Process Control Systems Episode 4 ppt

... 0 125 -36 P 127r&, 158 220 361 llOTd/T, 127 196 22%,/T, 2 54 540 Process 70 Gain 4. OOsd 0.64rd/r, 4. 80 0.76 6.00 0.95 8.00 1.27 -__ 3.197d 0.517&1 4. 00 0. 64 5.37 0.86 2.867d 0 .45 rJn 4. 00 0. 64 6.79 1.08 Perform- ance, PR/100 m 4 .52sd2/rl 3.65 4. 58 0.9772/71 0.81 0.96 2. ... 0.86 Interacting three-mode _- ? 1 , D 0 0 0 0 __- 0,907d 0. 64 0. 54 ,Controller R...

Ngày tải lên: 12/08/2014, 16:21

... textbooks 10/30/2006htt p ://en.wikibooks.or g /w/index. p h p ?title =Control _ S y stems/Print _ version& p rintable= y es Some systems may have dedicated summation or multiplication devices, that automatically add or multiply the transfer functions of multiple systems together Pa g e 105 of 20 9Control S y stems/Print ... Multipliers Pa g e 1 04 of 20 9Control S y stem...

Ngày tải lên: 09/08/2014, 07:20

... pallet. SPC charting of 98 Variables and process variation 1) 4. 1 2) 4. 0 3) 4. 2 4) 4. 2 5) 4. 4 6) 4. 2 7) 4. 3 8) 4. 2 9) 4. 2 10) 4. 1 11) 4. 3 12) 4. 1 13) 3.2 14) 3.5 15) 3.0 16) 3.2 17) 3.3 18) 3.2 19) ... 3.2 24) 2.9 25) 3.3 26) 3.0 27) 3 .4 28) 3.1 29) 3.5 30) 3.1 31) 3.2 32) 3.5 33) 2 .4 34) 3.5 35) 3.3 36) 3.6 37) 3.2 38) 3 .4 39) 3.5 40 ) 3.0 41 ) 3 .4 42)...

Ngày tải lên: 11/08/2014, 20:22

... s /4- amplitude damping under proportional-plus- derivative control. Repeat for a proportional-plus-reset controller, assuming 45 ” phase lag in the controller. 54 1 Ud n erstanding Feedback Control state ... capacit’y process is 40 0/al6 or 8 times as difficult to control. Recall that the pure dead-time process was 12.5 times as difficult to control as the most difficult two-...

Ngày tải lên: 12/08/2014, 16:21

... as the input to a controller is e - Controller c not recommended. Nonlinear Control Elements I 141 Linear 0’ Time, set 60 40 0 Time, set FIG 5.22. The nonlinear two-mode controller is superior ... prime variable. Secondary Controller Primary controller FIG 6.1. Cascade control resolves the process into two parts, each within a closed loop. 156 1 Multiple-loop Systems The vecto...

Ngày tải lên: 12/08/2014, 16:21

... in Chap. 7, Multivariable Process Control. But the deepest penetration into the 1 94 1 Multiple-loop Systems component blending system be as follows: am -I- bm (7. 14) (7.15) Let the coefficients ... 1963. 3. Shinskey, F. G.: Analog Computing Control for On-line Applications, Control Eng., November, 1962. 4. Mathias, R. A., and R. I. Van Nice: Adaptive Control Systems- A...

Ngày tải lên: 12/08/2014, 16:21

... 860 ,48 5, February 8, 1961. 3. MacMullan, E. C., and F. G. Shinskey: Feedforward Analog Computer Control of a Superfractionator, Control Eng., March, 19 64. 4. Shinskey, F. G.: Analog Computing Control ... feedback control could not be used, because the intent is to maximize or minimize their value rather than t,o control at a given set point. Optimizing Programs4 Feedforward...

Ngày tải lên: 12/08/2014, 16:21

... steam in the exchanger. Thus without being directly controlled, the exit temperature of the process fluid will nonetheless be well regulated. 244 1 Applications .heat content or enthalpy, of which ... The control system for once-through boiler must be as closely knit as the process itself. Control of Energy Transfer h P a Set boint to combustion- :ontrol system Set point to feedwat...

Ngày tải lên: 12/08/2014, 16:21

... OF/% 5000 185 5 .6 -18.!)5 -4. 27 10000 170 13.0 - i 09 -3 69 15000 155 22.9 - 3 .43 -3. 14 20000 140 3i 0 - 1.75 -2.62 3.6 With the pump off, 7” varies from 1 .4 to 4. 2 min; with the pump on, ... the system. 3.7 P = 6000/,. Chapter 4 4.1 $R = -60"; R = 0.28rd; P = 40 09& The period of the loop changes less with controller phase lag in the dead-time process. 4. 2...

Ngày tải lên: 12/08/2014, 16:21