Method of concentrating aqueous hydrogen peroxide solution

FIELD: chemistry.

SUBSTANCE: method is carried out in a device which includes a preliminary evaporating apparatus, a distillation column and a secondary steam compressor. The aqueous hydrogen peroxide solution to be concentrated is continuously fed into the preliminary evaporating apparatus. The secondary steam generated in the preliminary evaporating apparatus by evaporation is fed into a distillation column. The bottom product obtained in the preliminary evaporating apparatus is collected in the form of a first concentrated hydrogen peroxide stream. The secondary steam generated in the distillation column is collected into the top part of the column, compressed in a secondary steam compressor and used to heat the preliminary evaporating apparatus, and the bottom product obtained in the distillation column is collected in the form of a secondary concentrated stream of hydrogen peroxide. Part of the bottom product obtained in the preliminary evaporating apparatus is fed into the distillation column in liquid state.

EFFECT: invention enables to simultaneously produce two concentrated aqueous solutions of hydrogen peroxide with different concentration in a freely selected ratio.

10 cl, 2 dwg

 

Hydrogen peroxide usually get antrahinonovye way in which through extraction used in antrahinonovye way of working solution produces hydrogen peroxide in the form of an aqueous solution with a content of from 25 to 40 weight percent. To reduce transport costs this crude product antrahinonovye how concentrated by evaporation of water to a standard concentration of 50, 60 or 70 mass percent. For special applications require purified hydrogen peroxide, from which, by distillation of the hydrogen peroxide is separated volatile ingredients pollution.

When the concentration of hydrogen peroxide costs of energy for evaporation of water can be reduced by compression obtained by the evaporation of water vapor and heating evaporation apparatus in the same compressed secondary steam, as we know from "A. Meili, Proceedings of the 2nd International Conference on Process Intensification in Practice, BHR Group Conference Series 28, 1997, pages 309-318" and Avenue "H2About2Sulzer Chemtech Distillation and Heat-Pump Technology for the Concentration and Purification of Hydrogen Peroxide" by Sulzer Chemtech.

Known from the prior art methods have the disadvantage that for the production of concentrated hydrogen peroxide of various concentrations of distillation conditions should change, and such change of conditions of distillation temporarily formed not appropriate specification of the product, which should return to the process. While the known methods are obtained concentrated hydrogen peroxide and distilled hydrogen peroxide in different concentrations, the ratio of the amounts of both of these products can vary only within narrow limits. There is therefore a need for energy-efficient method of concentrating aqueous solutions of hydrogen peroxide, through which can simultaneously be made at least two concentrated aqueous hydrogen peroxide solution with different concentration in the range of from 50 to 70 mass % in a freely selectable value.

It was found that this problem can be solved in that the device for concentrating aqueous solutions of hydrogen peroxide with advanced evaporation apparatus, distillation column and a secondary steam compressor is operated so that the secondary steam from the pre-evaporator, and the part obtained in the preliminary evaporation apparatus of the cubic liquid product is fed to the distillation column.

Therefore, the object of the invention is a method for concentrating an aqueous solution of hydrogen peroxide in two streams of hydrogen peroxide with different concentrations, in which the device includes a preliminary evaporation apparatus, distillation to the Onna and the secondary steam compressor, preliminary evaporation apparatus continuously fail to be concentrated aqueous solution of hydrogen peroxide produced in the preliminary evaporation apparatus for evaporating the secondary steam is led to the distillation column, the part obtained in the preliminary evaporation apparatus of the cubic product is supplied in a liquid state to a distillation column, and obtained in the preliminary evaporation apparatus CBM product is taken in the form of the first concentrated stream of hydrogen peroxide produced in the distillation column the secondary steam is withdrawn from the distillation column in the upper part of the column, is compressed in the compressor of the secondary steam and used for pre-heating evaporation apparatus, and obtained in the distillation column CBM product is taken in the form of the second concentrated stream of hydrogen peroxide.

In Fig.1 shows the famous Avenue "H2About2Sulzer Chemtech Distillation and Heat-Pump Technology for the Concentration and Purification of Hydrogen Peroxide", page 6, method.

In Fig.2 shows a variant implementation of the method according to the invention. The method according to the invention is carried out in the device, which includes a preliminary evaporation apparatus, distillation column and the secondary compressor pair.

As a pre-evaporator can be is used are known from the prior art device, which are known to the expert as suitable for evaporation of an aqueous solution of hydrogen peroxide.

Preferably, as a pre-evaporator is used a single-stage evaporator apparatus, preferably a single-stage circulation evaporator apparatus. In yet another embodiment, pre-evaporating device is evaporating apparatus with a falling film.

As distillation columns can be used all known from the prior art columns, which are known to the expert as suitable for the distillation of an aqueous solution of hydrogen peroxide. Preferably, use a distillation column, which has a reinforcing portion and the evaporating portion, and at least one power zone between these parts. Preferably, use a distillation column, which is to improve the separating ability contains a filling element of the nozzle or structured downloading. The elements of the nozzle or structured boot can be made of metal, plastic or ceramic material, and particularly preferred is loading or filling of the metal. Belonging to the distillation column of the evaporator can be made as a separate evaporator, as shown in Fig.2, or may be performed as part of di is Collezioni columns, as you know according to Fig.2 in EP 04195406 A1. Preferably, the distillation column is in the upper part of the feed line, which may be lled with water to form phlegmy.

As the compressor secondary steam can be used all known from the prior art device for compressing water vapor. Preferably, the secondary steam compressor uses a mechanical compressor secondary steam, particularly preferably a single-stage mechanical compressor of the secondary pair. With a mechanical compressor secondary steam achieves high energy efficiency, and it becomes possible wide operating range. Alternatively, as the compressor secondary steam can be used jet pump, and preferably uses a gas-jet pump with water vapor as the working gas. The use of gas-jet pump as a compressor secondary steam has the advantage of lower investment costs and higher availability because of the more simple techniques.

In the method according to the invention to be concentrated aqueous solution of hydrogen peroxide is continuously fed to the pre-evaporation apparatus. Preferably, we are talking about is contained in the stage extraction antrahinonovye sposobrostey of hydrogen peroxide aqueous solution of hydrogen peroxide, which contains from 25 to 40 weight percent of hydrogen peroxide. Preferably, you want to concentration aqueous hydrogen peroxide solution also contains at least one stabilizer for stabilizing hydrogen peroxide against decomposition. As a stabilizer can be used all known to stabilize the hydrogen peroxide compound. Preferably, the stabilizer is used stannate alkali metal pyrophosphates, alkali metal polyphosphates, alkali metal and chelate complexing agents from a number hydroxycarbonic acids, aminocarbonyl acids, aminophosphonic acids, phosphonocarboxylate acids and hydroxyphosphonic acids and their alkali metal salts. Particularly preferred stabilizers are stannate sodium, Na4P2O7, Na2H2P2O7, aminotris (methylenephosphonate acid) and its sodium salt, and 1-hydroxyethane-2,2-diphosphonic acid and its sodium salt.

In the preliminary evaporation apparatus part be summed concentration of an aqueous solution of hydrogen peroxide is evaporated, and the evaporation is preferably carried out at a pressure of from 70 to 130 mbar and the temperature of the cube evaporator from 49 to 69°C. Produced in a preliminary evaporation apparatus PR is the evaporation of the secondary pairs are fully or partially fed to the distillation column, moreover, the secondary steam is directed through an additional refrigerator in which a portion of the secondary vapor condenses and is collected as a concentrated stream of hydrogen peroxide. Due to such partial condensation of secondary steam in the method according to the invention at low cost in addition to the two concentrated streams of hydrogen peroxide with various concentrations can be obtained and distilled, thereby purified from volatile ingredients impurities stream of hydrogen peroxide. Developed in the preliminary evaporation apparatus upon evaporation of the secondary steam is fed to the distillation column, preferably in the middle section, i.e. between the evaporation part and the amplification part of the distillation column. Thanks connected with the secondary couple in the middle section of the distillation column can be reduced energy consumption for distillation.

From the obtained in the preliminary evaporation apparatus of the cubic product one part is fed in the liquid state to the distillation column, while the remainder is withdrawn as of the first concentrated stream of hydrogen peroxide. Supplied to the distillation column in a liquid state CBM product from the pre-evaporator is fed to the distillation column in the middle section, i.e. between the evaporating portion and the amplifying part. Thanks to the supply of liquid cubic product in the middle section of the distillation column can be reduced energy consumption for distillation.

In the distillation column through inlet heat the water evaporates and the resulting consequence of this CBM product distillation column is selected as the second concentrated stream of hydrogen peroxide. Developed the secondary vapor is withdrawn from the distillation column in the upper part, fully or partially compressed by the compressor of the secondary steam and is used for heating the pre-evaporator. The extent to which selected from the distillation column secondary steam is not supplied to the compressor of the secondary vapor, it condenses in the condenser of distillation columns. Preferably, the distillation column is operated at a pressure in the upper part of the column from 60 to 120 mbar and at a temperature of cube columns from 51 to 74°C. Preferably, the distillation column is operated so that the temperature of the distillation columns in the cube at 5-15° above the temperature in the cube pre-evaporator, and the concentration of the second concentrated stream of hydrogen peroxide is higher than the concentration of the first concentrated stream of hydrogen peroxide. Through this choice of the temperatures in the distillation column and pre the preliminary evaporation apparatus, the energy consumption for compression secondary steam can be maintained low. In one preferred embodiment, to create phlegmy not used condensed head product of the column and in the upper part of the column of water in the liquid state. This can be achieved particularly low content of hydrogen peroxide in the secondary pair and minimized loss of hydrogen peroxide with secondary steam. Preferably required for the distillation column pressure generated by a vacuum pump, which is connected with the upper part of the column, preferably through the condenser of the distillation column. Preferably required for pre-evaporator pressure determined by pressure balance between the distillation column and pre-evaporation apparatus through the pipeline, which developed in the preliminary evaporation apparatus of the secondary steam is fed to the distillation column.

Using the method according to the invention, based on the aqueous solution of hydrogen peroxide, can be simultaneously received two concentrated flow of hydrogen peroxide solution with different concentrations, and the concentration of both threads, preferably, is in the range from 40 to 80 mass % and, particularly preferably, in the range from 49 to 75 mass%. When this ratio is osenia quantities of both streams can be installed in a wide range of topics that obtained in the distillation column secondary steam sets the ratio between the share of which in the compressor of the secondary steam is used for heating the pre-evaporator, and the proportion which is condensed in the condenser distillation column, and that obtained in Cuba pre-evaporator cubic product is set to the ratio between the share of which in the liquid state is fed to the distillation column, and the fractions, which is extracted in the form of the first concentrated stream of hydrogen peroxide.

Fig.1 and Fig.2 illustrate methods according to the invention in comparison with known prior art method.

In Fig.1 shows the famous Avenue "H2About2Sulzer Chemtech Distillation and Heat-Pump Technology for the Concentration and Purification of Hydrogen Peroxide" by Sulzer Chemtech, page 6, way. If this be the concentration of the solution (4) of hydrogen peroxide is supplied to the pre-evaporation apparatus (1), and developed in the preliminary evaporation apparatus for evaporation of the secondary pairs (5) is fed to the distillation column (2). Obtained in the preliminary evaporation apparatus (1) CBM product (6) is selected as the first concentrated stream (7) of hydrogen peroxide and in the prospectus of the company Sulzer denoted as TG (Purge). Produced in distillation is alone (2) secondary pairs (8) is withdrawn from the distillation column (2) in the upper part of the column, is compressed by the compressor (3) secondary steam and is used for pre-heating evaporation apparatus (1). Obtained in the distillation column (2) CBM product (9) is selected as the second concentrated stream (10) of hydrogen peroxide and in the prospectus of the company Sulzer denoted as CG (Product). In this way the entire hydrogen peroxide, which is selected with the flow (10) of the hydrogen peroxide must be evaporated in the pre-evaporation apparatus (1), and the ratio of the amounts of threads (7) and (10) of the hydrogen peroxide at a given concentration of both streams of hydrogen peroxide can be installed only in a narrow range.

In Fig.2 shows a variant implementation of the method according to the invention. In contrast to the known method according to Fig.1 in this method, the part obtained in the preliminary evaporation apparatus (1) of the cubic product (6) is fed to the distillation column in a liquid state. By setting the proportion of the cubic product (6), which is fed to the distillation column, and the fraction which is withdrawn as a concentrated stream (7) of hydrogen peroxide, in the method according to the invention also given concentrations of threads (7) and (10) of the hydrogen peroxide ratio quantities between these flows can be set within wide limits. Because the share of hydrogen peroxide, which is applied to distill is operating the column in the liquid state, in the way that is not evaporated, compared with the method according to Fig.1 also requires less energy. In the form shown in Fig.2 embodiment, the part of the developed in the preliminary evaporation apparatus (1) due to the evaporation of the secondary pair (5) is condensed in an additional refrigerator (11) and is selected as the third concentrated stream (12) of hydrogen peroxide. In this embodiment, the method according to the invention may additionally be obtained in substantially purified by distillation from the volatile ingredients of impurities, hydrogen peroxide, and the amount and concentration of this purified hydrogen peroxide can be selected within wide limits by the choice of operating conditions for the pre-evaporator (1) and additional refrigerator (11).

The following example displays shown in Fig.2 a variant of the method according to the invention. Preliminary evaporation apparatus (1) is operated at a pressure of 120 mbar and the temperature of the cube 61°C. the Distillation column (2) is operated at a pressure in the upper part of the column 104 mbar and the temperature of the cube 70°C. prior To evaporating apparatus summarizes 10000 kg/h subject to concentration of solution (4) of hydrogen peroxide with a concentration of 40.0 mass%. In the preliminary evaporation apparatus is kg/hour secondary steam (5) with hydrogen peroxide mass of 8.5 percent. From the secondary steam partial condensation in the secondary refrigerator (11) produces a concentrated stream (12) of hydrogen peroxide with a concentration 45,1 mass percent in the amount of 152 kg/hour, and not the secondary steam condensed in the form of vapour is fed to the distillation column (2). From the cubic product (6) pre-evaporator selected 1830 kg/hour as a concentrated stream (7) of hydrogen peroxide with a concentration of 50.5 mass%, and the remaining residual VAT product is supplied in a liquid state to a distillation column (2). To the distillation column (2) to create phlegmy is supplied 769 kg/h of water. In the distillation column hydrogen peroxide by supplying 1487 kW of heat to the evaporator of the distillation column advanced and concentrated from the cube columns selected concentrated stream (10) of the hydrogen peroxide with a concentration of 70.5 weight percent in the number 4173 kg/hour. From produced in the distillation column secondary steam 1094 kg/hour compressed by the compressor (3) secondary steam to a pressure of 320 mbar, and through the compressed secondary steam heated pre-evaporating device (1). The rest produced in the distillation column secondary steam is condensed. The energy consumption for compression secondary steam ferry made in the form of isostring pump compressor secondary steam is 976 kW.

LIST of REFERENCE SIGNS IN the FIGURES

(1) pre-evaporating device

(2) distilling column

(3) the secondary steam compressor

(4) subject to concentration of the hydrogen peroxide solution

(5) the secondary steam from the pre-evaporator

(6) CBM product from the pre-evaporator

(7) the first concentrated solution of hydrogen peroxide

(8) secondary vapor from the distillation column

(9) CBM product distillation columns

(10) the second concentrated solution of hydrogen peroxide

(11) additional refrigerator

(12) the third concentrated solution of hydrogen peroxide

1. A method for concentrating an aqueous solution of hydrogen peroxide in two streams of hydrogen peroxide with different concentrations, and in the device, which includes a preliminary evaporation apparatus (1), the distillation column (2) and a compressor (3) secondary steam, prior to evaporating apparatus continuously fail to be concentrated aqueous solution (4) of hydrogen peroxide produced in the preliminary evaporation apparatus for evaporation of the secondary pairs (5) fail to distillation column obtained in the preliminary evaporation apparatus CBM product (6) is taken as the first of concentrated flow (7) of hydrogen peroxide, in the operated in the distillation column secondary pairs (8) is withdrawn from the distillation column in the upper part of the column, compressed in the compressor of the secondary steam and used for pre-heating evaporation apparatus, and obtained in the distillation column CBM product (9) is taken in the form of the second concentrated stream (10) of the hydrogen peroxide, characterized in that the part received in the preliminary evaporation apparatus of the cubic product supplied to the distillation column in a liquid state.

2. The method according to p. 1, characterized in that the input to the distillation column portion received in the preliminary evaporation apparatus of the cubic product supplied to the distillation column in the middle section.

3. The method according to p. 1, characterized in that developed in the pre-evaporation apparatus for evaporating the secondary steam is led to the distillation column in the middle section.

4. The method according to p. 2, characterized in that developed in the pre-evaporation apparatus for evaporating the secondary steam is led to the distillation column in the middle section.

5. The method according to one of paragraphs.1-4, characterized in that the part of the developed in the preliminary evaporation apparatus for evaporating secondary steam condense additional refrigerator (11) and selected in the third concentrated stream (12) of hydrogen peroxide.

6. The method according to one of paragraphs.1-4, characterized in that the temperature in the cube distillation to the Onna 5-15°C above the temperature in the cube pre-evaporator.

7. The method according to one of paragraphs.1-4, characterized in that the concentration of the second concentrated stream of hydrogen peroxide is higher than the concentration of the first concentrated stream of hydrogen peroxide.

8. The method according to one of paragraphs.1-4, characterized in that the secondary steam compressor using a mechanical compressor of the secondary pair, preferably a single-stage mechanical compressor of the secondary pair.

9. The method according to one of paragraphs.1-4, characterized in that as the compressor of the secondary pair of used gas-jet pump with water vapor as the working gas.

10. The method according to one of paragraphs.1-4, characterized in that use distillation column with loading or filling of the metal.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to the process of separating hydrogen peroxide from reaction mixtures obtained by oxidation of isopropyl alcohol, and can be used in chemical and textile industry as well as in medicine. A reaction mixture obtained after oxidation of isopropyl alcohol, which contains hydrogen peroxide, acetone, isopropyl alcohol, water, organic peroxides, acetic acid and phosphates, is mixed with sodium sodium metastannate in amount of 1-25 mg/l and subjected to vacuum rectification at absolute pressure of 23-36 kPa and bottom temperature of 76-84°C. 5-100 mg/l diethylene triamine pentamethylene phosphonic acid or salt thereof is added to the stream of aqueous hydrogen peroxide solution coming out of the column.

EFFECT: invention reduces loss of hydrogen peroxide during rectification, increases output thereof by 3-6%, especially when using, at the step for separating aqueous hydrogen peroxide solution, equipment made from stainless steel and high-efficiency nozzles characterised by a developed surface, and increases safety of the process and enables to obtain a stable hydrogen peroxide solution.

4 cl, 1 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing hydrogen peroxide, involving a liquid-to-liquid extraction step. Said extraction step involves contacting an organic solvent containing hydrogen peroxide with an extraction solvent containing less than about 30 wt % water to achieve hydrogen peroxide extraction in said extraction solvent and obtaining an extract containing hydrogen peroxide.

EFFECT: invention enables to obtain high-purity hydrogen peroxide.

25 cl, 2 tbl, 7 ex

The invention relates to chemical technology, in particular to the purification of substances from organic impurities, and can be used for the purification of hydrogen peroxide obtained by the oxidation of isopropyl alcohol, acetic acid

The invention relates to a method of efficient purification of an aqueous solution of hydrogen peroxide from acetic acid

FIELD: oil and gas industry.

SUBSTANCE: dispenser for nozzle irrigation in rectification and adsorption towers include the system of liquid delivery to the dispenser in the form channels with rectangular cross-section and openings in the lateral walls matched to groves shaped as triangle in standard cross-section for the purpose of liquid phase draining, in their lower part there are splitters for liquid jets as a bundle of dispersing elements matched in the lower part of the grooves with upper ends of the dispersing elements oriented downwards by the lower ends. The dispersing elements are placed at angle α in regard to each other and their length L is divided by the following formula: , where L is length of a dispersing element; a is a channel width, mm; b is a groove width, mm; N is a number of dispersing elements, pieces; α is the angle between dispersing elements, degrees.

EFFECT: invention allows increasing square area and uniformity of irrigation for the mass-exchanging nozzle.

3 cl, 5 dwg, 2 ex

FIELD: process engineering.

SUBSTANCE: invention relates to catalytic cleaning of green heavy oil distillates. Reactor comprises at least one bed layer, in fact, liquid phase L and, in fact, gas phase G located at reactor bottom and separated by interface 38 and distribution tray furnished with at least one main pipe to circulate liquid phase L in bed direction and at least one channel to feed gas phase G to said bed. Tray has at least one combined pipe to circulate liquid phase in bed direction or to feed gas phase into said bed.

EFFECT: higher quality of cleaning.

9 cl, 4 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to separation of hydrocarbons. Unit for stripping of first component from the mix comprises distillation column with rectifier section with top steam flow outlet, section with bottom fluid flow outlet and raw stock section with stock inlet arranged between rectifier section and evaporator section, reboiler of bottom residue for re-evaporation of bottom fluid flow coming from evaporator section, upper steam flow condensation section, lateral steam bleed pipe, heat pump-compressor with inlet communicated with said lateral bleed pipe and outlet, second reboiler-heat exchanger with fluid side communicated with bottom flow from evaporator section and steam side communicated with outlet of heat pump-compressor.

EFFECT: efficient distillation, higher purity of bottom product, power savings.

9 cl, 4 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to improved method of obtaining, at least, one diaryl carbonate of formula (I) and/or alkylaryl carbonate of formula (IV) from, at least, one dialkyl carbonate and, at least, one aromatic hydroxy-compound of formula III , where R, R' and R" independent on each other represent hydrogen atom, linear or branched alkyl with 1-34 carbon atoms, alkoxy with 1-34 carbon atoms, cycloalkyl with 5-34 carbon atoms, alkylaryl with 7-34 carbon atoms, aryl with 6-34 carbon atoms or halogen residue, and R can also stand for - COO-R'" group, in which R'" can stand for hydrogen atom, linear or branched alkyl with 1-34 carbon atoms, alkoxy with 1-34 carbon atoms, cycloalkyl with 5-34 carbon atoms, alkylaryl with 7-34 carbon atoms or aryl with 6-34 carbon atoms, and R1 is linear or branched alkyl with 1-34 carbon atoms, in which (a) dialkyl carbonate or dialkyl carbonates in presence of, at least, one re-esterification catalyst is subjected to interaction with aromatic hydroxy-compound or aromatic hydroxy-compounds in first reaction column, which contains, at least, one strengthening part in head part of column and, at least one reaction zone under strengthening part, which contains, at least, two sections, (b) vapour, released in head part of first reaction column, is fully or partly condensed in, at least, one condenser, (c) cube product of first reaction column is supplied into, at least, one more reaction column, which contains, at least, one strengthening part in head part of column and, at least, one reaction zone under strengthening part, and it is subjected in said column (said columns) to further conversion, (d) non-converted in reaction columns or formed during reaction dialkyl carbonate is completely or partly separated from alkyl alcohol, formed during reaction, at least, at one more stage of method, which includes, at least, one distillation column and (e) separated at stage (d) dialkyl carbonate, in case of necessity, after further purification is re-supplied into first reaction column, where additional reaction column (additional reaction columns) is equipped with one or several condensers, and that condensation heat, formed in condensation in said condensers is directly or indirectly returned to process.

EFFECT: increased method efficiency.

12 cl, 4 dwg, 2 ex

FIELD: process engineering.

SUBSTANCE: set of invention relates to oil-and-gas industry and may be used for separation of hydrocarbons and liquefied gases. In compliance with this method mix of vapors is fed as condensed vapor and swirled inside vertical pipe to create countercurrent motion of swirled phase flows. Note here that condensate flows downward and from said pipe over its inner surface to get enriched with high-boiling component while vapor flows upward to escape from said pipe in axial region to get enriched with low-boiling component. Mix is fed tangentially and upward in pipe bottom while pipe inner surface is cooled to form condensate, a wet reflux, thereon. Pipe inner surface temperature is maintained to make temperature of target product, the vapor, approximate to low-boiling component boiling point. Proposed device comprises vertical cylindrical pipe with top and bottom ends, gas discharge branch pipe at top end, fluid discharge branch pipe at bottom end and means for tangential mix feed inside the pipe. Said cylindrical pipe is fitted in tangential larger-diameter pipe to form annular flow channel confined by top and bottom ends for heat carrier to circulate therein. Means for tangential mix feed inside the pipe are composed of end swirler arranged at pipe bottom end. Fluid discharge means represent clearance between inner cylindrical pipe swirler. Annular flow channel and gas discharge branch pipe accommodate temperature control means, for example, thermometers. Heat carrier flow rate regulator, for example, control valve, is arranged at annular channel.

EFFECT: higher purity of low-boiling component.

3 cl, 2 dwg, 1 ex, 1 tbl

FIELD: process engineering.

SUBSTANCE: invention relates to distributors of mass flows used in hydraulic processing reactors. Proposed device comprises some horizontal self-bearing structures acting as bearing transverse parts and plate-shape panels which, when installed, make a plate tightly fitted in structure joints and between the plate and apparatus inner wall. Self-bearing structure consists of lower panel with some equal holes wherein every hole corresponds to long channel for descending flow shaped to tube or any other geometrical figure with cross-section identical to that of plate hole. Every channel has inlet for straight two-phase flow. Note here that, at least, two channels are provided with common vertical nozzle.

EFFECT: simplified design, optimised sizes, lower costs and higher efficiency.

8 cl, 6 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to nuclear power engineering, particularly, to research and power reactors with liquid-metal lead-bearing heat carrier. Mass exchanger comprises housing with annular cover accommodating top grate arranged above heat carrier level and solid-phase oxidizer arranged above said top grate. Mass exchanger comprises also gas distributor arranged under solid-phase oxidiser, gas consumption booster and gas feed pipeline. One part of said pipeline communicates heat carrier chamber gas cavity while its other part communicated outlet of said booster with feed pipeline communicated with gas distributor. Note here that openings are made between annular cover and top grate, partly located above heat carrier level and partly in gas cavity.

EFFECT: friendly operation, efficient feed of oxygen.

4 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method of producing at least one diaryl carbonate of formula , where R, R' and R" independently denote a hydrogen atom, a straight or branched alkyl with 1-34 carbon atoms, an alkoxy with 1-34 carbon atoms, a cycloalkyl with 5-34 carbon atoms, an alkylaryl with 7-34 carbon atoms, an aryl with 6-34 carbon atoms and a halogen atom, wherein R also denotes a -COO-R"' group in which R'" denotes a hydrogen atom, a straight or branched alkyl with 1-34 carbon atoms, an alkoxy with 1-34 carbon atoms, a cycloalkyl with 5-34 carbon atoms, an alkylaryl with 7-34 carbon atoms and an aryl with 6-34 carbon atoms, and/or an alkylaryl carbonate of formula , where R, R' and R" have values given above, R1 denotes a straight or branched alkyl with 1-34 carbon atoms, from at least one dialkyl carbonate and at least one aromatic hydroxy compound of formula , where R, R' and R" have values given above, wherein (a) dialkyl carbonate, in the presence of at least one reesterification catalyst, reacts with an aromatic hydroxy compound of formula (III), in at least one reesterification column having at least an enrichment part in the top part of the column and at least one reaction zone below the enrichment part, wherein the enrichment part has at least two sections, (b) vapour collected from the top part of the reesterification column is completely or partially condensed in at least one condenser, where at least one enrichment part of the reesterification column is provided with at least one intermediate condenser, wherein heat released during condensation occurring therein is directly or indirectly returned into the process. The invention also relates to a column for carrying out said method, having at least one inlet opening for dialkyl carbonate and at least one inlet opening for the hydroxy compound, at least one outlet opening for the gaseous end product in the top part of the column which is linked to the condenser and at least one outlet opening for the liquid bottom product in the bottom part of the column, at least one enrichment part in the top part of the column and at least one reaction zone below the enrichment part, wherein the enrichment part has at least two sections, wherein at least one enrichment part is provided with at least intermediate condenser.

EFFECT: invention enables use of one or more intermediate condensers to optimise energy integration.

14 cl, 3 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to improved carbonylation methods in order to produce acetic acid, the methods involving: (a) carbonylating methanol or reactive derivatives thereof in the presence of water, a catalyst selected from a group which includes rhodium catalysts, iridium catalysts and mixtures thereof, and methyl iodide as a promoter to form an acetic acid containing reaction mixture in the reactor; (b) separating the stream of the acetic acid containing reaction mixture into a liquid recycled stream and a crude product stream containing acetic acid, methyl iodide, methyl acetate and water; (c) feeding the crude product stream to a stripping column having a distillation zone; (d) purifying the crude product stream in the distillation zone of the stripping column to remove methyl iodide and methyl acetate and obtain a purified product stream, the purified product stream characterised lower concentration of methyl iodide and methyl acetate than the crude product stream, and wherein the step of purifying the crude product stream involves: (i) condensing overhead vapour from the distillation zone of the stripping column, (ii) decanting the condensed vapour to obtain a heavy phase mainly containing methyl iodide and a light phase mainly containing acetic acid and water, and (iii) refluxing at least a portion of the condensed heavy phase to the distillation zone of the stripping column; and (iv) recycling the light phase into the reactor; and (e) drawing a purified product stream from the stripping column.

EFFECT: content of acetic acid in the overhead vapour of the stripping column and content of water in the product stream of the stripping column (side cut) is reduced, which increases efficiency of purification.

17 cl, 3 dwg, 1 tbl

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing a biodegradable intermolecular cyclic diester of alpha-hydroxycarboxylic acid. The method involves feeding a mixture of materials into a purification apparatus fitted with a column with a dividing wall, dividing the mixture of materials and extracting the purified diester. Said purification apparatus has the following components: a fractionating column, an outlet opening, a mass-exchange cap, a column with a dividing wall which is divided into two zones by a vertical dividing wall, an additional mass-exchange cap, an evaporator and an outlet opening on the collector side. The ratio of the length of the column with a dividing wall to the total length of the purification apparatus range from 0.5 to 0.9.

EFFECT: method enables cheap and efficient separation of diester from mixtures of materials when producing diester with high purity of material and/or optical purity.

19 cl, 9 dwg, 9 ex

FIELD: heat supply.

SUBSTANCE: the invention is pertaining to the field of the heat supply industry and is intended for preparation of fuel, in particular, petroleum for use in the boiler rooms being a source of a heat supply of remote settlements. The installation contains: a heater-evaporator, a heat exchanger for heating up a feed stock, the fuel feed stock pump and containers of the feed stock and collection of the light fractions. At that the installation is supplied with the second feed stock pump and three in series connected to each other heat exchangers of the light fractions condensation, the first and second feed stock pumps are connected by their inlets to a feed stock container. The outlet of the first feed stock pump is connected through the feed stock heating up heat exchanger to the heater-evaporator, which by its vapors outlet is connected to the first out of three in series connected to each other heat exchangers, the last of which is connected to its container of the light fractions condensate collection. The outlet of the second feed stock pump is connected in parallel to the heat exchangers of condensation of the light fractions and through them to the heater-evaporator. Each of heat exchangers in parallel connected to each other is supplied with a thermoregulator to keep in it a constant temperature of condensation of the light fractions vapors. The first and second of in series connected heat exchangers are connected through the placed in the feed stock container coiled pipes each to its container of the light fractions collection. The heater- evaporator through the feed stock heating up heat exchanger is connected to the container for fuel collection. In the result the invention allows to upgrade quality of the fuel preparation for the boiler plants at simultaneous production of several light fractions of the feed stock, mainly petroleum. The invention ensures improvement of the quality of the fuel preparation for the boiler plants at simultaneous separate production of several light fractions of a feed stock, mainly petroleum.

EFFECT: the invention ensures improvement of the quality of the fuel preparation for the boiler plants at simultaneous separate production of several light fractions of the feed stock, mainly petroleum.

1 dwg

Beer still // 2255973

FIELD: production of alcoholic drinks.

SUBSTANCE: proposed device contains evaporating tank for heating and evaporation of beer, running water cooler made in form of reservoir with conical bottom and ready product collector. Conical bottom of cooler is made so that vertex of cone is pointed upwards. Conical hole is made in upper part of conical of conical bottom. Elastic conical plug with hermetically fitted in thermometer is installed in conical hole. Ring collecting reservoir is arranged in lower part of cone over its periphery from inner side. Outer side wall of said reservoir is formed by conical surface of cooler bottom, and inner side wall, by branch pipe connected to evaporator reservoir. Bottom of ring collecting reservoir is hermetically welded to branch pipe and to conical bottom, being provided with union communicating with detachable collector of ready product. Hole is made on side surface of conical bottom in its upper part. Inlet end of coil arranged inside cooler is hermetically welded in said hole. Output end of coil is hermetically welded to outer side surface of cooler and is furnished with union communicating with ready product collector installed in holder secured on output end of coil for removal.

EFFECT: improved quality of ready product.

2 cl, 2 dwg

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: invention relates to low-size apparatuses for production of light and heavy petroleum products from petroleum feedstock. Plant comprises heat-insulated evaporation vessel provided with electroheating ring, heat-exchanger coupled with evaporation vessel, petroleum product storage vessel, and valves, said evaporation vessel is provided with secondary heating ring and said heat-exchanger is constituted by two different-volume vessels, which are connected over coils to petroleum product storage vessel also provided with heating ring. Minor heat-exchange vessel communicates with evaporation vessel space through perforated pipe and major one communicates with evaporation vessel and minor heat-exchange vessel through pumps.

EFFECT: simplified structure and increased output of motor distillates.

1 dwg, 1 tbl

FIELD: oil and gas production.

SUBSTANCE: invention relates to regeneration of saturated glycol solution used in the natural gas pre-transportation treatment and may also be employed for separating liquid thermolabile substances, whose destruction products are corrosion-active components. Regeneration is accomplished with the aid of mass-exchange column and evaporator. Glycol solution to be regenerated is first separated into at least two portions, of which one is used in unheated state as reflux for the mass-exchange column top vapors and finally gets into evaporator, whereas the rest of the glycol solution is heated and then fed directly into evaporator. Temperature of the column top vapors is controlled by amount of the cold portion of saturated glycol solution used as reflux.

EFFECT: lowered mass-exchange column corrosion intensity.

2 cl, 2 dwg, 1 tbl

FIELD: production of organic agents and rectification cleaning of such agents.

SUBSTANCE: proposed multi-purpose plant includes still and batch-operated packed rectifying column mounted on it and brought in communication with it; top of said column on side of vapor outlet is communicated with dephlegmator which is brought in communication with top of rectifying column on side of condensate outlet and with rectification production collecting reservoir; proposed plant is provided with two measuring reservoirs connected at their lower parts to starting solvent reservoir located above them and to still; at their upper parts they are connected to vacuum pump and to nitrogen source; measuring reservoirs are located above still for filling it by gravity; volume of measuring reservoirs ranges from 60 to 75% of still volume; dephlegmator is made in form of cylindrical water-cooled heat exchanger mounted at angle of 10 to 20° relative to level; in its lower part, dephlegmator is provided with bypass unit with combined vapor inlet and condensate outlet; bypass unit is used for connecting the dephlegmator to top of rectifying column on side of solvent vapor outlet and to point of introducing the phlegm to rectifying column and to reservoirs collecting predistillate and rectification products; besides that, dephlegmator is connected with separator for separation of water from condensate (Florence flask) which may be disconnected when necessary; water receiver is located below it and is brought into communication with it; stillage residue receiver located above still is connected to its lower part; stillage residue receiver is connected by its lower part to stillage residue utilization reservoirs; at the top it is connected to vacuum pump and to nitrogen source; predistillate and reaction qualification products are accumulated in separate reservoirs connected to column condensate outlet; plant is provided with trap for receiving non-condensed vapor of rectification products which is connected with water receiver, dephlegmator and water cooler; trap is connected to predistillate collecting reservoir; rectifying column consists of four drums of similar height hermetically interconnected together; their diameter ranges from 0.07 to 0.08 of rectifying column height; height of rectifying column ranges from 3800 to 4200 mm; volume of predistillate and stillage residue collecting reservoir is 20-30% of volume of still; volume of starting solvent reservoir is 200-300% of volume of still; rectifying column, starting solvent reservoir and rectification product collecting reservoir are made from stainless steel.

EFFECT: enhanced efficiency; possibility of performing thorough rectification cleaning of agents.

11 cl, 1 dwg, 9 tbl, 9 ex

Up!