Process for preparing alpha-methyl monobasic acid and esters thereof

Alkanoic acids containing largely the alpha-methyl isomers thereof, and/or the corresponding esters, are prepared by reacting an alpha-olefin, carbon monoxide and water and/or a monoalkanol in the presence of a catalytically effective amount of a catalyst composition comprising (i) a zero-valent Group VIII metal or metal alloy in which the Group VIII metal is the major component by weight thereof, (ii) an aryl ligand selected from the group consisting of arylarsine, arylstibine and arylbismuthine and (iii) a Lewis acid and/or hydrochloric acid.

BACKGROUND OF THE INVENTION 
1. Field of the Invention 
The present invention relates to the field of processes for the preparation 
of alkanoic acids and alkanoic acid esters and, more particularly, to the 
preparation of such acids and esters from the catalyzed reaction of 
olefin, carbon monoxide and water and/or alkanol (a type of carbonylation 
reaction). 
2. Description of the Prior Art 
It is known from U.S. Pat. No. 3,952,034 to react an olefin or acetylene, 
carbon monoxide and water or alkanol in the presence of a soluble, i.e., 
homogeneous, catalyst system containing a polynuclear complex of palladium 
and iron or metal of Groups IVA, VA or IIIB, or a mixture of a soluble 
palladium salt and metal halide, to provide a carboxylic acid or ester. A 
similar reaction is described in German Patent No. 27 39 096 which also 
employs a soluble palladium compound or complex in combination with an 
aryl arsine as catalyst. Still other soluble palladium-containing 
catalysts for the aforedescribed carbonylation reaction are disclosed in 
U.S. Pat. Nos. 3,641,074; 3,816,490; 3,859;319; 3,919,272; 3,892,788; 
3,917,677; 3,965,132; 3,968,133; and 3,987,089. While U.S. Pat. No. 
3,887,595 describes the use of zero-valent palladium metal as a component 
of the carbonylation catalyst system, the result of the reaction is to 
provide a high ratio of straight-chain to branch-chain carboxylic acids 
and esters. For some important industrial applications, for example, 
monomer precursors or lubricants, it is highly desirable to provide a 
reaction product which is exclusively made up of branched product or a 
product in which the branched product at least predominates. Although some 
of the fully soluble catalyst systems heretofore known in the 
carbonylation of alkenes and alkynes may be effective for providing 
relatively high ratios of branched carboxylic acids and esters in relation 
to the quantities of straight-chain product produced, nevertheless they 
are at an operational disadvantage compared to the insoluble, i.e., 
heterogenous, catalyst systems since the solubility of the former 
complicates product separation and recovery procedures. 
Accordingly, there has heretofore existed a need for an effective 
heterogenous catalyst system for the reaction of olefin, carbon monoxide 
and water and/or alkanol to provide predominantly alpha-methyl 
monoalkanoic acid and/or ester. 
SUMMARY OF THE INVENTION 
It has now been discovered that alpha-olefin of from 3 to 8 carbon atoms, 
carbon monoxide and water and/or monoalkanol can be reacted to provide 
predominantly alpha-methyl monoalkanoic acids of from 4 to 9 carbon atoms 
and/or the esters thereof by employing as catalyst, a catalytically 
effective amount of (i) at least one zero-valent Group VIII metal and/or 
metal alloy, (ii) at least one aryl ligand selected from the group 
consisting of arylarsine, arylstibine and arylbismuthine and (iii) a Lewis 
acid and/or hydrochloric acid. 
Use of the foregoing catalyst system which is heterogeneous in its Group 
VIII metal or metal alloy component greatly facilitates separation of such 
component from the liquid reaction product(s) leading to an overall 
simplification of the carbonylation process. 
DESCRIPTION OF THE PREFERRED EMBODIMENTS 
The alpha-olefins which are useful in the process of this invention contain 
from 3 to 8 carbon atoms and include propylene, 1-butene, 1-pentene, 
1-hexene, 1-heptene, 1-octene, 3-methyl-1-pentene, 4-methyl-1-pentene, 
4,4-dimethyl-1-pentene, and the like. 
When the desired carbonylation product is to be a branched carboxylic acid, 
water is employed as a reactant. The use of a monoalkanol reactant under 
the same conditions will provide a branched carboxylic acid monoester and 
aqueous monoalkanol will, of course, provide a mixture of acid and ester. 
The preferred monoalkanols are the monoalkanols of from 1 to 20 carbon 
atoms such as methanol, ethanol, propanol, butanol, isobutanol, decanol, 
dodecanol, and the like. 
The catalyst composition of the present invention comprises, as a first 
component, at least one zero-valent Group VIII metal which can be 
ruthenium, rhodium, palladium, osmium, iridium or platinum, alone or 
alloyed with one or more other Group VIII metals and/or minor amounts by 
weight of one or more other metals such as iron, cobalt, copper, gold, 
etc. Palladium metal is preferred for its high catalytic activity. It is 
further preferred to employ the metal and/or metal alloy in supported 
form, i.e., applied to an inert particulate carrier such as silica, silica 
xerogel, alumina, titania, zirconia, carbon, diatomaceous earth, etc., as 
is widely practiced in the art. 
The second component of the catalyst compositions of this invention is an 
aryl ligand selected from the arylarsines, arylstibines and 
arylbismuthines in which the aryl moiety can be chosen from such 
unsubstituted and substituted aromatic groups as phenyl, tolyl, xylyl, 
para-ethylphenyl, para-tertbutylphenyl, m-octylphenyl, 2,4-diethylphenyl, 
para phenylphenyl, meta-benzylphenyl, 2,4,6-trimethylphenyl, 
para-methoxyphenyl, meta-chlorophenyl, meta-trifluoromethylphenyl, 
para-propoxyphenyl, para-carbethoxyphenyl, and so forth. Triphenylarsine 
provides particularly good results and as it is readily commercially 
available, is preferred for use herein. 
The third component of the instant catalyst compositions is an acid which 
may be a Lewis acid such as aluminum chloride which is preferred, ferric 
chloride or chromic chloride and/or the Bronsted acid hydrochloric acid. 
The quantities of zero-valent Group VIII metal employed in the catalyst 
compositions herein can vary over wide limits, for example, from about 
0.00001 to about 1.0 mole percent of such metal per mole of alpha-olefin 
provides entirely acceptable results with from 0.0001 to about 0.1 mole 
percent being preferred. Similarly, the amounts of aryl ligand (provided 
it is in large molar excess compared to Group VIII metal) and Lewis acid 
and/or hydrochloric acid can also vary widely. Thus, a molar ratio of aryl 
ligand to Group VIII metal of from about 5:1 to about 100:1, and 
preferably from about 10:1 to about 20:1, and a molar ratio of Lewis acid 
and/or hydrochloric acid to Group VIII metal of from about 1:1 to about 
30:1, and preferably from about 1:1 to about 20:1, generally provides good 
results. 
The reaction of alpha-olefin, carbon monoxide, water and/or monoalkanol can 
be carried out batch-wise with agitation in an autoclave or similar 
pressure vessel or continuously in a tubular reactor. Although 
carbonylation consumes one mole of carbon monoxide for each mole of 
alpha-olefin, it is preferred to employ an excess of carbon monoxide 
relative to olefin, e.g., from about 2:1 to about 100:1 excess. Similarly, 
while the carbonylation reaction consumes one mole of water or monoalkanol 
per mole of olefin, it is also preferred to use a large excess of this 
reactant compared to olefin, e.g., from about 2:1 to about 20:1, to insure 
an efficient reaction. Operating temperatures and pressures are not 
critical and can be selected from over a wide range. Thus, temperatures on 
the order of from about 50.degree. C. to about 300.degree. C., and 
preferably from about 100.degree. C. to about 200.degree. C., are entirely 
satisfactory. Partial pressures of carbon monoxide of from about 300 psig 
to about 3,000 psig, preferably from about 500 psig to 2,000 psig, 
generally provides good results. The time of the reaction can vary from a 
few minutes to twelve hours or more with substantial conversions of 
alpha-olefin usually being achieved within 2 to 8 hours. While the use of 
a solvent is not required, it may be convenient or desirable to employ a 
liquid solvent or diluent which is inert under the reaction conditions 
such as the saturated or aromatic hydrocarbons, for example, pentane, 
cyclohexane, gasoline hydrocarbons, benzene, toluene, and the like, 
ketones, amides, ethers, esters, and so forth. Whenever a solvent is 
employed, the amount is not critical and can therefore vary widely. 
Amounts of solvent of from about 10% to about 500% by weight of the total 
reactants are usually satisfactory. 
Recovery of the carboxylic acids and/or ester products can be accomplished 
by known and conventional means such as distillation, solvent extraction, 
and the like.

EXAMPLE 1 
The following charge, designated Charge A, was placed in a 71 ml Parr 
Hastelloy C reactor: 16.6 ml (0.41 moles) methanol, 0.681 g (0.0187 moles) 
anhydrous HCl, 5 g (0.119 moles) propylene and 0.620 g (0.00203 moles) 
triphenylarsine. The catalyst charge was 0.5 g 5% palladium metal 
dispersed on carbon powder (2.35.times.10.sup.-4 g atom Pd.sup.0). The 
following procedure, designated Procedure B, was used to charge CO, carry 
out the reaction, and work up the reaction mixture: The reactor cover, 
having a valved port at its top was placed on the reactor and fastened. 
Carbon monoxide at 3000 psig and ambient temperature (about 25.degree. C.) 
was introduced into the vessel through the valve, after which the valve 
was closed, the reactor placed in a shaker in a heated constant 
temperature oven at 100.degree. C. and shaken six hours. After reaction, 
the reactor was cooled to ambient temperature, vented, then opened. The 
clear liquid was separated from the solid catalyst by decantation. Gas 
chromatographic analysis showed combined selectivity of methyl isobutyrate 
and methyl butyrate to be 98.4% and the mole ratio of methyl isobutyrate 
to methyl n-butyrate to be 5.56. Substantial yields of these esters were 
obtained. 
EXAMPLE 2 
A 71 ml Parr Hastelloy C reactor was charged with 0.614 g of the solid 
catalyst residue from Example 1 and charge A. After employing Procedure B, 
the liquid reaction mixture was analyzed as in Example 1. Substantial 
concentrations of methyl isobutyrate and methyl n-butyrate in a ratio of 
branched to straight chain esters of 5.7:1 were found. The selectivity of 
butyrate esters was 99.3%. 
EXAMPLE 3 
A 71 ml Parr Hastelloy C reactor was charged with 0.573 g of the solid 
catalyst residue recovered from Example 2 and Charge A. After employing 
Procedure B, the liquid reaction mixture was analyzed as in Example 1. 
Substantial concentrations of methyl isobutyrate and methyl n-butyrate in 
a ratio of branched to straight chain esters of 4.1:1 were found. The 
selectivity of butyrate esters was 98.7%. 
EXAMPLE 4 
The importance of using high mole ratios of aryl ligand compared to Group 
VIII metal (such as the 8.7 ratio used in Charge A) is demonstrated in 
this example by omitting added triphenylarsine from the charge and 
employing only that amount of triphenylarsine present in the previously 
recovered catalyst. 
A 71 ml Parr Hastelloy C reactor was charged with the solid catalyst 
residue from Example 3, and Charge A (omitting added triphenylarsine from 
the charge). After employing Procedure B and analyzing the liquid product, 
it was found that although some methyl isobutyrate and methyl n-butyrate 
were formed in a ratio of branched to unbranched esters of 4.3, the yield 
of esters was much lower than in any of the previous examples, amounting 
to only 7.6% of that formed in Example 3. The selectivity to butyrate 
esters was 94.5%. 
EXAMPLE 5 
Charge B, which is equivalent to Charge A except that 0.43 g (0.0032 moles) 
of AlCl.sub.3 were used instead of 0.681 g (0.0177 moles) of anhydrous 
HCl, was placed in a 71 ml Parr Hastelloy C reactor together with 0.5 g 5% 
Pd metal dispersed on carbon powder (2.35.times.10.sup.-4 g atom 
Pd.sup.0). Following Procedure B, the liquid product was found by 
chromatographic analysis to contain substantial concentrations of methyl 
isobutyrate and methyl n-butyrate in a ratio of branched to straight chain 
esters of 5.7 to 1, and a selectivity to butyrate ester of 99.1%. 
EXAMPLE 6 
A 71 ml Parr Hastelloy C reactor was charged with the solid catalyst 
residue from Example 5 and with Charge B. After following Procedure B, the 
liquid product was found by chromatographic analysis to contain 
substantial concentrations of methyl isobutyrate and methyl n-butyrate in 
a ratio of branched to straight chain esters of 4.3 to 1, and a 
selectivity to butyrate esters of 98.6%. 
EXAMPLE 7 
The following example shows that high mole ratios of triphenylarsine to 
Group VIII metal, e.g., at least about 5:1, are needed to obtain good 
yields of butyrate esters and high ratios of isobutyrate to n-butyrate 
esters. 
A 71 ml Parr Hastelloy C reactor was charged with 0.5 g 5% palladium metal 
dispersed on carbon catalyst (2.35.times.10.sup.-4 g atoms Pd metal) and 
Charge A with the exception that the triphenylarsine product was omitted. 
Following Procedure B, the liquid product was analyzed by gas 
chromatography. The yield of butyrate esters was very low, amounting to 
only 12.6% of that obtained in Example 1 where triphenylarsine was 
included. The mole ratio of branched to straight chain esters was only 2.8 
and selectivity of butyrate esters was 95.5%. 
EXAMPLE 8 
A 71 ml Parr Hastelloy C reactor was charged with 2 g of a palladium-gold 
alloy on silica carrier 1/8" extrudate containing 1.3% Pd metal and 0.6% 
gold metal corresponding to 2.44.times.10.sup.-4 g atoms palladium, and 
Charge C which is equivalent to Charge A except that 0.8 g anhydrous HCl 
was used instead of 0.681 g. Following Procedure B, the liquid product was 
analyzed and found to contain substantial concentrations of methyl 
isobutyrate and methyl n-butyrate with a mole ratio of branched chain 
ester to straight chain ester of 8.3. The selectivity of butyrate esters 
was 99.7%. 
EXAMPLE 9 
A 71 ml Hastelloy C Parr reactor was charged with the solid catalyst 
recovered from Example 8 and Charge C. After employing Procedure B, the 
liquid product was found to contain substantial concentrations of methyl 
butyrate esters with selectivity to butyrate esters of 99.9% and a mole 
ratio of methyl isobutyrate to methyl n-butyrate of 5.6 to 1.0. 
EXAMPLE 10 
A 71 ml Hastelloy C Parr reactor was charged with Charge C and a palladium 
metal catalyst consisting of 0.5 g of 5% Pd metal on ground alumina. After 
employing Procedure B, the liquid product was found to contain substantial 
concentrations of butyrate esters with selectivity of 99.4% and a mole 
ratio of methyl isobutyrate to methyl n-butyrate of 10.7 to 1. 
EXAMPLE 11 
A 71 ml Hastelloy C Parr reactor was charged with the solid catalyst from 
Example 10 and Charge C. After employing Procedure B, the liquid product 
was found to contain substantial concentrations of methyl butyrate esters 
with a selectivity of 99.6% and a mole ratio of methyl isobutyrate to 
methyl n-butyrate of 6.7 to 1. 
EXAMPLE 12 
A 71 ml Hastelloy C Parr reactor was charged with the solid catalyst from 
Example 11 and Charge C. After employing Procedure B, the liquid product 
was found to contain substantial concentrations of methyl butyrate esters 
with a selectivity of 99.7% and a mole ratio of methyl isobutyrate to 
methyl n-butyrate of 9.49 to 1. 
EXAMPLE 13 
A 71 ml Parr Hastelloy C reactor was charged with 1.0 g of 2% Pd metal 
dispersed on alpha-alumina pellets and Charge C. After employing Procedure 
B, the liquid product was found to contain substantial concentrations of 
methyl butyrate esters with a selectivity of 96.2% and a mole ratio of 
methyl isobutyrate to methyl n-butyrate of 6.3. 
EXAMPLE 14 
A 71 ml Parr Hastelloy C reactor was charged with the solid catalyst 
residue from Example 13 and Charge C. After employing Procedure B, the 
liquid product was found to contain substantial concentrations of methyl 
butyrate esters with a selectivity of 99.5% and a mole ratio of methyl 
isobutyrate to methyl n-butyrate of 7.7. 
EXAMPLE 15 
A 71 ml Parr Hastelloy C reactor was charged with the solid catalyst 
residue from Example 14 and Charge C. After employing Procedure B, the 
liquid product was found to contain substantial concentrations of methyl 
butyrate esters with a selectivity of 99.3% and a mole ratio of methyl 
isobutyrate to methyl n-butyrate of 6.2. 
EXAMPLE 16 
One of two 71 ml Parr Hastelloy C reactors (reactor X) was charged with 
Charge C, and 0.5 g of 5% Pd metal on alpha-alumina. The other reactor 
(reactor Y) was also charged with Charge C except that the 0.620 g of 
triphenylarsine was omitted. Added also were 0.186 g of 
dichlorobistriphenylarsine palladium (II) prepared by adding a solution of 
triphenylarsine in ethanol to an acidified aqueous solution of palladium 
dichloride salt. The gram atoms of palladium (2.35.times.10.sup.-4 g atoms 
Pd) was equivalent in the two reactors. However, reactor Y contained only 
4.71.times.10.sup.-4 moles of triphenylarsine while reactor X contained 
20.26.times.10.sup.-4 moles. After following Procedure B, the liquid 
products from the two reactors were analyzed. The selectivity of methyl 
butyrate esters was 99.9% for reactor X and 99.1% for reactor Y. The mole 
ratio of methyl isobutyrate to methyl n-butyrate was 9.56 for reactor X 
and 5.39 for reactor Y. The area percent on the chromatogram for methyl 
isobutyrate and for methyl n-butyrate were 39.98 % and 4.18% for reactor X 
but only 7.45% and 1.38% for reactor Y showing a much higher yield was 
obtained in reactor X than in reactor Y. 
EXAMPLE 17 
In this example, the product esters are distilled from the catalyst system 
(the residue) comprising supported palladium metal and triphenyl arsine, 
and the catalyst system reused. 
A 71 ml Hastelloy C Parr reactor was charged with Charge D consisting of 5 
g propylene, 16.6 ml of methanol containing 0.8 g HCL, 0.620 g triphenyl 
arsine and 0.5 g of 5% Pd metal on ground alpha-alumina. Procedure B was 
followed up to the point where the reactor was opened. At this point the 
reactor contents were analyzed by gas-liquid chromatography, then 
transferred to a rotoevaporator and the methyl butyrates, methanol and HCl 
removed by distillation. The residue including the palladium and 
triphenylarsine were returned to the reactor for reuse. The 
chromatographic analysis showed substantial concentrations of methyl 
butyrates to be present with 99.9% selectivity and a ratio of methyl 
isobutyrate to methyl n-butyrate of 5.9. 
The reactor containing the supported Pd metal and triphenylarsine portion 
of the used catalyst system was recharged with 5 g. propylene and 16.6 ml. 
methanol containing 0.8 g HCL and Procedure B again followed up to the 
point where the reactor was opened. The reactor contents were analyzed by 
gas-liquid chromatography, then transferred to the roto-evaporator and 
product esters, methanol and HCl removed by distillation after which the 
residue comprising a catalyst system (including palladium metal and 
triphenylarsine) was transferred to the reactor for a further reuse. 
Analysis of the reaction mixture showed substantial concentrations of 
methyl butyrates to be present with a selectivity of 99.8% and a mole 
ratio of methyl isobutyrate to methyl n-butyrate of 8.9. 
In a third use of the catalyst system carried out in the same manner as 
outlined above, the gas-liquid chromotographic analysis also showed 
substantial concentrations of methyl butyrate to be present with 
selectivity of 99.6% and mole ratio of methyl isobutyrate to methyl 
n-butyrate of 7.0. There were no significant losses of palladium or 
triphenylarsine in the above operations. 
EXAMPLE 18 
This example shows that by including methyl n-butyrate in the charge, an 
improvement can be effected in the mole ratio of methyl isobutyrate to 
methyl n-butyrate synthesized from propylene, methanol, and carbon 
monoxide using a supported Pd metal and triphenylarsine as catalyst. 
A 71 ml Hastelloy C Parr reactor was charged with 5 g. propylene, 13.6 ml 
methanol containing 0.8 g HCl, 3.0 ml methyl n-butyrate 
(26.4.times.10.sup.-3 moles), 0.620 g triphenylarsine and 0.5 g of 5% Pd 
on ground alpha-alumina. 
After following Procedure B, analysis of the liquid product showed 
substantial concentrations of methyl butyrates to be present with a 
selectivity of 99.9% with a calculated mole ratio of synthesized methyl 
isobutyrate to methyl n-butyrate of 16.4 to 1. The calculation took into 
account an analysis prior to carbonylation and a volume increase after 
carbonylation. 
EXAMPLE 19 
A 71 ml Hastelloy C Parr reactor was charged with 5 ml (319.times.10.sup.-4 
moles) octene-1, 0.4 g AlCl.sub.3, 15 ml (0.371 moles) methanol, 0.620 g 
(20.3.times.10.sup.-4 moles) triphenylarsine and 2.0 g 1.3% Pd/0.6% Au 
alloy on silica (corresponding to 2.44.times.10.sup.-4 g atom of Pd). The 
reactor was closed, pressurized to 3000 psi at ambient temperature with 
CO, and heated to 1000.degree. C. and shaken six hours. The final pressure 
at 100.degree. C. was 3,900 psig. 
After reaction, the reactor was cooled, opened and liquid contents 
analyzed. The analysis showed substantial concentrations of methyl 
2-methyloctanoate and methyl n-nonanoate in a mole ratio of branched to 
unbranched ester of 2.5 to 1. The conversion was 51% and selectivity to 
the above esters was above 99%. 
EXAMPLE 20 
A stirred pressure vessel at 3,000 psig partial CO pressure and at 
100.degree. C. is charged continuously at a selected rate with a slurry 
from a feed mixing tank containing aluminum chloride, methanol, 
triphenylarsine, methyl n-butyrate and a solid catalyst powder comprising 
5% palladium metal on ground alpha-alumina in corresponding mole ratios of 
0.32:41:0.203:1.4:0.0234, respectively. Propylene is also charged to the 
vessel from a propylene storage tank at a mole ratio to methanol of 
11.9:41. CO is added continuously on demand to maintain the pressure 3,000 
psig. 
Part of the liquid reaction slurry is continuously removed from the vessel 
through a valve into a flash drum at a rate approximating the feed rate 
but maintaining the reaction volume constant. Pressure is let down to 
atmospheric in the flash drum and dissolved gases are flashed off. These 
gases are comprised principally of unreacted propylene and carbon monoxide 
and are led to a compressor where they are continuously recompressed to 
3,000 psig and recycled to the reactor. 
The liquid reaction slurry is led to a centrifuge where solid catalyst 
residues are separated continuously and sent to a stirred catalyst slurry 
tank. The supernatant liquid reaction mixture is fed continuously to a 
continuous methanol still. 
Methanol is separated as overhead in the still and sent to methanol 
storage. The still bottoms are pumped to a continuous methyl isobutyrate 
still where methyl isobutyrate is separated as overhead and sent to methyl 
isobutyrate product storage. These still bottoms are then pumped to a 
continuous methyl n-butyrate still where methyl n-butyrate corresponding 
to the amount synthesized is sent to methyl n-butyrate storage, the 
remainder is recycled with the still bottoms (after removing a small 
purge) to the stirred catalyst slurry tank from which, together with solid 
catalyst residues, it is sent to the feed mixing tank. 
The feed mixing tank is initially charged with aluminum chloride, methanol, 
catalyst and triphenylarsine in the ratios set forth above. Under steady 
state conditions, however, only make-up quantities of these reagents need 
be added to replace material removed from the system by the purge and 
by-product separation. 
EXAMPLE 21 
Example 5 was repeated except that 3.56 g (0.039 moles) FeCl.sub.3 were 
used instead of 0.43 g (0.0032 moles) AlCl.sub.3. Following Procedure B, 
the liquid product contained methyl isobutyrate and methyl n-butyrate in a 
mole ratio of branched to straight chain esters of 5 to 1. 
EXAMPLE 22 
Example 7 was repeated except that 3.0 g (0.0343 moles) CrCl.sub.3 was used 
instead of the 3.56 g (0.039 moles) FeCl.sub.3. Following Procedure B, the 
liquid product contained methyl isobutyrate and methyl n-butyrate in a 
mole ratio of 4.2 to 1. 
EXAMPLE 23 
A fixed bed tubular reactor at 100.degree. C. and at 3,000 psig partial 
pressure CO and containing a solid catalyst of 5% palladium metal on an 
alpha-alumina support having a particle size in terms of the Martin 
diameter in the range of from 2 to 15 millimeters is continuously charged 
at the top with a liquid reaction mixture from a feed mixing tank 
containing methanol, HCl, methyl n-butyrate and tri-phenylarsine 
maintained at 100.degree. C. in corresponding mole ratios of 
41:2.2:1.4:0.203, with propylene in a ratio to methanol of 11.9 to 41, and 
with carbon monoxide to bring the pressure to 3,000 psig. From this point 
on, CO is added on demand to maintain a 3,000 psig pressure. 
Effluent liquid and gas from the bottom of the catalyst bed is removed 
continuously through a valve where pressure is let down to atmospheric. 
The effluent is passed into a flash drum where gas including dissolved gas 
comprised of unreacted propylene and carbon monoxide is separated and led 
to a compressor where it is compressed to 3,000 psig, then recycled to the 
reactor. 
The liquid product is fed continuously to a methanol still where methanol 
is separated as overhead and pumped to methanol storage for subsequent use 
in making up the feed in the feed mixing tank. 
Bottoms from the methanol still are pumped to a continuous methyl 
isobutyrate still where methyl isobutyrate is separated and pumped to 
methyl isobutyrate product storage. Bottoms from the methyl isobutyrate 
still are pumped to a methyl n-butyrate still and methyl n-butyrate 
corresponding to that synthesized is separated and pumped to methyl 
n-butyrate storage. The bottoms comprising triphenylarsine and residual 
methyl n-butyrate are pumped to the feed mixing tank. 
The composition of the feed mixing tank is kept constant by addition of 
feed ingredients as needed.