*NT—< Τ-Ή / —s 1—^ 100.00 3.921 63.00 -107.6 20.0 Η2, s ο /—Ν 〇/--N 〇/*—N d 0.04 98.12 00 Ν. r-^ /*—Ν s 1—Η 0.01 100.00 8.306 丨349.76 48.6 20.0 (Ν ffi /-Ν ο / -S rH Ο /--N o /—N y-—S o kl3_ 0.06 7.33 o 68.39 22.38 /—S 1—^ 0.80 100.00 2.155 丨125.00 107.5 20.0 <Ν Uh 0.10 /^―Ν d 15.17 S 0.10 52.00 0.50 31.54 0.58 /—Ν Ν /—Ν /—s ι·*Η 100.00 25.839 丨794.76 od 20.0 d rH o 0.30 /*—S 5 s^/ 98.69 1.00 〇/— Ν ^•Η /—Ν 1—^ /—N /—N 100.00 13.628 丨382.11 -29.2 20.0 98.69 99.00 0.15 0.09 22.34 /--s -N 76.64 0.78 /—sso /-Ν rH /—Ν /-*- v 100.00 17.550 445.11 -30.7 20.0 77.42 98.99 <Ν U 0.15 o 22.36 /—N 1—H 0.15 76.62 0.72 r—N o /-s /"ν /*—S i—H /—*S 1—H 100.00 17.534 445.00 -37.6 20.0 1 77.49 98.88 w 0.09 /—NT—H o 14.00 /—ST—· 0.10 47.99 0.46 29.68 0.62 5.27 1.72 /*—N 0.06 100.00 27.994 919.76 40.0 20.0 ω 0.09 /—N »—H o 13.45 0.03 0.09 46.22 0.45 28.80 0.61 5.22 1.66 2.87 0.50 100.00 29.156 947.29 40.0 oi Inert gas (calculated as N2) Hydrogen methane C02 Acetylene Ethane propylene Other C3 (calculated as propane) C4 (calculated as n-butene) C5 (calculated as n-pentene) H2 oxime oxime (calculated as methanol) Total molar flow rate (kmol/h) 1 |rv| a !» Temperature (°c) Absolute pressure (bar) Total ethylene, ethane, acetylene (% by volume) Ethylene/total ethylene, ethane, acetylene (%) -47- 201247595 The ethylene-containing composition C2" The molar flow rate reaches i 3 628 km 〇i/h, of which 13.449 kmol is ethylene. The total ethylene (ethylene in the C2" / ethylene in the effluent stream E) has a recovery of 99.80%. The ethylene content of the ethylene-containing composition C 2 " reaches 98.69% by volume and ethylene and total ethylene The ratio of ethane to acetylene is 99.00%. The acetylene content in the ethylene-containing composition C2" reached 19 4 ppm by volume and the propylene content in the ethylene-containing composition C2" was less than 5% by volume. The calculated thermal power in the reboilers of distillation columns T2 and T2', and the power in the reboiler of the demethanizer DM2 are given in Table 4. The heat loss rate of the ethylene-containing composition C2" reached 0.674 kwh/kg. Example 4 (Comparative Example) The same effluent stream E as in Example 3 was treated in the same manner as in Example 3. After that, The ethylene-containing composition C2" was sent to an ethylene splitter S2 (including a reboiler and a condenser) equipped with 40 theoretical stages. The ethylene-containing composition C2" is introduced to the first stage, the second stage is a condenser and the 40th stage is a reboiler. The mass reflux ratio of the column is fixed at 5. The ethylene is contained and the specific ethylene is enriched. A fraction of 360.00 kg/h of the light compound is separated at the top of the ethylene splitter S2 (the outlet of the condenser) and the ethylene-rich fraction H2" still separated at the bottom of the ethylene splitter S2. The absolute pressure at the top and bottom of the ethylene splitter S2 is fixed at 2 bar. The temperature at the top of the ethylene splitter S2 (the outlet of the condenser) was estimated to be -28.9 ° C and the temperature at the bottom of the ethylene splitter S2 was calculated to be -25.5 °C. The fraction containing ethylene and enriched in lighter than ethylene, -48-201247595, is then sent to a 20-theoretical "column dl2 (to further separate compounds lighter than ethylene) to produce a polymerization grade. Ethylene. This feed is introduced to the bottom of the column. The mass reflux ratio fixed at 100. 4 kg/h of fraction L2' was separated at the top of the column (the outlet of the condenser) and a polymerization grade of ethylene C2, ' was separated at the bottom of the column. The absolute pressure at the top and bottom of the tower is fixed at 20 bar. The temperature at the top of the distillation column DL2 (the outlet of the condenser) was estimated to be -37.5 °C and the temperature at the bottom of the distillation column DL2 was calculated to be -28.9 °C. The characteristics of this polymerization grade of ethylene C2" along with fractions H2" and L2' are given in Table 3b below. The amount of inert gas, hydrogen, methane, CO 2 , acetylene, ethylene, ethane, propylene, other C 3 , C 4 , C 5 , H 20 , oxygenates and the total amount expressed as % by volume, except those in brackets, They are Ppm by volume. -49- 201247595 Table 3b C2'" H2" L2, inert gas (calculated as N2) (<〇·!) (<0.1) (<〇.1) Hydrogen (<〇·!) (< 〇·!) (<0.1) Methane 0.06 (<0.1) 21.48 C〇2 (<1) (<1) (<1) Acetylene (03) 0.03 (<0.1) Ethylene 99.93 82.62 78.52 B Alkane 0.02 17.35 (<0.1) Propylene (<0.1) (5.4) (<0.1) Other C3 (calculated as propane) (<0.1) (<0.1) (<0.1) C4 (as n-butene) Calculation) (<1) (<1) (<1) C5 (calculated as n-pentene) (<1) (<1) (<1) h2o (<1) (<1 (<1) Oxygenate (calculated as methanol) (<1) (<1) (<1) Total 100.00 100.00 100.00 Molar flow rate (kmol/h) 12.693 0.778 0.157 Mass flow rate (kg/h) 356.00 22.11 4.00 Temperature (〇C) -28.9 -25.5 -37.5 Absolute pressure (bar) 20.0 20.0 20.0 Total ethylene, ethane, acetylene (% by volume) 99.95 Ethylene / total ethylene, ethane, acetylene (%) 99.98 The polymerization rate of the ethylene C2"' molar flow rate reached 12.693 kmol / h, of which 12.684 kmol ethylene / h. total ethylene (C2,,, The ethylene in the ethylene/outflow stream E) recovery rate reached 94.12%. The ethylene content of the polymerization grade of ethylene C2"' reached 99.93% by volume and the ratio of ethylene to total ethylene, ethane, acetylene was 9 9 · 9 8 %. The acetylene content of the polymerization reaction grade ethylene C2"' reached 0.3 ppm by volume and the propylene content in the fraction C2"' was less than 0.1 ppm by volume. Calculate the thermal power in the reboiler of distillation column T2 and T2' from -50 to 201247595, the power in the reboiler of the demethanizer DM2, the reboiler in splitter S2 and the DL2 in the column The thermal power in the reboiler is given in Table 4. The heat rate of ethylene C 2 ′′ of this polymerization grade reached 1.2 9 6 k Wh/kg. Table 4 Tower boiling heat power kW Example 3 Example 4 T2 138.051 138.051 T25 95.967 95.967 DM2 23.601 23.601 S2 - 198.046 DL2 - 5.622 Total 257.619 461.287 It can be seen from the data of Examples 3 and 4 that the thermal power required to obtain the ethylene grade C2"' of the polymerization grade appears to be greater than 1.9 times the thermal power required to obtain the ethylene-containing composition C2" Furthermore, from the above-mentioned total ethylene recovery rate, it seems that the loss of ethylene from the effluent stream E is carried out when the polymerization grade ethylene C2"' is separated from the ethylene-containing composition C2". About 5.68% of ethylene. This lost ethylene can be recovered after spending more investment and energy. Example 5 (according to the invention) The same effluent stream E as in Example 1 (composed in Table 5a below) The method of the ASPEN PLUS® AS PEN ONE® V7.2 software analogy described below is shown and graphically depicted in Figure 3. The Mohr flow rate is 29. 56 -51 - 201247595 kmol/h, of which 13.476 kmol ethylene / h. The flow The temperature of stream E is 40 ° C at the inlet of the process and its absolute pressure is 2.5 bar. After a pre-conditioning process PCT detailed in Example 1, the resulting compressed effluent stream E' is added to the equipment. a boiling vessel and a condenser and including 20 theoretical stages (including the reboiler and condenser) in the distillation column T3" introduces the effluent stream E' to the first stage, the first stage is the condenser and the 20th The stage reboiler. The mass reflux ratio of the column is fixed at 2. One 419.76 allows the 8/11 fraction 3 to be separated at the top of the distillation column 3 (condenser outlet) and a fraction F3' in the distillation column T3 The bottom is separated. The absolute pressure at the top and bottom of the distillation column T3 is fixed at 20 bar. The temperature at the top of the distillation column T3 (the outlet of the condenser) is estimated to be -38.2 ° C and the temperature at the bottom of the distillation column T3 is calculated to be 45.7. C. The fraction F3 is sent to a distillation column T3' equipped with a reboiler and a condenser and comprising 20 theoretical stages including the reboiler and condenser. The fraction F3' is introduced to the 10th stage. , the first level is the condenser and the 20th level is The mass reflux ratio of the column is fixed at 2.375.00 kg/h of a fraction F3" separated at the top of the distillation column T3' (the outlet of the condenser) and enriched with a compound containing at least 4 carbon atoms. Fraction H3 is separated at the bottom of distillation column T3'. The absolute pressure at the top and bottom of the distillation column T3 is fixed at 20 bar. The temperature at the top of the distillation column T3' (the outlet of the condenser) was estimated to be 44.3. (: and the temperature at the bottom of the distillation column T3' is calculated as 10 7.3 C. The tanks F3 and F3 are sent to a reboiler and a condenser and include 20 theoretical stages (including the reboiler and condensation) 1-52-201247595 distillation column Τ 3 ". The fractions F 3 and F 3 " are introduced to the 10th stage, the first system condenser and the 20th stage reboiler. The mass reflux ratio of the column An ethylene-containing composition C3 at 3.445.00 kg/h is separated off at the top of the distillation column (outlet of the condenser) and a fraction H3' enriched with a compound containing at least carbon atoms is at the bottom of the distillation column T3" The absolute pressure at the top and bottom of the distillation column T3" is fixed at 20 at the top of the distillation column T3" (the outlet of the condenser). The temperature is estimated to be -37.6 ° C and the temperature at the bottom of the distillation column T3" is calculated to be 48.6 ° C. The ethylene-containing composition C3 is then heated to 50 ° C and mixed with 0 kmol / h of pure H 2 at 50 ° C and an absolute pressure of 20 bar to a deacetylation reactor to Acetylene saturation is attenuated AS3. The conversion of acetylene is estimated to be 99%. It is estimated to be 60.1% and the selectivity of ethane is estimated to be 39.9%. After deuteration, the resulting ethylene-containing composition C3 is cooled to -30.7 ° C and added to a reboiler and a condenser. 20 derivatization distillation column DM3 of the theoretical stage (including the reboiler and condenser). The ethylene-containing composition C3' is introduced to the crucible stage, the first stage is a condenser and the 20th stage is Boiling. The mass reflux ratio of the deuterated distillation column is fixed at 10. A fraction L3 enriched with 63 kg/h of the compound of B is separated at the top of the demethanated steamed DM3 (the outlet of the condenser). And the vinylate-containing C3" is separated at the bottom of the demethanization distillation column. The absolute pressure at the top and bottom of the deuteration distillation column is fixed at 20 bar. The top of the demethanization distillation column (condenser) The temperature of the outlet) is estimated to be 1 fixed T3, 3 out. Bar. • 0528 and one of the selected group of methane and methane 15 methaneene light ends of the group methane is -53- 201247595 -l〇 7.6 〇C and the thermometer at the bottom of the demethanization distillation column Calculated as -29.2 ° C. The characteristics of the ethylene-containing compositions C3, C3, and C3" along with the effluent streams E and E' of the fractions F3, F3', F3,, H3, H3' and L3 are given in Table 5a. Exhaust gas, hydrogen, methane, CO 2 , acetylene, ethylene, ethane, propylene, other C 3 , C 4 , C 5 , H 20 , the amount of oxygenate and the total amount expressed as % by volume 'except in brackets Those 'they are PPm by volume» -54- 201247595 2 0.67 0.41 98.91 /—s /—N t /—·s c> »«—V Ο /—Ν Ο χ-ν /«—N /«— s τ— ,·*—s 100.00 29.156 947.29 40.0 (N cn κ d V, d /—so oo 〇{ CN^ /—N 1 /—N Ο 97.99 1.90 0.02 /-—N /*—N r—^ 0.04 100.00 8.305 349.76 48.6 20.0 m X /—*sd /—N o /-—N o \ r—^ o V 严, ο v^. Ο 7.88 0.79 68.30 22.37 N 0.67 100.00 2.156 125.00 107.3 20.0 rn /—S o /—N o /—so 0.10 9.13 0.56 88.44 1.71 0.02 0.00 r-^ 0.04 100.00 9.202 375.00 44.3 20.0 rn y^—so /—*N r·^ oo N 1-^ 0.08 7.40 0.45 _I 73.15 1.54 12.98 4.25 /— N 0.16 100.00 11.358 500.00 4 5.7 20.0 CO (X( 0.16 /—V »—H o 23.56 /—S »—< 0.10 75.70 0.47 Ci />-~Ν τ—^ /—S /—, r—H 100.00 16.637 419.76 -38.2 20.0 G /—N o /-N o 0.30 /—s T-^ 5 '<·«·✓ 98.69 1.00 /—S /-**Ν 1—Η ο /·—s r-^ /—N 100.00 13.628 382.11 -29.2 20.0 99.69 99.00 rn 0.15 0.09 22.34 /·<-NF-< /-s *r! N—✓ 76.64 0.78 /-*Ν Ν 1—^ ο /*—s T—H r-^ / -*s /—N 100.00 17.550 445.11 -30.7 20.0 77.42 98.99 G 015 1 /—s 22.36 /—s 1—< 0.15 76.62 0.72 ο /—Ν Ο r~H /—N /—S /«—N 100.00 17.534 445.00 -37.6 20.0 77.49 98.88 ω 0.09 1_ /—N 14.00 r·^ 0.10 47.99 0.46 29.68 0.62 5.27 1.72 0.00 _1 0.06 100.00 27.994 919.76 40.0 20.0 W 0.09 /—N 13.45 0.03 0.09 46.22 0.45 28.80 0.61 5.22 1.66 2.87 0.50 100.00 29.156 947.29 40.0 CN Inert gas (calculated as n2) Hydrogen methane C02 Acetylene ethylene Ethylene propylene Other C3 (calculated as propane) C4 (calculated as n-butene) C5 (calculated as n-pentene) h2 〇 oxygenate (as methanol Calculate) Total molar flow rate (kmol/h) Mass flow rate (kg/h) Temperature (°c) Absolute pressure (bar) K) Θ :p ,mm Line 舾κι m life increase mt Ethylene/total ethylene, ethane, Acetylene (%) -55- 201247595 The molar flow rate of the ethylene-containing composition C3" reached 13628 km〇l/h, of which 1.449 kmol ethylene/h. The recovery of total ethylene (c3', ethylene in ethylene / outflow E) was 99.8 0%. The ethylene-containing composition C3" has an ethylene content of 98.69% by volume and a ratio of ethylene to total ethylene, ethane, acetylene of 99%. The ethylene-containing composition C 3 ', acetylene contains II The 19.4 ppm by volume and the propylene content of the flammable composition C3" was less than 5% by volume. The calculated thermal power in the reboilers of distillation columns T3, T3' and T3", and the power in the reboiler of the demethanizer DM3 are given in Table 6. The ethylene-containing composition C3 The heat rate has reached 0.642 kWh/kg. Example 6 (Comparative Example) The same effluent stream E as in Example 3 was treated in the same manner as in Example 5. Thereafter, the ethylene-containing composition C3" is sent to an ethylene splitter S3 (including a reboiler and a condenser) equipped with 4 theoretical stages. The ethylene-containing composition C3" is introduced to the 10th In the first stage, the first stage is a condenser and the 40th stage is a reboiler. The mass reflux ratio of the column is fixed at 5. A fraction of 3 60.00 kg/h containing ethylene and enriched with a compound lighter than ethylene is separated at the top of the ethylene splitter S3 (outlet of the condenser) and still contains ethylene-rich ethane-rich fraction H3" in ethylene splitting The bottom of the S3 is separated at the bottom. The absolute pressure at the top and bottom of the ethylene splitter S3 is fixed at 20 bar. The temperature at the top of the ethylene splitter S3 (the outlet of the condenser) is estimated to be -28.9 ° C and the bottom of the ethylene splitter S3 The temperature is calculated to be -25.5 °C »The fraction containing ethylene and enriched with ethylene lighter than -56-201247595 is then sent to a tower equipped with 20 theoretical grades - column DL3 (to separate from the ethylene step) a compound lighter than ethylene) to produce a polymerization grade of ethylene. The feed is introduced to the bottom of the column. The mass reflux ratio is fixed at 100. 4 kg/h of the fraction L3' at the top of the column (condenser Evaporation and separation of a polymerization grade of ethylene C3"" at the bottom of the column. The absolute pressure at the top and bottom of the column is fixed at 20 bar. At the top of the distillation column DL3 (outlet of the condenser) of The temperature is estimated to be -3 7.5 ° C and the temperature at the bottom of the distillation column DL3 is calculated to be -28.9 ° C. The characteristics of the polymerization grade of ethylene C3"' along with the fractions H3" and L3' are given in Table 5b below. , hydrogen, methane, CO 2 , acetylene, ethylene, ethane, propylene, other C 3 , C 4 , C 5 , H 20 , the amount of oxime and the total amount expressed as % by volume 'except those in brackets, they are PPm ° -57- 201247595 by volume Table 5b C3, "H3" L3, inert gas (calculated as N2) (<n (<D 0.03 hydrogen P, __ί—·· (<ΐ) ( <1) 0 00 methane 0.06 (<l) 21 48 C〇2 (<D 1 V 1 ^ (<n (<\Λ acetylene (0.3) (<〇l) (<〇n Ethylene 99.93 82.62 78 52 Ethane 0.02 17.35 (<〇.l) Propylene (<〇.η (4.9) (<0.1) (<〇." (<0·1) Other C3 (calculated as propane (<〇.n C4 (calculated as n-butene) (<n (<D (<1) C5 (calculated as n-pentene) _ (<l) (<n (<] ) h2o (<1) r<n oxygenate (calculated as methanol) (<DLVA / (<l) (<n total 100.00 100 00 100 00 Mohr flow rate (kmol/h) 12.693 0 778 0 157 Mass S flow rate (kg/h) 356.00 22.11 4.00 Temperature (0C) -28.9 -25.5 -37 5 Absolute pressure (bar) 20.0 20.0 20.0 Total ethylene 'Ethane, acetylene (% by volume) 99.95 B / total ethylene, ethane, acetylene (%) 99.98 The polymerization rate of ethylene C3" 'mole flow rate reached 12.693 kmol / h, of which 12.684 kmol ethylene /h»Total ethylene (C3'', ethylene in the ethylene/outflow stream E) recovery rate reached 9412%. The ethylene content of the polymerization grade of ethylene C3"' reached 99.93% by volume and the ratio of ethylene to total ethylene, ethane, acetylene was 99.98%. The acetylene content of the polymerization grade of ethylene C3"' The 0.3 ppm by volume and the propylene content in the fraction C3"' is less than 0.1 ppm by volume. -58- 201247595 Calculated thermal attack in the reboilers of distillation columns 3, 3' and T3" The power in the reboiler of the demethanizer DM3, the heat power in the separator S3 boiler and in the reboiler of the column DL3 are shown in Table 6. The heat rate of the polymerization grade of ethylene C 3 ′′ reached kWh/kg. Table 6 Tower reboiler thermal power kW Example 5 Example 6 T3 25.297 25.297 T3· 96.211 96.211 T3" 100.033 100.033 DM3 23.602 23.602 S3 . DM3' - 5.622 Total 245.143 448.63 From the data of Examples 5 and 6, the thermal power required to obtain the C3"' of the polymerization grade is greater than 1.9 times the heat power required to obtain the composition C3". In addition, from the above total ethylene recovery rate appears to be 'as opposed to the ethylene-containing composition C3', when the graded ethylene C3"' is separated from the effluent stream E by about 5.68% Ethylene. This lost ethylene can be recovered after spending more and energy. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 shows a first preferred embodiment of the present invention. The rate of recurrence is given by 1.260 Ethylene Seeking for Aggregation and Loss Investment - 59 - 201247595 Figure 2 shows a second preferred embodiment of the present invention. Figure 3 shows a third preferred embodiment of the invention. [Description of main component symbols] E: effluent stream E': compressed effluent stream C1: ethylene-containing composition C1': ethylene-containing composition C1": ethylene-containing composition H1: fraction L1: fraction T1 Distillation column PCT: Preconditioning treatment DM1: Demethanation distillation column AS 1 : Acetylene saturation T2: Distillation column T2': Distillation column H2: Fraction H2': Fraction AS 2: Acetylene saturated DM2: Demethanation distillation column C2: Ethylene-containing composition C2': ethylene-containing composition C 2 ′′: ethylene-containing composition-60-201247595 L2: fraction F2: fraction F3: fraction F3': fraction F 3 ′′: fraction H3: fraction H3′: Fraction C 3 : Ethylene-containing composition C 3 ' : Ethylene-containing composition C 3 ′′: Ethylene-containing composition L3: Fraction T3: Distillation column T3′: Distillation column T3”: Distillation column AS 3 : Acetylene saturated DM3 : Demethanation Distillation Tower -61 -

Claims (1)

201247595 VII. Scope of application: 1. A composition containing ethylene comprising: (a) between 75% and 99.9% by volume of a hydrocarbon compound containing 2 carbon atoms: and (b) Ethylene, such that the ratio of the amount of ruthenium to the total amount of hydrocarbon compounds containing 2 carbon atoms is between 97% and 99.5%. 2. The ethylene-containing composition of claim 1, wherein the hydrocarbon compound having 2 carbon atoms is ethylene, ethane and acetylene. 3. The ethylene-containing composition according to any one of claims 1 to 2, wherein the composition comprises less than 100 ppm by volume of a hydrocarbon compound having at least 3 carbon atoms and less than 100 ppm by volume. Oxygenate and water. 4- A method for producing an ethylene-containing composition according to the method: a) subjecting an effluent stream E containing ethylene and other constituents from a monooxygenate to an olefin and having undergone a conventional treatment to a Pre-conditioning to obtain a compressed effluent stream E'; and b) separating the compressed effluent stream E' in one to three distillation columns to obtain one of claims 1 to 3 A composition containing ethylene. 5. The method of claim 4, wherein the effluent stream E comprising ethylene and other components is from a methanol to olefin. 6. The method of claim 4, wherein the compressed outflow E' comprises up to 1 〇〇〇 ppm of oxygenate by volume and up to 100 ppm of water by volume -62 to 201247595. 7. The method of claim 4, wherein after the step a), the compressed effluent stream E is separated in the distillation column 1 into an ethylene-containing composition C1 at the top of the distillation column T1. And is separated into a fraction H1 enriched in a compound containing at least 3 carbon atoms at the bottom of the distillation column T1. 8. The method of claim 4, wherein after step a), the compressed effluent stream E' is separated in two distillation columns by the following steps: bl) - a first separation step, The step consists in separating the compressed effluent stream E' into a fraction F2 at the top of the distillation column T2 in a first distillation column T2 and separating into a compound having at least 4 carbon atoms enriched at the bottom of the distillation column T2. Fraction H2; and b2) - a second separation step in which the fraction F2 is separated in a second distillation column T2' into an ethylene-containing composition C2 at the top of the distillation column T2' and separated into A fraction H2' of the compound containing at least 3 carbon atoms is enriched at the bottom of the distillation column T2'. 9. The method of claim 4, wherein after step a), the compressed effluent stream E' is separated in three distillation columns by the following steps: b 1 ) - a first separation step, the step The separated effluent stream E' is separated into a fraction F3 at the top of the distillation column T3 in a first distillation column T3 and separated into a fraction F3' at the bottom of the distillation column T3, b2) - a second separation a step of separating the fraction F3' into a fraction F3" at the top of the distillation column T3' in a second distillation column T3' of -63-201247595 and separating into an enrichment at the bottom of the distillation column 3' a fraction Η3 of a compound containing at least 4 carbon atoms; and b3) a third separation step in which the fractions F3 and F3" are separated into a distillation column T3" in a third distillation column T3" An ethylene-containing composition C3 at the top and separated into a fraction H3 enriched with a compound having at least 3 carbon atoms at the bottom of the distillation column T3", 10. As in the fourth to ninth application of the patent application a method in which, after step b), The composition of ethylene is subjected to a acetylene saturation. 11. The method of claim 1 wherein after the step b), the ethylene-containing composition is subjected to a separate separation step (referred to as demethanization). To thereby isolate a saturated product which is enriched with a compound lighter than ethylene. 12. A process for producing at least one ethylene derivative compound from the ethylene-containing composition according to any one of claims 1 to 3. Method 0. 13. A method for producing dichloroethane, according to which the ethylene-containing composition according to any one of claims 1 to 3 is subjected to monochlorination and/or oxygen. Chlorination to produce dichloroethane. 1 4 · The method of claim 13 of the patent scope further comprises pyrolyzing dichloroethane to produce vinyl chloride. 1 5 · as claimed in claim 14 The method further comprises polymerizing vinyl chloride to produce polyvinyl chloride.