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Tham khảo tài liệu 'arnold, k. (1999). design of gas-handling systems and facilities (2nd ed.) episode 1 part 4', kỹ thuật - công nghệ, cơ khí - chế tạo máy phục vụ nhu cầu học tập, nghiên cứu và làm việc hiệu quả | Heat Exchange rs 61 Table 3-3 Tube Materials Sweet Service Glycol MEA and Sulfinol Temperatures above -20 F A-214 ERW or A-179 seamless -50 F to -21 F A-334 Grade 1 -150 F to -5 i F. A334 Grade 3 Sour and Low Temperature 304 ss Brackish Waler 90 10 Cu-Ni 70 30 Cu-Ni Use higher nickel content the more brackish the water Sizing The required heat duty film coefficients conductivity etc. for a shell-and-tube heat exchanger can be calculated using the procedures in Chapter 2. Approximate U-values are given in Table 2-8. In the basic heat transfer equation it is necessary to use the log mean temperature difference. In Equation 2-4 it was assumed that the two fluids are flowing counter-current to each other. Depending upon the configuration of the exchanger this may not be true. That is the way in which the fluid flows through the exchanger affects LMTD. The correction factor IS a function of the number of tube passes and the number of shell passes. Figures 3-10 and 3-11 can be used to calculate a corrected LMTD from the formula. LMTD ATị - AT2 loge ATj AT2 _ 3-1 where Tj hot fluid inlet temperature F T2 hot fluid outlet temperature F T3 cold fluid inlet temperature F T4 cold fluid outlet temperature. F AT J larger temperature difference F AT2 smaller temperature difference F LMTD log mean temperature difference F F correction factor text continued on pane 64 FsLMTD CORRECTION FACTOR FsLMTD CORRECTION FACTOR F-LMTO CORRECTION FACTOR FcLMTD CORRECTION FACTOR PzTEMPERATURE EFFICIENCY P-TEMPER ATURE EFFICIENCY Figure 3-11. LMTD correction factors. From Gas Processors Suppliers Association Engineering Data Book 9th Edition.
