Title of Invention	A METHOD FOR PREPARING 3-(METHYLTHIO) PROPANAL & 2-HYDROXY-4-(METHYLTHIO) BUTANENITRILE
Abstract	Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein in the presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the heterogeneous catalyst is not soluble in the reaction medium which is a hydrocarbon, a halogenated hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio) butanenitrile, wherein the heterogeneous catalyst has the general formula where R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or heteroaryl; R1 can be different from R2; X is a number between 0 and 6; and A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C.

Title of Invention

A METHOD FOR PREPARING 3-(METHYLTHIO) PROPANAL & 2-HYDROXY-4-(METHYLTHIO) BUTANENITRILE

Abstract

Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein in the presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the heterogeneous catalyst is not soluble in the reaction medium which is a hydrocarbon, a halogenated hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio) butanenitrile, wherein the heterogeneous catalyst has the general formula where R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or heteroaryl; R1 can be different from R2; X is a number between 0 and 6; and A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C.

Full Text	polystyrene, dimethylaminomethylpolystyrene, diethylaminomethylmacroreticular resins, and especially diethylaminomethylpolystyrene. The said bases are already used in part in other fields of solid-phase chemistry (WO 03/009936, US 4,440,676) and some are commercially available. Furthermore, the synthesis of special derivatives is possible in a simple manner from described resins, e.g. Merrifield resin. Since the catalysts are soluble neither in the reaction product nor in one of the participating reaction partners, use may be made of any desired amount of catalyst for the reaction which leads to sufficient conversion rates and selectivities. To facilitate the reaction procedure, i.e. metering of the reaction partners, transport of the starting materials to the active centres of the catalyst and removal of the heat of reaction, a reaction medium should be present in which the catalyst is readily swellable. A resin is readily swellable in a solvent when it can absorb the same as its own mass up to five times its own mass of solvent. The resin increases its volume here with absorption of the solvent. Preferably, MMP or MMP- cyanohydrin itself can serve as matrix for the reaction. However, use can also be made of all customary solvents in which the reaction partners, but not the catalyst, are at least partially soluble, e.g. hydrocarbons, halogenated hydrocarbons or ethers. Reactive solvents such as water, alcohols and ketones which, together with the starting materials or the products, can form unwanted by-products are less suitable and may be used only with restrictions. Based on the active centres, in batch experiments for synthesizing MMP, a molar ratio of catalyst to acrolein of 0.001 to 0.02, preferably 0.001 to 0.01, particularly preferably 0.001 to 0.005 is suitable. In continuous reactions in which the reaction partners and the reaction medium flow continuously past the catalyst, the ratio of acrolein mass to catalyst mass per hour (LHSV value, m/m-h) is between 0.1 and 10 0, preferably between 1 and 50, particularly preferably between 5 and 50. The ratio of the reaction medium to acrolein is chosen in batch experiments as between 0.1 and 2. In continuous methods, the ratio of mass flow rate of reaction medium to acrolein should be between 0.5 and 20. To achieve a good conversion of the reactants and for achieving low degradation, the amounts of the starting materials used are controlled such that a slight excess of methylmercapan in the reaction mixture is maintained. The excess should be between 0.01 and 1%, preferably 0.05 and 0.2%, on a molar basis. An excess of acrolein leads to increased formation of high-boiling residues and is therefore not desirable. When the reaction is carried out, pressure is not a critical factor. It can vary within wide limits. However, since an excessive pressure, by compression of the catalyst bed, can reduce its activity, pressures above 10 bar should be avoided. Preferably, the reaction is to be carried out at atmospheric pressure. The reaction temperature, depending on pressure and reaction medium, can be selected between -20 and 100°C. At atmospheric pressure and with MMP as matrix, temperatures between 0 and 60°C are suitable, in particular temperatures between 30 and 50°C. Above these temperatures, the selectivity with respect to MMP formation falls, below 0°C, in contrast, the reaction velocity is too low to be able to bring economic advantages. In the case of batchwise production of MMP, in the reactor an initial content of MMP and reaction medium is charged. The catalyst is suspended in this reaction medium. It is necessary to allow the catalyst to swell in the reaction medium before the start of the reaction, that is to say at the first use, in order to enable the optimum accessibility of the active centres. Then the starting materials methylmercaptan and acrolein are introduced at the same time. The heat of reaction is removed by suitable internals or modifications. It is advantageous first to charge approximately 10% of the methylmercaptan and only then to continue with introducing acrolein and the remaining methylmercaptan. Methylmercaptan dissolves with reaction heat, forming a hemithioacetal in MMP. In this manner a continuous excess of methylmercaptan is ensured during the reaction. An excess of methylmercaptan leads to higher selectivities and thus to minimizing high-boiling by-products. In the event of a sufficient charge of MMP, it is possible to charge all of the methylmercaptan and not add acrolein until after. After the reaction is completed, the product is filtered off from the catalyst and if appropriate can be further purified. If the reaction product MMP is not soluble in the reaction medium, this MMP can be separated from the reaction medium by phase separation. The catalyst and the reaction medium can be reused in subsequent reactions without further swelling. When MMP is used as reaction medium, it is advantageous to discharge only a portion of the MMP formed and to retain a corresponding operating content together with the catalyst for following charges. If the crude MMP is to be reacted further to form MMP- cyanohydrin, this is successful simply by adding equimolar amounts of prussic acid to the reaction medium containing invented catalyst. In the batchwise production, for this the complete reaction of the acrolein with methylmercaptan must be completed. Purification of the crude MMP is not necessary. In continuous production, the prussic acid can be added at a point in the catalyst bed at which the conversion to the MMP is complete. A downstream reaction loop having a separate catalyst bed is also possible. To avoid unnecessary by-products, the reaction should be run with an excess of prussic acid. The molar excess of prussic acid based on MMP should be between 0.01 and 10%, preferably between 0.05 and 1%. The reaction temperature should be between 0 and 100°C, preferably between 20 and 70°C. Either liquefied or gaseous prussic acid can be used. Brief description of the ACCOMPANYING figures Figure 1 shows a diagrammatic structure of a continuous production of MMP using the inventive heterogeneous solid- phase catalyst in a fixed-bed reactor. Figure 2 shows a diagrammatic structure of continuous production of MMP using the inventive heterogeneous solid- phase catalyst in a fixed-bed reactor, extended for the reaction of MMP to form MMP-cyanohydrin with prussic acid metering and if appropriate a separate cyanohydrin reaction loop. In Figure 1 the central apparatus is a fixed-bed reactor having catalyst packing and circulation pump. On the circuit which also comprises a heat exchanger, metering devices for introducing methylmercaptan and acrolein and an ejection for taking off the resultant MMP reaction mixture are present. If the reaction medium is different from MMP, owing to the continuous ejection, a corresponding amount of the solvent taken off must be replenished into the reaction loop. Preferably, the methylmercaptan metering takes place upstream of the acrolein addition. This ensures an excess in time of methylmercaptan at the start of the reaction. Nevertheless, it can be advantageous, in contrast to the necessary stoichiometry, to add on average a slight excess of methylmercaptan. The excess can be between 0.01 and 1%. Higher amounts do not lead to further improvement in acrolein yield. The residence time of the reactants at the catalyst is determined via the catalyst volume and flow rate. Preferably, the ratio of acrolein mass to catalyst mass per hour (LHSV value, m/m.h) is between 0.1 and 100, preferably between 1 and 50, particularly preferably between 5 and 50. The mass ratio of reaction medium to acrolein should be between 1 and 20. The heat removal at the catalyst is controlled in such a manner that a temperature between 30 and 50°C is achieved. The reaction is operated at atmospheric pressure. Elevated pressures are possible, but do not have an effect on conversion rate. If the MMP produced is to be further reacted to form MMP- cyanohydrin, the structure is extended by prussic acid metering or if appropriate by a separate cyanohydrin reaction loop as shown in Figure 2. The inventive method has the advantage of not consuming catalyst or catalyst aid. This is cost-efficient and sustained. In addition, the reaction product MMP or MMP- cyanohydrin is not contaminated by catalysts or catalyst aids. This firstly facilitates the workup of the products and secondly minimizes unwanted side reactions in following stages which are caused by remainders of the catalysts. The present invention will be described in more detail hereinafter with reference to embodiment examples. These serve only to illustrate the invention and are in no way to be considered limiting in type and scope of these. Example 1 1.1 Synthesis of dimethylaminomethylpolystyrene resin 5 g (4.5 mmol) of Merrifield resin [CAS 55844-94-5] (0.9 mmol Cl/g), 6.9 g (50 mmol) of triethylamine and 2 00 ml of dimethylamine solution (4 00 mmol, 2 M in tetrahydrofuran, THF) are charged into a commercially conventional laboratory autoclave. The mixture is heated at 85°C for a period of 5 hours. After cooling and depressurising the mixture is filtered off by suction through a glass frit and the filter cake is washed first chloride-free with water, and then rewashed with 200 ml of THF. The resin dried at 60°C can, after swelling, be used directly in the following experiments. This produces 4.8 g of product which consists according to NMR of >90% of the dimethylbenzylamine-functionalized resin. In addition to unreacted benzyl chloride, benzyl alcohol is a minor functionality. 1.2 Batchwise synthesis of 3-(methylthio)propanal In a reaction flask having dropping funnel and gas introduction, 0.5 g of dimethylaminomethylpolystyrene resin (activity approximately 18 mmol/1 MMP) are dispersed in 25 ml of distilled pure MMP as charge. The resin is allowed to swell for 1 h. At 0°C, in the course of 10 min, 10 g (2 08 mmol) of methylmercaptan are then passed in, which immediately dissolves with formation of an MMP- hemimercaptal. After introduction is completed, 11.5 g (2 05 mmol) of acrolein are added dropwise and further stirred at 0°C. After two hours, the catalyst is filtered off and the MMP analyzed. This produces an acrolein conversion rate of 98% and a yield of 95%. The residue in the bottom phase on distillation of the crude MMP is 0.19%. The catalyst filtered off can be used directly in following experiments without further swelling. Use for ten times shows no loss of activity. 1.3 Batchwise synthesis of 2-hydroxy-4-(methylthio)- butanenitrile For the further reaction with prussic acid, the catalyst is not filtered off, but prussic acid (12.6 g, 46G mmol, 1.05 equivalent) is added dropwise to the MMP reaction mixture with cooling at approximately 35°C in the course of 30 min. After reaction is completed, the mixture is filtered off from the catalyst. This produces 62 g of MMP- cyanohydrin of a purity of >98%. The repeated reuse of the catalyst leads to no loss of activity. 1.4 Continuous synthesis of 3-(methylthio)propanal 4 mmol of dimethylaminomethylpolystyrene resin (equivalent to 4.4 g dry) previously swollen in MMP are packed into a reaction tube. The tubular reactor is connected into a circulation loop charged with pure MMP with a pump. The capacity in the loop is approximately 5 ml. A further pump permits the introduction of acrolein upstream of the reaction tube. In addition, a valve makes it possible to introduce liquid or gaseous methylmercaptan into the stream. An accompanying heat exchanger serves for heating the reaction loop to 50°C. To start the reaction 0.25 g of acrolein/min and 0.21 g of methylmercaptan/min are added. The volume fed to the reaction loop is removed at atmospheric pressure at a discharge point. The volumetric ratio of feed to circuit is 1/5. The reaction is in the steady state after approximately 30 min. Analysis of a representative crude MMP sample shows acrolein conversion rates > 99% and MMP purities of approximately 93%. The amount of MMP taken off from the reaction loop is reacted in a second reaction loop to give MMP-cyanohydrin. The set-up and procedure correspond to the above description for the reaction of acrolein with methylmercaptan. The amount of catalyst is 4 mmol, and the feed rate of HCN is 0.12 g/min. The volume fed to the reaction loop is taken off at atmospheric pressure at a discharge point. The volumetric ratio of feed to circuit is 1/5, and the temperature is maintained at 40°C. The reaction is in the steady state after approximately 3 0 min. Analysis of a representative MMP-cyanohydrin sample shows MMP conversion rates > 99% and purities of approximately 92%. Example 2 2.1 Synthesis of diethylaminomethylpolystyrene resin In a stirred flask having a reflux condenser, 30 g (27 mmol) of Merrifield resin [CAS 55844-94-5] (0.9 mmol Cl/g), 30.4 g (300 mmol) of triethylamine and 87.8 g (1.20 mol) of diethylamine are suspended in 420 ml of methyl isobutyl ketone. The mixture is kept at reflux for 6 hours. After it has cooled to room temperature it is filtered off by suction through a glass frit and the filtercake is washed chloride-free with water. The resin dried at 60°C can, after swelling, be used directly in following experiments. This produces 32 g of product of which, according to NMR, >90% consists of the diethylbenzylamino-functionalized resin. In addition to unreacted benzyl chloride, benzyl alcohol is a minor functionality. 2.2 Batchwise synthesis of 3-(methylthio)propanal Corresponding to the procedure of Example 1, 0.5 g of diethylaminomethylpolystyrene resin are reacted with acrolein and methylmercaptan. After 2 hours this produces an acrolein conversion rate of >99% and a yield of >96%. The residue in the bottom phase in distillation of the crude MMP is 0.15%. The further reaction to form MMP-cyanohydrin delivers this at conversion rates >99% at a purity of >95%. The catalyst filtered off can be used directly without further swelling in the following experiments. Use for ten times shows no loss of activity. 2.3 Continuous synthesis of 3-(methylthio)propanal Corresponding to the procedure from Example 1, 4.4 g (approximately 4 mmol) of diethylaminomethylpolystyrene resins are reacted with acrolein and methylmercaptan. Analysis of a representative crude MMP sample shows acrolein conversion rates > 99% and-MMP purities of approximately 94%, while analysis of a representative MMP- cyanohydrin sample after addition of prussic acid shows MMP conversion rates > 99% and purities of approximately 93%. Explanations to the figures: (1) Input of acrolein (2) Catalyst (3) Heat exchanger (4) Circulation pump (5) Discharge of MMP (6) Input of methylmercaptan (7) Input of prussic acid (8) Discharge of MMP-cyanohydrin We Claim: 1. Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein in the presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the heterogeneous catalyst is not soluble in the reaction medium which is a hydrocarbon, a halogenated hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio) butanenitrile, wherein the heterogeneous catalyst has the general formula where R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or heteroaryl; R1 can be different from R2; X is a number between 0 and 6; and A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C. 2. Method as claimed in claim 1, wherein A in the formula I is a polystyrene. 3. Method as claimed in claim 1, wherein the catalyst according to formula I is a polymer- bound base selected from the group consisting of the homologous dialkylaminoalkylpolystyrenes or dialkylaminomacroreticular resins. 4. Method as claimed in claim 3, wherein the catalyst according to formula I is diethylaminoethylpolystyrene, diethylaminomethylpolystyrene, dimethylaminomethylpolystyrene, diethylaminomethylmacroreticular resin or dimethylaminoethylpolystyrene. 5. Method as claimed in claim 1, wherein the reaction medium is 3-(methylthio) propanal. 6. Method as claimed in claim 1 wherein the temperature is between 0°C to 60°C. 7. Method as claimed in claim 1 or 6 wherein the temperature is between 30°C and 50°C. 8. Method as claimed in claim 1, wherein based on the active centres, the molar ratio of catalyst to acrolein is from 0.001 to 0.02. 9. Method as claimed in claim 8, wherein the molar ratio of catalyst to acrolein is from 0.001 to 0.01. 10. Method as claimed in claim 9, wherein the molar ratio of catalyst to acrolein is from 0.001 to 0.005. 11. Method as claimed in claim 1, wherein the molar excess of methylmercaptan based on acrolein is between 0.01 and 1%, preferably between 0.05 and 0.2%. 12. Method as claimed in claim 1, wherein the method is a batch method. 13. Method as claimed in claim 12 wherein the ratio of reaction medium to acrolein is between 0.1 and 2. 14. Method as claimed in claim 1, wherein the method is continuous. 15. Method as claimed in claim 14, wherein the ratio of flow rates by mass of reaction medium to acrolein is between 0.5 and 20. ABSTRACT Title: A METHOD FOR PREPARING 3-(METHYLTHIO) PROPANAL & 2-HYDROXY-4- (METHYLTHIO) BUTANENITRILE Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein in the presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the heterogeneous catalyst is not soluble in the reaction medium which is a hydrocarbon, a halogenated hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio) butanenitrile, wherein the heterogeneous catalyst has the general formula where R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or heteroaryl; R1 can be different from R2; X is a number between 0 and 6; and A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C.

Full Text

polystyrene, dimethylaminomethylpolystyrene,
diethylaminomethylmacroreticular resins, and especially
diethylaminomethylpolystyrene. The said bases are already
used in part in other fields of solid-phase chemistry
(WO 03/009936, US 4,440,676) and some are commercially
available. Furthermore, the synthesis of special
derivatives is possible in a simple manner from described
resins, e.g. Merrifield resin.
Since the catalysts are soluble neither in the reaction
product nor in one of the participating reaction partners,
use may be made of any desired amount of catalyst for the
reaction which leads to sufficient conversion rates and
selectivities. To facilitate the reaction procedure, i.e.
metering of the reaction partners, transport of the
starting materials to the active centres of the catalyst
and removal of the heat of reaction, a reaction medium
should be present in which the catalyst is readily
swellable. A resin is readily swellable in a solvent when
it can absorb the same as its own mass up to five times its
own mass of solvent. The resin increases its volume here
with absorption of the solvent. Preferably, MMP or MMP-
cyanohydrin itself can serve as matrix for the reaction.
However, use can also be made of all customary solvents in
which the reaction partners, but not the catalyst, are at
least partially soluble, e.g. hydrocarbons, halogenated
hydrocarbons or ethers. Reactive solvents such as water,
alcohols and ketones which, together with the starting
materials or the products, can form unwanted by-products
are less suitable and may be used only with restrictions.
Based on the active centres, in batch experiments for
synthesizing MMP, a molar ratio of catalyst to acrolein of
0.001 to 0.02, preferably 0.001 to 0.01, particularly
preferably 0.001 to 0.005 is suitable. In continuous
reactions in which the reaction partners and the reaction
medium flow continuously past the catalyst, the ratio of
acrolein mass to catalyst mass per hour (LHSV value, m/m-h)

is between 0.1 and 10 0, preferably between 1 and 50,
particularly preferably between 5 and 50.
The ratio of the reaction medium to acrolein is chosen in
batch experiments as between 0.1 and 2. In continuous
methods, the ratio of mass flow rate of reaction medium to
acrolein should be between 0.5 and 20. To achieve a good
conversion of the reactants and for achieving low
degradation, the amounts of the starting materials used are
controlled such that a slight excess of methylmercapan in
the reaction mixture is maintained. The excess should be
between 0.01 and 1%, preferably 0.05 and 0.2%, on a molar
basis. An excess of acrolein leads to increased formation
of high-boiling residues and is therefore not desirable.
When the reaction is carried out, pressure is not a
critical factor. It can vary within wide limits. However,
since an excessive pressure, by compression of the catalyst
bed, can reduce its activity, pressures above 10 bar should
be avoided. Preferably, the reaction is to be carried out
at atmospheric pressure.
The reaction temperature, depending on pressure and
reaction medium, can be selected between -20 and 100°C. At
atmospheric pressure and with MMP as matrix, temperatures
between 0 and 60°C are suitable, in particular temperatures
between 30 and 50°C. Above these temperatures, the
selectivity with respect to MMP formation falls, below 0°C,
in contrast, the reaction velocity is too low to be able to
bring economic advantages.
In the case of batchwise production of MMP, in the reactor an initial content of MMP and reaction medium is charged.
The catalyst is suspended in this reaction medium. It is
necessary to allow the catalyst to swell in the reaction
medium before the start of the reaction, that is to say at
the first use, in order to enable the optimum accessibility
of the active centres. Then the starting materials

methylmercaptan and acrolein are introduced at the same
time. The heat of reaction is removed by suitable internals
or modifications.
It is advantageous first to charge approximately 10% of the
methylmercaptan and only then to continue with introducing
acrolein and the remaining methylmercaptan. Methylmercaptan
dissolves with reaction heat, forming a hemithioacetal in
MMP. In this manner a continuous excess of methylmercaptan
is ensured during the reaction. An excess of
methylmercaptan leads to higher selectivities and thus to
minimizing high-boiling by-products. In the event of a
sufficient charge of MMP, it is possible to charge all of
the methylmercaptan and not add acrolein until after.
After the reaction is completed, the product is filtered
off from the catalyst and if appropriate can be further
purified. If the reaction product MMP is not soluble in the
reaction medium, this MMP can be separated from the
reaction medium by phase separation. The catalyst and the
reaction medium can be reused in subsequent reactions
without further swelling. When MMP is used as reaction
medium, it is advantageous to discharge only a portion of
the MMP formed and to retain a corresponding operating
content together with the catalyst for following charges.
If the crude MMP is to be reacted further to form MMP-
cyanohydrin, this is successful simply by adding equimolar
amounts of prussic acid to the reaction medium containing
invented catalyst. In the batchwise production, for this
the complete reaction of the acrolein with methylmercaptan
must be completed. Purification of the crude MMP is not
necessary.
In continuous production, the prussic acid can be added at
a point in the catalyst bed at which the conversion to the
MMP is complete. A downstream reaction loop having a
separate catalyst bed is also possible. To avoid

unnecessary by-products, the reaction should be run with an
excess of prussic acid. The molar excess of prussic acid
based on MMP should be between 0.01 and 10%, preferably
between 0.05 and 1%. The reaction temperature should be
between 0 and 100°C, preferably between 20 and 70°C. Either
liquefied or gaseous prussic acid can be used.
Brief description of the ACCOMPANYING figures
Figure 1 shows a diagrammatic structure of a continuous
production of MMP using the inventive heterogeneous solid-
phase catalyst in a fixed-bed reactor.
Figure 2 shows a diagrammatic structure of continuous
production of MMP using the inventive heterogeneous solid-
phase catalyst in a fixed-bed reactor, extended for the
reaction of MMP to form MMP-cyanohydrin with prussic acid
metering and if appropriate a separate cyanohydrin reaction
loop.
In Figure 1 the central apparatus is a fixed-bed reactor
having catalyst packing and circulation pump. On the
circuit which also comprises a heat exchanger, metering
devices for introducing methylmercaptan and acrolein and an
ejection for taking off the resultant MMP reaction mixture
are present. If the reaction medium is different from MMP,
owing to the continuous ejection, a corresponding amount of
the solvent taken off must be replenished into the reaction
loop. Preferably, the methylmercaptan metering takes place
upstream of the acrolein addition. This ensures an excess
in time of methylmercaptan at the start of the reaction.
Nevertheless, it can be advantageous, in contrast to the
necessary stoichiometry, to add on average a slight excess
of methylmercaptan. The excess can be between 0.01 and 1%.
Higher amounts do not lead to further improvement in
acrolein yield.
The residence time of the reactants at the catalyst is
determined via the catalyst volume and flow rate.

Preferably, the ratio of acrolein mass to catalyst mass per
hour (LHSV value, m/m.h) is between 0.1 and 100, preferably
between 1 and 50, particularly preferably between 5 and 50.
The mass ratio of reaction medium to acrolein should be
between 1 and 20. The heat removal at the catalyst is
controlled in such a manner that a temperature between 30
and 50°C is achieved. The reaction is operated at
atmospheric pressure. Elevated pressures are possible, but
do not have an effect on conversion rate.
If the MMP produced is to be further reacted to form MMP-
cyanohydrin, the structure is extended by prussic acid
metering or if appropriate by a separate cyanohydrin
reaction loop as shown in Figure 2.
The inventive method has the advantage of not consuming
catalyst or catalyst aid. This is cost-efficient and
sustained. In addition, the reaction product MMP or MMP-
cyanohydrin is not contaminated by catalysts or catalyst
aids. This firstly facilitates the workup of the products
and secondly minimizes unwanted side reactions in following
stages which are caused by remainders of the catalysts.
The present invention will be described in more detail
hereinafter with reference to embodiment examples. These
serve only to illustrate the invention and are in no way to
be considered limiting in type and scope of these.
Example 1
1.1 Synthesis of dimethylaminomethylpolystyrene resin
5 g (4.5 mmol) of Merrifield resin [CAS 55844-94-5]
(0.9 mmol Cl/g), 6.9 g (50 mmol) of triethylamine and
2 00 ml of dimethylamine solution (4 00 mmol, 2 M in
tetrahydrofuran, THF) are charged into a commercially
conventional laboratory autoclave. The mixture is heated at
85°C for a period of 5 hours.

After cooling and depressurising the mixture is filtered
off by suction through a glass frit and the filter cake is
washed first chloride-free with water, and then rewashed
with 200 ml of THF. The resin dried at 60°C can, after
swelling, be used directly in the following experiments.
This produces 4.8 g of product which consists according to
NMR of >90% of the dimethylbenzylamine-functionalized
resin. In addition to unreacted benzyl chloride, benzyl
alcohol is a minor functionality.
1.2 Batchwise synthesis of 3-(methylthio)propanal
In a reaction flask having dropping funnel and gas
introduction, 0.5 g of dimethylaminomethylpolystyrene resin
(activity approximately 18 mmol/1 MMP) are dispersed in
25 ml of distilled pure MMP as charge. The resin is allowed
to swell for 1 h. At 0°C, in the course of 10 min, 10 g
(2 08 mmol) of methylmercaptan are then passed in, which
immediately dissolves with formation of an MMP-
hemimercaptal. After introduction is completed, 11.5 g
(2 05 mmol) of acrolein are added dropwise and further
stirred at 0°C. After two hours, the catalyst is filtered
off and the MMP analyzed. This produces an acrolein
conversion rate of 98% and a yield of 95%. The residue in
the bottom phase on distillation of the crude MMP is 0.19%.
The catalyst filtered off can be used directly in following
experiments without further swelling. Use for ten times
shows no loss of activity.
1.3 Batchwise synthesis of 2-hydroxy-4-(methylthio)-
butanenitrile
For the further reaction with prussic acid, the catalyst is
not filtered off, but prussic acid (12.6 g, 46G mmol,
1.05 equivalent) is added dropwise to the MMP reaction
mixture with cooling at approximately 35°C in the course of
30 min. After reaction is completed, the mixture is
filtered off from the catalyst. This produces 62 g of MMP-

cyanohydrin of a purity of >98%. The repeated reuse of the
catalyst leads to no loss of activity.
1.4 Continuous synthesis of 3-(methylthio)propanal
4 mmol of dimethylaminomethylpolystyrene resin (equivalent
to 4.4 g dry) previously swollen in MMP are packed into a
reaction tube. The tubular reactor is connected into a
circulation loop charged with pure MMP with a pump. The
capacity in the loop is approximately 5 ml. A further pump
permits the introduction of acrolein upstream of the
reaction tube. In addition, a valve makes it possible to
introduce liquid or gaseous methylmercaptan into the
stream. An accompanying heat exchanger serves for heating
the reaction loop to 50°C. To start the reaction 0.25 g of
acrolein/min and 0.21 g of methylmercaptan/min are added.
The volume fed to the reaction loop is removed at
atmospheric pressure at a discharge point. The volumetric
ratio of feed to circuit is 1/5. The reaction is in the
steady state after approximately 30 min. Analysis of a
representative crude MMP sample shows acrolein conversion
rates > 99% and MMP purities of approximately 93%.
The amount of MMP taken off from the reaction loop is
reacted in a second reaction loop to give MMP-cyanohydrin.
The set-up and procedure correspond to the above
description for the reaction of acrolein with
methylmercaptan. The amount of catalyst is 4 mmol, and the
feed rate of HCN is 0.12 g/min. The volume fed to the
reaction loop is taken off at atmospheric pressure at a
discharge point. The volumetric ratio of feed to circuit is
1/5, and the temperature is maintained at 40°C. The
reaction is in the steady state after approximately 3 0 min.
Analysis of a representative MMP-cyanohydrin sample shows
MMP conversion rates > 99% and purities of approximately
92%.

Example 2
2.1 Synthesis of diethylaminomethylpolystyrene resin
In a stirred flask having a reflux condenser, 30 g
(27 mmol) of Merrifield resin [CAS 55844-94-5] (0.9 mmol
Cl/g), 30.4 g (300 mmol) of triethylamine and 87.8 g
(1.20 mol) of diethylamine are suspended in 420 ml of
methyl isobutyl ketone. The mixture is kept at reflux for
6 hours. After it has cooled to room temperature it is
filtered off by suction through a glass frit and the
filtercake is washed chloride-free with water. The resin
dried at 60°C can, after swelling, be used directly in
following experiments. This produces 32 g of product of
which, according to NMR, >90% consists of the
diethylbenzylamino-functionalized resin. In addition to
unreacted benzyl chloride, benzyl alcohol is a minor
functionality.
2.2 Batchwise synthesis of 3-(methylthio)propanal
Corresponding to the procedure of Example 1, 0.5 g of
diethylaminomethylpolystyrene resin are reacted with
acrolein and methylmercaptan.
After 2 hours this produces an acrolein conversion rate of
>99% and a yield of >96%. The residue in the bottom phase
in distillation of the crude MMP is 0.15%.
The further reaction to form MMP-cyanohydrin delivers this
at conversion rates >99% at a purity of >95%.
The catalyst filtered off can be used directly without
further swelling in the following experiments. Use for ten
times shows no loss of activity.

2.3 Continuous synthesis of 3-(methylthio)propanal
Corresponding to the procedure from Example 1, 4.4 g
(approximately 4 mmol) of diethylaminomethylpolystyrene
resins are reacted with acrolein and methylmercaptan.
Analysis of a representative crude MMP sample shows
acrolein conversion rates > 99% and-MMP purities of
approximately 94%, while analysis of a representative MMP-
cyanohydrin sample after addition of prussic acid shows MMP
conversion rates > 99% and purities of approximately 93%.

Explanations to the figures:
(1) Input of acrolein
(2) Catalyst
(3) Heat exchanger
(4) Circulation pump
(5) Discharge of MMP
(6) Input of methylmercaptan
(7) Input of prussic acid
(8) Discharge of MMP-cyanohydrin

We Claim:
1. Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein
in the presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the
heterogeneous catalyst is not soluble in the reaction medium which is a hydrocarbon, a
halogenated hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio)
butanenitrile, wherein the heterogeneous catalyst has the general formula
where
R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or
heteroaryl;
R1 can be different from R2;
X is a number between 0 and 6; and
A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C.
2. Method as claimed in claim 1, wherein A in the formula I is a polystyrene.

3. Method as claimed in claim 1, wherein the catalyst according to formula I is a polymer-
bound base selected from the group consisting of the homologous
dialkylaminoalkylpolystyrenes or dialkylaminomacroreticular resins.
4. Method as claimed in claim 3, wherein the catalyst according to formula I is
diethylaminoethylpolystyrene, diethylaminomethylpolystyrene,
dimethylaminomethylpolystyrene, diethylaminomethylmacroreticular resin or
dimethylaminoethylpolystyrene.
5. Method as claimed in claim 1, wherein the reaction medium is 3-(methylthio) propanal.
6. Method as claimed in claim 1 wherein the temperature is between 0°C to 60°C.
7. Method as claimed in claim 1 or 6 wherein the temperature is between 30°C and 50°C.
8. Method as claimed in claim 1, wherein based on the active centres, the molar ratio of
catalyst to acrolein is from 0.001 to 0.02.
9. Method as claimed in claim 8, wherein the molar ratio of catalyst to acrolein is from
0.001 to 0.01.

10. Method as claimed in claim 9, wherein the molar ratio of catalyst to acrolein is from
0.001 to 0.005.
11. Method as claimed in claim 1, wherein the molar excess of methylmercaptan based on
acrolein is between 0.01 and 1%, preferably between 0.05 and 0.2%.
12. Method as claimed in claim 1, wherein the method is a batch method.
13. Method as claimed in claim 12 wherein the ratio of reaction medium to acrolein is
between 0.1 and 2.
14. Method as claimed in claim 1, wherein the method is continuous.
15. Method as claimed in claim 14, wherein the ratio of flow rates by mass of reaction
medium to acrolein is between 0.5 and 20.

ABSTRACT

Title: A METHOD FOR PREPARING 3-(METHYLTHIO) PROPANAL & 2-HYDROXY-4-
(METHYLTHIO) BUTANENITRILE
Method for preparing 3-(methylthio) propanal by addition of methylmercaptan to acrolein in the
presence of a) a heterogeneous catalyst, and b) a reaction medium, wherein the heterogeneous
catalyst is not soluble in the reaction medium which is a hydrocarbon, a halogenated
hydrocarbon, an ether, 3-(methylthio) propanal or 2-hydroxy-4-(methylthio) butanenitrile,
wherein the heterogeneous catalyst has the general formula

where
R1 and R2 are hydrogen, alkyl having chain lengths between C1 and C12, aryl or heteroaryl;
R1 can be different from R2;
X is a number between 0 and 6; and
A is a natural or synthetic resin and it is carried out at temperatures of -20°C to 100°C.

A METHOD FOR PREPARING 3-(METHYLTHIO) PROPANAL & 2-HYDROXY-4-(METHYLTHIO) BUTANENITRILE

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