Reactor Setup

The same reactor setup described in Chapter-2 was used for this study also (sec.2.2.3). A schematic diagram of the experimental setup is shown in Fig. 2.1. It consisted of a glass reactor of 10 cm i. d. and 16 cm height. An outer jacket was provided in the reactor through which water at constant temperature could be circulated. The temperature in the jacket was maintained within 0.1 °C using a thermostat. A glass stirrer with four blades, turbine type impeller (1cm in width), was 

Reactions Reactions R 1 (POWERLAW) Input Data Browser 

0 Spetfkattorw 0 Simulation Optons streamda s r i SiJwtrftjMfM Ffl units-sats 

RMcijngp tr uhmJ 3 Rate boos neac ivpij y  

0 Report Options ift Components (ft Gfl Properties ffi Qfl Flowsheet Q Streams Q males EF Sleds 15 35 PI H- Al EH Gfi VI 

0 5 j0UQri Opbxit 0 Strum Oess y. Q SdKVwms iB 35 UWfSets 

---

Another example of enzyme- and acid-catalyzed DKR has been reported by Bornscheuer [45]. Acyloins were racemized by using an acidic resin through the formation of enol intermediates. The enzymatic resolution was catalyzed by CALB. Since deactivation of this enzyme occurred in the presence of the acidic resin, they designed a simple reactor setup with two glass vials cormected via a pump to achieve a spatial separation between the acidic resin and the enzyme (Figure 4.20). 

In less than one minute, half of the 2,4-dihydroxy benzoic acid is decomposed already at 160°C in the micro-reactor setup [18]. Thus, a study was conducted to find optimal process parameters for T and t to achieve efficient high p,T operation via discrimination between the desired electrophilic substitution and undesired decarboxylation routes. The best operation point was at (200°C 40 bar 2000 ml h" 16 s). 

Fig. 6 High p,T operation for the radical side-chain bromination of m-nitro toluene in a micro-mixer-reactor setup. The large increase in operational temperature increases conversion at good selectivities, which tend to decline slightly with temperature. The two-fold substituted product, m-nitro toluene benzal bromide, is formed in larger amounts at temperatures above 200°C (IMM, unpublished results)...

Fig. 1 shows the reactor setup used for continuous precipitation of lanthanum phosphate. A tube made of silicone rubber was used as a reactor. The inner diameter of the reactor tube... 

This system is a chip version of three dimensional micro mixer-tube reactor setups [21]. It comprises a triangular interdigital micro mixer with a focusing zone that thins the multi-lamellae and a subsequent reaction channel that is surrounded... 

On the reactor side, the gas mixture enters from the top and is separated into 16 individual streams, going to each one of the reactors. Figure 11.3 shows the side view of the high-throughput reactor setup. The reactors are vertical flow-through reactors with a... 

In subsequent work the same supported catalysts were used in different reactor setups [20] (Figure 3.3). A vapour-phase reactor in which the supported catalyst was mounted on a bed was used for the hydroformylation of volatile alkenes such as cis-2-butene and trifluoropropene. The initial activities and selectivity s were similar to those of the homogeneous solutions, i.e. a TOF of 114 and 90% ee in the hydroformylation of trifluoropropene was reported. No rhodium was detected in the product phase, which means less then 0.8% of the loaded rhodium had leached. The results were, however, very sensitive to the conditions applied and, especially at longer reaction times, the catalyst decomposed. In a second approach the polymer supported complex was packed in a stainless steal column and installed in a continuous flow set-up. 

A similar reactor setup was used by Keurentjes et /. 9,10 A Wilkinson catalyst with fluorinated ligands was applied in the hydrogenation of 1-butene in supercritical... 

The example of a biofilm reactor setup shown in Figure 7.1 demonstrates how an experiment can be performed under controlled conditions (Raunkjaer et al., 1997). The objective of the study is to determine substrate (acetate) and DO surface removal rates of biofilms that were grown on wastewater. Careful control is needed to do so during conditions where both the substrate and the DO should be studied as limiting factors for the removal rates. A great number of specific details that will not be dealt with here were considered for this experiment. 

FIGURE 7.1. An example of a reactor setup to study biofilm processes under controlled laboratory conditions. 

In order to achieve results with close-to-conventional testing conditions, the parallel reactor setup for liquid-phase reaction must mimic the real process conditions of the later process as nicely as possible. The main efforts to be realized lie in the miniaturization and integrated construction of the parallel testing setup and the automation of process control combined with suitable online and offline analytical methodologies. 

In a series of controlled experiments, Dosi et al. used the conversion of glucose to lactic acid as a model for the potential of controlling (automatically by computer) the concentrations of the constituents.45 Nice schematics for the reactor setup and connections to the computer/NIR spectrometer/microhltration unit, etc., are shown. Six cases are described, each using a conventional batch process. Transition from batch mode to automatic was triggered by predefined criteria such as degree of substrate conversion or biomass concentration. Control charts and comparisons of NIR data with conventional assays are given for all six cases. 

Previous studies in conventional reactor setups at Philip Morris USA have demonstrated the significant effectiveness of nanoparticle iron oxide on the oxidation of carbon monoxide when compared to the conventional, micron-sized iron oxide, " as well as its effect on the combustion and pyrolysis of biomass and biomass model compounds.These effects are derived from a higher reactivity of nanoparticles that are attributed to a higher BET surface area as well as the coordination of unsaturated sites on the surfaces. The chemical and electronic properties of nanoparticle iron oxide could also contribute to its higher reactivity. In this work, we present the possibility of using nanoparticle iron oxide as a catalyst for the decomposition of phenolic compounds. 

FIGURE 12.1. Schematic of tubular reactor setup for pyrolysis/catalytic/oxidation studies coupled to a molecular-beam mass spectrometer sampling system. 

To verify the homogeneous nature of Rh-3-SILP catalysts, as previously suggested based on IR and NMR spectroscopic studies, [30] kinetic experiments have also been conducted with the catalyst. Here, a continuous fixed-bed reactor setup equipped with online gas-chromatography, described elsewhere in detail, [31] was applied. The general rate law for the hydroformylation of propene was assumed ... 

The reactor setup shown in Fig. E6.1 consists of three plug flow reactors in two parallel branches. Branch D has a reactor of volume 50 liters followed by a reactor of volume 30 liters. Branch E has a reactor of volume 40 liters. What fraction of the feed should go to branch D ... 

We wish to explore various reactor setups for the transformation of A into R. The feed contains 99% A, 1% R the desired product is to consist of 10% A, 90% R. The transformation takes place by means of the elementary reaction... 

We wish to design a reactor setup for a specific duty. Sketch the scheme selected, and calculate the fraction of feed transformed into desired product as well as the volume of reactor needed. 

In the following problems sketch your recommended reactor setup with recycle, bypass, etc., and on each sketch indicate pertinent quantities. 

G = Gas Filters MFC = Mass Flow Controllers R = Reactor Setup CG = Carrier Gas FID = Flame Ionization Detector... 

Figure 16 Microplasma reactor setup for partial oxidation of methane (left) and photo of thin glass tube equipped with a twisted metal wire (right) (Nozaki et al., 2007a reproduced with permission).

DOW in Midland, USA, performed metallocene-catalyzed polymerization of ethylene using a homebuilt tube reactor setup with advanced microflow tailored plant peripherals for heating, temperature monitoring, pressure control and dosing via smart valves and injectors. Screening of process conditions was a driver [19]. Also, flexibility with regard to temperature and pressure at low sample consumption was an issue. Quality of the information is another motivation due to the advanced process control and sensing. 

Figure 14.12 Continous stirred reactor setup for the transesterification of glycerides.

---