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Reaction reactor configuration, schematic

Classical chemical reaction engineering provides mathematical concepts to describe the ideal (and real) mass balances and reaction kinetics of commonly used reactor types that include discontinuous batch, mixed flow, plug flow, batch recirculation systems and staged or cascade reactor configurations (Levenspiel, 1996). Mixed flow reactors are sometimes referred to as continuously stirred tank reactors (CSTRs). The different reactor types are shown schematically in Fig. 8-1. All these reactor types and configurations are amenable to photochemical reaction engineering. [Pg.240]

The modeling of mass transfer and reaction in catalytic filters can be compared, in a first approximation, with the twin problem concerning honeycomb catalysts. The pores of the filters will have as counterparts the channels of the monolith, whereas the catalyst layer deposited on the pore walls of the filter will be related to the wall separating the honeycomb channels, which in general are made exclusively of catalytic material. Considering, for example, the DeNOx reaction. Fig. 9 shows schematically the NO concentration profiles within the channels/pores and the catalyst wall/layer of the two reactor configurations. [Pg.429]

Figure 22.8 Sorption-reaction (SR) process for removal of trace organic contaminants (a) schematic drawing of a two column SR process, (b) shell and tube reactor configuration for the process, (c) isotherms for adsorption of trace vinyl chloride monomer (VCM) on an activated carbon. Figure 22.8 Sorption-reaction (SR) process for removal of trace organic contaminants (a) schematic drawing of a two column SR process, (b) shell and tube reactor configuration for the process, (c) isotherms for adsorption of trace vinyl chloride monomer (VCM) on an activated carbon.
A recycle reactor is a mathematical model describing a steady plug-flow reactor where a portion of the outlet is recycled to the Met, as shown schematically in Figure 9.5. Although this reactor configuration is rarely used in practice, the recycle reactor model enables us to examine the effect of mixing on the operations of continuous reactors. In some cases, the recycle reactor is one element of a complex reactor model. Below, we analyze the operation of a recycle reactor wifii multiple chemical reactions, derive its design equations, and discuss how to solve fiiem. [Pg.425]

An interesting application of proton-electron conducting membranes has recently been reported by Li et al. [2.76]. These authors studied the conversion of CH4 first to C2H4 and its subsequent direct catalytic aromatization to benzene and other valuable aromatic hydrocarbons. Their reactor configuration is shown schematically in Figure 2.3. The two distinct additional features of their work are the use of an active catalyst for the reaction itself, (Mo/H-ZSM5), and the use of asymmetric membranes with a thin (10-30 pm)... [Pg.23]

The design and operational requirements explained for tubular PBRs are also valid for PBRs in which the catalyst bed is packed in one vessel as described schematically in Figure 1.6a [4]. This reactor configuration is preferred when the reaction is carried out at adiabatic conditions. However, as demonstrated in Figure 1.6b and c [4], bed temperature can be changed by heat addition to/removal from the bed for obtaining a temperature... [Pg.6]

Example 1.3. Our third example illustrates a typical control scheme for an entire simple chemical plant. Figure 1.5 gives a simple schematic sketch of the process configuration and its control system. Two liquid feeds are pumped into a reactor in which they react to form products. The reaction is exothermic, and therefore heat must be removed from the reactor. This is accomplished by adding cooling water to a jacket surrounding the reactor. Reactor elHuent is pumped through a preheater into a distillation column that splits it into two product streams. [Pg.5]

Fig. 3. Schematic diagram of a CSTR. In the configuration shown, up to three different solutions can be pumped (by the peristaltic pump, PP) into the reactor, R. The detectors shown in the diagram are , light absorption (A/, monochromator PM, photomultiplier), platinum (redox), and iodide (or bromide) selective electrodes. The reference electrode is the Hg/Hg2S04 couple, in place of the usual calomel electrode, to avoid adventitious introduction of chloride into the reactor. In addition to these detectors, a thermocouple, or thermistor, and a pH electrode can be inserted into the reactor from above. The recordings of periodic behavior were taken from studies on the chlorite-iodide reaction... Fig. 3. Schematic diagram of a CSTR. In the configuration shown, up to three different solutions can be pumped (by the peristaltic pump, PP) into the reactor, R. The detectors shown in the diagram are , light absorption (A/, monochromator PM, photomultiplier), platinum (redox), and iodide (or bromide) selective electrodes. The reference electrode is the Hg/Hg2S04 couple, in place of the usual calomel electrode, to avoid adventitious introduction of chloride into the reactor. In addition to these detectors, a thermocouple, or thermistor, and a pH electrode can be inserted into the reactor from above. The recordings of periodic behavior were taken from studies on the chlorite-iodide reaction...
Fig. 1.2. Schematic flow configurations of heat-integrated processes for coupling endothermic and exothermic reactions, (a) Countercurrent flow of process streams, (b) Cocurrent flow of the process streams in the reactor stages and heat recovery in separate circuits. Fig. 1.2. Schematic flow configurations of heat-integrated processes for coupling endothermic and exothermic reactions, (a) Countercurrent flow of process streams, (b) Cocurrent flow of the process streams in the reactor stages and heat recovery in separate circuits.
We have developed a one-dimensional non-isothermal model for the countercurrent WGS membrane reactor with a C02-selective membrane in the hollow-fiber configuration using air as the sweep gas. Figure 1 shows the schematic of each hollow-fiber membrane with catalyst particles in the reactor. The modeling study of the membrane reactor is based on (1) the CO2 / H2 selectivity and CO2 permeance reported by Ho [1, 2] and (2) low-temperature WGS reaction kinetics for the commercial catalyst copper oxide, zinc oxide, aluminum oxide (CuO/ZnO/ AI2O3) reported by Moe [3] and others [4]. In this modeling study, the model that we have developed has taken into account critical system parameters including temperature, pressure, feed gas flow rate, sweep gas (air) flow rate, CO2 permeance, CO2 /H2 selectivity, CO concentration, CO conversion, H2 purity, H2 recovery, CO2 concentration, membrane area, water (H20)/C0 ratio, and reaction equilibrium. [Pg.365]

Figure 5.23. Schematic diagram of some typical postcolumn reaction configurations for liquid chromatography. A, non-segmented tubular reactor B, segmented tubular reactor C, extraction segmented reaction detector. P = pump, PS = phase separator, B = device for introducing bubbles and D = detector. Figure 5.23. Schematic diagram of some typical postcolumn reaction configurations for liquid chromatography. A, non-segmented tubular reactor B, segmented tubular reactor C, extraction segmented reaction detector. P = pump, PS = phase separator, B = device for introducing bubbles and D = detector.
Figure 12.11 A schematic diagram of two configurations for photo-assisted CVD. CVD reactors have windows inserted into the reactor tube (vacuum vessel) wall through which light supporting the reaction enters. A detector in parallel incidence can be included to measure absorption in the gas to determine the gas composition and density. Figure 12.11 A schematic diagram of two configurations for photo-assisted CVD. CVD reactors have windows inserted into the reactor tube (vacuum vessel) wall through which light supporting the reaction enters. A detector in parallel incidence can be included to measure absorption in the gas to determine the gas composition and density.

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