Method of continuous production of alkylamino(meth)acrylamides

FIELD: chemistry.

SUBSTANCE: invention relates to a method of continuous production of alkylamino(meth)acrylamide of formula (C) by reacting a formula (B) compound with a formula (A) compound in the presence of a re-esterification catalyst in the presence of at least one polymerisation inhibitor in a continuous re-esterification installation. Reacting substances are continuously fed into the corresponding reactor (1) and the alcohol formed from the reaction is continuously removed in form of an azeotropic mixture of methanol and methyl(meth)acrylate (13) (mixture of ethanol and ethylacrylate 13, respectively) using a distillation column (2). The reaction mixture is constantly fed from the reactor into the distillation column (3) or, respectively, into evaporator (5). Highly volatile components (A, B, methanol or, respectively, ethanol) and a very small part of amide end product (C) are tapped from the head of the column and returned to the reactor. Amide end products (C) together with catalyst and polymerisation inhibitor, as well as heavy by-products are tapped from the bottom of the column. Material flow (15) from the bottom of the distillation column (3) is continuously taken for distillation to obtain pure end product.

EFFECT: improved quality of product, high efficiency and output.

15 cl, 1 tbl, 1 ex, 1 dwg

 

The scope of the invention

The invention relates to another method of continuous receipt of alkylamino(meth)acrylamido (C) as a result of continuous aminolysis, for example, aminolysis methyl(meth)acrylate (A), amines (B) allocation of methanol (G) in accordance with the equation:

where

R1means a hydrogen atom or methyl group,

R2means linear, branched or cyclic alkyl residue, aryl residue, which can be from one to several times substituted alkyl groups, and this linear, cyclic or branched alkyl residue may have a length from two to twelve carbon atoms, for example, ethyl, sawn, ISO-propyl, bucilina, isobutylene, tert-bucilina, pentilla, hexeline, heptylene, anjilina, isooctyl, Danilina, decile, angellina group that may be unsubstituted or one to several times substituted groups

-NR3R4or

-OR5,

or R3or R4can mean a hydrogen atom and, in addition,

R3, R4or R5may be the same or different and represent an alkyl group with the number of carbon atoms ranging from one to twelve, for example, metal, ethyl, sawn, ISO-propyl, and b is a stylish, isobutylene, tert-boutelou, pentelow, hexeline, heptylene, octillo, isooctanol, nonalloy, decile, undecyloxy group or a hydrogen atom,

R2may in addition to mean a group

[(R6-O)n]-R7and

R6can mean an unbranched or branched alkyl group with the number of carbon atoms of from one to six, for example, metal, ethyl, sawn, ISO-propyl, boutelou, isobutylene or tert-boutelou group,

n takes values from 1 to 4

R7could mean a metal group or ethyl group.

In the role of amines can be considered the following compounds: diethylaminoethylamine, diethylaminoethylamine, dipropylenetriamine, diisopropylaminoethanol, dibutylaminoethanol, diisobutylamine, dimethylaminopropylamine, diethylaminopropylamine, dipropylenetriamine, diisopropylaminoethanol, dibutylaminoethanol, diisobutylamine, diethylaminoethylamine, diethylaminoethylamine, dipropylenetriamine, diisopropylaminoethanol, dibutylaminoethanol, diisobutylaluminum, methylamine, cyclohexylamin.

Particular preference is given to dimethylaminopropylamine and along with it diethylaminoethylamine, diethylaminoethylamine, diethylaminoethylamine and diethylaminoethylamine.

The level of technology

The literature describes numerous ways interesterification are intermittent (periodic)process, in combination with various catalysts.

The search for more efficient methods led to the development of ways of interesterification on the continuous scheme, under which continuously served the original connection and continuously discharge the reaction products. Compared with periodic ways ways interesterification on the continuous scheme are listed further advantages: the process easier to automate and its implementation you can do with fewer people, better playing quality products and deviations in quality not so great, improves the performance of the installation due to the absence of the sequence of individual operations (loading, carrying out the reaction, the separation of low-boiling products, the separation of the target product, unloading). This process has better performance in time and volume, than the process for a periodic scheme.

Methods continuous interesterification known.

In European patent No. 0960877 (EIf Atochem S.A.) describes a continuous method of obtaining methacrylate esters dialkylamino alcohols. Spend interaction dialkylamino alcohols in General SL is tea with methyl(meth)acrylate and get dialkylaminoalkyl(meth)acrylates are presented below.

A mixture of original substances (methyl(meth)acrylate and dialkylaminoalkyl alcohol) is continuously fed into the reactor with a stirrer together with tetraalkylammonium as a catalyst for interesterification (for example, this tetrabutyl-, tetraethyl -, or Tetra-(2-ethylhexyl)titanate) and with at least one polymerization inhibitor (e.g. phenothiazines, tert-butyl pyrocatechin, onomatology ether of hydroquinone or hydroquinone), which can be used in quantities of from 100 to 5000 hours/million calculated for the reaction mixture while at a temperature of from 90 to 120C has place the formation of dialkylamino(meth)acrylate with a simultaneous selection of the azeotropic mixture of methyl(meth)acrylate and methanol. The crude reaction mixture (crude ether) are sent to the first distillation column, and from the head of the distillation column at reduced pressure divert practically free from catalyst material flow and from a bottom part of the distillation column divert the catalyst with a small amount of dialkylaminoalkyl(meth)acrylate. Material flow, taken from the head of the first distillation column, send then to the second distillation column, from the head part which under reduced pressure selected stream of low-boiling products with a small amount of dialkylaminoalkyl(meth)acrylate, and from the bottom part of the selected flux is, consisting mainly of dialkylaminoalkyl(meth)acrylate and inhibitor (inhibitors) polymerization sent to the third distillation column. In the third distillation column carry out the distillation under reduced pressure, resulting from the head of column select clean target dialkylaminoalkyl ester of (meth)acrylic acid, and from a bottom part are selected mainly inhibitor of polymerization or polymerization inhibitors. The material flow from a bottom part of the first distillation column after additional purification using a film evaporator is returned to the reactor as the product of the head part of the second distillation column.

In this way refuse dehydration of alcohols before using them, which can lead to increased inactivation used tetraallylsilane due to hydrolysis up to the formation of undesirable precipitation of solids. In addition, the disadvantage of this method is that in the bottom part of the first distillation column, the catalyst is subjected to relatively high temperatures. This can easily lead to decomposition of the catalyst. In accordance with this method, as unreacted starting materials and the reaction product is in General twice undergo rectification with selection through goals the second part of the columns. This entails very high energy costs and demands in the sum of four distillation columns, which in some cases must be very large. In accordance with the above, this process requires very high investment and operating costs.

In European patent No. 0968995 (Mitsubishi Gas Chemical List.) the described method of continuous receipt alilovic esters of (meth)acrylic acid using the reaction column. This interesterification reaction takes place directly in the distillation column (i.e. the reactor and distillation column for distillation azeotrope consisting of methyl(meth)acrylate and methanol, to form one unit, which continuously served the original substance (methyl(meth)acrylate and alcohol). The desired catalyst is in the distillation column, and in this case, preference is given to the compound of titanium. If we are talking about a homogeneous catalyst, it is continuously metered into the distillation column. However, the use of homogeneous catalysts in the distillation column leads to increased consumption of catalysts due to the effect of flushing in the distillation column liquid phlegm and dirt and dust embedded in the column elements formed precipitate solids-based catalyst. If we are talking about heterogeneous catalyst, what about it is in the reaction column. Needless to say that the placement of the catalyst in the distillation column marked disadvantage consisting in that the distillation column in this case is lost pressure and in addition to regular cleaning of distillation columns have to exert great efforts. In addition, heterogeneous catalysts can inaktivirovanie, for example, as a result of undesirable polymerization.

In the Federal Republic of Germany patent No. 4027843 (Rhm GmbH) describes the way the continuous obtaining N-substituted amides of (meth)acrylic acid in the interesterification alilovic esters of (meth)acrylic acid with aliphatic and aromatic amines. The reaction temperature lies at >150C, the pressure is about 160 bar. Work carried out without a catalyst.

Statement of the problem

The present invention is to develop a continuous method of aminolysis methyl ether (meth)acrylic acid amines with boiling points in excess of the boiling point of methanol, which is devoid of the disadvantages of both of the above methods. The concept of esters of (meth)acrylic acid or alkyl(meth)acrylate refers hereinafter to such esters and derivatives of acrylic acid and methacrylic acid, such as methyl ester of methacrylic acid or ethyl ester of methacrylic acid. In addition, the new method should provide is to obtain a product superior in quality to the quality of the products received to date on sale. If it's about superior quality, this refers to a lower content of substances that form a mesh structure, and to a lower content of products attach amine to the double bond of the source of ester or on the double bond of the ester product. The quality of the product, forming a net structure can be formed alkylmethacrylamide. In addition, the new method should provide amino(meth)acrylates with a lower cost and with less energy consumption (i.e. lower cost). Should be reduced, the number of jobs required for maintenance of the installation.

This problem and others are not listed in detail the problems and easily recoverable from the preceding description of the prior art, are solved by a method with the features of claim 1 of the claims. Preferred options for implementing the invention method is protected in the paragraphs that refer to claim 1 of the claims.

Description of the method

The method represented by the diagram in the drawing.

Explanation of symbols on the drawing:

1. The reaction apparatus

2. Distillation column for azeotrope

3. Distillation column for low-boiling products

<> 5. Film evaporator

11. Supply line methyl(meth)acrylate and catalyst

12. Supply line Amin

13. The azeotrope of methanol and methyl(meth)acrylate

14. Line of recycling low-boiling products

15. The crude product

The original product methyl(meth)acrylate (MMA, 11) continuously served in the appropriate reaction apparatus (1), and can be used as one capacitive reactor, and the cascade of series-connected capacitive reactors. It is advisable that all capacitive reactors were connected to the distillation column for azeotrope (2) Abhazia line to exhaust emitted in the reaction of methanol.

Amin (12) is continuously fed to the column for distillation of the azeotrope to remove water.

Used as catalyst tetraalkoxysilane (in the preferred case, the content of tetraalkoxysilane about using methyl(meth)acrylate is from 0.2 to 4 wt.%) as well as the inhibitor (inhibitors) polymerization in the preferred case of continuously metered into the reaction apparatus (1).

However, as catalysts for the transesterification can be used all known from the prior art catalysts for the transesterification. So, for example, as catalysts can be used acetylacetonate zirconium and other 1,3-diketonates is irginia, can also be used a mixture of tiantou alkali metal or thiocyanato alkali metals and halides of alkaline metals, in addition to them, also zinc compounds, for example, dioctylsebacate, oxides of alkaline earth metals or hydroxides of alkaline earth metals, e.g. calcium oxide, calcium hydroxide, magnesium oxide, magnesium hydroxide, or mixtures of the above compounds, in addition to them, also hydroxides of alkali metals, alkoxides of alkali metals, and lithium chloride and lithium hydroxide may also be used mixtures of the above compounds to the above compounds of alkaline earth metals and salts of lithium, dialkylamide, for example, dioctylmaleate, carbonates of alkali metals, carbonates of alkali metals together with such Quaternary ammonium salts, such as tetrabutylammonium hydroxide or bromide of hexadecyltrimethylammonium but they also mixed catalysts of diagonalised and organolanthanide, sour ionoobmennye resin, phosphomolybdenum heteroalicyclic, such alcoholate of titanium, such as, for example, isopropylidene compounds, chelate compounds of the metals titanium, zirconium, iron or zinc with 1,3-dicarbonyl compounds, such compounds of lead, such as lead oxides, hydroxides lead alkoxides of lead, carbonate of lead, or the Oli lead with carboxylic acids. Particular preference is given to mixtures of catalysts consisting of dialkylated and alkylsilane, for example, from dioctyloxy and isopropylacetate in the ratio of 1:1 (wt.% to wt.%). A mixture of catalysts are used in quantities of from 0.1 to 10 wt.% based on Amin used.

As polymerization inhibitors can be used, for example, hydroquinone, 4-hydroxy-2,2,6,6-tetramethylpiperidinyloxy or bis(2-methoxycarbonylethyl)sulfide. We can talk about monopetalum ether of hydroquinone in combination with oxygen.

Used amine may contain water. The amount of water used in Amina is in the range from 50 to 500 ppm (0.05 to 0.005 wt.%). In the preferred case, Amin before entering into the reaction apparatus is released from water distillation through the column for azeotrope (2). This is contained in Amina water goes through the head of the column. To avoid contamination of the used amine azeotropic mixture of methanol and methyl methacrylate (13) filing amine is preferably carried out in the lower part of the distillation column (2). Used amine may be dehydrated and in other ways:

- due to the connected input distillation column for dehydration,

or

due to the processing dehydrating agent such as molecular sieves,

or

- due to the use of membrane technologies, such as evaporation through a semipermeable membrane.

The importance of dehydration is that contained in Amina water can lead to irreversible decomposition of the catalyst (for example, tetraallylsilane) in the reactor. Contained in Amina water leads to the formation of by-products and, therefore, its presence should be completely excluded. Due to this operation to prevent dehydration hydrolysis catalyst and associated costs for increasing the amount used of the catalyst and on the problem of precipitation of solids. It also improves the purity of the product by reducing the proportion of by-products.

The interaction proceeds in the reaction apparatus (1) at temperatures in the range from 80 to 160C. Preference is given to temperatures of from 110 to 135C. To increase the rate of reaction released in the reaction, the methanol is distilled off from the reaction mixture in the distillation column (2) in the form of an azeotrope with methyl(meth)acrylate (13). The reaction mixture, consisting mainly of the target product of alkyl(meth)acrylamide, unreacted methyl(meth)acrylate and amine, as well as small amounts of methanol, catalyst, polymerization inhibitors, and very minor amounts of by-products, after a residence time in the reactor example is about 0.5 to 3 hours (in the preferred case, the residence time ranges from 0.75 to 1.5 hours) served in a film evaporator continuous action (5). Formed in the evaporator falling film (5) pairs served in the distillation column for low-boiling products (3). It under reduced pressure, in the preferred case in the range from 10 to 500 mbar, separates the components which boil at a lower temperature than the ester product in the first place is methanol, methyl(meth)acrylate and neprevyshenie the starting amine. They are selected at the head of the distillation column and sent back (14) in the reactor or in the azeotrope column (2).

Due to this recycling is guaranteed in the overall process almost complete conversion of methyl(meth)acrylate and amine source.

In the preferred case obtained at the outlet of the evaporator with a falling film (5) of the crude amide (15), contaminated by the catalyst, polymerization inhibitor and high-boiling by-products, contains more than 93 wt.% the target ester product; for further processing it is sent to the next stage vacuum distillation, which in the preferred case, is under pressure from 20 to 200 mbar. At this stage distillative Department amine product of high purity in the form of the head of the faction.

Formed in the process by-products are components with boiling points in excess of the boiling point of methyl(meth)is crylate and the original amine, and accordingly they fall in the form of impurities in the target ester product, significantly reducing its quality. This problem can be solved due to the fact that for the Department amine product from the catalyst and the polymerization inhibitors, as well as from high-boiling side connections use the apparatus by evaporation of the film (5), which spares the processed products. Suitable apparatus for this case are evaporators, falling-film, thin-film evaporators and installation for molecular acceleration.

Getting alkylamino(meth)acrylamido may in appropriate cases be completed in distillative obtain pure product, which can also operate at reduced pressure, for example when 500-50 mbar.

Corresponding to the invention of the method in more detail further illustrated by the following examples, which may not be used to limit the scope of the claims.

Example: aminals of amino esters by continuous scheme

To obtain the N-dimethylaminopropionitrile (aminoethyl) described the continuous scheme in the first reaction tank through a distillation column to azeotrope serves 235 kg/h initial mixture of methyl methacrylate and catalyst content of 3.8 wt.% isopropylacetate and 3.0 wt.% dioctyloxy and 244 kg/h N-dimethy is aminopropylene (DMAPA). In addition, in the first reaction apparatus through the column azeotrope is continuously flows return flow from the head of the distillation column for low-boiling component (195 kg/h composition: 78,9 wt.% of methyl methacrylate, 2,12 wt.% methanol, 10.1 wt.% dimethylaminopropylamine and 8,88 wt.% by-products). The molar ratio of MMA:DMAPA in entering the reactor, the flow rate of 1.23:1. In addition, in the first reaction apparatus of the cube column azeotrope comes freed from methanol in the column azeotrope Abhazia pair of devices with a stirrer. Under these conditions, the reaction in the first reaction apparatus is set to the reaction temperature, equal to 107C. From the column to azeotrope selected 117 kg/h of distillate containing 56,54 wt.% methanol, 39,12 wt.% of methyl methacrylate, was 4.02 wt.% isopropanol and 0.5 wt.% products.

The material flow from the first reaction apparatus enters the second reaction apparatus, and the material flow of the second reaction apparatus enters the third reaction apparatus. When the residence time in the first reaction unit, equal to approximately 15 minutes, in the second reaction apparatus, approximately 30 minutes, and in the third reaction apparatus, is equal to about 60 minutes, the reactor are compounds, which are presented below.

T-RA (C)MMA wt.%DMAPA wt.%Aminoether wt.%Methanol wt.%Side wt.%
The first reactor10762,710,2322,070,62of 4.38
The second reactor11155,610,1527,690,595,97
The third reactor13046,84,8641,291,24of 5.81

The pair emerging from individual reaction apparatus, continuously fed to the azeotrope column.

Material flow emerging from the third reaction apparatus, continuously enters the thin-film evaporator of the column for low-boiling component, the output of which neprevyshenie dimethylaminopropylamine, methyl methacrylate and methanol are taken in the form of di is tillate (195 kg/h) and again fed to the first reaction Alpert. Material flow Cuba thin-film evaporator of the column for low-boiling component is 426 kg/h and has the composition: 93% of the target product, representing aminoether, 0.5% dimethylaminopropylamine, 0.2% methyl methacrylate, 2.15 wt.% adduct of methyl methacrylate and amine and 4.25 wt.% other by-products.

1. Method for continuous receipt of alkylamino(meth)acrylamide of formula (In)
,
where R1means a hydrogen atom or methyl, and
R2means linear, branched or cyclic alkyl residue, aryl residue with the number of carbon atoms from two to twelve, or group [(R6-O)n]-R7and
R6denotes unbranched or branched alkyl group with the number of carbon atoms of from one to six,
n takes values from 1 to 4
R7means methyl or ethyl,
by reacting the compounds of formula (B)
,
where R2has the above significance, with a compound of formula (A)
,
where R1means a hydrogen atom or methyl, and R3may means methyl or ethyl, in the presence of an interesterification catalyst and in the presence of at least one inhibitor of polymerization in the continuous conduction interesterification, characterized in that the Rea is yousie substances continuously served in the appropriate reaction apparatus (1) and released during the reaction the alcohol is continuously disperses in the form of azeotropic mixture of methanol and methyl(meth)acrylate (13) (respectively, a mixture of ethanol and ethyl acrylate 13) using a distillation column (2), the reaction mixture is continuously supplied from the reaction apparatus in the distillation column (3) or, respectively, in the evaporator (5), and the distillation under reduced pressure from the head of the column selected volatile components (a, B, methanol or ethanol) and a very small part of the amide of the desired product () and return them to the reaction system, and the cube of the column select amide target products (C) together with the catalyst and the polymerization inhibitors, and high-boiling by-products, and material flow (15) of the cube distillation column (3) is continuously fed to the distillation to obtain pure desired product.

2. The method according to claim 1, characterized in that the vapour phase of the evaporator (5) continuously served in another distillation column in the distillation under reduced pressure from the head part divert amide target product (In) high purity, from the cube and assign the catalyst and the polymerization inhibitors, and high-boiling by-products with a small amount of amide product ().

3. The method according to claim 1, wherein the amine (B) is served in the reaction apparatus through the distillation column (2) with a view to its dehydration.

4. The method according to claim 1, otlichayushiesya, that the molar ratio of methyl(meth)acrylate or ethyl(meth)acrylate to amine in the feed, the reactor mixture is (A):(B) from 1 to 2, in the preferred case from 1.05 to 1.15.

5. The method according to claim 1, characterized in that as a catalyst for interesterification use tetraallylsilane.

6. The method according to claim 1, characterized in that the catalyst is used in quantities of from 0.1 to 10 wt.% based on used methyl(meth)acrylate or ethyl(meth)acrylate.

7. The method according to claim 6, characterized in that the catalyst is used in quantities of from 0.2 to 7 wt.% based on used methyl(meth)acrylate or ethyl(meth)acrylate.

8. The method according to claim 1, characterized in that as the catalyst a mixture of dioctylsulfosuccinate and isopropylacetate in the ratio of 1:1 (wt.%).

9. The method according to claim 8, characterized in that this mixture is used in an amount of from 0.1 to 10 wt.% based on used methyl(meth)acrylate or ethyl(meth)acrylate.

10. The method according to claim 1, characterized in that as the polymerization inhibitor used phenothiazines, tert-butylpyrocatechol, onomatology ether of hydroquinone, hydroquinone or mixture thereof, and the amount of inhibitor is from 100 to 5000 million-1based on the reaction mixture.

11. The method according to claim 1, characterized in that as inhibito is and polymerization optionally use more oxygen.

12. The method according to claim 1, characterized in that as an amine (B) is preferably used dimethylaminopropylamine.

13. The method according to claim 1, characterized in that the pressure in the first distillation column (3) is in the range from 20 to 500 mbar.

14. The method according to claim 1, characterized in that the residence time in the reaction apparatus is from 0.5 to 1.5 hours

15. The method according to claim 1, characterized in that the evaporator (5) is a film evaporator.



 

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13 cl, 2 tbl, 43 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing amido acid ester that is useful as an intermediate substance in synthesis of agrochemical preparation. Invention relates to amido acid ester represented by compound of the general formula (7): wherein A represents substituted or free lower alkylene group, and so on; R1 represents substituted or free lower alkyl group, and so on; R3 represents hydrogen atom or lower alkyl group. Method for preparing amido acid ester involves interaction of amino acid represented by compound of the general formula (1): in presence of water with halogenated carboxylic acid ester represented by compound of the general formula (2): wherein X represents halogen atom with formation of amide represented by compound of the formula (3): Then amide compound interacts with halogenated carboxylic acid ester represented by compound of the general formula (4): wherein R2 represents substituted or free lower alkyl group, and so on; X represents halogen atom with preparing carboxylic acid mixed anhydride represented by compound of the general formula (5): Then carboxylic acid mixed anhydride interacts with amine compound represented by compound of the general formula (6): A, R1 and R3 have the same values as given above; Het represents substituted of free heterocyclic group. Invention provides reducing economic indices of the process.

EFFECT: improved preparing method.

9 cl, 2 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention provides improved 2,7-bis[2-(diethylamino)ethoxy]fluorenone dihydrochloride production process comprising stages of sulfurization of fluorenone followed by neutralization of obtained reaction mass, isolation of purified fluorenone-2,7-disulfonic acid disodium salt, "alkaline melting" of this salt in presence of sodium nitrate to form 4.4'-dihydroxydiphenyldicarboxylic acid, cyclization to form 2,7-dihydroxyfluorene and alkylation thereof. More specifically, 2,7-dihydroxyfluorene obtained in cyclization stage is converted into alkali metal salt and toluene solution of 2-diethylaminoethyl chloride is added to preheated aqueous solution of the above salt at molar ratio 1:(3-5), preferably 1:4, to form 2,7-bis[2-(diethylamino)ethoxy]fluorenone, which is then treated with concentrated aqueous hydrochloric acid at molar ratio 1:(3.5-4), preferably 1:3.5.

EFFECT: increased yield and improved quality of product, and simplified process.

3 cl, 3 dwg, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of 3,4'-diamino-4-R-benzophenones of the general formula: wherein R means Cl, Br, F, -CH3, -OCH3,

that are used as intermediate product in synthesis of azo dyes useful for staining protein fibers and possessing the unique indices of thermal stability. Method involves steps for nitration reaction of substituted benzophenones with potassium nitrate in concentrated H2SO4, nucleophilic replacing halogen (wherein R means Cl) in interaction with O- and N-nucleophilic compounds in dimethylsulfoxide (DMSO) medium in the presence of K2CO3 and reduction of 3,4'-dinitro-4-R-benzophenones. The nitration reaction of synthesized benzophenones is carried out at temperature 20oC for 5 h in the mole ratio 4'-nitro-4-R-benzophenone : KNO3 = 1.0:1.15. Nucleophilic replacing halogen is carried out at temperature 40-60oC for 1-5 h in the mole ratio substrate : nucleophilic compound = 1.0:1.05, and reduction of dinitrobenzophenones is carried out with SnCl2 x 2H2O in 18% HCl medium, in the mole ratio 3,4'-dinitro-4-R-benzophenone : SnCl2 x 2H2O = 1:6, at temperature 20oC for 0.15 h. Invention provides decreasing cost of synthesis, reducing time and temperature in carrying out the process, enhancing purity and yield of end products.

EFFECT: improved method of synthesis.

4 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of continuous production of alkylamino(meth)acrylamide of formula (C) by reacting a formula (B) compound with a formula (A) compound in the presence of a re-esterification catalyst in the presence of at least one polymerisation inhibitor in a continuous re-esterification installation. Reacting substances are continuously fed into the corresponding reactor (1) and the alcohol formed from the reaction is continuously removed in form of an azeotropic mixture of methanol and methyl(meth)acrylate (13) (mixture of ethanol and ethylacrylate 13, respectively) using a distillation column (2). The reaction mixture is constantly fed from the reactor into the distillation column (3) or, respectively, into evaporator (5). Highly volatile components (A, B, methanol or, respectively, ethanol) and a very small part of amide end product (C) are tapped from the head of the column and returned to the reactor. Amide end products (C) together with catalyst and polymerisation inhibitor, as well as heavy by-products are tapped from the bottom of the column. Material flow (15) from the bottom of the distillation column (3) is continuously taken for distillation to obtain pure end product.

EFFECT: improved quality of product, high efficiency and output.

15 cl, 1 tbl, 1 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: improved method of producing 2,7-bis[2-(diethylamino)ethoxy]fluoren-9-one dihydrochloride, known as thylorone or amixine, and used as an immunostimulating and antiviral agent, involves treating 2,7-bis[2-(diethylamino)ethoxy]fluoren-9-one in methylene chloride with hydrogen chloride in gaseous state of in form of hydrochloric acid, preferably in molar ratio 2,7-bis[2-(diethylamino)ethoxy]fluoren-9-one : hydrochloric acid equal to 1:2.05-3.0. A solution of 2,7-bis[2-(diethylamino)ethoxy]fluoren-9-one dihydrochloride in methylene chloride is obtained, which is cooled to temperature not below minus 12C to obtain a suspension and then filtered and dried. The filtered residue is dried in inert gas or air at temperature from 90 to 110C or in a vacuum, as a rule. Completion of salt formation is usually controlled from increase in temperature of the reaction mass and its stabilisation to a value between 32 and 34C, as well as from the pH value, which must not be higher than 4.0. The filtered residue is dried in an inert gas or air, at temperature from 90 to 110C or in a vacuum, as a rule.

EFFECT: simplification of the process due to exclusion of inflammable solvents and obtaining a product of high quality with high output.

6 cl, 1 dwg, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing and aminophenol compound of formula (1) , where each of R1 and R2, which can be identical or different, are a hydrogen atom, C1-C6 alkyl group, which can be substituted with phenyl, or phenyl; R1 and R2 together with the neighbouring nitrogen atom can form a 5- or 6-member heterocyclic group, selected from piperidinyl and piperazinyl; the heterocyclic group can be substituted with one substitute selected from hydroxyl group, C1-C6 alkyl group and phenoxy group, which can have a C1-C6 alkoxy group, substituted with 1-3 halogen atoms. The method involves reacting a cyclohexanedione compound of formula (2) with a amine compound of formula (3) , where R1 and R2 assume values given above, in neutral or basic conditions.

EFFECT: wider range of use of the compound.

8 cl, 4 dwg, 13 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method for synthesis of 4-(dimethylamino)-1-alkyl-1-methyl-2-alkyn-1-ols of general formula (1): where R=C2H5, C4H9, C6H13, which are substances with physiological activity, particularly cholinolytic properties. The method involves reacting 3-alkyl-3-methyl-1-alkyn-3-ols with N,N,N1,N1-tetramethylmethanediamine in the presence of a copper monochloride catalyst in molar ratio 3-alkyl-3-methyl-1-alkyn-3-ol: N,N,N1,N1-tetramethylmethanediamine: CuCl=10:(10-12):(0.4-0.6) in an argon atmosphere at temperature 50-90C and atmospheric pressure, predominantly at 80C, for 3-5 hours. Output of 4-(dimethylamino)-1-alkyl-1-methyl-2-alkyn-1-ols (1) is 84-96%.

EFFECT: method increases output of products.

1 cl, 3 dwg, 1 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method of producing 2-[(dimethylamino)methyl]phenol used in the food industry and medicine, as well as lubrication and engine oil additives, corrosion inhibitors for different types of steel, stabilisers of motor car and rocket fuel, monomers, plastic and different types of rubbers. The method involves reacting phenol with N,N,N,N-tetramethylmethylenediamine. The reaction is carried out in the presence of a copper (I) chloride catalyst in molar ratio phenol: N,N,N,N-tetramethylmethylenediamine: CuCl=10:(10-11):(0.2-0.4) at atmospheric pressure, mainly at temperature of 50C for 3.5-4.5 hours.

EFFECT: increased selectivity of the process and output of the desired product, reduced reaction temperature.

1 cl, 2 dwg, 1 tbl, 1 ex

FIELD: medicine, pharmaceutics.

SUBSTANCE: in the given invention, there is offered a method for preparing a compound of formula , where Y is specified of CH3, CH2OH, CH2CH2OH, CH2Br and Br; involving the stages: (1) reaction of the compound of formula where OX represents hydroxy or O-M+ where M+ represents cation chosen of Li+, Na+ and K+ and Y is such as specified above; with trans-cynnamaldehyde , with a secondary amine compound added; then (2) acid treatment of a product from the previous stage to prepare a compound of formula (I). The aforesaid method can be used for preparing tolterodine and fezoterodine which are effective in treating the hyperactive urinary bladder. There are also declared compounds of formulae V, VI and VII.

EFFECT: development of the effective method for preparing the compound.

25 cl, 19 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of continuous production of alkylamino(meth)acrylamide of formula (C) by reacting a formula (B) compound with a formula (A) compound in the presence of a re-esterification catalyst in the presence of at least one polymerisation inhibitor in a continuous re-esterification installation. Reacting substances are continuously fed into the corresponding reactor (1) and the alcohol formed from the reaction is continuously removed in form of an azeotropic mixture of methanol and methyl(meth)acrylate (13) (mixture of ethanol and ethylacrylate 13, respectively) using a distillation column (2). The reaction mixture is constantly fed from the reactor into the distillation column (3) or, respectively, into evaporator (5). Highly volatile components (A, B, methanol or, respectively, ethanol) and a very small part of amide end product (C) are tapped from the head of the column and returned to the reactor. Amide end products (C) together with catalyst and polymerisation inhibitor, as well as heavy by-products are tapped from the bottom of the column. Material flow (15) from the bottom of the distillation column (3) is continuously taken for distillation to obtain pure end product.

EFFECT: improved quality of product, high efficiency and output.

15 cl, 1 tbl, 1 ex, 1 dwg

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