Patent Application
20090171125
1. Field of the Invention
The present invention relates to a hydroformylation process of cyclic olefins in the presence of a metal catalyst, and in particular relates to the separation of the desired products from the metal catalyst by phase separation.
2. Description of the Related Art
It is known in the art that compared to a heterogeneous catalyst, the homogeneous catalyst has advantages such as high reactivity, high selectivity, and a relatively milder reaction condition. However, many homogeneous catalyst systems cannot be commercially applied mainly due to difficulties in separating, recovering, and reusing the homogeneous catalysts, as it is well known.
It is known in the art that distillation is one of the favorable methods for the separation of catalysts and products. If the volatility of the product is low, the temperature required to separate the product by distillation should be higher. Most homogeneous catalysts, however, are thermal sensitive, such that the homogeneous catalyst may decompose during higher distillation temperatures and fail to be recovered for reuse. Other methods for recovering the homogeneous catalyst, e.g. chromatography, are inefficient. Accordingly, an effective and low cost separation process is critical for development of the homogeneous catalyst.
Hydroformylation of olefins with carbon monoxide (hereinafter CO) and hydrogen (hereinafter H2) to form aldehydes is an important homogeneous catalytic reaction. The catalysts used for the hydroformylation of olefins are usually rhodium or cobalt catalysts, especially the rhodium catalysts due to their high reactivity and selectivity. Although rhodium catalysts have higher reactivity, their cost is much higher than the cobalt catalysts. The effective recovery and reuse of the rhodium catalysts determines their realization in the industry. If the volatility of the hydroformylation products(less than C5) is relatively low, the low temperature distillation method can be used to separate the products and the catalysts without significantly decomposing the catalysts. On the other hand, if the volatility of the hydroformylation products is high, the abovementioned distillation method for separation is unfavorable, due to the higher temperatures decomposing the catalyst such that the catalyst cannot be recovered and reused, thus increasing costs.
As described above, the products from hydroformylation of cyclic olefins have a higher boiling point. If the product and catalyst are separated by vacuum distillation, a higher distillation temperature is needed, thereby decomposing the rhodium catalyst. In WO 93/02024, a mixture of first alcohol having 1 to 3 carbon atoms and water is reported to be used as an extraction solution to separate the rhodium catalyst and high boiling-point aldehydes from hydroformylation. The efficiency of this method is, however, not good, and a better method for the efficient separation of the hydroformylation products and catalyst is still needed.
The invention provides a hydroformylation process, comprising: (i) Reacting a cyclic olefin compound with carbon monoxide and hydrogen in a solvent in the presence of a metal-organophosphorus ligand complex catalyst, optionally free organophosphorus ligand to obtain a hydroformylation product liquid containing cycloalkyl aldehydes; (ii) Mixing the hydroformylation product liquid with an extraction liquid comprising a first cycloalkyl alcohol, and allowing the resultant mixture to separate into a first layer and a second layer, and a substantial part of the first layer comprises the rhodium catalyst and a substantial part of the second layer comprises the first cycloalkyl alcohol and the cycloalkyl aldehyde; and (iii) Separating the first layer from the second layer.
A detailed description is given in the following embodiments.
The following description is of the best-contemplated mode of carrying out the invention. This description is made for the purpose of illustrating the general principles of the invention and should not be taken in a limiting sense. The scope of the invention is best determined by reference to the appended claims.
The invention provides a hydroformylation process. First, a rhodium compound and an organophosphorus compound are mixed in an appropriate solvent. The rhodium compound includes rhodium trichloride hydrate (RhCl3.xH2O), dicarbonyl acetylacetone rhodium (Rh(acac)(CO)2), bis(dicarbonyl chloro rhodium ((RhCl(CO)2)2), carbonyl rhodium (Rh6(CO)16 or R4(CO)12), rhodium (III) nitrate (Rh(NO3)3, and the likes. The rhodium catalyst solution has a concentration of 10 ppm to 1000 ppm, and preferably 100 ppm to 600 ppm. The organophosphorous compound can be any phosphorous-containing organics, such as tris(2,4-di-tert-butylphenyl)phosphite, triphenylphosphite, tris(3-methyl-6-tert-butylphenyl)phosphite, tris(2,4-di-tert-butylphenyl)phosphate, di(2-tert-butylphenyl)-tert-butylphosphite, trialkyl phosphine or other suitable phosphorous-containing organics. The rhodium compound and the organophosphorous compound have a molar ratio of 1:1 to 1:300, and preferably 1:10 to 1:150. The solvent used for the catalytic reactions can be alkane, cycloalkane, or other solvent with low polarity. In one embodiment, the solvent is methyl cyclohexane.
The described rhodium catalyst solution is charged in a high pressure reaction vessel, and then added a cyclic olefin to undergo a hydroformylation reaction under high pressure of H2 and CO to obtain the cycloalkyl aldehyde product. The molar ratio of H2 and CO in this reaction is 1:10 to 10:1, and preferably of 1:3 to 3:1. The reaction temperature is at 40° C. to 160° C., and preferably 70° C. to 140° C. The pressure of the H2 and CO is bet 0.5 MPa and 15 MPa, and preferably 2 MPa to 10 MPa. The cyclic olefin may have one carbon-carbon double bond or multiple carbon-carbon double bonds, such as dicyclopentadiene (hereinafter DCPD), tricyclepentadiene (hereinafter TCPD), dicyclohexadiene (hereinafter DCHD), cylcohexene, cyclohexene-1-carbaldehyde, (abbreviated CHCA), 1,2,3,6-tetrahydrobenzaldehyde,or other cyclic olefin such asmethy-3-cyclohexene-1-carboxaldehyde, methy-4-cyclohexene-2-carboxaldehyde, 3-cyclohexene-1-carbonitrile, 3-cyclohexene-1-methanol, methyl 3-cyclohexene-1-carboxylate, 3-cyclohexene-1-carboxylate, 4-acetyl-1-cyclohexene, 1-methyl-4-cyclohexene-2-carboxylate, 1-phenyl-4-cyclohexene-2-carboxaldehyde, 1,2,3,6-tetrahydrophthalic anhydride.
The cycloalkyl aldehydes formed from cyclic olefins such as DCPD, TCPD, DCHD, cyclohexene, CHCA by hydroformylation reactions are shown in Formulae 1-8.
The R in Formula 8 can be hydrogen or a substituent selected from alkyl, alcohol, aldehyde, carboxylic acid, or other functional groups.
After the hydroformylation reaction process, the resulting hydroformylation product liquid was mixed with an extraction liquid including a cycloalkyl alcohol. Subsequently, the mixture was divided into two layers. One layer was substantial of the rhodium catalyst, and another layer was substantial of the extraction liquid and the clcloalkyl aldehyde product. The described two layers were separated to complete the so-called separation of the cycloalkyl aldehyde and the rhodium catalyst solution. Not that the cycloalkyl alcohol of the extraction liquid may have one or multiple alcohol functional groups.
The separated rhodium catalyst solution can be added another cyclic olefin to undergo another hydroformylation reaction. The separation method described recovers and reuses the rhodium catalyst, and efficiently separates the rhodium catalyst solution and the clcloalkyl aldehyde with high boiling point. The clcloalkyl aldehyde dissolved in the extraction liquid including the cycloalkyl alcohol, can be further hydrogenated under high pressure of H2. This hydrogenation reaction can be carried out at 40° C. to 200° C., and preferably 60° C. to 180° C. The pressure of H2 for the reaction is from 0.1 MPa to 10 MPa, and preferably from 1 MPa to 10 MPa. The metal catalyst used for the hydrogenation reaction can be nickel, cobalt, ruthenium, palladium, rhodium, platinum, copper chromium alloy, copper zinc alloy, and the likes. After the described hydrogenation reaction, the corresponding cycloalkyl alcohols are formed from the cycloalkyl aldehydes dissolved in the extraction liquid. In one embodiment, the hydrogenation product cycloalkyl alcohol serves as the extraction liquid to separate the rhodium catalyst and the product cycloalkyl aldehyde during the hydroformylation reaction process. Because the extraction liquid and the hydrogenation product are similar, the additional separation step of the extraction liquid and the cycloalkyl aldehyde before subsequent hydrogenation can be eliminated. The cycloalkyl alcohols formed from cycloalkyl aldehydes through the hydrogenation reaction are shown in Formulae 9 to 15.
Rh(acac)(CO)2 (114 mg; 0.435 mmol) and tris(2,4-di-tert-butylphenyl)phosphite (5.625 g; 8.7 mmol) were added into a flask, followed by the addition of dry methylcyclohexane (26 g) in the dry box. A high pressure reaction vessel was heated to 80° C., followed by vacuum and recharging with nitrogen for three times, and cooled to room temperature. The rhodium solution was transferred to the high pressure reaction vessel, and the nitrogen in the high pressure reaction vessel was replaced with a mixture of CO/H2(1:1). The pressure inside the vessel was built-up to 40 atm, the reaction vessel was heated to 100° C., and the pressure was then built to 50 atm.
DCPD (40 g; Fluka) and dry methylcyclohexane (4 g) were weighted and charged into a feeding bottle. The DCPD was then fed into the high pressure reaction vessel (20 mL/hours) from the feeding bottle with a feeding time of about 2 hours. The total pressure of the CO/H2 was maintained at 50 atm, and the reaction temperature was also maintained at 100±2° C. throughout the reaction. Two hours after the complete of the DCPD feeding, the reaction vessel was cooled to room temperature, and the pressure of the reaction vessel was decreased to the atmospheric pressure. The cycloalkyl alcohol of Formula 9 was then added to the reaction product fluid to be divided into two layers. The layers were separated and then analyzed by a gas chromatograph (GC) and an inductively coupled plasma mass spectrometry (ICP-MS). According to the GC data, the cycloalkyl aldehyde had a yield of 99% and a partition coefficient between the upper and lower layer layers of 15.3. According to the ICP-MS data, the partition coefficient of the rhodium catalyst between the upper and lower layers was 18.5.
The lower layer, substantial of cycloalkyl aldehyde and cycloalkyl alcohol of Formula 9, was added THF (100 g), added ruthenium catalyst (6g; 5 wt % Ru/C; Aldrich), and reacted under 1 MPa H2 at 120° C. for 2 hours to hydrogenate the cycloalkyl aldehyde to obtain a corresponding cycloalkyl alcohol. According to the GC analysis, the product cycloalkyl alcohol had a yield greater than 99%.
While the invention has been described by way of example and in terms of the preferred embodiments, it is to be understood that the invention is not limited to the disclosed embodiments. To the contrary, it is intended to cover various modifications and similar arrangements (as would be apparent to those skilled in the art). Therefore, the scope of the appended claims should be accorded the broadest interpretation so as to encompass all such modifications and similar arrangements.
| Number | Date | Country | Kind |
|---|---|---|---|
| 096151426 | Dec 2007 | TW | national |
