The method of purification from carbon monoxide-olefins and saturated hydrocarbons

 

(57) Abstract:

The inventive a-olefins and saturated hydrocarbons clear of carbon monoxide by contacting at 0-150°C with a catalytic system containing a mixture and/or product of the reaction of copper oxide with one or more oxides of metals of the II group of the Periodic table at a molar ratio of copper oxide and a metal oxide IV In groups of from 1:10 to 10:1. 7 C. p. F.-ly, 1 table.

The invention relates to a method of removing carbon monoxide from a-olefins and saturated hydrocarbons, in order to make the above-olefins and saturated hydrocarbons suitable for use in the processes of polymerization Ziegler-Natta. In particular, the method of the invention can be successfully used for cleaning2-C4-olefins, obtained by a process of thermal cracking, which constitute the main source of production of the above-olefins.

It is known that olefins, obtained by thermal cracking of petroleum products, even after the complex treatment of the separation and purification contain small amounts of impurities, many of which, including carbon monoxide, have a deleterious effect on the catalyst CIG is giving a halide of titanium, put on magnesium chloride, and the connection alkyl aluminum as socializaton.

Carbon monoxide is usually present in the above-olefins in an amount ranging from 0.5 to 10 million shares (hereinafter, assume that million shares are moles), and at such levels, it significantly lowers the efficiency of the catalysts of the Ziegler-Natta. On the other hand, not so easy to further reduce said concentration of carbon monoxide in C2-C4-olefins by means of simple distillation, given the low boiling point above-olefins. In particular, when the concentration of carbon monoxide is lower than or equal to 2 million shares distillation becomes even disadvantageous from an economic point of view.

Economic damage due to the presence of carbon monoxide in the polymerization process, is enhanced when, as often happens, the carbon monoxide concentration varies within the above limit, because it causes oscillation of the polymer yield at the stage, where the latter emerges from the polymerization reactors, and is forced to take continuous and expensive operation to regulate the supply systems of the catalyst and not always with positive results. This dokatyvayutsya catalysts of the Ziegler-Natta becomes insignificant.

The methods used to date to reduce the specified content of carbon monoxide in-olefins, obtained by processing petroleum products (including thermal cracking), based essentially on the use of the ability of some compounds of transition metals, in particular copper compounds, in the form of an aqueous solution, or dispersed on an inert solid support such as alumina or dvuoksid silicon), to form complexes with carbon monoxide.

For example, in accordance with U.S. Pat. USA 3014973-olefins, which must be cleaned, in particular ethylene and propylene, treated with an aqueous copper-ammonia solution and then selectively emit thus to separate them from carbon monoxide, which remains bound in the complex compound of copper.

To further reduce the content of carbon monoxide assumed the additional processing-olefins by contacting them with alkali metal hydroxide at temperatures higher than 170aboutC.

From the data presented in U.S. patent 3014973, it is not necessary is made possible by use of the above-mentioned method of reducing the concentration of the horns and requires an additional stage liquefaction purified olefin, whenever, as often happens in the case of propylene and 1-butene, want to carry out the polymerization in liquid monomer.

According to the invention offers a method of removing carbon monoxide from a-olefins and saturated hydrocarbons, whereby carry out the contacting of the olefin or saturated hydrocarbon containing carbon monoxide, at temperatures in the range from 0 to 150aboutWith, preferably, from 20 to 95aboutWith, with a catalytic system comprising the mixture and/or reaction product:

A) one or more metal oxides selected from the group consisting of cu, Fe, Ni, Co, Pt and Pd; and

C) one or more metal oxides selected from the group consisting of metals of groups V, VI, or VII In the Periodic Table.

The method of the invention for the removal of carbon monoxide from a-olefins, enables a particularly simple and effective method, at low temperatures and conservation-olefins, in particular propylene and 1-butene in the liquid state.

In addition, the same method can be used for removal of carbon monoxide from saturated hydrocarbons which may be present as diluents in the polymerization of olefins. As well as the different hydrocarbons, in particular, C2-C4that have low boiling points, which creates difficulties when carbon monoxide is removed by distillation.

Pre-declared method of the present invention allows to reduce the content of carbon monoxide in-olefins and saturated hydrocarbons, while the concentration does not fall below 0,03 million shares, in particular, when the concentration is set lower than 0.02 million shares.

In the case of propylene, 1-butene and easily liquefied saturated hydrocarbon operation is performed preferably in a liquid state.

Mentioned catalytic system comprising the mixture and/or reaction product (A)+(B), are catalytic oxidation systems, and, therefore, they are able to transform the carbon monoxide present in the olefin, or a saturated hydrocarbon, carbon dioxide.

As levels above which carbon dioxide can affect the activity of catalysts of the Ziegler-Natta, are significantly higher than the levels of carbon monoxide, and usually higher than 5 million shares of presence in quantities up to 5 million shares of carbon dioxide, which replaces the carbon monoxide in the olefins and feast upon

The initial concentration levels of carbon monoxide within which the method of the invention can be used most advantageously lower than or equal to about 5 million shares in particular, from 0.5 to 5 million shares.

If necessary, the content of carbon dioxide in the olefins and saturated hydrocarbons can be easily reduced to concentrations lower than or equal to 5 million shares through contact with hydroxides of alkali metals, in particular, Na or K, randomly deposited on inert carriers such as calcium carbonate or activated carbon. It is possible, for example, skip-olefins or saturated hydrocarbons to flow through the fixed layer containing the above-mentioned hydroxide in the solid state and homogeneous distributed; in this case, the carbon dioxide bound in the complex in the form of carbonate.

Among the catalytic systems used in the method according to the invention, especially preferred are systems in which the component (A) comprises or consists of copper oxide (CuO); for component (C) preferred catalytic systems are systems in which the specified component includes or consists of a metal oxide selected from the group consisting of Depending on the cooking method, the catalytic system may also include the reaction products of oxides of (b) and (A). For example, the catalytic system obtained from SIO and CR2O3may include or consist of CuCr2O4.

Components (a) and (b), in a mixture or in the form of reaction products between them, are usually present in the catalytic system used in accordance with the invention, the molar relationship (A):(B) ranging from 1:10 to 10:1, preferably from 1:2 to 5:1. Especially preferred are catalyst system comprising SIO and Cr2ABOUT3as such and/or in the form of CuCr2O4in the above-mentioned proportions.

The catalytic system used in the method of the invention can also be deposited on inert carriers, such as silica, alumina, diatomaceous earth and activated charcoal.

The preparation methods mentioned catalytic systems vary mainly depending on the desired chemical composition and morphology.

For example, it is possible to mix (a) and (b) oxides through joint crushing or by thermal decomposition of various compounds of the corresponding metals, which can be turned into ACS the water by thermal decomposition, usually chosen from salts of organic and inorganic acids, such as, for example, alcoholate, nitrates or carbonates. These salts can also be used in solution in appropriate solvents, preferably in water, for impregnation mentioned inert carriers, thereby obtaining through evaporation of the solvent and subsequent thermal decomposition of the deposited catalytic system. Thermal decomposition respectively performed by heating at a temperature usually in the range from 150 to 800aboutIn the presence of air or oxygen.

Some of these catalytic systems are usually used in a reduced state, that is, after they have been processed by hydrogen, as catalysts for hydrogenation-dehydrogenation or hydration in various organic syntheses, and, therefore, they are industrially available.

In contrast to the above methods of application after treatment with hydrogen, in the method according to the invention the catalytic system described above is used as such, or after processing in a stream of air or oxygen, usually at temperatures in the range of 80 and 500aboutAnd time ranges in prorisovany successfully in the method of the invention, are si-C and Cu-E types, manufactured by ENGELHARD. Catalyst C-0203 T contains SIO and CR2O3in quantities 79 and 17 wt. respectively. Catalyst Cu 1230 E contains SIO and Cr2O3in numbers 30 and 31 wt. respectively, and deposited on the alumina. I believe that some of the oxides in these catalysts is in the form of CuCr2O4.

-Olefins and saturated hydrocarbons containing carbon monoxide, is preferably introduced into contact in the liquid state with a catalytic systems comprising a mixture and/or reaction product (A)+(B).

Commonly used operating pressure that is required to support-olefins or saturated hydrocarbons in the liquid state corresponding to the used temperature. For example, in the case of propylene or 1-butene is in the range from 1 to 200 ATM. preferably, from 2 to 50 ATM.

When it is not necessary for polymerization to liquefy-olefins or saturated hydrocarbon-olefin or a saturated hydrocarbon may be introduced into contact with the catalytic system in the gaseous state. In this case, preferably operate at pressures in the range from 20 to 100 ATM.

In accordance with sponsoredreviews a fixed or mixed layer. The average diameter of the particles ranges preferably in the range from 500 to 10,000 microns.

-Olefins or saturated hydrocarbons is passed through the above-mentioned layers of the catalyst bulk velocity, usually varying from 2 to 20 h-1. The work is usually continuous and lasts anywhere from 10 to 500 hours, preferably from 40 to 250 hours These time periods correspond to the lifetime of the catalytic system, i.e. the period of time during which the catalytic system maintains a satisfactory level of efficiency in the removal of carbon monoxide, based mainly on the chemical composition and physical and morphological patterns used catalytic system; terms of use; and the contents of carbon monoxide and other impurities present in the olefins and saturated hydrocarbons, which must be cleared.

Working in these conditions, you can remove the amount of carbon monoxide of approximately 1 kg per 100 kg of catalytic system, thus cleansing liquid propylene containing 1-3 million shares of carbon monoxide.

A further advantage of the method of the invention is that the radio is usually performed by heating the catalytic system in air or oxygen to 80-500aboutWith, preferably 150-200aboutC for 1-10 hours, preferably within 4-30 PM

The following examples illustrate but do not limit the present invention.

In all examples, the concentration of CO and CO2determined by gas chromatographic analysis.

The control example 1. In order to test the effectiveness of the catalytic system for removing carbon monoxide from a liquid propylene, the test was carried out at high concentrations of carbon monoxide using the following methods.

In a stainless steel autoclave with a volume of 1.8 liters, equipped with a stirrer and a heating device with a silicone oil, in an atmosphere of nitrogen load of 50 g ENGELHARD si 1230 E. 1/16-3F catalyst, previously activated by treatment with a stream of air at 170aboutC for 4 h Then add 676 g of liquid propylene containing 1500 million shares of carbon monoxide and about 2 million shares of CO2.

The support autoclave with stirring for 6.5 h at 44aboutWith, and in the course of 15.5 h at the 31aboutS, after which the sample liquid propylene was taken. Gas chromatographic analysis performed on the specified sample shows the contents of co and CO266/SUB>.

Control example 2. Example 1 is repeated, but in this case used propylene has a content equal to 1800 million shares and 2 million shares of CO2and the autoclave was maintained at a temperature varying from 42 to 47aboutWith over 21 hours of the Final CO content is 640 million shares; T. O. was quantitatively converted into CO2.

Reference example 3 (comparative).

Control example 1 is repeated, but in this case used propylene has a content equal to 1300 million shares and 2 million shares of CO2and add 50 grams of ENGELHARD IN A-006-06-T 1/8 catalyst, maintaining the autoclave 45aboutWith over 31 PM

The above catalysts containing CuO deposited on silicon dioxide.

The final CO content is 1200 million shares, thus the catalyst, which is solely based on copper oxide, is not effective in removing carbon monoxide from a liquid propylene.

P R I m e R 4. The one W the catalyst used in the control example 1 is used in a series of three experiments for purification of liquid propylene containing FROM in amounts usual for the obtained propylene industry "curing with the giving of liquid propylene, moreover, the specified vessel equipped with feeding tubes, which are used for the introduction of propylene, CO and nitrogen (necessary to maintain a constant supply pressure of the liquid propylene).

On bottom of the vessel is the sampler for analysis of the initial CO content and the pipe for discharging propylene, you need to clean up. The specified discharge pipe attached to the bottom of the purifier through water heater/steam. The latter consists of a cylinder made of stainless steel with an inner diameter of 50 mm and a height of 500 mm, equipped with both ends of the disks and mesh filters to prevent leakage of the catalyst. The cylinder is heated to the desired temperature by circulating water/steam in the outer jacket. Propylene, which comes from the bottom, comes in contact with the catalyst within the desired period of time the sampler allows you to regularly remove samples that are analyzed for the final content.

659 g of catalyst were used in all experiments. The main operating parameters and the initial and final concentrations shown in the table.

P R I m e R 5. Three of experience in the cleaning liquid propylene is carried out, using the same Sie parameters as well as the initial and final concentrations shown in the table.

1. The METHOD of PURIFICATION FROM CARBON MONOXIDE-OLEFINS AND SATURATED HYDROCARBONS by contact with a catalytic system containing copper oxide, characterized in that the use of a catalytic system containing a mixture and/or product of the reaction of copper oxide with one or more metal oxides selected from the group YIB, when the molar ratio of copper oxide and a metal oxide YIB group 1 10 10 1 and the contacting is carried out at 0 to 150oC.

2. The method according to p. 1, characterized in that the metal oxides of group YIB include or consist of Cr2O3.

3. The method according to p. 1, characterized in that the catalytic system contains CuCr2O4.

4. The method according to p. 1, characterized in that the specified catalytic system is pre-heated in a current of air or oxygen at 80 500oC for 1 to 100 hours

5. The method according to p. 1, characterized in that a-olefins or saturated hydrocarbons, which must be clear, contain 2 to 4 carbon atoms.

6. The method according to p. 5, characterized in that a-olefins or saturated hydrocarbons, which must be clear, contain (0,05 5,0) million-what about the clear, is propylene, which enter into contact in the liquid state with the specified catalytic system.

8. The method according to p. 5, wherein the a-olefin which is to be cleaned is ethylene.

 

Same patents:

The invention relates to a method of separation of isobutene from a hydrocarbon fractions by treating them with water in the presence of an acid catalyst with the formation of tertiary butyl alcohol, which is then subjected to decomposition with obtaining isobutylene or used as a commercial product
The invention relates to the field of allocation of tertiary olefins from mixtures of hydrocarbons of varying degrees of saturation and can be used in the production of monomers for IC
The invention relates to the separation of tertiary olefins from mixtures of hydrocarbons of varying degrees of saturation and can be used in industry to obtain monomers for IC

FIELD: petroleum processing.

SUBSTANCE: catalyst contains 15-30% hydrogenation components including groups VU and VIII metals, 20-40% acid component, and 1-4% promoter, the rest being binder: alumina, aluminosilicate, clay, or their mixture. Catalyst is distinguished by having three-component system composed by nickel, molybdenum, and tungsten in the form of their oxides at weight ratio Ni/Mo/W equal to 25:35:40. Above-mentioned acid component contains aluminum fluoride and promoter contains boron oxide and/or zirconium oxide. Preparation technology is simple and completely suppresses production of waste water. Invention describes hydrocracking process in presence of the claimed catalyst, which is carried out at 380-430оС, pressure 3 to 10 MPa, and volume flow rate 1 -3 h-1 at H2/feedstock ratio 250 to 1000. Process is especially appropriate for diesel fuel production.

EFFECT: enabled preparation of high-activity and high-selectivity catalyst at any catalyst production plant without additional equipment.

2 cl, 3 tbl, 7 ex

FIELD: petrochemical processes.

SUBSTANCE: 1,3-butadiene is obtained via catalytic dehydrogenation of n-butylenes at 580-640°C and essentially atmospheric pressure while diluting butylenes with water steam at molar ratio 1:(10-12) and supplying butylenes at space velocity 500-750 h-1. Catalyst is composed of, wt %: K2O 10-20, rare-earth elements (on conversion to CeO2) 2-6, CaO and/or MgO 5-10. MoO3 0.5-5, Co2O3 0.01-0.1, V2O5 0.01-0.1, and F2O3 the balance. Once steady condition is attained, dehydrogenation is carried out continuously during all service period of catalyst.

EFFECT: increased yield of 1,3-butadiene and process efficiency.

2 ex

FIELD: industrial inorganic synthesis and catalysts.

SUBSTANCE: invention provides ammonia synthesis catalyst containing VII group and group VIB metal compound nitrides. Ammonia is produced from ammonia synthesis gas by bringing the latter into contact with proposed catalyst under conditions favoring formation of ammonia.

EFFECT: increased ammonia synthesis productivity.

8 cl, 2 tbl, 19 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalytic system is prepared by consecutively charging into reactor alumino-cobalt and alumino-nickel-molybdenum catalysts containing 12.0-25.0% molybdenum oxide, 3,0-6.0% nickel oxide, and 3.0-6.9% cobalt oxide provided that alumino-cobalt and alumino-nickel-molybdenum catalysts are charged at ratio between 1.0:0.1 and 0.1:1.0, preparation of catalysts employs mixture of aluminum hydroxide and/or oxide powders, to which acids are added to pH 1-5. More specifically, aluminum hydroxide powder mixture utilized is a product of thermochemical activation of gibbsite and pseudoboehmite AlOOH and content of pseudoboehmite in mixture is at least 70%, and aluminum oxide powder mixture utilized comprises powders of γ-Al2O3 with particle size up to 50 μm and up to 50-200 μm taken at ratio from 5:1 to 2:5, or γ-Al2O3 powders with particle size up to 50 μm, 50-200 μm, and up to 200-400 μm taken at ratio between 1:8:1 and 3:6:1.

EFFECT: method of preparing catalytic systems for large-scale high-sulfur hydrocarbon feedstock hydrofining processes is provided allowing production of products with desired levels of residual sulfur and polycyclic aromatic hydrocarbons.

4 tbl, 3 ex

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: catalyst composition intended for hydrogen processing contains component of non-precious metal of group VIII, two components of group VIB metals, and 1 to 30% of combustible binder including at least 50 wt % carbon.

EFFECT: achieved preparation of high-strength catalyst easily controllable during a process.

17 cl

FIELD: production of catalytic compositions.

SUBSTANCE: proposed method includes combining and bringing into interaction at least one component of non-precious metal of group VII and at least two components of metal of VIB group in presence of proton liquid; then composition thus obtained is separated and is dried; total amount of components of metals of group VIII and group VIB in terms of oxides is at least 50 mass-% of catalytic composition in dry mass. Molar ratio of metals of group VIB to non-precious metals of group VIII ranges from 10:1 to 1:10. Organic oxygen-containing additive is introduced before, during or after combining and bringing components into interaction; this additive contains at least one atom of carbon, one atom of hydrogen and one atom of oxygen in such amount that ratio of total amount of introduced additive to total amount of components of metals of group VIII to group VIB should be no less than 0.01. This method includes also hydraulic treatment of hydrocarbon material in presence of said catalytic composition.

EFFECT: enhanced efficiency.

29 cl, 8 ex

FIELD: petroleum processing.

SUBSTANCE: invention provides oil stock hydrotreatment catalyst containing alumina-supported hydrogenation components: cobalt, molybdenum, and tungsten in the form of oxides at weight ratio Co/Mo/W = 20:45:35 (15-25% in total), aluminum fluoride (10-30%), and promoter (2.5-16.5%): silicon oxide and/or rare-earth element oxides, in particular lanthanum oxide or lanthanum/cerium oxide mixture. Promoter may further contain up to 3% zirconium oxide. Alumina functions as binding material. Invention also covers oil stock hydrotreatment process, which is conducted in presence of claimed catalyst at 340-430°C, pressure 3-10 MPa, oil stock flow rate 0.5 to 3 h-1, and hydrogen-to-oil stock ratio 250 to 1000 nm3/m3. Catalyst is characterized by elevated hydrocracking and hydro-desulfurization activity and selectivity in oil stock hydrotreatment processes resulting in production of diesel distillates meeting European requirements (EN-590). Catalyst can be prepared on any existing catalyst preparation equipment.

EFFECT: simplified catalyst preparation technology and avoided formation of effluents.

5 cl, 3 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention describes method of obtaining aggregated catalyst for hydrogen treatment of oil fractions. The catalyst is a composition of components in the form of compounds of one VIII group metal and two VIB group metals. Method involves mixing and chemical interaction of components, producing active complex by mechanic and chemical activation of components, which remain in solid state during the whole process performed in aggregates of mechanic and/or hydrodynamic effect, preferably in planetary centrifugal mill, at room temperature for 5-30 minutes, with free pass distance of milling bodies equal to 4.0-5.0 cm, relative collision speed of milling bodies equal to 17-34 m/s, reaction layer thickness for component mix on the surface of milling bodies equal to (0.4-2.6)·10-2 cm, with further drying, tempering and sulfidation. Active complex is dried for 10-15 minutes.

EFFECT: high-grade purification of oil products from sulfur.

1 cl, 1 tbl, 2 dwg, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to catalyst production, particularly to production of catalysts for dehydrogenating olefin hydrocarbons. Described is a catalyst based on iron oxide, containing potassium compounds, chrome oxide, molybdenum oxide, ceric oxide and portland cement with the following ratios of components, wt %: potassium compounds (in terms of potassium oxide) 10.0-25.0; chrome oxide 0.5-7.0; molybdenum oxide 0.7-7.0; ceric oxide 1.0-15.0; portland cement 0.5-13.0; the rest is iron oxide.

EFFECT: increased selectivity of catalyst.

3 cl, 1 tbl, 2 dwg, 16 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method and catalyst composition, used in hydroconversion of heavy hydrocarbon starting material. A catalyst composition is described, which is suitable for use in hydroconversion of heavy hydrocarbon starting material. The said catalyst composition contains: a component based on a group VIB metal; a component based on a group VIII metal; a component based on phosphorus; and carrier material, which contains aluminium oxide, where the said carrier material is characterised by average pore diametre ranging from 100 Å to 140 Å, pore size distribution width less than 33 Å, and pore volume at least equal to 0.7 cm3/g, where less than 5% of the said pore volume in the said carrier material is made up of pores in the said carrier material, exceeding 210 Å, and the carrier material contains less than 3 wt % silicon dioxide. A method of hydroconversion of heavy hydrocarbon starting material is also described, where the said method involves the following stage: bringing the said heavy hydrocarbon starting material into contact with the above mentioned catalyst in suitable conditions, where the said catalyst is effective in hydroconversion of at least part of the said heavy hydrocarbon starting material, obtaining lighter hydrocarbons. A composition is also described, which is suitable for use as a component of the carrier material based on aluminium oxide or a catalyst composition, meant for use during hydroconversion of heavy hydrocarbon starting material, where the said composition contains: aluminium oxide, which enables obtaining the said carrier material based on aluminium oxide which has pores which are characterised by average diametre in the range from 100 Å to 140 Å, pore size distribution width less than approximately 33 Å, pore volume at least equal to 0.75 cm3/g where less than 5% of the said pore volume is made up of the said pores with diametre exceeding 210 Å, and where the carrier material contains less than 3 wt % silicon dioxide.

EFFECT: catalyst compositions with improved catalyst activity and stability with respect to hydroconversion of heavy hydrocarbon starting material.

8 cl, 5 tbl, 3 dwg, 6 ex

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: crude alpha-olefin is heated, raw vinylidene olefins are isomerized in the presence of catalyst and alpha-olefin is separated from isomerized vinylidene olefin by rectification. Separation of alpha-olefin is carried out for at least two successive steps at similar temperatures on top of vat and reducing pressure of rectifying column at each following step. Condensed phase removing from top of the rectifying column at previous step is fed to feeding zone of the following step and the rectifying column at top and vat section is sprayed. For spraying the top section of column the condensed phase removing from the top of rectifying column at the same step is used and for spraying the vat section of column the vat liquid of rectifying column at the same step is used. Separated alpha-olefin is purified additionally from oxygen-containing impurities by adsorption up to polymerization degree of purity. Raw heating, isomerization, separation and adsorption are carried out in atmosphere in inert gas. The unit used for treatment of alpha-olefin includes reactor for isomerization of vinylidene olefins in raw, rectifying column wherein feeding zone is joined with reactor outlet and wherein alpha-olefin of high purity degree is removed from the column top. The unit includes also at least one rectifying column for additional treatment of alpha-olefin of high purity from isomerized vinylidene olefins and adsorption column for separation of oxygen-containing impurities in alpha-olefin of high purity wherein the column inlet is joined with the top outlet of the last rectifying column used for additional treatment of alpha-olefin of high purity and outlet is used for removing alpha-olefin of the polymerization purity degree. Invention provides enhancing quality of the end product.

EFFECT: improved method for treatment.

8 cl, 1 dwg, 1 ex

FIELD: petrochemical processes.

SUBSTANCE: invention relates to treatment of C5-hydrocarbons in order to remove cyclopentadiene impurities, which process may be, in particular, used in rubber production industry when producing hydrocarbon monomers applicable in stereospecific polymerization processes. Treatment of hydrocarbons is accomplished with cyclohexane in presence of organic solvent and alkali catalyst, after which C5-hydrocarbons are separated from reaction products via rectification. Organic solvent is selected from alkylene glycol monoalkyl ethers including their mixtures taken in amounts 0.5 to 5.0 wt % based on C5-hydrocarbons.

EFFECT: increased degree of cyclopentadiene extraction at lower reagent consumption.

8 cl, 1 tbl, 23 ex

FIELD: organic chemistry.

SUBSTANCE: invention refers to enhanced method of propane and/or butanes flow separation from original hydrocarbons containing alkylmercaptan impurities by means of fractional distillation resulted in liquid phase and separated flow from column head at pressure providing that separated flow from column head containing propane and/or butanes has temperature within 50 to 100°C, including (i) addition to specified origin hydrocarbons an amount of oxygen sufficient for mercaptan oxidation, (ii) fractional distillation of produced mixture containing at least one catalyst layer oxidising mercaptans to sulphur compounds with higher boiling temperatures and (iii) separation of sulphur compounds with higher boiling temperatures as portion of distillation liquid phase.

EFFECT: improved method of propane and/or butanes flow separation from of original hydrocarbons by means of fractional distillation resulted in liquid phase and separated flow.

8 cl, 2 tbl, 1 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: invention relates to method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids. The method includes the following stages: (a) contact in the oxidation reaction zone of the alkane, which contains molecular oxygen gas, not necessarily corresponding to the alkene and not necessarily water in the presence of at least one catalyst, effective with the oxidation of the alkane to the corresponding alkene and carboxylic acid, alkane, oxygen and water; (b) separation in the first separating agent at least part of the first stream of products in a gaseous stream, which includes alkene, alkane and oxygen, and a liquid stream, which includes carboxylic acid; (c) contact of the mentioned gaseous stream with the solution of a salt of metal, capable of selectively chemically absorbing alkene, with the formation of a liquid stream rich in chemically absorbed alkene; (d) isolation from the flow of the solution of salt of the metal. The invention also relates to combined methods of obtaining alkyl-carboxylate or alkenyl-carboxylate (for example vinyl acetate), moreover these methods include oxidising of alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acid, isolation of alkene from the mixture of alkene, alkane and oxygen by absorption using the solution of the salt of metal and extraction of the stream rich in alkene from the solution of the salt from metal for using when obtaining alkyl-carboxylate and alkenyl-carboxylate.

EFFECT: improved method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids.

46 cl, 1 dwg

Up!