CA1190565A - Catalytic hydrogenation of di(4-aminophenyl)methane - Google Patents
Catalytic hydrogenation of di(4-aminophenyl)methaneInfo
- Publication number
- CA1190565A CA1190565A CA000400847A CA400847A CA1190565A CA 1190565 A CA1190565 A CA 1190565A CA 000400847 A CA000400847 A CA 000400847A CA 400847 A CA400847 A CA 400847A CA 1190565 A CA1190565 A CA 1190565A
- Authority
- CA
- Canada
- Prior art keywords
- methane
- weight
- aminophenyl
- trans
- amount
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/68—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton
- C07C209/70—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton by reduction of unsaturated amines
- C07C209/72—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton by reduction of unsaturated amines by reduction of six-membered aromatic rings
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
Abstract
CATALYTIC HYDROGENATION OF
DI(4-AMINOPHENYL)METHANE
ABSTRACT OF THE DISCLOSURE
The present invention relates to an improved proc-ess for the catalytic hydrogenation of di(4-aminophenyl) methane to a liquid di(4-aminocyelohexyl) methane mixture containing from 15 to 40% by weight of the trans, trans isomer. The invention resides in the use of a ruthenium-on-alumina catalyst, the use of an aliphatic alcohol during hydrogenation and the use of ammonia during hydro-genation, with the hydrogenation being conducted under specific process conditions. The hydrogenation reaction is conducted for no more than about sixty minutes at a temperature of from 150 to 217°C and at a hydrogen pres-sure of at least 500 psi.
DI(4-AMINOPHENYL)METHANE
ABSTRACT OF THE DISCLOSURE
The present invention relates to an improved proc-ess for the catalytic hydrogenation of di(4-aminophenyl) methane to a liquid di(4-aminocyelohexyl) methane mixture containing from 15 to 40% by weight of the trans, trans isomer. The invention resides in the use of a ruthenium-on-alumina catalyst, the use of an aliphatic alcohol during hydrogenation and the use of ammonia during hydro-genation, with the hydrogenation being conducted under specific process conditions. The hydrogenation reaction is conducted for no more than about sixty minutes at a temperature of from 150 to 217°C and at a hydrogen pres-sure of at least 500 psi.
Description
-1 Mo-2230 CATALYTIC HYDROGENATION OF
DI(4-AMINORHENYL)METHANE
BACKGROUND OF THE INVENTION
In the production of di(4-aminocyclohexyl) methane by the catalytic hydrogenation of di(4-aminophenyl)methane, essentially three skereoisomers are produced:
DI(4-AMINORHENYL)METHANE
BACKGROUND OF THE INVENTION
In the production of di(4-aminocyclohexyl) methane by the catalytic hydrogenation of di(4-aminophenyl)methane, essentially three skereoisomers are produced:
2 ~ ~ CH2 ~ ~ WH2 CIS CIS
2 ~ / 2 ~ IH~2 CIS TRANS
H ~ CH2 \ / H
TRANS TRANS
It is known in the art that in order to produce a corresponding isocyanate (via the known phosgena-tion process) which is liquid and storage stable at room temperature (i.e., from 20 to 25C), the mixture of amine stereoisomers used for phosgenation must contain the trans, trans stereoisomer in relatively narrow amounts (typically from 15 to 40~ by weight).
Mo-2230 ~9~
Numerous techniques are known in the art for the production of amine mixtures containing the requisite amount of the trans, trans isomer. Typical of these known techniques are those described in U.S.
Patent Numbers 3,153,088; 3,155,724; 3,393,236;
2 ~ / 2 ~ IH~2 CIS TRANS
H ~ CH2 \ / H
TRANS TRANS
It is known in the art that in order to produce a corresponding isocyanate (via the known phosgena-tion process) which is liquid and storage stable at room temperature (i.e., from 20 to 25C), the mixture of amine stereoisomers used for phosgenation must contain the trans, trans stereoisomer in relatively narrow amounts (typically from 15 to 40~ by weight).
Mo-2230 ~9~
Numerous techniques are known in the art for the production of amine mixtures containing the requisite amount of the trans, trans isomer. Typical of these known techniques are those described in U.S.
Patent Numbers 3,153,088; 3,155,724; 3,393,236;
3,644,522; 3,711,550 and 3,766,272. These known techniques generally require the separation of an amine mixture containing the re~uisite amount of the trans, trans isomer from an amine mixture formed after hydrogenation and containing around 50% by weight of the trans, trans isomer. Processes are known in the art for the production of a di(4-aminocyclohexyl)methane mixture containing the requisite amount of the trans, trans isomer directly rom di(4-aminophenyl)methane without the need for an inter-mediate separation step (see, e.g., U.S. Patent Number 2,606,928); however, ~he rates of reaction are much too slow for commercial application.
Numerous processes are known in the art for the production of di~4-aminocyclohexyl)methane from di(4-aminophenyl)methane via catalytic hydrogenation using supported and unsupported ruthenium catalysts.
Typical of these processes are those disclosed in U.S. Patent Numbers 2,494,563; 2,606,924; 2,606,928;
2,606,925; 3,347,917; 3,676,495; 3,959,374; 3,743,677;
3,914,307; 3,825,586; 3,636,108 and 4,161,492. While some of these processes yield an amine mixture containing the trans, trans isomer in an amount necessary to allow for the production of an isocyanate which is liquid and storage stable at room temperature, the rates of reaction are much too slow for commercial use.
Mo-2230 Ruthenium-based catalysts have also been described as being useful in the hydrogenation of (a) polycycloaromatic polyamines formed from aniline and formaldehyde (see U.S. Patent Number 4,226,737);
(b) 2,4-bis(p-aminobenzyl)aniline (see U.S. Patent Number 3,557,180); (c) 2,4'-diaminodiphenylmethane (see U.S. Patent Number 3,590,002); (d) tolylene diamine/formaldehyde condensates (see U.S. Patent Numbers 3,330,850 and 3,361,~14; and (e) di(4-nitrophenyl)~ethane (see U.S. Patent 3,742,049).However, none of these processes relate to the present problem, i.e., production of a di(4-amino-cyclohexyl)methane containing from 15 to 40~ by weight of the trans, trans isomer.
Finally, the use of a solvent and ammonia during the hydrogenation of di(4-aminophenyl)methane in the presence of a ruthenium catalyst is also known (see, eOg., U.S. Patent Numbers 3,347,917; 3,636,108 and 3,644,522). The '917 patent describes the hydrogenation of di(4-an~inophenyl)methane at temperatures of 180 to 300C and pressures above 500 psi in the presence of ruthenium, ammonia and solvent to obtain a high yield of di(4-aminocyclohexyl) methane rich in trans, trans isomer (i.e., above 45~
by weight). The '108 patent describes the hydrogena-tion of di(4-aminophenyl)methane at temperatures of from 100 to 300C and pressures in excess of 200 psi in the optional presence of ammonia and solvent and in the presence of a supported ruthenium catalyst which has been alkali moderated. In those examples of the '108 patent where the trans, trans content is described as being low (Examples 21, 22 and 27), neither organic solvent nor ammonia were used.
Finally, the '522 patent is similar to the '108 Mo-2230 patent except that the ruthenium catalyst used is supported on a specific substrate. Like the ']08 patent, where the trans, trans content is described as being low (Examples 17, 18 and 19), neither organic solvent nor ammonia were used.
DESCRIPTION OF THE I_VENTION
The present invention is directed to the discovery that liquid d1(4-aminocycloheYyl)methanes containing from 15~ to 40% by weight of the trans, trans isomer can be produced directly from di(4-aminophenyl)methane by hydrogenating in the presence of (i) a ruthenium-on~alumina catalyst, (ii) an aliphatic alcohol, and (iii) ammonia and under specific process conditions. Specifically, the hydrogen pressure must be at least 500 psi, the temperature must be from 150 to 217C, and the time of hydrogenation must not exceed about sixty minutes.
The ruthenium-on-alumina catalysts used in the present invention are well known in the art and are commercially available, and comprise elementary ruthenium deposited on an alumina carrier. The presently preferred catalyst is available from Engelhard and comprises 5~ by weigh~ ruthenium on an alumina carrier.
In conducting the process of the invention, the procedures commonly used in the art are employed, the only requirements being the presence of the alcohol and ammonia and the pressure, temperature and time conditions noted above.
Mo-2230 s The hydrogenation must be conducted in the presence of an aliphatic alcohol. The aliphatic alcohols used in the present invention include any Cl to C10 aliphatic alcohol. Suitable specifl~ d] cohols include methanol, 5 ethanol, n-propanol isopropanol and the like. The presently preferred solvent is methanol. The amount of alcohol must be at least 25% by weight based on the total weight of alcohol and starting diamine. The upper limit on the amount of solvent is dictated by the economics 10 of the process, and will generally not exceed 60% by weight based on the total weight of alcohol and starting diamine. The preferred range of alcohol is from 30% to 50% by weight based on the weight of alcohol and start-ing diamine.
~nonia must also be present during the hydrogen ation reaction. In general, the amount of ammonia used is such that the molar ratio of ammonia to starting diamine is fxom 0.5:1 to 10:1. The ammonia is prefer-ably used in an amount such that the molar ratio noted 20 is from 0.5:1 to 5:1 and most preferably about 1:1.
The higher amounts of ammonia noted are not generally preferred since higher pressures are generally neces-sary.
The amount of catalyst employed is such that the 25 amount of ruthenium is at least 0.05% by weight of the starting diamine, is preferably from 0.1% to 3% by ~eight, and is most preferably from 0.1% to I% by weight.
As noted~ the amount of catalyst should be at least 0.05~. Economics generally dictate the upper limit 30 since the catalyst is relatively expensive and since little practical advantage is gained by using relatively large amounts.
In general, the materials are mixed and added to the reactor in a batch process but, of course, a 35 continuous process ~ould also be used.
Mo-2230 ~6--The hydrogenation is conducted at a -temperature of from 150 to 217C, and preferably from 170 to 200C
The exact choice of temperatl7re in any given instance is a function of the reaction rate and the trans, trans content desired. In general, the higher the temperature, the faster the reaction rate and the higher the trans, trans content of the final product.
Thus, the tempexaturP will be generally selected within the range noted to yield the best balance of reaction time and trans, trans content.
The hydrogenation pressure employed in the process of the invention must be maintained at at least 500 psi, and will generally be from about 1500 psi to 4000 psi. of course, the pressures used are dependent on the equipment used and could be as high as 8000 psi or higher. In general r it has been found that the yield will increase with increasing pressure.
The progress of the hydrogenation reaction is followed readily by observation of the amount of hydrogen taken up by the reaction mixture and the hydrogenation is terminated at the point at which the theoretical quantity of hydrogen has been absorbed. In general, under the conditions noted, the total hydrogenation time will not exceed about sixty minutes and will typically be from about lO
to 50 minutes. Longer reaction times, particularly at higher temperatures, yenerally causes an increase in the trans, trans content. Following hydrogena-tion, the catalyst is separated from the solution of reduced material and the material is distilled to isolate the di(4-aminocyclohexyl)mathane.
Mo-2230 The invention is further illustrated, but is not intended to be limited by the following examples in which all parts and percentages are by weight unless other specified.
EXAMPLES
200 parts of di(4-aminophenyl)methane, 200 parts of a methyl alcohol solution which contained about 16 parts of ammonia, and the amount of catalyst noted in Table 1 were added to a high pressure autoclave.
The catalyst used was an Engelhard ruthenium-on-alumina catalyst containing 5~ ruthenium. The auto~
clave was sealed and pressurized to the pressure noted in Table 1, and the contents were heated to the temperatures noted in Table 1. The hydrogenation times were as set forth in Table 1. The contents of the autoclave were removed and vacuum filtered and then distilled to strip off the methyl alcohol and low boiling products. The resultant hydrogenated products (taken as overhead) were then analy~ed for yield and trans, trans content wlth the results being set forth in Table 1. Examples 6 and 11 through 14 are comparison examples and do fall under the scope of the present invention.
Mo-2230 ~J
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Mo-2230
Numerous processes are known in the art for the production of di~4-aminocyclohexyl)methane from di(4-aminophenyl)methane via catalytic hydrogenation using supported and unsupported ruthenium catalysts.
Typical of these processes are those disclosed in U.S. Patent Numbers 2,494,563; 2,606,924; 2,606,928;
2,606,925; 3,347,917; 3,676,495; 3,959,374; 3,743,677;
3,914,307; 3,825,586; 3,636,108 and 4,161,492. While some of these processes yield an amine mixture containing the trans, trans isomer in an amount necessary to allow for the production of an isocyanate which is liquid and storage stable at room temperature, the rates of reaction are much too slow for commercial use.
Mo-2230 Ruthenium-based catalysts have also been described as being useful in the hydrogenation of (a) polycycloaromatic polyamines formed from aniline and formaldehyde (see U.S. Patent Number 4,226,737);
(b) 2,4-bis(p-aminobenzyl)aniline (see U.S. Patent Number 3,557,180); (c) 2,4'-diaminodiphenylmethane (see U.S. Patent Number 3,590,002); (d) tolylene diamine/formaldehyde condensates (see U.S. Patent Numbers 3,330,850 and 3,361,~14; and (e) di(4-nitrophenyl)~ethane (see U.S. Patent 3,742,049).However, none of these processes relate to the present problem, i.e., production of a di(4-amino-cyclohexyl)methane containing from 15 to 40~ by weight of the trans, trans isomer.
Finally, the use of a solvent and ammonia during the hydrogenation of di(4-aminophenyl)methane in the presence of a ruthenium catalyst is also known (see, eOg., U.S. Patent Numbers 3,347,917; 3,636,108 and 3,644,522). The '917 patent describes the hydrogenation of di(4-an~inophenyl)methane at temperatures of 180 to 300C and pressures above 500 psi in the presence of ruthenium, ammonia and solvent to obtain a high yield of di(4-aminocyclohexyl) methane rich in trans, trans isomer (i.e., above 45~
by weight). The '108 patent describes the hydrogena-tion of di(4-aminophenyl)methane at temperatures of from 100 to 300C and pressures in excess of 200 psi in the optional presence of ammonia and solvent and in the presence of a supported ruthenium catalyst which has been alkali moderated. In those examples of the '108 patent where the trans, trans content is described as being low (Examples 21, 22 and 27), neither organic solvent nor ammonia were used.
Finally, the '522 patent is similar to the '108 Mo-2230 patent except that the ruthenium catalyst used is supported on a specific substrate. Like the ']08 patent, where the trans, trans content is described as being low (Examples 17, 18 and 19), neither organic solvent nor ammonia were used.
DESCRIPTION OF THE I_VENTION
The present invention is directed to the discovery that liquid d1(4-aminocycloheYyl)methanes containing from 15~ to 40% by weight of the trans, trans isomer can be produced directly from di(4-aminophenyl)methane by hydrogenating in the presence of (i) a ruthenium-on~alumina catalyst, (ii) an aliphatic alcohol, and (iii) ammonia and under specific process conditions. Specifically, the hydrogen pressure must be at least 500 psi, the temperature must be from 150 to 217C, and the time of hydrogenation must not exceed about sixty minutes.
The ruthenium-on-alumina catalysts used in the present invention are well known in the art and are commercially available, and comprise elementary ruthenium deposited on an alumina carrier. The presently preferred catalyst is available from Engelhard and comprises 5~ by weigh~ ruthenium on an alumina carrier.
In conducting the process of the invention, the procedures commonly used in the art are employed, the only requirements being the presence of the alcohol and ammonia and the pressure, temperature and time conditions noted above.
Mo-2230 s The hydrogenation must be conducted in the presence of an aliphatic alcohol. The aliphatic alcohols used in the present invention include any Cl to C10 aliphatic alcohol. Suitable specifl~ d] cohols include methanol, 5 ethanol, n-propanol isopropanol and the like. The presently preferred solvent is methanol. The amount of alcohol must be at least 25% by weight based on the total weight of alcohol and starting diamine. The upper limit on the amount of solvent is dictated by the economics 10 of the process, and will generally not exceed 60% by weight based on the total weight of alcohol and starting diamine. The preferred range of alcohol is from 30% to 50% by weight based on the weight of alcohol and start-ing diamine.
~nonia must also be present during the hydrogen ation reaction. In general, the amount of ammonia used is such that the molar ratio of ammonia to starting diamine is fxom 0.5:1 to 10:1. The ammonia is prefer-ably used in an amount such that the molar ratio noted 20 is from 0.5:1 to 5:1 and most preferably about 1:1.
The higher amounts of ammonia noted are not generally preferred since higher pressures are generally neces-sary.
The amount of catalyst employed is such that the 25 amount of ruthenium is at least 0.05% by weight of the starting diamine, is preferably from 0.1% to 3% by ~eight, and is most preferably from 0.1% to I% by weight.
As noted~ the amount of catalyst should be at least 0.05~. Economics generally dictate the upper limit 30 since the catalyst is relatively expensive and since little practical advantage is gained by using relatively large amounts.
In general, the materials are mixed and added to the reactor in a batch process but, of course, a 35 continuous process ~ould also be used.
Mo-2230 ~6--The hydrogenation is conducted at a -temperature of from 150 to 217C, and preferably from 170 to 200C
The exact choice of temperatl7re in any given instance is a function of the reaction rate and the trans, trans content desired. In general, the higher the temperature, the faster the reaction rate and the higher the trans, trans content of the final product.
Thus, the tempexaturP will be generally selected within the range noted to yield the best balance of reaction time and trans, trans content.
The hydrogenation pressure employed in the process of the invention must be maintained at at least 500 psi, and will generally be from about 1500 psi to 4000 psi. of course, the pressures used are dependent on the equipment used and could be as high as 8000 psi or higher. In general r it has been found that the yield will increase with increasing pressure.
The progress of the hydrogenation reaction is followed readily by observation of the amount of hydrogen taken up by the reaction mixture and the hydrogenation is terminated at the point at which the theoretical quantity of hydrogen has been absorbed. In general, under the conditions noted, the total hydrogenation time will not exceed about sixty minutes and will typically be from about lO
to 50 minutes. Longer reaction times, particularly at higher temperatures, yenerally causes an increase in the trans, trans content. Following hydrogena-tion, the catalyst is separated from the solution of reduced material and the material is distilled to isolate the di(4-aminocyclohexyl)mathane.
Mo-2230 The invention is further illustrated, but is not intended to be limited by the following examples in which all parts and percentages are by weight unless other specified.
EXAMPLES
200 parts of di(4-aminophenyl)methane, 200 parts of a methyl alcohol solution which contained about 16 parts of ammonia, and the amount of catalyst noted in Table 1 were added to a high pressure autoclave.
The catalyst used was an Engelhard ruthenium-on-alumina catalyst containing 5~ ruthenium. The auto~
clave was sealed and pressurized to the pressure noted in Table 1, and the contents were heated to the temperatures noted in Table 1. The hydrogenation times were as set forth in Table 1. The contents of the autoclave were removed and vacuum filtered and then distilled to strip off the methyl alcohol and low boiling products. The resultant hydrogenated products (taken as overhead) were then analy~ed for yield and trans, trans content wlth the results being set forth in Table 1. Examples 6 and 11 through 14 are comparison examples and do fall under the scope of the present invention.
Mo-2230 ~J
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Mo-2230
Claims (13)
1. A process for the catalytic hydrogenation of di(4-aminophenyl)methane to a liquid di(4-aminocyclo-hexyl)methane containing from 15% to 40% by weight of the trans, trans isomer comprising hydrogenating di(4-aminophenyl)methane in the presence of (i) a ruthenium-on-alumina catalyst, (ii) at least 25% by weight of an aliphatic alcohol, based on the weight of the total weight of the di(4-aminophenyl)methane and the alcohol, and (iii) ammonia, the amount of ammonia present being such that the mol ratio of ammonia to di(4-aminophenyl) methane is from 0.5:1 to 10:1, the hydrogenation being conducted at a hydrogen pressure of at least 500 psi, at a temperature of from 150°C to 217°C, and for a time not exceeding sixty minutes.
2. The process of Claim 1 wherein said alcohol contains from 1 to 10 carbon atoms.
3. The process of Claim 2, wherein said alcohol is methanol.
4. The process of Claim 1 wherein the amount of alcohol is from 25 to 60% by weight.
5. The process of Claim 4 wherein the amount of alcohol is from 30 to 50% by weight.
6. The process of Claim 1 wherein said mol ratio is from 0.5:1 to 5:1.
7. The process of Claim 6 wherein said mol ratio is about 1:1.
8. The process of Claim 1 wherein the amount of said catalyst is such that the amount of ruthenium is at least 0.05% by weight of the di(4-aminophenyl) methane.
9. The process of Claim 8 wherein the amount of ruthenium is from 0.1 to 3% by weight of the di(4-amino-phenyl)methane.
10. The process of Claim 9 wherein the amount of ruthenium is from 0.1 to 1% by weight of the di(4-amino-phenyl)methane.
11. The process of Claim 1 wherein the temperature is from 170 to 200°C.
12. The process of Claim 1 wherein the pressure is at least 1500 psi.
13. The process of Claim 1 wherein said time is between ten and fifty minutes.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US269,200 | 1981-06-01 | ||
| US06/269,200 US4394523A (en) | 1981-06-01 | 1981-06-01 | Catalytic hydrogenation of di (4-aminophenyl) methane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1190565A true CA1190565A (en) | 1985-07-16 |
Family
ID=23026227
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000400847A Expired CA1190565A (en) | 1981-06-01 | 1982-04-13 | Catalytic hydrogenation of di(4-aminophenyl)methane |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US4394523A (en) |
| EP (1) | EP0066210B1 (en) |
| JP (1) | JPS57203043A (en) |
| CA (1) | CA1190565A (en) |
| DE (1) | DE3260105D1 (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4448995A (en) * | 1982-12-13 | 1984-05-15 | Mobay Chemical Corporation | Catalytic hydrogenation of di(4-aminophenyl)methane |
| US4754070A (en) * | 1986-01-23 | 1988-06-28 | Air Products And Chemicals, Inc. | Hydrogenation of methylenedianiline to produce bis(para-aminocyclohexyl)methane |
| US5196594A (en) * | 1988-01-14 | 1993-03-23 | Miles, Inc. | Process for the production of 4,4'-diamino-dicyclohexylmethane with a low trans-trans isomer content by the catalytic hydrogenation of 4,4'-diamino-diphenylmethane |
| US4960941A (en) * | 1988-03-30 | 1990-10-02 | Air Products And Chemicals, Inc. | Hydrogenation of aromatic amines to produce their ring hydrogenated counterparts |
| US5245082A (en) * | 1990-09-06 | 1993-09-14 | Bayer Aktiengesellschaft | Process for the production of di-(4-aminocyclohexyl)-methane containing 15 to 25% by weight of the trans-trans isomer |
| US5214212A (en) * | 1992-02-27 | 1993-05-25 | Olin Corporation | Promoters for hydrogenation of aromatic amines |
| US5550294A (en) * | 1992-02-05 | 1996-08-27 | Olin Corporation | Method of increasing hydrogenation rate of aromatic amines |
| US5364971A (en) * | 1993-08-25 | 1994-11-15 | Texaco Chemical Inc. | Decolorization of polyethylene polyamines using ruthenium |
| DE19533718A1 (en) * | 1995-09-12 | 1997-03-13 | Basf Ag | Process for the hydrogenation of aromatic compounds in which at least one amino group is bonded to an aromatic nucleus |
| DE10119136A1 (en) * | 2001-04-19 | 2002-11-14 | Bayer Ag | Ruthenium catalyst for the hydrogenation of diaminodiphenylmethane to diaminodicyclohexylmethane |
| US7049273B2 (en) * | 2002-07-17 | 2006-05-23 | Afton Chemical Intangibles Llc | Hybridized olefin copolymer additives |
| US7743738B2 (en) * | 2007-03-01 | 2010-06-29 | Afton Chemical Corporation | Scavenging phosphorus, sulfur, and lead from combustion exhaust using tungsten compounds and lubricant |
| US7794512B2 (en) * | 2007-03-16 | 2010-09-14 | Afton Chemical Corporation | Supplying tungsten to a combustion system or combustion system exhaust stream containing iron |
| CN102093227B (en) | 2011-01-07 | 2013-08-07 | 烟台万华聚氨酯股份有限公司 | Method for producing 4,4'-diamino dicyclohexyl methane with low trans-trans isomer content |
| TWI534131B (en) | 2014-11-27 | 2016-05-21 | 財團法人工業技術研究院 | Catalyst and method for hydrogenation of 4,4'-methylenedianiline |
Family Cites Families (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2494563A (en) * | 1947-01-08 | 1950-01-17 | Du Pont | Bis (4-aminocyclohexyl) methane |
| US2606928A (en) * | 1947-11-18 | 1952-08-12 | Du Pont | Preparation of amino alicyclic compounds |
| US2606924A (en) * | 1949-06-09 | 1952-08-12 | Du Pont | Bis (4-aminocyclohexyl)-methane |
| US2606925A (en) * | 1949-12-15 | 1952-08-12 | Du Pont | Ruthenium catalyzed hydrogenation process for obtaining aminocyclohexyl compounds |
| US3153088A (en) * | 1961-12-29 | 1964-10-13 | Du Pont | Selective alteration of the ratios of mixtures of bis-(4-aminocyclohexyl) methane isomers |
| US3155724A (en) * | 1961-12-29 | 1964-11-03 | Du Pont | Process for bringing stereoisomeric mixture of bis-(4-aminocyclohexane) methane close to the equilibrium concentration |
| US3347917A (en) * | 1961-12-29 | 1967-10-17 | Du Pont | Process for the preparation of di (paraaminocyclohexyl) methane |
| US3361814A (en) * | 1964-09-18 | 1968-01-02 | Mobay Chemical Corp | Cycloaliphatic tetraamines |
| US3330850A (en) * | 1964-09-18 | 1967-07-11 | Mobay Chemical Corp | Cycloaliphatic tetraisocyanates |
| US3393236A (en) * | 1965-06-09 | 1968-07-16 | Du Pont | Stereoisomeric preparation of bis(p-aminocyclohexyl) methane |
| US3636108A (en) * | 1965-12-23 | 1972-01-18 | Du Pont | Catalytic hydrogenation of aromatic nitrogen containing compounds over alkali moderated ruthenium |
| CH515882A (en) * | 1965-12-23 | 1971-11-30 | Du Pont | 4,4'-Methylene di-(cyclohexylamine) prepn - with control of stereoisomer concn |
| US3590002A (en) * | 1967-07-21 | 1971-06-29 | Mobay Chemical Corp | Mixtures of 2,4'-diisocyanato dicyclohexylmethane with lower aliphatic and cycloaliphatic polyisocyanates |
| US3557180A (en) * | 1968-07-02 | 1971-01-19 | Du Pont | 2,4-bis(isocyanatocyclohexylmethyl) cyclohexyl isocyanate |
| US3644522A (en) * | 1969-04-04 | 1972-02-22 | Du Pont | Catalytic hydrogenation of nitrogen containing compounds over supported ruthenium catalysts |
| JPS4939994B1 (en) * | 1969-10-16 | 1974-10-30 | ||
| US3825586A (en) * | 1969-11-21 | 1974-07-23 | Du Pont | Process for enriching trans-trans salts of bis(4-aminocyclohexyl)methane and 1,12-dodecanedioic acid |
| US3711550A (en) * | 1970-02-16 | 1973-01-16 | Du Pont | Isomerization of 4,4'-methylenedi (cyclohexylamine) over moderated ruthenium catalyst |
| US3676495A (en) * | 1970-09-16 | 1972-07-11 | Du Pont | 2,4-bis(4-aminocyclohexylmethyl)cyclohexylamine |
| US3743677A (en) * | 1971-08-03 | 1973-07-03 | Basf Ag | Continuous manufacture of bis(aminocyclohexyl)-alkanes or bis(aminocyclohexyl)ethers |
| US3766272A (en) * | 1972-08-25 | 1973-10-16 | Du Pont | 4,4'-methylenedi(cyclohexylamine)isomerization over a supported catalyst |
| US3856862A (en) * | 1973-06-25 | 1974-12-24 | Upjohn Co | Process for hydrogenation of di(4-aminophenyl)methane with a rhodium catalyst |
| US3914307A (en) * | 1973-12-27 | 1975-10-21 | Universal Oil Prod Co | Hydrogenation of aromatic amines |
| US3959374A (en) * | 1974-05-30 | 1976-05-25 | Jefferson Chemical Company, Inc. | Process for the preparation of mixed isomeric methylene-bridged polycyclohexylpolyamines |
| US4161492A (en) * | 1975-01-24 | 1979-07-17 | Bayer Aktiengesellschaft | Cycloaliphatic amines and process for preparing same |
| US4226737A (en) * | 1977-11-10 | 1980-10-07 | Milliken Research Corporation | Polycycloaliphatic polyamines |
-
1981
- 1981-06-01 US US06/269,200 patent/US4394523A/en not_active Expired - Lifetime
-
1982
- 1982-04-13 CA CA000400847A patent/CA1190565A/en not_active Expired
- 1982-05-21 DE DE8282104441T patent/DE3260105D1/en not_active Expired
- 1982-05-21 EP EP82104441A patent/EP0066210B1/en not_active Expired
- 1982-05-28 JP JP57090053A patent/JPS57203043A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| US4394523A (en) | 1983-07-19 |
| EP0066210A1 (en) | 1982-12-08 |
| EP0066210B1 (en) | 1984-04-11 |
| DE3260105D1 (en) | 1984-05-17 |
| JPS57203043A (en) | 1982-12-13 |
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