CA1153771A - Production of hydrocarbylthioaldoxime in aqueous methanol solvent - Google Patents
Production of hydrocarbylthioaldoxime in aqueous methanol solventInfo
- Publication number
- CA1153771A CA1153771A CA000377983A CA377983A CA1153771A CA 1153771 A CA1153771 A CA 1153771A CA 000377983 A CA000377983 A CA 000377983A CA 377983 A CA377983 A CA 377983A CA 1153771 A CA1153771 A CA 1153771A
- Authority
- CA
- Canada
- Prior art keywords
- methanol
- product
- hydrocarbylthioaldoxime
- solvent
- product solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Abstract
PRODUCTION OF HYDROCARBYLTHIOALDOXIME
IN AQUEOUS METHANOL SOLVENT
ABSTRACT OF THE DISCLOSURE
An aldoxime is reacted with chlorine or bromine to form a haloaldoxime in aqueous solution including methanol, and the haloaldoxime in aqueous solution including methanol is reacted with an alkali hydrocarbylmercaptide, or a hydro-carbylthiol and a base, to form a hydrocarbylthioaldoxime product in aqueous solution including methanol. The product solution is neutralized; methanol is evaporated from the product solution; and the product is recovered as a solid.
The product, such as methylthioacetaldehyde oxime, is a pesticide intermediate.
IN AQUEOUS METHANOL SOLVENT
ABSTRACT OF THE DISCLOSURE
An aldoxime is reacted with chlorine or bromine to form a haloaldoxime in aqueous solution including methanol, and the haloaldoxime in aqueous solution including methanol is reacted with an alkali hydrocarbylmercaptide, or a hydro-carbylthiol and a base, to form a hydrocarbylthioaldoxime product in aqueous solution including methanol. The product solution is neutralized; methanol is evaporated from the product solution; and the product is recovered as a solid.
The product, such as methylthioacetaldehyde oxime, is a pesticide intermediate.
Description
77~
D~SCRIPTION
.
PRODUCTION OF HYDROCARBYLTHIOALr)OXIME
IN AQUEOUS ME~HANC)L SOLVEIIT
BACKGROUNJ) OF THE INVENTIOrl The production of hydrocarbylthioaldoximes of the formula (1) R--C=rlOH ( 1 ) S-R' where R is alkyl of 1-3 carbons, hydroxyalkyl of 1-3 carbons, phenyl or cyclohexyl and R' is alkyl of 1 3 carbons, phenyl or cyclohexyl is well known. Conven-tionally, the aldoxime R-CH=~OH is reacted with chlorine 0 or bromine to form a haloaldoxime of formula (2) R-C=NOH (2) X
where X is Br or Cl, with the formation of by-product HCl or I~Br. The haloaldoxime is then reacted with either an alkali mercaptide of the formula M-S-~' or with the alkanethiol R'-S-H and the base M-OH, where !~1 is sodium, potassium or lithium to form the product of formula (1)~ Again, by-product HX is theoretically liberated; however, conventionally, excess base is added, either in forming the alkali mercaptide or with the alkanethiol, so as to neutralize the by-product acid of each step.
While the alkylthioaldoxime of formula (1) may be further reacted in solution (especially if non-7~
aqueous) to form additional products, such asthiocarbamates, it is frequently desirable to isolate the hydrocarbylthioaldoxime. It is desirable to trans-port same as a dry solid, especially since, in the presence of water and/or acidity, it is capable of hydrolysis, melting and decomposition. One method of recovering the hydrocarbylthioaldoxime from solution is to neutralize the product solution and then cool until most of the hydrocarbylthioaldoxime precipitates, and thereafter separate the precipitate from the ~other liquor. The mother liquor presentsl however, a disposal problem since it generally contains some dissolved product hydrocarbylthioaldoxime and various by-products including dialkyl disulfides, mercaptan, aldehydes, nitriles, free hydroxylamine and the like, in addition to large amounts of the alkali halide MX. In order to dispose of this liquid in an environmentally safe manner, it has been necessary to heat same to elevated temperatures with acid, phase separate the organics and then steam strip the remaining organics for incineration before seweraying the aqueous salt solution.
Solvents for the above two reactions have been described in the literature. Thus, for example, U.S.
Patents 3,658,869, 3,574,736 and 3,987,096 describe such reactions in water. U.S. Patent 3,658,869 requires essentially only water as the liquid reaction medium.
U.S. Patent 3,574,736 requires that the aldoxime he present in solution in an amount from 1 to 13 percent by weight. U.S. Patent 3,752,841 requires that the solvent 3~ contain at least 1~ percent by weight of dimethylfor-mamide. U.S. Patent 3r987,096 requires that the process be continuous or semi-continuous and that the aldoxime, namely acetaldoxime, be at a concentration below 1~.
U.S. Patent 3,574,736 indicates the desirability of `35 keeping the temperature ran~e during the chlorination reaction between 25C and -15C, preferably near the freezing point of the solution. It also indicates the desirability of adding a water-miscible organic solvent .
which does not react with chlorine under reaction con-ditions to depress the freezing point of the reaction mass, and suggests methanol, dioxane and dimethylfor-mamide.
J.M.J. Tronchet et al. have described in Pharm, Acta ~elv, vol. 50, No. 11, pp. 404-414 (1975) various intermediates in the following reaction sequence:
(3) (4) (5) Cl Cl R-CH=IIOH - - - > R-C~-r~=O - ~ R~C=NOH
r ~ I
Cl O- Cl ~ ~ ' R-CH-N=N-CH-R
+
O-(6) It will be appreciated that the starting material (3) is an aldoxime and the product ~5) is a haloaldoxime included within above formula (2). The compound of primary interest herein is where R is methyl: that is the chlorination of acetaldoxime to chloroacetaldoxime.
This article indicates the structure of the "nitroso"
intermediate ~4) and the "dimer" by-product (6) which is in equilibrium therewith.
It is also known that oximes generally, and including acetaldoxime and chloroacetaldoxime, are capable of side reactions including hydrolysis to aldehydes and hydroxamic acids, respectively, and, in the case of halogenated compounds, further hydrolysis to free acids. It is also known that, in the presence of excess chlorine, chloroacetaldoxime (5) ~where R is methyl) or the intermediate nitroso compound ~4) can be further chlorinated to l,l-dichloro-l-nitroso ethane or '7~
CH3-CC12-N=O. All of the following products are also eapable of explosive decomposition at even slightly elevated temperatures:
(6) The dimer (at about 53C or above) (5) Chloroacetaldoxime (acetohydroxamyl chloride) ~above about 25C) BRIEF DESCRIPTION OF THE DRAWING
Figure 1 is a schematic of one embodiment of the present process.
BRIEF DESCRIPTION OF THE I~IVE~ITIO~
The present invention includes an improvement in a process for preparing a hydrocarbylthioaldoxime of the formula:
P~-C=~IOH
S-R' wherein R iS alkyl of 1-3 earbons, hydroxyalkyl of 1-3 earbons, phenyl or eyclohexyl and R' is alkyl of 1-3 carbons, phenyl or cyelohexyl by the steps eomprising:
(a) reaeting an aldoxime of the formula R-CH=NOH in aqueous media with ehlorine or bromine to form a first product solution of haloaldoxime of the formula R-CX=NOH where X is Cl or Br in aqueous media, and ~ b) reactlng the first produet solution formed in (a) with a thiohydrocarbylatlon reagent seleeted from the group eonsisting of an alkali hydroearbylmereaptide and a mixture of an alkali hydroxide with a hydrocarbylthiol to form a second product solution of the hydrocarbylthioaldoxime in aqueous media, (c) neutralizing the second product solution;
and (d) recovering the hydrocarbylthioaldoxime as a solid from the neutralized second product ~olutionO
In the improvement, both reactions are carried out in a solvent consisting essentially of 80-99% water and 1-~0%
methanol by weight and methanol is evaporated from ~he second product solution before the hydrocarbylthio-aldoxime is recovered.
The starting material of the present invention S is an aldoxime of formula (3) wherein R is alkyl or hydroxyalkyl of 1-3 carbons, phenyl or cyclohexyl.
Examples include acetaldehyde oxime, propionaldehyde oxime, n-butyraldehyde oxime, hydroxyacetaldehyde oxime, 4-hydroxybutyraldehyde oxime, benzaldehyde oxime and cyclohexanecarboxaldehyde oxime. Acetaldehyde oxime is preferred. The halogenating agent is chlorine or bromine, preferably chlorine.
The thiohydrocarbylation agent may be an alkali hydrocarbylmercaptide such as the sodium, potassium lithium methylmercaptides, ethylmercaptides, propyl mercaptides, phenylmercaptides and cyclohexyl-mercaptides. Alternatively, an alkali hydroxide such as NaOH, KOH or LioH may be introduced together with the hydrocarbylthiol such as methanethiol, ethanethiol, propanethiol, benzenethiol or cyclohexanethiol. In either event it is preferred that some excess hydroxide be present: e.g. a small amount on a molar basis with the alkali hydrocarbylmercaptide or a small excess over the molar amount of the hydrocarbylthiol. Thus the thiohydrocarbylation is preferably conducted ~t a basic p~ producin~ a basic (over p~l 7) second product solution.
The reaction temperature for the halogenation can vary from the freezing point of the reaction mixture to the temperature at which the haloaldoxime becomes susceptible to violent decomposition ~about 25C, at least in the case of chloroacetaldehyde oxime)D The reaction temperature for the thiohydrocarbylation is subject to similar constraints and to an increasing pressure of mercaptan in some instances if it is volatile (as is methanethiol). In general, thè reaction temperatures of the present invention are those of the prior art patents discussed above. The preferred 77~
temperature range for halogenation is between about -15C and about 10C. The preferred temperature range for the thiohydrocarbylation is between about 0C and about 30C.
The product hydrocarbylthioaldoxime may be recovered from the second product solution by a variety of techniques. It is desirable to first neutralize the second product solution to a moderate p~ such as about 6.5 to about 8.0, and preferably to no more than p~l 7.5.
The methanol may be evaporated from the second product solution before, durin~ or after neutralization. At least with R' being methyl or ethyl, the hydrocarbyl-mercaptan R'-SH is frequently also evaporated with the methanol. They may be separated by conventional techniques (e.g. distillation) and recycled, e.g. by recycling the methanol to the chlorination step and the mercaptan to either an alkali hydrocarbylmerca?tide-forming step or to the thiohydrocarbylation step.
After the methanol has been evaporated and the second solution has been neutralized, the product may then be recovered, preferably by cooling the organic solution to precipitate the product hydrocarbylthio-aldoxime. Alternatively, the neutralized aqueous solu-tion may be extracted with an oryanic solvent such as methylene chloride, toluene or the like to separate the hydrocarbylthioaldoxime from the aqueous system, and then the organic solution concentrated to isolate the solid. The recovered solvent can be recycled to reextract the product from the neutralized aqueous solution. Whether the product is precipitated frol-n the aqueous solution or from an organic solvent, it is preferred to thoroughly dry it for stability purposes, particulary against hydrolysis.
An overall continuous process for the production of solid hydrocarbylthioaldoxime according to the present process is depicted in Figure 1. For sim-plicity, the simplest product methylthioacetaldehyde oxime (hereinafter MTAAO) is used as the product and the 3~:7:a ~ 7-appropriate raw materials acetaldehyde oxime and methyl mercaptan are shown as reactants introduced into the system~
A first reactor 10 equipped with agitation S means is shown. Methanol is introduced into reactor 10 through stream 11 and aqueous acetaldehyde oxime is introduced into reactor 10 through stream 12. The con-centration of acetaldehyde oxime and the relative rates in streams 11 and 12 are designed to form a solvent system of 1-20% methanol and 80-99% water, with the acetaldehyde oxime introduced being between about 15 and about 40%, preferably between about 15 and about 30%, of the solvent, by weight. Chlorine is also introduced into reactor 10 through stream 13 at a rate regulated by a variable flow valve 14 controlled as described below.
Reaction mixture is continuously withdrawn from the bottom of reactor 10 through stream 15 and pumped through a meter 16 which determines the presence of free chlorine and then through a heat exchanger to cool the reaction mixture. Meter 16 is operatively connected to variable flow valve 14 so as to admit chlorine at essentially the maximum rate permissible without producing free chlorine in stream 15. After cooling, the fluid in stream 15 is split into stream 17 which is reintroduced into reactor 10 and stream 1~
which is carried forward to thiomethylation reactor 20.
Reactor 20 is also equipped with agitation. A
conventional system for the production of sodium methyl mercaptide 21 is present so as to produce a stream 22 containing approximately equal molar amounts of free sodium hydroxide and sodium methyl mercaptide CF~3SNa.
The reaction mass is continuously withdrawn from the - 35 bottom of reactor 20 in stream 23 and pumped throuqh a heat exchanger to cool same and then split into a recycle stream 24 which is reintroduced into reactor 20 and a for~ard stream 25.
~i,,3~
Stream 25, now containing the second aqueous product solution of methylthioacetaldehyde oxime (MTAA~) is introduced into neutralization reactor 26, also eq~ipped with agitation, where free acid HCl is mixed therewith coming in through stream 27. Methanol is evaporated from the solution in vessel 26 through stream 28, which also may contain free methyl mercaptan. A
separation vessel 29 (e.g. a still equippe~ with pressure and temperature control and reflux, all being conven tional and not illustrated) separates the methyl mercaptan from the methanol by distillation or other physical or chemical process. The methyl mercaptan is returned from vessel 29 in stream 30 to system 21. The methanol is returned from vessel 29 in stream 31 to stream 11 and reintroduced into the chlorination reactor 10 .
The effluent from the neutralization vessel 26 is removed in stream 32 and cooled in heat exchanger 33 and then conducted to liquid-solid separation device 34 (a centrifugation system or the like). Solid product MTAAO 35 is removed from separation vessel 34 and then dried. The remaining liquid is removed from separation vessel 34 in stream 36 and conducted to a disposal system 37 which may include acidification of the stream, separation into aqueous an~ organic phases, evaporation of residual organics in the aqueous ~hase, incineration of the cor,lbined organic phases and the safe disposal of the remaining aqueous sodium chloride solution.
The presence of methanol in the solvent has several desirable effects. In chlorination reactor 10, methanol retains any dimer formed in solution so that it may revert to nitroso compound (based on the equili-brium) and then irreversibl~7 rearrange to the chloro-aldehyde oxime. The absence of free dimer as a slurried solid in stream 18 avoids such hazards as explosivity and a source of acidity that causes isomerization and violent M,AAO decomposition during drying.
In addition, the ability of the system to _9_ prevent dimer from precipitating out permits the concentration of acetaldoxime relative to solvent introduced in streams 11 and 12 to exceed the 13~
permissible maximum set when water is the sole solvent.
Therefore, the concentration of oximes (including acetaldoxime, chloroacetaldoxime and MTAAO) throughout the system can be significantly increased. The result is that the MTAAO is much more concentrated in stream 32 than would be possible if methanol were not introduced into the system. Accordingly, the quantity of liquid in stream 36 sent to disposal system 37 is decreased. This enables higher overall yields of solid product (since stream 36 invariably contains a ~ew percent ~TAAO)~ less heating in system 37 to evaporate the organics and less load on heat exchanger 33, separation vessel 34 and the incineration system portion of disposal system 37.
Finally, the evaporation of methanol from vessel 26 into stream 28 causes a cooling of the liquid in vessel 26.
This in turn further reduces the cooling load upon heat exchanger 33 in order to cool the slurry in stream 32 sufficiently to maximize solid product 35.
Example 1 Starting Materials:
Aqueous acetaldoxime ~54% by wt) 185 g (1.69 moles) Water 265 g Methanol 50 ml, t40 g) Chlorine 120 y (1.69 moles) A one liter jac}~.eted resin flas~ was equipped with an over-head agitator and connected to a dry ice-cooled methanol bath. A platinum depolarizer device wasemployed to indicate level of chlorination. The tem-perature of the reaction was recorded by a thermometer placed in the ~eactor.
The acetaldoxime, water and methanol were mixed together and placed in the reactor. This produced a 20% acetaldehyde oxime solution in 10.3-89.7%
methanol-water. Agitation and cooling were started.
The temperature was brought to -2C. Chlorine gas was ~;3~
sparged in from a pre~weighed lecture bottle througll a calibrated flow meter.
Chlorine addition was completed over 30 min-utes, while the temperature was maintained between -5 and 0C. mhe solution was light bluish-colored and there was no indication of any solid dimer being formed.
After holding for 30 minutes with cooliny, the chlorination mass was run into sodium thio~ethylate solution (excess) prepared from methyl mercaptan and 50%
sodium hydroxide. After the addition was completed, a pH of 1~.5 was found. Stirring continued for 15 minutes more, and then pH was adjusted to 7.0 with HCl.
A white precipitate of methylthioacetaldehyde oxime separated out. This precipitate was filtered out after cooling to 0C.
On drying, 118 g of the methylthioacetalde oxime was collected and its melting point was determined to be 90-92C~ This represents about a 77% yield based upon acetaldehyde oxime.
Gas chromatographic analysis showed no new impurities compared to a sample from operation (at about 13~) employing only water as reaction medium.
Example 2 Example 1 was repeated by forming the 20~
acetaldehyde oxime solution in methanol-waterl adding chlorine and holding for 30 minutes in an identical manner. Likewise, addition of sodium thiomethylate and neutralization were conducted as in Example 1. The slurry was then subjected to vacuum (about 50 mm mercury or 6.7 kPa) for two hours while holAing the temperature at about 3QC. The residue was then cooled to 0C, and the thick slurry that formed was filtered. The solid was then dried to produce 146 g of MTAAO, melting point 90-92C. The purity level based on gas chromatography was no different from the product of Example 1, but the yield (based on acetaldehyde oxime) was about 95 instead of about 77%.
7~7:~
Example 3 Example 1 was repeated with the ~ollowing starting materials:
Aqueous acetaldehyde 27~ g~(2.54 moles) oxime (54% by wt.) Water 172 g Methanol 150 mL (119 g) Chlorine 180 g (2.54 moles~
The 25% acetaldehyde oxime in 2P,.4-71.6% methanol-water formed from the first three materials was cooled to -2C.
Chlorine was adde3 over 45 minutes, and the mixture was held at 0C for 30 minutes. The clear light blue solution was added, with stirring, to sodium thio-methylate solution (350 g, or an excess) keeping the temperature below 20C. After 15 minutes, HCl was added to lower the pH from 12.9 to 7.5. ~ethanol was then evaporated off at about 50 mm mercury (6.7 kPa) and about 30C over two hours. The residual slurry was cooled to -5C to produce a thick slurry which was filtered. The product collected was dried and weighed as 224 g of MTAAO, melting point 90-92C. The higher methanol content and oxime concentration had no apparent adverse effect on the product which was produced in about 97% yield, based on acetaldehyde oxime.
D~SCRIPTION
.
PRODUCTION OF HYDROCARBYLTHIOALr)OXIME
IN AQUEOUS ME~HANC)L SOLVEIIT
BACKGROUNJ) OF THE INVENTIOrl The production of hydrocarbylthioaldoximes of the formula (1) R--C=rlOH ( 1 ) S-R' where R is alkyl of 1-3 carbons, hydroxyalkyl of 1-3 carbons, phenyl or cyclohexyl and R' is alkyl of 1 3 carbons, phenyl or cyclohexyl is well known. Conven-tionally, the aldoxime R-CH=~OH is reacted with chlorine 0 or bromine to form a haloaldoxime of formula (2) R-C=NOH (2) X
where X is Br or Cl, with the formation of by-product HCl or I~Br. The haloaldoxime is then reacted with either an alkali mercaptide of the formula M-S-~' or with the alkanethiol R'-S-H and the base M-OH, where !~1 is sodium, potassium or lithium to form the product of formula (1)~ Again, by-product HX is theoretically liberated; however, conventionally, excess base is added, either in forming the alkali mercaptide or with the alkanethiol, so as to neutralize the by-product acid of each step.
While the alkylthioaldoxime of formula (1) may be further reacted in solution (especially if non-7~
aqueous) to form additional products, such asthiocarbamates, it is frequently desirable to isolate the hydrocarbylthioaldoxime. It is desirable to trans-port same as a dry solid, especially since, in the presence of water and/or acidity, it is capable of hydrolysis, melting and decomposition. One method of recovering the hydrocarbylthioaldoxime from solution is to neutralize the product solution and then cool until most of the hydrocarbylthioaldoxime precipitates, and thereafter separate the precipitate from the ~other liquor. The mother liquor presentsl however, a disposal problem since it generally contains some dissolved product hydrocarbylthioaldoxime and various by-products including dialkyl disulfides, mercaptan, aldehydes, nitriles, free hydroxylamine and the like, in addition to large amounts of the alkali halide MX. In order to dispose of this liquid in an environmentally safe manner, it has been necessary to heat same to elevated temperatures with acid, phase separate the organics and then steam strip the remaining organics for incineration before seweraying the aqueous salt solution.
Solvents for the above two reactions have been described in the literature. Thus, for example, U.S.
Patents 3,658,869, 3,574,736 and 3,987,096 describe such reactions in water. U.S. Patent 3,658,869 requires essentially only water as the liquid reaction medium.
U.S. Patent 3,574,736 requires that the aldoxime he present in solution in an amount from 1 to 13 percent by weight. U.S. Patent 3,752,841 requires that the solvent 3~ contain at least 1~ percent by weight of dimethylfor-mamide. U.S. Patent 3r987,096 requires that the process be continuous or semi-continuous and that the aldoxime, namely acetaldoxime, be at a concentration below 1~.
U.S. Patent 3,574,736 indicates the desirability of `35 keeping the temperature ran~e during the chlorination reaction between 25C and -15C, preferably near the freezing point of the solution. It also indicates the desirability of adding a water-miscible organic solvent .
which does not react with chlorine under reaction con-ditions to depress the freezing point of the reaction mass, and suggests methanol, dioxane and dimethylfor-mamide.
J.M.J. Tronchet et al. have described in Pharm, Acta ~elv, vol. 50, No. 11, pp. 404-414 (1975) various intermediates in the following reaction sequence:
(3) (4) (5) Cl Cl R-CH=IIOH - - - > R-C~-r~=O - ~ R~C=NOH
r ~ I
Cl O- Cl ~ ~ ' R-CH-N=N-CH-R
+
O-(6) It will be appreciated that the starting material (3) is an aldoxime and the product ~5) is a haloaldoxime included within above formula (2). The compound of primary interest herein is where R is methyl: that is the chlorination of acetaldoxime to chloroacetaldoxime.
This article indicates the structure of the "nitroso"
intermediate ~4) and the "dimer" by-product (6) which is in equilibrium therewith.
It is also known that oximes generally, and including acetaldoxime and chloroacetaldoxime, are capable of side reactions including hydrolysis to aldehydes and hydroxamic acids, respectively, and, in the case of halogenated compounds, further hydrolysis to free acids. It is also known that, in the presence of excess chlorine, chloroacetaldoxime (5) ~where R is methyl) or the intermediate nitroso compound ~4) can be further chlorinated to l,l-dichloro-l-nitroso ethane or '7~
CH3-CC12-N=O. All of the following products are also eapable of explosive decomposition at even slightly elevated temperatures:
(6) The dimer (at about 53C or above) (5) Chloroacetaldoxime (acetohydroxamyl chloride) ~above about 25C) BRIEF DESCRIPTION OF THE DRAWING
Figure 1 is a schematic of one embodiment of the present process.
BRIEF DESCRIPTION OF THE I~IVE~ITIO~
The present invention includes an improvement in a process for preparing a hydrocarbylthioaldoxime of the formula:
P~-C=~IOH
S-R' wherein R iS alkyl of 1-3 earbons, hydroxyalkyl of 1-3 earbons, phenyl or eyclohexyl and R' is alkyl of 1-3 carbons, phenyl or cyelohexyl by the steps eomprising:
(a) reaeting an aldoxime of the formula R-CH=NOH in aqueous media with ehlorine or bromine to form a first product solution of haloaldoxime of the formula R-CX=NOH where X is Cl or Br in aqueous media, and ~ b) reactlng the first produet solution formed in (a) with a thiohydrocarbylatlon reagent seleeted from the group eonsisting of an alkali hydroearbylmereaptide and a mixture of an alkali hydroxide with a hydrocarbylthiol to form a second product solution of the hydrocarbylthioaldoxime in aqueous media, (c) neutralizing the second product solution;
and (d) recovering the hydrocarbylthioaldoxime as a solid from the neutralized second product ~olutionO
In the improvement, both reactions are carried out in a solvent consisting essentially of 80-99% water and 1-~0%
methanol by weight and methanol is evaporated from ~he second product solution before the hydrocarbylthio-aldoxime is recovered.
The starting material of the present invention S is an aldoxime of formula (3) wherein R is alkyl or hydroxyalkyl of 1-3 carbons, phenyl or cyclohexyl.
Examples include acetaldehyde oxime, propionaldehyde oxime, n-butyraldehyde oxime, hydroxyacetaldehyde oxime, 4-hydroxybutyraldehyde oxime, benzaldehyde oxime and cyclohexanecarboxaldehyde oxime. Acetaldehyde oxime is preferred. The halogenating agent is chlorine or bromine, preferably chlorine.
The thiohydrocarbylation agent may be an alkali hydrocarbylmercaptide such as the sodium, potassium lithium methylmercaptides, ethylmercaptides, propyl mercaptides, phenylmercaptides and cyclohexyl-mercaptides. Alternatively, an alkali hydroxide such as NaOH, KOH or LioH may be introduced together with the hydrocarbylthiol such as methanethiol, ethanethiol, propanethiol, benzenethiol or cyclohexanethiol. In either event it is preferred that some excess hydroxide be present: e.g. a small amount on a molar basis with the alkali hydrocarbylmercaptide or a small excess over the molar amount of the hydrocarbylthiol. Thus the thiohydrocarbylation is preferably conducted ~t a basic p~ producin~ a basic (over p~l 7) second product solution.
The reaction temperature for the halogenation can vary from the freezing point of the reaction mixture to the temperature at which the haloaldoxime becomes susceptible to violent decomposition ~about 25C, at least in the case of chloroacetaldehyde oxime)D The reaction temperature for the thiohydrocarbylation is subject to similar constraints and to an increasing pressure of mercaptan in some instances if it is volatile (as is methanethiol). In general, thè reaction temperatures of the present invention are those of the prior art patents discussed above. The preferred 77~
temperature range for halogenation is between about -15C and about 10C. The preferred temperature range for the thiohydrocarbylation is between about 0C and about 30C.
The product hydrocarbylthioaldoxime may be recovered from the second product solution by a variety of techniques. It is desirable to first neutralize the second product solution to a moderate p~ such as about 6.5 to about 8.0, and preferably to no more than p~l 7.5.
The methanol may be evaporated from the second product solution before, durin~ or after neutralization. At least with R' being methyl or ethyl, the hydrocarbyl-mercaptan R'-SH is frequently also evaporated with the methanol. They may be separated by conventional techniques (e.g. distillation) and recycled, e.g. by recycling the methanol to the chlorination step and the mercaptan to either an alkali hydrocarbylmerca?tide-forming step or to the thiohydrocarbylation step.
After the methanol has been evaporated and the second solution has been neutralized, the product may then be recovered, preferably by cooling the organic solution to precipitate the product hydrocarbylthio-aldoxime. Alternatively, the neutralized aqueous solu-tion may be extracted with an oryanic solvent such as methylene chloride, toluene or the like to separate the hydrocarbylthioaldoxime from the aqueous system, and then the organic solution concentrated to isolate the solid. The recovered solvent can be recycled to reextract the product from the neutralized aqueous solution. Whether the product is precipitated frol-n the aqueous solution or from an organic solvent, it is preferred to thoroughly dry it for stability purposes, particulary against hydrolysis.
An overall continuous process for the production of solid hydrocarbylthioaldoxime according to the present process is depicted in Figure 1. For sim-plicity, the simplest product methylthioacetaldehyde oxime (hereinafter MTAAO) is used as the product and the 3~:7:a ~ 7-appropriate raw materials acetaldehyde oxime and methyl mercaptan are shown as reactants introduced into the system~
A first reactor 10 equipped with agitation S means is shown. Methanol is introduced into reactor 10 through stream 11 and aqueous acetaldehyde oxime is introduced into reactor 10 through stream 12. The con-centration of acetaldehyde oxime and the relative rates in streams 11 and 12 are designed to form a solvent system of 1-20% methanol and 80-99% water, with the acetaldehyde oxime introduced being between about 15 and about 40%, preferably between about 15 and about 30%, of the solvent, by weight. Chlorine is also introduced into reactor 10 through stream 13 at a rate regulated by a variable flow valve 14 controlled as described below.
Reaction mixture is continuously withdrawn from the bottom of reactor 10 through stream 15 and pumped through a meter 16 which determines the presence of free chlorine and then through a heat exchanger to cool the reaction mixture. Meter 16 is operatively connected to variable flow valve 14 so as to admit chlorine at essentially the maximum rate permissible without producing free chlorine in stream 15. After cooling, the fluid in stream 15 is split into stream 17 which is reintroduced into reactor 10 and stream 1~
which is carried forward to thiomethylation reactor 20.
Reactor 20 is also equipped with agitation. A
conventional system for the production of sodium methyl mercaptide 21 is present so as to produce a stream 22 containing approximately equal molar amounts of free sodium hydroxide and sodium methyl mercaptide CF~3SNa.
The reaction mass is continuously withdrawn from the - 35 bottom of reactor 20 in stream 23 and pumped throuqh a heat exchanger to cool same and then split into a recycle stream 24 which is reintroduced into reactor 20 and a for~ard stream 25.
~i,,3~
Stream 25, now containing the second aqueous product solution of methylthioacetaldehyde oxime (MTAA~) is introduced into neutralization reactor 26, also eq~ipped with agitation, where free acid HCl is mixed therewith coming in through stream 27. Methanol is evaporated from the solution in vessel 26 through stream 28, which also may contain free methyl mercaptan. A
separation vessel 29 (e.g. a still equippe~ with pressure and temperature control and reflux, all being conven tional and not illustrated) separates the methyl mercaptan from the methanol by distillation or other physical or chemical process. The methyl mercaptan is returned from vessel 29 in stream 30 to system 21. The methanol is returned from vessel 29 in stream 31 to stream 11 and reintroduced into the chlorination reactor 10 .
The effluent from the neutralization vessel 26 is removed in stream 32 and cooled in heat exchanger 33 and then conducted to liquid-solid separation device 34 (a centrifugation system or the like). Solid product MTAAO 35 is removed from separation vessel 34 and then dried. The remaining liquid is removed from separation vessel 34 in stream 36 and conducted to a disposal system 37 which may include acidification of the stream, separation into aqueous an~ organic phases, evaporation of residual organics in the aqueous ~hase, incineration of the cor,lbined organic phases and the safe disposal of the remaining aqueous sodium chloride solution.
The presence of methanol in the solvent has several desirable effects. In chlorination reactor 10, methanol retains any dimer formed in solution so that it may revert to nitroso compound (based on the equili-brium) and then irreversibl~7 rearrange to the chloro-aldehyde oxime. The absence of free dimer as a slurried solid in stream 18 avoids such hazards as explosivity and a source of acidity that causes isomerization and violent M,AAO decomposition during drying.
In addition, the ability of the system to _9_ prevent dimer from precipitating out permits the concentration of acetaldoxime relative to solvent introduced in streams 11 and 12 to exceed the 13~
permissible maximum set when water is the sole solvent.
Therefore, the concentration of oximes (including acetaldoxime, chloroacetaldoxime and MTAAO) throughout the system can be significantly increased. The result is that the MTAAO is much more concentrated in stream 32 than would be possible if methanol were not introduced into the system. Accordingly, the quantity of liquid in stream 36 sent to disposal system 37 is decreased. This enables higher overall yields of solid product (since stream 36 invariably contains a ~ew percent ~TAAO)~ less heating in system 37 to evaporate the organics and less load on heat exchanger 33, separation vessel 34 and the incineration system portion of disposal system 37.
Finally, the evaporation of methanol from vessel 26 into stream 28 causes a cooling of the liquid in vessel 26.
This in turn further reduces the cooling load upon heat exchanger 33 in order to cool the slurry in stream 32 sufficiently to maximize solid product 35.
Example 1 Starting Materials:
Aqueous acetaldoxime ~54% by wt) 185 g (1.69 moles) Water 265 g Methanol 50 ml, t40 g) Chlorine 120 y (1.69 moles) A one liter jac}~.eted resin flas~ was equipped with an over-head agitator and connected to a dry ice-cooled methanol bath. A platinum depolarizer device wasemployed to indicate level of chlorination. The tem-perature of the reaction was recorded by a thermometer placed in the ~eactor.
The acetaldoxime, water and methanol were mixed together and placed in the reactor. This produced a 20% acetaldehyde oxime solution in 10.3-89.7%
methanol-water. Agitation and cooling were started.
The temperature was brought to -2C. Chlorine gas was ~;3~
sparged in from a pre~weighed lecture bottle througll a calibrated flow meter.
Chlorine addition was completed over 30 min-utes, while the temperature was maintained between -5 and 0C. mhe solution was light bluish-colored and there was no indication of any solid dimer being formed.
After holding for 30 minutes with cooliny, the chlorination mass was run into sodium thio~ethylate solution (excess) prepared from methyl mercaptan and 50%
sodium hydroxide. After the addition was completed, a pH of 1~.5 was found. Stirring continued for 15 minutes more, and then pH was adjusted to 7.0 with HCl.
A white precipitate of methylthioacetaldehyde oxime separated out. This precipitate was filtered out after cooling to 0C.
On drying, 118 g of the methylthioacetalde oxime was collected and its melting point was determined to be 90-92C~ This represents about a 77% yield based upon acetaldehyde oxime.
Gas chromatographic analysis showed no new impurities compared to a sample from operation (at about 13~) employing only water as reaction medium.
Example 2 Example 1 was repeated by forming the 20~
acetaldehyde oxime solution in methanol-waterl adding chlorine and holding for 30 minutes in an identical manner. Likewise, addition of sodium thiomethylate and neutralization were conducted as in Example 1. The slurry was then subjected to vacuum (about 50 mm mercury or 6.7 kPa) for two hours while holAing the temperature at about 3QC. The residue was then cooled to 0C, and the thick slurry that formed was filtered. The solid was then dried to produce 146 g of MTAAO, melting point 90-92C. The purity level based on gas chromatography was no different from the product of Example 1, but the yield (based on acetaldehyde oxime) was about 95 instead of about 77%.
7~7:~
Example 3 Example 1 was repeated with the ~ollowing starting materials:
Aqueous acetaldehyde 27~ g~(2.54 moles) oxime (54% by wt.) Water 172 g Methanol 150 mL (119 g) Chlorine 180 g (2.54 moles~
The 25% acetaldehyde oxime in 2P,.4-71.6% methanol-water formed from the first three materials was cooled to -2C.
Chlorine was adde3 over 45 minutes, and the mixture was held at 0C for 30 minutes. The clear light blue solution was added, with stirring, to sodium thio-methylate solution (350 g, or an excess) keeping the temperature below 20C. After 15 minutes, HCl was added to lower the pH from 12.9 to 7.5. ~ethanol was then evaporated off at about 50 mm mercury (6.7 kPa) and about 30C over two hours. The residual slurry was cooled to -5C to produce a thick slurry which was filtered. The product collected was dried and weighed as 224 g of MTAAO, melting point 90-92C. The higher methanol content and oxime concentration had no apparent adverse effect on the product which was produced in about 97% yield, based on acetaldehyde oxime.
Claims (7)
1. In the process for preparing a hydro-carbylthioaldoxime of the formula:
wherein R is alkyl of 1-3 carbons, hydroxylalkyl of 1-3 carbons, phenyl or cyclohexyl and R1 is alkyl of 1-3 carbons, phenyl or cyclohexyl by the steps comprising:
(a) reacting an aldoxime of the formula R-CH=NOH in aqueous media with chlorine or bromine to form a first product solution of a haloaldoxime of the formula R-CX=NOH where X is Cl or Br in aqueous media, (b) reacting the first product solution formed in (a) with a thiohydrocarbylation reagent selected from the group consisting of an alkali hydrocarbylmercaptide and a mixture of an alkali hydroxide with a hydrocarbylthiol to form a second product solution of hydrocarbylthioaldoxime in aqueous media;
(c) neutralizing the second product solution;
and (d) recovering the hydrocarbylthioaldoxime as a solid from the neutralized second product solution;
the improvement wherein both reactions are carried out in a solvent consisting essentially of 80-99% water and 1-20% methanol, by weight, and methanol is evaporated from the second solution before the hydrocarbylthioaldoxime is recovered.
wherein R is alkyl of 1-3 carbons, hydroxylalkyl of 1-3 carbons, phenyl or cyclohexyl and R1 is alkyl of 1-3 carbons, phenyl or cyclohexyl by the steps comprising:
(a) reacting an aldoxime of the formula R-CH=NOH in aqueous media with chlorine or bromine to form a first product solution of a haloaldoxime of the formula R-CX=NOH where X is Cl or Br in aqueous media, (b) reacting the first product solution formed in (a) with a thiohydrocarbylation reagent selected from the group consisting of an alkali hydrocarbylmercaptide and a mixture of an alkali hydroxide with a hydrocarbylthiol to form a second product solution of hydrocarbylthioaldoxime in aqueous media;
(c) neutralizing the second product solution;
and (d) recovering the hydrocarbylthioaldoxime as a solid from the neutralized second product solution;
the improvement wherein both reactions are carried out in a solvent consisting essentially of 80-99% water and 1-20% methanol, by weight, and methanol is evaporated from the second solution before the hydrocarbylthioaldoxime is recovered.
2. The process of claim 1 wherein R and R' are methyl and X is Cl.
3. The process of claim 1 wherein the total concentration of aldoxime and haloaldoxime during step (a) is between about 15 and about 40% by weight of solvent.
4. The process of claim 3 wherein said con-centration is between about 15 and about 30% by weight of solvent.
5. The process of claim 1 or 2 wherein the second product solution has a pH of at least about 7 and the second product solution is neutralized to a pH
about 6.5 to about 8.0 while the methanol is evaporated.
about 6.5 to about 8.0 while the methanol is evaporated.
6. The process of claim 2 wherein the total concentration of aldoxime and haloaldoxime during step (a) is between about 15 and about 40% by weight of solvent.
7. The process of claim 6 wherein said concen-tration is between about 15 and about 30% by weight of solvent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000377983A CA1153771A (en) | 1981-05-21 | 1981-05-21 | Production of hydrocarbylthioaldoxime in aqueous methanol solvent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000377983A CA1153771A (en) | 1981-05-21 | 1981-05-21 | Production of hydrocarbylthioaldoxime in aqueous methanol solvent |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1153771A true CA1153771A (en) | 1983-09-13 |
Family
ID=4120003
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000377983A Expired CA1153771A (en) | 1981-05-21 | 1981-05-21 | Production of hydrocarbylthioaldoxime in aqueous methanol solvent |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1153771A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109627183A (en) * | 2018-12-12 | 2019-04-16 | 湖南海利化工股份有限公司 | A kind of preparation method of chloroacetaldehyde oxime |
| CN110818603A (en) * | 2019-12-03 | 2020-02-21 | 湖南海利化工股份有限公司 | Preparation method of methomyl oxime |
-
1981
- 1981-05-21 CA CA000377983A patent/CA1153771A/en not_active Expired
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109627183A (en) * | 2018-12-12 | 2019-04-16 | 湖南海利化工股份有限公司 | A kind of preparation method of chloroacetaldehyde oxime |
| CN109627183B (en) * | 2018-12-12 | 2021-11-05 | 湖南海利化工股份有限公司 | Preparation method of chloroacetaldehyde oxime |
| CN110818603A (en) * | 2019-12-03 | 2020-02-21 | 湖南海利化工股份有限公司 | Preparation method of methomyl oxime |
| CN110818603B (en) * | 2019-12-03 | 2022-04-15 | 湖南海利化工股份有限公司 | Preparation method of methomyl oxime |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4524077A (en) | Liquid 2-hydroxy-4-methylthiobutyric acid and process for the preparation thereof | |
| US3361827A (en) | Preparation of benzalacetophenone | |
| NO147102B (en) | METHOD FOR PREPARING 2,4,6-TRI- (3,5-DI-TERTIAER-BUTYL-4-HYDROXYBENZYL) MESITYLENE | |
| CA1153771A (en) | Production of hydrocarbylthioaldoxime in aqueous methanol solvent | |
| US4937387A (en) | Processes for preparing diaryl sulfones | |
| US4052460A (en) | Production of 3,3-dimethyl-2-oxo-butyric acid salt | |
| JPS59141556A (en) | Manufacture of 4-chlorophenylsulfonyl compound | |
| EP0064091A1 (en) | Production of hydrocarbylthioaldoxime in aqueous methanol solvent | |
| US4335260A (en) | Process for the preparation of N-di-n-propyl-2,6-dinitro-4-trifluoromethylaniline having a low content of nitrosamines | |
| US5068427A (en) | Process for the preparation of alkane- and arenesulfonamides | |
| EP0371271B1 (en) | Preparation of alkanesulfonamides | |
| US4490307A (en) | Process for the production of β-mercaptopropionic acid derivatives | |
| US4845300A (en) | Synthesis of 2-(perfluoroalkyl) ethanethiols | |
| JPS5899436A (en) | Selective preparation of 2-hydroxynaphthalene-6- carboxylic acid | |
| US5998670A (en) | Method of making high purity substituted diphenyldisulfides | |
| US3998880A (en) | Production of N,N-diethyl 2(α-naphthoxy)propionamide | |
| US3133971A (en) | Process for producing sulfonium compounds | |
| US4241226A (en) | Preparation of 2-nitro-2-methyl-1-propanol | |
| US4400541A (en) | Process for preparing bis-(diphenylsulfoniophenyl)-sulfide bis-chloride | |
| CA1275657C (en) | Processes for preparing diaryl sulfones | |
| US3331205A (en) | Preparation of chlorothiophenols | |
| US4898974A (en) | Production of 3,3-dimethyl-2-oxo-butyric acid salt | |
| US5087759A (en) | Synthesis of vicinal alkanedithiols | |
| KR950008208B1 (en) | Method for preparation of mercaptobenzoates | |
| CA1203551A (en) | 4-(.alpha.-ALKYL-.alpha.-CYANO-METHYL)2,6-DI-SUBSTITUTED PHENOLS |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |