# Patent

## Title
Fast filtering powder catalytic mixtures

## Abstract

The catalytic mixture resulting of a metal powder catalyst with a solid material (referred to here as a reaction-aid) that has good filtering properties, does not interfere with the reaction, does not interfere with recycling the catalyst back into the reaction, does not interfere with the refining and recovery of the metal from the catalyst after it is spent, and will not become separated from the catalyst during the preparation of this catalytic mixture, the chemical reaction or the separation of this catalytic mixture from the reaction medium, whereas the ratio of the reaction aid to the catalyst ranges from 0.05 to 20 on a weight basis. A preferred metal powder catalyst is acetylene black supported precious metal. Preferred reaction aids are sibunit powder or activated carbon. The catalytic mixture can be used for the catalytic transformation of compounds, such as the hydrogenation of olefins, or the hydrogenation of nitro compounds.

## Background
CROSS REFERENCE TO RELATED APPLICATIONS
The present application is US national stage of international application PCT/EP2007/060942, which had an international filing date of Oct. 15, 2007, and which was published in English under PCT Article 21(2) on Apr. 23, 2009.
The invention of this patent concerns itself with a fast filtering powder catalytic mixture that it highly effective for chemical reactions on the basis of the amount of its catalytic metal. This invention involves forming a mixture of the metal powder catalyst with a solid material (referred to here as the reaction aid) that has excellent filtering properties, does not interfere with the reaction, does not interfere with recycling the catalyst back into the reaction, does not interfere with the refining and recovery of the metal from the catalyst after it is spent, and will not become separated from the catalyst during the preparation of this catalytic mixture, the chemical reaction or the separation of the catalytic mixture from the reaction medium.
Powder metal catalysts are used for a large number of hydrogenation, dehydrogenation, isomerization, reductive amination, reductive alkylation, oxidation, hydration and other reactions of compounds. These powdered metal catalysts are prepared by supporting small metal crystals onto a powder support such as activated carbon, carbon black, acetylene black, silica, alumina, magnesia, silica-alumina, ceria, zeolites, hydrothalcites, mixed metal oxides and other powder supports. The carbon supports have been found to be the most useful for use with the present invention and they may come from one or more sources such as, but not limited to, wood, peat, coal, saw dust, carbon containing waste materials (e.g., wood palates, agricultural waste material, plastic waste materials, polymer waste materials and others), rice husks, coconut shells, bones, lignite, petroleum based residues and sugars. Commercially available carbons which may be used in this invention include, but are not limited to, Barneby & SutcliffeTM, DarcoTM, NucharTM, Columbia JXNTM, Columbia LCKTM, Calgon PCBTM, Calcon BPLTM, WestvacoTM, NoritTM, CECATM and Barnaby Cheny NBTM. The present invention is especially effective when used together with carbon blacks.
Carbon black is elemental carbon in a very fine particulate form that is more amorphous than graphite. It consists of planes of carbon atoms fused randomly together to form spherical particles that adhere to each other to create chainlike aggregates which in turn form agglomerates. The spherical particles range from  ̃10 to 500 nm and the average aggregate diameters range from 100 to 800 nm. The typical classes of carbon black are characterized by the size distribution of the spherical particles, the degree of aggregation, degree of agglomeration, the types of surface moieties and the method of production. The two main types of carbon black are produced by either the incomplete combustion method where the carbon source is oxidized in a limited amount of oxygen or the thermal decomposition method in the absence of oxygen (vide-infra). The furnace blacks are made via the incomplete combustion method and they may contain up to 15 wt % oxygen and acetylene black is made by the thermal decomposition method and is relatively oxygen free. Furnace blacks have surface areas ranging from 100 to 1500 m2/g and the surface areas of acetylene blacks range from 60 to 300 m2/g. These macro porous materials are generally believed to have “flat-surfaces” with relatively very few meso and micro pores. Furnace blacks are typically produced by burning natural gas and liquid aromatics in a furnace with a limited and controlled amount of oxygen at about  ̃1400° C. The ensuing cracking and polymerization of the hydrocarbons followed by their dehydrogenation lead to the formation of turbostratic carbon particles. Immediately after the reaction zone, the carbon black is quenched to 200-250° C. with a water spray to impede its further reaction with oxidizing gases such as steam and CO2. Nonetheless, some oxidation does occur during the quenching step and this creates additional surface oxide groups. Acetylene black is produced in the absence of oxygen via thermal decomposition at very high temperatures (>2500° C.) and its surface is rather devoid of surface oxide groups. Thus the adsorptive properties of acetylene black are determined by its olefinic character (i.e., the ratio of its pi-to-sigma bonds). Carbon blacks conduct electrical charges and this may also play a strong role in their use as a catalyst support. Carbon blacks are also very compressible and the level of compression not only changes the physical aspects of the support, but it also effects the chemical properties such as electrical conductivity and the influence this can have on the metal crystallites supported on the carbon black where the catalysis occurs. The table below describes some of the typical carbon blacks one can use with this invention and their sources.







TABLE 1







Typical carbon blacks and their sources.










Carbon Black
Chemical
Particle



Type
Process
Diameter, nm
Feedstock





Lamp Black
Incomplete
 50-100
Coal Tar



Combustion

Hydrocarbons


Channel
Incomplete
10-30
Natural Gas


Black
Combustion


Furnace
Incomplete
10-80
Natural Gas/


Black
Combustion

Liquid





Aromatic


Thermal
Thermal
150-500
Natural Gas


Black
Decomposition


Acetylene
Thermal
35-70
Acetylene


Black
Decomposition









These catalysts are typically prepared by suspending the powder support in a solution, adding one or more precious metal compounds to the liquid suspension with the support, fixing the metal onto the support and optionally reducing the fixed metal. The fixing agent may be added before the metal, with the metal, after the metal, during the whole process and/or combinations thereof. The fixed metal may also be oxidized before reduction, after reduction or be oxidized instead of being reduced. Another possible high temperature treatment could be in the presence of an inert gas such as nitrogen and this could be applied in various sequences and temperatures in combination with the other preparation steps mentioned above. Other gases (CO, CO2, and others) and vaporized compounds (e.g., organic compounds and others) could be used as well in order to achieve the various desired effects. The suspension liquid may be aqueous, it may be organic or it could be composed of many phases and the properties of the suspension and/or its phases can be further changed at various preparation steps to modify the resulting catalyst. One such property could be the pH of the suspension at various steps of the catalyst preparation, where the addition of various bases (KOH, NaOH, Na2CO3, NaHCO3 and others) and/or acids (HCl, HNO3, H2SO4 and others) to a liquid suspension of the support before, after and/or during the various preparation steps can greatly impact the properties and performance of the catalyst. In the case the catalyst contains more than one metal the acid and/or base can be added before, after, during and/or in the solution containing one or more metals before addition. In the case that the different metals or metal combinations are added at different times during the various preparation steps of the catalyst, one could add the acid and/or base before, after, during and/or in the solution containing one or more metals for each of these metal additions. For further details about pH effects on catalyst preparation with aqueous phases please see F. P. Daly, W. M. Jensen and D. J. Ostgard, in Catalysis of Organic Reactions, edited by M. G. Scaros and M. L. Prunier, vol. 62 (1995) p 13-21. The catalyst could be made of one metal or more than one metal. In the case that the catalyst is made of more than one metal, all the metals could be added at once or various combinations of metals could be added during the various steps of the catalyst's preparation. The metal compounds could be salts, organic complexes, combinations thereof and others as well. The metal and/or its compound may dissolve during the preparation of the catalyst and/or the metal compound may change in-situ during preparation to produce the desired catalyst. Other suitable catalyst preparation methods for this invention include but are not limited to the use of metal evaporation, the incipient wetness spray impregnation of the various solutions used in preparing the catalyst, the wet spray impregnation of the various solutions used in preparing the catalyst, dipping the catalyst powder in various liquids and other methods as well. All commercially available powder metal catalysts can be used with the invention of this patent.
The metals used in the preparation of these catalysts can be one or more precious metals, one or more base metals, one or more alkali and alkaline metals, one or more rare earth metals or combinations of metals from one or more of these groups. This invention of this patent may also be used with Raney-type catalysts that are made by leaching out most of the Al from an alloy of Al with one or more metals that contain at least one catalytic metal and potentially modifying metals that can function as promoters, inhibitors or co-catalysts. After leaching, this activated metal powder catalyst may or may not be washed to various degrees before it is applied to the present invention.
Metal powder catalysts are typically used with liquid suspensions in tank reactors, where eventually the catalyst must be separated from the reaction mixture by sedimentation, filtration and/or other suitable methods. Other reactor types such loop reactors, cascade reactors, tube reactors and others may also take advantage of the present invention and the reaction in question may be performed batch wise, continuous, semi-continuous or by any other process method. The catalytic reaction may also involve a gas phase of one or more gases (e.g., H2 for hydrogenation, O2 for oxidation and N2 may be used as an inert diluent) that needs to diffuse through the liquid phase to reach the solid surface of the catalyst before it can adsorb, be activated (e.g., via dissociation of H2 or O2) and participate in the reaction. The gas reactant may be added to the compound being transformed or it may just simply facilitate the reaction. Unfortunately some of the properties that make a catalyst very active, such as a very small support particle size and unique morphology, may also make it very difficult to filter after the reaction is performed. Hence the goal of this invention is to maintain and increase, if possible, the effectiveness of the metal in the chemical reaction while improving the filterability of the catalyst. Catalyst filtration can be performed with various screens, sintered metal discs, candle filters (e.g., Dr. M filters), membrane filters, Schenk filters, Rosemond filters and other devices for the separation of solids from liquids with or without the use of gas pressure to accelerate this separation. These methods as well as others may be used in combination with the present invention for the improved efficiency of a chemical transformation with a metal powder catalyst by allowing one to keep the best powder metal catalyst properties for the reaction while enhancing its ability to be separated from the reaction mixture at the particular time it needs to be so that the reaction can proceed smoothly and the catalyst can be easily recycled back into the system over its expected lifetime.
The present invention involves forming a mixture of the metal powder catalyst with a solid material (referred to here as a reaction aid) that has excellent filtering properties, does not interfere with the reaction, does not interfere with recycling the catalyst back into the reaction, does not interfere with the refining and recovery of the metal from the catalyst after it is spent, and will not become separated from the catalyst during the preparation of this catalytic mixture, the chemical reaction or the separation of the catalyst mixture from the reaction medium. This mixture can range from 0.05 part of reaction aid to 1 part of catalyst on a weight basis to a combination of 20 parts of reaction aid to 1 part of catalyst on a weight basis. The optimal combinations of reaction aid to catalyst on a weight basis range from 12 to 1 down to 0.5 to 1 on a weight basis. The weight ratio of reaction aid to catalyst of 5 to 1 was found to be the best for the reactions performed here.
One of the most effective materials used here was found to be a powder form of sibunit from the Institute of Hydrocarbons Processing (IHP) of the Siberian Branch of the Russian Academy of Science. Sibunit is a three dimensional matrix porous carbonaceous material that is described in U.S. Pat. No. 4,978,649, which is hereby incorporated by reference herein in its entirety. Of note are the three dimensional matrix carbonaceous materials which are obtained by introducing gaseous or vaporous carbon-containing compounds (e.g., hydrocarbons) into a mass of granules of carbonaceous material (e.g., carbon black); decomposing the carbon-containing compounds to deposit carbon on the surface of the granules; and treating the resulting material with an activator gas comprising usually of steam to provide a porous carbonaceous material in the form of a hollow body that has taken the shape of the original granule carbon material. This material can be ground to a course powder that has a surface area about  ̃410 m2/g and a pore volume  ̃0.6 cm3/g (for the pores smaller than 1500 angstroms) with  ̃95% of the particles being between 5 and 400 microns. Of course, other sibunit materials with different particle sizes, pore volumes and surface areas can be also used with the present invention. The sibunit powders with particle size distribution D50 values (the value where half of the particles are greater or lower than this value) between 1000 μm and 5 μm are especially effective as reaction aids.
Other reaction aids that were found to be very effective are activated carbons. The preferred activated carbons were steam activated and/or phosphoric acid activated and had particle size distribution (PSD) D50 values ranging from 1000 μm to 5 μm. Other activated carbons with different PSD D50 values that were activated by other methods can also be used in the current invention.
The reaction aid may not be the best support for the catalyst in question and its function is to assist in the removal of the catalyst from the reaction suspension. In the best case, the reaction aid may also provide additional absorptive properties for the removal of catalyst poisons from the reaction mixture as the reaction proceeds. Another benefit is that it will facilitate the removal of heat during exothermic reactions by the collisions of its particles with the catalyst particles in the reaction mixture.
The reaction aid can also be specially designed to fulfill its role in the reaction medium. Specially designed activated carbons and other materials or the use of those most appropriate commercially available activated carbons and other materials for the functions of a reaction aid that meet all the above mention requirements insomuch as the catalyst remains mixed with the reaction aid during catalyst preparation, the reaction, separation of the catalytic mixture from the reaction medium and the refining of the spent catalyst for metal recovery to where none of these processes are interfered with by the reaction aid itself. During metal recovery, the activated carbon or sibunit that was used as a reaction aid can be burnt along with the spent catalyst to yield an ash rich in the catalytic metal that can be further processed. In inorganic catalytic support systems, the reaction aid will have to be as soluble as the support in the acid solution or whatever solution is used to dissolve the catalyst before the metal is recovered.
Sibunit powder is very effective as a reaction aid, in that it remains homogeneously mixed with the catalyst during catalyst preparation, the reaction, separation of the catalytic mixture from the reaction medium and the refining of the spent catalyst for metal recovery to where none of these processes are interfered with by sibunit itself. The sibunit powder can also be burnt with the spent catalyst resulting in a rapid recovery of the catalytic metal. Additional benefits of the sibunit powder is its graphitic-like conductive structure that seems to practically agglomerate with catalysts on conductive supports impregnated with metals such as the Pd+Pt+Fe on acetylene black catalysts used for the hydrogenation of aromatic nitro groups (e.g., aniline and dinitrotoluene) and the curved shape of these particles that resulted from the crushing of sibunit's original graphitic carbon hollow structures (vide-supra) which provides preferred channels in the catalyst filter cake for the reaction medium to flow through. Another benefit is that it is easier to remove more water from the catalyst in the presence of sibunit than with the catalyst alone. This will result in lower water contents meaning that one can send lower product weights when shipping the catalyst. The lower water content will also benefit catalysts that are more active in their oxidic states (e.g., the above mentioned Pd+Pt+Fe catalyst used for the hydrogenation of aromatic nitro groups) in that air can keep the catalytic metal oxidic without reduction by the support (i.e, activated carbons and other supports may be reducing agents for metals). Actually the properties of sibunit allow one to adjust the wetness of the catalytic mixture with far fewer difficulties than with the catalyst by itself, thereby improving the flexibility of this system for optimal product design and production.
The reaction aid can be added to the catalyst during any, many and/or all of the catalyst preparation steps during this procedure and this is usually, but not always, done during the last step where the catalyst preparation slurry in being homogenized by stirring before it is filtered. Another possibility would be to prepare the catalyst as it is normally done, the catalyst is then separated from the preparation slurry (via normal methods such as but not limited to sedimentation, filtration and centrifugation), the catalyst could then be optionally washed, the catalyst is then re-suspended into a slurry, the reaction aid is added to this new slurry and after it has been homogenized by stirring the new catalyst mixture is then filtered. Another possibility would be to mix the catalyst with the reaction aid in a fluidized bed of either a reactive or inert gas. In principle, any method that provides a uniform mixture between the catalyst and the reaction aid can be used to produce the invention of this patent.
One method of particular interest involves preparing the catalyst as it is normally done, allow the catalyst to settle to the bottom of the suspension's vessel after the last washing step, draw off the over-standing solution, add fresh water, add the reaction aid, stir to homogeneity and separate it from the liquid phase by a suitable method such as filtration, decantation, centrifugation, combinations of methods and other suitable means as well. One could also wash the freshly mixed catalytic mixture by allowing it to settle to the bottom of the vessel, drawing off the over-standing water, adding fresh water, stirring to homogeneity and repeat as necessary before the final catalytic mixture is separated from its last wash suspension. Instead of decantation, one could also use other suitable solid-liquid separation techniques, such as but not limited to, filtration, centrifugation and combinations of many methods for the washing of the catalyst and reaction aid mixture.
This mixture of the above mentioned reaction aid and catalyst can be used for a large range of organic transformations including, but not limited to, hydrogenation, dehydrogenation, isomerization, reductive amination, reductive alkylation, oxidation, hydration and other reactions. The moieties that can be transformed include but are not limited to: olefinic groups, acetylenic groups, nitro groups, hydroxylamines, oximes, enamines, nitrates, nitrile groups, aromatic rings, heterocyclic aromatic rings, carbonyl compounds (e.g., aldehydes and ketones), carboxylic acids, carboxlate salts, acid chlorides, imine groups, imides, esters, amides and others. The 2 main examples described here are the hydrogenation of olefinic groups such as the hydrogenation of cinnamic acid to the saturated acid and the hydrogenation of nitro groups such as with the reduction of dinitrotoluene to toluene diamine.
The hydrogenation of olefins on metal catalysts such as precious metal catalysts proceeds rapidly and the preferred support type may not be the best for filtration. Not only that, the dilution of these very active catalysts with the above mentioned reaction aids allows the reaction to progress with far fewer mass transfer limitations and the reaction's overall exotherm is considerably more controllable.
The catalytic hydrogenation of nitro groups with metal catalysts is a very demanding reaction due to the high hydrogen demand (3 hydrogen molecules per nitro group) and the very exothermic nature of this reaction. There are many types of nitro-compound hydrogenations performed in industry. One of the more commercially interesting and technically challenging is the hydrogenation of dinitrotoluene (DNT) to toluenediamine (TDA). This hydrogenation is performed with precious metal powder catalysts at temperatures ranging from room temperature to 200° C. and pressures ranging from atmospheric pressure to 200 bar. The preferred reaction conditions are within the ranges of 50° to 130° C. and 3 to 12 bar. This reaction can be performed in an excess of hydrogen or under a stoichiometric amount of hydrogen.
As mentioned earlier, the hydrogenation of DNT is a very exothermic and hydrogen demanding reaction that is further complicated by this reactant's strong adsorption onto the catalyst. Hence, it is easy to have a hydrogen deficient surface during this reaction and this usually leads to enhanced metal leaching and rapid catalyst deactivation due to coke formation. FIG. 1 displays the DNT hydrogenation scheme. The DNT hydrogenation data over a Pd/C catalyst from Neri et al. (please see, Neri, M. G. Musolino, S. Galvagno, Ind. Eng. Chem. Res., 34 (1995) 2226-2231) has shown that this reaction can take 3 or more parallel routes. The 2,4-DNT can be hydrogenated through an intermediate 4-hydroxyamino-2-nitrotoluene (4HA2NT) before it is converted to 4-amino-2-nitrotoluene (4A2NT) and eventually TDA. It is possible that 4HA2NT goes directly to TDA without forming 4A2NT. The 2,4-DNT can also directly form 4A2NT and then TDA without generating 2HA4NT at all.
The last route forms the 2-amino-4-nitrotoluene (2A4NT) intermediate that proceeds further to TDA. Interestingly, 2-hydroxyamino-4-nitrotoluene (2HA4NT) has not been found in any of the reaction mixtures and due to the explosive nature of hydroxylamines, the 4HA2NT should always be avoided. Regardless of the route, all of the above mentioned intermediates are very active and adsorb strongly. Thus, these intermediates and DNT can all readily yield undesired side products such as tars (e.g., dimers), light boilers (e.g., ring hydrogenated products and toluidines), products with water (e.g., methylaminocyclohexenones) and others (e.g., N-allyl-diamino toluenes) if the catalytic surface is hydrogen deficient. This can be avoided by suspending the catalyst in a hydrogen rich TDA/water mixture having the same TDA-to-water ratio as the stoichiometric product mixture produced by this hydrogenation and only pumping in enough DNT so that it is immediately hydrogenated to completion (please see U.S. Pat. No. 2,619,503) at  ̃6.9 bars and between 90 and 110° C. This is typically how this reaction is performed on a commercial scale, however this may not be the best testing method on a lab scale since the activity of the catalyst is dependent on the pump speed and the lifetime of the catalyst could last for days. Another laboratory testing method would be to pulse the DNT into the hydrogen rich stoichiometric TDA/water mixture (vide-supra) so that there would be only a very slight DNT access over a very limited period of time. In this way, one could measure the activity of the catalyst as a function of how much TDA per kg of precious metal that has been formed to give a catalyst deactivation profile. Based on this information, it was decided to use the above mentioned pulse test procedure at 10 bars and 120° C. for the hydrogenation of DNT over catalysts of the present invention to determine their effectiveness for this reaction.
This precious metal catalyst supported on carbonaceous materials has been optimized over the years (please see: U.S. Pat. Nos. 2,823,235, 3,127,356, and J. R. Kosak, in Catalysis of Organic Reactions, edited be R. E. Malz Jr., (1968) 31-41) and the best support was found to be acetylene black due to its highly olefinic nature. Palladium was initially chosen as the main catalytic metal due to its high activity and relatively low cost. This was improved by promoting it with a small amount of platinum, however this catalyst was too active and yielded unwanted side products via reactions like ring hydrogenation. The selectivity of this catalyst was then corrected by the addition of iron oxide that impeded the undesired reactions. Iron has also been proven to be a promoter for the hydrogenation of aliphatic nitro compounds [please see: E. Auer, M. Berweiler, M. Gross, J. Pietsch, D. J. Ostgard, P. Panster, in Catalysis of Organic Reactions, edited by M. E. Ford, vol. 82 (2001)293-300] as well as for nitro-aromatics, where it was additionally useful for avoiding ring hydrogenation. One of the catalysts from this optimization work has a 0.75 wt. % Pd+0.083 wt. % Pt+0.853 wt. % Fe metal combination supported on acetylene black that not only exhibited high activity, but also high selectivity. This catalyst was made by precipitating 4.5 wt. % Pd+0.5 wt. % Pt+5 wt. % Fe onto the acetylene black support followed by the dilution of the catalyst with fresh acetylene black at the ratio of 5 parts of acetylene black to 1 part of the 4.5 wt. % Pd+0.5 wt. % Pt+5 wt. % Fe on acetylene black catalyst to result in the overall metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.853 wt. % Fe. While acetylene black is the best support for the highest hydrogenation rate, its above mentioned physical and chemical properties make if very difficult to separate from the reaction mixture by filtration or any other method even if one mixes fresh acetylene black at a ratio of 5-to-1 with the catalyst. Hence the choice to use an acetylene black supported catalyst means that one favors a fast and selective hydrogenation over fast filtration.
Activated carbon supported catalysts have also been found to be useful for the hydrogenation of DNT to TDA [please see, Neri, M. G. Musolino, S. Galvagno, Ind. Eng. Chem. Res., 34 (1995) 2226-2231] and while the activated carbon supported catalysts filter much faster than the acetylene black supported ones, these catalysts are far less active and less selective. Activated carbons have far more meso and micro pores than acetylene black. If the metal crystals deposit in these smaller pores, the resulting activated carbon supported catalyst will have more problems with mass transfer limitations into and out of the pores and in this case, the hydrogenation rate can quickly become dependent on the diffusion rate of hydrogen into these smaller pores for these metal crystals. Not only does that make the metal crystals in these pores less active, they are also more likely to form tars due to the strong adsorption strength of DNT under hydrogen deficient conditions resulting in faster deactivation rates and lower reaction selectivity. The resulting TDA and potential side products can also readsorb on other metal crystals as they diffuse out of the carbon's pore system and that will increase the chances of even more secondary reactions leading to even lower reaction selectivity. Moreover, activated carbons are not conductive and they cannot take advantage of this mild metal-to-support interaction between the active site on the catalytic metal and the electronic structure of the support, as is the case with acetylene black. Hence the choice to use an activated carbon supported catalyst means that one favors a fast filtration over faster hydrogenation rates and better product selectivity.
Thus the choice of catalyst determines the bottleneck of the process and it wasn't until the present invention that one could have high activity with high selectivity and fast filtration. The catalyst systems that worked the best for the hydrogenation of DNT were the different acetylene black supported 4.5 wt. % Pd+0.5 wt. % Pt+5 wt. % Fe catalysts that were diluted 5-to-1 with the sibunit powder. It was also found to be rather useful to wash the catalyst before it was mixed with the reaction aid.
Another preferred embodiment of this invention was the 5-to-1 dilution of an 4.5 wt. % Pd+0.5 wt. % Pt+5 wt. % Fe on acetylene black catalyst with a steam activated carbon made from wood and comprising of needle shaped particles that pack to form catalyst beds with preferred channels for the liquid reaction medium to flow through. Other activated carbons from other sources, carbons activated by different methods, carbons activated by more than one method and carbons that are not even activated at all along with carbons having different morphologies can also be preferred reaction aids if they fulfill the reaction aid requirements described in this patent.
The hydrogenation of nitro-compounds can take place in the vapor, slurry, trickle, aerosol and/or liquid phase. The reaction could be performed as a batch process or it could be performed as a continuous process. The continuous processes may involve, but they are not limited to, a type of circulation process. This invention also includes a continuous process where the nitro-compound is added at a rate that is the same or slower than the rate of hydrogenation, so that the concentration of the nitro-compound is kept to a very low level. The feeding rate of the nitro-compound may be so low that the level of the nitro-compound is 1000 ppm or lower. Of course, this reaction can be performed at a controlled excess of DNT by balancing the rate of DNT addition to catalyst's hydrogenation rate. This invention also includes the use of the previously mentioned catalyst of this invention in a continuous process that utilizes a second hydrogenation reactor (or more) to hydrogenate any nitro-compounds and/or intermediates that were remaining from the hydrogenation in the first hydrogenation reactor.
The nitro-compound hydrogenation of this invention may take place in the presence of the neat nitro-compound, at high concentrations of the reactant, at very low concentrations of the reactant and/or in the presence of the product mixture that would be acting like a solvent. This hydrogenation may also take place in the presence of practically only the desired amine or under lower water contents than what is stoichiometrically produced if the water is removed by a satisfactory method (e.g., distillation) during the reaction. The nitro-compound hydrogenation of this invention may take place in the presence of a solvent. The reactor type could be, but is not limited to, a stirred tank reactor, a continuous stirred tank reactor, a loop reactor or a tube reactor. This nitro-compound hydrogenation may occur between atmospheric pressure and 200 bars of hydrogen and the temperature can range from  ̃10° C. to 210° C.
This invention encompasses the preparation and the use of a catalytic mixture comprising of a reactive and selective catalyst along with a reaction aid for the effective (on a metal basis) catalytic transformation of compounds into their products followed by the rapid separation of this mixture from the reaction medium as facilitated by the reaction aid. The reaction aid has to have good filtration properties, does not interfere with the reaction, does not interfere with recycling the catalyst back into the reaction, does not interfere with the refining and recovery of the metal from the catalyst after it is spent, and will not become separated from the catalyst during the preparation of this catalytic mixture, the chemical reaction, separation of the catalytic mixture from the reaction medium and during the refining and recovery of metal from the spent catalytic mixture. This invention also includes the above mentioned catalytic mixture as a composition of matter.



BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1: FIG. 1 illustrates the hydrogenation of DNT to TDA.
FIG. 2: FIG. 2 illustrates an apparatus used to determine the filterability of catalysts, supports, reaction aids and mixtures thereof.
FIG. 3: FIG. 3 is a graph showing DNT pulse hydrogenation data for various catalyst compositions.



APPLICATION EXAMPLE 1
The pulse hydrogenation of dinitrotoluene (DNT) to toluenediamine (TDA).
DNT is typically hydrogenated in an industrial setting via a continuous mode, where the DNT feed rate is slow enough to keep its concentration low enough so that it doesn't poison the catalyst or become a safety hazard. This means that the hydrogenation rate will be dependent on the DNT feed rate. The goal of our pulse hydrogenation method was to keep the DNT concentration low enough so that it would be comparable to the industrial setting while measuring the activity of the catalyst. We were able to do so by pulsing in the DNT feed at a rate that was slightly faster than the rate of hydrogenation so that we could measure catalyst activity while keeping the time of the slight excess of DNT to a minimum.
The pulse hydrogenation method was started by placing enough catalyst in the reactor so that exactly 3 milligrams of precious metal sum total are present along with 101 grams of TDA and 59 grams of water (the reaction's stoichiometric TDA-to-water ratio) in the 500 ml autoclave. The autoclave was then closed, purged with nitrogen 3 times, purged 3 times with hydrogen and heated to the reaction temperature of 120° C. over a period of 20 minutes while the reactor was stirring at 300 rpm and kept under 5 bar hydrogen. Once the autoclave reached 120° C., the hydrogen pressure was adjusted to 10 bar hydrogen and the stirring rate was increased to 1700 rpm. The reaction was then started by pulsing 4 milliliters of molten DNT into the reactor over 30 seconds with an HPLC pump. The HPLC pump head, the DNT reservoir and all the stainless tubing used for the transport of DNT was kept at 95° C. to keep the DNT molten. A Büchi hydrogen press flow controller (bpc 9901) was used to monitor the hydrogen consumption and once the reaction stopped to consume hydrogen, another pulse of DNT was introduced at the same feed rate. This procedure was continued up to a maximum of 45 pulses had been introduced. The data from these hydrogenations can be seen in FIG. 3 and in data tables 4 to 14.
APPLICATION EXAMPLE 2
The batch hydrogenation of cinnamic acid.
The low pressure hydrogenation of cinnamic acid was carried out over 200 milligrams of catalyst slurried into 40 ml of ethanol and added to 80 ml of a 0.844 M cinnamic acid ethanolic solution at 25° C. and atmospheric pressure in a baffled glass reactor outfitted with a hallow shaft bubble inducing stirrer. The reaction began as the stirrer was started and spun at 2000 rpm during the reaction. The total hydrogenation uptake between the third and eighth minutes of the reaction was divided by 5 and then divided by 200 to calculate the cinnamic acid activity value in units of ml of hydrogen per minute per mg of catalyst. The cinnamic acid hydrogenation activity was also calculated on the mg of precious metal basis to facilitate the comparison of the different catalysts. The results of these hydrogenations are listed in table 1.







TABLE 2







The cinnamic acid hydrogenation data.












Cinnamic Acid
Cinnamic Acid




Activity
Activity




ml H2/min/
ml H2/min/mg



Catalyst
mg catalyst
precious metal















Comparative Example 3
67
8043



Comparative Example 4
222
4440



Comparative Example 6
196
3920



Comparative Example 8
34
1700



Example 1
86
10324



Example 2
96
11525



Example 4
76
9124










APPLICATION EXAMPLE 3
Determining the Filterability of the Catalyst
The apparatus in FIG. 2 is used for determining the filterability of the catalyst. The lid of this apparatus has a t-tube outfitted with an inlet for a pressurized gas (e.g., nitrogen or air) and a monometer so that the pressure can be monitored and controlled. The lid can be attached and tightened onto the main vessel with a hand-wheel and a locking nut, and this is made airtight by the use of a viton-o-ring gasket. The main vessel consists of a jacketed container (a stainless steel cylinder) that can be connected in an airtight fashion with the help of a viton-o-ring to an intermediate ring (or cylinder) that goes over another viton-o-ring, a filter cloth, a perforated plate and finally the draining funnel that can be locked into place with a hand-wheel and a locking nut. At the bottom of the draining funnel is a drainage tube that is directed to an empty beaker. Before carrying out each test, a blank run is performed with 400 ml of deionised water to check if the filter cloth is free of support materials, reaction aids and catalyst particles from the previous tests. The blank test is performed by placing a stopper in the drainage tube coming from the draining funnel, 400 ml of deionised water is poured into the jacketed container, the filtration unit is then closed by putting on the lid and tightening it, the plug is then removed from the drainage tube, the device is pressurized with a gas from the T-tube on the lid to exactly 1 bar and the stopwatch is started simultaneously. The time it takes for all of the water to be pressed out is measured in seconds and the stopwatch is stopped after all the liquid is pushed out and at the appearance of the first gas bubbles. If the blank test is quicker than 4 seconds, then the filter cloth is still O.K. If not, the filter cloth will have to be replaced. The test is performed by placing a stopper in the drainage tube followed by suspending 10 grams of the catalyst, support, reaction aid or mixtures thereof into 390 ml of deionised water. Any agglomerates that are present should be broken up by swirling the beaker of the suspension. The suspension is then stirred 15 seconds with a Krups 3 mix 4004 high speed mixing rod on level 3 before it is immediately poured into the filtration unit and the beaker is then rinsed out into the filtration unit with 10 ml of deionised water. In a very quick fashion, The lid is tightened in place, the stopper is removed from the drainage tube, the gas pressured is adjusted to exactly 1 bar and the stopwatch in simultaneously started. The time runs until all of the water comes out of the drainage tube and the first gas bubbles appear. After the measurement the filtration apparatus is taken apart and cleaned thoroughly with water. The filter cloth can be cleaned by forcing water back up the drainage tube and through the filter cloth before the next blank run is performed. Each catalyst, support, reaction aid or mixture thereof is measured 3 times and the average values of these tests are listed in table 3 for the above mentioned materials measured here.







TABLE 3







The filterability of the catalysts, supports,


reaction aids and mixtures thereof.











Filtration Time, in minutes



Catalyst or Support
(m) and seconds (s)







Comparative Example 1
5 m 15 s



Comparative Example 2
0 m 41 s



Comparative Example 3
4 m 30 s



Comparative Example 4
>8 m



Comparative Example 5
4 m 28 s



Comparative Example 6
>8 m



Comparative Example 8
0 m 35 s



Example 1
2 m 03 s



Example 2
2 m 15 s



Example 3
2 m 24 s



Example 5
2 m 41 s



Example 6
3 m 08 s



Example 9
3 m 72 s



Example 10
2 m 18 s



Example 11
0 m 38 s










COMPARATIVE EXAMPLE 1
A commercially available 50% compressed acetylene black used as a support for the catalysts in this patent contained less than 1 wt. % water and had a filtration time of 5 minutes and 15 seconds (please see Application example 3 and table 3).
COMPARATIVE EXAMPLE 2
A sibunit powder (vide-supra) with 95% of its particles between 5 and 400 microns, a BET surface area of  ̃410 m2/gram and a pore volume of 0.6 cm3/gram (for the pores smaller than 1500 angstroms) was used as a support and a reaction aid for the catalysts in this patent. This material contained less than 1 wt. % water and had the filtration time of 0 minutes and 41 seconds (please see Application example 3 and table 3).
COMPARATIVE EXAMPLE 3
One part of a commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 50% compressed acetylene black catalyst made by Degussa's proprietary technology was mixed with 5 parts of a fresh 50% compressed acetylene black on a weight basis in an aqueous suspension, stirred to homogeneity, and filtered. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 74.2 wt. % water and had a filtration time of 4 minutes and 30 seconds (please see Application example 3). This catalytic mixture had a cinnamic acid hydrogenation activity of 8043 ml H2 per minute per milligram of precious metal (please see application example 2) and it was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 4 and FIG. 3. The maximum DNT hydrogenation activity during this test was 429 ml H2/min/mg of precious metal and the final activity was 236 ml H2/min/mg of precious metal at the yield of 39.9 MT of TDA per kg of precious metal resulting in a deactivation rate of 45% over this range.







TABLE 4







The dinitrotoluene hydrogenation data for


comparative example 3.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.6
235



1.3
277



2.1
316



3.1
400



4.1
400



5.2
429



6.3
420



7.4
427



8.6
424



9.7
402



10.8
417



11.9
407



13.0
383



14.1
393



15.2
374



16.4
369



17.5
359



18.6
351



19.7
320



20.8
341



22.0
343



23.1
332



24.2
326



25.4
315



26.5
310



27.6
300



28.7
283



29.8
290



30.9
270



32.1
271



33.2
266



34.3
263



35.4
255



36.5
266



37.7
246



38.8
244



39.9
236










COMPARATIVE EXAMPLE 4
A commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 50% compressed acetylene black catalyst made by Degussa's proprietary technology contained 81.1 wt. % water and had a filtration time longer than 8 minutes (please see Application example 3). This catalyst had a cinnamic acid hydrogenation activity of 4440 ml H2 per min per milligram of precious metal (please see application example 2) and it was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 5 and FIG. 3. The maximum DNT hydrogenation activity during this test was 367 ml H2/min/mg of precious metal and the final activity was 219 ml H2/min/mg of precious metal at the yield of 40 MT of TDA per kg of precious metal resulting in a deactivation rate of 40.3% over this range.







TABLE 5







The dinitrotoluene hydrogenation data for


comparative example 4.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.7
207



1.4
238



2.1
294



3.2
320



4.3
347



5.4
367



6.5
354



7.6
336



8.7
365



9.9
356



11.0
348



12.1
338



13.2
360



14.4
343



15.5
336



16.6
321



17.7
332



18.8
330



20.0
332



21.1
314



22.2
298



23.3
289



24.4
290



25.5
288



26.7
281



27.7
270



28.9
278



30.0
264



31.1
253



32.2
258



33.3
254



34.4
239



35.5
252



36.6
233



37.8
237



38.9
219



40.0
219










COMPARATIVE EXAMPLE 5
One part of a commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 50% compressed acetylene black catalyst made by Degussa's proprietary technology was mixed with 5 parts of a fresh 50% compressed acetylene black on a weight basis in an aqueous suspension, stirred to homogeneity, and filtered. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 77.8 wt. % water and had a filtration time of 4 minutes and 28 seconds (please see Application example 3).
COMPARATIVE EXAMPLE 6
A commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 100% compressed acetylene black catalyst made by Degussa's proprietary technology contained 78 wt. % water and had a filtration time longer than 8 minutes (please see Application example 3). This catalyst had a cinnamic hydrogenation activity of 3920 ml H2 per min per milligram of precious metal (please see application example 2).
COMPARATIVE EXAMPLE 7
A commercially available 4 wt. % Pd+1.0 wt. % Pt+1.0 wt. % Fe on an activated carbon catalyst made by Degussa's proprietary technology was tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 6 and FIG. 3. The maximum DNT hydrogenation activity during this test was 216 ml H2/min/mg of precious metal and the final activity was 173 ml H2/min/mg of precious metal at the yield of 24.28 MT of TDA per kg of precious metal resulting in a deactivation rate of 19.9% over this range.







TABLE 6







The dinitrotoluene hydrogenation data for


comparative example 7.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.56
158



1.20
167



1.87
174



2.50
204



3.21
209



3.90
199



4.61
198



5.37
191



6.01
203



6.72
216



7.39
207



8.09
216



8.82
209



9.53
212



10.25
203



10.96
213



11.69
200



12.38
207



13.09
207



13.79
196



14.48
190



15.21
193



15.94
188



16.61
197



17.33
194



18.00
188



18.62
186



19.33
182



20.04
187



20.75
192



21.47
190



22.14
182



22.85
177



23.56
185



24.28
173










COMPARATIVE EXAMPLE 8
A commercially available catalyst consisting of 1.8 wt. % Pd+0.2 wt. % Pt+2.0 wt. % Fe on sibunit powder (this powder sibunit is described in comparative example 2) that was made by Degussa's proprietary technology contained 27.3 wt. % water and had a filtration time of 0 minutes and 35 seconds (please see Application example 3). This catalyst had a cinnamic acid hydrogenation activity of 1700 ml H2 per min per milligram of precious metal (please see application example 2) and it was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The activity results for the DNT hydrogenation test were so low that they could not be reliably measured and the experiment had to be stopped quite early after its start so as to avoid the unsafe build up of nitro bodies in the reaction medium. One can safely assume that this catalyst is relatively inactive for the hydrogenation of DNT.
EXAMPLE 1
One part of a commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 50% compressed acetylene black catalyst made by Degussa's proprietary technology was washed very well with deionised water and after washing, it was mixed with 5 parts of sibunit powder (this sibunit powder was described in comparative example 2) on a weight basis in an aqueous suspension, stirred to homogeneity, and filtered. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 0.9 wt. % water and had a filtration time of 2 minutes and 03 seconds (please see Application example 3). This catalytic mixture had a cinnamic acid hydrogenation activity of 10324 ml H2 per min per milligram of precious metal (please see application example 2) and it was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 7 and FIG. 3. The maximum DNT hydrogenation activity during this test was 632 ml H2/min/mg of precious metal and the final activity was 510 ml H2/min/mg of precious metal at the yield of 40.1 MT of TDA per kg of precious metal resulting in a deactivation rate of 19.3% over this range.







TABLE 7







The dinitrotoluene hydrogenation data for


example 1.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.8
397



1.7
406



2.7
420



3.8
511



4.8
490



6.0
500



7.1
556



8.3
554



9.5
576



10.7
563



11.9
547



13.1
567



14.3
603



15.5
574



16.7
600



17.9
563



19.0
602



20.2
632



21.4
602



22.5
632



23.7
612



24.9
576



26.0
622



27.2
592



28.4
548



29.6
628



30.8
574



31.9
559



33.1
583



34.3
552



35.5
613



36.6
565



37.8
507



39.0
578



40.1
510










EXAMPLE 2
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 100% compressed acetylene black made by Degussa's proprietary technology, sibunit powder (this sibunit powder was described in comparative example 2) was added to the aqueous suspension of the catalyst in the ratio of 5 parts sibunit powder to 1 part catalyst on a weight basis. This mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting catalytic mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 29.7 wt. % water and had a filtration time of 2 minutes and 15 seconds (please see Application example 3). This catalytic mixture had a cinnamic acid hydrogenation activity of 11525 ml H2 per minute per milligram of precious metal (please see application example 2) and it was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 8 and FIG. 3. The maximum DNT hydrogenation activity during this test was 418 ml H2/min/mg of precious metal and the final activity was 297 ml H2/min/mg of precious metal at the yield of 39.9 MT of TDA per kg of precious metal resulting in a deactivation rate of 28.9% over this range.







TABLE 8







The dinitrotoluene hydrogenation data for


example 2.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.79
212



0.82
289



1.72
314



2.48
327



3.33
358



4.17
373



4.69
368



5.78
365



6.90
357



7.68
398



9.92
396



11.04
383



12.22
392



13.37
418



14.55
409



15.67
407



16.85
400



17.97
407



19.12
411



20.27
385



21.45
365



22.60
387



23.75
374



24.93
367



26.08
368



27.22
350



28.40
354



29.55
341



30.61
319



31.76
318



32.91
339



34.06
329



35.24
327



36.42
308



37.57
300



38.72
294



39.90
297










EXAMPLE 3
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 100% compressed acetylene black made by Degussa's proprietary technology, sibunit powder (this sibunit powder was described in comparative example 2) was added in the ratio of 5 parts sibunit powder to 1 part catalyst on a weight basis to an aqueous suspension of the catalyst. This mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting catalytic mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 35.7 wt. % water and had a filtration time of 2 minutes and 24 seconds (please see Application example 3). This catalytic mixture was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 9 and FIG. 3. The maximum DNT hydrogenation activity during this test was 407 ml H2/min/mg of precious metal and the final activity was 295 ml H2/min/mg of precious metal at the yield of 38.7 MT of TDA per kg of precious metal resulting in a deactivation rate of 27.5% over this range.







TABLE 9







The dinitrotoluene hydrogenation data for


example 3.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














1.1
340



2.1
321



3.2
348



4.3
341



5.4
359



6.5
361



7.6
365



8.7
370



9.7
357



10.9
378



11.9
368



13.0
352



14.2
365



15.2
407



16.3
395



17.5
376



18.6
395



19.7
381



20.8
404



21.9
387



23.1
375



24.2
375



25.3
402



26.4
393



27.5
385



28.6
350



29.8
371



30.9
354



32.0
356



33.1
335



34.2
317



35.3
336



36.5
316



37.6
307



38.7
295










EXAMPLE 4
One part of a commercially available 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe on a 50% compressed acetylene black catalyst made by Degussa's proprietary technology was diluted with 5 parts of sibunit powder (this sibunit powder was described in comparative example 2) on a weight basis in an aqueous suspension that was stirred to homogeneity and filtered. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe and had a cinnamic acid hydrogenation activity of 9124 ml H2 per min per milligram of precious metal (please see application example 2). This catalyst was also tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 10 and FIG. 3. The maximum DNT hydrogenation activity during this test was 487 ml H2/min/mg of precious metal and the final activity was 327 ml H2/min/mg of precious metal at the yield of 38.99 MT of TDA per kg of precious metal resulting in a deactivation rate of 32.9% over this range.







TABLE 10







The dinitrotoluene hydrogenation data for


example 4.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.45
234



0.48
300



1.18
327



1.94
360



2.84
383



3.69
409



4.60
448



5.75
446



6.93
444



7.99
455



10.16
473



11.34
433



12.52
487



13.73
437



14.91
463



16.09
468



17.30
469



18.51
461



19.69
454



20.84
416



22.02
427



23.14
426



24.35
404



25.47
389



26.62
420



27.74
367



28.31
353



28.98
344



29.83
340



30.95
359



32.13
370



33.27
354



34.42
364



35.57
347



36.72
333



37.90
332



38.99
327










EXAMPLE 5
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 50% compressed acetylene black made by Degussa's proprietary technology, an activated carbon (steamed activated and based on wood—this is the first type of such a support used here) was added to an aqueous suspension of the catalyst in the ratio of 5 parts activated carbon to 1 part catalyst on a weight basis. This mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting catalytic mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 13.1 wt. % water and had a filtration time of 2 minutes and 41 seconds (please see Application example 3).
EXAMPLE 6
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 50% compressed acetylene black made by Degussa's proprietary technology, activated carbon (steam activated and based on wood—this is the second type of such a support used here) was added to an aqueous suspension of the catalyst in the ratio of 5 parts activated carbon to 1 part catalyst on a weight basis. This catalytic mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 31.1 wt. % water and had a filtration time of 3 minutes and 08 seconds (please see Application example 3). This catalytic mixture was tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 11 and FIG. 3. The maximum DNT hydrogenation activity during this test was 483 ml H2/min/mg of precious metal and the final activity was 303 ml H2/min/mg of precious metal at the yield of 38.8 MT of TDA per kg of precious metal resulting in a deactivation rate of 37.3% over this range.







TABLE 11







The dinitrotoluene hydrogenation data for


example 6.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.9
275



1.7
312



2.5
364



3.5
396



4.1
362



5.1
417



6.1
430



7.0
400



7.6
381



8.9
413



9.9
467



11.0
483



12.0
449



13.2
447



14.0
412



15.1
483



16.2
483



17.3
433



18.3
432



19.3
426



19.9
409



20.9
395



22.0
409



22.9
349



24.0
398



24.9
328



25.9
354



27.0
349



28.0
332



29.1
343



30.2
350



31.2
346



32.3
335



33.4
335



34.5
321



35.5
302



36.7
309



37.8
302



38.8
303










EXAMPLE 7
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 50% compressed acetylene black made by Degussa's proprietary technology, activated carbon (steam activated and based on wood—this is the second type of such a support used here) was added to an aqueous suspension of the catalyst in the ratio of 5 parts activated carbon to 1 part catalyst on a weight basis. This mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting catalytic mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 66 wt. % water and was tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 12 and FIG. 3. The maximum DNT hydrogenation activity during this test was 497 ml H2/min/mg of precious metal and the final activity was 319 ml H2/min/mg of precious metal at the yield of  ̃39.3 MT of TDA per kg of precious metal resulting in a deactivation rate of 37.3% over this range.







TABLE 12







The dinitrotoluene hydrogenation data for


example 7.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














1.1
442



2.0
376



2.9
392



4.0
437



5.1
424



6.2
396



7.3
453



8.4
436



9.6
477



10.7
453



11.8
460



13.0
497



14.1
443



15.2
486



16.4
477



17.5
465



18.7
462



19.8
468



21.0
463



22.1
458



23.3
465



24.4
465



25.6
455



26.7
440



27.9
422



29.0
454



30.2
433



31.3
431



32.5
409



33.6
409



34.7
402



35.9
367



37.0
370



38.2
341



39.3
319










EXAMPLE 8
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 100% compressed acetylene black made by Degussa's proprietary technology, sibunit powder (this sibunit powder was described in comparative example 2) was added to an aqueous suspension of the catalyst in the ratio of 5 parts sibunit powder to 1 part catalyst on a weight basis. This mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting catalytic mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe and it was tested for the pulse hydrogenation of DNT to TDA as according to application example 1. The results for the DNT hydrogenation test can be seen in table 13 and FIG. 3. The maximum DNT hydrogenation activity during this test was 439 ml H2/min/mg of precious metal and the final activity was 312 ml H2/min/mg of precious metal at the yield of 37.1 MT of TDA per kg of precious metal resulting in a deactivation rate of 28.9% over this range.







TABLE 13







The dinitrotoluene hydrogenation data for


example 8.











Hydrogenation Activity in



Metric Tons TDA yielded per
ml H2 per minute per milligram



kilogram of precious metal
of precious metal














0.7
274



1.4
302



1.9
279



2.8
347



3.7
411



4.7
388



5.8
402



6.9
398



8.0
407



9.1
435



10.2
419



11.3
419



12.4
439



13.6
409



14.7
407



15.9
416



17.0
404



18.1
416



19.2
416



20.4
404



21.5
413



22.7
378



23.8
366



24.9
372



26.0
373



27.0
346



28.0
365



29.1
348



30.2
350



31.4
336



32.5
340



33.6
341



34.8
333



35.9
335



37.1
312










EXAMPLE 9
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 100% compressed acetylene black made by Degussa's proprietary technology, sibunit powder (this sibunit powder was described in comparative example 2) was added to an aqueous suspension of the catalyst in the ratio of 5 parts sibunit powder to 1 part catalyst on a weight basis. This catalytic mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 49.3 wt. % water and had a filtration time of 3 minutes and 43 seconds (please see Application example 3).
EXAMPLE 10
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on a 100% compressed acetylene black made by Degussa's proprietary technology, activated carbon (steam activated and based on wood—this is the second type of such a support used here) was added to an aqueous suspension of the catalyst in the ratio of 5 parts activated carbon to 1 part catalyst on a weight basis. This catalytic mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 64.6 wt. % water and had a filtration time of 2 minutes and 18 seconds (please see Application example 3).
EXAMPLE 11
During the last steps of the preparation of a 4.5 wt. % Pd+0.5 wt. % Pt+5.0 wt. % Fe catalyst on an steam activated wood based carbon (type 1) made by Degussa's proprietary technology, sibunit powder (this sibunit powder was described in comparative example 2) was added to an aqueous suspension of the catalyst in the ratio of 5 parts sibunit powder to 1 part catalyst on a weight basis. This catalytic mixture was stirred to homogeneity, filtered and then washed with deionised water. The resulting mixture had the final metal loading of 0.75 wt. % Pd+0.083 wt. % Pt+0.83 wt. % Fe, contained 3.0 wt. % water and had a filtration time of 0 minutes and 38 seconds (please see Application example 3).
Table 14 summarizes the data measured on the catalysts, supports, reaction aids and catalytic mixtures described here. One can see that the addition of a reaction aid not only improves the filterability of the catalyst system, but is also improves the activity of the catalysts on a active metal basis. In any case, neither the activity nor the selectivity of the catalyst is made worse by the addition of the reaction aid. Another advantage was that one could more readily control the final amount of water in the catalyst from either very high levels of  ̃80 wt. % to practically 0 wt. % depending of the desired properties of the catalyst.







TABLE 14







The summary of the catalyst data



















Rxn
Cat. to
wt. %
CA
DNT max
DNT fina1
Final
% Deact.
Filter Time


Cat1
Sup.2
Add3
Add. Ratio4
H2O
Act.5
Act.6
act.7
TDA Yield8
DNT test9
in m & s10





CE1
AB 50%
—
—
<1
—
—
—
—
—
5 m 15 s


CE2
Sib
—
—
<1
—
—
—
—
—
0 m 41 s


CE3
AB 50%
—
1:5 AB 50%
74
8043
429
236
39.9
45 
4 m 39 s


CE4
AB 50%
—
—
81
4440
367
219
40 
40.3
>8 m


CE5
AB 50%
—
1:5 AB 50%
78
—
—
—
—
—
4 m 28 s


CE6
AB 100%
—
—
78
3920
—
—
—
—
>8 m


CE7
AC
—
—
—
—
216
173
24 
19.9
—














CE8
Sib
—
—
27
1700
Activity was too low to measure
0 m 35 s

















E1
AB 50%
Sib
1:5
 1
10324 
632
510
40 
19.3
2 m 03 s


E2
AB 100%
Sib
1:5
30
11525 
418
297
39.9
28.9
2 m 15 s


E3
AB 100%
Sib
1:5
36
—
407
295
38.7
27.5
2 m 24 s


E4
AB 50%
Sib
1:5
58
9124
487
327
39 
32.9
—


E5
AB 50%
1-AC11
1:5
13
—
—
—
—
—
2 m 41 s


E6
AB 50%
2-AC12
1:5
31
—
483
303
38.8
37.3
3 m 08 s


E7
AB 50%
2-AC
1:5
66
—
497
319
39.3
39.3
—


E8
AB 100%
Sib
1:5
—
—
439
312
37.1
28.9
—


E9
AB 100%
Sib
1:5
49
—
—
—
—
—
3 m 43 s


E10
AB 100%
2-AC
1:5
65
—
—
—
—
—
2 m 18 s


E11
1-AC
Sib
1:5
30
—
—
—
—
—
0 m 38 s





1Catalyst designation in patent: CE = comparative example and E = example.


2Sup. = Support type: AB = Acetylene Black with % compression, AC = activated carbon (with type number) and Sib = sibunit powder.


3Reaction aid: AC = activated carbon (with type number) and Sib = sibunit powder.


4The catalyst to additive ratio on a weight basis, where the additive is either fresh support or a reaction aid.


5The cinnamic acid hydrogenation activity in ml H2/min/milligram of precious metal.


6The maximum activity of the DNT pulse hydrogenation test in the units of ml H2/min/mg precious metal.


7The final activity of the DNT pulse hydrogenation test in the units of ml H2/min/mg precious metal.


8The final TDA yield during the DNT test in units of MT TDA/kg precious metal.


9The % of deactivation during the DNT pulse hydrogenation test to the final yield.


10The filtration time as determined by the filtration test in minutes (m) and seconds (s).


111-AC = Activated carbon type 1.


121-AC = Activated carbon type 2.






The DNT hydrogenation results (see application example 1) are graphically demonstrated in FIG. 3.
While modifications may be made by those skilled in the art, such modifications are encompassed within the spirit of the present invention as defined by these disclosures and claims.

## Claims

1. A catalytic mixture comprising:
a) a metal powder catalyst comprising metal crystals that have been fixed to a powder support by a fixing agent; and
b) a reaction aid which aids in filtering but does not interfere with a reaction, which comprises particles with a particle size distribution, D50, of 5 μm-1000 μm and which is selected from the group consisting of a sibunit powder and an activated carbon;
wherein the ratio of said reaction aid to said catalyst is 0.05-20 on a weight basis.

2. The catalytic mixture of claim 1, wherein the ratio of reaction aid to catalyst is from 4 to 6 on a weight basis.

3. The catalytic mixture of claim 1, wherein the ratio of reaction aid to catalyst is 5 on a weight basis.

4. The catalytic mixture of claim 1, comprising an acetylene black supported precious metal catalyst and sibunit powder, wherein the ratio of sibunit powder to catalyst is from 0.05 to 20 on a weight basis.

5. The catalytic mixture of claim 4, wherein the ratio of sibunit powder to catalyst is 5 on a weight basis.

6. The catalytic mixture of claim 1, comprising an acetylene black supported precious metal catalyst and activated carbon, wherein the ratio of said activated carbon to catalyst is from 0.3 to 20 on a weight basis.

7. The catalytic mixture of claim 6, wherein the ratio of activated carbon to catalyst is from 4.0 to 6.0 on a weight basis.

8. The catalytic mixture of claim 7, wherein the ratio of activated carbon to catalyst is 5 on a weight basis.

9. The catalytic mixture of claim 1, comprising an activated carbon derived from one or more sources selected from the group consisting of wood, peat, coal, saw dust, carbon containing waste materials, rice husks, coconut shells, bones, lignite, petroleum based residues and sugars.

10. The catalytic mixture of claim 9, further comprising a metal selected from the group consisting of: Pt or Fe.

11. The catalytic mixture of claim 9, further comprising Pd.

12. The catalytic mixture of claim 11, further comprising acetylene black.

13. In a chemical reaction in which an organic compound or a nitrate undergoes a hydrogenation, dehydrogenation, isomerization, reductive amination, reductive alkylation, oxidation and/or hydration, the improvement comprising catalyzing said reaction with the catalytic mixture of claim 1.

14. The improvement of claim 13, wherein said chemical reaction is the hydrogenation of an olefin.

15. The improvement of claim 13, wherein said chemical reaction is the hydrogenation of a nitro compound.

16. The improvement of claim 13, wherein said chemical reaction is the hydrogenation of an aromatic nitro compound.

17. The improvement of claim 13, wherein said chemical reaction is the hydrogenation of dinitrotoluene to toluenediamine.

18. The improvement of claim 17, wherein said catalytic mixture comprises a precious metal powder catalyst containing Pd, Pt and Fe.

19. The improvement of claim 18, wherein said Pd, Pt and Fe are present in said precious metal powder catalyst at the weight ratios of 9:1:10 for Pd:Pt:Fe.

20. The improvement of claim 19, wherein the reaction aid in said catalytic mixture comprises sibunit powder.