Charts permissions

For composition see footnote to Table 2-310. Some values read from charts are approximate. Material used hy permission of DuPont Fluoroproducts. 

V, h, and 5 from DuPont bull. T—MP 66—SI, Jan. 1993 (17 pp.). Cp, i, and k from DuPont bull. ART 10, Jan. 1993 (27 pp.). Some values read from charts maybe approximate. Material used by permission of DuPont Fluoroproducts. h = normal boiling point. 

Unpublished data of General Chemicals Division, Allied Chemical Company. Used by permission, c = critical temperature. No material in SI units appears in the 1993 ASHRAE Handbook—Fundamentals (SI ed.). Tables and a chart to 50 ata, 200 C are given by Mathias, H. and H. J. Loffler, Techn. Univ. Berhn rept., 1966 (42 pp.). A chart to 1500 psia, 500 F was given by Mears, W. H., E. Rosenthal, et al.,y, Chem. Eng. Data, 11, 3 (1966) 338-. l43. 

Figure B-24. Generalized compressibility chart. (Excerpted by special permission from Chemical Engineering, July 1959, copyright 1954, by McGraw-Hill, Inc., New York, NY.)...

Figure B-31. Natural gas compressibility chart, 0.75 S.G (Reprinted by permission and courtesy of Ingersoll-Rjiid i...

In order to assist with the design of the ribbed plate, Fig. 2.28 shows a chart to enable permissible combinations of dimensions to be chosen. For example, suppose that we wish the plate thickness to be 2 mm and there are to be five ribs (= N) across the plate. 

Figure 11-24. Pulsation bottle sizing chart lapproximotion). (Reprinted with permission from GPSA Engineering Data Book, 10th Ed.j...

Figure 1-1. A process engineering section supervision chart. By permission, E. E. Ludwig [7].

Figure 2-3. Moody or regular Fanning friction factors for any kind and size of pipe. Note the friction factor read from this chart is four times the value of the f factor read from Perry s Handbook, 6th Ed. [5]. Reprinted by permission, Pipe Friction Manual, 1954 by The Hydraulic Institute. Also see Engineering DataBook, 1st Ed., The Hydraulic Institute, 1979 [2]. Data from L. F, Moody, Friction Factors for Pipe Flow by ASME [1].

Figure 2-17. Flow coefficient C for nozzles. C based on the internal diameter of the upstream pipe. By permission, Crane Co. [3]. Crane reference [9] is to Fluid Meters, American Society of Mechanical Engineers, Part 1-6th Ed., 1971. Data used to construct charts. Chart not copied from A.S.M.E. reference.

Figure 2-32. Steam flow chart. (By permission, Walworth Co. Note use for estimating only (this author).)...

Figure 2-38C. Critical Pressure Ratio, r, for compressible flow through nozzles and venturi tubes. By permission, Crane Co., Technical Paper 410, 1957. Also see 1976 edition. See note at Figure 2-18 explaining details of data source for chart. Note P = psia p= ratio of small-to-large diameter in orifices and nozzles, and contractions or enlargements in pipes.

Figure 2-54. Sarco flashing steam condensate line sizing flow chart. By permission, Spirax-Sarco, Inc., Allentown, Pa. [59].

Rgure 2-55. Flashing steam condensate line sizing chart. By permission, Ruskin, R. R, Calculating Line Sizes for Flashing Steam Condensate, Chem. Eng., Aug. 18,1985,... 

Figure 3-56. Viscosity performance correction chart for centrifugal pumps. Note do not extrapolate. For centrifugal pumps only, not for axial or mixed flow. NPSH must be adequate. For Newtonian fluids only. For multistage pumps, use head per stage. (By permission. Hydraulic Institute Standards for Centrifugal, Rotary, and Reciprocating Pumps, 13th ed.. Hydraulic Institute, 1975.)...

Figure 4-4. Comparison chart showing ranges of performance of severai collection/control devices in air streams. By permission, Vandegrift, ef. a/. Chemical Engineering, Deskbook issue, June 18, 1973, p. 109.

Figure 5-2. Generai seiection chart for mixing. By permission, Lyons, E. J. and Parker, N. H., Chem. Engr. Prog., V. 50,1954, p. 629 [12],...

Figure 5-7. Analysis flow chart for examining types of turbine impeller applications. By permission, Gates, L. E., et a ., Chem. Eng., Dec. 8, 1975, p. 110 [26].

Figure 6-38. Chart for liquid ring vacuum pump to estimate the total volume to be displaced to evacuate a closed vessel to a predetermined vacuum. By permission, Graham Manufacturing Co., Inc.

Figure 7-7A. Pressure level relationship conditions for pressure relief valve installed on a pressure vessel (vapor phase). Single valves (or more) used for process or supplemental valves for external fire (see labeling on chart). Reprinted by permission, Sizing, Selection and Installation of Pressure Relieving Devices in Refineries, Part 1 Sizing and Selection, API RP-520, 5th Ed., July 1990, American Petroleum Institute.

Figure 7-23. Liquids viscosity correction using chart method for Kp. By permission, Teledyne Farris Engineering Co.

Figure 8-4B. DePriestsr Charts K-Values of light hydrocarbon syst s, generalized correlations, high-temperature range. Used by permission, The American Institute of Chemical Engineers, Chemicai Engineering Progress Ser. 49, No. 7 (1953), all rights reserved.

Figure 8-24B. Chart for reflux vs. trays. Use this nomogram for Gilliland s calculations for number of theoretical plates/trays. Used by permission, Mapstone, G.E., Hydrocarbon Processing, V. 47 No. 5 (1968), p. 169, Gulf Publishing Co., all rights reserved.

Figure 8-51. Working chart for Yaws, et. al short-cut method for multicomponent distillation for estimating component recovery in distillate and bottoms. Used by permission, Yaws, C. L. et al., C/iem. Eng., Jan. 29 (1979), p. 101.

Figure 8-100. Segmental downcomer design chart. Used by permission, Belles, W. L. Pet. Processing Feb. thru May (1956).

Figure 8-123. Sieve tray capacity chart. Used by permission, Biddulph, M. W., et al. The American Institute of Chemical Engineers, Chem. Eng. Prog. V. 89 No. 12 (1993), p. 56, all rights reserved.

Figure 8-141A. Typical performance chart perforated tray with downcomer. Used by permission, Huang, Chen-Jung and Hodson, J. R., Pet. Refiner, V. 37 (1958) p. 104, Guif Pubiishing Co., aii rights reserved.

Figure 9-26. SLE Data Chart for 1-in. metal Pall rings, aqueous systems, pressure drop only. Data from 15-84 in. dia. test columns with packed heights of 2-10 ft. Reproduced with permission of the American Institute of Chemical Engineers, Kister, H. Z. and Gill, D. R., Chemical Engineering Progress, V. 87, No. 2 (1991) p. 32 all rights reserved.

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