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Operating Procedures steady-state

Consider the segment of tubular reactor shown in Figure 8.3. Since the fluid composition varies with longitudinal position, we must write our material balance for a reactant species over a different element of reactor (dVR). Moreover, since plug flow reactors are operated at steady state except during start-up and shut-down procedures, the relations of major interest are those in which the accumulation term is missing from equation 8.0.1. Thus... [Pg.263]

The material balance equation for a PFR is obtained by considering a differential longitudinal section of the reactor, followed by integration of the differential balance over the length of the reactor. This procedure gives the following result for a PFR operating at steady state ... [Pg.175]

Catalyst Preparation. "Reactor-equilibrated VPO catalysts were prepared by a nonaqueous procedure detailed in previous papers [14], and operated at steady-state conditions (1.5% n-butane, 15 psig reactor inlet pressure and 2000 GHSV) for approximately 3000 hours. Under steady-state conditions the catalyst gave selectivities to MA of approximately 66% at 78% conversion. XRD analysis of the reactor-equilibrated samples showed that they were monophasic (VO)2P20 . Chemical analysis gave a P/V ratio of 1.01 and vanadium oxidation state of 4.02. The samples had a BET surface area of 16.5 m /gm. [Pg.200]

The strong parametric sensitivity resulting from this coupling largely determines the start-up procedure, steady-state and transient operations (Ruiz et al., 1995). Moreover, even small variations in the input variables might lead to unstable conditions (Alejski and Duprat, 1996). This fact implies that a feasible operation of a RD column requires several control loops to mitigate the effects of disturbances. [Pg.144]

Here, we call all the different units. In this case, we operate in steady-state conditions for all the units, specified in the tasks before. gPROMS always solves the entire model at once. In case there is a unit or units that operate in unsteady state, we can define an operating procedure so that the products of the batch process are obtained and used in the next unit. [Pg.414]

The technique of internal normalization is commonly apphed in both MC-ICP-MS and TIMS for the precise correction of the instrumental mass bias (see also Chapter 5) that is encountered during the analysis of radiogenic isotopic compositions [33, 34]. The ICP ion source of MC-ICP-MS, however, also features two characteristics that play an important role for isotopic analysis, where internal normalization cannot be applied. First, an ICP source operates at steady state and therefore mass fractionation is not primarily a time-dependent process, as in TIMS where the measured isotopic compositions change with time due to the progressive evaporation of a sample from the filament. The steady-state operation of an ICP ion source is beneficial for the correction of instrumental mass bias by external standardization, where the isotope ratio data obtained for a sample are referenced to the values obtained for bracketing analyses of an isotopic standard [27, 35]. Hence, this procedure is commonly termed standard-sample bracketing. [Pg.287]

The laboratory studies utilized small-scale (1-5-L) reactors. These are satisfactoiy because the reaction rates observed are independent of reac tor size. Several reac tors are operated in parallel on the waste, each at a different BSRT When steady state is reached after several weeks, data on the biomass level (X) in the system and the untreated waste level in the effluent (usually in terms of BOD or COD) are collected. These data can be plotted for equation forms that will yield linear plots on rec tangular coordinates. From the intercepts and the slope or the hnes, it is possible to determine values of the four pseudo constants. Table 25-42 presents some available data from the literature on these pseudo constants. Figure 25-53 illustrates the procedure for their determination from the laboratory studies discussed previously. [Pg.2219]

All processes may be classified as batch, continuous, or semibatch depending on how materials are transferred into and out of the system. Also, the process operation may be characterized as unsteady state (i.e., transient) or steady state, depending on whether the process variables (e.g., pressure, temperature, compositions, flowrate, etc.) are changing with time or not, respectively. In a batch process, the entire feed material (i.e., charge) is added instantaneously to the system marking the beginning of the process, and all the contents of the system including the products are removed at a later time, at the end of the process. In a continuous process, the materials enter and leave the system as continuous streams, but not necessarily at the same rate. In a semibalch process, the feed may be added at once but the products removed continuously, or vice versa. It is evident that batch and semibatch processes are inherently unsteady state, whereas continuous processes may be operated in a steady or unsteady-state mode. Start-up and shut-down procedures of a steady continuous production process are examples of transient operation. [Pg.332]

The utihty stream gets started at operating temperature and flow rate. In the following experiments, the utihty stream is heated so as to initiate the reaction. The main and secondary process tines are fed with water at room temperature and with the same flow rate as one of the experiments. Once steady state is reached, operating parameters are recorded. Process tines are then fed with the reactants, hydrogen peroxide and sodium thiosulfate. At steady state, operating parameters are recorded, and a sample of a known mass of reactor products is introduced in the Dewar vessel. Temperature in the Dewar vessel is recorded until equilibrium is reached, that is, until the reaction ends. This calorimetric method is aimed at calculating the conversion rate at the product outlet and thus the conversion rate in the reactor. The latter is also determined by thermal balances between process inlet and outlet of the reactor. Finally, the reactor is rinsed with water. This procedure is repeated for each experiment... [Pg.278]

The main advantage of the above estimation procedure is that there is no need to assume steady-state operation. Since practice has shown that steady state operation is not easily established for prolonged periods of time, this approach enables the determination of average specific rates taking into account accumulation terms. [Pg.128]

With the exception of this method, all the methods described solve the stage equations for the steady-state design conditions. In an operating column other conditions will exist at start-up, and the column will approach the design steady-state conditions after a period of time. The stage material balance equations can be written in a finite difference form, and procedures for the solution of these equations will model the unsteady-state behaviour of the column. [Pg.545]

After the processing steps have been selected and ordered, the amount and composition of each process stream entering and leaving each unit must be specified. This is an accounting procedure. It assumes a steady-state operation. That is, at any point in space there is no change occurring with respect to time. [Pg.84]

The design q>roblem can be approached at various levels of sophistication using different mathematical models of the packed bed. In cases of industrial interest, it is not possible to obtain closed form analytical solutions for any but the simplest of models under isothermal operating conditions. However, numerical procedures can be employed to predict effluent compositions on the basis of the various models. In the subsections that follow, we shall consider first the fundamental equations that must be obeyed by all packed bed reactors under various energy transfer constraints, and then discuss some of the simplest models of reactor behavior. These discussions are limited to pseudo steady-state operating conditions (i.e., the catalyst activity is presumed to be essentially constant for times that are long compared to the fluid residence time in the reactor). [Pg.491]

Some recent applications have benefited from advances in computing and computational techniques. Steady-state simulation is being used off-line for process analysis, design, and retrofit process simulators can model flow sheets with up to about a million equations by employing nested procedures. Other applications have resulted in great economic benefits these include on-line real-time optimization models for data reconciliation and parameter estimation followed by optimal adjustment of operating conditions. Models of up to 500,000 variables have been used on a refinery-wide basis. [Pg.86]

This procedure (based on sample variance and covariance) is referred to as the direct method of estimation of the covariance matrix of the measurement errors. As it stands, it makes no use of the inherent information content of the constraint equations, which has proved to be very useful in process data reconciliation. One shortcoming of this approach is that these r samples should be under steady-state operation, in order to meet the independent sampling condition otherwise, the direct method could give incorrect estimates. [Pg.203]

Whenever multiple steady states in a reactor are possible, we must be very concerned that we are operating on the desired steady-state branch. This requires a proper startup procedure to attain the desired steady state and suitable operation limits to make sure that we never exhibit a sufficiently large transient to cause the system to fall off the desired conversion branch. We will consider transients in the CSTR in the next section. [Pg.256]

The details of the experimental apparatus and procedures are outlined in another paper (76). The reactor consisted of a quartz tube with an inside diameter of 18 mm which held the monolith or gauze pack. The reactor was operated at a steady state temperature which is a function of the heat generated by the exothermic reactions and... [Pg.417]

The equations and procedure described here apply only to steady-state operation. If there is large fluctuation in basin temperature, or if a more precise day-to-day evaluation is desired, another term must be included in the heat balances. This is the... [Pg.165]

Once the actual extraction-section aqueous feed is started, the process should be close to steady state after three residence times of the fluid have passed through the contactor stages. This action will typically take 15 to 30 min. If the above startup procedure is used, the decontamination factor for the extraction section will always be greater than the desired value, even during startup. Once steady-state operation is reached, the process is easy to control. The operator needs to check that the required feed flow rates are maintained, that the feed in each feed tank is appropriate, and that the rotors are spinning at the proper speed. Also, the feed tanks need to be monitored to avoid them running dry, and the effluent tanks need to be monitored for overflow. In plant operation, these tasks are usually automated. [Pg.592]

API Recommended Practice 520 Part I, Sizing and Selection This API design manual includes basic definitions and information about the operational characteristics and applications of various pressure relief devices. It also includes sizing procedures and methods based on steady state flow of Newtonian fluids. This RP covers equipment that has a maximum allowable pressure of 15 psig (1.03 barg) or greater. [Pg.76]

A modular reactor similar to the approach of Adler et al. [11] was introduced by Muller and co-workers [37, 38, 56], The screening procedure was separated into a number of process operations. In chemical process engineering, these so-called unit operations are essential components of every complex plant. As catalyst screening involves many different processes such as heat exchange, flow distribution, sampling, analysis and reaction, such a subdivision into unit operations is justified. The flexibility of such a system was demonstrated with two exemplified configurations later, one of which was used for transient studies and one for steady-state experiments (Figure 3.30). [Pg.440]

Whereas the operation of batch reactors is intrinsically unsteady, the continuous reactors, as any open system, allow for at least one reacting steady-state. Thus, the control problem consists in approaching the design steady-state with a proper startup procedure and in maintaining it, irrespective of the unavoidable changes in the operating conditions (typically, flow rate and composition of the feed streams) and/or of the possible failures of the control devices. When the reaction scheme is complex enough, the continuous reactors behave as a nonlinear dynamic system and show a complex dynamic behavior. In particular, the steady-state operation can be hindered by limit cycles, which can result in a marked decrease of the reactor performance. The analysis of the above problem is outside the purpose of the present text ... [Pg.11]


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