Reactor studies

Mueller M A, Yetter R A and Dryer F L 1999 Flow reactor studies and kinetic modelling of the... 

Work in the area of simultaneous heat and mass transfer has centered on the solution of equations such as 1—18 for cases where the stmcture and properties of a soHd phase must also be considered, as in drying (qv) or adsorption (qv), or where a chemical reaction takes place. Drying simulation (45—47) and drying of foods (48,49) have been particularly active subjects. In the adsorption area the separation of multicomponent fluid mixtures is influenced by comparative rates of diffusion and by interface temperatures (50,51). In the area of reactor studies there has been much interest in monolithic and honeycomb catalytic reactions (52,53) (see Exhaust control, industrial). Eor these kinds of appHcations psychrometric charts for systems other than air—water would be useful. The constmction of such has been considered (54). 

Model Development PreHminary modeling of the unit should be done during the familiarization stage. Interactions between database uncertainties and parameter estimates and between measurement errors and parameter estimates coiJd lead to erroneous parameter estimates. Attempting to develop parameter estimates when the model is systematically in error will lead to systematic error in the parameter estimates. Systematic errors in models arise from not properly accounting for the fundamentals and for the equipment boundaries. Consequently, the resultant model does not properly represent the unit and is unusable for design, control, and optimization. Cropley (1987) describes the erroneous parameter estimates obtained from a reactor study when the fundamental mechanism was not properly described within the model. 

Data from die results of an industrial reactor study produced the result a — 0.606 + 0.012 ... 

Figure 1.3.2 gives another perspective for scale-down to recycle reactor studies. In this actual case, after preliminary studies in a recycle reactor, a 5-stage adiabatic reactor was envisioned (Betty 1979.) Scaling down the proposed commercial reactor, a 3 diameter tube was designed with elaborate temperature compensation (heating and insulation) for pilot-plant studies (Betty 1968, 1969.) Small squares in the proposed reactor represent side views of cylindrical catalyst cutouts for the recycle reactor... 

The geometrical data and characteristic sizes of the HEX reactor studied in our lab are described in Table 12.2. 

One of the major interests of the HEX reactor is to offer a large ratio surface to reaction volume. Therefore, even if most of the time the laminar flow regime is not suitable to enhance transport phenomena with a moderate overall coefficient, the heat performances are expected to be high, since the compacity factor is always large. This fact is clearly exhibited in Table 12.4, where the results relative to the various HEX reactors studied in our laboratory have been plotted. 

In summary, the results from the fixed bed reactor study provided evidence as to the effect of Au and KOAc on the performance of the catalyst, though, these experiments did not give any information on the perturbation of the reaction pathways with the addition of Au and KOAc. For this type of information, additional experiments were performed using the TAP reactor with 1,2 C-labeled ethylene used as an isotopic tracer of the kinetics. 

Competitive Reaction Pathways in Propane Ammoxidation over V-Sb-Oxide Catalysts an IR and Flow Reactor Study... 

In order to investigate whether COj reacts in a concerted way with surface carbon or whether it dissociates first to CO and adsorbed oxygen and the adsorbed oxygen reacts, infrared spectroscopy, pulse reactor studies and XANES measuremerrts were used. The i.r. spectrum of a prereduced (Ihour at 675K in S /oHj/Nj) Pt/ZrOj catalyst in contact with CO2 at 775K is shown in Fig 6 The spectrum shows the presence of linearly bound CO on Pt at 2053 cm [15]. Additionally, bands of carbonate type species appeared in the region between 1375 and 1540 cm . Over pure supports (in the absence of Pt) the CO band was not seen, but peaks in the carbonate region were observed... 

Many high-ranked catalysis experts have opened their research to micro-reactor studies and have become active. Engineering and catalysis journals have their eye on the field. Thus, cross-border expertise is approaching chemical micro processing. Virtually all chemical-engineering conferences have a micro-reactor session. One can say that micro reactors are now accepted and in a positive sense being absorbed by the catalysis community. 

However, in contrast to the field of catalysis, not many high-ranked organic chemistry experts have so far opened their research to micro-reactor studies and have become active (for some exceptions see, e.g., [29,47, 338-341]). Organic synthesis journals and conferences have yet not recognized to a great extent micro reactors, an exception being [82, 342]. This is, however, not true for researchers oriented towards analytical chemistry. In conjimction with pTAS developments, more and more work is being done in that area. 

Rippin, D.W.T., L.M. Rose and C. Schifferli. "Nonlinear Experimental Design with Approximate Models in Reactor Studies for Process Development", Chem. Eng. 5c/., 35, 356 (1980). 

The technical feasibility of a relatively low-pressure (less than 1000 psig) and low-temperature (less than 100°C) process for the hydrogenation of depolymerized (ammonolysis) Nylon-6,6 and/or a blend of Nylon-6 and -6,6 products has been described. While Raney Co 2724 showed little or no sign of deactivation during the semi-batch hydrogenation of the ammonolysis products, before and after C02 and NH3 removal, Raney Ni 2400 showed signs of deactivation even in the presence of caustic. Raney Co 2724 proved to be an effective and robust catalyst in a continuous stirred tank reactor study. 

The time variations of the effluent tracer concentration in response to step and pulse inputs and the frequency-response diagram all contain essentially the same information. In principle, any one can be mathematically transformed into the other two. However, since it is easier experimentally to effect a change in input tracer concentration that approximates a step change or an impulse function, and since the measurements associated with sinusoidal variations are much more time consuming and require special equipment, the latter are used much less often in simple reactor studies. Even in the first two cases, one can obtain good experimental results only if the average residence time in the system is relatively long. 

Killmeyer, R., K. Rothenberger, B. Howard, M. Ciocco, B. Morreale, R. Enick, and F. Bustamante, Water-Gas Shift Membrane Reactor Studies, Proceedings of 2003 U.S. DOE Hydrogen Annual Merit Review Meeting, Berkeley, CA, May 2003. 

Madikizela-Mnqanqeni N.N. and Coville N.J. 2004. Surface and reactor study of zinc on titania-supported Fischer-Tropsch cobalt catalysts. Appl. Catal. A Gen. 272 339 46. 

Though cycle time plays an important role in the SBR for the decolorization process, not many reports are found in the literature. The long retention times are often applied in the anaerobic phase of the reactor studies, such as 18 and 21 h. In several studies, it was reported that there is a positive correlation between the anaerobic cycle time and the color removal [30, 31]. Indeed, in combined anaerobic-aerobic SBRs, since bacteria shifted from aerobic to anaerobic conditions, or vice versa, anaerobic azo reductase enzyme can be adversely affected by aerobic conditions, which is essential for aromatic amine removal, thereby resulting in insufficient color removal rate. To investigate the effect of cycle time on biodegradation of azo dyes, inar et al. [20] operated SBR in three different total cycle times (48-, 24- and 12-h), fed with a synthetic textile wastewater. The results indicated that with a... 

Since long retention times are often applied in the anaerobic phase of the SBR, it can be concluded that reduction of many azo dyes is a relatively a slow process. Reactor studies indicate that, however, by using redox mediators, which are compounds that accelerate electron transfer from a primary electron donor (co-substrate) to a terminal electron acceptor (azo dye), azo dye reduction can be increased [39,40]. By this way, higher decolorization rates can be achieved in SBRs operated with a low hydraulic retention time [41,42]. Flavin enzyme cofactors, such as flavin adenide dinucleotide, flavin adenide mononucleotide, and riboflavin, as well as several quinone compounds, such as anthraquinone-2,6-disulfonate, anthraquinone-2,6-disulfonate, and lawsone, have been found as redox mediators [43—46]. 

Performances and differences of the reactors studied and reported in Table 1 may be interpreted by means of the appropriate material balance, (l)-(4), and by considering the increase in the conversion rate with DyeL. 

Catalysts Catalysts used in the flow reactor study for activity and selectivity measurements are described in Table I. They were monolithic... 

DESCRIPTION OF MONOLITHIC CATALYSTS USED IN FLOW REACTOR STUDY... 

The performance of a reactor for a gas-solid reaction (A(g) + bB(s) -> products) is to be analyzed based on the following model solids in BMF, uniform gas composition, and no overhead loss of solid as a result of entrainment. Calculate the fractional conversion of B (fB) based on the following information and assumptions T = 800 K, pA = 2 bar the particles are cylindrical with a radius of 0.5 mm from a batch-reactor study, the time for 100% conversion of 2-mm particles is 40 min at 600 K and pA = 1 bar. Compare results for /b assuming (a) gas-film (mass-transfer) control (b) surface-reaction control and (c) ash-layer diffusion control. The solid flow rate is 1000 kg min-1, and the solid holdup (WB) in the reactor is 20,000 kg. Assume also that the SCM is valid, and the surface reaction is first-order with respect to A. 

---