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Platinum Metals Rev., 2010, 54, (3), 137

doi:10.1595/147106710x501782

Studies of Precious Metal Catalysts in the CARMAC Programme

Improved catalyst specificity and selectivity through a combination of chemical engineering and greater understanding of reaction mechanisms

    • Robbie Burch
    • CenTACat, School of Chemistry and Chemical Engineering,
    • Queen's University Belfast, Belfast BT9 5AG, UK
    • Lynn Gladden
    • Department of Chemical Engineering and Biotechnology, University of Cambridge,
    • New Museums Site, Pembroke Street, Cambridge CB2 3RA, UK
    • and Stan Golunski*§
    • Johnson Matthey Technology Centre,
    • Blounts Court, Sonning Common, Reading RG4 9NH, UK;

Present address: Cardiff Catalysis Institute, School of Chemistry, Cardiff University, Main Building, Park Place, Cardiff CF10 3AT, UK; *E-mail: golunskise@cardiff.ac.uk

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Article Synopsis

One of the recurrent challenges in catalysis is how to ensure that the right reactions take place. In a recent collaborative programme between academic and industrial partners, some of the key issues relating to reactant specificity and product selectivity in liquid and gas media have been tackled using a combination of computational modelling, catalyst chemistry and chemical engineering. As well as providing solutions to several real-life problems from the chemical manufacturing industry, essential skills required for in situ studies have been established within the academic centres during the course of the programme. These developing skills are intended to have an ongoing impact on the understanding and application of complex multiphase processes, in which platinum group metals and other precious metals are often present as catalysts.

The Scope of the CARMAC Programme


The programme known as Controlling Access of Reactive Molecules to Active Centres (CARMAC) was set up to study and promote catalytic specificity and selectivity. The intended applications include manufacturing processes in which either a specific reactant needs to be consumed from a mixture, or one target product has to be formed selectively from a reactant feed that can undergo several parallel or consecutive reactions. It was planned as a series of complementary projects addressing clearly defined problems, which were grouped under three main themes:

(a) Hydrogenation of difficult molecules in liquid media (where hydrogen can attack different parts of the molecules, but reaction of only one functional group is required);

(b) Overcoming equilibrium limitations to allow one product to predominate;

(c) Enrichment and clean-up of multicomponent gas streams.

In addition to the technical targets, the stated aim of the programme was to improve the catalysis skills base in the UK. This specific aim was endorsed and supported by one of the UK's major academic funding bodies, the Engineering and Physical Sciences Research Council (EPSRC), as part of its commitment to building capability in key areas of science, engineering and technology.

From its start in late 2003, CARMAC brought together chemists and chemical engineers from the Universities of Cambridge and Reading and Queen's University Belfast in the UK and the University of Virginia, USA, along with their counterparts from industry. The industrial partners represented the full range of relevant catalyst application skills, namely catalyst support manufacture (Grace Davison), catalyst production and catalytic process engineering (Johnson Matthey PLC), and catalyst use in chemical manufacture (Robinson Brothers Ltd).

The five-year lifetime of the programme was intentionally longer than the usual duration of a PhD studentship or typical postdoctoral fellowship. This allowed greater continuity, and also encouraged more flexibility in starting, interrupting or even stopping the various experimental and modelling activities within the programme. A loose matrix of overlapping teams, led jointly by academic and industrial project leaders, enabled effective input from all partners into the component projects, and allowed the emergent techniques to be used as transferable resources between the programme themes. Two technical experts, Brian Harrison and Colin Gent, monitored progress throughout and provided feedback to the project partners and to the EPSRC.

Reflecting the broad range of target applications, a diverse range of catalytic materials was studied during the programme. This included base metals for the isomerisation of alkanes (1, 2) and modified zeolites for the methylation of toluene to p-xylene (3, 4). However, pgms and other precious metals featured in many of the projects, and it is from this body of work that we have selected the examples that are highlighted below.

Hydrogenation of Difficult Molecules


Organo-sulfur compounds, such as mercaptans, are key intermediates in the production of bulk and speciality chemicals. Although aliphatic mercaptans can be produced by the direct reaction of alcohols with hydrogen sulfide over alkali metal catalysts, the same route cannot be used for the manufacture of aromatic mercaptans. Instead, aromatic sulfonic acids or sulfonyl chlorides are reduced either with phosphorus, or with nascent hydrogen formed by reacting a metal with a mineral acid. These reactions are highly selective, but have the drawback of generating phosphoric acid and metal compounds as byproducts. A potential alternative route is by reductive breaking of the sulfur–sulfur bond in the corresponding bis-disulfide, as in Equation (i):

C6H5–S–S–C6H5 + H2 → 2C6H5–SH (i)

However, the reducing agent is usually a stoichiometric reagent, such as sodium borohydride, triphenylphosphine or semicarbazide. In attempting to develop an equivalent catalytic reaction, the challenges lay in identifying selective catalysts that would not break the carbon–sulfur bonds, and would not themselves be deactivated by the sulfur compounds.

In CARMAC, we showed that, contrary to expectation, palladium-based heterogeneous catalysts are both active and resistant to sulfur poisoning in the hydrogenation/hydrogenolysis of aromatic disulfides. This conclusion came as a result of a fundamental study that was targeted at identifying and understanding the underlying scientific barriers, and not through an empirical trial-and-error approach. In this case, a combination of density functional theory (DFT) calculations and systematic experiments (5), in which the aromatic substituent was varied, provided us with a mechanistic model which allows the disulfide to adsorb in parallel or perpendicular to the palladium surface
(Figure 1). The perpendicular conformation allows a high surface concentration of adsorbed hydrogen, which in turn enables a high rate of reaction, and encourages cleavage of the S–S bond by hydrogenation in preference to reduction of the aromatic substituent.

Fig. 1

Predicted surface species formed by adsorption of 2,2′-dinitrodiphenyldisulfide on a palladium surface. (a) Flat-lying monomer species formed by parallel adsorption; (b) Upright dimer species formed by perpendicular adsorption (5). Colour coding for the ball-and-stick atoms is: grey = C, white = H, blue = N, red = O, yellow = S

Predicted surface species formed by adsorption of 2,2′-dinitrodiphenyldisulfide on a palladium surface. (a) Flat-lying monomer species formed by parallel adsorption; (b) Upright dimer species formed by perpendicular adsorption (5). Colour coding for the ball-and-stick atoms is: grey = C, white = H, blue = N, red = O, yellow = S

 

Overcoming Equilibrium Limitations


Carbazole (CZ), 1, and its derivatives are valuable chemical intermediates in the production of pharmaceuticals, dyes, pigments and agrochemicals. A key step in the synthesis of CZ is the endothermic liquid-phase dehydrogenation of 1,2,3,4-tetrahydrocarbazole (THCZ), 2, which is carried out catalytically, preferably in a batch reactor. However, the yield is limited by the chemical equilibrium between the forward and reverse reactions. Using Le Chatelier's principle (6), the simplest means of increasing the yield is by either raising the temperature or continuously removing the H2 coproduct. Raising the temperature has a direct impact on the running costs of the process, while the physical removal of H2 requires fundamental changes to the process design, such as operating the reactor in semi-batch mode. Having recognised these inherent limitations in the dehydrogenation reaction, the contribution from CARMAC was to think ‘outside the box’ and recognise that chemical removal of hydrogen using cheap, readily available hydrogen scavengers could also be used to manipulate the equilibrium and improve the yield of the desired product. In the past the most effective additives identified for related reactions have been relatively high-value organic chemicals (7).

 

Once again, through a combination of experiments and computational studies, we were able to propose a solution based on a mechanistic understanding of the catalytic process (8). Our experiments showed that simple gas-phase hydrogen acceptors, such as ethene, propene and but-1-ene, produce a fivefold increase in the rate of THCZ dehydrogenation at a fixed temperature (135°C) over a supported palladium catalyst. DFT calculations revealed that alkene hydrogenation competes effectively with the back-hydrogenation of the intermediates formed on the catalyst surface, causing the equilibrium to shift in favour of CZ formation. As well as being more cost effective than liquid-phase H2-acceptors, such as nitrotoluene or diethyl maleate, the alkenes and their product alkanes can be readily separated from the reaction medium.

Enrichment and Clean-Up of Gas Streams


Preferential Combustion of Carbon Monoxide


Maleic anhydride, 3, is used mainly in the production of unsaturated polyester resins, but it is also an intermediate in the production of pesticides, reactive plasticisers and lubricating oil additives. In the manufacture of maleic anhydride, the catalytic partial oxidation of butane is usually performed under single-pass conditions of high conversion, but relatively low product selectivity (9). In principle, the process could be operated under less wasteful conditions, where the per-pass conversion would be lower but the selectivity much higher. However, before recycling the unconverted butane back to the catalytic reactor, any carbon monoxide contaminant would have to be removed (or converted to carbon dioxide) to avoid poisoning the vanadium-based partial oxidation catalyst.

 

Prior to CARMAC, collaborative work between Queen's University Belfast and Johnson Matthey had shown that a continuous NaA zeolite membrane, grown over the active sites of a platinum-iron catalyst supported on silica, would allow CO to be preferentially combusted in the presence of butane (10). The growth of the crystalline membrane (estimated to be 50 nm to 70 nm thick) required pretreatment of the 3 mm-diameter Pt-Fe/SiO2 particles with a polyelectrolyte to reverse the surface charge, before the zeolite was hydrothermally synthesised in situ over the particles at high pressure. The coherence of the membrane was attributed to the fact that it was crystallised from a precursor gel that, following the charge-reversal step, perfectly wetted the catalyst surface. The specificity of the membrane could be simply related to the pore size of the NaA zeolite (0.4 nm), which allowed entry and egress to molecules with a small enough kinetic diameter (CO: 0.376 nm; O2: 0.346 nm; CO2: 0.33 nm) while excluding butane (0.43 nm).

In CARMAC, a similar degree of discrimination between CO and butane was achieved by forming a largely amorphous aluminium–silicon–oxygen layer (about 500 nm thick) over the catalyst particles (Figure 2), using a much simpler preparative route (11). Following pretreatment to reverse the surface charge, the particles were immersed in the NaA zeolite precursor gel, before simply being heated in open air. The increase in path length from the gas phase to the active sites, which results from applying the amorphous layer, seemed to explain why the molecule with the higher diffusivity (CO) was preferentially oxidised. However, it became clear that the presence of this physical barrier is not the sole reason for the molecular discrimination. We demonstrated that chemical modification of the Pt-Fe catalyst by the Na+ ions present in the precursor gel also plays a part, by altering the specificity of the active sites (Figure 2).

Fig. 2

(a) Poor reactant-specificity of Pt-Fe/SiO2 catalyst for the oxidation of carbon monoxide (×) in the presence of butane (□); (b) Improved reactant-specificity (CO: closed symbols; butane: open symbols) after the catalyst has been coated with an aluminium-silicon-oxygen layer. Both methods of applying the coating (represented by the triangles and circles) are equally effective (11)

(a) Poor reactant-specificity of Pt-Fe/SiO2 catalyst for the oxidation of carbon monoxide (×) in the presence of butane (□); (b) Improved reactant-specificity (CO: closed symbols; butane: open symbols) after the catalyst has been coated with an aluminium-silicon-oxygen layer. Both methods of applying the coating (represented by the triangles and circles) are equally effective (11)

 

Reactive Removal of Oxygen


Dehydrogenation reactions are widely used for converting low value feedstocks (e.g. alkanes) to higher value intermediates (e.g. alkenes). One of the most promising means of promoting dehydrogenation of hydrocarbons over a pgm catalyst is by the inclusion of oxygen, which can shift the equilibrium, cause an adiabatic temperature rise and prevent soot formation on the catalyst surface. Combustion is suppressed either by limiting the proportion of O2 in the feed (12) or by using very high space velocities (13). However, traces of unreacted O2 can remain in the product stream, which may interfere with or inhibit any subsequent reaction. For example, even parts per million (ppm) concentrations of residual O2 will have a detrimental impact on ethene polymerisation.

Prior to CARMAC, the only reported study of the selective removal of O2 by reaction with excess H2 in the presence of light alkenes was described in a patent that disclosed the use of a partially-poisoned Pd catalyst at relatively high temperatures (>350°C) (14). In CARMAC, a range of potential precious and base metal catalysts was screened for low-temperature activity, with silver emerging as the best candidate for further development and scale-up (15). Silver had been included in the screening on the basis that it is known to: (a) activate oxygen (16); (b) be a poorer hydrogenation catalyst than platinum and palladium (17); and (c) inhibit ethene hydrogenation when added to palladium-based acetylene hydrogenation catalysts (18). In our tests, a catalyst containing 7.6% (by weight) silver dispersed on alumina gave full conversion of O2 at 50°C, with negligible loss of the alkene, when either ethene or propene was used in the gas stream.

Increasing the Hydrogen Concentration in Reformate


When mainstream hydrocarbon fuels or biofuels are reformed to produce hydrogen, the product stream (reformate) invariably contains CO, CO2 and water in addition to H2 (19). If the reformer is to be coupled with a low-temperature fuel cell as part of an integrated power source, the CO concentration has to be reduced from per cent levels to below 50 ppm to prevent the fuel cell anode being poisoned (20). The most efficient way to do this is by converting as much CO as possible to CO2 using the water-gas shift (WGS) reaction, which increases the hydrogen concentration at the same time (Equation (ii)):

CO + H2O ⇆ CO2 + H2 (ii)

Although thermodynamically favoured at low temperatures (21), the reaction requires a highly active WGS catalyst to reduce the CO concentration to 0.5%. The remainder can then be removed by preferential oxidation or methanation, either of which will consume some of the H2.

Commercial low-temperature WGS catalysts are generally copper-based, but these need to be carefully activated by reduction, kept in their reduced state, and protected from contact with air, with which they can react pyrophorically. Therefore, for fuel cell applications, a new generation of potential WGS catalysts has to be developed. Initial screening of potential catalysts identified a number of promising candidate catalysts in which either platinum or gold was the preferred metal, and oxides with redox character (such as cerium oxide) were the preferred supports (Figure 3).

Fig. 3

Water-gas shift activity of gold catalysts compared to platinum (▲ = 2%Pt/CeO2). The results show that the performance of the gold catalysts is very sensitive to the metal loading and the support material used (♦ = 2%Au/TiO2; × = 2%Au/CeO2; ■ = 0.2%Au/CeZrO4; ● = 2%Au/CeZrO4). Platinum catalysts are much less sensitive (23)

Water-gas shift activity of gold catalysts compared to platinum (▲ = 2%Pt/CeO2). The results show that the performance of the gold catalysts is very sensitive to the metal loading and the support material used (♦ = 2%Au/TiO2; × = 2%Au/CeO2; ■ = 0.2%Au/CeZrO4; ● = 2%Au/CeZrO4). Platinum catalysts are much less sensitive (23)

 

The development of improved catalysts was based on fundamental investigations of the nature of the active catalyst, the mechanism of deactivation, and the mechanism of the WGS reaction itself. Supported by DFT calculations (22) the experimental work in CARMAC provided a complete mechanistic model for the WGS reaction over the most active catalysts (gold supported on cerium zirconium oxide (Au/CeZrO4) in which it was proposed that a key intermediate was a surface carboxylate species (23, 24). Although such a species could not be detected experimentally, it provides a feasible route from COads to CO2(ads) by reaction with OHads, and with hindsight seems much more plausible than the widely favoured ‘formate model’ (25). In the latter, a C–H bond is formed through the (energetically very difficult) step of insertion into an O–H bond but then, in order to generate CO2, this C–H bond has to be broken again. Detailed experimental work, using fast transient kinetic isotope techniques coupled with infrared spectroscopy and mass spectrometry (26), showed that the formate species seen by infrared are not relevant to the main reaction pathway, on any of the very active low-temperature catalysts developed in this programme (27, 28).

Although the Au/CeZrO4 catalysts are extremely active they have a tendency to deactivate under reaction conditions. By undertaking a detailed investigation of their structure, primarily using extended X-ray absorption fine structure (EXAFS), X-ray absorption near edge structure (XANES) and high-pressure X-ray photoelectron spectroscopy (XPS), again supplemented by DFT calculations (29), we began to realise that the high activity of gold supported on redox oxides requires a strong interaction with the support. The loss in activity of the catalyst appears to be caused by a change in morphology of the gold particles, leading to the breakdown of this strong interaction (Figure 4), rather than a loss of exposed gold surface area (30). Armed with this knowledge, further experimentation was focused on developing precious metal catalysts that would enhance the formation of such strong interactions, and on maintaining these interactions by optimising the process conditions.

Fig. 4

Stages in the activation and deactivation of a gold water-gas shift catalyst. High activity is associated with the formation of small gold particles that interact strongly with a reducible support. Under deactivating conditions, the particles change shape, leading to a weaker interaction with the support

Stages in the activation and deactivation of a gold water-gas shift catalyst. High activity is associated with the formation of small gold particles that interact strongly with a reducible support. Under deactivating conditions, the particles change shape, leading to a weaker interaction with the support

 

A further important outcome of the multidisciplinary research in CARMAC has been the recognition that the definition of an ‘active site’ in heterogeneous catalysis is non-trivial. Frequently, we think of an active site as a single entity, such as a few atoms on a metal crystal (possibly differentiating between planar, edge or corner atoms), a cation or an anion, or a Lewis or Brønsted acid or base site. In fact, for almost all heterogeneously catalysed reactions the active ‘site’ is much more complex. For example, for the low-temperature WGS reaction on supported gold catalysts, it now seems that the active site requires metallic gold atoms in a specific arrangement, probably with cationic gold to connect the metallic gold atoms to the support with sufficient strength of interaction to activate the gold/oxide interface, and oxygen vacancies adjacent to this interface. As each component may be involved in one or several reaction steps, the absence of any one component can completely eradicate the low-temperature activity. By comparison, the structurally simpler platinum analogues are easier to stabilise, but have yet to match the performance of gold at temperatures below 200°C (31).

New Preparative and Investigative Techniques


In tackling the technical challenges posed in the individual projects, CARMAC also had the key objectives of: (a) advancing catalyst design, (b) developing state-of-the-art techniques for studying catalysts under reaction conditions, and (c) improving collaboration between chemists and engineers.

Using a new preparative technique, in which a surfactant was used to pre-form a platinum-containing microemulsion (32), chemists at the University of Reading were able to encapsulate platinum nanoparticles in ceria (Figure 5), rather than disperse them over the surface. The resulting catalyst was more active than conventionally prepared Pt/CeO2 for the WGS reaction, and had the added advantage of not forming any methane when tested in a gas stream rich in H2 (i.e. representative of a reformate). Detailed characterisation at the University of Reading and Queen's University Belfast, showed that encapsulating the platinum inhibited the strong CO adsorption that can lead to the non-selective methanation reaction taking place, and indicated that the WGS reaction was taking place exclusively on the ceria shell. As ceria on its own has low WGS activity, the results imply that the platinum nanoparticle core exerts (electronic) control over the metal oxide shell (33).

Fig. 5

High resolution transmission electron micrograph showing platinum nanoparticle cores covered in a ceria shell

High resolution transmission electron micrograph showing platinum nanoparticle cores covered in a ceria shell

 

Mechanistic studies of heterogeneously catalysed gas-phase processes, such as those described above for the WGS reaction, require measurements that are made on a relevant timescale. In the study of the WGS reaction, Queen's University Belfast developed in situ infrared spectroscopy (Figure 6) to study catalyst surfaces under real reaction conditions with a time resolution of around 10 s (34). When combined with kinetic experiments on a similar timescale, the spectroscopic measurements provided us with unequivocal information (27), where previously several plausible but often conflicting mechanisms had been proposed.

Fig. 6

Diffuse reflectance Fourier transform infrared (FTIR) cell for in situ catalyst studies: (a) viewed from above; (b) cross-sectional schematic

Diffuse reflectance Fourier transform infrared (FTIR) cell for in situ catalyst studies: (a) viewed from above; (b) cross-sectional schematic

 

Throughout the programme, chemical engineers at the University of Cambridge used and, in some cases, developed new, in situ magnetic resonance techniques to measure the characteristics of catalysts. Novel measurements included spatial mapping of both chemical composition (35) and fluid transport within a working catalytic reactor (36). We were able to monitor the distribution of liquid throughout the inter-particle space (Figure 7), and calculate the average concentration gradient between the outside and the inside (i.e. within the pores) of the catalyst particles. We believe these are the first direct measurements of concentration gradients across the inter- and intra-particle space of a reactor resulting from mass transfer limitations. This knowledge can be used to guide the selection of the porosity and shape characteristics of catalyst particles, and the operation of the reactor. The results were correlated with molecular models from the University of Virginia together with kinetic measurements and characterisation studies from Queen's University Belfast creating a cross-scale representation of the events taking place in a packed bed of catalyst particles within a liquid medium (37) and providing insights into catalyst deactivation and regeneration (38).

Fig. 7

Two-dimensional magnetic resonance image of the spatial distribution of liquid in a trickle bed reactor containing Pd/Al2O3 catalyst, during the hydrogenation of 1-octene (35)

Two-dimensional magnetic resonance image of the spatial distribution of liquid in a trickle bed reactor containing Pd/Al2O3 catalyst, during the hydrogenation of 1-octene (35)

 

Pulsed-field gradient nuclear magnetic resonance (PFG-NMR) was also used to demonstrate the first spatially-resolved, chemically-specific measurements of the diffusion coefficients of reactants and products during reaction. The reaction considered was the esterification of ethanol with acetic acid over an ion-exchange resin. It was even possible to discriminate between diffusion inside and outside the ion-exchange resin catalyst particles.

Other developments included the application of PFG-NMR techniques to directly measure two distinct molecular diffusion coefficients within the pore space of a catalyst. In collaboration with Queen's University Belfast, it was possible to compare these experimental data directly with the results of molecular simulations. Remarkably good agreement was obtained between the two approaches. The simulation showed evidence of a strongly-influenced surface layer of molecules which was characterised by diffusion processes at least an order of magnitude slower than the molecular diffusion in the bulk of the internal pore space of the catalyst. Related to this work was the development of NMR relaxometry (the determination of spin-lattice relaxation time, T1, and spin-spin relaxation time, T2). It was demonstrated that the attenuation of the T1 and T2 values, characteristic of a liquid when it is contained within the catalyst, can be used as a direct indicator of the strength of the surface interaction between the catalyst and the particular liquid molecule under consideration. This method opens up the possibility of probing competitive adsorption processes inside the pore space of catalysts (39).

Achievements of the CARMAC Programme


One of the major achievements of CARMAC was the creation, within the academic centres, of a suite of ‘state of the art’ scientific and engineering competencies, which were designed to address specific technical problems in collaboration with industry. These competencies allowed us to investigate and understand the heterogeneously-catalysed target reactions in the liquid and gas phases. It is significant that many of the catalysts identified, designed or developed in this programme were pgm or other precious metal formulations. With their low loadings of highly dispersed metal, often interacting with the support, these catalysts were the most difficult to study. However, they challenged us to develop cutting-edge methodologies that will allow us to understand catalytic function across the length scales, from molecular rearrangements on the surface of metal nanoparticles to mass transfer in a catalytic reactor.

The programme also enhanced the transfer of knowledge and technology between academia and industry, and provided trained and highly skilled researchers for both sectors. In terms of direct technology transfer it is worth remarking that at the end of the ‘normal’ three-year PhD or two-year postdoctoral project there would have been few results that could have been transferred to industry. During the CARMAC programme much more time was available, and as a result it achieved practical outputs for industry, by first identifying the key questions and then providing the knowledge required to address those questions. This process typically took four years.

Beyond CARMAC: The CASTech Programme


So, what happens next? A new five-year programme, Catalytic Advances through Sustainable Technologies (CASTech), is already underway, having started as CARMAC finished. Most of the partners from CARMAC (including the University of Cambridge, Queen's University Belfast, Johnson Matthey PLC and Robinson Brothers Ltd) have been joined by several new members: the University of Birmingham, Borregaard, Forestry Commission Research Agency, Questor Centre and Sasol Technology Research Laboratory. Again, the academic centres are largely funded by the EPSRC, with industry contributing substantial in-kind support. In CASTech, the individual projects relate to renewable energy, protecting our environment, and developing truly benign chemical manufacturing processes. Led by industry, and building on the core competencies created in the CARMAC programme, we believe that CASTech has the capability and momentum to take on some of the current ‘grand challenges’ in science and technology.

Precious metal catalysts are likely to feature strongly once again, particularly in the challenges associated with processing complex bio-feedstocks, and with the generation and storage of renewable energy. A key aim throughout will be designing or re-engineering the catalyst manufacturing processes to ensure that they too are pollution-free.

Dedication


This article is dedicated to the memory of Colin Gent (former Head of Catalysts at ICI and Technical Director of the Institute of Applied Catalysis (iAc), London) who, as an advisor to the programme, contributed greatly to the successes of CARMAC.

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The Author

Professor Robbie Burch OBE was the Programme Manager of CARMAC, based at Queen's University, Belfast, UK, where he is now Emeritus Professor of Physical Chemistry. His research is concerned with developing a fundamental understanding of catalytic processes of industrial importance, including automotive emissions control, hydrocarbon processing for fuel cell applications and clean organic synthesis. LINK http://www.ch.qub.ac.uk/staff/burch/index.html

Professor Lynn Gladden CBE was the Principal Investigator for CARMAC at the University of Cambridge, UK, where she is Head of the Department of Chemical Engineering and Biotechnology. Her group's primary research interest is in the development of magnetic resonance techniques to study research problems in chemical engineering. LINK https://www.ceb.cam.ac.uk/directory/lynn-gladden

Professor Stan Golunski, who was at the Johnson Matthey Technology Centre at Sonning Common in the UK at the time, was the Programme Director of CARMAC. He is now Deputy Director of the Cardiff Catalysis Institute, Cardiff, UK. His research interests lie in the field of gas-phase heterogeneous catalysis. LINK http://www.cardiff.ac.uk/chemy/contactsandpeople/academicstaff/golunski-stan-overview_new.html

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