Continuous process for the preparation of thiocarboxylate silane
View Patent ↗The invention is directed to a process for the preparation of thiocarboxylate silane comprising reacting an aqueous solution of a salt of a thiocarboxylic acid with a haloalkylalkoxysilane in the presence of a solid supported catalyst. The invention is also directed to a process for the preparation of an aqueous solution of a salt of a thiocarboxylic acid which comprises reacting an aqueous solution of a sulfide and/or hydrosulfide with a carboxylic acid halide and/or acid anhydride.
1. A process for the continuous preparation of thiocarboxylate silane comprising
(i) continuously feeding into a continuous plug flow reactor containing a solid supported catalyst comprising a salt of a positively charged nitrogen-containing functional group,
(a) an aqueous liquid phase solution of an ammonium or alkali metal salt of thiocarboxylic acid, and
(b) a non-aqueous liquid phase haloalkylalkoxysilane:
(ii) continuously contacting the aqueous liquid phase solution of the ammonium or alkali metal salt of thiocarboxylate acid (a) with the non-aqueous liquid phase haloalkylalkoxysilane (b)
(iii) continuously reacting the ammonium or alkali metal salt of thiocarboxylate acid with the haloalkylalkoxysilane to form a non-aqueous liquid phase thiocarboxylate silane and an aqueous liquid phase solution of the ammonium or alkali metal salt of the halide;
(iv) continuously removing from the plug flow reactor the non-aqueous liquid phase thiocarboxylate silane and the aqueous liquid phase solution of the ammonium or alkali metal salt of the halide formed in step (iii); and
(v) separating the non-aqueous liquid phase thiocarboxylate silane from the aqueous liquid phase solution of the ammonium or alkali metal salt of the halide formed in step (iv),
to provide a continuous stream of thiocarboxylate silane reaction product.
2. The process of claim 1 wherein the continuous plug flow reactor is a continuous tubular plug-flow fixed bed reactor.
3. The process of claim 2 wherein the continuous tubular plug-flow fixed bed reactor has a ratio of internal diameter to length of from 3 to 100.
4. The process of claim 2 wherein the continuous tubular plug-flow fixed bed reactor has an average contact time r in a single pass of from 5 to 40 minutes.
5. The process of claim 2 wherein the continuous tubular plug-flow fixed bed reactor has an average space velocity in a single pass 6 of from a 0.01 to about 0.20 minutes −1 .
6. The process of claim 1 further comprising continuously sending the continuous stream of thiocarboxylate silane reaction product to a continuous phase separator and continuously separating the continuous stream of thiocarboxylate silane reaction product into an organic phase containing thiocarboxylate silane product and an aqueous waste phase in the continuous phase separator.
7. The process of claim 6 wherein the continuous phase separator is a two-phase product decanter.
8. The process of claim 6 wherein the rate of the continuous sending of the continuous stream of thiocarboxylate silane reaction product from the continuous plug flow reactor to the continuous phase separator is such that the phase separation is continuous.
9. The process of claim 6 further comprising sending the separated organic phase to at least one separatory column and continuously removing byproducts and/or unreacted haloalkyl silane in the at least one separatory column.
10. The process of claim 9 wherein the at least one separatory column comprises at least two separatory columns in series wherein a first separatory column operating at a first temperature and a first vacuum removes at least one of alkanol, water and tetraalkylorthosilicate and a second separatory column operating at a second temperature and a second vacuum which are higher than the first temperature and first vacuum wherein the second separatory column removes unreacted haloalkyl silane.
11. The process of claim 9 wherein the rate of feed from the continuous phase separator to the at least one separatory column is such that the rate of removal of byproducts and/or unreacted haloalkylalkoxysilane in the at least one separatory column is continuous.
12. The process of claim 1 wherein the continuous stream of thiocarboxylate silane reaction product is recycled into the continuous plug flow reactor at least one time prior to being sent to the continuous phase separator.
13. The process of claim 12 wherein the continuous stream of thiocarboxylate silane reaction product is recycled into the continuous plug flow reactor from 5 to 10 times prior to being sent to the continuous phase separator.
14. The process of claim 1 wherein the aqueous solution of a salt of a thiocarboxylic acid and the haloalkylalkoxysilane are first continuously premixed in a premix reactor.
15. The process of claim 14 wherein the aqueous solution of a salt of a thiocarboxylic acid and the haloalkylalkoxysilane are continuously sent to the premix reactor from two separate vessels wherein one of the separate vessels contains and/or is continuously fed with the aqueous solution of a salt of a thiocarboxylic acid and the other of the two separate vessels contains and/or is continuously fed with the haloalkylalkoxysilane.
16. The process of claim 15 wherein the rate of the continuous feed of the aqueous solution of a salt of a thiocarboxylic acid and the rate of the continuous feed of the haloalkylalkoxysilane is such that it provides a continuous stream of reactants to the premix reactor and the rate of the feed of the premixed reactants in the premix reactor to the continuous plug flow reactor is such that the reaction of aqueous solution of a salt of a thiocarboxylic acid and haloalkylalkoxysilane in the continuous plug flow reactor is continuous.
17. The process of claim 1 wherein the solid supported catalyst comprising a salt of a positively charged nitrogen-containing functional group, wherein the positively charged nitrogen-containing functional group has the chemical Formula (1):
[—R 1 N(R 2 ) 2 —R 3 ] + X − (1)
wherein
R 1 is a divalent alkylene, cycloalkylene, alkenylene, aralkylene, arylene, arenylene group having from 1 to 20 carbon atoms;
each R 2 is independently a monovalent alkyl, cycloalkyl, alkenyl, aralkyl, aryl or arenyl group having from 1 to 20 carbon atoms or hydrogen,
each R 3 is a monovalent alkyl, cycloalkyl, alkenyl, aralkyl, aryl or arenyl group having from 1 to 20 carbon atoms, hydrogen or —C(═NR 2 )—NR 2 group;
X − is fluoride, chloride, bromide or iodide.
18. The process of claim 1 wherein the solid supported catalyst comprising a salt of a positively charged nitrogen-containing functional group has the chemical Formula (2):
[SiO 4/2 ] m [[Si(O—) (3-x)/2 (CH 3 ) a (—R 1 N(R 2 ) 2 —R 3 )] + X − ] n [Si(O—) (3-y)/2 (CH 3 ) b R 4 ] o (2)
wherein
R 1 is a divalent alkylene, cycloalkylene, alkenylene, aralkylene, arylene, arenylene group having from 1 to 20 carbon atoms;
each R 2 is independently a monovalent alkyl, cycloalkyl, alkenyl, aralkyl, aryl or arenyl group having from 1 to 20 carbon atoms or hydrogen,
each R 3 is a monovalent alkyl, cycloalkyl, alkenyl, aralkyl, aryl or arenyl group having from 1 to 20 carbon atoms, hydrogen or —C(═NR 2 )—NR 2 group;
each R 4 is independently monovalent alkyl, cycloalkyl, arenyl, aryl or arenyl group containing from 1 to 18 carbon atoms, and optionally containing at least one oxygen, nitrogen or sulfur atom, —OH or —OR 2 group, and m is greater than 1; n is greater than 1; o is greater than 1; x is 0, 1 or 2; and y is 0, 1 or 2.
19. The process of claim 18 wherein m is 50 to 10,000; n is greater than 5 to 500; o is 0 to 500; x is 0, 1 or 2; y is 0, 1 or 2; R′ is methylene, ethylene or propylene; R 2 is methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-pentyl or n-hexyl; R 3 is methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-pentyl, n-hexyl, —(C═N(CH 3 ) 2 N(CH 3 ) 2 ) or —(C═N(CH 2 CH 3 ) 2 N(CH 2 CH 3 ) 2 ); R 4 is methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-pentyl or n-hexyl, hydroxyl, methoxy, ethoxy, propoxy, isopropoxy, butoxy or pentoxy; and X is chloride or bromide.
20. The process of claim 18 wherein the solid supported catalyst comprising a salt of a positively charged nitrogen-containing functional group is selected from the group consisting of chloride, tributylammonium propyl, silica; chloride, tributylammonium propyl 2-hydroxyethylsulfide ethyl silica; chloride, tributylammonium propyl dodecylsulfide ethyl silica; bromide, tributylammonium propyl, silica; combinations thereof and aqueous solutions thereof.
21. The process of claim 1 wherein the thiocarboxylate silane is 3-octanoylthio-1-propyltriethoxy silane.
22. The process of claim 1 wherein the aqueous liquid phase solution of an ammonium or alkali metal salt of thiocarboxylic acid of step (i)(a) is prepared by continuously reacting in a continuous stirred tank reactor an aqueous solution of a sulfide and/or hydrosulfide with a carboxylic acid halide and/or acid anhydride to provide a continuous stream of aqueous solution of thiocarboxylic acid salt.
23. The process of claim 22 wherein the aqueous solution of a sulfide and/or hydrosulfide and the carboxylic acid halide and/or acid anhydride are continuously added at a fixed rate to the continuous stirred tank reactor and the continuous stream of aqueous solution of thiocarboxylic acid salt and H 2 S are continuously removed from the continuous stirred tank reactor at a fixed rate wherein the rate of addition and removal are such that the reaction is continuous.
24. The process of claim 23 wherein the continuous stirred tank reactor is maintained at a temperature of from 20° C. to 35° C.
25. The process of claim 22 wherein prior to the commencement of the continuous reaction, the aqueous solution of a sulfide and/or hydrosulfide and the carboxylic acid halide and/or acid anhydride are provided to the continuous stirred tank reactor until the contents of the continuous stirred reactor occupy a desired volume of from 50 to 90 percent of the volume of the continuous stirred reactor.
26. The process of claim 22 wherein the continuous stirred tank reactor further contains a homogenous catalyst, tetrabutyl ammonium bromide.
27. The process of claim 1 wherein the continuous plug flow reactor is a continuous tubular plug-flow fixed bed reactor, having a ratio of internal diameter to length of from 3 to 100, an average contact time τ in a single pass of from 5 to 40 minutes and an average space velocity σ in a single pass of from 0.01 to 0.20 minutes.
28. The process of claim 1 , wherein separating the non-aqueous liquid phase thiocarboxylate silane from the aqueous liquid phase solution of the ammonium or alkali metal salt of the halide formed in step (iv) is carried out in the two-phase product decanter.
29. The process of claim 1 further comprising sending the separated continuous stream of thiocarboxylate silane reaction product to at least two separatory columns in series wherein a first separatory column operating at a first temperature and a first vacuum removes at least one of alkanol, water and tetraalkylorthosilicate and a second separatory column operating at a second temperature and a second vacuum which are higher than the first temperature and first vacuum wherein the second separatory column removes unreacted haloalkylalkoxysilane.
30. The process of claim 1 wherein the solid supported catalyst comprising a positively charged nitrogen-containing functional group is selected from the group consisting of chloride, tributylammonium propyl, silica; chloride, tributylammonium propyl 2-hydroxyethylsulfide ethyl silica; chloride, tributylammonium propyl dodecylsulfide ethyl silica; bromide, tributylammonium propyl, silica; combinations thereof and aqueous solutions thereof.