CN100383097C - Method for the hydrodecomposition of ammonium formates in polyol-containing reaction mixtures - Google Patents

Method for the hydrodecomposition of ammonium formates in polyol-containing reaction mixtures Download PDF

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CN100383097C
CN100383097C CNB2004800220241A CN200480022024A CN100383097C CN 100383097 C CN100383097 C CN 100383097C CN B2004800220241 A CNB2004800220241 A CN B2004800220241A CN 200480022024 A CN200480022024 A CN 200480022024A CN 100383097 C CN100383097 C CN 100383097C
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catalyzer
tmp
titanium dioxide
ruthenium
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CN1829674A (en
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M·科赫
A·瓦尔蒂尼
S·马斯
T·西尔希
M·德恩巴赫
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/462—Ruthenium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
    • B01J35/30—
    • B01J35/392—
    • B01J35/615—
    • B01J35/633—
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/06—Washing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/12—Oxidising
    • B01J37/14—Oxidising with gases containing free oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/16—Reducing
    • B01J37/18—Reducing with gases containing free hydrogen

Abstract

Disclosed is a method for removing trialkylammonium formate from methylolalkanes obtained by condensing formaldehyde with a higher aldehyde. The inventive method is characterized in that trialkylammonium formate is decomposed at an increased temperature on a catalyst which is placed on a titanium dioxide support and contains ruthenium in the presence of a gas containing hydrogen. Said method makes it possible to separate the trialkylammonium formate from methylolalkanes produced according to the organic Cannizzaro method and the hydration method.

Description

The method of the ammonium formiate in the reaction mixture that contains polyvalent alcohol is decomposed in hydrogenation
The present invention relates to the organic chemistry industrial circle.More particularly, the invention provides a kind of available hydrogen and divide the method for separating the trialkyl ammonium formiate, this trialkyl ammonium formiate is present in the methylol alkane, and is by being used as the trialkylamine of catalyzer and forming as the formic acid that by product forms in preparation methylol alkanal.
Formaldehyde and the condensation of CH-acid higher alkane aldehyde form methylol alkanal (being generally dihydroxymethyl alkanal and trishydroxymethyl alkanal) and the gained compound is converted into polyvalent alcohol is widely used method in the chemical industry.The example of the important trivalent alcohol that obtains in this way is TriMethylolPropane(TMP), trimethylolethane and tri hydroxy methyl butane, and they are widely used in and produce topcoating, urethane and polyester.Other important compound are by formaldehyde and the obtainable tetramethylolmethane of acetaldehyde condensation and the neopentyl glycol that obtains from isobutyric aldehyde and formaldehyde.The tetravalent alcohol tetramethylolmethane also in being commonly used in topcoating industry, but also very important in producing explosive.
Above-mentioned polyvalent alcohol can prepare by several different methods.A kind of method is the Cannizzaro method, is further divided into inorganic Cannizzaro method and organic C annizzaro method.In inorganic scheme, excess formaldehyde and corresponding alkanal are at the mineral alkali of stoichiometry for example NaOH or Ca (OH) 2There is reaction down.The methylol alkanal that forms in the first step reacted in disproportionation reaction with excess formaldehyde in second step, to form the formate of corresponding polyvalent alcohol and corresponding alkali, i.e. and for example sodium formiate or calcium formiate.
In organic C annizzaro method, use tertiary amine (being generally trialkylamine) to replace described mineral alkali.React as mentioned above, form 1 equivalent ammonium formiate of corresponding amine.Can further handle by suitable method, so that described at least amine can be recovered and return in this reaction.The rough polyvalent alcohol of gained can be handled to obtain purified polyvalent alcohol with several different methods.
A kind of further improvement is that wherein suitable alkanal and formaldehyde are not in stoichiometry at least but (are generally the method for hydrogenation that reacts to each other in the presence of about 5～10mol%) the tertiary amine at catalytic amount.In this method, be reflected at 2, the 2-dihydroxymethyl alkanal stage stops, and is translated into tri methylol alkane by hydrogenation subsequently.Description to effective ways can be found in the applicant's WO 98/28253.
Especially the many conversion scheme to this method for hydrogenation are described in patent application DE-A-2507461, DE-A-2702582, DE-A-2813201 and DE-A-3340791.
Though form the formate of stoichiometry described method for hydrogenation does not advantageously resemble in organic C annizzaro method, the trialkyl ammonium formiate can form as the product of the intersection Cannizzaro reaction that takes place as side reaction on the small degree.
The trialkyl ammonium formiate reacts the tri methylol alkane solution dehydrates or the heating of gained (for example to) under given conditions to form trialkylamine and TriMethylolPropane(TMP) manthanoate.These can reduce the productive rate of tri methylol alkane, and are difficult to separate under the situation that undesirable DeR does not take place.Therefore removing the trialkyl ammonium formiate merits attention especially.
DE 19848569 discloses a kind of decomposition is present in the tertiary amine formate in the tri methylol alkane solution for preparing by organic C annizzaro method as by product method.These formate by heating, preferably the noble metal catalyst of modification exist and super-atmospheric pressure under be decomposed into hydrogen and carbonic acid gas and/or water and carbon monoxide and tertiary amine.The transformation efficiency of formate can not be satisfactory in this method, forms other by product but also observe.
DE 10152525 discloses and decomposed the trialkyl ammonium formiate on heterogeneous catalyst, and this heterogeneous catalyst contains at least a metal in the periodic table of elements 8～12 families, particularly preferably is the catalyzer that contains copper, nickel and/or cobalt that supports.
In addition, aforesaid method is applicable to the effective processing to the trishydroxymethyl alkylating mixture that obtains by following method for hydrogenation only limitedly: wherein only use the trialkylamine of catalytic amount, and therefore described product mixtures also only contains a spot of trialkyl ammonium formiate.
The object of the present invention is to provide a kind of method that is suitable for handling the reaction mixture that obtains by method for hydrogenation and passes through the reaction mixture of organic C annizzaro method acquisition.In addition, this method makes and can decompose the trialkyl ammonium formiate with the transformation efficiency higher than the currently known methods that uses prior art.In addition, this decomposition can produce easy-to-handle and can not cause the degradation production of side reaction with technical scale, thereby the more economical method for preparing high-purity trimethylopropane is provided.
We find, this purpose can realize by a kind of method of removing the trialkyl ammonium formiate from the methylol alkane that formaldehyde and senior aldehyde condensation obtain, this method comprises at elevated temperatures, in the presence of the hydrogen gas, containing and supporting decomposition trialkyl ammonium formiate on the catalyzer of the ruthenium on the titanium dioxide.
The methylol alkane that can handle by the inventive method for example is neopentyl glycol, tetramethylolmethane, TriMethylolPropane(TMP), tri hydroxy methyl butane, trimethylolethane, 2-ethyl-1, ammediol, 2-methyl isophthalic acid, 3-propane-glycol, glycerine, dihydroxy methylpropane, Dipentaerythritol and 1,1-, 1,2-, 1,3-and 1,4 cyclohexane dimethanol.
In the methods of the invention, preferably under hydrogenation conditions, from the tri methylol alkane that makes by described organic C annizzaro method or described method for hydrogenation, remove the trialkyl ammonium formiate.Preferred purifying is by the tri methylol alkane of described method for hydrogenation preparation, and preferred especially TriMethylolPropane(TMP) is designated hereinafter simply as TMP.
The rough TMP that contains the trialkyl ammonium formiate by the preparation of Cannizzaro method has for example done open in DE 19848569.
In described method for hydrogenation, TMP obtains by butyraldehyde-n and formaldehyde condensation and the formed dihydroxymethyl butyraldehyde of subsequent catalytic hydrogenation mixture in the presence of the tertiary amine of catalytic amount.This rough TMP does not contain formate or other impurity that forms of any basic metal or alkaline-earth metal in inorganic Cannizzaro method.Equally, rough TMP only contains trialkyl ammonium formiate or the free trialkylamine of a small amount of about 5～10mol%, and this is different from the product that obtains from organic C annizzaro method.
Contain TriMethylolPropane(TMP) and water from described hydrogenization and to its rough TMP that carries out purification process of the present invention, adduct on TriMethylolPropane(TMP) of line style that methyl alcohol, trialkylamine, trialkyl ammonium formiate, long-chain are arranged together and branching alcohol and dibasic alcohol (for example, methyl butanol or ethyl glycol), formaldehyde and methyl alcohol, acetal be dihydroxymethyl butyraldehyde TMP acetal and two-TMP for example.
Use contains 10～40 weight % TriMethylolPropane(TMP)s, 0～10 weight %2, and 2-dihydroxymethyl butyraldehyde, 0.5～5 weight % methyl alcohol, 0～6 weight % methyl butanol, 1～10 weight % trialkyl ammonium formiate, 0～5 weight %2-ethyl glycol, 0.1～10 weight % higher-boiling compound (for example two-TMP or other adducts) and the rough hydrogenated products of 5～80 weight % water can obtain good result.Rough hydrogenated products with this composition can for example obtain by the method for describing among the WO 98/28253.Carrying out purifying of the present invention with before decomposing described trialkyl ammonium formiate, can be at first by rough hydrogenated products as described in handling as DE-A-199 63 435 embodiment 2 and 3 continuous still batterys of describing.Yet, preferably implement according to the purifying to described rough hydrogenated products of the present invention not carrying out by distillatory under the pretreated situation.
The present invention also provides a kind of catalyzer, it contains the ruthenium that supports on the titanium dioxide molding, this titanium dioxide molding is before shaping or the commercially available titanium dioxide of acid treatment that can be slightly soluble in wherein by the titanium dioxide with 0.1～30 weight % after being shaped obtains, and this catalyzer is used in the inventive method.Ruthenium can be with form of pure metal or as for example oxide compound or the sulfide use of its compound.
Apply the ruthenium of described catalytic activity by known method itself, preferably put on prefabricated TiO as solid support material 2On.
Be preferred for the titania support of described ruthenium-containing catalyst can be described in DE 197 38 464 by before shaping or the back that is shaped use based on titanium dioxide be 0.1～30 weight % as described in the titanium dioxide commercially available titanium dioxide of acid treatment that can be slightly soluble in wherein obtain.The preferred titanium dioxide that uses anatase form.The example of suitable acid is formic acid, phosphoric acid, nitric acid, acetate and stearic acid.
Can use one or more impregnation steps described activeconstituents ruthenium to be put on the titania support that obtains by this way with ruthenium salts solution form.Dry then described impregnated carrier is calcined if necessary.Yet, also can be preferably from the ruthenium salts solution, ruthenium be deposited in as powder and be present on the titanium dioxide in the aq suspension by yellow soda ash.Wash described throw out, drying is calcined if necessary and is shaped.In addition, can for example methyl ethyl diketone ruthenium or ruthenium become gas phase and put on the described carrier with the volatility ruthenium compound with known method (chemical vapour deposition) itself.
The catalyst-loaded of acquisition can be all known finished states in this way.Example is extrusion profile, globe or particle.Before the use, described ruthenium catalyst precursor is by with hydrogen gas, preferably reduce handling more than 100 ℃.Before described catalyzer is used for method of the present invention, preferably under 0～50 ℃, preferred room temperature, make this catalyst deactivation by oxygenous gaseous mixture, preferred air/nitrogen mixture.Described catalyzer can also be installed in the hydrogenation reactor with oxidised form, and can under reaction conditions, make its reduction.
Based on the gross weight of the catalyzer that contains catalytically-active metals and carrier, the ruthenium content of catalyzer of the present invention is 0.1～10 weight %, preferred 2～6 weight %.Based on the gross weight of described catalyzer, the sulphur content of catalyzer of the present invention can be 0.01～1 weight %, measures sulphur by coulometric determination.
Described ruthenium surface-area is 1～20m 2/ g, preferred 5～15m 2/ g, BET surface-area (measuring according to DIN 66131) is 5～500m 2/ g, preferred 50～200m 2/ g.
The pore volume of catalyzer of the present invention is 0.1～1ml/g.In addition, the cutting hardness of described catalyzer is 1～100N.
The above-mentioned ruthenium-containing catalyst that supports on titanium dioxide that is used for decomposing the trialkyl ammonium formiate that is present in rough TMP according to the present invention also is applicable to the precursor (2,2-dihydroxymethyl butyraldehyde) of hydrogenation TMP.
It is economical especially using same catalyst to be used for hydrogenation dihydroxymethyl butyraldehyde and being used to decompose described trialkyl ammonium formiate, because in the case, carry out in the hydrogenation reactor of the method for hydrogenation that the decomposition of trialkyl ammonium formiate can be described in WO 98/28253, and do not need additional reactor.Yet, decompose the trialkyl ammonium formiate by the inventive method and can independently carry out in the reactor equally.
In the methods of the invention, the decomposition of trialkyl ammonium formiate is generally carried out under 100～250 ℃, preferred 120～180 ℃.Used pressure generally is higher than 1 * 10 6Pa is preferably 2 * 10 6～15 * 10 6In the Pa scope.
The inventive method can be carried out continuously or off and on, preferred continuous processing.
In continuous processing, be preferably about 0.05～about 3kg/l catalyzer h, more preferably about 0.1～about 1kg/l catalyzer h from the amount of the rough tri methylol alkane of described method for hydrogenation or organic C annizzaro method.
The inventive method is carried out under hydrogenation conditions,, uses the hydrogenated gas that adds from external source that is.
As hydrogenated gas, can use and contain free hydrogen and do not contain for example any gas of CO of harmful catalyzer poison of measuring.For example, can use waste gas from reformer.The preferred pure hydrogen that uses.
Below by embodiment method of the present invention is described.
Embodiment
I. the method by WO 98,/28 253 prepares rough TMP
Comprise two by upflow tube but interconnective heated and stirred container and total volume are to infeed fresh formalin (aqueous solution of 4300g/l 40% concentration) and butyraldehyde-n (1800g/h) in 72 liters the equipment, and infeed fresh Trimethylamine 99 (130g/h) as catalyzer with the aqueous solution form of 45% concentration.Keep this reactor under 40 ℃.
Output is directly infeeded top with the falling-film evaporator that is placed on top post (11bar heating steam), and under atmospheric pressure it is carried out fractionation, with lower boiling overhead product and the high boiling point bottom product that obtains mainly forming by butyraldehyde-n, ethyl acrylic aldehyde, formaldehyde, water and Trimethylamine 99.
With the overhead product continuous concentration and be recycled in the above-mentioned reactor.
To mix continuously from the high boiling point bottom product (about 33.5kg/h) of described vaporizer and fresh Trimethylamine 99 catalyzer (50g/h, the aqueous solution of 45% concentration), and infeed that random packing and void volume are housed is in 12 liters the heated tubular reactor.Keep this reactor under 40 ℃.
To infeed the top of another distiller from the output of described post-reactor continuously, in other words, remove formaldehyde (11bar heating steam), carry out fractionation there, with lower boiling overhead product and the high boiling point bottom product that obtains mainly forming by ethyl acrylic aldehyde, formaldehyde, water and Trimethylamine 99.With described lower boiling overhead product (27kg/h) continuous concentration and be recycled in first stirred vessel, collect described high boiling point bottom product simultaneously.
The bottom product that obtains in this way mainly is made up of water and dihydroxymethyl butyraldehyde, formaldehyde and trace monomethylol butyraldehyde.Then with its continuous hydrogenation.For this purpose, under 90bar and 115 ℃, this reaction soln of hydrogenation in the main reactor of circulation/downward stream mode operation and the downstream post-reactor operated in a looping fashion.Described catalyzer is to be similar to the method preparation of catalyzer J among the DE 19809418.It contains 40% CuO, 20% Cu and 40% TiO 2Equipment used comprises the long heated main reactor of 10m (internal diameter: 27mm) and the long heated post-reactor (internal diameter: 25mm) of 5.3m.Flow around loop is the liquid of 25l/h, and the charging of setting reactor is 4kg/h.Therefore, take out the hydrogenated products of 4kg/h.Described hydrogenated products has following composition: the TMP of the methyl butanol of the dihydroxymethyl butyraldehyde of the TMP of 22.6 weight %, 1.93 weight %, the methyl alcohol of 1.4 weight %, 1.1 weight %, the ethyl glycol of 0.7 weight %, 1.2 weight % and the adducts of formaldehyde and methyl alcohol,＜the TMP manthanoate of 0.1 weight %, the TMP-dimethyl butyraldehyde acetal of 1.2 weight %, the high boiling product of 2.9 weight %, the trimethylammonium ammonium formiate of 0.57 weight % and the water of 66.2 weight %.
II. the measurement of porosity
Measure the porosity of described catalyzer by mercury penetration method according to DIN 66133.
The measurement of III.BET surface-area
Measure the BET surface-area of described catalyzer according to DIN 66131.
IV. the measurement of cutting hardness
In order to measure cutting hardness, separate sample with cutting unit.The power that cutting unit is applied in order to cut sample is cutting hardness (N (newton)).
V. by the described formate content of ion chromatography measurement
Pass through the described formate content of ion chromatography measurement according to DEV ISO 10304-2.
Embodiment 1:Ru/TiO 2Preparation of catalysts
With 121.3g nitrosyl radical nitric acid ruthenium solution (Ru content: 10.85 weight %) be diluted with water to 90ml.(it is the 1.5mm extrusion profile, and the BET surface-area is 104m with describing the titanium dioxide extrusion profile of producing among 250g such as DE 19738463 embodiment 3 2/ g, porosity is 0.36ml/g) slowly flood with ruthenium solution.Then with the extrusion profile of humidity 100 ℃ dry 2 hours down, 120 ℃ dry 16 hours down.By with the nitrogen of the hydrogen of 10 standard l/h and 10 standard l/h 300 ℃ down reduction reach 4 hours and make this catalyst activation.Then at room temperature by air/this catalyzer of nitrogen mixture passivation.
The Ru content of described finished catalyst extrusion profile is 4.2 weight %, and the BET surface-area is 103m 2/ g, pore volume are 0.26ml/g, and the ruthenium surface-area is 12m 2/ g, cutting hardness are 21.2N.
Embodiment 1～4
The used TMP of preparation as mentioned above has following composition: the TMP of the methyl butanol of the dihydroxymethyl butyraldehyde of the TMP of 22.6 weight %, 1.93 weight %, the methyl alcohol of 1.4 weight %, 1.1 weight %, the ethyl glycol of 0.7 weight %, 1.2 weight % and the adducts of formaldehyde and methyl alcohol,＜the TMP manthanoate of 0.1 weight %, the TMP dimethyl butyraldehyde acetal of 1.2 weight %, the high boiling product of 2.9 weight %, the trimethylammonium ammonium formiate of 0.57 weight % and the water of 66.2 weight %.Under 180 ℃ and 90bar, provide as table 1 in the presence of the catalyzer of prereduction under 180 ° and the 25bar, this crude solution of usefulness hydrogen treat 180ml.After 1 hour, measure the content of dihydroxymethyl butyraldehyde by vapor-phase chromatography.By the described concentration of formate greater of ion-chromatographic determination.Gained is the result be summarized in the table 1.
Figure C20048002202400101
1GC analyzes (anhydrous detection)
2Pass through ion chromatography measurement
3DMB=2, the 2-dimethyl butyraldehyde
From this table as can be seen, under 150 ℃ on ruthenium catalyst used according to the invention with high conversion catalytic decomposition ammonium formiate, these catalyzer are obviously more effective than copper, nickel and cobalt catalyst.Effluent gas analysis shows that methane is the primary product of described formate Decomposition.

Claims (6)

1. method of from the methylol alkane that obtains by formaldehyde and senior aldehyde condensation, removing the trialkyl ammonium formiate, it comprises at elevated temperatures, in the presence of hydrogen gas, containing and supporting decomposition trialkyl ammonium formiate on the catalyzer of the ruthenium on the titanium dioxide.
2. according to the process of claim 1 wherein that the ruthenium content of described catalyzer is 0.1～10 weight %.
3. according to the method for claim 1 or 2, wherein use by before shaping or the titanium dioxide molding that formic acid, phosphoric acid, nitric acid, acetate and the commercially available titanium dioxide of stearic acid treatment obtain that is selected from of back that be shaped with 0.1～30 weight %.
4. according to each method in the claim 1～3, wherein said method is carried out under 100～250 ℃.
5. according to each method in the claim 1～4, wherein said method is 1 * 10 6～15 * 10 6Carry out under the pressure of Pa.
6. according to each method in the claim 1～5, wherein said method is carried out in the hydrogenation reactor of described hydrogenation process.
CNB2004800220241A 2003-07-29 2004-07-07 Method for the hydrodecomposition of ammonium formates in polyol-containing reaction mixtures Expired - Fee Related CN100383097C (en)

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DE10334489A DE10334489A1 (en) 2003-07-29 2003-07-29 Trialkylammonium by-products obtained in methylolalkane products from Cannizzaro or hydrogenation reactions are decomposed using a novel titanium dioxide-supported ruthenium-containing catalyst
DE10334489.6 2003-07-29

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1952738A1 (en) * 1968-12-17 1970-07-09 Leuna Werke Veb Production of trimethylopropane
US4647592A (en) * 1984-01-05 1987-03-03 Exxon Research & Engineering Company Start-up with ruthenium catalysts
US5149861A (en) * 1987-05-06 1992-09-22 Basf Aktiengesellschaft Recovery of trialkylamines and methyl formate from mixtures obtained in the preparation of trimethylolalkanes
US5484757A (en) * 1994-06-02 1996-01-16 Norton Chemical Process Products Corp. Titania-based catalyst carriers
DE19530528A1 (en) * 1995-08-19 1997-02-20 Dornier Gmbh Carbon di:oxide methanisation catalyst with good activity
US5672558A (en) * 1995-04-17 1997-09-30 Engelhard Corporation Formed compositions
US6034285A (en) * 1997-10-22 2000-03-07 Koei Chemical Company, Limited Producing method for trimethylolalkane
CN1269787A (en) * 1997-09-03 2000-10-11 巴斯福股份公司 Moudable material which can be used as catalyst
DE10152525A1 (en) * 2001-10-24 2003-05-08 Basf Ag Process for the decomposition of ammonium formates in polyol-containing reaction mixtures

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3217751A1 (en) * 1982-05-12 1983-11-17 Degussa Ag, 6000 Frankfurt Pressed pieces of pyrogenically produced titanium dioxide, a process for the production thereof, and the use thereof
US6235797B1 (en) * 1999-09-03 2001-05-22 Battelle Memorial Institute Ruthenium on rutile catalyst, catalytic system, and method for aqueous phase hydrogenations

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1952738A1 (en) * 1968-12-17 1970-07-09 Leuna Werke Veb Production of trimethylopropane
US4647592A (en) * 1984-01-05 1987-03-03 Exxon Research & Engineering Company Start-up with ruthenium catalysts
US5149861A (en) * 1987-05-06 1992-09-22 Basf Aktiengesellschaft Recovery of trialkylamines and methyl formate from mixtures obtained in the preparation of trimethylolalkanes
US5484757A (en) * 1994-06-02 1996-01-16 Norton Chemical Process Products Corp. Titania-based catalyst carriers
US5672558A (en) * 1995-04-17 1997-09-30 Engelhard Corporation Formed compositions
DE19530528A1 (en) * 1995-08-19 1997-02-20 Dornier Gmbh Carbon di:oxide methanisation catalyst with good activity
CN1269787A (en) * 1997-09-03 2000-10-11 巴斯福股份公司 Moudable material which can be used as catalyst
US6034285A (en) * 1997-10-22 2000-03-07 Koei Chemical Company, Limited Producing method for trimethylolalkane
DE10152525A1 (en) * 2001-10-24 2003-05-08 Basf Ag Process for the decomposition of ammonium formates in polyol-containing reaction mixtures

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