Method of processing carbon-carbonate mineral

FIELD: chemistry.

SUBSTANCE: method of processing carbon-carbonate mineral involves burning limestone in a reactor, obtaining calcium oxide, production of calcium carbide by reacting part of calcium oxide obtained from burning limestone with carbon, bringing part of the obtained calcium carbide into contact with water, obtaining acetylene and caustic lime, bringing gaseous wastes from burning limestone into contact with water to obtain carbonic acid. Limestone is burnt using heat obtained from burning part of the volume of acetylene, obtained from part of the volume of calcium carbide. At least part of the obtained acetylene is used in synthesis of ethanol and/or dichloroethane and/or ethyleneglycol and/or acetone. During synthesis of ethanol and/or dichloroethane, acetylene is reacted with hydrogen in the presence of palladium as catalyst, after which at least part of synthesised C2H4 material is reacted with water vapour, obtaining ethanol, and/or reacted with chlorine, obtaining dichloroethane. Also at least part of the obtained acetylene is subjected to hydrolysis, obtaining ethyleneglycol. Also during synthesis of acetone, part of the obtained acetylene is reacted with water vapour, where the hydrogen obtained is used in said synthesis of ethanol and/or dichloroethane and/or burnt in the burning process. Carbon dioxide obtained from synthesis of acetone is used in the process of producing carbonic acid.

EFFECT: wide range of obtained finished products and prevention of formation of industrial wastes.

4 cl, 1 ex, 1 dwg

 

The invention relates to a method of processing Plekhanovo minerals and can be used in deep processing of obtaining calcium carbide and/or acetylene.

A method of refining Plekhanovo mineral raw materials, including the burning of limestone in the reactor feed into it and the burning of high-temperature energy source (SU # 1449553, SW 2/02, 1989).

However, this technical solution is also a small range of derived products (lime), low environmental friendliness of the production process, in addition, complicated process to ensure the production of high-temperature energy source.

Also known is a method of processing Plekhanovo mineral raw materials, including the burning of limestone in the reactor with the receipt of calcium oxide, when used for roasting heat generated by the combustion of part of the amount of acetylene produced from the amount of calcium carbide, as one of the products of the recycling process, along with caustic calcium and carbonic acid (RU 2256611, SW 31/32, SW 2/02, C01F 11/06, SS 11/24, 2005).

However, in this solution a small depth of processing of the source material, resulting in a range of derived products expanded with the simplest of materials that do not have high demand in the market.

The task we address is the proposed solution, is the expansion of the spectrum produced commercial products, and the elimination of environmental pollution waste production.

The technical result is expressed in the expansion of the spectrum produced commercial products of deep processing of acetylene with high commercial potential (ethanol, dichloroethane, ethylene glycol, acetone), while ensuring a high level of diversification of production and the elimination of the appearance of man-made waste.

The problem is solved in that a method of processing Plekhanovo mineral raw materials, including the burning of limestone in the reactor with the receipt of calcium oxide, the production of calcium carbide by the reaction of parts of calcium oxide obtained by calcination of limestone, carbon, contacting the portion of the amount received calcium carbide with water to obtain acetylene and caustic calcium, contacting the waste gases of the burning process the limestone with water to produce carbonic acid, for burning limestone is used, the heat produced by the combustion of part of the amount of acetylene produced from the amount of calcium carbide, characterized in that at least part of the received acetylene use for the synthesis of ethanol and/or dichloroethane, and/or ethylene glycol and/or acetone, in the process of synthesis of ethanol and/or dichloroethane acetylene is introduced into reacts the Yu with hydrogen in the presence of palladium as a catalyst, then, at least a portion of the synthesized material With2H4enter into reaction with water vapor obtaining ethanol and/or react with chlorine to obtain dichloroethane, in addition, at least a portion of the acetylene is subjected to hydrolysis to obtain ethylene glycol, in addition, in the synthesis of acetone of a portion of the acetylene is introduced into reaction with water vapor, and hydrogen produced at the same time, used in the above-mentioned processes for the synthesis of ethanol and/or dichloroethane and/or burned in the firing process, with carbon dioxide, resulting from the synthesis of acetone, used in the process of obtaining carbonic acid. In addition, ethanol synthesized at pressures up to 80 bar and temperatures up to 300°C in the presence of sulfuric acid as a catalyst. In addition, the dichloride synthesized in the presence of Fe and FeCl2as the catalyst. In addition, acetone is synthesized in the presence of Fe and/or In the catalyst at temperatures up to 460°C.

Comparative analysis of the characteristics of the claimed solution with the characteristics of the prototype and analogues demonstrates compliance of the claimed solution to the criterion"novelty".

Signs of a distinctive part of the formula of the invention provide a solution to the following functional tasks.

Signs of "at least a portion of the acetylene used for the synthesis of et is Nola and/or dichloroethane, and/or ethylene glycol and/or acetone" enable spread spectrum produced commercial products of deep processing of acetylene with high commercial potential (ethanol, dichloroethane, ethylene glycol, acetone), thus providing a high level of diversification of production.

Signs in the synthesis of ethanol and/or dichloroethane acetylene is introduced into reaction with hydrogen in the presence of palladium as catalyst" provide an intermediate material (ethylene), used later to obtain ethanol and/or dichloroethane.

Signs "at least part of the synthesized material With2H4enter into reaction with water vapor obtaining ethanol" provide the possibility of obtaining ethanol.

Signs indicating that at least part of the synthesized material

With2H4enter "react with chlorine to obtain dichloroethane" provide the possibility of obtaining dichloroethane.

Signs "at least part of the received acetylene is subjected to hydrolysis to obtain ethylene glycol" provide the possibility of obtaining ethylene glycol.

Signs "in the synthesis of part of the obtained acetone acetylene is introduced into reaction with water vapor" specify the schema of the synthesis of acetone.

Signs indicating that the hydrogen produces the text (in the synthesis of acetone), use in the above-mentioned processes for the synthesis of ethanol and/or dichloroethane and/or burned in the firing process, provide opportunities for the recycling of waste one of the stages of production to their use either as a reagent or as an energy source.

Signs of "carbon dioxide produced during the synthesis of acetone, used in the process of obtaining carbonic acid" provide for the disposal of gaseous waste process for the synthesis of acetone with gaseous waste firing limestone turning them into additional product.

Signs of the second-fourth paragraphs formulas reveal the possible range of commercial products obtained in the proposed method.

The invention is illustrated by the drawing, which is a schematic diagram of implementation of the method.

To implement the method using a processing scheme, including reactors 1-4 schemes to generate acetylene, the first sampling unit 5, dispensers 6 and 7, the second sampling unit 8, naturally nodes 9 and 10, transportation of the node 11, the boot node 12, a coal-loading node 13, the pipeline 14, the pipeline 15, the water supply 16, the steam line 17, additional reactors 18-22, steam generator 23, the chlorine source 24, catalyzation nodes 25-28, the third sampling unit 29, the dispenser 30.

As the first reactor 1 is oven for life safety is ha limestone of known construction, equipped with loading the node 12, which feeds the limestone. The first reactor 1 is connected by a pipeline 15 to the first sampling unit 5 (which are used as known sets of gas-cleaning equipment, providing selection of CO2and the pipeline 14, for example made in the form of a guide channel with feeder 6, which provides the selection of the flow of lime (Cao) obtained by the calcination of limestone in the area designated for transmission to the consumer, it is clear that if this is not provided, this node is used only as a feeder of the second reactor 2.

As the second reactor 2 is a furnace for the production of calcium carbide, equipped with a coal-loading node 13 of known construction and sampling unit 8 (which are used as known sets of gas-cleaning equipment, providing the selection). If at this stage of production is provided by the use of acetylene as a high temperature energy source, a furnace for the production of calcium carbide must have appropriate heat exchange elements (not shown), supporting the use of waste heat generated by combustion of acetylene and transferring materials-reagents (Cao).

Sampling units 5 and 8 through pipeline 15 is connected with the third reactor 3, also connected to dipodoidea node 11 (made in the form of water containers, equipped with a pumping and metering and measuring equipment of known construction, providing pipeline 16 water flow in the reactor 3 for the synthesis of H2CO3and to the steam generator 23). The output of the third reactor 3 through produktovod 14 associated with the storage of carbon dioxide (not shown), the construction of which is determined by the form of supply of carbon dioxide to the consumer, i.e. liquefied or "dry ice", and does not differ from known designs.

The output of the reactor 2 through a pipeline 14, for example made in the form of a guide channel, is connected with the metering device 7 which enables the selection of the flow of calcium carbide produced in the reactor, part of the products intended for transmission to the consumer, it is clear that if this is not provided, this node is used only as a feeder of the second reactor 4.

As the fourth reactor 4 use the generator, designed for the generation of acetylene from calcium carbide. Reactor 4 is connected with the pump node 11, and his "gas" exit through the gas distribution unit 9 is associated with either a gas holder (not shown, designed for the storage of acetylene before sending it to the consumer), or with the gas distribution node 10, regulating the flow of acetylene in the reactors 1 and 2 (structurally, these nodes are similar to known Gator Opredelitel devices and are selected according to their operating parameters, the flow of acetylene and the section of pipeline 15). The second output of the reactor 4 through the respective pipeline 14 is associated with the storage of hydrated lime (not shown).

The reactor 18 is a hydrolysis reactor of known construction and is arranged to produce ethylene glycol. The reactor inlet is connected with the corresponding output distribution unit 9 through the pipeline 15 and the output store of ethylene glycol (not shown), the construction of which is known and determined by the properties of the stored product. Reactor reactor 19 is of known construction, made with the possibility of the synthesis of ethylene (C2H4used in the future for ethanol production and/or production of dichloroethane. The reactor contains catalization node 25 containing Pd as a catalyst for the reaction of acetylene with hydrogen, with the first gas inlet of the reactor 19 is connected with the corresponding output distribution unit 9 through the pipeline 15 and the second gas inlet is connected with the first gas outlet of the reactor 20 through the sampling unit 29 (which are used as known sets of gas-cleaning equipment, providing selection of H2). The output of the reactor 19 (ethylene) through the dispenser 30 is connected with the main inputs of the reactor 21 and 22.

The reactor 20 is react the rum of known construction, made with the possibility of the synthesis of acetone. The reactor contains catalization node 26 containing Fe or In, as a catalyst for the reaction of acetylene with water vapor, is supplied by known means of applying heat and is designed for a temperature of not less than 500°C, while the first gas inlet of the reactor 20 is connected with the corresponding output distribution unit 9 through the pipeline 15 and the second gas inlet is connected by a steam pipe 17 with the steam generator 23. The output of the reactor 20 is connected with the storage of acetone (not shown), the construction of which is known and determined by the properties of the stored product. His first gas outlet (hydrogen) through the sampling unit 29 is connected with the second gas inlet of the reactor 19 and the second gas outlet (carbon dioxide) through the first sampling unit 5 is connected with the reactor 3.

Reactor reactor 21 is of known construction, made with the possibility of the synthesis of ethanol. The reactor contains catalization node 27 containing H2SO4as a catalyst for the reaction of ethylene (C2H4) with water vapor, is supplied by known means of applying heat (e.g., providing waste heat obtained from the combustion of part of the volume of acetylene, and calculated at a temperature of at least 350-400°C, and the reactor inlet 21 through the dispenser 30 is associated with a corresponding vyhoda the reactor 19, in addition, the reactor 21 is connected by a steam pipe 17 with the steam generator 23. The output of the reactor 21 is associated with the storage of ethanol (not shown), the construction of which is known and determined by the properties of the stored product.

Reactor reactor 22 is of known construction, made with the possibility of synthesis of dichloroethane. The reactor contains catalization node 28 containing Fe and/or FeCl2as a catalyst for the reaction of ethylene (C2H4with chlorine, equipped with known means of applying heat (e.g., providing waste heat obtained from the combustion of part of the volume of acetylene, and calculated at a temperature of at least 350-400°C, and the reactor inlet 22 through the dispenser 30 is connected with the corresponding output of the reactor 19 in addition, the reactor 22 is connected with a source of chlorine 24. The output of the reactor 21 is connected with the storage dichloroethane (not shown), the construction of which is known and determined by the properties of the stored product. The design of other devices used to implement the method, no different from machines and devices designed to solve similar functional tasks.

The claimed method is implemented as follows.

Limestone is injected into the reactor 1 and produce his firing, which use the heat produced by the combustion of part of the amount of acetylene produced is from the amount of calcium carbide, get on the next stage of the process Plekhanovo mineral raw materials.

In the process of burning the limestone decomposes into lime and carbon dioxide according to the formula

Ready lime (Cao) remove the pipeline 14 to the dispenser 6, providing a selection of the total amount of lime used for transmission to the consumer, and the part intended for further processing. Part lime intended for further processing in the calcium carbide is fed to the second reactor 2, where in the presence of carbon (in the form of coke or coal particle size of 20-25 mm and a sulfur content of less than 1%) is converted into calcium carbide. The process of production of calcium carbide "is" according to the formula

Ready calcium carbide (CAC2) removes the pipeline 14 to the dispenser 7, providing a selection of the total production of parts of calcium carbide, intended for transmission to the consumer, and the part intended for further processing. Part of calcium carbide, used for conversion to acetylene, served in the fourth reactor 4, which is put into contact with water where and processed. Process for the production of acetylene "is" according to the formula CAC2+2H2O=C2H2+CA(Oh)2.

Slaked lime (CA(Oh)2) transmitted p is the consumer to use. Ready acetylene (C2H2) is removed through the pipeline 15 and through the gas distribution unit 9 is fed either to the consumer, or only in the first reactor 1, or the first and the second reactor 2, or used for the synthesis of ethanol and/or dichloroethane, and/or acetone, and/or ethylene glycol. The flow of acetylene in the respective reactors are controlled by the known distribution valves (not shown)installed on the branching pipeline 15 connecting gas distribution node 9 with the reactors 18, 19, 20 and 21.

While the synthesis of ethanol and/or dichloroethane carry out well-known scheme - initially synthesize ethylene, which is then used in the synthesis of target products (ethanol and dichloromethane)

With2H2+H2=C2H4With2H4+H2O=C2H5OH

Moreover, if the reaction is carried out at pressures up to 23 ATM and the temperature to 75-80°C, the yield of ethanol up to 90%, and at a pressure up to 80 bar and temperatures up to 280-300°C, the yield of ethanol reaches 95%.

Thus synthesis of dichloroethane are carried out by the well-known scheme using ethylene, introducing the latter into contact with chlorine

With2H4+Cl2=CH2Cl-CH2Cl

While ethylene glycol is produced by hydrolysis of acetylene.

While the synthesis of acetone is well-known scheme in tempera what ur about 460°C

With2H2+H2O(steam)=CH3PINES3+CO2+H2

Acetone is passed to the consumer, and gaseous products - waste process - utilizada on site (CO2used in the production of carbon dioxide and hydrogen in the synthesis of ethanol and/or dichloroethane). Of course, it is possible and combustion of hydrogen, i.e. the use as an energy source in the firing process or synthesis of acetone, but it is not the most expedient way of its use.

Thus, as the main processing products Plekhanovo mineral raw materials get calcium carbide, and/or calcium oxide and/or acetylene, and/or ethanol, and/or dichloroethane, and/or acetone, and/or glycol, as well as additional products are carbon dioxide and hydrated lime. However, in the presence of consumers and the appropriate additional components, the main products Plekhanovo mineral raw materials can be used for further processing in known schemes with obtaining, for example, superphosphate, urea, ammonia, etc.

Operational parameters of the implementation of the method at all stages do not differ from the known.

1. A method of processing Plekhanovo mineral raw materials, including the burning of limestone in the reactor with the receipt of calcium oxide, the production of calcium carbide by the reaction of the Asti of calcium oxide, obtained by calcination of limestone, carbon, contacting the portion of the amount received calcium carbide with water to obtain acetylene and caustic calcium, contacting the waste gases of the burning process the limestone with water to produce carbonic acid, for burning limestone is used, the heat produced by the combustion of part of the amount of acetylene produced from the amount of calcium carbide, characterized in that at least part of the received acetylene, is used for the synthesis of ethanol and/or dichloroethane and/or ethylene glycol and/or acetone, in the process of synthesis of ethanol and/or dichloride, acetylene is injected in the reaction with hydrogen in the presence of palladium as a catalyst, then at least part of the synthesized material-C2H4enter into reaction with water vapor obtaining ethanol and/or react with chlorine to obtain dichloroethane, in addition, at least a portion of the acetylene is subjected to hydrolysis to obtain ethylene glycol, in addition, in the synthesis of acetone, a portion of the acetylene is introduced into reaction with water vapor, and hydrogen produced at the same time, used in the above-mentioned processes for the synthesis of ethanol and/or dichloroethane and/or burned in the firing process, with carbon dioxide, resulting from the synthesis of acetone, used in the process of obtaining the angle of the Noah acid.

2. The method according to claim 1, characterized in that ethanol is synthesized at pressures up to 80 bar and temperatures up to 300°C in the presence of sulfuric acid as a catalyst.

3. The method according to claim 1, characterized in that the ethylene dichloride synthesized in the presence of Fe and FeCl2as a catalyst.

4. The method according to claim 1, wherein the acetone is synthesized in the presence of Fe and/or In the catalyst at temperatures up to 460°C.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: method of producing cumene includes interaction of benzene with acetone and hydrogen with catalytic compound added as containing one or more zeolite in acid form or preferentially acid form, copper and, optionally, one or more element chosen from elements of groups IIIA, VIB, VIIB. Additionally the given invention concerns method of producing phenol with using cumene prepared by the method as described, catalytic compound for production cumene, and also methods of producing catalytic compound for cumene.

EFFECT: application of the methods and catalytic compounds specified above allows simplifying considerably producing phenol from cumene, allowing for simultaneous one-stage reaction for all chemical transformations required to produce high-yield cumene from acetone, benzene and hydrogen with minimum amount of secondary reactions of various reagents, intermediate compounds and products.

69 cl, 16 ex, 2 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: one of method versions is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification and possibly partial recycling into reaction zone(s) of one or several components of reaction mixture. Decomposition is carried out in presence of inert easily-boiling solvent, which contains mainly hydrocarbons, whose boiling temperature is lower than 70°C, preferably lower than 40°C, but not lower than minus 1°C, which is partially evaporated directly from reaction zone(s) and partially distilled from obtained reaction mixture, is in liquid state returned to reaction zone(s) with supporting in it (them) temperature from 1 to 70°C, preferably from 10 to 45°C. Second method version is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification. Applied is easily-boiling solvent, which after separation from reaction mixture, possibly with part of ketone, is recycled into reaction zone(s), and sulfocationite catalyst in H+ form, resistant in liquid media, containing alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons in large amount, at temperatures up to 70°C, in fine-grain or coarse-grain form, possibly, in form of mass-exchange filling with size from 1.5 to 25 mm.

EFFECT: obtaining phenol and ketones without formation of large amount of by-products and resins and practically without equipment corrosion.

14 cl, 1 dwg, 6 ex

FIELD: chemistry.

SUBSTANCE: cumane hydroperoxide is decomposed in presence of catalyst from processed with acid clay in order to transform cumane hydroperoxide into mass, which after decomposition contains mainly phenol and acetone, and mass reaction after decomposition is carried out in presence of cation catalyst, composed of cation-exchange resin and mercaptane promoter or promoter in form of mercaptoalkane acid in order to transform phenol and acetone in mass after decomposition mainly into diphenol A.

EFFECT: high product output with low admixture formation without necessity of stages of intermediate purification.

10 cl, 3 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: cumane hydroperoxide is decomposed in presence of acid catalyst from sulfated metal in order to transform cumane hydroperoxide into mass, which after decomposition contains mainly phenol and acetone, and mass reaction after decomposition is carried out, preferably without intermediate purification, in presence of cation catalyst, composed of cation-exchange resin and mercaptane promoter or promoter in form of mercaptoalkane acid in order to transform phenol and acetone in mass after decomposition mainly into diphenol A.

EFFECT: high product output with low admixture formation without necessity of stages of intermediate purification.

10 cl, 3 dwg, 6 ex

FIELD: chemistry.

SUBSTANCE: H-form of ultrastable dealuminated Y-zeolites HUSY with SiO2/Al2O3 ratio within 5 to 120 is used as catalyst. As a rule, zeolites are combined with a binding agent represented by aluminum oxide, silicon oxide or their mix. Usually the catalyst is preliminarily activated by calcination in air at 300-600°C, while the method is implemented at 20-100°C. As a rule, cumol hydroperoxide concentration in the raw mix varies within 3 to 80%, and acetone, cumol, phenol or their mix with various component ratio are used as solvent.

EFFECT: increased process selectivity in relatively mild conditions.

7 cl, 1 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: method includes two-stage acid-catalysed decompounding of cumene hydroperoxide in series reactors under heat resulted in simultaneous generation dicumene peroxide in the first stage followed with its decompounding in reaction medium environment in the second stage. Thus any catalytic agent is not used; it is prepared in separate reactor immediately prior to introduce to the first reactor of cumene hydroperoxide decompounding by mixing sulphuric acid with phenol in ratio 2:1 to 1:1000 and keeping produced mixture at temperature 20-80°C within 1-600 minutes.

EFFECT: method allows for considerable yield reduction of hydroxyacetone.

4 cl, 7 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to the method of obtaining phenol and acetone by acid-catalysable decomposition of hydro-peroxide of cumene in the environment of the reaction products at elevated temperatures in one stage. In this case the process is carried out in the presence of a catalyst, prepared immediately before its introduction into the reactor for the decomposition of hydro-peroxide of cumene by mixing sulfuric acid with phenol at the ratio of from 2:1 till 1:1000 and the waiting time from mixing till putting into the reactor for the decomposition of hydro-peroxide of cumene from 1 to 600 minutes at a temperature from 20 to 80°C. As a rule, sulfuric acid has a concentration of higher than 75% or oleum is used.

EFFECT: it makes it possible to decrease the output of the by-product hydroxyacetone, improves the quality of market-grade phenol and decreases the consumption of sulfuric acid.

2 cl, 4 tbl, 4 ex

FIELD: main organic synthesis.

SUBSTANCE: proposed method is used for production of ketones, for example dimethyl ketone (CH3COCH3), methyl ethyl ketone (CH3COC2H5) by direct catalytic oxidation of respective alkenes, for example propylene, n-butenes, as well as catalysts for realization of this method. Oxidation of alkenes is performed in the presence of metallocomplex catalysts containing organic component where nitrogen oxide (I) is used as oxidant. Used for process is catalyst on base of peroxopolyoxo metallate complexes of terakis (oxo diperoxo metallate)-phosphate (3-) together with quaternary ammonium cationes having formula Q3{PO4[MeO(O2)2]4}, where Me-Mo, W,V; Q3 is quaternary ammonium catione containing alkyl chains C4-C8 or N-hexadecyl pyridinium.

EFFECT: enhanced selectivity of process.

10 cl, 14 ex

FIELD: chemical industry; methods of production of phenol and acetone.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the industrial process of production of phenol and acetone by the cumene method. The method is realized by decomposition of the technological cumene hydroperoxide in the in series connected reactors in two stages with formation on the first stage of the dicumylperoxide at the temperature of 40-65°С at presence as the catalytic agent of 0.003-0.015 mass % of the sulfuric acid with its subsequent decomposition on the second stage in the reaction medium at the temperature of 90-140°С. The process is conducted at the excess of phenol in the reaction mixture at the molar ratio of phenol : acetone exceeding 1, preferentially - from 1.01 up to 5. Excess of phenol is formed either by distillation (blowing) of acetone or addition of phenol in the reaction medium. The technical result of the invention is reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

EFFECT: the invention ensures reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

5 cl, 4 ex, 8 tbl

FIELD: organic chemistry, in particular production of carbonyl compounds such as aldehydes and ketones.

SUBSTANCE: claimed method includes reaction of nitrous oxide with alkenes in presence of inert gas as diluent. Reaction is carried out in gas phase at 401-700°C and under pressure of 2-300 atm. Target compounds represent value intermediates for precise and base organic synthesis.

EFFECT: method of high selectivity in relation to target products and improved explosion proofing.

5 cl, 1 tbl, 14 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing glycol aldehyde, involving reaction of formaldehyde with hydrogen and carbon monoxide in the presence of a catalyst composition, which is based on a) rhodium source, b) ligand with general formula R1P-R2 (I), where R1 is a bivalent radical, which, together with the phosphorous atom to which it is bonded, is 2-phospha-1,3,5,7-tetraC1-20alkyl-6,9,10-trioxatricyclo[3.3.1.1{3,7}]decile group, and where R2 is a monovalent radical, which is chosen from an alkyl group, containing 4 to 34 carbon atoms or a radical with general formula: -R3-C(O)NR4R5 (II), where R3 represents methylene, ethylene, propylene or butylene, and R4 and R5 independently represent an alkyl group containing 1 to 22 carbon atoms, and c) anion source. The invention also relates to a catalyst composition used in the production of glycol aldehyde, and to a method of producing ethylene glycol from glycol aldehyde obtained using the described method.

EFFECT: easy conversion of formaldehyde to glycol aldehyde in the presence of a stable catalyst.

6 cl, 11 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to methods of producing a catalytic composition, to the method of producing olefin oxide and method of producing 1,2-diol or 1.2-diol ether. Described is a method of producing a catalytic composition, involving deposition of silver on a carrier and deposition of a promoter - alkali metal on the carrier. The alkali metal contains potassium in amount of at least 10 mcmol/g and lithium in amount of at least 1 mcmol/g in terms of mass of catalytic composition. The alkali metal is deposited on the carrier before depositing silver, at the same time or after depositing silver on the carrier. Described is a method of producing a catalytic composition, involving use of potassium as a promoter in amount of at least 10 mcmol/g and sodium in amount of at least 5 mcmol/g in terms of mass of the catalytic composition. Description is given of a method of producing olefin oxide by reacting olefin, which has at least three carbon atoms, with oxygen in the presence of a catalytic composition, obtained using the method described above. This invention also pertains to the method of producing 1,2-diol or 1,2-diol ether using olefin oxide, obtained using the said method.

EFFECT: increased selectivity and stability of the catalytic composition.

20 cl, 5 tbl, 37 ex

FIELD: medicine.

SUBSTANCE: method of inhibiting polyresistant bacteria growth includes local introduction of pharmaceutical composition, containing 15 wt % or more of pentan-1,5-diol and pharmaceutically acceptable carrier. Method of disinfecting bacteria-contaminated surface includes obtaining disinfecting composition, which contains 15 wt % or more of pentan-1,5-diol and water carrier, application of said composition onto said surface; possibly, keeping it in contact with said surface for time period from 5 minutes to 24 hours at environment temperature and washing said surface with water or water composition with detergent.

EFFECT: inhibiting polyresistant bacteria and eliminating risk of further selection of poliresistant bacterial strains.

18 cl, 2 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention refers to method of producing 1,3-propanediol by hydrogenation of 3-hydroxypropanal (versions). The first version of the method includes the stages as follows: (a) formation of aqueous 3-hydroxypropanal mixture, (b) delivery of aqueous mixture containing 3-hydroxypropanal through hydrogenation zone wherein it includes, at least, two stages with hydrogenation at the first stage performed at temperature 50 to 130°C with static bed of suspended in the presence of a motionless layer hydrogenation catalyst, and with at least, one of last stages involves adding acid cocatalyst, or acid cocatalyst is being chosen of the group consisting of acid zeolites, acid cation-exchange resins, acid or amphoteric metal oxides, heteropolyacids, and soluble acids chosen of the group consisting of mineral acids, phosphoric acid, acetic acid, propionic acid and 3-hydroxypropionic acid, herewith hydrogenation at the specified last stages is performed at higher temperatures, than at the first stage, within 70 to 155°C, to produce 1,3-propanediol aqueous solution; and (c) release of 1,3-propanediol specified.

EFFECT: invention makes enables effective reverse reaction with improved-yield transforming acetal by-products in 1,3-propanediol.

24 cl, 3 tbl, 18 ex

FIELD: chemistry.

SUBSTANCE: method of obtaining 1,3-propandiol includes preparation of 3-hydroxypropanal water solution; removal from solution catalyst, probably used during said preparation; adding to solution hydroxide, selected from group, consisting of ammonium hydroxide, alkali metal hydroxides, alkali earth metal hydroxides, except sodium hydroxide, for neutralization of any contained in it acid in such way that pH constitutes at least 5; hydrogenating neutralised water solution in order to obtain mixture of raw 1,3-propandiol, which is subjected to distillation, obtaining 1,3-propandiol, water and reaction-able heavy components.

EFFECT: reduction of viscosity of reaction-able heavy components.

6 cl, 5 ex

FIELD: chemistry.

SUBSTANCE: method of separating multi-atom alcohols, for instance, neopentylglycol and sodium formiate, includes evaporation and cooling of reaction mixture, addition of organic solvent, crystallisation of sodium formiate, separation of sodium formiate from saturated solution of multi-atom alcohol, for instance, by filtration, and crystallisation of multi-atom alcohol. Reaction mixture is evaporated until two liquid layers are formed, which are separated into light phase - water-multi-atom alcohol and heavy phase -water-salt, separated water-salt fraction of solution is cooled until sodium formiate contained in it in form of cryslallohydrate is crystallised, sodium formiate crystals are separated, and remaining mother-solution is returned to process head, to evaporation stage, then separated light phase - water-multi-atom alcohol is additionally evaporated until 70% of contained in it sodium formiate is crystallised, then cooled to 25-30°C and subjected to processing with organic solvent from line of single-atom saturated alcohols, for instance, methane, for removal of remaining admixtures, with further crystallisation of multi-atom alcohol from remaining mother-solution.

EFFECT: reduction of amount of used organic solvent, elimination of high-temperature stage of extraction, preservation of yield of pure target products.

2 cl, 2 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: principle refers to the method of producing olefin oxide, method of application of the produced olefin oxide and the production of 1,2-diol or simple ether 1-,2-diol and catalytic composition. The mentioned catalytic composition for the production of olefin oxide contains silver and activating agent, that consists of an alkaline metal on a bearer where the activating alkaline metal contains potassium whose quantity is not less than 5 mcmol/g of metal relative to the mass of the catalytic composition and not less than 1 mcmol/g alkaline metal from the group that contains lithium, sodium and there mixtures in which the mentioned bearer contains calcium carbonate joined with silver. The relative mass of silver: calcium carbonate is 1:5 to 1:100, and the unit surface area of the bearer is from 1 m/g to 20 m/g, and the apparent porosity of the bearer is 0.05 ml/g to 2 ml/g. The explained method of producing olefin oxide, include interaction of olefin, that has 3 or more carbon atoms, with oxygen in the presence of the above mentioned catalytic system, and the method of producing 1,2-diol or simple ether 1,2-diol, in which the olefin oxide is produced from the explained method.

EFFECT: increasing of selectivity, activity and stability of catalyst.

10 cl, 5 tbl, 37 ex

FIELD: organic chemistry, biotechnology.

SUBSTANCE: invention relates to variants of a method for extraction of 1,3-propanediol from enzymatic broth. The first variant involves steps for contacting enzymatic broth containing water, 1,3-propanediol and at least one impurity chosen from glycerol, glucose and butanetriol with at least one extractant chosen from alkanols, ketones, esters, acids, ethers or vegetable oils to form the first mixture. Then the first mixture is separated for the first phase and the second phase wherein the first phase comprises the greater part of extractant and at least some amount of 1,3-propanediol from enzymatic broth in the mass ratio 1,3-propanediol to at least one component taken from glycerol, glucose or butanetriol in the first phase above the mass ratio 1,3-propanediol and the same impurity in enzymatic broth before contacting enzymatic broth with the extractant wherein the second phase comprises the greater part of water and at least some amount of impurity from enzymatic broth followed by extraction of 1,3-propanediol by separation of the first phase from the second phase, contacting the first separated phase with aqueous solution to form the second mixture, and separation of the second mixture for the third and forth phases wherein the third phase comprises the greater part of the extractant from the first phase, and wherein the fourth phase comprises 1,3-propanediol and the greater part of the first amount of the first amount of aqueous solution, and wherein the mass ratio in the forth phase of 1,3-propanediol to any presenting mixture is more as compared with the mass ratio of 1,3-propanediol to the same impurity in the enzymatic broth being before contacting the enzymatic broth with the extractant, and extraction of 1,3-propanediol, and separating the fourth phase from the third phase. Invention provides enhancing purity of 1,3-propanediol.

EFFECT: improved method of extraction.

30 cl, 15 tbl, 9 dwg, 10 ex

FIELD: chemical technology.

SUBSTANCE: invention relates to a method for synthesis of 1,3-propanediol involving the following steps: (a) formation of aqueous solution of 3-hydroxypropanal; (b) hydrogenation of 3-hydroxypropanal to form crude mixture of 1,3-propanediol, water and cyclic acetal of molecular mass 132 Da (MW 132 cyclic acetal) and/or cyclic acetal of molecular mass 176 Da (MW 176 cyclic acetal); (c) distillation (drying) of indicated crude mixture of 1,3-propanediol for water removing and formation of the second crude mixture of 1,3-propanediol (the first flow of residues after distillation) containing 1,3-propanediol and MQ 132 cyclic acetal and/or MW 176 cyclic acetal; (d) contact of the flow containing MW 132 cyclic acetal and/or MW 176 cyclic acetal with acid-base cation-exchange resin or with acid zeolite, or with soluble acid, and (e) removal of MW 132 cyclic acetal. Method provides enhancing effectiveness for extraction and purification of 1,3-propanediol.

EFFECT: improved method of treatment.

10 cl, 9 tbl, 1 dwg, 6 ex

FIELD: chemical technology, catalysts.

SUBSTANCE: invention relates to a method for catalytic conversion of organic carbonate to a corresponding alcohol. Method involves contacting organic carbonate with alcohol or water in the presence of zinc catalyst on a carrier. Reactive particles on the zinc catalyst carrier are retained by a carrier separately, and the indicated catalyst can be represented by the formula: Zn/MxAy wherein M represents metal; A represents nonmetal, and x and y can have values 0-3. Except for, invention relates to using abovementioned catalyst on a carrier for alcoholysis or hydrolysis of organic carbonate. Method provides increasing conversion of organic carbonates.

EFFECT: enhanced effectiveness of conversion, improved and valuable properties of catalyst.

11 cl, 1 tbl, 1 ex

FIELD: food products; alcoholic beverages.

SUBSTANCE: according to the method, initial flow is supplied to the first distillation steam-stripping column while its distillate is passed to the second distillation rectifying column. Initial flow is refined using first membrane separation method. Obtained concentrate is passed to the first distillation column and derived permeate is supplied to the second distillation column. Distillate from the second distillation column is refined using second membrane separation method.

EFFECT: increasing pureness of obtained ethanol.

16 cl, 2 dwg, 2 tbl

Up!