Batch reactor systems

The reaction rate ( rco) for a constant volume batch reactor system is equal to the rate of mass transfer (r coy. 

For a batch reactor system only the accumulation and dissipation terms are important. Thus... 

A detailed description of hardware, software and mathematical analysis of the computer controlled batch reactor system is... 

Figure 1. Schematic Flow Diagram of the Computer Controlled Batch Reactor System. (Reproduced with permission from Ref. 9. Copyright 1987 Pergamon Journals Ltd.)...

Hydroformyl ati on of Polybutadiene - A number of hydroformyl at ion experiments were performed using the automated batch reactor system in order to synthesize the hydroformylated polybutadiene with varying degree of reaction completion (2 to 20% of the total C=C present). The following reaction conditions were employed PBD = 1.55 x 103 mol/m3, RhH(CO) (P(C6HJ3 )3 = 0.58... 

Operating conditions. Optimization variables such as batch cycle time and total amount of reactants have fixed values for a given batch reactor system. However, variables such as temperature, pressure, feed addition rates and product takeoff rates are dynamic variables that change through the batch cycle time. The values of these variables form a profile for each variable across the batch cycle time. 

Commercial plastics HDPE, PP, PS and PVC in granulate form have been used as model feed. The degradation of pure polymers was followed using either at thermoanaly-tical method (MOM Derivatograph Q) or in a laboratory batch reactor system with gaschromatographic product analysis. 

Ong SA, Toorisaka E, Hirata M et al (2005) Treatment of azo dye orange II in a sequential anaerobic and aerobic-sequencing batch reactor system. Environ Chem Lett 2 203-207... 

The RC1 is designed to simulate closely the operation of large scale batch and semi-batch reactor systems. The RC1 equipment consists of the reaction vessel, overhead condenser for reflux/distillation operations, receiver, metering pumps, and a heat transfer fluid heating/cooling circulating unit. Me-... 

Many of the above factors apply to semi-batch reactor systems as well. Also, the following factor is important for semi-batch reactor systems ... 

BATCHD - Dimensionless Kinetics in a Batch Reactor System... 

According to the vendor, the estimated price of remediation using a soil slurry-sequencing batch reactor system was 50 to 110/m of waste treated in 1995. Costs are usually 1.5 to 2 times less than excavation and inceration. The quantity of waste and initial contaminant concentration were cited as the most significant factors effecting price (D10036N, p. 15 D15328G, p. 7). 

For the activity tests an 8-fold batch reactor system (reactor volume 20 ml) with magnetic stirring which allows the measurement of hydrogen uptake at constant hydrogen pressure was used. Analysis of substrates and products was performed offline by GC for determining selectivity values. Activity values were derived from hydrogen up-take within a defined time interval. Hydrogenation of both cinnamic acid and dibenzylether were carried out at 10 bars and 25°C. 

Design of a batch reactor system for adsorption and ion exchange Suppose that the system obeys the following equilibrium equation ... 

The finite solution volume model for solid-diffusion control (Patterson s model) will be used (eq. (4.52)). Following the procedure presented in the section Design of a batch reactor system for adsorption and ion exchange (eqs. (4.119)-(4.125)), we obtain the results shown in Table 4.23. 

In conclusion, the maximum adsorption capacity should be measured in fixed-bed experiments under dynamic conditions, and if models are applicable, diffusion coefficients should be also determined in fixed-bed apparatus. Due to the fact that the equilibrium isotherms require extended data series and thus are time-consuming experiments, the latter are quite difficult to be conducted in fixed-bed reactors and from this point of view, it is more practical to evaluated equilibrium isotherms in batch reactor systems. Then, it is known that when applying fixed-bed models using an equilibrium isotherm obtained in batch-type experiments, the equilibrium discrepancy (if it exists) can be compensated by a different estimate for the solid diffusion coefficient (Inglezakis and Grigoropoulu, 2003 Weber and Wang, 1987). 

As the feed concentrations of aromatic contaminants are increased, low concentrations of gas-phase intermediate products are occasionally reported. During the photocatalytic oxidation of aromatic contaminants in the 25-500-ppm range, some researchers have observed up to several ppm of gas-phase intermediate products. For example, Ibusuki and Takeuchi [8] detected 1-2 ppm of benzaldehyde in the gas phase following photocatalytic oxidation of 80 ppm of toluene in a batch-reactor system. Even at moderate aromatic feed concentrations, gas-phase intermediate concentrations may be too low to be detected reliably. 

An important parameter in a number of fields is the study of inorganic phosphate. Recently, Kwan et al. [206,207] have reported on a screen-printed phosphate biosensor based on immobilised pyruvate oxidase (PyOD) for monitoring phosphate concentrations in a sequencing batch reactor system [206] and in human saliva [207]. The enzyme was immobilised by drop-coating a Nation solution onto the working electrode surface this was then covered by a poly(carbamoyl) sulfonate (PCS) hydrogel membrane. 

This fed-batch example illustrates some of the fascinating aspects of design and operating a batch reactor system. The issue of dynamic controllability dominates in most systems, but the economics of the operation can also be strongly affected by the impact of control on conversion and yield. 

Figure 1. Flow diagram of batch reactor system.

From the above mole balance equation we can develop the design equation for various reactor types. By solving the design equation we can then determine the time required for a batch reactor system or a reactor volume for a continuous flow system to reach a specific conversion of the reactant to products. 

As a test reaction, the alkylation of benzene with dodecene was chosen. The batch reactor system consisted of a round-bottomed flask (slurry reactor) provided with a cooler, gas-inlet valve, and sampling exit. A magnetic stirrer equipped with a thermostat and a silicon oil bath were used to maintain the reaction temperature and ensure the homogeneity of reactants. The catalyst was weighed in the reactor and then benzene was added according to the proportion desired, followed by the addition of dodecene. 

Two reports of the use of molecular hydrogen to reduce the N—O bond have appeared for the trinuclear cluster HRu3(CO)io(NO) (84, 85). Equation (39) represents the results obtained using a batch reactor system... 

Plot the fractional conversion and temperature as a function of time for the batch reactor system described in Example 9.3.3 if the reactor is now adiabatic (U = 0). Compare your results to those for the nonisothermal situation given in Figure 9.3.3. How much energy is removed from the reactor when it is operated nonisothermally ... 

For batch-reactor systems in which the volume varies while the reaction is proceeding, the volume may usually be expressed either as a function of time alone or of conversion alone, for either adiabatic or isothermal reactors. Consequently, the variables of the differential equation (2-6) can be separated in one of the following ways ... 

Bae T-H, Han S-S, and Tak T-M. Membrane sequencing batch reactor system for the treatment of dairy industry wastewater. Process Biochem, 2003 39(2) 221-231. 

Comparative tests have been performed in the semi-batch reactor system to evaluate the Ru/Ti02 cataly versus a more conventional nickel-based catalyst. These tests show that rutlienium at only 3% metal loading has about the same activity as nickel at S0% metal loading. This comparison is only for short-term activity of the catalyst. As demonstrated in the continuous flow tests, the nickel catalyst loses activity readily in tlie first hours on stream, while the ruthenium maintains its activity. 

It is known that formic acid is synthesized from H2/CO2 as ester in alcohol solvent using metal complex catalysts such as HM(CO)5 (M W,Cr,Ru) in batch reactor system.[61] However, specific activity (TOF) of these system are relatively low. Recently, Noyori et al. found a significant increase of formic acid in a supercritical mixture of H2/CO2 with N(C2H5)3 using RuH2 P(CH3)3)4 complex at the condition of 20.5 Mpa, 5013 and H2/C02=l/1.4.[62] TOF increased one order of magnitude over that of conventional process because of high miscibdity of H2 with supercritical CO2. It is also noted that methyl formate produced from H2/CO2 is easdy converted to acetic acid by isomerization reaction. 

The EUREKA process is a commercially proven thermal craeking process of semi-batch reactors system to produce valuable cracked oil and aromatic petroleum pitch from heavy residual material. The first unit was built in Sodegaura Refinery of Fuji Oil, Japan in 1975. The second unit was built in Nanjing, P. R. China in 1988. Both the units are now operated effectively for heavy oil upgrading. 

Garrido, J. M., Omil, F., Arrojo, B., Mendez, R., and Lema, J. M. (2001). Carbon and nitrogen removal from a wastewater of an industrial dairy laboratory with a coupled anaerobic filter-sequencing batch reactor system. Water Sci. Technol. 43, 249-256. 

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