Method of separating methanol from mixtures with hydrocarbons4or5
(57) Abstract:Usage: in chemical technology for the separation of methanol from mixtures with hydrocarbons, C4or C5formed in the processes of obtaining highly active additives to motor fuels. The inventive product is methanol. Methanol from mixtures with hydrocarbons4and C5allocate passing through the adsorbent filled sulfonium molded catalyst having a static exchange capacity of not more than 1.7 mEq H+/, Adsorption is carried out at 10-30oC. 1 C.p. f-crystals. The invention relates to a method of separating methanol from mixtures with hydrocarbons4or5. Such mixtures are detected, for example, in producing high-octane additives to motor fuels-tert-butyl ether (MTBE) or tert-amyl ether (tame) by the interaction of methanol and hydrocarbon fractions containing tert-olefin WITH4or C5. B these processes using rectificatio commodity MTBE or tame selected kubovy product and unreacted hydrocarbons WITH4or5and methanol top.There is a method of separating methanol from hydrocarbon WITH4orThe disadvantage of these methods is their high energy consumption because of the separation of methanol and extractant used rectificatio.Also known methods of recovery of methanol from mixtures with hydrocarbons4or5using adsorption followed by desorption. As adsorbents used, for example, silica gel, molecular sieves, Malopolskie and crystalline, and ion-exchange resin (U.S. Pat. USA N 4605787, Pat. USA N 4814517, European Pat. N205562, Pat. GERMANY N 3124293). For regeneration after adsorption through the sorbent miss nesorbiruyushchegosya liquids or gases.Most deep cleaning hydrocarbons from methanol (20 PPT) was achieved by using as the adsorbent a special zeolites. In this way as desorbent used fresh hydrocarbon fraction, which after saturation with methanol is directed to the synthesis of MTBE (Int. application N 8/03483).Closest to the present invention is a method of separating methanol from mixtures with hydrocarbons4or5that includes passing the mixture through adsorb is desorbent carry out desorption of methanol fresh portion of the hydrocarbon mixture, containing tert-olefin (U.S. Pat. USSR N 1456006, 1986).In this way the depth of cleaning is somewhat lower and is equal to 1000 ppm. However, carrying out the process at lower temperatures leads to lower energy consumption in comparison with the known methods, using as liquid extractants, and other solid sorbents.In the method according to the patent N 1456006 as adsorbents using a strongly acidic stiroldivinilbenzol cations in the salt form, weak acid ion exchangers or anion exchangers. It should be noted that the use of fine-grained ion-always complicated by their relative osmotic instability (grinding) and ash from the contact zone, which affects their consumption. Given the significant rates listed on the ion exchangers, the cost sorbents comprise a significant share in the cost of phase separation of methanol.The task of the invention is to cheapen the process of separating methanol from hydrocarbon fractions WITH4or5while achieving almost the same sorption characteristics and high selectivity.We propose a method of separating methanol from hydrocarbon fractions WITH4or5that includes passing scost (SOY) not more than 1.7 mEq H+/, Adsorption is carried out at a temperature of 10-30oC.After adsorption recovery of methanol is carried out, for example, passing through the sorbent hydrocarbon fraction WITH4or5that after saturation of methanol is directed to the synthesis of MTBE or tame.Used in the proposed method, the catalyst may be obtained from its natural poisoning with preservation of porosity in the implementation of processes, for example, the synthesis of MTBE, hydration of isobutylene, etc.The same catalyst can be obtained by subjecting the alkaline processing solution of the catalyst prior to unloading from the reactor or after loading in the adsorber-desorber. The catalyst, if necessary, dehydrated, for example, with methanol, then to delete the last used IsolatedStorage fraction.It should be noted that sulfonate molded catalysts inherently differ significantly from ionoobmennika used by the patent of the USSR N 1456006. Proposed in the invention ionite molded catalysts in its composition are thermoplastic materials such as, for example, polypropylene (KU-FPP) or sulphonated, politi the battle deterioration of their sorption properties relative to methanol. In practice this is not observed. This phenomenon can be explained by the presence in sulfonitric catalysts a certain number of SO3H - groups instead of SO3Na, -COOH, -OH and nitrogen-containing groups in the ion-exchange materials for the patent of the USSR N 1456006. Perhaps the acid strength of the proposed sorbent in combination with high porosity reduces the effect of the presence of thermoplastics-fillers ionite molded catalysts. While the invention the presence of SO3H-groups is limited by the amount not higher than 1.7 mg-EQ H+/, With a higher value of SOY deteriorating the selectivity of the adsorption process due to the chemical reactions on the basis of components4-C5fraction and methanol. The result can worsen the quality of waste fractions, as well as the target product. Furthermore, the high-boiling impurities can clog the pores of the catalyst and reduce its sorption properties. When SOY is not more than 1.7 mEq H+/g sorption properties of ion exchangers molded catalysts are saved in a wider temperature range (10-30oC) that is of interest in the CIS and the countries where the annual temperature variations are significant.The catalyst, more granule size (5-10 mm vs. 0.3-1.5 mm in U.S. Pat. N 1456006). All this improves the hydrodynamics of the process and eliminates the problem of entrainment of catalyst, providing a lower flow rate.Thus, it is proposed a method of separating methanol from mixtures with hydrocarbons4or5cheaper compared to well-known due to the reduction of consumption of sorbent, as well as through the use of the spent catalyst. This improves the ecology of the whole process, because it is still a question of the disposal of an additional quantity of ion exchange material required for the separation of methanol on the prototype.Compared with known processes solvent extraction with methanol, followed by a significant flow of steam, the inventive method allows to reduce the energy intensity of the process, leads to the practical exclusion of wastewater.Example 1. The adsorption-desorption was performed by running the installation contactor, made in the form of a tube of stainless steel, which was filled with a sorbent in 400 ml. Temperature in the contactor was maintained at the expense of water from a thermostat, supplied in a shirt contactor.As sorbent was used partially swollen in methanol ionite molded kata is tion-adsorption.Desorption of methanol produced isobutane-isobutilene fraction with 30% of isobutylene, which was served in a number 680 ml/h at a temperature of 40oC and a pressure of 0.8 MPa. The content of methanol in the stream at the outlet of the contactor determined chromatography with thermal conductivity detector, the first was 3 wt. then it fell off and after 1 h was 0.3% after 1.5 h,1% Then the contactor reduced the temperature to 10oC and started the cycle when submitting 480 ml/h isobutane fraction with 2% methanol. After 2 h 30 min, the methanol content at the outlet of the contactor was 0.1% and after 3 h of 1.1 wt.Then raised the temperature in the contactor 50oC and started the desorption cycle with supply the same isobutane-isobutilene fraction, as in the initial cycle of desorption, in the amount of 750 ml/h After 2 h when the methanol content at the output of desorber of 0.1% reduced the temperature in the contactor to the 25oC and switched the setting on the adsorption cycle. Feed isobutane fraction with 2% methanol in the amount of 440 ml/h at 25oC was carried out for 3.5 hours While after 3 h, the methanol content at the outlet of the contactor was 0.1 wt. after 3.5 h 1%
Such operations switching contactor cycle desorption at temperatures of 40 and Oranta has not changed.Example 2. In the same contactor as in example 1, was loaded exhaust on stage tame and optionally treated with a solution of caustic soda, washed and dehydrated with methanol catalyst KIF with SOY of 1.7 mEq H+/,Desorption was performed by the fraction of hydrocarbons WITH5containing 37% tert-Milanov in the amount of 800 ml/h at a temperature of 50oC and a pressure of 1 MPA. After 1 h the methanol content at the outlet of the contactor amounted to 0.1% after 1 h 30 min 1% When it detected the presence of tame in trace quantities. Then in the contactor reduced the temperature to 30oC and started the cycle of adsorption in the flow of 600 ml/h of hydrocarbon fractions WITH5from 1.8% methanol and 0.1% tame. The content of methanol and tame in the stream at the outlet of the contactor, respectively after 2 h 0,1% 0,1% and 2 h 30 min to 0.9% and 0.1%
Such operation switch contactor from the desorption cycle at 50oC per cycle adsorption at 30oC was carried out 20 times. This adsorption capacity was almost unchanged.Example 3. In the same contactor as in example 1, was loaded partially swollen in methanol, used in the production of isobutylene, optionally processed by an ammonia solution to SOY 1.0 mg s of hydrocarbons4the following composition, isobutylene 40,35; butane 7,5; isobutane 4,4; p-butylene, 48,8, which was applied in the amount of 400 ml/h at a temperature of 50oC and a pressure of 0.8 MPa. After 2 h, the methanol content in the stream at the outlet of the contactor amounted to 0.1% after 3 h 1% Then the temperature in the contactor has dropped to 20oC and pressure up to 0.5 MPa, began the cycle of adsorption in the flow of butane-butylene fractions of 500 ml/h of the following composition, isobutylene 3,1; p-propane 11,8; isobutene-6,9; n-butylenes 76,3 and methanol and 1.9. After 2 h 30 min, the methanol content at the outlet of the contactor was 0.1% in 3 hours 1%
Such operation switch contactor from the desorption cycle at 50oC per cycle adsorption at 20oC was carried out 20 times. This adsorption capacity of the sorbent was almost unchanged.Example 4. (For comparison). In the same contactor that in examples 1-3, were loaded exhaust at the stage of synthesis of MTBE catalyst KU - FPP with SOY to 1.8 mEq H+/g, partially swollen in methanol.Desorption and adsorption of methanol were carried out in the same conditions and in the same sequence as in example 3.After 2 h, the methanol content at the outlet of the contactor (desorber) was 0.1% MTBE 0.5% of the dimer is Ola at the outlet of the contactor amounted to 0.1% after 3 h -1%
Such operation switch contactor from the desorption cycle to cycle adsorption at 20oC was carried out 20 times.This adsorption capacity decreased slightly. So, starting with 10 switch in the faction after adsorption of traces of dimer of isobutylene, and the flow after 20 switch-methanol content after 2.5 hours was 0.2% MTBE 0.1% dimer of isobutylene 0,1%
Example 5. In the same contactor as in example 1 was loaded with the catalyst KU-2 FRR, pre-treated with alkali solution to a value of SOY 0,5 mEq H+/g, washed and dehydrated in methanol.Operations desorption and adsorption was carried out under the same conditions and using the same feed and the composition of the hydrocarbon fractions With that in example 3.The content of methanol in the stream of the first cycle was:
The output of desorber after 1.5 h of 0.1%
Through 3,0 h 1%
At the outlet of the adsorber after 2.5 h of 0.1%
Through 3,0 h 1%
Such switching operation of the contactor from the desorption cycle at 50oC on a cycle of adsorption at 20oC was carried out 20 times. This adsorption capacity of the sorbent has not changed. 1. Method of separating methanol from mixture with uglev is m, characterized in that as ionite material used sulphidity molded catalyst having a static exchange capacity of not more than 1.7 mmol H+/g, and spend adsorption at 10 30oC.2. The method according to p. 1, characterized in that as sulfonates molded catalyst with static exchange capacity of not more than 1.7 mmol H+/g use the spent catalyst in the production of isobutylene, methyl tert-butyl ether or methyl tert-amyl ether.
FIELD: chemical technology.
SUBSTANCE: invention relates to removing impurities, such as aldehydes, from ethylene glycol aqueous solutions by treatment with bisulfite-treated strong-base anion-exchange resin. Invention describes a method for reducing the content of aldehydes in ethylene glycol aqueous solution containing about from 0.2 wt.-% to 20 wt.-% of ethylene glycol containing about from 80 wt.-% to 99.7 wt.-% of water and about from 100 mln-1 (mas.) to 0.1 wt.-% of aldehydes. Method involves contacting indicated solution with bisulfite-treated solid strong-base anion-exchange resin that before treatment with bisulfite comprises quaternary ammonium functional groups in hydroxide form. Invention provides the improvement in removing impurities, such as aldehydes, from flows of ethylene glycol aqueous solutions.
EFFECT: improved method for treatment.
2 cl, 1 ex
FIELD: chemical technology.
SUBSTANCE: invention relates to a method for treatment of aluminum alcoholates. Method involves passing aluminum alcoholates through a column filled with extrudates of aluminum oxide in γ-form with pore volume from 0.4 to 0.8 cm3/g prepared by preliminary hydrolysis of aluminum alcoholates, molding the prepared aluminum oxide to extrudates with diameter from 1.6 to 3 mm and length 3-4 mm and their following purification by calcinations at temperature 400-500°C. As a rule, the treatment of alcoholates is carried out at temperature 20-150°C in column for 1-5 h. Method provides the development of simple and available technology for treatment of aluminum alcoholates with hydrocarbon chain length from C3 to C6 and above from impurities up to the level 10-3-10-4 wt.-%.
EFFECT: improved treatment method.
2 cl, 5 ex
FIELD: chemical technology.
SUBSTANCE: invention relates to a method for preparing alkaline- and thermostable composition based on sugar alcohols of the optical density less or equal to 0.100 in S-test. Method involves treatment of sugar-base composition with strong-base anion-exchange resin in hydroxide form at temperature 30-100°C. Method provides decreasing consumption of chemical reagents and providing carrying out the combined a single-step process for alkaline stabilization and decolorizing.
EFFECT: improved preparing method.
18 cl, 7 tbl, 8 ex
SUBSTANCE: claimed invention relates to method of methanol recuperation from mixtures which contain it and water. Method lies in the following: a) carried out is multi-step evaporation in at least two steps of evaporation, each of which includes evaporator, with consecutive reduction of pressure with transition from each previous step of evaporation to each further step of evaporation and with heating of evaporators of second step of evaporation and each further step of evaporation with vapour-like main product from corresponding previous step of evaporation, and also b) carried out is multi-step distillation in at least two steps of distillation, in each of which distillation column and evaporator are included, with supply into each following distillation step of bottom product from corresponding previous distillation step and with consecutive pressure increase with transition from each previous distillation step to further distillation step, as well as with heating of evaporator at each distillation step, excluding last distillation step, with vapour-like main product from distillation column corresponding to following distillation step, obtained during evaporation at last step of multi-step evaporation (a) product is supplied for distillation into first step of multi-step distillation (b).
EFFECT: method allows to reduce consumption of energy used for methanol recuperation.
8 cl, 1 dwg, 1 ex
SUBSTANCE: present invention relates to a method for synthesis of pentaerythritol and dipentaerythritol, involving reaction of acetaldehyde with formaldehyde in the presence of sodium hydroxide, purification of the reaction solution through distillation of excess formaldehyde, evaporation and crystallisation of technical pentaerythritol, washing the residue, recrystallisation of technical pentaerythritol, separation of the residue from the solution and drying commercial-grade pentaerythritol and treatment of the product after drying. After drying the product is treated through separation, thereby extracting the pentaerythritol fractions most contaminated with non-volatile impurities of dipentaerythritol and cyclic formalin, and the extracted fractions are processed by leaching pentaerythritol with demineralised water at 10-80°C and ratio of liquid phase to solid phase equal to (5.5-8)/1, and subsequent separation of the formed pentaerythritol solution and dipentaerythritol precipitate and taking the pentaerythritol solution to the technical pentaerythritol recrystallisation step.
EFFECT: method enables to obtain pentaerythritol with low content of dipentaerythritol and cyclic formalin impurities, as well as recycling of dipentaerythritol.
6 cl, 1 tbl, 7 ex
SUBSTANCE: present invention relates to a method of processing alcohol production wastes: concentrate of head impurities of ethyl alcohol (CHI) and an intermediate fraction of ethyl alcohol (IFEA). The method involves obtaining a water-alcohol solution of CHI or IFEA with density (0.837-0.940) g/cm3 (I) and conducting continuous extraction of impurities (C3-C5 alcohols, esters, carbonyl compounds) in a packed column with a mixture of aromatic hydrocarbons (II) or a mixture of aromatic and aliphatic hydrocarbons (III) with ratio of volume flow I: II or, respectively, I : III, equal to 1:(1-4) (preferably 1:1.2). To intensify mass exchange into solution (I), (0.1-0.5) wt % mixture (IV) of anionic alkyl sulphates and noionic oxyethylated alkyl phenols in ratio (25-20):(70-75) wt% (IV). The desired processing products: raffinate - aqueous of ethanol with weight ratio of the latter equal to (80-20) wt % can be used to obtain high-purity edible ethyl alcohol and as an anti-icing agent for glass used on cars, and extract - solution of alcohol and esters in a mixture of hydrocarbons is used to prepare mixed solvents for the paint industry.
EFFECT: high efficiency of the method of processing alcohol production wastes.
4 cl, 8 ex, 1 tbl, 2 dwg
SUBSTANCE: present invention relates to a method of producing dehydrated ethyl alcohol, which can be used in chemical, electronic and pharmaceutical industry. The method involves feeding crude alcohol or a water-alcohol solution into a preliminary dehydration column operating under a vacuum to obtain a distillate which is fed into a final dehydration column operating at excess pressure, where dehydrated alcohol is collected in form of a residue and the distillate is fed into the preliminary dehydration column in form of reflux. The distillation process in the preliminary dehydration column takes place at absolute pressure of 8.0-13.3 kPa to obtain a distillate with alcohol content 98.2-98.9 vol. %, and the distillation process in the final dehydration column takes place at absolute pressure 0.1-0.5 MPa and alcohol content in the reflux of 96.5-97.2 vol. %.
EFFECT: method enables to obtain an end product of high quality using an improved an improved process scheme.
1 tbl, 1 dwg, 2 ex
SUBSTANCE: invention relates to cleaning of ethanol used as solvent for optical measurements. Proposed method consists in processing ethanol by oxidiser and base with subsequent rectification. Note here that iodine in concentration of, at least, 0.0125 wt % is used as oxidiser. Note also that processing by iodine and base is performed in boiling.
EFFECT: lower costs, translucent (up to 210 nm) ethanol.
SUBSTANCE: present invention relates to a method of separating liquid phase by-products of Fischer-Tropsch synthesis, which involves the following steps: a) feeding the liquid phase by-products into a standard fractionation column (1) in its middle part with output of a portion of the stream I, having a boiling point range from 50 to 120°C, as a side cut to obtain light components having boiling point below 50°C from the top of the column, and heavy components, having boiling point higher than 120°C from the bottom of the column; b) feeding the stream I into a column (2) for separating acetic acid in its middle part to obtain a stream of aqueous solution II, containing alcohols and ketones, having boiling point range from 50 to 100°C from the top of the column, and a stream III of aqueous solution of acetic acid from the bottom of the column; and c) feeding the stream II into a column (3) for separating ethanol in its middle part to obtain a stream IV of a mixture of methanol and acetone from the top of the column and a stream V of aqueous solution of ethanol and n-propanol from the bottom of the column (see dwg 3).
EFFECT: high efficiency of the process.
9 cl, 4 dwg, 30 tbl, 30 ex
SUBSTANCE: invention relates to improved method of obtaining polyols, which includes the following stages: a) oxidation of unsaturated natural fats, unsaturated natural fatty acids and/or esters of fatty acids with dinitrogen oxide; b) interaction of the product, obtained at stage a), with hydrating reagent in presence of catalyst, which contains, at least, one transition metal from groups from 6 to 11; c) interaction of the reaction product from stage b) with alkylene oxides in presence of multimetalcyanide catalyst. Invention also relates to method of obtaining polyurethanes, which includes oxidation of unsaturated natural fats, unsaturated natural fatty acids and/or esters of fatty acids with dinitrogen oxide, interaction of the obtained product with hydrating reagent in presence of catalyst, which contains, at least, one transition metal from groups from 6 to 11, interaction of the reaction product with alkylene oxides in presence of multimetalcyanide catalyst with obtaining polyols, interaction of polyisocyanates with polyols as compounds, which have two hydrogen atoms, reactionable with respect to isocyanate groups.
EFFECT: simple methods make it possible to obtain wide spectrum of products without application of expensive initial reagents.
10 cl, 8 ex
FIELD: technology for production of methanol from syngas.
SUBSTANCE: claimed method includes mixing of hydrocarbon raw material with water steam to provide syngas by steam conversion of hydrocarbon raw material and subsequent methanol synthesis therefrom. Conversion of hydrocarbon raw material and methanol synthesis are carried out under the same pressure from 4.0 to 12.0 MPa. In one embodiment hydrocarbon raw material is mixed with water steam and carbon dioxide to provide syngas by steam/carbonic acid conversion of hydrocarbon raw material in radial-helical reactor followed by methanol synthesis therefrom under the same pressure (from 4.0 to 12.0 MPa). In each embodiment methanol synthesis is carried out in isothermal catalytic radial-helical reactor using fine-grained catalyst with grain size of 1-5 mm. Methanol synthesis is preferably carried out in two steps with or without syngas circulation followed by feeding gas from the first or second step into gasmain or power plant.
EFFECT: simplified method due to process optimization.
12 cl, 3 tbl, 3 dwg
FIELD: organic chemistry, chemical technology.
SUBSTANCE: invention relates to the improved method for preparing methanol. Method involves the successive feeding hydrocarbon-containing gas, injection of chemically purified water, carrying out the preliminary steam reforming for preparing synthesis gas and carrying out the final reforming if formed gas with addition of oxygen under pressure for carrying out synthesis of methanol, heating reactor for preliminary reforming by flow of obtained synthesis gas going out from reactor for the final reforming that is fed to intertubular space of reactor for preliminary reforming followed by cooling synthesis gas obtained as result of reforming by vapor-gas mixture and carrying out synthesis of methanol in 2-step reactor. Cooling the reaction mixture for carrying out isothermal reaction for synthesis of methanol in intermediate external heat exchanger of two-step reactor is carried out with vapor-gas mixture and cooling flow going out from reactor for synthesis of methanol is carried out with vapor-gas mixture and chemically purified water. Also, invention relates to unit for preparing methanol including the source of hydrocarbon-containing gas and unit for complex preparing gas, reactor for preliminary vapor reforming heated with flow going out from reactor for final reforming, two-step reactor for synthesis of methanol, heat exchangers for cooling synthesis gas, heat exchangers for cooling flow going out from reactor for synthesis of methanol, separator for separation of reaction products and exhausting gases and crude methanol. The unit for preparing methanol is assembled with unit for complex gas preparing including block for preparing chemically purified water, block for preparing raw, additional manufacture involving torch making, cleansing constructions, sources of electric energy, air of control and measuring instruments and automatic equipment, chemical laboratory and operating block. Two-step reactor for synthesis of methanol joined with heat exchanger for cooling synthesis gas with vapor-gas mixture, intermediate external heat exchanger for cooling the reaction mixture with vapor-gas mixture is joined in-line with heat exchanger for cooling flow obtained in reactor with vapor gas mixture, heat exchanger for cooling of chemically purified water and separator for separation of reaction products. Ignition device is assembled in reactor for final reforming that promotes to carry out the start of unit without trigger furnace. Water is injected in flow hydrocarbon gas directly before heat exchanger for the reaction mixture that provides excluding boiler-utilizer and trigger boiler from schedule and to solve the problem for cooling the reaction mixture in reactor for synthesis of methanol also. Based on integration of the device for preparing methanol in technological schedule with unit for complex preparing gas and significant change of the conventional schedule for preparing methanol method provides 3-fold reducing capital investment.
EFFECT: improved method for preparing methanol.
2 cl, 1 dwg
FIELD: organic chemistry, chemical technology.
SUBSTANCE: method for synthesis of methanol involves the following stages: removing hydrocarbon gas to be processed, sulfur elimination, catalytic steam conversion to obtain converted gas, heat utilization with separation of water, synthesis of methanol and separation of condensed methanol. Hydrocarbon gas with unstable composition is removed under pressure 0.001 MPa, not less, and sulfur elimination of hydrocarbon gas with unstable composition is combined with stage of step-by-step stabilization of pressure to form steam-gaseous mixture. Methanol synthesis is carried out for at least two successive flow steps with reducing volume of catalyst under pressure 1.5 MPA, not less, and separation of methanol between successive stages. Method provides significant reducing cost of gas processing and service of devices and allows carrying out the processing in mobile traveling devices in field conditions. Invention can be used in processing gas with unstable composition, for example, casing-head petroleum gas in petroleum-extracting holes, in field conditions in small traveling devices.
EFFECT: improved preparing method.
2 cl, 2 dwg
FIELD: organic chemistry, chemical technology.
SUBSTANCE: invention relates to a new method for preparing methanol and other aliphatic alcohols by gas-phase interaction of hydrocarbon gases with water vapor under effect of ultraviolet radiation. Methanol and other aliphatic alcohols are prepared by direct hydroxylation of hydrocarbon gas or mixture of hydrocarbon gases with water vapor. For this aim hydrocarbon gas and vapor or mixture of gases and vapor are fed into reactor wherein the reaction mass is subjected for effect of ultraviolet radiation in wavelength range 240-450 nm at temperature lower vapor formation point. The end product is isolated from vapor-gaseous mixture by condensation and unreacted gas or mixture of gases removed from the reaction zone is purified from the end product by bubbling through water layer and recovered into reactor by adding the parent gaseous component in the amount equal to consumed one. The process is carried out for a single stage and can be realized under atmosphere pressure. Invention can be used in chemical, petroleum chemical, petroleum processing and petroleum and gas extracting industry.
EFFECT: improved preparing method.
2 cl, 1 tbl, 8 ex