Institute of Thermodynamics and Kinetics of Chemical Processes, Ivanovo State University of Chemistry and Technology, Ivanovo, Pr F Engelsa 7, 153000, Russia
Received Date: June 07, 2016; Accepted Date: July 05, 2016; Published Date: July 15, 2016
Citation: Andrei AV, Tatiana OY, Dmitrii PA. Selective Blockage of the Catalyst Active Sites for the Hydrogenation of Various Functional Groups over Raney Nickel and Nickel Supported on Silica. Trends Green Chem. 2016, 2:1. doi:10.21767/2471-9889.100012
Nickel supported on silica and Raney nickel was used. Hydrogenation was carried out of compounds with >C=C< bond and -NOÂ¬2 bond in different solvents with different degree of deactivation of the nickel catalysts. It is shown the usability of the method for analysis of poisoning behavior not only for gas reaction, but also for the liquid phase hydrogenation. It was shown that catalyst support as well as the media has a significant effect on the poisoning behavior. It was demonstrated while different reducible groups are hydrogenating there is different poisoning behavior
Raney Ni catalyst; Supported Ni catalyst; Deactivation poisoning behavior
Liquid phase hydrogenation processes are the important part of modern high technologies of fine organic synthesis. It is produced by the hydrogenation: caprolactam, aniline, alcohols. It is subject of hydrogenation: fats, rosin, vegetable oil, 1,3-butadiene, furfural, bio-oil, diene rubbers and many others [1-6]. High-performance eco-friendly liquid-phase hydrogenation technology provides a high yield and quality of the target products, saves materials and energy, can eliminate or substantially reduce the anthropogenic impact of existing production on the regional ecological environment as a result of a sharp decline in the volume of toxic gas emissions, waste water and solid waste. That is why the technology is the basis of a synthesis of various organic products in the chemical industry countries - leading manufacturers of fine chemicals production: USA, Germany, Japan, France and others. It is no accident the problem of expanding the applications of catalytic technologies is formulated by industrial section of the European Federation of Catalysis Societies (EFCATS) as one of the priorities. The hydrogenation is frequently carried out in the presence of a catalyst based on noble metals such as Pd/C or Rh/C . However, catalysts based on noble metals have a number of disadvantages; it is the high cost, limited availability, and the need for high reaction temperatures and pressures. On the other hand, catalysts based on nickel can be used. There are pros and cons. Catalysts based on nickel are inexpensive and have low toxicity, but metallic nickel has lower activity than noble metal catalysts [8-10].
Despite long history of Raney nickel it is still actively studied and applied in the industry [11-16]. The nickel has a number of well-known advantages: high activity and selectivity and disadvantages: low stability and life time [17-19].
For this investigation Raney nickel was selected as the catalyst, because it is reproducible and well-studied, it is convenient to use as a model of a nickel catalyst, since many properties similar to other kinds of nickel hydrogenation catalysts .
However, it was taken nickel inflicted on silica Ni/SiO2, prepared according to a specially developed method, by direct reduction of a precursor consisted from a mixture of NiO and Ni2O3 supported on silica, to account for the influence of the media.
There is hydrogenation step to receive a number of substances, such as p-aminobenzoic acid, m-aminobenzoic acid, sulfanilamide, 2,5-dichloro-3-aminobenzoic acid, p-toluidine, adrenalon, sarcolysine, sorbitol, p-aminophenyl allyl ether, p-chloroaniline. Such substances are very important in various fields, particularly in medicine, thus for medical use the obtaining of highly pure product becomes critically important. However, the above substances are obtained with a number of byproducts. One of the reasons for the large number of by-products is the presence of several hydrogenation-sensitive substituents [20-23].
It is known all heterogeneous catalysts have nonuniform surface that contains different surface active sites and different type of energy adsorption bond [24,25]. A detailed review article published by Hochard and Renouprez  deals with the problems of different hydrogen species on Raney Nickel. Basically, the methods of TPD, adsorption calorimetry, potentiometry, spectroscopy, quantum chemistry calculations and XPS were found forms of hydrogen on Ni [24,25,27-31]. The first state of the adsorbed hydrogen is M - H2 - loosely coupled α2-form of molecular hydrogen with linear structure. Area of hydrogen desorption from the nickel is in the range 193-293 K . The second state of M - H2δ+ is α1-molecular form of hydrogen, but the bridge structure. Area of hydrogen desorption from the nickel is in the range 293-393K [28,31]. The third form is medium coupled γ-form (M - H2δ+). For all transition metals are characterized by a wide area of hydrogen desorption M - H2δ+ from 393 to 658 K [25,31]. Form M - H2δ- is atomic most strongly associated with the surface of transition metals β2-form. This type of chemisorption is a kind of dissolution, when the hydrogen atom is located on the 0,5Å under electronic metal surface inside the lattice. Area of desorption is in the range 673-1173 K . It was found that on the surface of the Raney Nickel hydrogen is adsorbed in three forms: two-centred molecular α1-form, single-centred atomic γ- and multi-centred β2-form [29,31].
Thus for the selective reduction of a chosen functional group it becomes important that these sites have different activity for the hydrogenation of the different groups. In this case, it is apparent that the blocking of certain active sites will allow changing the selectivity of the hydrogenation of the chosen functional group. Sodium sulphide was chosen as an agent that is capable to block such sites because sulphur compounds, including sulphide ion, are the most studied catalytic poisons, that are blocking the active sites of the catalyst surface, and lower the activity of the catalysts for hydrogenation reactions [33-35]. In this case, the degree of deactivation is convenient to characterize by the initial amount of the entered sodium sulphide per gram of nickel, or as a part of the value of a certain amount of poison [33,36].
The aim of this work was to determine the possibility of purposeful blocking of certain catalyst active sites, which are the most active in certain reactions to change the selectivity of the catalyst. With the ultimate goal should be to develop a method for producing high-efficiency catalytic system for hydrogenation of multiple bonds "carbon-carbon" and of a nitro group. The investigation of high-efficiency catalytic systems based on supported nickel and Raney nickel for synthesis of compounds with few hydrogenation-sensitive substituents, such as in the preparation of 4-aminophenyl allyl ether, which is an enzyme inhibitor.
We used a Raney nickel catalyst (hereinafter Niskel), received by treatment of a nickel-aluminium alloy by sodium hydroxide according to known method . The nickel catalyst prepared by this method had such characteristics: specific surface area (BET) is 170 ± 5 m2·g-1, porosity is 0.5 ± 0.05, size pore radius is 2 nm.
Also nickel on silica (hereinafter Ni/SiO2) was used. "Silica L 5/40 m" was used for the synthesis as support. The average particle radius of silica is 5 μm, the specific surface is 276 ± 5 m2·g-1.
The synthesis of supported catalysts had the steps: preparing support, impregnating by an aqueous 2M solution of nickel nitrate, drying and recovery of nickel oxides. The support was impregnated once with constant stirring at 5 Hz and the ratio of the support to solution is 1 to 15. The impregnation time was 4 hours at a temperature of 30°C. The impregnated support was separated from the solution by a glass filter. Further drying was carried out at t = 80°C till receiving supported crystalline hydrates. Then, thermal decomposition of crystalline hydrates was carried out. The crude product was placed into a furnace and heated at t = 470°C for 2 h. ± 30 min. So obtained crude product was placed into a tube furnace and reduced in a hydrogen flow (hydrogen flow rate is 2.10 cm3·min-1.) at t = 450°C until no H2O (2 hours. ± 10 min.).
Equipment and methods
The distribution of particle size of a catalyst powder was checked by a laser granulometer Analysette 22 Compact by Fritsch. The specific surface area was determined by means hardware complex “Flowsorb II 2300”, via the low-temperature nitrogen adsorption by a BET method.
Solutions of sodium sulphide in the chosen solvent for the deactivation were used. Direct potentiometric method was used to determine the concentration of S2- ions in the solution. Deactivation of the catalyst was carried out by the method described in .
Kinetic studies of the reaction liquid phase hydrogenation were carried out by a static method at nonstationary conditions in a pressurized liquid reactor with intense stirring of the reaction mass at atmospheric hydrogen pressure [17,36]. In all experiments, the weight of active metal was 0.25 - 0.5 g, the activity of the catalyst was calculated by hydrogenation rate of model compound at less than 0.05 from conversion level.
The characterization of poisoning behaviour (selectivity of deactivation) was carried out by the Bartholomew’s method . The one is based on the analysis of the kinetic parameters of the process and is specially modified for the use in the liquid phase hydrogenation, the essence of which is the determination of preferential adsorption of deactivating agent on the certain atomic ensembles of the surface.
Diagram illustrating such analysis of poisoning behaviour is shown in Figure 1, where the activity of the catalyst A and the quantity of poison C are normalized via :
A = r0,C / r0,C=0
C = ni / nmax
Where r0,C and r0,C=0 are the initial hydrogenation reaction rates in the solvent (activity) of deactivated catalysts and nondeactivated, respectively; ni is quantity of the added catalyst poison per gram of catalyst; nmax is the added quantity of catalyst poison per gram of catalyst, wherein the catalyst completely loses its activity. The dependence of the activity vs poison concentration shown in Figure 1 is based on the assumption of a homogeneous poisoning of catalyst surface and reaction surface, i.e. at insignificant diffusion resistance of pores.
“Selective” poisoning involves preferential adsorption of the poison on the most active sites at low concentrations. If sites of lesser activity are blocked initially, the poisoning is “antiselective”. If the activity loss is proportional to the concentration of adsorbed poison, the poisoning is “non-selective” .
Basic physical and chemical parameters of catalysts investigated for the article are presented in Table 1.
|Catalyst||w(Ni), %||Sspecific, m2/g||rø, μm||A*|
|Niskel||88.3 ± 0.5||170 ± 5||4.8 ± 0.1||250 ± 10|
|Ni/SiO2||11.0 ± 0.3||71 ± 5||5 ± 0.1||580 ± 30|
Table 1: Properties of the catalyst samples.
According to Table 1, the catalytic activity of the supported nickel catalyst is more than 2 times higher than traditional Raney nickel for the reduction reactions of multiple bonds in the molecule of sodium maleate. While the supported catalyst has a lower specific surface for the same catalyst particle radius. Obviously, this fact should be explained by different ratios of the active metal on the surface involved in the reaction to the bulk metal mass. Thus, the contradiction is only apparent and should be eliminated by the appropriate experimental data processing.
Figure 2a shows the dependences of the observed rate of the reaction of sodium maleate hydrogenation over Ni/SiO2 in an aqueous medium and at presence of the catalyst poison (sodium sulphide) vs conversion level. Figure 2b shows the dependences of the activity (initial rate from Figure 2a) of the catalyst for the hydrogenation of sodium maleate from the added quantity of catalyst poison. Figure 2b shows the absolute values to assess the stability of the catalyst to its sulphide poisoning, and Figure 2c in relative terms, that allows to judge the nature of this deactivation via Bartholomew’s method, i.e. the selectivity of blocking the active sites of the catalyst.
Figure 2A: The dependence of the observed rate for reaction of sodium maleate hydrogenation over Ni/SiO2 from conversion level, with different quantity of the added sulphide ion per gram of metal: 1-0; 2-0.12; 3-0.24; 4-0.36 mmol (Na2S)/g(Ni). Reaction conditions: T = 303K; P = 0.1 MPa; medium: distilled water.
According to the experimental data, we can reasonably say that resistance to deactivation of supported nickel at low concentrations of sulphide ion is higher because decrease of catalytic activity for Raney nickel with 0.24 mmol of sodium sulphide addition per gram of nickel was 84%, while it was just 12% supported one.
Such a difference in the rate of deactivation can be explained by the fact that a part of atoms of the catalyst poison can be adsorbed not only by the nickel but also by the support (SiO2). A further sharp decrease in activity was due to the blocking of support pores by sulphide ion.
Figures 2d-2f show graphs similar to 2c, but with additives in a solvent to demonstrate the effect from solvent to the behaviour of the catalyst poisoning.
According to Figure 2c Niskel at the experimental conditions shows a non-selective behaviour of poisoning, but Ni/SiO2 shows mixed behaviour of deactivation, i.e. the combined surface (surface of the nickel structures, of the SiO2 structures and of their combination) gives a more complex picture of Ni/SiO2 poisoning than Niskel. Therefore, using acidic or basic support even in neutral media it is possible to change the selectivity of nickel deactivation, which leads to the possibility of creating highly selective catalytic systems.
In the Table 2 are depicted the hydrogenation reactions sodium maleate and sodium p-nitrophenoxide in alkali media. Maleic acid diethyl ester and p-Nitrotoluene was used in alcohol solution.
|NaMal Ã¢ÂÂ sodium maleat||NaSuc Ã¢ÂÂ sodium succinate|
|NaPNP Ã¢ÂÂ sodium p-nitrophenoxide||NaPAP Ã¢ÂÂ sodium p-aminophenoxide|
|MADE Ã¢ÂÂ Maleic acid diethyl ester||SADE Ã¢ÂÂ Succinate acid diethyl ester|
|PNTÃ¢ÂÂ 4-Nitrotoluene||PATÃ¢ÂÂ p-Toluidine|
Table 2: The hydrogenation reactions.
This was chosen due to their solubility.
Summarized information about the character of deactivation behavior while using compounds with different functional groups represented in Table 3.
|H2O Ã¢ÂÂ NaOH 0.01M||Selectivea||Mixtureb|
|H2O Ã¢ÂÂ NaOH 0.1M||Antiselectivea||Selectiveb|
|H2O Ã¢ÂÂ NaOH 1M||Non-selectivea||-|
|H2O Ã¢ÂÂ i-PrOH (0.073**)||Selectivec||Antiselectived|
|H2O Ã¢ÂÂ i-PrOH (0.191**)||Antiselectivec||Mixtured|
|H2O Ã¢ÂÂ i-PrOH (0.68**)||Mixturec||Mixtured|
Table 3: Summarized information from figures number 2 of media influence.
When experiments to determine the behaviour of deactivation by the method proposed Bartholomew  for the gas phase and modified by us for the liquid phase were carried out, the reactants with different hydrogenation-sensitive substituents were used. If reactants were hydrogenated by the same active surface sites, then the behaviour of deactivation would be the same for the different reactants. Table 3 shows that by using a reactants with different hydrogenation-sensitive substituents the behavior of deactivation in the same condition was different. This means that different active sites are involved in the hydrogenation of different functional groups. As well, it can be concluded that the sulphide is able to selectively remove from the reaction zone the certain active sites. This fact allow us to create a catalytic system with defined active sites, which able to a selectively hydrogenate chosen functional group. For example, if we have substance with >C=C< and –NO2 group, but it is need to hydrogenate predominantly >C=C< to ≡C–C≡ and left –NO2 as it is, then H2O – NaOH 0.1M media is a preferred; and opposite for hydrogenate –NO2 to –NH2 and left >C=C< as it is, then H2O – i-PrOH (0.073 mole fraction) media is a preferred. Thereby it is need to choose a system with a maximum difference in the Bartholomew Curves.
That number of identified regularities gives a theoretical basis for the fine adjustment of quantity of different active sites on the catalyst surface and for purposeful change of a nickel catalyst activity in a selected reaction.
The practical part of the work was carried out as part of the State task (project 1800).
The theoretical part of the work is supported by the Russian Ministry of Education and Science (project №4.1385.2014/K)
Work is executed at the Institute of Thermodynamics and kinetics of chemical laboratories processes “Ivanovo State University of Chemistry and Technology”.
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