# Patent

## Title
Oxygen sorbent

## Abstract

This application is a continuation-in-part of commonly assigned copending U.S. patent application Ser. No. 323,002, filed Nov. 19, 1981, now U.S. Pat. No. 4,429,056 as a continuation of commonly assigned U.S. patent application Ser. No. 142,287, filed Apr. 21, 1980, now abandoned, the contents of which are incorporated by reference herein.

## Background
This invention is concerned with the production of acetaldehyde and ethanol by reaction of carbon monoxide and hydrogen in the presence of a ruthenium catalyst.

Acetaldehyde is a very valuable commercial chemical with a wide variety of uses particularly as an intermediate for production of commercial chemicals. Ethyl alcohol is also an important valuable commercial chemical useful for a wide variety of purposes including as a chemical intermediate, as a solvent, and perhaps more importantly as a component of gasohol.

The reaction of mixtures of carbon monoxide and hydrogen (e.g., synthesis gas) has long been known and can result in a variety of products depending on reaction conditions and the type of catalyst employed. U.S. Pat. No. 2,623,893 describes the reaction of carbon monoxide and hydrogen in the presence of one or more hydrogenation catalysts such as iron, nickel, cobalt or copper oxide-chromium oxide to provide oxygenated compounds such as aldehydes and ketones which are thereafter hydrogenated to the corresponding alcohols. U.S. Pat. No. 2,653,959 describes a process for separating oxygenated compounds, e.g., alcohol, esters, acids, ketones and aldehydes, from the oil phase of the product obtained from the reaction of carbon monoxide and hydrogen over an iron catalyst. U.S. Pat. No. 3,833,634 describes the reaction of carbon monoxide and hydrogen over rhodium catalyst to produce ethylene glycol, propylene glycol, glycerol, methanol, ethanol, methyl acetate and other products. U.S. Pat. No. 4,136,104 describes the conversion of synthesis gas to acetic acid and related oxygenated products such as ethanol, acetaldehyde and ethyl acetate employing a supported rhodium-ruthenium bimetallic alloy as catalyst. U.S. Pat. No. 4,157,338 describes a process for producing hydrocarbon mixtures useful in forming gasoline boiling range products wherein a mixture of carbon monoxide and hydrogen is contacted with a catalyst composition containing ruthenium, rhodium and/or osmium and a crystalline aluminosilicate zeolite. U.S. Pat. No. 4,246,186 describes the conversion of synthesis gas to two-carbon atom oxygenated hydrocarbons, namely, acetic acid, ethanol and acetaldehyde, employing a rhodium metal catalyst. U.K. Pat. No. 940,666 describes the conversion of synthesis gas to hydrocarbons and straight chain alcohols employing prereduced ruthenium chloride as catalyst. French Pat. No. 2,259,077 discloses producing ethanol from carbon monoxide and hydrogen using rhodium on silica gel as catalyst at 300.degree.-350.degree. C. and 1000-2500 psi pressure. West German Specification No. 2,644,185 describes conversion of carbon monoxide and hydrogen to hydrocarbons employing Ru.sub.3 (CO).sub.12 in tetrahydrofuran as solvent. Use of the same ruthenium carbonyl catalyst on solid supports to produce hydrocarbon products is described in J.A.C.S. 100, 2590 (1978). The conversion of carbon monoxide and hydrogen over ruthenium carbonyl clusters to methanol and methyl formate has been described [ACS/CSJ Chemical Congress Abstracts, INORG. 428 (1979)].

It has now been found that the reaction of carbon monoxide and hydrogen over certain selected ruthenium catalysts provides C.sub.2 -oxygenated products, that is, acetaldehyde and ethanol. The reaction apparently proceeds in several stages, with acetaldehyde being the predominant product in the early stages and ethanol predominating in later stages, so that the process can give rise to one or the other product, or mixtures of these products, which can be readily separated as by fractionation. Thus, by controlling reaction parameters, the process can be controlled to favor one or the other product, as desired. Methanol is the principal by-product obtained in the present process.

Thus, in accordance with this invention, a process is provided for forming acetaldehyde in a first stage reaction and then reducing said aldehyde to form ethanol in a second stage reaction which comprises reacting carbon monoxide and hydrogen at a temperature of from about 150.degree. to about 300.degree. C. and superatmospheric pressure in the presence of a catalyst system comprising (a) a preformed ruthenium carbonyl complex or a ruthenium carbonyl complex formed in situ by reaction between ruthenium metal and carbon monoxide or a ruthenium compound which undergoes reaction with carbon monoxide to provide said ruthenium carbonyl complex and (b) a source of halide anion, said catalyst system being present at least during said first reaction stage. The term "complex" as used herein and in the appended terms shall be understood in its generally recognized sense as defining a compound formed by combination of at least two other compounds, usually involving coordinate covalent bonds, and often reconvertible to the original simpler compounds.

If desired, the overall process of the invention can be conducted in separate stages, the initial stage resulting in production of acetaldehyde as the principal product, and the final stage resulting in production of ethanol as the principal product.

The very desirable results obtained in accordance with the present process renders the process particularly amenable to commercial production of acetaldehyde and ethanol, not only from the viewpoint of the substantial yields of the products, but also the ease of recovery from the co-produced methanol, e.g., by fractional distillation. The ease of recovery is extremely important since it permits separation of the products from the reaction mixture even in those process runs where methanol may be produced in substantial amount. Thus, for example, even where acetaldehyde is present in amounts corresponding to about 10 mole-percent, and even less, of the reaction product mixture, the ease of separation will permit recovery of the aldehyde.

Acetaldehyde is also produced in a high order of purity. Usually, the initial stage reaction mixture can be used as such in the final stage reaction to produce ethanol by reduction of acetaldehyde.

The results obtained with the present invention are indeed quite surprising and totally unexpected. In particular, ruthenium carbonyl complexes have been known to catalyze the reaction of carbon monoxide and hydrogen to form only one-carbon products such as methanol, methane and methyl formate. Further, under the relatively mild reaction conditions employed in the present process, particularly the moderate reaction temperatures, ruthenium carbonyl, Ru.sub.3 (CO).sub.12, forms little if any of the C.sub.2 -oxygenated products of this invention. Thus, the results obtained with the present catalysts are unobvious, particularly in view of the high conversions and specificity of the process in producing two-carbon oxygenated products.

The process of the present invention is accomplished by contacting carbon monoxide and hydrogen in the presence of certain ruthenium-containing catalysts in a suitable solvent at elevated temperature and superatmospheric pressure. The major products of the reaction are acetaldehyde and ethanol, with the major by-product being methanol. The manner of contact is not critical since any of the various procedures normally employed in this type of reaction can be used as long as efficient gas-liquid contact is provided. Thus, the processes may be carried out by contacting the ruthenium catalyst in reaction solvent with a mixture of carbon monoxide and hydrogen at the selected conditions. Where convenient, trickle phase operation can be used.

In view of the two-stage nature of the present process, the implementation can take several forms to produce ethanol. The reaction can be accomplished by allowing both stages to proceed consecutively at suitable temperature and pressure, or alternatively, the reaction can be stopped at the end of the first phase where the product is acetaldehyde and the second phase can be carried out under any applicable reduction process which will result in conversion of the aldehyde group of acetaldehyde to the primary alcohol group of ethanol. In most cases, however, the production of ethanol occurs quite readily. Usually, ethanol predominates as product when employing usual reaction conditions, the product mix being at least about 50/50 in most cases.

A wide variety of reduction processes can be employed for the second phase reaction including the well-known chemical reducing agents employed in reducing aldehydes to primary alcohols. For commercial processes, however, where possible, catalytic reductions employing hydrogen are usually preferred since they are more practical and efficient especially with catalysts which can be regenerated and thus are re-usable. In the present process, catalytic hydrogenation is preferred for these same reasons, especially with catalysts which can be regenerated. Any hydrogenation catalyst can be employed.

Thus, typical hydrogenation catalysts include, for example, Raney Nickel, cobalt, copper chromite, rhodium, palladium, platinum, and similar such metal catalysts, which can be used conveniently on supports such as charcoal, silica, alumina, kieselguhr and the like. The conditions of catalytic hydrogenation are well-known and, in general, the reaction can be conducted at temperatures ranging from about 30.degree. to about 150.degree. C., usually at pressures of from about 100 to about 5000 psig. The use of higher temperatures and pressures, though operable, provides no special advantage and usually requires special equipment which economically is disadvantageous and therefore not preferred.

Particularly preferred hydrogenation catalysts are those which characteristically require short reaction times, e.g., palladium and nickel, which is most desirable for commercial processes for economic reasons.

The active catalyst species of the catalyst system for the present process has not been fully identified but it is assumed to be comprised of ruthenium in complex combination with carbon monoxide together with a halide ligand. It is sufficient that the catalyst system initially comprise a source of ruthenium and a source of halide and the active catalyst species then forms on initiation of the process, e.g., the complex ruthenium carbonyl will form on addition of the reactants, i.e., carbon monoxide and hydrogen. Alternatively, the ruthenium source can be a preformed complex carbonyl. Further, the source of both ruthenium, or ruthenium carbonyl complex, and halide can be the same compound, e.g., ruthenium carbonyl halides which are commercially available. The catalyst system can be formed with ruthenium carbonyl halides or alternatively by the combination of ruthenium carbonyl or halocarbonyl complexes with a separate source of halide. The catalyst systems can be employed as such or deposited or affixed to a solid support such as molecular sieve zeolites, alumina, silica, ion exchange resin or a polymeric ligand. The preferred halides are chloride and bromide. The ruthenium halocarbonyl catalysts can be represented by the formula Ru.sub.a (CO).sub.b X.sub.c wherein a, b and c are integers and X is halide. Such catalysts can be prepared by reaction of ruthenium halides with carbon monoxide or by reaction of ruthenium carbonyl complexes with halogen-containing compounds. Alternatively, ruthenium carbonyl halides are available commercially, (e.g., from Matthey-Bishop, Malverne, PA).

The catalysts of this invention can contain other ligands in addition to halide ligand which must be present for the present process. As described in U.S. Pat. No. 3,833,634, suitable ligands are compounds which contain at least one nitrogen and/or at least one oxygen atom, said atoms having a pair of electrons available for formation of coordinate bonds with ruthenium. Illustrative organic ligands include various piperazines, dipyridyls, N-substituted diamines, aminopyridines, bis(triphenylphosphine)iminium chloride, glycolic acid, alkoxy-substituted acetic acids; tetrahydrofuran, dioxane, 1,2-dimethoxybenzene, alkyl ethers of alkylene glycols, alkanolamines, iminodiacetic acid, nitrilotriacetic acid, ethylenediaminetetraacetic acid, and the like. In U.S. Pat. No. 3,527,809 are described phosphorus-containing ligands such as trialkyl, triaryl and tricycloalkyl phosphites and phosphines, as well as analogous antimony and arsenic compounds. Other ligands such as tin halides, e.g., SnCl.sub.3 and SnBr.sub.3, or NO may be present.

The activity of the ruthenium catalyst system of this invention is increased by the addition of alkali metal salts, particularly halide salts. In present experience, the most preferred are lithium halides, especially lithium chloride, lithium bromide and lithium iodide. At 200.degree. C., a LiCl/Ru ratio of 15 resulted in reduction of 40 moles CO/mole Ru/hr. with a 44% selectivity to C.sub.2 -oxygenated products. Comparative figures for lithium bromide activation were 13 moles CO and 44% selectivity.

For most purposes, the amount of halide employed can be varied considerably, with molar ratios of at least about 0.1 mole per mole of ruthenium being operable. The alkali metal halides may be present in large molar excess, e.g., about 115 moles/mole ruthenium, and even higher.

In lieu of addition of alkali metal salts, preferably halides, the salts can be used with the selected catalyst to produce ruthenium halocarbonyl anions which, for the purpose of this disclosure, are represented by the general formula M.sub.a Ru.sub.b X.sub.c (CO).sub.d wherein a, b, c and d are integers, e.g., NaRuBr.sub.3 (CO).sub.3 and NaRuCl.sub.3 (CO).sub.3. Such compounds can be preformed and then added to the reaction in solvent as the catalyst system.

The hydrohalic acids HCl and HBr also promote the activity of the ruthenium halocarbonyls of the present new process but to a lesser extent than alkali metal halides. The addition of HCl increased the catalytic activity of [RuCl.sub.2 (CO).sub.3 ].sub.2 only to about 25% that of lithium chloride with a decrease of selectivity to ethanol and acetaldehyde, while both HCl and HBr promoted the activity of Ru.sub.3 (CO).sub.12. Large excesses of hydrogen halides are of no advantage and are usually avoided since they may tend to decrease catalyst activity.

In addition, the catalyst systems for this invention can also be formed by addition of halide to a suitable ruthenium compound in the selected solvent or in the reaction mixture, if preferred. For example, ruthenium acetylacetonate in combination with hydrogen halide in reaction solvents provides essentially the same results as preformed catalyst, e.g., [RuCl.sub.2 (CO).sub.3 ].sub.2. It is noted that, in the absence of halide, e.g., chloride or bromide, the ruthenium catalysts, such as ruthenium carbonyl, form methanol as the principal product with negligible or trace amounts of ethanol or acetaldehyde. The amounts of halide added to the catalyst need not be stoichiometric since even small amounts will result in the production of some ethanol. For most purposes, however, it is preferred to employ at least an equimolar amount of halide which can be added as aqueous solution, e.g., hydrohalic acid, or solution in organic solvents such as the lower alkanols.

When lithium chloride was employed at equimolar ratios with Ru.sub.3 (CO).sub.12, at 200.degree. C., 13 moles CO/mole Ru/hr. were reduced with a selectivity to two-carbon products of 48%. With excess lithium bromide (.about.60 moles/mole Ru) at 250.degree. C., enhanced productivity to two-carbon products was observed.

Other catalyst-potentiating materials which are advantageously employed herein include alkaline earth metal halides such as magnesium chloride and calcium chloride, quaternary ammonium halides such as tetramethylammonium bromide, quaternary phosphonium halides, such as tetramethylphosphonium bromide halides, and especially the chlorides and bromides of Group IIIb metals, e.g., those of scandium, and yttrium, and halides of metals of the lanthanide series, e.g., those of lanthanum and neodymium.

The determination of suitability of starting ruthenium compounds to be used for in situ formation of the halide-containing catalyst can be accomplished by a simple test procedure which involves running small scale reactions with the selected ruthenium compound, halide and reactants CO and H.sub.2 in solvent. At the completion of the miniature reactions, gas-liquid chromatographic analyses of the reaction mixture will identify the products and, of course, will identify those ruthenium compounds which are suitable, through in situ treatment, for production of ethanol and/or acetaldehyde. Using this test procedure, suitable starting ruthenium compounds are easily identified.

When acetaldehyde is the desired product, of course, only the first stage reaction need be carried out. The product can be separated from the co-produced methanol, any ethanol formed and reaction solvent, if necessary, by fractional distillation.

As should be apparent, the ruthenium catalyst employed in the first stage reaction can also serve as the hydrogenation catalyst for the second stage reaction to produce ethanol. Thus, if the first phase reaction is allowed to continue, eventually the hydrogenation reaction will yield ethanol. In general, the ruthenium catalyst of the first stage reaction is an effective catalyst for the second stage hydrogenation, but other hydrogenation catalysts can be used in lieu of the ruthenium catalyst. If desired, the ruthenium catalyst can be converted to a more effective hydrogenation catalyst by addition of a phosphine ligand, particularly triaryl phosphines such as triphenyl phosphine and other phosphine ligands as described in U.S. Pat. No. 3,527,809.

The first stage reaction can be conducted in a first reactor under selected conditions of temperature and pressure and after completion, the first stage product, with or without isolation from the reaction mixture, can then be transferred to a second reactor under selected conditions of temperature and pressure to effect the hydrogenation reaction over metal catalysts such as palladium and nickel, or copper chromite.

There is, of course, no criticality about stopping the reaction exactly at the termination of the first stage, or holding the second stage reaction until all acetaldehyde is reduced to ethanol. The reaction can be stopped at any convenient point which will be dictated by the product desired, along with other considerations. Thus, after substantially maximum yield of acetaldehyde is obtained, usually within about 2 hours, the reaction can be stopped and the aldehyde recovered. However, the reaction mixture will undoubtedly contain quantities of ethanol formed through the second stage reaction. The products, however, are easily separable and are almost equally commercially important. Obviously, where ethanol is desired, the reaction can be allowed to proceed, within economic considerations, until reasonably complete to obtain ethanol as the major product and, of course, acetaldehyde as the minor product.

The present invention, therefore, provides a simplified process for production of acetaldehyde. In addition, this invention affords a simplified process for obtaining ethanol by either allowing the initial process for aldehyde production to continue so that hydrogenation yields ethanol or, alternatively, the aldehyde product of the first stage reaction is reduced employing art-recognized reduction processes to ethyl alcohol. In the latter process, the acetaldehyde product of the first stage reaction can be used in the form of the reaction mixture, or the product can be isolated, as by fractionation, and used in purified form.

The amount of catalyst employed in the present process does not seem to be critical and can vary considerably. At least a catalytically effective amount of catalyst should be used, of course. In general, an amount of catalyst which is effective to provide a reasonable reaction rate is sufficient. As little as 0.001 gram atoms of ruthenium per liter of reaction medium can suffice while amounts in excess of 0.1 gram atoms do not appear to materially affect the rate of reaction. For most purposes, the effective preferred amount of ruthenium is in the range of from about 0.002 to about 0.05 gram atoms per liter.

The reaction conditions are not overly critical in that wide ranges of elevated temperature and superatmospheric pressures are operable. The practical limitations of production equipment will dictate to a great extent the selection of temperatures and pressure at which the reaction is to be effected. Thus, using available production systems, the selected elevated temperature should be at least about 150.degree. C. and can range up to about 300.degree. C. For most purposes, the preferred operating temperature ranges from about 175.degree. to about 275.degree. C. The superatmospheric pressure should be at least about 10 atmospheres and can range up to almost any pressure attainable with production apparatus. Since extremely high pressure apparatus is quite expensive, pressures to about 700 atmospheres are suggested. Most desirably, the pressure should be in the range of from about 150 to about 600 atmospheres, particularly when employing the aforesaid preferred temperature range.

The reaction is preferably carried out in a solvent which will dissolve polar materials and which preferably is aprotic. The preferred solvents are N-substituted amides in which each hydrogen of the amido nitrogen is substituted by a hydrocarbon group, e.g., 1-methyl-pyrrolidin-2-one, N,N-dimethylacetamide, N,N-diethylacetamide, N-methylpiperidone, 1,5-dimethylpyrrolidin-2-one, 1-benzyl-pyrrolidin-2-one, N,N-dimethylpropionamide, hexamethylphosphoric triamide and similar such liquid amides. The amides are preferred solvents since their use results in the highest yields of product in present experience. Other solvents, usually aprotic, can be used but the yields in some cases may be substantially less than those obtained with the preferred amide solvents. Such solvents include for example, cyclic ethers such as tetrahydrofuran, dioxane and tetrahydropyran; ethers such as diethyl ether, 1,2-dimethoxybenzene; alkyl ethers of alkylene glycols and polyalkylene glycols, e.g, methyl ethers of ethylene glycol, propylene glycol and di-, tri- and tetraethylene glycols; ketones such as acetone, methyl isobutyl ketone, and cyclohexanone; esters, such as ethyl acetate, ethyl propionate and methyl laurate; and alkanols, such as methanol, ethanol, propanol, 2-ethylhexanol and the like; tetramethylurea; gamma-butyrolactone; and mixtures thereof. The selected solvent should preferably be liquid under the reaction conditions.

The preferred solvents are aprotic organic amides. The contemplated amides include cyclic amides, i.e., in which the amido group is part of a ring structure such as in pyrrolidinones and piperidones; acylated cyclic amines, such as N-acyl piperidines, pyrroles, pyrrolidines, piperazines, morpholines, and the like, preferably in which the acyl group is derived from a lower alkanoic acid, e.g., acetic acid; as well as acyclic amides, i.e., wherein the amido group is not part of a ring structure as in acetamides, formamides, propionamides, caproamides and the like. The most preferred of the amides are those in which the amido hydrogen atoms are fully replaced by hydrocarbon groups preferably containing not more than 8 carbon atoms. Exemplary hydrocarbon groups are alkyl, preferably lower alkyl such as methyl, ethyl and butyl; aralkyl, such as benzyl and phenethyl; cycloalkyl, such as cyclopentyl and cyclohexyl; and alkenyl, such as allyl and pentenyl. The preferred amido nitrogen substituents are lower alkyl, especially methyl, ethyl and propyl groups and aralkyl groups, especially benzyl. The most preferred amide solvents include 1-methylpyrrolidin-2-one, 1-ethylpyrrolidin-2-one, and 1-benzylpyrrolidin-2-one. Of course, mixtures of the solvents can be used, e.g., amide solvent with other solvents.

Combinations of solvents may also be used to good effect. It has been found that a solvent medium containing a major amount of an aprotic solvent such as gamma-butyrolactone and a minor amount, e.g., from about 5 to about 40 weight percent, and preferably from about 10 to about 10 weight percent, of a tertiary amine such as N-methylpyrrolidine may be especially advantageous where the production of methanol is concerned since such a mixed solvent system primarily provides methanol with smaller amounts of methane and ethanol also being formed. The tertiary amine seems to function as a promoter for the ruthenium-containing, halide-containing catalyst composition of this invention. Further improvement selectivity of the process of this invention employing the foregoing mixed solvent system can be achieved by the addition of a co-promoting amount of one or more alkali metal halides such as any of those described above. Lithium bromide is especially preferred as a co-promoter for such system.

Water is not critical to the reaction and can be present without serious adverse effect. It tends to react with carbon monoxide to form CO.sub.2 and hydrogen (water gas shift). Water can be excluded since it can reduce the selectivity of conversion of carbon monoxide, or the water-gas shift can be used advantageously to generate hydrogen.

The reaction pressures represent the total pressure of the gases contained in the reactor, i.e., carbon monoxide and H.sub.2, and, if present, any diluent gas such as nitrogen. As in any gaseous system, the total pressure is the sum of partial pressures of component gases. In the present reaction, the molar ratio of hydrogen to carbon monoxide can range from about 1/10 to about 10/1, with the preferred ratio from about 1/5 to about 5/1, and the reaction pressure can be achieved by adjusting the pressure of these gases in the reactor.

Where the second phase reaction is carried out in a separate reactor, whether over the originally present ruthenium catalyst or a different metal hydrogenation catalyst, the reaction is normally conducted under hydrogen gas without diluent gas, as is usual in catalyzed hydrogenation reactions.

As with any process of this kind, the present process can be conducted in batch, semi-continuous, and/or, continuous operation. The reactor should be constructed of materials which will withstand the temperatures and pressures required and the internal surfaces of the reactor should be substantially inert. The usual controls can be provided to permit control of the reaction, e.g., heat-exchangers and the like. The reactor should be provided with means achieving gas-liquid contact such as by shaking, stirring, oscillation, trickle column operation and like methods. Catalyst as well as reactants may be introduced into the first stage or the second stage reactor at any time during the process for replenishment. Recovered catalyst, solvent and unreacted starting materials can be recycled.

The relative yields of ethyl alcohol, acetaldehyde and methanol are not overly critical since the product mixture can be readily separated into the components by known techniques, especially by fractional distillation, regardless of the proportions contained in the mixture. Therefore, even where the desired product is 10-20% of the reaction mixture, it can be readily separated from the mixture, especially under continuous processing. Of course, the preferred processes yield mixtures in which acetaldehyde and ethanol predominate as the reaction product and methanol, as a by-product, is minimal.

The process conditions for the separate first stage reaction are essentially the same as employed in the first stage of the combined two-stage reaction. Thus, the reaction is carried out at a temperature of at least about 150.degree. C. to obtain a reasonable reaction rate and up to about 300.degree. C. for best results, the temperature should be in the range of from about 175.degree. C. to about 275.degree. C. The total pressure of gas used is generally maintained at from about 10 up to about 700 atmospheres with from about 150 to about 600 atmospheres being preferred. Of course, high pressure and higher temperatures can be used but with no appreciable advantage and, since they require the use of special high pressure equipment, they are usually avoided.

The reaction conditions employed in the second reaction stage, i.e. the hydrogenation, can be any of the standard reaction temperatures and pressures employed for such reactions since neither temperature nor pressure are critical for this reaction. Preferably, the hydrogenation is conducted at a temperature of at least about 100.degree. C. in order to effect a reasonable reaction rate. Of course, lower temperatures can be used if longer reaction times can be tolerated. The pressure of hydrogen gas is not excessively critical as long as sufficient gas is available for the hydrogenation. For convenience, the pressure will range from about 500 psi to as much as 5000 psi, although even higher pressures can be employed.

When the catalyst selected for the hydrogenation step is other than ruthenium, it is preferred to remove the ruthenium catalyst from the first stage reaction mixture. This preference is primarily predicated on the desirability of avoiding concomitant catalytic effects which may tend to reduce the yield of ethanol.

The following examples further illustrate the invention. The equipment, synthetic procedure and analyses employed are as follows:

Reactions were carried out in Parr 71 ml reactors constructed of 310SS having one Type A 1/4" coned socket (Cat. #4740, Parr Instrument Co., Moline, IL). Glass liners with open tops were employed. Reactor seal was a modified Brideman type, incorporating a special two piece gasket (Cat. #61 HD), comprising silver (exposed to process) with a nickel back-up ring. This gasket arrangement was necessitated due to attack by carbon monoxide of the originally supplied one-piece nickel gasket.

The reactors were capped with 316SS Whitey severe service valves with high temperature Grafoil packing (Cat. #SS3NBS4-GTA09K-3N, Whitey Co., Oakland, CA). The valves were coupled to the reactors with 316SS Sno-Trik Co., Solon, OH, and Swagelok port connectors (Cat. #SS-401-PC, Crawford Fitting Co., Cleveland, OH).

The arm of a Burrell wrist action shaker was projected into an oven comprising an insulated box and electrical stripheaters. Reactors were clamped to the shaker arm. Oven temperature was measured by a thermocouple which connected to a controller (on-off type). A timer was used to control reaction time by interrupting power to the temperature controller at the desired time. The temperature controller was used to activate a relay coil. A Variac was used to regulate the voltage going to the heater from the relay.

In cases where more vigorous agitation was required, the reactors (without glass liners) were bolted to a paint shaker by means of a special bracket which prevented whip action of the valve which would cause the port connector to sever.

Custom carbon monoxide-hydrogen mixtures (Union Carbide Corp., Linde Division, South Plainfield, NJ) were piped into an air driven, double-ended compressor (Cat. #46-14035, American Instrument Co., Silver Spring, MD) and then into the reactor through a line containing shut-off and vent valves and a pressure gauge.

Reactor charging and sealing generally were carried out in a nitrogen atmosphere (glove bag). Catalyst (about 0.02 gm) and additives were weighed into a glass liner which then was placed in the reactor. Solvent (5 ml) and liquid additives (usually air free) were added by syringe or pipette. The reactor was sealed and capped with a valve.

The reactor was connected to the compressor discharge system and purged with the desired gas by pressurizing, then venting several times. Then gas was compressed into the reactor to the desired pressure (2000-4500 psig) as indicated on the system gauge. After gas feed-line venting, the reactor was disconnected, and the valve plugged to prevent leakage through the seal.

After heating (80.degree.-250.degree. C.) and shaking the reactor for the desired time, it was cooled then vented through a wet test meter with a gas sample being taken. The liquid contents were discharged, and the reactor and liner rinsed with solvent. The combined liquid for analysis was 15 gm.

GLC analyses were performed on a Varian-Aerograph Series 1400 Chromatograph equipped with hydrogen flame detector. A 6'.times.1/8" O.D. 316SS column packed with 80-100 mesh Chromosorb 101 was utilized. The column was operated at 100.degree. C. for 9 minutes then temperature was increased by 6.degree. C./min. to 200.degree. C. This procedure provided reproducable isothermal analysis of lower boiling component and decreased retention times for higher boiling materials.

The components of the reaction mixtures employing Ru catalysts were identified by GLC-MS analysis. Besides the major products--methanol, ethanol and acetaldehyde--several other components were found. These were formaldehyde, ethylene glycol, propionaldehyde, n-propanol, acetic acid, methyl acetate, 1,3-dioxolane, 2-methyl-1,3-dioxolane, hydroxy-2-propanone and 1,2-propanediol. In a few cases, methane was observed.

Using the described Synthesis Procedure, the catalysts produced with various alkali metal chlorides and Ru.sub.3 (CO).sub.12 were evaluated using the following materials and reaction conditions:

The reaction was conducted at 200.degree. C. for two hours. The results are given in TABLE I. ______________________________________ Turnover Number Product  Moles Mole     Product/ Products, mmoles       Ratio    Mole Ru Salt   CH.sub.3 OH CH.sub.3 CHO C.sub.2 H.sub.5 OH C.sub.1 /C.sub.2 C.sub.1 C.sub.2 ______________________________________ --     0        0         0      --     0    0 LiCl   1.25     .47       .10    2.2    13   6.1 NaCl   .75      .15       tr.    5.0    8.1  1.6 KCl    .37      .11       --     3.4    4.0  1.2 RbCl   .57      .20       --     2.8    6.1  2.2 RbCl (1) .74      tr.       tr.    --     8.0  -- CsCl   .48      .07       --     6.8    5.2  .8 ______________________________________ (1) .5 mmole salt

Various catalysts formed in situ from lithium salts and Ru.sub.3 (CO).sub.12 were evaluated using the same procedure as in EXAMPLE 1 excepting the salts were added at a level of 0.1 mmole.

The results are given in TABLE II. ______________________________________ Turnover Number Product  Moles Mole     Product/ Products, mmoles       Ratio    Mole Ru Salt   CH.sub.3 OH CH.sub.3 CHO C.sub.2 H.sub.5 OH C.sub.1 /C.sub.2 C.sub.1 C.sub.2 ______________________________________ --     0        0         0      --     0    0 LiF (1) tr.      0         0      --     tr.  0 LiCl   1.25     .47       .10    2.2    13   6.1 LiBr   .51      .27       0      1.9    5.5  2.9 LiBr (2) 1.59     tr.       .06    27     17   .6 LiI    .30      .05       0      6.0    3    .5 LiOAc  .16      tr.       0      --     1    -- Li.sub.2 CO.sub.3 0        0         0      --     0    0 ______________________________________ (1) .15 mmole (2) .6 mmole

Various catalysts formed with hydrogen halides and Ru.sub.3 (CO).sub.12 were evaluated using the procedure of EXAMPLE 2. In addition, the effect of hydrogen halides on preformed ruthenium chlorocarbonyls was also evaluated using the same procedure.

The results are shown in TABLE III. __________________________________________________________________________ Product Turnover Number Products, mmoles Mole Ratio Moles Product/Mole Ru Catalyst Acid CH.sub.3 OH CH.sub.3 CHO C.sub.2 H.sub.5 OH C.sub.1 /C.sub.2 C.sub.1 C.sub.2 __________________________________________________________________________ Ru.sub.3 (CO).sub.12 --  0    0     0    --    0     0 Ru.sub.3 (CO).sub.12 HCl .65  .16   .12  2.3   7.0   3.0 Ru.sub.3 (CO).sub.12 HBr .66  .32   .20  1.3   7.1   5.6 Ru.sub.3 (CO).sub.12 HI (1) 0    0     0    --    --    -- [RuCl.sub.2 (CO).sub.3 ].sub.2 --  1.2  .20   .20  3.0   12    4 [RuCl.sub.2 (CO).sub.3 ].sub.2 HCl 2.0  tr.   .26  7.7   20    2.6 [RuCl.sub.2 (CO).sub.3 ].sub.2 HBr 1.4  tr.   .23  6.1   14    2.3 [RuCl.sub.2 (CO).sub.3 ].sub.2 HI  0    0     0    --    --    -- __________________________________________________________________________ (1) 8 mmoles HI

The effect of increasing lithium chloride molar ratio was evaluated using the procedure of EXAMPLE 2 with the results given in TABLE IV, with [Ru(CO).sub.3 Cl.sub.2 ].sub.2 preformed catalyst. __________________________________________________________________________ ##STR1## CH.sub.3 OHCH.sub.3 CHOC.sub.2 H.sub.5 OHProducts, C.sub.1 /C.sub.2Mole RatioProduct C.sub.1C.sub.2Moles Product/Mole RuTurnover Number __________________________________________________________________________ 0      1.18 .20   .20  2.9   12    4.1 .9     2.44 .37   .43  3.0   25    8.2 2.0    3.05 .51   .55  2.9   31    11 7.7    4.08 .62   .88  2.7   42    15 15     4.41 .62   1.1  2.6   45    17 __________________________________________________________________________

Various temperature, catalyst and additive effects on the reaction were evaluated using the procedure of Example 1.

The results are given in TABLE V. __________________________________________________________________________ Catalyst   Promoter, P ##STR2## .degree.C.Temp., CH.sub.3 OHCH.sub.3 CHOC.sub.2 H.sub.5 OHProducts, mMoles C.sub.1 /C.sub.2Mole RatioProduct C.sub.1C.sub.2Moles Product/Mole RuTurnover __________________________________________________________________________ Number Ru.sub.3 (CO).sub.12 --     --     175 0    0     0    0     0     0 Ru.sub.3 (CO).sub.12 --     --     200 .05  0     0    --    .5    0 Ru.sub.3 (CO).sub.12 --     --     250 .47  0     0    --    5.0   0 Ru.sub.3 (CO).sub.12 LiCl   1      175 .38  .29   0    1.3   4.1   3.1 Ru.sub.3 (CO).sub.12 LiCl   1      200 1.25 .47   .10  2.2   13.4  6.1 Ru.sub.3 (CO).sub.12 LiCl   16     250 25.  0     .24  104   263.  2.5 Ru.sub.3 (CO).sub.12 HBr    1      185 .24  .11   .16  .9    2.6   2.9 Ru.sub.3 (CO).sub.12 HBr    1      200 .66  .32   .20  1.3   7.1   5.6 Ru.sub.3 (CO).sub.12 HBr    1      250 11.0 0     .44  .25   118.  4.7 [RuCl.sub.2 (CO).sub.3 ].sub.2 --     --     150 tr.  tr.   tr.  --    tr.   tr. [RuCl.sub.2 (CO).sub.3 ].sub.2 --     --     175 .26  tr.   .10  2.6   2.6   1.0 [RuCl.sub.2 (CO).sub.3 ].sub.2 --     --     200 1.20 .20   .20  3.0   12.2  4.1 [RuCl.sub.2 (CO).sub.3 ].sub.2 --     --     250 7.6  tr.   .32  24.   78.   3.3 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl   7.5    185 1.4  .32   .47  1.7   14.   8.1 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl   7.7    200 4.1  .62   .88  2.8   42.   15. [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl   15     200 4.4  .62   1.1  2.6   45.   18. [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl   15     250 23.2 0     1.32 18.   237.  13. [RuCl.sub.2 (CO).sub. 3 ].sub.2 LiBr   15     200 1.47 .30   .27  2.6   15.   5.8 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiBr   15     250 11.7 .27   1.96 5.2   119.  23. [RuCl.sub.2 (CO).sub.3 ].sub.2 LiBr   58     250 14.5 .35   3.96 3.4   148.  44. [RuCl.sub.2 (CO).sub.3 ].sub.2 LiBr   115    250 8.0  .47   4.99 1.5   82.   56. [RuCl.sub.2 (CO).sub.3 ].sub.2 * LiI    15     250 13.5 --    5.00 2.7   13.5  50. RuCl.sub.2 (CO).sub.2 (Ph.sub.3 P).sub.2 LiCl   1      200 1.02 tr.   .03  34.   10.4  .31 RuCl.sub.2 (CO).sub.2 (Ph.sub.3 P).sub.2 LiCl   1      250 5.8  tr.   .09  64.   59.2  .92 (SnCl.sub.3)Ru.sub.2 Cl.sub.3 (CO).sub.5 --     --     200 .89  .08   .16  3.7   9.1   2.4 (SnCl.sub.3)Ru.sub.2 Cl.sub.3 (CO).sub.5 LiCl   54     200 4.36 .81   1.71 1.7   44.   26. __________________________________________________________________________ *.1 mMole Ru

Referring to TABLE V, it is noted that the use of higher reaction tempeature over 200.degree. C. and preferably above 225.degree. C., results in significant increases in methanol production and, in some cases, in extremely high selectivities to methanol, as evidenced by the Product Mole Ratio C.sub.1 /C.sub.2 values, and the Turnover Number values. This increase in methanol production is further enhanced by added halide, especially chlorides which generally appear to be more effective than other halides in this regard.

The combination of increased reaction temperature and addition of halide, i.e., metal halide and/or hydrogen halide, in present experience gives the best productivities to methanol and therefore comprises a particularly preferred embodiment of this aspect of the present new process.

Ruthenium and rhodium chlorocarbonyl are compared with and without lithium chloride as a promoter in the procedure of EXAMPLE 1 with the results given in TABLE VI.

From these data, it is apparent that lithium chloride does not promote but rather inhibits the rhodium catalyst. __________________________________________________________________________ Turnover Number mMole              Product Yields, mMoles Moles Product/Mole Metal Catalyst Metal Additive, mMole Temp.,.degree.C. CH.sub.3 OH CH.sub.3 CHO C.sub.2 H.sub.5 OH C.sub.1 C.sub.2 __________________________________________________________________________ [Rh(CO).sub.2 Cl].sub.2 .129 --   --  175   .066 .012  .046 .5    .4 [RuCl.sub.2 (CO).sub.3 ].sub.2 .098 --   --  175   .26  tr.   .10  2.6   1.0 [Rh(CO).sub.2 Cl].sub.2 .129 LiCl  .129 200   .023 .013  0    .2    .1 [RuCl.sub.2 (CO).sub.3 ].sub.2 .098 LiCl  .098 200   2.44 .37   .43  25    8.2 [Rh(CO).sub.2 Cl].sub.2 .129 --   --  200   .24  tr.   .056 1.9   .4 [RuCl.sub.2 (CO).sub.3 ].sub.2 .098 --   --  200   1.18 .20   .20  12    4.1 [Rh(CO).sub.2 Cl].sub.2 .129 LiCl .75 200   0    0     0    0     0 [Rh(CO).sub.2 Cl].sub.2 .098 LiCl .75 200   0    0     0    0     0 [RuCl.sub.2 (CO).sub.3 ].sub.2 .098 LiCl .77 200   4.08 .62   .88  42    15 __________________________________________________________________________

Various preformed ruthenium halocarbonyl anions were evaluated using the procedure of EXAMPLE 1 with the results given in TABLE VII. The alkali metal salt and ruthenium carbonyl halide of EXAMPLE 1 are replaced by the indicated anionic complex. __________________________________________________________________________ YIELDS (mmole) Catalyst Additive T (.degree.C.) MeOH CH.sub.3 CHO EtOH CH.sub.4 __________________________________________________________________________ CsRu(CO).sub.3 Cl.sub.3 --     250  8.4 .22    .54 0 CsRu(CO).sub.3 Cl.sub.3 CsBr   250  6.5 .28    .54 .5 (1.5 mmoles) Cs.sub.2 Ru(CO).sub.3 Cl.sub.4 --     250  9.1 .2     .56 .8 Cs.sub.2 Ru(CO).sub.3 Cl.sub.4 CsBr   250  9.0 tr.    .97 1.2 (1.5 mmoles) K.sub.2 Ru(NO)Cl.sub.5 --     200  1.2 .31    .37 .4 K.sub.2 Ru(NO)Cl.sub.5 --     250  7.1 tr.    4.3 6.8 LiRu(CO).sub.3 Cl.sub.3 --     200  2.7 .77    .71 0 LiRu(CO).sub.3 Cl.sub.3 --     250  7.7 tr.    .58 0 LiRu(CO).sub.3 Br.sub.3 --     200  1.4 .25    .5  0 LiRu(CO).sub.3 Br.sub.3 --     250  11  .37    1.5 1.9 CsRu(CO).sub.3 Cl.sub.3 --     200  1.0 .22    .21 0 Cs.sub.2 Ru(CO).sub.2 Cl.sub.4 --     200  .93 .14    .26 0 __________________________________________________________________________

The procedure of the preceding examples was repeated employing HBr or HCl with Ru.sub.3 (CO).sub.12 (at 0.093 mmole Ru) and with H.sub.4 Ru.sub.4 (CO).sub.12 (at 0.1 mmole Ru) at H.sub.2 /CO of 1.5:1 and initial pressure of 4500 psig for two hours at the indicated temperatures. The results are given in TABLE VIII. __________________________________________________________________________ YIELDS (mmole) Catalyst Additive T (.degree.C.) MeOH CH.sub.3 CHO ETOH CH.sub.4 __________________________________________________________________________ H.sub.2 Ru.sub.4 (CO).sub.12 HBr     200 .51 .23   .24 0 (.1 mmole) H.sub.2 Ru.sub.4 (CO).sub.12 --      200 .06 tr.   tr. 0 Ru.sub.3 (CO).sub.12 HBr     200 0   0     0   0 (.5 mmole) Ru.sub.3 (CO).sub.12 HBr     200 .55 .17   .15 0 (.1 mmole) Ru.sub.3 (CO).sub.12 --      200 .05 0     0   0 Ru.sub.3 (CO).sub.12 HCl     200 .65 .16   .12 0 (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     200 .66 .32   .2  0 (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     200 .5  .35   .18 0 (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     200 .89 tr.   .55 0 (.2 mmole) Ru.sub.3 (CO).sub.12 HBr     185 .24 .11   .16 0 (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     250 11  0     .44 1.1 (.1 mmole) LiCl (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     200 2.0 .89   .42 0 (.1 mmole) Ru.sub.3 (CO).sub.12 HBr     175 .15 .04   .14 .98 (.1 mmole) LiBr (5.8 mmole) Ru.sub.3 (CO).sub.12 HBr     200 3.2 .56   .24 0 (.1 mmole) LiBr (5.8 mmole) Ru.sub.3 (CO).sub.12 HBr     250 14.9 .08   2.19 6.1 (.1 mmole) __________________________________________________________________________

This example demonstrates the generally improved rates of conversion of CO to CH.sub.3 OH obtained with the use of a variety of catalyst promoters in accordance with this invention. The addition of metal chlorides, especially lithium chloride (at a concentration of 1.5 mmoles per 5 ml NMP), to ruthenium complex catalysts (0.095.+-.0.003 mmole per 5 ml NMP) enhance direct syn-gas reaction to produce greater yields of methanol at 250.degree. C. As seen from TABLE IX, below, there appears to be an optimum salt concentration and reaction temperature for a particular salt as shown by LiCl at 200.degree. and 250.degree. C. and with a concentration of 1.5 and 5.7 mmoles at 250.degree. C. ______________________________________ Moles CO Con- Moles CO         verted to Converted        CH.sub.3 OH Catalyst   per Mole  CH.sub.3 OH per Mole Promoter   Ru per    Select- Ru per Catalyst  mmole      hour      ivity, % hour ______________________________________ Ru.sub.3 (CO).sub.12 --             2.5     100    2.5 Ru.sub.3 (CO).sub.12 LiCl    1.5    138     92     127 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl    1.5    42      52     22 (200.degree. C.) [RuCl.sub.2 (CO).sub.3 ].sub.2 --             44      86     38 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl    1.5    141     82     116 [RuCl.sub.2 (CO).sub.3 ].sub.2 LiCl    5.7    94      76     71 [RuCl.sub.2 (CO).sub.3 ].sub.2 MgCl.sub.2 0.08   81      89     72 [RuCl.sub.2 (CO).sub.3 ].sub.2 NdCl.sub.3 0.56   76      96     73 [RuCl.sub.2 (CO).sub.3 ].sub.2 CaCl.sub.2 1.1    68      88     60 ______________________________________

This example illustrates the process of the invention employing tetramethylammonium bromide as a promoter. Following the general procedure, 0.0247 g [RuCl.sub.2 (CO).sub.3 ].sub.2, 0.2297 g tetramethylammonium bromide and 5.0 ml deaerated NMP were charged to the reactor which was thereafter pressurized to 4500 psig with hydrogen and carbon monoxide in a mole ratio of 1.5:1. Reaction was carried out at 200.degree. C. for 2 hours after which the reactor was vented to atmospheric pressure and cooled to room temperature. The following GLC analytical data were obtained on the contents of the reactor. Component       Millimoles ______________________________________ dimethylether   .01 methanol        2.8 ethanol         .6 methane         0 ______________________________________

The procedure of the previous example was substantially repeated at 250.degree. C. employing 0.0253 g [RuCl.sub.2 (CO).sub.3 ].sub.2, 0.2297 g tetramethylammonium bromide and 5.0 ml NMP. The results of GLC analysis were as follows: Component       Millimoles ______________________________________ dimethylether   .2 methanol        14.8 methyl formate  trace methylethylether .4 ethanol         5.4 methyl acetate  .5 n-propanol      .7 ethyl acetate   .3 methane         10. ______________________________________

This example illustrates the use, as promoter, of the rare earth halide neodymium trichloride hexahydrate. Following the general procedure of the previous examples, 0.0254 g [RuCl.sub.2 (CO).sub.3 ].sub.2, 0.2003 g NdCl.sub.3.6H.sub.2 O and 5.0 ml deaerated NMP were introduced into the reactor which was then pressurized to 4,500 psig with a 1.5:1 mole ratio of H.sub.2 :CO and the contents thereof reacted at 250.degree. C. for 2 hours. GLC analysis of the vented, cooled reactor contents were as follows: Component       Millimoles ______________________________________ dimethylether   .08 methanol        14.7 methylformate   trace ethanol         .29 methane         0 ______________________________________

Substantially the same procedure as the previous example was employed except that 0.0250 g [RuCl.sub.2 (CO).sub.3 ].sub.2 and 0.1994 g LaCl.sub.3 were used and the reaction was carried out at 200.degree. C. The GLC analytical results were as follows: Component       Millimoles ______________________________________ dimethylether   .01 methanol        2.2 acetaldehyde    .1 methylformate   trace ethanol         .3 methane         0 ______________________________________

The previous example was repeated at 250.degree. C. reaction temperature with 0.0249 g [RuCl.sub.2 (CO).sub.3 ].sub.2 and 0.3 g lanthanium bromide. The results of GLC analysis were as follows: Component       Millimoles ______________________________________ dimethylether   .7 methanol        6.8 acetaldehyde    .2 methylethylether .8 ethanol         7.0 methylacetate   .48 n-propanol      1.5 ethylacetate    .2 methane         35.0 ______________________________________

This example illustrates the use, as promoter, of bis(triphenylphosphine)iminium chloride. Following substantially the same procedure as the previous examples, 0.0249 g [RuCl.sub.2 (CO).sub.3 ].sub.2 and 0.8596 g bis(triphenylphosphine) iminium chloride and a reaction temperature of 200.degree. C. were employed. The results of GLC analysis of the reaction products were as follows: Component       Millimoles ______________________________________ dimethylether   .1 methanol        11.6 acetaldehyde    .29 methylformate   trace ethanol         1.44 methane         0 ______________________________________

This example illustrates the use, as promoter, of yttrium bromide. Following substantially the same procedure as the previous examples, 0.0252 g [RuCl.sub.2 (CO).sub.3 ].sub.2 and 0.6403 g yttrium bromide were introduced into the reactor and a reaction temperature of 250.degree. C. and a reaction period of 1 hour were employed. GLC analysis of the reactor contents was as follows: Component       Millimoles ______________________________________ dimethylether   .07 methanol        7.56 acetaldehyde    trace methylformate   trace methylethylether .07 ethanol         1.24 n-propanol      .25 methane         1.4 ______________________________________

The previous example was substantially repeated except that 0.0255 g [RuCl.sub.2 (CO).sub.3 ].sub.2 and 0.5498 g scandium bromide were employed. The results of GLC analysis were as follows: Component       Millimoles ______________________________________ dimethylether   .04 methanol        2.68 methylethylether .04 ethanol         2.24 ethylacetate    .59 methane         1.7 ______________________________________

This example illustrates the use of a mixed solvent medium, namely, gammabutyrolactone (GBL) and N-methylpyrrolidine.

A 71 ml Parr, Hastelloy C autoclave reactor provided with a glass liner was charged with 0.250 g [RuCl.sub.2 (CO).sub.3 ].sub.2 0.5 ml N-methylpyrrolidine and 5.0 ml GBL under a nitrogen atmosphere. The reactor was sealed and pressurized to 4,500 psig with 1.5:1 H.sub.2 /CO mixture. The reactors were placed in a Burrell shaker/oven and heated to 250.degree. C. at which temperature the reactor was held for 2 hours. The results of GLC analysis of the principal reaction products were as follows: Component       Millimoles ______________________________________ dimethylether   .05 methanol        11.6 ethanol         .25 ______________________________________

As these data show, the use of such a mixed solvent system results in a reaction mixture predominantly containing methanol.

This example illustrates the catalyst-promoting affect of an alkali metal halide, namely, lithium bromide, employing the mixed solvent medium Example 18.

Following substantially the same procedure as described in Example 18 and using the same equipment, the reactor was charged with 0.0247 g [RuCl.sub.2 (CO).sub.3 ].sub.2, 0.04997 LiBr, 0.5 ml N-methylpyrrolidine and 5.0 GBL. Following charging of the reactor with 1.5:1 H.sub.2 /CO mixture and a reaction period of 2 hours at 250.degree. C., GLC analysis of the principal reaction products was as follows: Component       Millimoles ______________________________________ dimethylether   .23 methanol        8.97 methylethylether .1 ethanol         2.55 n-propanol      .59 ______________________________________

As shown in these data, alcohols, especially methanol, predominated in the reaction mixture.

## Claims

1. A process for forming acetaldehyde in a first stage reaction and then reducing said aldehyde to form ethanol in a second stage reaction which comprises reacting carbon monoxide and hydrogen at a temperature of from about 150.degree. to about 300.degree. C. and superatmospheric pressure in the presence of a catalyst system comprising (a) a preformed ruthenium carbonyl complex or a ruthenium carbonyl complex formed in situ by reaction between ruthenium metal and carbon monoxide or a ruthenium compound which undergoes reaction with carbon monoxide to provide said ruthenium carbonyl complex and (b) a source of halide anion, said catalyst system being present at least during said first reaction stage.

2. A process according to claim 1 wherein said ruthenium carbonyl complex is present during said second stage reaction.

3. A process according to claim 1 wherein a hydrogenation catalyst is present during said second stage reaction.

4. A process according to claim 3 wherein said ruthenium carbonyl complex is removed from the first reaction stage product prior to said second stage reaction.

5. A process according to claim 3 wherein said hydrogenation catalyst comprises palladium.

6. A process according to claim 1 wherein said first and second stage reactions are conducted at a temperature of from about 175.degree. to about 275.degree. C.

7. A process for producing acetaldehyde and/or ethanol which comprises reacting carbon monoxide and hydrogen at a temperature of from about 150.degree. to 300.degree. C. and superatmospheric pressure in the presence of a catalyst system comprising (a) a preformed carbonyl complex or a ruthenium carbonyl complex formed in situ by reaction between ruthenium metal and carbon monoxide or a ruthenium compound which undergoes reaction with carbon monoxide to provide said ruthenium carbonyl complex and (b) a source of halide anion, and recovering acetaldehyde and/or ethanol from said reaction.

8. A process according to claim 7 wherein said temperature is in the range of from about 175.degree. to about 275.degree. C. and said pressure is in the range of from about 150 to about 600 atmospheres.

9. A process according to claim 7 wherein the source of halide ion is an alkali metal chloride, bromide or iodide.

10. A Process according to claim 7 wherein the source of halide ion is hydrogen chloride or hydrogen bromide.

11. A process according to claim 7 wherein the molar ratio of hydrogen to carbon monoxide is from about 1/10 to about 10/1.

12. A process according to claim 9 wherein the alkali metal is lithium.

13. A process according to claim 7 wherein the reaction is carried out in the presence of a solvent comprising an aprotic organic amide.

14. A process according to claim 13 wherein the solvent comprises an N-lower alkyl pyrrolidin-2-one.

15. A process according to claim 13 wherein the solvent comprises an N,N-di(lower alkyl)acetamide.

16. A process according to claim 13 wherein the solvent comprises N-methyl pyrrolidin-2-one.

17. A process according to claim 13 wherein the solvent comprises N,N-diethyl acetamide.

18. A process according to claim 13 wherein the solvent comprises N,N-diethyl propionamide.

19. A process for producing ethanol and/or acetaldehyde by reacting carbon monoxide and hydrogen in a solvent comprising an aprotic organic amide at a temperature of from about 150.degree. to about 300.degree. C. and superatmospheric pressure in the presence of a catalyst system comprised of ruthenium in complex combination with carbon monoxide and a halide ligand as catalyst therefor and recovering ethanol and/or acetaldehyde.

20. A process according to claim 19 wherein the solvent comprises an N-lower alkyl pyrrolidin-2-one.

21. A process according to claim 19 wherein the solvent comprises N-methyl pyrrolidin-2-one.

22. A process according to claim 19 wherein the temperature is from about 175.degree. to about 275.degree. C. and the pressure is from about 150 to about 600 atmospheres.

23. The process according to claim 1 wherein said source of ruthenium carbonyl complex and said source of halide ion are present as a ruthenium halocarbonyl complex of the formula Ru.sub.a (CO).sub.b X.sub.c in which a, b and c are integers and X is halide.

24. The process according to claim 23 wherein the source of said halide anion is an alkali metal halide.

25. The process according to claim 24 wherein ruthenium metal and carbon monoxide or ruthenium compound capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex, and alkali metal halide, react to provide an alkali ruthenium halocarbonyl complex of the formula M.sub.a Ru.sub.b X.sub.c (CO).sub.d in which M is alkali metal, X is halogen and a, b, c and d are integers.

26. The process according to claim 1 wherein the ruthenium compound capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex and the source of halide anion is ruthenium chloride.

27. The process according to claim 23 wherein the ruthenium compound capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex and the source of halide anion is ruthenium chloride.

28. The process according to claim 25 wherein the ruthenium compound capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex and the source of halide anion is ruthenium chloride.

29. The process according to claim 1 wherein the the ruthenium compound capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex is ruthenium acetylacetonate and the source of halide anion is hydrogen halide.

30. The process according to claim 23 wherein said ruthenium halocarbonyl complex is preformed.

31. The process according to claim 25 wherein said alkali ruthenium halocarbonyl complex is preformed.

32. The process according to claim 1 wherein the ruthenium salt capable of undergoing reaction with carbon monoxide to provide ruthenium carbonyl complex is ruthenium halide and the source of halide anion is a halide other than ruthenium halide.

33. The process according to claim 32 wherein the catalyst system comprises ruthenium halocarbonyl and an alkali metal halide.

34. The process of claim 1 wherein said halide source is a quaternary ammonium halide.

35. The process of claim 34 wherein said halide source is tetramethylammonium bromide.

36. The process of claim 1 wherein said halide anion source is a halide of a Group III b or lanthanide metal.

37. The process of claim 1 wherein said halide anion is a chloride or bromide of a Group III b or lanthanide metal.

38. The process of claim 1 wherein said halide anion is a halide of scandium, yttrium, lanthanum or neodymium.

39. The process of claim 1 wherein said halide anion is a chloride or bromide of scandium, yttrium, lanthanum or neodynium.

40. The process of claim 1 wherein a phosphorus-containing ligand is also present in the reaction medium.

41. The process of claim 1 wherein bis(triphenylphosphine)iminium halide is present in the reaction medium.

42. The process of claim 1 carried out in the presence of a mixed solvent system containing a major amount of an aprotic solvent and a minor amount of a tertiary amine.

43. The process of claim 42 wherein the catalyst system comprises ruthenium halocarbonyl.

44. The process of claim 43 wherein the mixed solvent system contains a major amount of gamma-butyrolactone and a minor amount of N-methylpyrrolidine.

45. The process of claim 42 wherein a co-promoting amount of alkali metal halide is present.

46. The process of claim 45 wherein the alkali metal co-promoter is lithium bromide.