Method and apparatus for producing methanol with improved distillation section

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method for synthesis of methanol, wherein raw methanol (101) is obtained in a synthesis section and purified in a distillation section (D) to obtain pure methanol (104), a stream (103) of instantaneously escaping gas and by-products (105, 106). At least a portion of said stream (103) of instantaneously escaping gas is treated to separate from said gas a stream (110) containing methanol, and that methanol-containing stream (110) is returned to the distillation section (D) to increase pure methanol production volume, wherein pressure of at least a portion of the stream (103) of the instantaneously escaping gas is raised before treating the stream (103) of the instantaneously escaping gas to separate the methanol-containing stream. The invention also relates to an apparatus for carrying out said method and a method of renovating said apparatus.

EFFECT: method enables to increase pure methanol production volume, safe power consumption and reduce emission of pollutants.

10 cl, 3 dwg, 2 tbl, 2 ex

 

The technical field to which the invention relates.

The present invention relates to a method and installation for methanol synthesis, in particular, to improvements in the distillation section on installation for the production of methanol.

The level of technology

Methanol is produced by the catalytic reaction of synthesis gas containing hydrogen and carbon monoxide at high temperature and pressure, typically 200-300C and 40-150 bar. The reaction product is a stream of so-called raw (untreated) methanol, which is subjected to distillation process with the aim of obtaining clear, pure methanol and water separation and by-products.

In General, the section of the distillation get purified methanol and separated instantly eye-catching gas, water, fusel oil and (or) other by-products. The crude methanol is usually served in the distillation section of light fractions, for example, in column distillation light ends, for gas separation and light (low-boiling) components, receiving the stabilized crude methanol; then, the stabilized crude methanol is fed to the cleaning section for the production of methanol of high purity.

Figure 3 shows a typical prior art installation, in which the crude methanol 1 refer to the section T distillation light ends, getting stabilized crude methanol 2 and instantly bideleux is the action scene gas 3; then the above methanol 2 serves in section R of cleaning, getting purged methanol 4 and separating fusel oil 5 and cubic water 6. Section distillation light ends and the section cleaning section comprises distillation D.

Instantly eye-catching gas discharge section of the distillation light ends (stream 3), receive low pressure, typically less than 1 bar, and used as fuel gas at the inlet of the plant for producing methanol or in some cases burned at the flare burner. However, the burning instantly eye-catching gas with low pressure requires the use of special burners, designed for low pressure.

Currently, there are ongoing efforts to increase production facilities for the production of methanol, i.e. the number of purified methanol obtained in the cleaning sections, which is a useful product of this process. This applies to new installations and also to reconstruct or to increase the capacity of existing units.

As for increasing the capacity of existing or old installations, for economic reasons it is desirable to abandon the corresponding changes in the input set. In some cases, the input portion of setup is already running at full capacity and further increase its capacity impossible.

Summary of sunstainable

The task underlying the present invention is to find an effective way of increasing amounts of purified methanol produced at the facility of methanol.

The basic idea underlying the invention consists in the extraction of the methanol contained in the stream instantly dissolved gas. Accordingly, the invention proposes a method for the synthesis of methanol, the implementation of which crude methanol receive section of the synthesis and purified in the distillation section, receiving the purified methanol stream instantly dissolved gas and by-products; moreover, this method is characterized in that at least part of the above thread instantly dissolved gas process for allocation of instantly dissolved gas stream containing methanol, and the stream containing methanol, return to re-process in the distillation section with the aim of increasing production of purified methanol.

In accordance with the first feature of the invention, the treated stream instantly dissolved gas is subjected to washing, if possible, the water obtained in the distillation section; in the process of the above-mentioned washing obtain an aqueous solution of methanol and this solution is returned to the distillation section for re-processing.

Instantly eye-catching gas main is entrusted washed in countercurrent and in at least one washing column, getting in Cuba columns (columns) aqueous solution of methanol, and the top of the same column - combustible fuel gas. Above the combustible gas mainly contains CO2N2, CO and CH4and can be used as fuel or sent to the flare burner.

In accordance with another feature of the invention before processing instantly dissolved gas for the extraction of the methanol, that is, separation of the above stream containing methanol, the pressure is instantly released gas increase. Preferably, the pressure is instantly released gas increase in the ejector. Driving the flow in the above-mentioned ejector in various embodiments of the invention is any flow at a higher pressure than the pressure instantly dissolved gas; driving the flow, preferably, is a purge gas or residual gas from a section of the synthesis, or water vapor from low pressure (2-20 bar) or medium pressure (20-60 bar).

The distillation section typically includes the section of the distillation light ends, which serves crude methanol, and the cleaning section, which serves stabilized crude methanol obtained in the distillation section of light fractions; in the above section of the distillation light ends receive the stream instantly dissolved gas. In accordance with the invention, the pot is to instantly dissolved gas or at least part of this flow process, as described above, receiving a stream containing methanol, which is returned for re-processing on the inlet side (upstream in the direction of flow) section of the distillation of light fractions by mixing with the input stream of the crude methanol or by direct submission to the section of the distillation light ends.

For example, in a preferred embodiment of the invention instantly escaping gas taken from the top of the distillation columns of light fractions, washed in a countercurrent washing column type; in the upper part of the wash column receive fuel gas, while in Cuba (lower part) of the same column receive an aqueous solution of methanol and return it for re-processing in the distillation column of light fractions. In accordance with the above features of the invention, the flow pressure is instantly released gas before it enters the wash column can be improved by means of the ejector, and, in addition, between the ejector and the wash column can be installed in the condenser.

Another object of the invention is an installation for the production of methanol, adapted for implementing the said method comprising at least the section of the synthesis, in which the crude methanol, and the section of distillation, in which the above crude methanol is treated to obtain the purified methane is La, receiving the stream instantly dissolved gas and by-products; moreover, this setting differs in that it includes means of recycling, designed to collect at least part of the stream instantly dissolved gas and adapted for separation from the collected flow instantly dissolved gas stream containing methanol, and return that stream containing methanol in a distillation section with the aim of increasing production of purified methanol.

In a preferred embodiment of the invention the above-mentioned tools are used in the form of a wash column, which preferably serves water, and more preferably operate in a countercurrent system.

In addition, to implement the preferred embodiments of the method proposed in the invention, provided the ejector designed to increase the pressure of the stream instantly dissolved gas, for example, when applying instantly dissolved gas in the above leaching column. The driving flow in the above-mentioned ejector may be any suitable stream, for example, the purge gas, the residual gas or water vapor. If you are using water vapor, which on the outlet side of the ejector and on the inlet side of the rinsing of the column preferably includes a capacitor.

Another object of the invention is one which by way of modernization of installations for the production of methanol, including at least a section of the synthesis, in which the crude methanol, and the section of distillation, in which the above crude methanol is treated to obtain a purified methanol, simultaneously receiving stream instantly dissolved gas and by-products; moreover, this method differs in that it provides means adapted to collect at least part of the stream instantly dissolved gas, to separate from the above thread instantly dissolved gas stream containing methanol, and to return the above stream containing methanol in a distillation section, with the aim of increasing production of purified methanol. Depending on needs, there are also relevant (pressure piping).

The main advantage is that the production of purified methanol is increased when the installation is relatively simple and inexpensive equipment without the need to change the so-called input part, namely, sections compress the synthesis gas and sections of synthesis. This is an important advantage, because the change of the input part is usually expensive.

The above advantage is particularly evident in cases of reconstruction of the plant for production of methanol, in which the input part is already working at full capacity and further the increase of power is impossible. For this case, the invention offers a cost-effective and simple way to increase production of purified methanol.

Production of purified methanol is usually increased by 1-2%; however, depending on the circumstances, you can get some advantage. In some cases it is possible to increase production by about 3%. Basically, the invention preferably relates to installations of medium and high power.

Another advantage is the reduction of pollutant emissions and CO2in the environment as methanol contained in instantly eye-catching gas instead of burning flare burner return for re-processing.

If before the separation of the stream containing methanol, flow pressure instantly dissolved gas increases, there is another advantage in that the fuel gas is produced at a higher pressure than the pressure instantly dissolved gas in a known way (less than 1 bar); this means that the special burner designed for low pressure, is not required.

These and other advantages of this invention will be more apparent through the following description of preferred and non-limiting variants of its implementation with reference to the drawings, in which the s:

Brief description of drawings

figure 1 is a simplified view of the circuit implementing the method in accordance with the first embodiment of the invention,

figure 2 presents a second variant embodiment of the invention.

Detailed description of preferred embodiments of the invention

As shown in figure 1, the crude methanol 101 receives in the normal section of methanol synthesis (not shown) and serves in section T distillation light ends, getting stabilized crude methanol 102 and stream 103 instantly dissolved gas. Then the stabilized crude methanol 102 obtained in section T distillation light ends, serves in section R of cleaning, getting purged methanol 104 and separating fusel oil 105 and cubic water 106. Section T distillation light ends and section R cleaning are part of section D of distillation on an installation for the production of methanol.

Stream 103 instantly dissolved gas or at least part of this flow through the ejector E is driven by the driving stream 107, served in the leaching column C. From leaching columns With out a stream containing methanol, in this embodiment, aqueous solution 110 methanol, which returns to the input section T distillation light ends, mixing with the flow of 101 crude methanol. In addition, in the upper part of the column To receive the fuel gas 109.

In particular, rinsing alonna With preferably represents a leaching column (absorber) counterflow type, in which water serves 108 may, the same water 106 (or part of it), which is obtained from the cleaning sections. A solution of 110 receives at the bottom of column C and return to the section T distillation light ends by means of a pump or possibly due to hydrostatic pressure.

Driving (ejecting) stream 107 in the ejector E is any suitable stream, for example, the flux of water vapor from low pressure, for example, 2-20 bar, or medium pressure, for example, 20-60 bar. The advantage of using water vapor is that the compressed stream at the outlet of the ejector E (line 111), and then the fuel gas 109 received in the upper part of the column, not diluted driving the flow.

If the stream 107 is a water vapor low or medium pressure stream 111, coming out of the ejector E, to enter it in the column is preferably fed into the condenser (not shown) for condensing water vapor and separating the absorbed methanol.

Thanks to the return of the methanol contained in the stream 110, production of purified methanol (stream 104) increases by a few percent, typically about 1-2% or even more. For a partition T of the distillation light ends may be a small increase in the load of the boiler.

It should also be noted that due to the increase in pressure when passing through the ejector E topl is wny gas 109 is received with a higher pressure, than the pressure of stream 103. Therefore, for fuel gas 109 does not need a special burner designed for low pressure. You can use a regular burner, simpler construction and less costly compared to the design that is used.

In a simplified embodiment of the invention, represented in figure 2, the stream 103 is sent directly to the wash column, without increasing its pressure. In the present embodiment of the invention the bottom part of the water 106 obtained in section R cleaning, forms a flow 108 water for submission to wash the column With and formed in the column With a stream 110 containing methanol, return to repeat the processing directly in the partition T distillation light ends.

It should be noted that the return flow 110 for re-processing to the input section T distillation light ends (figure 2) or directly in the above section T distillation light ends (figure 3) represent different embodiments of the method proposed in the invention is equally applicable when the pressure is instantly released gas before processing for recovery of methanol in the column With and without increasing the pressure.

Depending on the requirements of section T distillation light ends and partition R filters are used, for example, one Il the several columns of the distillation of light fractions/treatment. It should be noted that the drawings are in simplified form and are not shown auxiliary devices such as valves, etc. that are well known to the person skilled in the technical field.

This invention relates also to method of reconstruction of the known installation for the production of methanol. In the first embodiment, when installing at least wash the column With, ejector E to increase the pressure instantly dissolved gas and pipeline 110 for returning solution from the cube columns With the input section T distillation light ends can change the layout for installing, operating in accordance with figure 3, after receiving a new scheme presented in figure 1. When installing at least a column and tubing 110 to return the solution of methanol from the column With section T distillation light ends can change the layout of the same installation, getting the scheme presented in figure 2.

The following are examples.

Example 1

Below table 1 refers to a known method, shown in figure 3. Table 2 refers to the same method, implemented under the new scheme, shown in figure 1, which instantly escaping gas 103 is compressed in the ejector E, using as the driving flow 107 residual is th gas membrane installation extract the hydrogen, and compressed gas 111 is washed with water in the column, receiving stream 110 containing methanol, which is returned for re-processing, mixing with the input crude methanol 101.

The molar flow rate of 104 purified methanol is 7903,9 in comparison with the molar flow 7809 thread 4 on the known installation when you enter the same amount of crude methanol. Thus, the increase in production is 1.2%.

Example 2

Known installation, shown in figure 3, modified in accordance with the scheme presented in figure 2, which offers a rinsing instantly dissolved gas 103 water 108 received from the cube column purification. Production of purified methanol increases with 7809 to 7895,9 kg/s, 1.1%.

Table 1
Stream123456
Steam fraction (mol)0,000,001,000,000,000,00
Temperature is (C) 49,586,345,045,090,4118,8
Pressure (bar abs)6,211,911,261,521,841,91
Mass flow (kg/h)320504,3309949,810553,2250214,71014,958676,9
The molar flow rate (KMOL/h)11368,311102,0266,27809,035,03256,4
Composition (mol % moist.)
CO--0,020%---
CO21,458%-62,241%---
H20,008%-0,357%---
H2O28,771%29,460%0,021%-41,283%99,975%

Stream123456
CH40,003%-amount of 0.118%---
AG0,001%-0,052%-- -
N20,006%-0,239%---
CH3HE69,676%70,492%35,657%99,999%44,008%0,022%
Acetone0,001%-0,022%---
Dimethyl ether0,013%-0,548%---
Ethanolto 0.032to 0.032%-0,001%9,955%0,003%
1-propanol0,015%0,015%--4,754% -
Methyl
formate
0,017%-0,724%---

Table 2
Stream101102103104105106
Steam fraction (mol)0,000,001,000,000,000,00
Temperature (C)49,586,845,045,091,2118,8
Pressure (bar abs)6,211,911,261,521,841,91
Mass flow (kg/h)32004,3 321621,710617,6253255,4996,967424,0
The molar flow rate (KMOL/h)11368,311679,3267,67903,935,03742,6
Composition (mol % moist.)
CO--0,027%---
CO21,458%-62,008%---
H20,008%-0,358%---
H2About 28,771%32,170%0,023%-44,996%99,999%
CH40,003%-amount of 0.118%---
AG0,001%-0,052%---
N20,006%-0,238%---
CH3HE69,676%67,785%35,632 Yes%99,999%40,093%0,001%
Acetone0,001%-0,029%---
Dimethyl ether 0,013%-0,581%---
Ethanolto 0.032%0,031%-0,001%10,140%-
1-propanol0,015%0,014%--4,771%-
Mailformat0,017%-0,932%---

1. The method of synthesis of methanol, in which the crude methanol (101) are obtained in section synthesis and purified in the distillation section (D), getting purged methanol (104), stream (103) instantly dissolved gas and by-products (105, 106), characterized in that at least part of the specified stream (103) instantly dissolved gas is processed for separation from the gas stream (110)containing methanol, and that containing methanol stream (110) return in section (D) distillation to ensure increased volume of production is cleaned TBA methanol, and before treatment instantly dissolved gas to highlight containing methanol flow increases the pressure in at least part of the stream (103) instantly dissolved gas.

2. The method according to claim 1, in which at least part instantly dissolved gas (103) is treated by washing, getting an aqueous solution (110) of methanol, and the solution returns to repeat the processing in the distillation section.

3. The method according to claim 2, in which the flushing flow (103) instantly dissolved gas carry water (108)separated from the crude methanol (101) section (D) distillation.

4. The method according to claim 2 or 3, wherein the flushing flow (103) instantly dissolved gas is carried out in countercurrent and in at least one washing column (C), while in the lower part of the column (columns) get the specified solution (110) of methanol, and in the upper part - combustible fuel gas (109).

5. The method according to claim 1, in which the pressure is instantly released gas (103) increase in the ejector (E).

6. The method according to claim 5, in which the entraining stream (107) in the ejector (E) represents the water vapor low or medium pressure, and coming out of the jet stream (111) is subjected to condensation to processing for allocating the specified containing methanol stream.

7. The method according to one of claims 1 to 3, wherein said stream (103) instantly released gas is obtained in section (T) distillation is agcih fractions, which serves crude methanol (101), receiving the specified stream instantly dissolved gas and stabilized crude methanol (102), sent for further purification, and obtained containing methanol stream (110) is mixed with the crude methanol (101), the incoming section of the distillation light ends, or return for re-processing directly in the section of the distillation light ends.

8. Installation for synthesis of methanol, suitable for implementing the method according to any one of claims 1 to 7, the installation including at least a section of the synthesis, in which synthesis gas is converted into crude methanol (101), and section (D) distillation, in which the crude methanol (101) cleanse, getting purged methanol (104), and stream (103) instantly dissolved gas and by-products, characterized in that it includes means (C, E) recycling mounted with the possibility of collecting at least part of the stream (103) instantly dissolved gas and ensure the allocation of the collected stream instantly dissolved gas stream (110)containing methanol, and return that contains methanol flow in section (D) distillation and contains the ejector (E)increasing the pressure of the collected stream (103) instantly dissolved gas and installed in the direction of flow in front of the wash column.

9. Installation according to claim 8, in which section (D) distillation includes a section (T) from once light fractions, which serves crude methanol (101), and section (R) treatment, and those means of recycling include leaching column (C) With water in a countercurrent, which takes a stream (103) instantly dissolved gas, assembled from sections (T) distillation light ends, and a line for returning water solution of methanol (110) from the wash column in the distillation section of the light fractions.

10. The method of reconstruction of the plant for the synthesis of methanol, comprising at least a section of the synthesis, in which the crude methanol (101), and section (D) distillation, in which the crude methanol is treated to obtain a purified methanol (104), receiving the stream (103) instantly dissolved gas and by-products, characterized in that it provides the means (C, E) and recirculated air line adapted to collect at least part of the stream (103) instantly dissolved gas for discharge from this part of the stream (110)containing methanol, and return that contains methanol stream (110) in section (D) distillation.



 

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4 cl, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing rectified ethyl alcohol and apparatus for realising said method. The method involves distillation of alcohol and attendant impurities in a mash column, purification of alcohol from head impurities in an epuration column, concentration of alcohol and purification thereof from intermediate impurities and residues of heat impurities in an alcohol column, and separation of impurities in a column for concentration of head and intermediate impurities. The wash distillate is fortified in the concentration part of the mash column; extraction of impurities in the epuration column is carried out with intense feeding of hot water for hydro-selection into the top tray and the middle part of the epuration column; purification of alcohol from methanol is carried out in a methanol column; lutter water from the alcohol column is fed into the top tray and the middle part of the column for concentration of head and intermediate impurities; lutter from the column for concentration of head and intermediate impurities is fed into the top tray and the middle part of the epuration column.

EFFECT: invention enables to obtain ethyl alcohol of high quality with minimum loss thereof with by-products.

2 cl, 1 tbl, 1 dwg

FIELD: explosives.

SUBSTANCE: method to produce isopropanol is carried out in process of at least two reaction stages of hydrogenation, at the same time each reaction stage includes a reaction zone of hydrogenation, where the hydrogenation product released from the reaction zone of the first reaction stage contains a non-reacted acetone, and a flow of products containing acetone and isopropanol is supplied into the reaction zone of the next reaction stage, at the same time the specified flow of products at the inlet to the reaction zone of the specified next stage has temperature from 60 to 100C. At the same time the temperature of the flow of products released from the reaction zone of the specified next reaction stage, at the outlet of the specified reaction zone is at least by 40C higher than the temperature of the flow of products arriving into the specified reaction zone at the inlet to the specified reaction zone, and the temperature in the specified next reaction zone does not exceed 125C.

EFFECT: method makes it possible to produce isopropanol of high degree of purity.

23 cl, 2 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of separating a solution of homogeneous catalyst from unrefined monoethylene glycol (MEG) and purifying MEG, for use in catalytic conversion of ethylene oxide (EO) to MEG, where the method involves the following steps: separating the catalyst solution in a catalyst separation section by evaporating unrefined MEG and feeding the unrefined MEG into a rectification section, a section for separating light fractions and from there into a pasteurisation section, where each section works at pressure lower than atmospheric pressure of 0.5105 Nm-2 or lower, where the rectification and pasteurisation sections are at pressure lower than that of the catalyst separation section, where the method provides pressure difference between the catalyst separation section and the rectification section, and where the vapour phase of the unrefined MEG from the catalyst separation section is fed essentially as vapour-phase feed into the rectification section. The invention also relates to apparatus where said method can be realised, as well as use of said method and apparatus in a process or block for catalytic conversion of EO into MEG.

EFFECT: invention enables to reduce the process to a one-run process of evaporating a stream of monoethylene glycol, which enables to transport vapour from the catalyst separation section into the monoethylene glycol purification step without using a mechanical pump.

12 cl, 3 dwg

FIELD: industrial organic synthesis.

SUBSTANCE: invention provides a method for purifying 1,3-propanediol comprising: (a) optional removal of water from raw mix containing 1,3-propanediol; (b) distillation of raw mix containing 1,3-propanediol in distillation column under conditions favoring maximum separation of mix components, which are heavier than 1,3-propanediol, from 1,3-propanediol and components, which are lighter than 1,3-propanediol; (c) withdrawal of stream containing at least major part of 1,3-propanediol and at least some components, which are lighter than 1,3-propanediol; (d) separation of stream from step (c) from components, which are heavier than 1,3-propanediol; and (e) distillation of stream from step (c) in distillation column to separate 1,3-propanediol from components of stream, which are lighter than 1,3-propanediol, and any residual components heavier than 1,3-propanediol.

EFFECT: enhanced purification efficiency.

10 cl, 3 dwg, 2 ex

FIELD: rectification of organic compounds.

SUBSTANCE: all-purpose installation enables purification of high-boiling vacuum rectification solvents, in particular ethylene glycol, monoethanolamine, methyl cellosolve, ethyl cellosolve, butyl cellosolve, N-methylpyrrolidone, and benzyl alcohol.

EFFECT: enhanced purification efficiency.

8 cl, 1 dwg, 7 tbl, 7 ex

FIELD: petrochemical industry; methods of production of ethylene chlorohydrin.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of the vacuum rectifying separation of ethylene chlorohydrin (EChH) both from the mixtures with the high-boiling hydrins and at the regeneration of EChH in the process of the synthesis of the different compounds on its base. The method provides for the vacuum rectification of EChH with the continuous feeding of ethylene oxide into the distillation residue section of the column of separation up to its content in the distillation residue liquid within the interval of 0.01-0.15 mass % at the temperatures exceeding 90°C. As a rule the ethylene oxide is introduced in the form of the solution in the material flow of the phase of the rectification. The method ensures reduction of the corrosion activity of the medium, the increased reliability and the service life of the equipment, stabilization of the commercial EChH quality and the raised efficiency.

EFFECT: the invention ensures reduction of the corrosion activity of the medium, the increased reliability and the service life of the equipment, stabilization of the commercial EChH quality and the raised efficiency.

2 cl, 1 tbl, 9 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to improved process for production of 2-ethylhexanal, which is raw material for production 2-ethylhexanoic acid and/or 2-ethylhexanol. Starting material of invention is bottom residue from rectification of butyl alcohols produced in oxo synthesis, from which bottom residue a fraction mainly containing saturated and unsaturated C8-alcohols with 5-15% of C12-acetals is isolated on two columns operated at column top residual pressure 50-90 mm Hg. This fraction is subjected to vapor-phase processing at atmospheric pressure on copper-containing catalyst at 200-300°C followed by rectification of catalysate on two columns to isolate, as first-column top distillate, fraction obtained at 20-50 mm Hg and containing light components and 2-ethylhexanal, which fraction is fed into second column operated at column top residual pressure 60-100 mm Hg to isolate distilled fraction containing light components and 30-60% of 2-ethylhexanal, whereas desired 2-ethylhexanal is recovered as bottom product or as product tapped from the side of bottom column section.

EFFECT: improved quality and yield of desired product.

2 cl, 14 ex

FIELD: alcohol production.

SUBSTANCE: method comprises direct distillation of concentrate of top ethyl alcohol impurities or rectification of intermediate ethyl alcohol fraction in presence of an alkali agent selected from sodium and potassium oxide, carbonate, and bicarbonate hydrates, and aqueous ammonia in case of top ethyl alcohol impurities processing and selected from sodium and potassium oxide, carbonate, and bicarbonate hydrates, calcium oxide, and aqueous ammonia in case of intermediate ethyl alcohol fraction rectification at alkali agent concentration 0.01 to 3.0 wt % and vat temperature 80-86°C. Desired processing product is commonly used as a binary mixture component and vat residue obtained in distillation and rectification operation is commonly used as additional component of fuel oil.

EFFECT: achieved wasteless processing of alcohol production wastes and utilization of all processing products.

6 cl

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

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