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Pilot distillation column

RGA Example In order to illustrate use of the RGA method, consider the following steady-state version of a transfer function model for a pilot-scale, methanol-water distillation column (Wood and Berry, Terminal Composition Control of a Binaiy Distillation Column, Chem. Eng. Sci, 28, 1707, 1973) Ku = 12.8, K = -18.9, K. i = 6.6, and Koo = —19.4. It follows that A = 2 and... [Pg.738]

Mutalib MIA, Zeglam AO and Smith R (1998) Operation and Control of Dividing Wall Distillation Columns Part II Simulation and Pilot Plant Studies Using Temperature Control, Trans IChemE, 76A 319. [Pg.233]

The experimental facility is a pilot-scale distillation column connected to an industrial ABB MOD 300 distributed control system, which in turn is connected to a VAX cluster. The control system consists of a turbo node (configuration, history, console) remote I/O, and an Ethernet gateway, which allows communication with the VAX-station cluster through the network. This connection allows time-consuming and complex calculations to be performed in the VAX environment. Figure 10 shows the complete setup. [Pg.261]

Nooraii, A., Barton, G., and Romagnoli, J. A. (1994). On-line data reconciliation, simulation and optimising control of a pilot-scale distillation column. Process Syst. Eng. PSE 94 2, 1265-1268. [Pg.270]

A summary of several example cases illustrated in Mujtaba and Macchietto (1998) is presented below. Instead of carrying out the investigation in a pilot-plant batch distillation column, a rigorous mathematical model (Chapter 4) for a conventional column was developed and incorporated into the minimum time optimisation problem which was numerically solved. Further details on optimisation techniques are presented in later chapters. [Pg.39]

In the mid Eighties, 99 batch processes within 74 UK companies were identified (Parakrama, 1985). In the last decade or more a continuous shift towards batch processes has been noticed and many small-scale companies are using their existing continuous columns for batch distillation (Willet, 1995) without much realising the implications of such practice. Also R D sections of many multi-national chemical companies do the pilot plant study in CBD columns for their continuous distillation columns which are in operation in the plant (Chen, 1995 Jenkins, 2000 Greaves, 2003). Because of confidentiality the results of such studies are not available in public. [Pg.331]

In Greaves et al. (2001), a hybrid model for an actual pilot plant batch distillation column is developed. However, taking advantage of some of the inherent properties of batch distillation processes a simpler version (new algorithm) of the general optimisation framework is developed to find optimal reflux ratio policies which minimises the batch time for a given separation task. [Pg.368]

Discrete reflux ratio used in most pilot plant batch distillation columns, including those used in industrial R D Departments (Jenkins, 2000 Greaves, 2003), does not allow a direct implementation of the optimum reflux ratio (treated as a continuous variable) obtained using a model based technique (as presented in earlier chapters of this book). In Greaves et al. (2001), a relationship between the continuous and the discrete reflux ratio is developed. This allows easy communication between the model and the process and comparison on a common basis. [Pg.368]

Hybrid Model Development for Pilot Batch Distillation Column... [Pg.373]

In Greaves et al. (2001) and Greaves (2003), instead of using a rigorous model (as in the methodology described above), an actual pilot plant batch distillation column is used. The differences in predictions between the actual plant and the simple model (Type III and also in Mujtaba, 1997) are defined as the dynamic process-model mismatches. The mismatches are modelled using neural network techniques as described in earlier sections and are incorporated in the simple model to develop the hybrid model that represents the predictions of the actual column. [Pg.373]

Pilot-plant data are almost always required for the design of filters unless specific information is already available for the type of materials and conditions involved. Heat exchangers, distillation columns, pumps, and many other types of conventional equipment can usually be designed adequately without using pilot-plant data. [Pg.36]

Implementation of a Reactive Dividing Wall Distillation Column in a Pilot Plant... [Pg.229]

The pilot plant has been running since late 1978. It was proved in a test run with a feed of more than 150 car tyres, that the process is self-sufficient in its energy needs, producing at a temperature of 720°C, even excess pyrolysis gas to supply other heat necessary. Waste heat from the reactor heating is sufficient to heat the distillation column. [Pg.421]

Aittamaa (1981) simulated a number of experiments with the systems ethanol-benzene-n-heptane, and chloroform-benzene-n-heptane (data were obtained at Hoffmann-La Roche in a fair size pilot scale column) and 1-butanol-ethanol-water in a 12 sieve-tray column. The Hoffman-La Roche data were taken in a column having 24 sieve trays and 30-cm inside diameter. Unlike many studies of distillation efficiency, these experiments were not carried out at total reflux. The measured flow rates and compositions of the feed, distillate, and... [Pg.391]

A pilot-scale distillation column located at the University of Sydney, Australia is used as the case study [60]. The 12-tray distillation column separates a 36% mixture of ethanol and water. The following process variables are monitored temperatures at trays 12, 10, 8, 6, 4, and the reflux stream, bottom and top levels (condenser), and the flow rates of bottoms, feed, steam, distillate and reflux streams. The column is operated at atmospheric pressure using feedback control. Three variables are controlled during the operation top product temperature, condenser level, and bottom level. Temperature at tray 8 is considered as the inferential variable for top product composition. To maintain a desired product composition, PI controllers cascaded on flow were used to manipulate the reflux, top product and bottom product streams. [Pg.198]

The best known and most used empirical method is that of O Connell (Figure 12.60), for distillation columns and absorbers. The curves are based on plant data for several bubble-cap columns plus a few pilot-scale units. Efficiency is related to two properties of the feed mixture liquid viscosity and relative volatility a. Higher values of the p a product indicate larger liquid-side mass transfer resistance and hence a lower efficiency. For a vapor feed or a mixed vapor-liquid feed, the correlating viscosity should be that of the feed tray liquid. [Pg.1048]

The over-all performance of /3-methoxypropionitrile solvent in the pilot plant tests qualify it as a superior replacement solvent for furfural in butadiene extractive distillation plants. It offers distinct economic and operational advantages. Operation at lower solvent-to-C4 feed ratios greatly increases existing extractor capacity. In addition, the improved separation of trans-2-butene and butadiene in the extractive distillation column reduces the load on the final butadiene purification column. Operation at lower solvent-to-C4 feed ratio and lower reboiler temperature provides substantial utility savings. The lower reboiler temperature also reduces the rate of butadiene dimer formation. [Pg.234]

Analyse the feasibility of different control structures by a controllability analysis for a distillation column methanol-water. Consider the data of the EboAkademi pilot-scale column (Haggblom Waller, 1992). [Pg.494]

When chromatographic separations (7) are operated in a batch mode, a portion of the mixture to be separated is introduced at the column inlet. A solute-free carrier fluid is then fed continually through the column, the solutes separating into bands or zones. Some industrial operations such as mixed-vapor solvent recovery and sorption of the less volatile hydrocarbons in natural gas or natural gasoline plants are being carried out on pilot plant and semiworks scales. Continuous countercurrent systems designed along the basic principles of distillation columns have been constructed. [Pg.24]


See other pages where Pilot distillation column is mentioned: [Pg.202]    [Pg.366]    [Pg.28]    [Pg.36]    [Pg.14]    [Pg.108]    [Pg.68]    [Pg.470]    [Pg.433]    [Pg.31]    [Pg.192]    [Pg.198]    [Pg.228]    [Pg.107]    [Pg.295]    [Pg.330]    [Pg.10]    [Pg.387]   
See also in sourсe #XX -- [ Pg.242 ]

See also in sourсe #XX -- [ Pg.242 ]




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