Estimate check list

A partial check list of operations for an industrial chemical laboratory is shown in Table 1. The format of a formal list will vary considerably from one laboratory to another, but with such an aid, one can easily see which operations are compatible and then group these together. Those that need special treatment will readily stand out. The planner will also be able to estimate the number of rooms required for the total operation. Finally, a complete list of all laboratory functions will facilitate the next step, an estimate of space requirements. 

Satisfactory estimation of the direct operating costs for a computer installation is usually not difficult. It is naturally one of the first thoughts when selection of a computer is considered. There are many factors to be taken into account, since the total cost is meaningful only when related to the computer s capabilities. Wainwright (Wl) gives an extensive check list of features to be considered in any comparative evaluation of digital computers. 

Of the many factors which contribute to poor estimates of capital investments, the most significant one is usually traceable to sizable omissions of equipment, services, or auxiliary facilities rather than to gross errors in costing. A check list of items covering a new facility is an invaluable aid in making a complete estimation of the fixed-capital investment. Table 1 gives a typical list of these items. 

Safety Systems. Major expenditures here include the flare system (the flare structures and large lines extending throughout the plant) and the iirevvater system (high-capacity pumps and extensive piping). Safety systems, fortunately, are usually given particular attention. At this study phase, the main thrust should be to check the completeness of licensor equipment lists for cost estimation purposes. 

Local ones are listed in the yellow pages of the telephone directory. The laboratory operator should contact more than one for suggestions and estimates. In such discussions, a disposal service vdll ask detailed questions as to the exact nature of the waste and quantities involved. An agreement will be made about the types of shipping containers to be used. These are non-returnable. The disposal service may sell suitable containers and require these for certain types of waste. In other cases, the laboratory may provide its own. If drums are needed, they are available from companies engaged in drum reconditioning. Manufacturers of chemicals may have used drums available at reasonable prices, but since these wdll contain residues of their former contents, a check for compatibility must be made before using them. 

There are to be found lists of chemical substances in handbooks for each of which log P = f (T), and whose coefficients are to be inserted, are given. These lists are limited but nevertheless provide solutions for the most common chemical substances. When there are several experimental estimates of vapour pressures it is possible to estimate the importance of the experimental uncertainty from the standard deviation of the measurements. The relevance of the values can be verified from a series of different sources (to be rigorous, checking that it is a Gaussian sequence would be required). 

To illustrate this with a few cases to demonstrate the possibilities and iimits of this method, chemicais wiil be chosen for which there are numerous vaiues of LC and/or LD50 avaiiabie to be abie to check the quality of the estimates. For each of these the values that are listed in the safety data in Part Three will be given. 

If the maximum number of allowable iterations is reached, the software provides intermediate values of all quantities calculated. These intermediate values are used as initial estimates to continue the solution. However, if any one of Ha, kM, or D is at the upper or lower boundary specified above, values of kM, D, a, pAout, L, and usg are all reset to their initial values as listed above for the other quantities, the intermediate values are used. This latter procedure is also used to check a solution that has apparently converged with any one of the three quantities at a boundary. 

The molecular weight distribution obtained from SEC analysis was also shown in Fig. 8. In order to check the effect of the estimated exponent a(-0.55) on molecular weight distribution for Ei branched PVAc, we used another a(-0.58) value to compute a new calibration curve as shown in Fig. 9. The two calibration curves almost overlapped with each other. The results are listed in Table 2. In both cases, we obtained the same weight-average molecular weight and the polydispersity index (M /M ). Thus, we could confirm that in using a two-point (Bq and %l) estimate for a, we have not introduced an appreciable error in the determination of molecular weight distribution of branched PVAc. 

These pieces of equipment are not installed. Preliminaiy estimates have indicated that all of these pieces of equipment have adequate capacity for the present design. They are valued at a total of 300,000. For the purpose of your cost estimates, you may assume that 300,000 will cover the cost of the listed equipment. However, your design should include complete specifications for all fee equipment necessary for toe new plant In this wry, we will be able to have a final check to show us if the present equipment on hand is satisfactory. 

Of the 14 formulations listed in Table 1, six experimental runs were required to fit the quadratic mixture model, four additional distinct runs were used to check for the lack of fit, and finally four runs were replicated to provide an estimate of pure error. Design-Expert used the vertices, the edge centers, the overall centroid, and one point located halfway between the overall centroid and one of the edge centers as candidate points. Additionally, four vertices of the design region were used as check points [106],... 

To further check the consistency of the method, we compare the copolymer s diffusion coefficient in THF, calculated from equation 3, with an independent measurement. Using our experimentally determined values of My and [ry], equation 3 predicts a D value of 9.85 X 10 cm /s this is in good agreement with the value of 9.79 X 10 cm s measured independently using NMR by workers at Exxon. (A similar comparison in toluene cannot be made because an independent value of D in toluene is not available.) A treatment of the propagation of errors is summarized in Table II. Here, uncertainties in My and Xa propagated by estimated uncertainties in the independent variables are listed. The largest uncertainty comes from the Dt values, but accurate retention data are also critical. For example, a 2% uncertainty in retention parameter X translates to a 9-10% uncertainty in My and a 5-8% uncertainty inXA. 

It was precisely this phenomenon, which had reached full tide by the middle of the nineteenth century, that Proudhon had in mind when he declared, "To be ruled is to be kept an eye on, inspected, spied on, regulated, indoctrinated, sermonized, listed and checked off, estimated, appraised, censured, ordered about.. .. To be ruled is at every operation, transaction, movement, to be noted, registered, counted, priced, admonished, prevented, reformed, redressed, corrected. ... 

The column converges quickly with the good estimate provided from the shortcut model. The column profiles can be checked by selecting the Performance tab in the column environment and then selecting Plots from the menu on the left and Composition from the list of possible plots, as shown in Figure 4.24. This generates composition profiles like those presented in Figures 4.12 to 4.17. 

The metal dispersion and the average particle sizes calculated from the hydrogen chemisorption data are listed in Table 2 and are in close correspondence with the TEM estimated values. The reproducibility of the HDP procedure was checked several times and always high dispersions and rutheirium particles were found with TEM in the 1-2 nm range. 

Regarding quality of the values listed. Dr. Barin has wisely relied heavily on critically evaluated data (CODATA and JANAF) in cases where such values are available. For other substances he has drawn on a wide variety of sources, including the USBM Bulletins, other compilations, the periodical literature, and his own estimation of some thermochemical data. As new measurements are made, and as new critical evaluations become available, many of the Barin tables will require revision, but this is a characteristic of any attempt to compile thermochemical data. Anyone making thermochemical calculations who insists on the best possible data, will use a compilation, such as that of Barin or JANAF, as a starting place, but he will then check the recent periodical literature for new measurements that may have rendered the compiled values obsolete. This in no way detracts from the value of the compilation by Dr. Barin, which offers a starting place that is far more comprehensive than others, particularly for those concerned with metallurgical and similar systems. 

Thermal expansion and fire cases are not required to be checked, if the existing equipment is re-used, with the same service and also the same level control setting. Overpressure relief requirements due to each utility failure, fire cases and any other combination scenarios need to be estimated. API 521 (2014) has a comprehensive list of effects for utilities failure. All the PRV manifolds shall be checked to estimate back pressures at the PRVs. PRD overpressure calculations for equipment shall be documented as shown in Table 3.4. Vacuum relief (if the vessel/s is/are not designed to withstand full vacuum) shall also be documented. All the flare scenarios and flare network shall be properly documented. An example of PRV sizing calculations for the system shown in Figure 3.5 is presented in Table 3.4. 

A preliminary estimate of the height of the probable maximum storm surge should then be made by using the values of parameters representing the characteristics listed as inputs to empirical relationships. Whenever possible, these results should be compared with historical records of storm surges to check the suitability of the method used. A method that results in a calculated extreme event that is lower in magnitude than any event that was recorded is unacceptable. 

The ESR spectra do not themselves yield estimates of the CEF parameters. However, when taken in conjunction with other data the wave-functions of the lowest levels can be accurately checked by the g-factor values which they yield. In the case of Pr in lanthanum ethyl sulfate, for example. Baker and Bleaney (1958) originally estimated the CEF parameters on the basis of the magnetic susceptibility data then available. Subsequently, these parameters have been determined from high resolution optical data for all of the lanthanide ions in the ethylsulfates. A complete listing of these is given, for example, in Abragam and Bleaney (1970). 

---