NisrUNITED STATES

DEPARTMENT OF COMMERCE

TECHNOLOGY ADMINISTRATION

NATIONAL INSTITUTE OF STANDARDS

AND TECHNOLOGY

,""} INST. OF STAND a. TECH R.I.C.

A11103 T2T0m

NISI

PUBLICATIONSi

NIST Technical Note 1356

Flow Conditioner Location Effects in

Orifice Flowmeters

Jennifer L. Scott

Charles F. SIndt

Michael A. Lewis

Chemical Engineering Division

Chemical Science and Technology Laboratory

National Institute of Standards and Technology

325 Broadway

Boulder, Colorado 80303-3328

January 1993

U.S. DEPARTMENT OF COMMERCE, Barbara Hackman Franklin, Secretary

TECHNOLOGY ADMINISTRATION, Robert M. White, Under Secretary for Technology

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY, John W. Lyons, Director
National Institute of Standards and Technology Technical Note

Natl. Inst. Stand. Techno!., Tech. Note 1356, 72 pages (January 1993)

CODEN:NTNOEF

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1992

For sale by the Superintendent of Documents, U.S. Governnrient Printing Office, Washington, DC 20402-9325
CONTENTS

Page

LIST OF FIGURES iv

LIST OF TABLES viii

1

.

INTRODUCTION 1

2 SYSTEM DESCRIPTION 4

3 . TESTS AND RESULTS 5

3 . 1 Baseline Configuration Comparison 5

3 . 2 Reducer and Elbow Disturbances 6

3 . 3 Longer Meter Lengths 7

3.4 Tap Location vs. Flow Conditioner Location 8 3.5 52 mm (2 in) Orifice Meter 9

4

.

CONCLUSIONS AND RECOMMENDATIONS 10

5

.

REFERENCES 12

FIGURES 13

TABLES 3 7
LIST OF FIGURES

Page

Figure la. In-line, 19 tube bundle flow conditioner. 13

Figure lb. In-line, 7 tube bundle flow conditioner. 13

Figure Ic. Zanker flow conditioner. 13

Figure 2. Flange pressure tap position code. 14

Figure 3. Baseline configuration, 104 mm (4 in) orifice 14

meter.

Figure 4. Discharge coefficient vs. Reynolds number for the 14

0.43 beta ratio plate with an elbow and 104D

straight pipe.

Figure 5. Discharge coefficient vs. Reynolds number for the 15

0.55 beta ratio plate with an elbow and 104D

straight pipe.

Figure 6. Discharge coefficient vs. Reynolds number for the 16

0.67 beta ratio plate with an elbow and 104D

straight pipe.

Figure 7. Discharge coefficient vs. Reynolds number for the 16

0.73 beta ratio plate with an elbow and 104D

straight pipe.

Figure 8. Test configuration, 104 mm (4 in) orifice meter, 17

reducer disturbance.

Figure 9. Test configuration, 104 mm (4 in) orifice meter, 17

elbow disturbance.

Figure 10. Discharge coefficient vs. Reynolds number for the 18

0.55 beta ratio plate with a reducer or elbow at

21D, in-line 19 tube bundle at 19D.

Figure 11. Discharge coefficient vs. Reynolds number for the 18

0.55 beta ratio plate with a reducer or elbow at

17D, in-line 19 tube bundle at 15D.

Figure 12. Discharge coefficient vs. Reynolds number for the 19

0.55 beta ratio plate with a reducer or elbow at

13D, in-line 19 tube bundle at IID,

Figure 13. Percent change in discharge coefficient vs. 19

disturbance location for the 0.55 beta ratio

plate and a reducer or elbow disturbance.

Figure 14. Discharge coefficient vs. Reynolds number for the 20

0.67 beta ratio plate with a reducer or elbow at

21D, in-line 19 tube bundle at 19D.

Figure 15. Discharge coefficient vs. Reynolds number for the 20

0.67 beta ratio plate with a reducer or elbow at

17D, in-line 19 tube bundle at 15D.

Figure 16. Discharge coefficient vs. Reynolds number for the 21

0.67 beta ratio plate with a reducer or elbow at

13D, in-line 19 tube bundle at IID.

IV
LIST OF FIGURES

Page

Figure 17. Percent change in discharge coefficient vs. 21

disturbance location for the 0.67 beta ratio

plate and a reducer or elbow disturbance.

Figure 18. Test configuration, 104 mm (4 in) orifice meter, 22

elbow disturbance.

Figure 19. Discharge coefficient vs. Reynolds number for the 2 2 0.55 beta ratio plate with an elbow at 17D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 20. Discharge coefficient vs. Reynolds number for the 23

0.55 beta ratio plate with an elbow at 22D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 21. Discharge coefficient vs. Reynolds number for the 23

0.55 beta ratio plate with an elbow at 34D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 22. Percent change in discharge coefficient vs. elbow 24

location for the 0.55 beta ratio plate with an in-line, 19 tube bundle at 15D and 2 flange tap

locations.

Figure 23. Discharge coefficient vs. Reynolds number for the 24

0.67 beta ratio plate with an elbow at 17D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 24. Discharge coefficient vs. Reynolds number for the 25

0.67 beta ratio plate with an elbow at 22D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 25. Discharge coefficient vs. Reynolds number for the 2 5 0.67 beta ratio plate with an elbow at 34D, an in-line 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 26. Percent change in discharge coefficient vs. elbow 26

location for the 0.67 beta ratio plate with an in-line, 19 tube bundle at 15D and 2 flange tap

locations.

Figure 27. Test configuration, 104 mm (4 in) orifice meter, 26

elbow at 17D.

Figure 28. Discharge coefficient vs. Reynolds number for the 27

0.55 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at 13D, and 2 flange tap

locations.

Figure 29. Discharge coefficient vs. Reynolds number for the 27

0.55 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at IID, and 2 flange tap

locations.
LIST OF FIGURES

Page

Figure 30. Percent change in discharge coefficient vs. 28

flow conditioner location for the 0.55 beta ratio

plate with an elbow at 17D and 2 flange tap

locations.

Figure 31. Discharge coefficient vs. Reynolds number for the

0.67 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at 13D, and 2 flange tap

locations.

28

Figure 32. Discharge coefficient vs. Reynolds number for the

0.67 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at IID, and 2 flange tap

locations.

29

Figure 33. Percent change in discharge coefficient vs. flow 29

conditioner location for the 0.67 beta ratio plate

with an elbow at 17D and 2 flange tap locations.

Figure 34. Discharge coefficient vs. Reynolds number for the 3 0.73 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at 15D, and 2 flange tap

locations.

Figure 35. Discharge coefficient vs. Reynolds number for the

0.73 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at 13D, and 2 flange tap

locations.

30

Figure 36. Discharge coefficient vs. Reynolds number for the

0.73 beta ratio plate with an elbow at 17D, an in-line, 19 tube bundle at IID, and 2 flange tap

locations.

31

Figure 37. Percent change in discharge coefficient vs. flow 31

conditioner location for the 0.73 beta ratio plate

with an elbow at 17D and 2 flange tap locations.

Figure 38. Discharge coefficient vs. Reynolds number for the 32

0.55 beta ratio plate with an elbow at 17D, a Zanker 16D, and 2 flange tap locations.

Figure 39. Discharge coefficient vs. Reynolds number for the 32

0.67 beta ratio plate with an elbow at 17D, a Zanker at 16D, and 2 flange tap locations.

Figure 40. Discharge coefficient vs. Reynolds number for the 33

0.73 beta ratio plate with an elbow at 17D, a Zanker at 16D, and 2 flange tap locations.

Figure 41. Baseline configuration, 52 mm (2 in) orifice 34

meter, oversize Sprenkle at 44D.

Figure 42. Discharge coefficient vs. Reynolds number for the 34

0.54 beta ratio plate, oversize Sprenkle at 44D,

and 4 flange tap locations.

Figure 43. Discharge coefficient vs. Reynolds number for the 35

0.67 beta ratio plate, oversize Sprenkle at 44D,

and 4 flange tap locations.

VI
LIST OF FIGURES

Page

Figure 44. Test configuration, 52 mm (2 in) orifice meter, 35

elbow at 17D.

Figure 45. Discharge coefficient vs. Reynolds number for 36

the 0.54 beta ratio plate, elbow at 17D, and an in-line, 7 tube bundle at 12D.

Figure 46. Discharge coefficient vs. Reynolds number for 36

the 0.67 beta ratio plate, elbow at 17D, and an in-line, 7 tube bundle at 12D.

Vll
LIST OF TABLES

Page

Table 1. Cross reference chart. 3

Table 2. Flow conditioner codes, descriptions, and measurements. 4 Table 3. Measured and calculated quantities for 0.4 3 beta ratio, 37

elbow at 104D.

Table 4. Measured and calculated quantities for 0.55 beta ratio, 37

elbow at 104D.

Table 5. Measured and calculated quantities for 0.67 beta ratio, 37

elbow at 104D.

Table 6. Measured and calculated quantities for 0.73 beta ratio, 38

elbow at 104D.

Table 7. Measured and calculated quantities for 0.55 beta ratio, 38

reducer at 21D, ITl at 19D, flange taps at position A.

Table 8. Measured and calculated quantities for 0.55 beta ratio, 38

elbow at 21D, ITl at 19D, flange taps at position A.

Table 9. Measured and calculated quantities for 0.55 beta ratio, 39

reducer at 17D, ITl at 15D, flange taps at position A.

Table 10. Measured and calculated quantities for 0.55 beta ratio, 39

elbow at 17D, ITl at 15D, flange taps at position A.

Table 11. Measured and calculated quantities for 0.55 beta ratio, 39

reducer at 13D, ITl at IID, flange taps at position A.

Table 12. Measured and calculated quantities for 0.55 beta ratio, 40

elbow at 13D, ITl at IID, flange taps at position A.

Table 13. Measured and calculated quantities for 0.67 beta ratio, 40

reducer at 21D, ITl at 19D, flange taps at position A.

Table 14. Measured and calculated quantities for 0.67 beta ratio, 40

elbow at 21D, ITl at 19D, flange taps at position A.

Table 15. Measured and calculated quantities for 0.67 beta ratio, 41

reducer at 17D, ITl at 15D, flange taps at position A.

Table 16. Measured and calculated quantities for 0.67 beta ratio, 41

elbow at 17D, ITl at 15D, flange taps at position A.

Table 17. Measured and calculated quantities for 0.67 beta ratio, 41

reducer at 13D, ITl at IID, flange taps at position A.

Table 18. Measured and calculated quantities for 0.67 beta ratio, 42

elbow at 13D, ITl at IID, flange taps at position A.

Table 19. Measured and calculated quantities for 0.55 beta ratio, 42

elbow at 17D, ITl at 15D, flange taps at position A.

Table 20. Measured and calculated quantities for 0.55 beta ratio, 42

elbow at 17D, ITl at 15D, flange taps at position C.

Table 21. Measured and calculated quantities for 0.55 beta ratio, 43

elbow at 22D, ITl at 15D, flange taps at position A.

Vlll
LI8T OF TABLES

Page

Table 22. Measured and calculated quantities for 0.55 beta ratio, 43

elbow at 22D, ITl at 15D, flange taps at position C.

Table 23. Measured and calculated quantities for 0.55 beta ratio, 43

elbow at 34D, ITl at 15D, flange taps at position A.

Table 24. Measured and calculated quantities for 0.55 beta ratio, 44

elbow at 34D, ITl at 15D, flange taps at position C.

Table 25. Measured and calculated quantities for 0.67 beta ratio, 44

elbow at 17D, ITl at 15D, flange taps at position A.

Table 26. Measured and calculated quantities for 0.67 beta ratio, 44

reducer at 17D, ITl at 15D, flange taps at position C.

Table 27. Measured and calculated quantities for 0.67 beta ratio, 45

elbow at 22D, ITl at 15D, flange taps at position A.

Table 28. Measured and calculated quantities for 0.67 beta ratio, 45

elbow at 22D, ITl at 15D, flange taps at position C.

Table 29. Measured and calculated quantities for 0.67 beta ratio, 45

elbow at 34D, ITl at 15D, flange taps at position A.

Table 30. Measured and calculated quantities for 0.67 beta ratio, 46

elbow at 34D, ITl at 15D, flange taps at position C.

Table 31. Measured and calculated quantities for 0.55 beta ratio, 46

elbow at 17D, ITl at 13D, flange taps at position A.

Table 32. Measured and calculated quantities for 0.55 beta ratio, 46

elbow at 17D, ITl at 13D, flange taps at position C.

Table 33. Measured and calculated quantities for 0.55 beta ratio, 47

elbow at 17D, ITl at IID, flange taps at position A.

Table 34. Measured and calculated quantities for 0.55 beta ratio, 47

elbow at 17D, ITl at IID, flange taps at position C.

Table 35. Measured and calculated quantities for 0.67 beta ratio, 47

elbow at 17D, ITl at 13D, flange taps at position A.

Table 36. Measured and calculated quantities for 0.67 beta ratio, 48

elbow at 17D, ITl at 13D, flange taps at position C.

Table 37. Measured and calculated quantities for 0.67 beta ratio, 48

elbow at 17D, ITl at IID, flange taps at position A.

Table 38. Measured and calculated quantities for 0.67 beta ratio, 48

elbow at 17D, ITl at IID, flange taps at position C.

Table 39. Measured and calculated quantities for 0.73 beta ratio, 49

elbow at 17D, ITl at 15D, flange taps at position A.

Table 40. Measured and calculated quantities for 0.73 beta ratio, 49

elbow at 17D, ITl at 15D, flange taps at position C.

Table 41. Measured and calculated quantities for 0.73 beta ratio, 49

elbow at 17D, ITl at 13D, flange taps at position A.

IX
LIST OF TABLES

Page

Table 42. Measured and calculated quantities for 0.73 beta ratio, 50

elbow at 17D, ITl at 13D, flange taps at position C.

Table 43. Measured and calculated quantities for 0.73 beta ratio, 50

elbow at 17D, ITl at IID, flange taps at position A.

Table 44. Measured and calculated quantities for 0.73 beta ratio, 50

elbow at 17D, ITl at IID, flange taps at position C.

Table 45. Measured and calculated quantities for 0.55 beta ratio, 51

elbow at 17D, Zanker at 16D, flange taps at position A.

Table 46. Measured and calculated quantities for 0.55 beta ratio, 51

elbow at 17D, Zanker at 16D, flange taps at position C.

Table 47. Measured and calculated quantities for 0.67 beta ratio, 51

elbow at 17D, Zanker at 16D, flange taps at position A.

Table 48. Measured and calculated quantities for 0.67 beta ratio, 52

elbow at 17D, Zanker at 16D, flange taps at position C.

Table 49. Measured and calculated quantities for 0.73 beta ratio, 52

elbow at 17D, Zanker at 16D, flange taps at position A.

Table 50. Measured and calculated quantities for 0.73 beta ratio, 52

elbow at 17D, Zanker at 16D, flange taps at position C.

Table 51. Measured and calculated quantities for 0.54 beta ratio, 52

oversize Sprenkle at 44D, flange taps at position A.

Table 52. Measured and calculated quantities for 0.54 beta ratio, 53

oversize Sprenkle at 44D, flange taps at position B.

Table 53. Measured and calculated quantities for 0.54 beta ratio, 53

oversize Sprenkle at 44D, flange taps at position C.

Table 54. Measured and calculated quantities for 0.54 beta ratio, 53

oversize Sprenkle at 44D, flange taps at position D.

Table 55. Measured and calculated quantities for 0.67 beta ratio, 54

oversize Sprenkle at 44D, flange taps at position A.

Table 56. Measured and calculated quantities for 0.67 beta ratio, 54

oversize Sprenkle at 44D, flange taps at position B.

Table 57. Measured and calculated quantities for 0.67 beta ratio, 54

oversize Sprenkle at 44D, flange taps at position C.

Table 58. Measured and calculated quantities for 0.67 beta ratio, 55

oversize Sprenkle at 44D, flange taps at position D. Table 59. Measured and calculated quantities for 0.54 beta ratio 55

plate, elbow at 17D, IT3 at 12D, flange taps at position

A.

Table 60. Measured and calculated quantities for 0.54 beta ratio 55

plate, elbow at 17D, IT3 at 12D, flange taps at position

B.

Table 61. Measured and calculated quantities for 0.54 beta ratio 56

plate, elbow at 17D, IT3 at 12D, flange taps at position

C.
Table 62

LIST OF TABLES

Page

Measured and

plate, elbow

D.

calculated quantities for 0.54 beta ratio 56

at 17D, IT3 at 12D, flange taps at position

Table 63, Measured and

plate, elbow

A.

calculated quantities for 0.67 beta ratio 56

at 17D, ITS at 12D, flange taps at position

Table 64. Measured and

plate, elbow

B.

calculated quantities for 0.67 beta ratio 57

at 17D, IT3 at 12D, flange taps at position

Table 65. Measured and

plate, elbow

C.

calculated quantities for 0.67 beta ratio 57

at 17D, IT3 at 12D, flange taps at position

Table 66. Measured and

plate, elbow

D.

calculated quantities for 0.67 beta ratio 57

at 17D, IT3 at 12D, flange taps at position

XI

FLOW CONDITIONER LOCATION EFFECTS IN ORIFICE FLOWMETERS

Jennifer L. Scott, Charles F. Sindt

Michael A. Lewis

Chemical Engineering Division

Chemical Science and Technology Laboratory

National Institute of Standards and Technology

325 Broadway

Boulder, Colorado 80303-3228

Tests sponsored by Gas Research Institute were conducted with

orifice flowmeters of two nominal sizes: 104 mm (4 in) and 52 mm (2

in) . For the 104 mm orifice meter we compared discharge

coefficients measured in two common piping configurations used by

laboratories to establish baseline flow conditions. The discharge

coefficients are similar for beta ratios of 0.43, 0.55, and 0.67,

but not for the 0.7 3 beta ratio plate. For other tests with this

orifice meter, a 90° elbow or a reducer was located upstream of the

orifice plate and flow conditioner. Two beta ratios (0.54, 0.67) were tested in the 52 mm orifice meter in baseline configuration

and with an elbow at 17D and a flow conditioner at 12D. For many

of the tests, differential pressures were measured at more than one flange tap location. Placing the flow conditioner too close to the

orifice plate in either meter yields discharge coefficients below

baseline values. The location of the flow conditioner with respect

to the orifice plate appears to influence meter performance more

significantly than the type or location of flow disturbance

upstream of it. With larger beta ratio plates, the flange tap

location affected the value of the discharge coefficients.

Key words: baseline; beta ratio; discharge coefficient; flange tap

position; flow conditioner; flow disturbance; flow measurement;

gas; orifice flowmeter; tube bundle

1. INTRODUCTION

A continuing research project at this laboratory is the measurement of

the effect of upstream conditions on orifice flowmeter performance. The

ultimate purpose of the work is to provide information that will lead to

improved standards for orifice meter installations as specified in American

Petroleum Institute (API) 14 . 3-American Gas Association (A.G.A.) Report No.

3, Part 2 [1] and International Organization for Standardization (ISO) 5167

[2]. Creating general installation standards is difficult due to the large

variety of installation configurations used in the field.

The equation found in API 14.3-A.G.A. 3, Part 1 [3] for determining

discharge coefficients in orifice flow measurement was derived from data

produced in flow that was considered fully developed or 'ideal.' A

coordinated program between this laboratory and others, sponsored by the Gas

Research Institute, has been designed to test certain piping configurations,

beta ratios (the ratio of the diameter of the hole in the orifice plate to

the inner diameter of the meter tube) , flow conditioners, and pressure tap

locations to help answer the question: How can 'non-ideal' flow be

conditioned to achieve accurate measurement? A goal of our research is to
characterize flow measurement in orifice meters for numerous installation

configurations while keeping tests to a minimum.

Research was conducted with orifice meters of two nominal sizes of

104 mm (4 in) and 52 mm (2 in) . The first phase of the 104 mm orifice meter

work was to compare the discharge coefficients measured in two common baseline configurations: (1) 46 pipe diameters (D) of straight pipe preceded

by a Sprenkle flow conditioner, or (2) 104D of straight pipe. Further tests

with the 104 mm orifice meter included placing an in-line, 19 tube flow

conditioner (ITl) directly downstream of a long-radius elbow or a 154 mm

X 104 mm (6 in X 4 in) reducer, with the elbow or reducer located varying

distances from the orifice plate.

Tests were also conducted with the 104 mm (4 in) orifice meter in which

the distance between the long-radius elbow and orifice plate was varied while

the flow conditioner remained fixed at a location 15D from the plate. Then

the 104 mm orifice meter was tested with the flow conditioner at various

locations with the elbow fixed 17D upstream of the plate. In these last two

tests, measurements were made at more than one flange tap position. Flange

taps were used in all measurements.

Testing with the 52 mm (2 in) orifice meter was begun by gathering

baseline data for two beta ratio plates (0.54, 0.67). The piping

configuration consisted of an oversize Sprenkle flow conditioner and 44D of

straight pipe upstream of the orifice plate. We also measured discharge

coefficients using the same two orifice plates with an elbow 17D from the

orifice plate and an in-line, 7-tube bundle flow conditioner (IT3) located

12D from the plate.

Table 1 shows the various piping configurations, orifice plates, and

flange tap locations tested, and identifies the appropriate tables and

figures where results for each configuration are summarized.
Table 1, Cross reference chart.

Figure

no.

Beta ratio Flow

cond.

Table

no.

Test

conf ig.

Tap location**

0.43 0.55 0.67 0.73 A B c D

104 mm

4 X 2 FIG. 3 X

5 X 3 FIG. 3 X

6 X 4 FIG. 3 X

7 X 5 FIG. 3 X

10 X ITl 6,7 8,9 X

11 X ITl 8,9 8,9 X

12 X ITl 10,11 8,9 X

13 X ITl SUMM. 8,9 X

14 X ITl 12,13 8,9 X

15 X ITl 14,15 8,9 X

16 X ITl 16,17 8,9 X

17 X ITl SUMM. 8,9 X

19 X ITl 18,19 FIG. 18 X X

20 X ITl 20,21 FIG. 18 X X

21 X ITl 22,23 FIG. 18 X X

22 X ITl SUMM. FIG. 18 X X

23 X ITl 24,25 FIG. 18 X X

24 X ITl 26,27 FIG. 18 X X

25 X ITl 28,29 FIG. 18 X X

26 X ITl SUMM. FIG. 18 X X

28 X ITl 30,31 FIG. 27 X X

29 X ITl 32,33 FIG. 27 X X

30 X ITl SUMM. FIG. 27 X X

31 X ITl 34,35 FIG. 27 X X

32 X ITl 36,37 FIG. 27 X X

33 X ITl SUMM. FIG. 27 X X

34 X ITl 38,39 FIG. 27 X X

35 X ITl 40,41 FIG. 27 X X

36 X ITl 42,43 FIG. 27 X X

37 X ITl SUMM. FIG. 27 X X

38 X ZAN 44,45 FIG. 27 X X

39 X ZAN 46,47 FIG. 27 X X

40 X ZAN 48,49 FIG. 27 X X

52 mm

42 0.54 OS 50-53 FIG. 41 X X X X

43 X OS 54-57 FIG. 41 X X X X

45 0.54 IT3 58-61 FIG. 44 X X X X

46 X IT3 62-65 FIG. 44 X X X X

* See table 2 for details,

** See figure 2.
2. SYSTEM DESCRIPTION

The gas research facility at the National Institute of Standards and

Technology in Boulder, Colorado (NIST-B) , is a closed loop thermodynamic

cycle in which the process fluid, nitrogen, is circulated between temperature

limits of 85 K and 290 K at pressures of 0.5 MPa to 4 . 1 MPa. The portion of

the loop in which the orifice meter is located operates near the upper ends

of the pressure and temperature ranges, 4 MPa and 289 K (580 psia, 60 **F) . After the nitrogen gas is passed through the orifice meter test section it is

expanded and cooled to liquid phase and weighed to determine mass flow rate.

The nominal 104 mm (4 in) orifice meter is made from schedule 40

stainless steel that has been bored to an internal diameter of 103.657 mm

(4.081 in). The orifice meters consist of three sections: approach,

upstream, and downstream. Meter tube sections are pinned to ensure

alignment. One of two approach sections was used in the research conducted

with this orifice meter, depending upon the piping configuration. One

approach section is 8D in length with an Ra of 0.76 ^m (30 ^iin) ; the other is

6D with an Ra of 2.5 um (100 /iin) • Ra is the mean absolute deviation value

of the surface finish measurement. The upstream section is IID with an internal roughness of 3.8 /xm (150 iJiin) Ra and the downstream section is 16D.

The nominal 52 mm (2 in) orifice meter is a commercially available

stainless steel flowmeter with an actual internal diameter of 52.502 mm

(2.067 in). We also used two approach sections with this meter. One of the

sections is 34D in length with an internal surface roughness of 4.3 um (170

/iin) Ra and was used for baseline work. The other approach section is 8D and

is constructed of standard schedule 40 carbon steel pipe and weld-neck

flanges. The upstream section is 9D with a roughness of 4.1 fim (160 Min) , and the downstream section is 20D with a roughness of 4.4 um (175 Min) RaFigures la, lb, and Ic show the flow conditioners used during the course

of our research. The dimensions and salient features are described in table

2.

Table 2, Flow conditioner codes, descriptions, and measurements.

Identification

Name Number

tubes/

blades

Pattern/

In-line (I)

Flanged (F)

Dimension

Length OD mm (in)

Tube ID

ITl tube

bundle

19 round-I 254

(10)

97

(3.8)

15

(0.6)

IT3 tube

bundle

7 round-I 152

(6)

48

(1.9)

13

(0.5)

ZAN Zanker 32

holes

perf. plate

with

honeycomb-F

108

(4.3)

102

(4)

OS Sprenkle three perf.

plates (I)

20.3

(8)

102

(4)

During some of the tests, we measured differential pressures at more

than one flange tap position. Figure 2 illustrates how each tap position is

referenced in this report. Location A is in the plane of the nearest upstream
elbow, along the inside of the bend. Location C is in the same plane but

along the outside of the bend. Location B is in a plane perpendicular to the

elbow and on top of the pipe, and location D is opposite of B. For each beta ratio tested, we calculated discharge coefficients at four

flow rates. A complete data set included at least four measurements at each

flow rate taken over two days to include any effects of daily variability.

For some tests we limited the number of orifice plates tested to those that

would best characterize the effects of the configuration of interest.

For every configuration and/or flow conditioner we tested, a comparative

method was used to evaluate the performance of the orifice meter. The

discharge coefficient is compared to a 'baseline' discharge coefficient at

the same pipe Reynolds number. The baseline values for the 104 mm (4 in)

meter were determined by testing each orifice plate in a specific piping

configuration consisting of an oversize Sprenkle flow conditioner and 46D of

straight pipe upstream of the orifice plate. The baseline data used in this

report also include discharge coefficients calculated using two other

upstream configurations: 56D of straight pipe and 4 6D of straight pipe with

no Sprenkle flow conditioner. The results were similar for these three

configurations; therefore, data from all configurations were combined [4].

These data sets were fitted to a linear curve for each beta ratio, and these curves are indicated on all figures.

Baseline data for the 52 mm (2 in) meter at selected beta ratios are included in this report. The curves representing these data are shown on the

figures as will the Reader-Harris/Gallagher (RG) equation for determination

of discharge coefficient found in API 14.3-A.G.A. 3, Part 1 [3].

The percent shift in orifice meter discharge coefficients resulting from

specific upstream piping configurations and flow conditioner locations at

selected Reynolds numbers was computed as follows:

(c,-c;)xioo (1)

where Ct is the discharge coefficient that was experimentally determined with

the baseline configurations and C^ is the discharge coefficient calculated for

the various test configurations.

3. TESTS AND RESULTS

3.1 Baseline Configuration Comparison

Baseline data from U.S. and European facilities were used to derive the

recent equation revision in API 14.3-A.G.A. 3, Part 1 [3]. U.S. data were taken with a defined piping configuration of a Sprenkle flow conditioner

followed by 46D of straight pipe upstream of the orifice plate. In many

cases, the Sprenkle flow conditioner was larger that the meter size. No

European baseline data were collected with a Sprenkle flow conditioner;

however, the facilities had much longer metering runs than those used in the

United States [5]

We installed 104 D of straight pipe upstream of the orifice plate of the

104 mm (4 in) orifice meter and measured differential pressures for beta

ratios of 0.43, 0.55, 0.67, and 0.73. The goal of this task was to compare

these data with those used for our baseline [4]. Figure 3 illustrates the
piping configuration. The flange pressure tap was located in the plane of

the elbow along the inside of the bend, location A. Figures 4 through 7 display the data for each beta ratio. Also shown in each figure is the

previously determined baseline for each beta ratio [4]. The data are listed

in tables 3 through 6.

Figures 4, 5, and 6 indicate that for beta ratios of 0.43, 0.55, and

0.67, there was little difference between the discharge coefficients and the

baseline curves. The differences that can be seen for these beta ratios are within the reproducibility of our gas flow system. We tested the impact that

these data would have on the baseline curve by combining them with previous

baseline data and creating new baseline curves. When the curves from the

combined data sets were compared to the original baseline curves, the

difference between the curves was less than 0.1 percent over the entire

Reynolds number range for these three beta ratios.

Figure 7 shows an obvious bias in discharge coefficient between these

data and the baseline for the 0.7 3 beta ratio plate. The discharge

coefficients were higher than baseline values over the Reynolds number range.

When these data were added to those making up the baseline, the new curve was from 0.15 percent to 0.2 percent higher than the baseline curve. We think

that this bias warrants further investigation.

3 . 2 Reducer and Elbow Disturbances

Previous work with the 104 mm (4 in) orifice meter at this laboratory

indicated that with a flow conditioner placed at the outlet of a tee

disturbance, the discharge coefficients would be near baseline values [7].

For that work the flange taps were located in the plane of the tee and along

the inside of the bend. The purpose of this test phase was to determine

whether this was a good flow conditioner location for other type of

disturbances that are referred to in the standard [1].

We ran tests with a single, long-radius elbow or a 154 mm x 105 mm (6 in

X 4 in) reducer as the upstream disturbance (fig. 8, 9). The disturbance was

21, 17, or 13 pipe diameters upstream of the orifice plate as indicated by

the ' z' dimension in the figures, and an in-line, 19 tube bundle flow

conditioner (ITl) was placed directly downstream of the disturbance. The

flange taps were located in the plane and along the inside of the last bend,

location A (fig. 2). Orifice plates with beta ratios of 0.55 and 0.67 were tested in these configurations.

Figures 10 through 12 reflect the discharge coefficients when the 0.55

beta ratio plate was used. Each figure displays data from both the reducer

and the elbow disturbance. These data are found in tables 7 through 12.

Figure 13 shows the relationship between experimental discharge coefficients

and baseline values for both disturbances.

The results for the elbow disturbance are very similar to those reported

in NIST Technical Note 1330 [6] which described the effects of flow

conditioner location in undisturbed flow conditions. This work showed that,

for our test facility, placing the flow conditioner more than 17D from the

orifice plate increased the discharge coefficients above baseline values.

Results presented here indicate that the discharge coefficients are affected more by flow conditioner location than the type and location of the

disturbance upstream of it. The range of tube bundle locations for which the

discharge coefficients are near baseline values is between 15D and 19D
upstream of the orifice plate for the 0.55 beta ratio plate.

With the reducer disturbance and the 0.55 beta ratio plate the discharge

coefficients approached baseline values as the flow conditioner was moved

away from the orifice plate; however, the discharge coefficients were always

below baseline values. When the tube bundle was 15D upstream of the orifice

plate, the shift in the discharge coefficient was -0.25 percent from baseline

values. At 19 diameters, the shift from baseline values was -0.15 percent.

Results were similar with the 0.67 beta ratio plate. These data are shown in figures 14, 15, and 16 and are listed in tables 13 through 18. Once

again we have plotted the results from both disturbances on each graph. The

differences between experimental and baseline discharge coefficients are shown in figure 17.

Figure 17 indicates that, with either of these disturbances, placing the

flow conditioner around 15D upstream of the orifice plate will result in

discharge coefficients near baseline values. The differences between

experimental data and baseline values are within ±0.1 percent at this

location. As previously reported, placing the flow conditioner too close to

the orifice plate causes a negative shift in discharge coefficient. If it is

too far from the plate, a positive shift occurs, unless it can be moved so far that the piping approaches baseline configuration.

If the disturbance is an elbow, a good location for the flow conditioner

with the 0.55 and 0.67 beta ratio plates is apparently around 15D upstream of

the orifice plate. This is consistent with previous results with a tee as a disturbance [7]. However, work at this laboratory and others has shown that

the position of the flange pressure taps with respect to the elbow is

important when larger beta ratio plates are used [7-10]

3 . 3 Longer Meter Lengths

Much of the recent work at this facility has been directed toward

finding a good location for a flow conditioner in short metering stations

[4,7]. We have considered configurations with 17 to 19 pipe diameters

between the last disturbance and the orifice plate to simulate required

piping distances specified in API 14.3-A.G.A. 3, Part 2 [1]. The standard

requires a minimum distance between a partially closed valve and the 0.75

beta ratio orifice plate of 17D when a flow conditioner is used. There are metering stations that have more than the minimum distance between the

disturbance and the plate. We examined this point by testing a tube bundle

flow conditioner located 15D upstream of the orifice plate while we altered

the overall meter length. The test plan was expanded to include simultaneous

measurements at two flange tap locations: position A, inside the bend of the

elbow, and position C, outside the bend of the elbow. The configurations

tested are illustrated in figure 18.

The test with the elbow at 17D and the tube bundle directly downstream

was repeated, but measurements were taken at two tap locations. The results

with the 0.55 beta ratio plate are shown in figure 19. These data can be

found in tables 19 and 20. At a pipe Reynolds number of 1.25 x 10^ the

difference between the discharge coefficients at the two tap locations was

less than 0.1 percent (the repeatability of our transducers), and the values

at each tap location were below baseline values as shown in figure 22.

Figures 20 and 21 display the discharge coefficient data for the 0.55

beta ratio plate with the elbow at distances of 22D and 34D. These data can
be found in tables 21 through 24. There is no effect of tap location, but as the elbow was moved farther from the orifice plate, the values of the

discharge coefficients moved away from baseline values (figure 22)

.

The results for these configurations and the 0.67 beta ratio plate are shown in figures 23, 24, and 25 and are listed in tables 25 through 30. The

difference in discharge coefficient resulting from tap location was about 0.1

percent when the elbow was 17 or 22 diameters upstream of the orifice plate,

but there was no difference in the data at the two tap locations when the

elbow was at 34D. In addition, figure 26 shows that all discharge

coefficients were near baseline values regardless of the piping

configuration.

3.4 Tap Location vs. Flow Conditioner Location

The magnitude of the effect of tap location increases with beta ratio.

Research completed at this facility with a tee disturbance indicated that as much as a 0.5 percent difference in measurement can occur between tap

locations when the 0.73 beta ratio plate is used [7]. For these tests the

in-line tube bundle flow conditioner was directly downstream of the tee.

Researchers at another laboratory found similar results [8]. They tested the

0.75 beta ratio plate with an elbow disturbance 17D upstream of the orifice

plate and a sliding, 19 tube bundle flow conditioner, which could be placed

anywhere between the plate and the disturbance. Their results indicate that

if the flow conditioner is moved away from the elbow, the tap location effect

diminishes. However, as the flow conditioner approaches the orifice plate,

the discharge coefficients move away from baseline values. We attempted to

duplicate these results in our laboratory. In our tests we placed the flow

conditioner at two locations between the elbow and orifice plate and included

three beta ratios in the test plan.

With an elbow 17D from the orifice plate, we tested the in-line tube

bundle flow conditioner at two locations: IID and 13D upstream of the orifice

plate. We tested the 0.55, 0.67, and 0.73 beta ratio plates in the

configuration shown in figure 27. Tests results for beta ratios of 0.55 and

0.67 with the flow conditioner at the elbow outlet are described above. The

0.73 beta ratio measurements are included here.

Discharge coefficients for the 0.55 beta ratio plate are shown in

figures 28 and 29, and are listed in tables 31 through 34. There is no tap

location effect with this beta ratio. The summary plot shown in figure 30

indicates that for this beta ratio, the best location for the flow

conditioner in this piping configuration is at the outlet of the elbow.

For the 0.67 beta ratio plate, the same conclusions can be drawn.

Figures 31 and 32 show a small tap location effect when the flow conditioner

was at both the IID and 13D positions. These data are listed in tables 35

through 38. This effect was as large as the effect seen when the flow

conditioner was at the elbow outlet. Figure 33 shows that the discharge

coefficients were nearest baseline values when the flow conditioner was at

the elbow outlet.

The results for the 0.73 beta ratio plate are inconclusive because of

the measurable tap location effect in all configurations. Figures 34 through

36 show the discharge coefficients at two tap locations with the flow

conditioner in three positions downstream of the elbow. The data can be

found in tables 39 through 44.
The difference in discharge coefficients between the two tap locations

did not diminish as the flow conditioner was moved away from the elbow. At

a pipe Reynolds number of 1.25 x 10^ the difference in discharge coefficients

between tap locations was 0.18 percent when the flow conditioner was located

at the outlet flange of the elbow, and the difference was 0.3 percent when

the flow conditioner was 13D upstream of the orifice plate. Figure 37

indicates that the flow conditioner could be placed between 13D and 15D

upstream of the orifice plate, but depending upon the location of the

pressure tap, a possible error of 0.3 percent could result.

We also conducted tests with the Zanker flow conditioner located at the

elbow outlet for beta ratios of 0.55, 0.67, and 0.73. Previous tests have

shown that placing this flow conditioner at lOD with a tee located at 19D

resulted in discharge coefficients within 0.15 percent of baseline values for

each orifice plate used [7]. However, those tests included only one tap

location: position A. Figures 38, 39, and 40 show the data with the Zanker

conditioner at 16D. The figures 30, 33, and 37 compare the performance of

the Zanker conditioner to the tube bundle flow conditioner. The Zanker

conditioner did not perform as well as the tube bundle in this location, and

a pressure tap location effect was evident. These data can be found in

tables 45 through 50. After analyzing one data set taken with the Zanker

flow conditioner, we found that this flow conditioner did not perform as well

as the tube bundle at this location, and we discontinued testing with it.

3.5 52 mm (2 in) Orifice Meter

Many gas metering stations are equipped with 52 mm (2 in) orifice

meters, but there is little available gas research data in this meter size.

Extensive research with water in 52 mm (2 in) orifice meters has been

conducted at the National Institute of Standards and Technology in

Gaithersburg [11,12]. A recent modification to our laboratory to conduct gas

research in this meter size will complement the NIST-Gaithersburg work.

The lower flow rate limits for our mass-based weighing system is 0.5

kg/s (1.1 Ib/s) . In order to test the 52 mm (2 in) orifice meter at low flow

rates, we installed two turbine meters, in series, upstream of the orifice

meter. Using a system of control valves, we bypassed part of the gas through

the turbine-orifice meter arrangement while maintaining the overall flow

above 0.5 kg/s. One of the turbine meters was used as the primary

measurement device. We used the other turbine meter as a constant reference

to the primary turbine meter by monitoring the output ratio between the two

meters.

The turbine meters were calibrated over the range of our mass system.

The turbine meters and associated piping were then sent to the Colorado

Engineering Experimental Station Incorporated (CEESI) in Nunn, Colorado, to

be calibrated at lower flow rates. This calibration was done using air at

pressures and temperatures similar to those at which our facility operates

(3.83 MPa, 290 K) . These calibration data were combined to arrive at a calibration curve for the turbine meters which covers the entire flow range.

Testing began with two beta ratios: 0.54 and 0.67. The piping

configuration used for baseline measurements is shown in figure 41. It

consisted of a 104 mm (4 in) Sprenkle flow conditioner and 44D of straight

pipe upstream of the orifice meter. We measured differential pressure at

four flange tap locations, simultaneously. For each beta ratio tested,
approximately half of the data used the mass system and the other half used

the turbines to calculate discharge coefficients. Baseline data, as well as the API 14.3-A.G.A. 3 (RG) [3] equation curve are shown in figures 42 and 43.

The data are listed in tables 51 through 58.

Figure 42 indicates that for the 0.54 beta ratio plate, the discharge

coefficients at all tap locations were near the values predicted by the API

14.3-A.G.A. 3 equation [3]. Baseline data for the 0.67 beta ratio plate

shown in figure 43 indicate good agreement between the data and the equation

at Reynolds numbers below 1.4 x 10^. Work to investigate the shift in

discharge coefficients above RG equation values at higher Reynolds numbers is

scheduled. Future work will also cover a wider range of Reynolds numbers.

The approach section was replaced to create a configuration with 17D

between the last elbow and the orifice plate, as shown in figure 44. An inline, 7 tube bundle flow conditioner was placed at 12D and the 0.54 and 0.67

orifice plates were tested.

The data for the 0.54 beta ratio plate are shown in figure 45 and are listed in tables 59 through 62. Data are about 0.2 percent lower than the

values measured in the baseline configuration. There is no difference

between values at the various tap locations.

The results for the 0.67 beta ratio plate are similar but exhibit a slight tap location effect. These results are shown in figure 46, and the

data are in tables 63 through 66. The largest difference in discharge

coefficients occurs between the B and D tap locations but is less than 0.2

percent at all Reynolds numbers. The values for the A and C location fall

between these values. In general, the discharge coefficients are about 0.2

percent below values measured in the baseline configuration but are close to

equation values over the flow range.

4. CONCLUSIONS AND RECOMMENDATIONS

Flow measurement laboratories throughout the world use various piping

configurations to establish fully developed turbulent flow. Discharge

coefficient data measured in these configurations were compiled and used to

establish the Reader-Harris/Gallagher equation for calculation of discharge

coefficients. In our system, we found no difference between discharge

coefficients measured with an oversize Sprenkle flow conditioner and 46D of

straight pipe or 104D of straight pipe upstream of the orifice plate for

lower beta ratio values. The 0.73 beta ratio plate was consistently the most

sensitive to any changes in upstream conditions in our system.

Results of the tests with the elbow and the reducer disturbances show

that the flow conditioner location has a greater impact on the discharge

coefficients than the location of the upstream disturbance. For beta ratios

of 0.55 and 0.67, a good location for the flow conditioner is around 15D from

the orifice plate when the disturbance is located directly upstream of the

flow conditioner; however, the effect of the flange tap location was not

measured. Tests with the flow conditioner at 15D and the elbow at 17D, 220, or 3 4D also indicate that 15D is a good location. There was a small tap

location effect with the 0.67 beta ratio plate, only.

With an elbow at 17D, moving the flow conditioner closer to the orifice

plate caused a negative shift in discharge coefficient which was more significant than any change in effect of the flange tap location.

10
API 14. 3 -A. G. A. Report No. 3 [3] states that measurement uncertainties

can increase with beta ratios larger than 0.6. In our system, discharge

coefficients with the flow conditioner at 15D and the 0.67 beta ratio plate were within 0.15 percent of baseline values for each of the tap location and

piping configuration tested. Although work with the 0.73 beta ratio plate

was limited, current and previous results show tap location effects and other

inconsistencies for this beta ratio.

More work is needed with an elbow or reducer at 17D. Tests will include

an examination of the effect of using no flow conditioner or using a 7 tube

bundle flow conditioner. These tests should include differential pressure

measurements at more than one flange tap location. Other disturbances such

as a header should be tested to see if results are similar to those using an elbow disturbance.

The limited work with the 52 mm (2 in) orifice meter indicates that for

the 0.54 beta ratio plate, values measured in the baseline configuration are near RG equation values. For the 0.67 beta ratio, there is a shift in

discharge coefficient at a Reynolds number of about 1.4 xlO^ which warrants

further investigation.

With the flow conditioner located 12D upstream of the orifice plate and

an elbow at 17D, the discharge coefficients at a Reynolds number of 1.2 5 x 10^

for the 0.54 and 0.67 beta ratios were from 0.2 to 0.25 percent below

baseline values, an indication that the flow conditioner is too close to the

orifice plate.

Additional research is needed with the 52 mm (2 in) orifice meter. Work

with an expanded range of beta ratios and a 19 tube bundle flow conditioner

would help determine whether results with the 104 mm (4 in) orifice meter can

be translated to other sizes. Research with high pressure gas is needed to

complement the work completed with water and oil in this orifice meter size.

ACKNOWLEDGEMENTS

The work described in this report was funded by the Gas Research

Institute, Chicago, Illinois, under GRI Contract No. 5088-271-1680. This

report is also cited as GRI Report Number GRI-92/0363. The technical support

and guidance of John Gregor, project manager, is gratefully acknowledged.

The authors also wish to acknowledge the support and input of the American

Gas Association's Gas Metering Research Council (Task Group Number 16 of the

Transmission Measurement Committee) as well as the assistance of Mary Yannutz

and Nick Sanchez in preparing this report.

11
5 . REFERENCES

[I] Orifice metering of natural gas and other related hydrocarbon fluids,

Part 2 - Specification and installation requirements, A.G.A. Report No.

3-API 14.3, Third Edition, American Gas Association, Arlington,

Virginia; February 1991.

[2] Measurement of fluid flow by means of orifice plates, nozzles and

venturi tubes inserted in circular cross-section conduits running full.

International Standard ISO 5167, First Edition, International

Organization for Standardization; (1980)

.

[3] Orifice metering of natural gas and other related hydrocarbon fluids.

Part 1 - General equations and uncertainty guidelines, A.G.A. Report No.

3-API 14.3, Third Edition, American Gas Association, Arlington,

Virginia; October 1990.

[4] Sindt, C.F., Lewis, M.A. , and Brennan, J.A. , Orifice meter performance

downstream of a tube bundle flow conditioner, elbows, and a tee. Natl.

Inst. Stand. Tech. Tech. Note 1344; 1990.

[5] Gallagher, J.E., The A.G.A. Report No. 3 orifice plate discharge

coefficient equation, Second International Symposium on Fluid Flow

Measurement, Calgary, Alberta, Canada; June 6-8, 1990.

[6] McFaddin, S.E., Sindt, C.F., and Brennan, J.A. , Optimum location of flow

conditioners in a 4-inch orifice meter, Natl. Inst. Stand. Tech. Tech.

Note 1330; 1989.

[7] Scott, J.L., Sindt, C.F., Lewis, M.A. , and Brennan, J.A. , The effects

of flow conditioners and tap location on orifice flowmeter performance,

Natl. Inst. Stand. Tech. Tech. Note 1352; 1991.

[8] McKee, R.J., and Sparks, C.R., GRI Metering Research Facility update,

26th Annual Gulf Coast Measurement Short Course, Houston, Texas;

September 1991.

[9] Park, J.T., and Morrow, T.B., Orifice meter installation effects:

Sliding vane test with a 17D meter tube and a 19-tube bundle

straightening vane downstream of a tee. GRI Technical Memorandum MRF-UE05, SWRI, San Antonio, Texas; April 1992.

[10] Morrow, T.B., and Park, J.T., Orifice meter installation effects:

Sliding vane test with a 17D meter tube and a 7 tube bundle

straightening vane downstream of a tee. GRI Technical Memorandum MRF-UE07, SWRI, San Antonio, Texas; April 1992.

[II] Mattingly, G.E., and Yeh, T.T. , Summary report of NIST's industrygovernment consortium research program on flowmeter installation effects

with emphasis on research period May 1989-Feb. 1990: Tube bundle

effects. Natl. Inst. Stand. Tech. NISTIR 4751; 1991.

[12] Mattingly, G.E., and Yeh, T.T., Summary report of NIST's industrygovernment consortium research program on flowmeter installation effects

with emphasis on research period Feb. -Dec. 1990: Tee, used as an elbow

configuration. Natl. Inst. Stand. Tech. NISTIR 4753; 1992.

12
Figure la. In-line, 19 tube bundle flow conditioner.

Figure lb. In-line, 7 tube bundle flow conditioner.

Figure Ic. Zanker flow conditioner.

13
Orifice Plate

Figure 2. Flange pressure tap position code.

Figure 3. Baseline configuration, 104 nnm (4 in) orifice meter.

14
CD

OO

0)

o

m

0.62

0.61

0.60

0.59

0,2

^ 0.43

\2} Flange tap location A

Baseline

0.6 1.0

D = 104 mm

1.8 Pipe Reynolds Number/10

Fu ure 4. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio plate with an elbow and 104D straight pipe.

0.62

• I—

t

o

a;o

u

cu

o

m• I—

I

Q

0.61

0.60

0.59

0.2

^ 0.55

\J^ Flange tap location A

Baseline

J \ s_

o

o

D = 104 mm

0.6 1.0 1.4

Fig

Pipe Reynolds Number/10

ure 5. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow and 104D straight pipe.

15
I—

H

O

o

OJ

COowQ

0.62

0.61

0.60

0.59

(3 = 0.67

(^ Flange tap location A

Baseline D = 104 mm

0.6 1.0 1.4 1.8

Fig

Pipe Reynolds Number/10

ure 6. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow and 104D straight pipe.

• I—

I

o

OJou

CD

OjO

?-( COo

C/3 Q

0.62

0.61

0.60

0.59

/S 0.73

QJ) Flange tap location A

Baseline D = 104 mm

0.6 1.4 1.8 Pipe Reynolds Number/lO

Figure 7. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio plate with an elbow and 104D straight pipe.

16
Z = 21D, 17D,or13D

F'igure 8. Test configuration, 104 mm (4 in) orifice meter, reducer

disturbance.

Z = 21D, 17D, or13D

Figure 9. Test configuration, 104 mm (4 in) orifice meter, elbow

disturbance.

17
a

0)oo

q;

.-H

o

Q

0.52

0.61

0.60

0.59

(3 = 0.55

^

'\7 Elbow, flange lap localion A

Cj) Reducer, flange tap location A Baseline D = 104 mm

0.2 5 1.0 1 46

Pipe Reynolds Number/10

Figure 10, Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with a reducer or elbow at 21D, in-line, 19 tube

bundle at 19D.

OU

o;

o

Q

0.52

0.61

0.50

0.59

(3 = 0.55

V^

'yy Elbow, flange tap location A

C_) Reducer, flange tap localion A Baseline

_L

D = 104 mm

0.2 0.5 1.0 1.46

Pipe Reynolds Number/10

Figure 11. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with a reducer or elbow at 17D, in-line, 19 tube

bundle at 15D.

18
0.62

•I—

I

O

O

iafl

o

Q

0.61

0.60 -

0.59

0,2

j8 = 0.55

""~^-

\7 Elbow, flange tap location A

Cj) Reducer, flange tap location A

Baseline

0,6 1.0

D = 104 mm

1.4 Pipe Reynolds Number/10

Figure 12. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with a reducer or elbow at 13D, in-line, 19 tube

bundle at IID.

1.0

• 1—1

(U

-l-J

O

Sh

(D

0.0

-0.5

1.0

- (S = 0.55

- V

<:—

7

V

o

o

^Elbow disturbance D = 104 mm

(^Reducer disturbance Pipe Reynolds No. = 1.25 x 10'

1 1

Fig

5 10 15 20 25

Flow Conditioner Location, Pipe Diameters

ure 13. Percent change in discharge coefficient vs. disturbance

location for the 0.55 beta ratio plate and a reducer or elbow disturbance.

19
0.62

(DO

OU

0)

O

Q

0.61

0.60

0.59

0.6

/S = 0.67

S/ Elbow, flange tap location A

(_J) Reducer, flange tap location A

Baseline D = 104 mm

1.0 1 ,4 Pipe Reynolds Number/10

Figure 14. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with a reducer or elbow at 21D, in-line, 19 tube

bundle at 19D.

0.62

O

oU

cu

a

0.61 -

0.60

0.59

13 = 0.67

0.6

Figure 15.

\7 Elbow, flange tap location A (^ Reducer, flange tap location A Baseline

1,0

D = 104 mm

14 1.8 Pipe Reynolds Number/10

Discharge coefficient vs. Reynolds number for the 0,67 beta

ratio plate with a reducer or elbow at 17D, in-line, 19 tube

bundle at 15D,

20
0.62

O

O

u

COoQ

0.61

0.60

0.59

0.6

^ = 0.67

"\7 Elbow, flange tap location A

Cj) Reducer, flange tap location A

Baseline

1.0

D = 104 mm

1.4 1.8 6

Pipe Reynolds Number/10

Figure 16. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with a reducer or elbow at 13D, in-line, 19 tube

bundle at IID.

U

0)

O

QJO

CD a.

1.0

0.5

-0,5

1.0

v-O

^Elbow disturbance (~)Reducer disturbance

iS = 0.67

O

V

v-

..O.

D = 104 mm

Pipe Reynolds No = 1.25 x 10" J \

Fi

5 10 15 20 25

Flow Conditioner Location, Pipe Diameters

gure 17. Percent change in discharge coefficient vs. disturbance

location for the 0.67 beta ratio plate and a reducer or elbow disturbance.

21
Z = 17D, 22D, or34D

a

OU

Q)

iafl

CO s:o

m

Q

Figure 18. Test configuration, 104 mm (4 in) orifice meter, elbow

disturbance.

0.62

0.61

0.60

0.59

0.2

^ = 0.55

^-frj) Flange tap location A ^^ Flange tap location C

Baseline D = 104 mm

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 19. Discharge coefficient vs. Reynolds number for the 55 beta

ratio plate with an elbow at 17D, an m-lme, 19 tube bundle

at 15D. and 2 flange tap locations.

22
0.62

CD

•rHO

a;o

o

%-i

o

0.61 -

0.60

0.59

-

/? = 0,55 —- ^f

—

i — s_

i

~~^

p

(^ Flange tap loce ^ Flange tap loce Baseline

1

ilion itionA

C

1 1 1

D = 104 mm

1 0.2 6 1.0 1.4 Pipe Reynolds Number/10

Figure 20. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow at 22D, an in-line, 19 tube bundle

at 15D, and 2 flange tap locations.

0.62

O

o

o

0.6'

0.60

0.59

0.2

Figure 21.

^ 0.55

~~~~^'

Qj) Flange tap location A ^ Flange tap location C Baseline

m

D = 104 mm

_L 0.6 1.0 1.4 Pipe Reynolds Number/lO

Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow at 34D, an in-line, 19 tube bundle

at 15D, and 2 flange tap locations.

23
u

a• (—I

CD

cuo

ex

1.0

0.5 -

0.0

-0.5

1.0

iS 0.55

V

(^Flange tap location A ^^Flange tap location C D = 104 mm

Pipe Reynolds No = 1.25 x 10'

I

\ I 15 20 25 30 35 40

Upstream Elbow Location, Pipe Diameters

Figure 22. Percent change in discharge coefficient vs. elbow location

for the 0.55 beta ratio plate with an in— line, 19 tube bundle

at 15D and 2 flange tap locations.

0.62

CDO

O

<v

COo

CA) Q

0.61

0.60

0.59

(S = 0.67

(J) Flange tap location A y^ Flange tap location C

Baseline ^ D = 104 mm

0.6 1.0 1.4 Pipe Reynolds Number/10

Figure 23. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 17D, an m— line, 19 tube bundle

at 15D, and 2 flange tap locations.

24
0.62

OU

q;

COo

mQ

0.61

0.60

0.59

0.5

Figure 24.

)8 = 0.67

(^ Flange tap location A ^^ Flange tap location C

Baseline

1.0

D = 104 mm

1.4 6

Pipe Reynolds Number/10

Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 22D, an in-line, 19 tube bundle

at 15D, and 2 flange tap locations.

0.62

CDO

ou

CD

COo

mQ

0.61

0.60

0.59

0.6

/? 0.67

5

\~^ Flange tap location A ^^ Flange tap location C

Baseline ±

^®

D = 104 mm

1.0 1.4 1.8 6

Pipe Reynolds Number/lO

Figure 25. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 34D, an in-line, 19 tube bundle

at 15D, and 2 flange tap locations.

25
Q

o

o

.0

0.5

0.0

-0.5

..0-.

(^Flange tap location A ^^Flange tap location C

/? = 0.67

M.

D = 104 mm

Pipe Reynolds No = 1 25 x 10'

J \ \ \

Fig

-1.0 5 10 15 20 25 30 35 40

Upstreani Elbow Location, Pipe Diameters

ure 26. Percent change in discharge coefficient vs. elbow location

for the 0.67 beta ratio plate with an in-line, 19 tube bundle

at 15D and 2 flange tap locations.

Orifice Plate

Y = 11D, 13D, or15D

Long Radius

Elbow

Figure 27. Test configuration, 104 mm (4in) orifice meter, elbow at 17D.

26
OJoO

COo

Q

0.62

0.61

0.60

0.59

0.2

iS 0.55

(^ Flange tap location A ^^ Flange tap location C

Baseline

m

D = 104 mm

0.6 1.0 1 46

Fig

Pipe Reynolds Number/10

ure 28. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow at 17D, an in-line, 19 tube bundle

at 13D, and 2 flange tap locations.

0.62

•I—

O

0)oU

O

0.61

0.60

0.59

0.2

13 = 0.55

Fij

rj) Flange tap location A ^^ Flange tap location C Baseline D = 104 mm

0.6 1.0 14

Pipe Reynolds Number/10

;ure 29. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow at 17D, an in — line, 19 tube bundle

at IID, and 2 flange tap locations.

27
I—

I

CD

0)o

cu

1.0

0.5

0.0

-0.5 -

1.0

(3 = 0.55

(^ Flange tap location A, ITl \7 Flange tap location C, ITl ^ Flange tap location A, Zanker ^ Flange tap location C, Zanker

I

V

D = 104 mm

Pipe Reynolds No. = 1.25 x 10'

5 10 15 20

Flow Conditioner Location, Pipe Diameters

Figure 30. Percent change in discharge coefficient vs. flow conditioner

location for the 0.55 beta ratio plate with an elbow at 17D

and two flange tap locations.

0.62

o

CDO

o

CD

o

C/Q

.—

I

Q

^ 0.67

0.61

0.60

(_J) Flange tap location A ^ Flange tap location C

Baseline D = 104 mm

0.59

0.6

Figure 31.

1.0 1.8 6

Pipe Reynolds Number/10

Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 17D, an in-line, 19 tube bundle

at 13D, and 2 flange tap locations.

28
0.62

CD r—

(

o

(DOO

o

J—

I

Q.

0.61

0.60 -

0.59

(3 = 0.67

(_) Flange lap location A ^ Flange tap location C

Baseline D = 104 mm

1 ,4 6

0.6 1.0 Pipe Reynolds Number/10

Figure 32. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 17D, an in-line, 19 tube bundle

at IID, and 2 flange tap locations.

U

G• r-H

CD

U

O

cu Ph

0.5

0.0

'0.5

-1.0

(3 = 0.67

o

rj) Flange tap location A, ITl \—

7

\y Flange tap location C, ITl ^ Flange tap location A, Zanker ^ Flange tap location C, Zanker

G

V

D = 104 mm

Pipe Reynolds No. = 1.25 x 10'

\ 10 15 20

Flow Conditioner Location, Pipe Diameters

Figure 33. Percent change in discharge coefficient vs. flow conditioner

location for the 0.67 beta ratio plate with an elbow at 17D

and two flange tap locations.

29
• I—

I

O

O

CJ

CD

o

0.62

0.61

0.60

0.59

0.6

/S

rj) Flange tap location A y^ Flange tap location C

Baseline

_j \

0.73

O

D = 104 mm

1.0 1 .4 1.8

Fig

Pipe Reynolds Number/10

ure 34. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio plate with an elbow at 17D, an in-line, 19 tube bundle

at 15D, and 2 flange tap locations.

0.62

<DO

CDOO

CD

o

C/Q r—

I

Q

0.61

0.60

0.59

0.6

iS 0.73

(/^ Flange tap location A ^ Flange tap location C Baseline

f>

D = 104 mm

1.0 1.4

Fig

Pipe Reynolds Number/lO

ure 35. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio plate with an elbow at 17D, an in-hne, 19 tube bundle

at 13D. and 2 flange tap locations.

30
0.62

CDo

OU

QJ

cdo

Q

0.61 -

0.60

0.59

0.6

(8 = 0.73

(_) Flange lap location A ^ Flange lap location C

Baseline _j ^

= 104 mm

10 1.4

Fig

Pipe Reynolds Number/10

ure 36. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio plate with an elbow at 17D, and in-line, 19 tube bundle

at IID, and 2 flange tap locations.

• i-H

OX)

q;o

1.0

0.5

0.0

-0,5

-1.0

- /?

--= 0.73

- O

_ /r~^ V '^ u

o V

•

(y) Flange tap location A, \7 Flange tap location C,

ITl

ITl ^ D = 104 mm

^ Flange tap location A, Zanker ^ Flange tap location C, Zanker

1

Pipe Rey aolds

1

No. = 1.25 X 10"

15 20

Flow Conditioner Location, Pipe Diameters

Figure 37. Percent change in discharge coefficient vs. flow conditioner

location for the 0.73 beta ratio plate with an elbow at 17D

and two flange tap locations.

31
0.62

O

u

COo

Q

0.61 -

0.60

0.59

^ 0.55

^^..

W

(_) Flange lap location A ^ Flange lap localion C Baseline

_L

»

D = 104 mm

Fig

0.2 0.6 1.0 1,4 1.8

, 6

Pipe Reynolds Number/10

ure 38. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio plate with an elbow at 17D, a Zanker at 16D, and 2

flange tap locations.

0.62

CDO

o

o

CO x:o

(/} Q

0.61

0.60

0.59

^ 0.67

5 3^

(_J) Flange lap location A ^T Flange tap location C Baseline _i \

D = 104 mm

Fig

0.6 1.0 1.4 1.8

. 6

Pipe Reynolds Number/10

ure 39. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate with an elbow at 17D, a Zanker at 16D, and 2

flange tap locations.

32
0.62

a;o

cuoU

(D

oQ

0.61

0.60

0.59

0.6

^ 0.73

rj) Flange tap location A ^^ Flange tap location C Baseline D = 104 mm

1.0 1 .4 Pipe Reynolds Number/10

Figure 40. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio plate with an elbow at 17D, a Zanker at 16D, and 2

flange tap locations.

33
Figure ^11. Baseline configuration, 52 mm (2 in) orifice meter, oversize

Sprenkle at 44D.

0.62

• r—

O

OU

QJ

COowQ

0.61

0.60

0.59

0.2

-

(3 = 0.54

,

- Q Flange tap location A /\ Flange tap location B \7 Flange tap location C

1

1 Flange tap location D till API 14 3-A G A 3 (RG) equation

D = 52 mm

0.6 1.0 1.4

Fig

Pipe Reynolds Number/10

ure 42. Discharge coefficient vs. Reynolds number for the 0.54 beta

ratio plate, oversize Sprenkle at 44D, and 4 flange tap locations.

34
0.62

• I—

I

O

CDOU

OJ

CO

CJ&Q Q

0.61 -

0.60 -

0.59

; (3 = 0.67

(^ Flange lap location A /\ Flange tap location B \/ Flange tap location C

1

1 Flange tap location D

API 14.3-A G A 3 (RG) equation

1 , 1 1 1 . 1

D =

1

52 mm

1 2.2 2.6

Fig

02 0.5 1.0 1.4 1.8

, 6

Pipe Reynolds Number/ 10

ure 43. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate, oversize Sprenkle at 44D and 4 flange tap locations.

Orifice Plate

Long Radius

Elbow

Figure 44. Test configuration, 52 mm (2 in) orifice meter, elbow at 17D.

35
0.62

• 1—1 O

O

u

CD

?-, COu

w

Q

0.61 -

0.50 -

0.59

-

|g = 0.54

- i i «

^

-

(J) Flange tap location A /\ Flange tap location B

- Sy Flange tap location C

1

1 Flange tap location D

Baseline

- API 14.3-A.G.A- 3 (RG) equation

D == 52 mm

1

1

1 0.2

Fig

0.6 1.0 Pipe Reynolds Number/10

ure 45. Discharge coefficient vs. Reynolds number for the 0.54 beta

ratio plate, elbow at 17D, and an in-line, 7 tube bundle at 12D.

0.62

QJ

-Ii U

oO

CD

cdo

0.51

0.60

0.59

^ 0.6?

Fig

Q Flange tap location A /\ Flange lap location B \/ Flange tap location C

I I Flange tap location D

Baseline

API 14.3-A.G.A. 3 (RG) equation

\ i \ , L

D = 52 mm

0.2 0.6 1.0 1.4 2.2 2.6

, 6

Pipe Reynolds Number/lO

ure 46. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio plate, elbow at 17D, and an m-lme, 7 tube bundle at 12D.

36
Table 3. Measured and calculated quantities for 0.^3 beta ratio, elbow at 104D.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 lun Orifice Diameter = A. 4437 cm (1.7495 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (k9/m^) (kPa) (kg/s) (/10^)

CY,

042491- 1 3.8308 286.81 45.36 27.945 1 .5059 1.0250 0.5986 0.5996

042491- 2 3.8430 286.72 45.52 27.930 1.5090 1.0272 0.5990 0.5999

042491- 3 3. 8836 287.29 45.90 15.728 1.1404 0.7749 0.6011 0.6017

042491 - 4 3.8884 287.09 45.99 15.740 1.1426 0.7766 0.6014 0.6020

042491 - 5 3.9692 288.24 46.75 6.686 0.7512 0.5087 0.6022 0.6025

042491 - 6 3.9556 288.11 46.61 6.762 0.7556 0.5119 0.6032 0.6035

042491- 7 3.7495 286.31 44.48 44.443 1.8807 1.2829 0.5981 0.5996

042491 - 8 3.7766 285.91 44.87 44.401 1.8900 1.2901 0.5987 0.6003

042591- 1 3.9556 287.02 46.81 14.112 1.0916 0.7415 0.6016 0.6021 042591- 2 3.9590 286.86 46.87 13.971 1.0880 0.7393 0.6022 0.6027

042591 - 3 3.7812 285.34 45.02 46.450 1.9450 1.3294 0.6013 0.6029

042591- 4 3.7879 286.14 44.97 45.680 1.9245 1.3128 0.6004 0.6020

042591- 5 3.8842 286.42 46.06 29.642 1.5693 1.0685 0.6010 0.6020

042591 - 6 3.8831 286.22 46.09 29.948 1.5754 1.0731 0.6001 0.6011

042591 - 7 4.0201 287.53 47.48 6.903 0.7698 0.5219 0.6027 0.6029

042591- 8 4.0176 287.69 47.42 7.175 0.7846 0.5317 0.6029 0.6031

Table 4. Measured and calculated quantities for 0.55 beta ratio, elbow at 104D.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa)

042391- 1 3.8773

042391- 2 3.8710

042391- 3 3.9454

042391- 4 3.9493

042391- 5 3.7199

042391- 6 3.7162

042391 - 7 4.0292

042391- 8 4.0275

042391- 9 3.8571 042391- 10 3.8518

042591- 1 3.9493

042591- 2 3.9435

042591- 3 3.7345

042591- 4 3.7255

042591- 5 3.8423

042591- 6 3.8345

042591- 7 3.9968

042591- 8 3.9968

CY,

(K) (kg/m^) (kPa) (kg/s) (/10^)

-•^

286.73 45.93 12.827 1.7571 1.1956 0.6011 0.6015 286.49 45.89 12.779 1.7548 1.1947 0.6016 0.6020 287.19 46.65 6.198 1.2371 0.8401 0.6042 0.6044 287.08 46.72 6.255 1.2433 0.8445 0.6041 0.6043

278.90 45.43 20.542 2.2192 1.5424 0.6031 0.6038

275.50 46.00 20.203 2.2108 1.5498 0.6021 0.6028

287.21 47.65 2.504 0.7973 0.5409 0.6066 0.6066

287.45 47.58 2.938 0.8635 0.5855 0.6068 0.6069

286.32 45.76 12.579 1.7421 1.1868 0.6029 0.6033 286.26 45.71 12.347 1.7267 1.1765 0.6035 0.6039

286.70 46.79 6.219 1.2456 0.8469 0.6065 0.6067

286.66 46.73 6.174 1.2383 0.8420 0.6056 0.6058

285.01 44.52 19.645 2.1377 1.4631 0.6000 0.6006 284.77 44.46 19.771 2.1485 1.4715 0.6015 0.6022

286.29 45.59 13.645 1.8085 1.2324 0.6021 0.6025

285.90 45.56 13.214 1.7827 1.2161 0.6032 0.6037

287.13 47.28 3.049 0.8744 0.5935 0.6051 0.6052

287.30 47.24 3.037 0.8737 0.5928 0.6061 0.6062

Table 5. Measured and calculated quantities for 0.67 beta ratio, elbow at 104D.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /un Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

042391- 1 3.8924 286.81 46.09 3.887 1.5598 1.0609 0.6061 0.6062

042391- 2 3.8873 286.38 46.11 3.873 1.5505 1.0557 0.6035 0.6036

042391- 3 3.8869 286.46 46.09 3.876 1.5550 1.0586 0.6051 0.6052

042391- 4 3.8078 285.99 45.23 5.783 1.8695 1.2754 0.6012 0.6014

042391- 5 3.7981 286.48 45.03 5.787 1.8731 1.2765 0.6035 0.6037

042391- 6 3.7172 285.06 44.31 7.805 2.1609 1.4792 0.6043 0.6045

042391- 7 3.7350 285.52 44.44 7.357 2.1029 1.4375 0.6048 0.6050

042391- 8 3.9161 286.72 46.39 2.574 1.2735 0.8661 0.6062 0.6062

042391- 9 3.9181 286.82 46.40 2.595 1.2789 0.8696 0.6062 0.6063

042391- 10 3.7907 286.00 45.02 5.824 1.8830 1.2848 0.6047 0.6049

042591- 1 3.8605 285.93 45.87 5.811 1.8924 1.2904 0.6028 0.6030

042591- 2 3.8597 285.91 45.86 5.797 1.8929 1.2908 0.6038 0.6039

042591- 3 3.9789 286.87 47.11 2.581 1.2863 0.8738 0.6068 0.6068

042591- 4 3.9743 287.16 47.00 2.595 1.2872 0.8739 0.6O63 0.6063

042591- 5 3.7585 285.51 44.72 8.068 2.2056 1.5074 0.6038 0.6041 042591 - 6 3.7667 285.45 44.83 7.603 2.1418 1.4638 0.6033 0.6035

042591- 7 3.9202 286.32 46.51 3.759 1.5358 1.0455 0.6042 0.6043

042591- 8 3.9139 286.43 46.42 3.821 1.5470 1.0529 0.6042 0.6043

37
Table 6. Measured and calculated quantities for 0.73 beta ratio, elbow at 10AD.

Pipe Diameter = 10.366 cm (A. 081 in), 3.8 iim Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (HPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

042291- 4 3.8179 285.93 45.36 4.159 2.0077 1.3697 0.6032 0.6033

0A2291

5 3.8665 286.56 45.83 3.258 1.7850 1.2152 0.6028 0.6029

042291- 6 3.8592 285.94 45.85 3.282 1.7936 1.2230 0.6033 0.6034

042291- 7 3.7767 285.53 44.94 4.935 2.1751 1.4861 0.6027 0.6028

042291- 8 3.7217 285.29 44.32 5.073 2.1850 1.4947 0.6013 0.6014

042291- 1 3.8423 286.28 45.59 3.148 1.7527 1.1944 0.6037 0.6038

042291- 2 3.8453 286.21 45.64 3.152 1.7509 1.1933 0.6024 0.6025

042491- 1 3.8415 286.00 45.63 3.204 1.7747 1.2102 0.6057 0.6058

042491- 2 3.8432 286.35 45.59 3.208 1.7722 1.2074 0.6048 0.6048

042491- 3 3.7154 285.26 44.25 5.095 2.1974 1.5034 0.6039 0.6040

042491- 4 3.7132 278.61 45.39 4.940 2.1892 1.5228 0.6034 0.6035

042491 - 5 3.8599 286.28 45.80 2.732 1.6361 1.1146 0.6036 0.6037

042491- 6 3.8620 285.67 45.93 2.740 1.6421 1.1204 0.6040 0.6041 042491- 7 3.7721 286.27 44.75 4.168 1.9951 1.3607 0.6028 0.6029

042491- 8 3.7709 285.04 44.95 4.109 1.9864 1.3589 0.6031 0.6032

042491- 9 3.8144 286.03 45.30 3.548 1.8519 1.2631 0.6027 0.6028

042491- 10 3.8042 285.86 45.21 3.556 1.8514 1.2635 0.6026 0.6026

Table 7. Measured and calculated quantities for 0.55 beta ratio, reducer at 21D, III at 19D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 jtm Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)CY,

052191- 1 3.9498 285.78 46.96 13.613 1 .8350 1.2503 0.6026 0.6030

052191- 2 3.9389 285.80 46.83 13.488 1.8224 1.2419 0.6021 0.6025

052191- 3 3.8191 284.47 45.63 20.006 2.1827 1.4944 0.5996 0.6003

052191- 4 3.8185 284.46 45.63 19.952 2.1819 1.4939 0.6003 0.6009

052191- 5 4.0021 285.84 47.57 6.394 1.2684 0.8636 0.6041 0.6043

052191- 6 4.0079 286.40 47.54 6.473 1.2760 0.8676 0.6042 0.6044

052191- 7 4.0336 286.84 47.77 2.658 0.8222 0.5582 0.6063 0.6064

052291- 1 3.9914 286.83 47.27 2.681 0.8223 0.5586 0.6069 0.6070

052291- 2 4.0380 286.89 47.81 2.734 0.8372 0.5683 0.6084 0.6085

052291- 3 3.9597 285.77 47.08 5.911 1.2162 0.8286 0.6056 0.6058

052291- 4 3.9540 285.94 46.98 5.884 1.2143 0.8270 0.6067 0.6068

052291 - 5 3.7468 284.73 44.72 20.819 2.2228 1.5222 0.6047 0.6053

052291- 6 3.7541 285.15 44.73 20.340 2.1913 1.4989 0.6030 0.6036

052291- 7 3.8534 285.83 45.80 13.798 1.8253 1.2450 0.6029 0.6033

052291- 8 3.8478 285.21 45.84 13.918 1.8346 1.2534 0.6031 0.6035

Table 8. Measured and calculated quantities for 0.55 beta ratio, elbow at 21D, IT1 at 19D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Ra C CY2

(MPa) (.<•> (kg/m^) (kPa) (kg/s)

060491- 1 3.8682 286.06 45.94 18.990 2.1441 060491- 2 3.8598 285.13 46.00 18.751 2.1334

060491- 4 4.1087 286.90 48.65 2.879 0.8673

060491 - 5 4.0305 286.06 47.87 5.923 1.2329

060491- 6 4.0263 286.31 47.78 5.910 1.2304 060491- 7 3.9302 285.68 46.75 13.031 1.7989

060491- 8 3.9248 285.33 46.74 12.958 1.7921 060591- 1 4.0525 286.71 48.02 3.004 0.8801 060591- 2 4.0510 286.94 47.95 3.002 0.8769

060591- 3 3.9131 285.01 46.66 12.603 1.7656 060591- 4 3.9325 285.46 46.81 12.616 1.7695 060591- 5 3.8089 284.32 45.54 19.069 2.1439

060591- 6 3.8176 284.96 45.53 18.924 2.1301 060591 - 7 3.9699 285.76 47.20 6.279 1.2543 060591- 8 3.9650 286.34 47.04 6.439 1.2664

(/10°)

1.4614 0.6026 0.6032

1.4575 0.6030 0.6036

0.5882 0.6089 0.6090 0.8387 0.6082 0.6084

0.8365 0.6083 0.6084

1.2263 0.6052 0.6056

1.2228 0.6046 0.6050 0.5976 0.6089 0.6090

0.5951 0.6072 0.6073

1.2058 0.6046 0.6049

1.2069 0.6046 0.6050

1.4685 0.6039 0.6045

1.4566 0.6024 0.6030

0.8545 0.6052 0.6053 0.8616 0.6044 0.6046

38
Table 9. Measured and calculated quantities for 0.55 beta ratio, reducer at 17D, IT1 at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /un Orifice Diameter = 5.7U2 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C era

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

052891- 1 3.9862 286.66 47.24 6.315 1.2559 0.8535 0.6040 0.6042

052891- 2 3.9788 286.16 47.24 6.305 1.2518 0.8519 0.6026 0.6028

052891- 3 3.7978 284.97 45.29 20.257 2.1894 1.4975 0.6000 0.6006

052891- 4 3.7934 285.89 45.07 20.502 2.2009 1.5021 0.6009 0.6016

052891- 5 4.0394 286.87 47.83 3.192 0.9012 0.6118 0.6060 0.6061 052891- 6 4.0295 286.97 47.69 3.279 0.9122 0.6192 0.6060 0.6061 052891- 7 3.9010 285.04 46.51 12.892 1.7816 1.2168 0.6041 0.6045 052891- 8 3.8929 285.33 46.36 12.800 1.7676 1.2066 0.6025 0.6029

052991- 1 3.9271 285.27 46.78 13.386 1.8189 1.2412 0.6035 0.6039

052991- 2 3.9210 284.94 46.77 13.325 1.8119 1.2376 0.6027 0.6031 052991- 3 4.0013 286.16 47.51 6.477 1.2724 0.8657 0.6026 0.6028

052991- 4 4.0107 286.13 47.62 6.581 1.2866 0.8753 0.6037 0.6039

052991- 5 3.8205 284.45 45.65 20.410 2.2192 1.5194 0.6035 0.6041 052991- 6 3.8322 285.19 45.66 19.870 2.1814 1.4906 0.6011 0.6018

Table 10. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, ITl at 150, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 (im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

053091- 1 4.0538 286.24 48.12 5.731 1.2086 0.8216 0.6046 0.6048

053091- 2 4.0506 286.75 47.98 5.732 1.2044 0.8177 0.6033 0.6034 053091- 3 3.8670 284.45 46.21 19.296 2.1679 1.4835 0.6027 0.6033 053091- 4 3.8543 285.38 45.89 18.913 2.1351 1.4579 0.6016 0.6022

053091- 5 4.0823 286.43 48.42 3.052 0.8856 0.6015 0.6053 0.6054

053091 - 6 4.0730 286.62 48.27 3.120 0.8964 0.6086 0.6069 0.6070

053091- 7 3.9193 285.96 46.56 13.443 1.8254 1.2437 0.6058 0.6062 053091- 8 3.9155 284.94 46.70 13.276 1.8106 1.2367 0.6038 0.6042 053191- 1 3.8717 286.37 45.92 13.427 1.8072 1.2308 0.6043 0.6047

053191- 2 3.8704 285.21 46.12 13.350 1.8041 1.2322 0.6037 0.6042

053191- 3 4.0123 286.53 47.57 3.085 0.8846 0.6012 0.6068 0.6068

053191- 4 4.0107 286.66 47.53 3.134 0.8910 0.6054 0.6065 0.6066

053191- 5 3.7868 285.59 45.05 18.965 2.1217 1.4492 0.6025 0.6031 053191- 6 3.7735 285.42 44.92 19.682 2.1593 1.4757 0.6028 0.6034

053191- 7 3.9397 286.04 46.79 6.467 1.2654 0.8618 0.6042 0.6044

053191- 8 3.9642 286.11 47.08 6.568 1.2784 0.8702 0.6039 0.6041

Table 11. Measured and calculated quantities for 0.55 beta ratio, reducer at 13D, ITl at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) C/IO^)

052391- 1 3.9370 286.13 46.75 12.906 1.7766 1.2097 0.6006 0.6010

052391- 2 3.9393 285.19 46.94 12.847 1.7800 1.2148 0.6019 0.6023 052391- 3 3.8491 286.24 45.68 19.273 2.1447 1.4615 0.6000 0.6006

052391- 4 3.8541 284.54 46.04 18.991 2.1396 1.4640 0.6007 0.6012

052391- 5 4.0068 286.26 47.55 5.983 1.2236 0.8322 0.6026 0.6028

052391- 6 4.0087 286.41 47.55 6.083 1.2330 0.8383 0.6022 0.6024

052391- 7 4.0851 286.68 48.41 2.951 0.8692 0.5900 0.6042 0.6043

052391- 8 4.0940 286.98 48.46 2.970 0.8761 0.5942 0.6067 0.6068

052491 -1 3.7480 285.67 44.57 19.878 2.1586 1.4748 0.6019 0.6026

052491- 2 3.7512 285.22 44.69 19.697 2.1430 1.4657 0.5996 0.6002

052491 - 3 3.9202 286.06 46.56 6.784 1.2891 0.8781 0.6025 0.6027

052491- 4 3.9150 286.23 46.47 6.847 1.2936 0.8808 0.6024 0.6026

052491- 5 3.8403 285.97 45.62 13.447 1.7904 1.2210 0.6002 0.6006

052491- 6 3.8370 286.29 45.52 13.426 1.7919 1.2211 0.6018 0.6022

052491- 7 3.9876 286.46 47.29 3.369 0.9179 0.6241 0.6042 0.6043

052491- 8 3.9834 286.49 47.23 3.445 0.9271 0.6303 0.6038 0.6039

39
Table 12. Measured and calculated quantities for 0.55 beta ratio, elbow at 13D, IT1 at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 im Orifice Diameter = 5.7U2 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2 (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

060691 -1 4.0382 286.59 47.87 5.910 1.2230 0.8308 0.6040 0.6042

060691- 2 4.0356 286.26 47.90 5.889 1.2213 0.8303 0.6041 0.6042

060691- 3 4.0905 286.65 48.48 3.189 0.9053 0.6145 0.6050 0.6051 060691- 4 4.0953 286.72 48.52 3.208 0.9106 0.6180 0.6064 0.6065

060691 - 5 3.9388 285.10 46.95 13.179 1.8031 1.2308 0.6019 0.6023

060691- 6 3.9353 286.27 46.70 13.183 1.7982 1.2240 0.6018 0.6022

060691 - 7 3.8458 284.68 45.91 19.083 2.1405 1.4642 0.6003 0.6009

060691 - 8 3.8489 285.51 45.80 18.900 2.1274 1.4523 0.6002 0.6008

060791- 1 4.0083 286.34 47.56 2.706 0.8241 0.5604 0.6037 0.6038

060791- 2 4.0092 286.48 47.54 2.708 0.8266 0.5619 0.6053 0.6054

060791- 3 3.8623 284.93 46.07 12.960 1.7738 1.2124 0.6028 0.6032

060791- 4 3.8622 284.69 46.11 12.871 1.7668 1.2083 0.6022 0.6026

060791- 5 3.9321 285.89 46.73 6.414 1.2569 0.8564 0.6031 0.6033

060791- 6 3.9321 285.96 46.72 6.463 1.2648 0.8617 0.6046 0.6048

060791 - 7 3.7607 285.80 44.70 19.983 2.1651 1.4785 0.6013 0.6019

060791- 8 3.7581 285.38 44.74 19.726 2.1511 1.4705 0.6010 0.6016

Table 13. Measured and calculated quantities for 0.67 beta ratio, reducer at 21D, IT1 at 19D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 lun Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

052191- 1 3.9866 285.74 47.41 3.876 1.5791 1.0756 0.6059 0.6060

052191- 2 3.9894 285.71 47.45 3.829 1.5697 1.0693 0.6058 0.6059

052191- 3 3.9091 285.09 46.60 5.938 1.9336 1.3204 0.6046 0.6047

052191- 4 3.9204 286.09 46.55 5.924 1.9279 1.3131 0.6038 0.6039

052191- 5 4.0162 286.46 47.63 2.816 1.3558 0.9216 0.6089 0.6090

052191- 6 4.0117 286.27 47.61 2.810 1.3601 0.9250 0.6117 0.6117

052191- 7 4.0125 286.27 47.62 2.807 1.3557 0.9220 0.6101 0.6101 052191- 8 3.8476 284.84 45.91 7.485 2.1589 1.4762 0.6057 0.6059

052191- 9 3.8523 286.22 45.72 7.385 2.1374 1.4566 0.6050 0.6052

052191- 10 3.9839 285.49 47.42 3.204 1.4418 0.9827 0.6085 0.6086

052191- 11 3.9018 283.86 46.74 2.975 1.3799 0.9452 0.6088 0.6089

052291- 1 3.7951 285.84 45.10 7.533 2.1380 1.4593 0.6032 0.6034

052291- 2 3.8027 284.67 45.40 7.409 2.1287 1.4570 0.6036 0.6038

052291- 3 3.9590 285.94 47.04 2.720 1.3260 0.9030 0.6098 0.6099

052291- 4 3.9539 286.24 46.93 2.735 1.3283 0.9040 0.6099 0.6100

052291- 5 3.8511 284.94 45.93 6.058 1.9379 1.3247 0.6043 0.6044

052291- 6 3.8479 285.64 45.77 6.035 1.9301 1.3172 0.6040 0.6041 052291- 7 3.9273 285.83 46.68 4.049 1.6035 1.0928 0.6067 0.6068

052291- 8 3.9199 285.31 46.69 4.081 1.6127 1.1005 0.6077 0.6078

Table 14. Measured and calculated quantities for 0.67 beta ratio, elbow at 21D, 1T1 at 19D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 jim Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

CY,

060491- 1 3.8888 286.46 46.11 6.010 1.9357 1.3178 0.6047 0.6049

060491- 2 3.8841 286.57 46.04 6.005 1.9349 1.3169 0.6052 0.6054

060491 - 3 3.8258 284.57 45.69 7.572 2.1652 1.4819 0.6054 0.6056

060491- 4 3.8258 286.36 45.38 7.547 2.1488 1.4643 0.6038 0.6040

060491- 5 3.9470 285.72 46.94 4.080 1.6081 1.0960 0.6044 0.6045

060491 - 6 3.9457 285.36 46.99 4.121 1.6167 1.1028 0.6043 0.6044

060491- 7 3.9868 285.78 47.40 2.638 1.3024 0.8870 0.6059 0.6059

060491- 8 3.9881 285.66 47.44 2.613 1.2993 0.8852 0.6071 0.6071 060591- 1 3.9744 286.03 47.21 3.998 1.5981 1.0879 0.6051 0.6052

060591- 2 3.9730 286.53 47.10 3.995 1.5942 1.0840 0.6044 0.6045

060591- 3 3.9013 285.73 46.39 5.827 1.9078 1.3009 0.6035 0.6036

060591- 4 3.8995 285.75 46.37 5.799 1.9040 1.2982 0.6039 0.6041 060591- 5 3.9903 285.88 47.43 2.685 1.3142 0.8948 0.6058 0.6058

060591- 6 4.0066 285.82 47.63 2.697 1.3226 0.9005 0.6070 0.6070

060591- 7 3.8420 286.14 45.61 7.355 2.1274 1.4502 0.6040 0.6042

060591- 8 3.8405 285.01 45.79 7.255 2.1135 1.4447 0.6030 0.6032

40
Table 15. Measured and calculated quantities for 0.67 beta ratio, reducer at 17D, IT1 at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (A. 081 in), 3.8 im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Densiti (MPa) (K) (kg/m^

052891- 1 3.8564 285.03 45.98

052891- 2 3.8503 285.16 45.88

052891- 3 3.9290 286.42 46.60

052891- 4 3.9236 285.76 46.65 052891- 5 3.7893 284.70 45.23

052891- 6 3.8048 284.94 45.38

052891- 7 3.9458 286.43 46.80

052891- 8 3.9446 286.09 46.84

052991- 1 3.9127 286.21 46.44

052991- 2 3.9079 285.19 46.57

052991- 3 3.9641 285.39 47.20

052991- 4 3.9687 285.85 47.17

052991- 5 4.0153 286.28 47.65

052991- 6 4.0218 286.06 47.77

052991- 7 3.8501 285.06 45.90

052991- 8 3.8532 285.14 45.92

Dif Press Flow Rate Pipe Re No

(kPa) (kg/s)

5.968 1.9236

5.945 1.9156 3.766 1.5370

3.781 1.5401 7.661 2.1609 7.557 2.1455

2.654 1.2937 2.708 1.3089 5.887 1.9108 5.847 1.9097 4.039 1.6013

4.071 1.6042 2.510 1.2702 2.520 1.2764 7.844 2.2018

7.731 2.1837

CY,

(/10^)

1.3145 0.6039 0.6041 1.3088 0.6032 0.6034

1.0459 0.6034 0.6035

1.0498 0.6032 0.6033

1.4791 0.6037 0.6039

1.4675 0.6026 0.6028

0.8802 0.6038 0.6039

0.8913 0.6045 0.6046

1.3012 0.6010 0.6011 1.3037 0.6019 0.6021 1.0919 0.6032 0.6033

1.0926 0.6021 0.6022 0.8638 0.6041 0.6042

0.8684 0.6052 0.6053

1.5047 0.6035 0.6037

1.4920 0.6027 0.6030

Table 16. Measured and calculated quantities for 0.67 beta ratio, elbow at 170, IT1 at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Dens it (MPa) (K) (kg/m^

053091- 1 3.9595 285.70 47.09

053091- 2 3.9690 285.08 47.32

053091- 3 3.9834 285.77 47.36

053091- 4 3.9798 286.22 47.24

053091- 5 3.8788 286.31 46.02

053091- 6 3.8791 285.56 46.16

053091- 7 3.8189 284.32 45.66

053091 - 8 3.8250 285.36 45.55

053191- 1 3.9485 286.13 46.88

053191- 2 3.9459 285.71 46.93

053191- 4 3.8029 285.47 45.26

053191- 5 3.7965 284.20 45.41 053191- 6 3.8624 285.66 45.94

053191- 7 3.8480 285.41 45.81 053191- 8 3.9508 285.65 47.00

053191- 9 3.9510 286.05 46.93

Dif Press Flow Rate Pip>e Re No

(kPa) (kg/s)

4.057 1.6127 4.060 1.6131 2.565 1.2814 2.582 1.2873 5.853 1.9058 5.766 1.8967

7.440 2.1421

7.351 2.1233

3.912 1.5695 3.915 1.5704 7.533 2.1385 7.670 2.1652 6.049 1.9321 6.087 1.9344 2.679 1.3040 2.713 1.3099

CY, (/10^)

1.0989 0.6069 0.6070

1.1007 0.6053 0.6054 0.8728 0.6047 0.6048

0.8759 0.6064 0.6064

1.2980 0.6039 0.6041 1.2942 0.6047 0.6048

1.4671 0.6044 0.6047

1.4505 0.6035 0.6037

1.0685 0.6028 0.6029

1.0703 0.6026 0.6027

1 .4609 0.6023 0.6025

1.4838 0.6034 0.6036

1.3183 0.6028 0.6030

1.3209 0.6025 0.6026 0.8888 0.6045 0.6046

0.8919 0.6039 0.6039

Table 17. Measured and calculated quantities for 0.67 beta ratio, reducer at 130, IT1 at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID

052391- 1 052391 - 052391-

052391-

052391-

052391- 052391- 7 052391- 8 052391- 9 052391-10

052491- 1 052491-

052491-

052491-

052491-

052491-

052491-

Pressure Temperature

(MPa) (K)

9725

9681 0044

0001 9013

9151 8232

8221 9536

9521 8464

8414 9306

9282 8946

8955

7585

052491- 8 3.7592

285.91 286.54 286.18

285.94 285.29

285.49

285.96

285.88

285.94

285.32 285.89

285.44 286.23

286.13 285.39 285.89

285.17 284.37

Density

(kg/m^)

47.21 47.04

47.54 47.53 46.47

46.60 45.42

45.42

46.98

47.08

45.71 45.73

46.65

46.64 46.37

46.29

44.78

44.93

Dif Press Flow Rate Pipe Re No

(kPa) (kg/s)

4.157 1.6307 4.159 1.6254

2.791 1.3387 2.782 1.3354 5.949 1.9247

5.935 1.9234 7.842 2.1882

7.791 2.1720 4.107 1.6064 4.157 1.6176 5.780 1.8754 5.773 1.8721 2.533 1.2593 2.544 1.2596 3.968 1.5665 3.965 1.5647

7.820 2.1614

7.710 2.1496

CY, (/10^)

1.1105 0.6054 0.6056

1.1053 0.6044 0.6045 0.9107 0.6045 0.6046

0.9090 0.6041 0.6041 1.3138 0.6020 0.6022

1.3121 0.6016 0.6017

1.4926 0.6030 0.6032

1.4819 0.6005 0.6007

1.0941 0.6016 0.6017

1.1034 0.6015 0.6016

1.2791 0.6001 0.6003

1.2784 0.5993 0.5995 0.8573 0.6026 0.6026 0.8578 0.6015 0.6016

1.0691 0.6007 0.6008

1.0666 0.6007 0.6008

1.4784 0.6007 0.6009

1.4732 0.6007 0.6009

41
Table 18. Measured and calculated quantities for 0.67 beta ratio, elbow at 130, IT1 at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY,

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

£.

060691- 2 4.0051 286.45 47.50 2.533 1.2798 0.8700 0.6069 0.6069

060691- 3 3.9696 285.96 47.16 3.900 1.5782 1.0746 0.6052 0.6053

060691- 4 3.9646 285.79 47.14 3.891 1.5755 1.0733 0.6051 0.6052

060691- 5 3.8922 285.98 46.24 5.989 1.9297 1.3151 0.6031 0.6032

060691- 6 3.8900 284.51 46.48 5.932 1.9211 1.3140 0.6018 0.6020

060691- 7 3.8269 284.73 45.68 7.638 2.1601 1.4778 0.6014 0.6016

060691- 8 3.8247 286.04 45.42 7.615 2.1508 1.4668 0.6014 0.6016

060691- 9 3.9595 285.78 47.08 3.511 1.4921 1.0166 0.6037 0.6038

060791- 3 3.9493 285.77 46.96 2.535 1.2708 0.8659 0.6058 0.6059

060791- 4 3.9485 285.73 46.95 2.534 1.2673 0.8636 0.6044 0.6044

060791 - 5 3.7819 285.93 44.93 7.896 2.1827 1.4897 0.6026 0.6028

060791- 6 3.7825 285.51 45.01 7.805 2.1684 1.4815 0.6017 0.6019

060791- 7 3.9040 285.36 46.49 4.279 1.6356 1.1162 0.6032 0.6033

060791- 8 3.9000 285.47 46.42 4.315 1.6441 1.1217 0.6042 0.6043

060791- 9 3.8358 286.29 45.51 6.190 1.9427 1.3239 0.6020 0.6021

Table 19. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, ITl at 150, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

061091- 1 3.9224 285.10 46.76 12.857 1 . 7774 1.2135 0.6020 0.6023

061091- 2 3.9294 286.38 46.61 12.610 1.7624 1.1994 0.6036 0.6040

061091- 1 3.8309 284.46 45.78 19.608 2.1724 1.4872 0.6019 0.6025 061091- 2 3.8200 283.82 45.76 19.544 2.1676 1.4864 0.6017 0.6023

061091- 3 3.9899 286.07 47.39 6.201 1.2483 0.8495 0.6049 0.6050

061091- 4 4.0024 285.86 47.58 6.316 1.2634 0.8602 0.6054 0.6056

071191- 2 4.0089 283.68 48.06 6.166 1.2575 0.8606 0.6068 0.6070

071191- 3 3.8227 282.00 46.12 19.397 2.1770 1.4995 0.6042 0.6049

071191- 4 3.8236 282.06 46.12 19.271 2.1640 1.4903 0.6026 0.6032

071191- 5 4.0797 288.46 48.02 2.994 0.8764 0.5924 0.6073 0.6073

071191- 6 4.0746 287.84 48.07 3.009 0.8791 0.5951 0.6073 0.6074

071291- 1 3.9857 285.04 47.53 6.154 1.2460 0.8501 0.6052 0.6054 071291- 2 3.9841 285.12 47.49 6.151 1.2464 0.8503 0.6058 0.6060

071291- 3 3.8039 283.12 45.69 19.834 2.1835 1.5001 0.6021 0.6027

071291- 4 3.8037 282.90 45.73 19.568 2.1696 1.4914 0.6021 0.6027

071291- 5 3.9881 285.54 47.46 3.113 0.8889 0.6057 0.6075 0.6076

071291- 6 3.9912 285.96 47.42 3.130 0.8904 0.6061 0.6072 0.6073

071291- 7 3.8992 283.19 46.83 13.114 1 .8009 1.2356 0.6035 0.6039

071291- 8 3.8983 282.99 46.85 13.096 1.8008 1.2362 0.6037 0.6041 071291- 9 3.8983 283.01 46.85 13.068 1.7942 1.2316 0.6022 0.6026

071291- 10 3.9049 283.48 46.84 13.062 1.7917 1.2284 0.6015 0.6019

Table 20. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, ITl at 150, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 (im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

CY,

061091- 1 3.9224 285.10 46.76 12.866 1 . 7774 1.2135 0.6018 0.6021 061091- 2 3.9294 286.38 46.61 12.625 1 . 7624 1.1994 0.6033 0.6037

061091- 1 3.8309 284.46 45.78 19.650 2.1724 1.4872 0.6013 0.6019

061091- 2 3.8200 283.82 45.76 19.575 2.1676 1.4864 0.6012 0.6018

061091- 3 3.9899 286.07 47.39 6.204 1.2483 0.8495 0.6047 0.6049

061091- 4 4.0024 285.86 47.58 6.319 1.2634 0.8602 0.6053 0.6055

071191- 2 4.0089 283.68 48.06 6.174 1.2575 0.8606 . 6064 0.6066

071191- 3 3.8227 282.00 46.12 19.474 2.1770 1.4995 0.6030 0.6036

071191- 4 3.8236 282.06 46.12 19.348 2.1640 1.4903 0.6014 0.6020

071191- 5 4.0797 288.46 48.02 3.007 0.8764 0.5924 0.6059 0.6060

071191- 6 4.0746 287.84 48.07 3.022 0.8791 0.5951 0.6060 0.6061 071291- 1 3.9857 285.04 47.53 6.161 1.2460 0.8501 0.6049 0.6050

071291- 2 3.9841 285.12 47.49 6.161 1 . 2464 0.8503 0.6053 0.6054

071291- 3 3.8039 283.12 45.69 19.893 2.1835 1.5001 0.6012 0.6018

071291- 4 3.8037 282.90 45.73 19.627 2.1696 1.4914 0.6012 0.6018

071291- 5 3.9881 285.54 47.46 3.122 0.8889 0.6057 0.6067 0.6068

071291- 6 3.9912 285.96 47.42 3.142 0.8904 0.6061 0.6061 0.6062

071291- 7 3.8992 283.19 46.83 13.145 1.8009 1.2356 0.6028 0.6032

071291- 8 3.8983 282.99 46.85 13.132 1.8008 1.2362 0.6029 0.6033

071291- 9 3.8983 283.01 46.85 13.097 1.7942 1.2316 0.6015 0.6019

071291- 10 3.9049 283.48 46.84 15.097 1.7917 1.2284 0.6007 0.6011

42
Table 21. Measured and calculated quantities for 0.55 beta ratio, elbow at 220, IT1 at 150, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 5.71A2 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C Cl'2 (MPa) (K) (l(g/m^) (kPa) (kg/s) (/10^)

072591- 1 3.8462 286.62 45.58 12.836 1.7523 1.1930 0.6015 0.6019

072591 - 2 3.8459 286.18 45.65 12.734 1.7447 1.1891 0.6009 0.6013

072591- 3 3.9399 287.56 46.52 3.354 0.9111 0.6182 0.6060 0.6061 072591- A 3.9415 287.72 46.51 3.310 0.9027 0.6123 0.6045 0.6046

072591 - 5 3.9233 287.83 46.28 6.228 1.2338 0.8368 0.6036 0.6038

072591- 6 3.9247 287.08 46.43 6.224 1.2376 0.8409 0.6047 0.6049

072591- 7 3.9218 287.09 46.39 6.222 1.2336 0.8382 0.6031 0.6033

072591- 8 3.7483 286.95 44.36 19.627 2.1350 1.4542 0.6006 0.6012

072591 - 9 3.7512 285.69 44.61 19.409 2.1272 1.4532 0.6001 0.6007

072691- 1 3.9348 287.29 46.51 6.028 1.2180 0.8271 0.6042 0.6044

072691 - 2 3.9393 287.03 46.61 6.032 1.2246 0.8320 0.6066 0.6068

072691- 3 3.9648 287.58 46.81 3.534 0.9377 0.6360 0.6056 0.6057

072691- 4 3.9626 287.51 46.80 3.533 0.9411 0.6385 0.6080 0.6081 072691- 5 3.8683 287.11 45.75 12.738 1.7508 1.1903 0.6021 0.6025

072691- 6 3.8670 286.63 45.82 12.645 1.7531 1.1933 0.6047 0.6051

072691 - 7 3.9348 286.81 46.60 6.588 1.2817 0.8713 0.6076 0.6078

072691- 8 3.7520 286.27 44.52 20.403 2.1805 1.4875 0.6005 0.6012

072691 - 9 3.7536 286.50 44.50 20.313 2.1831 1.4884 0.6027 0.6033

Table 22. Measured and calculated quantities for 0.55 beta ratio, elbow at 22D, III at 150, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)CY,

072591- 1 3.8462 286.62 45.58 12.815 1.7523 1.1930 0.6020 0.6024

072591 - 2 3.8459 286.18 45.65 12.711 1.7447 1.1891 0.6014 0.6018

072591- 3 3.9399 287.56 46.52 3.358 0.9111 0.6182 0.6056 0.6057

072591- 4 3.9415 287.72 46.51 3.316 0.9027 0.6123 0.6039 0.6040

072591 - 5 3.9233 287.83 46.28 6.220 1.2338 0.8368 0.6040 0.6042

072591- 6 3.9247 287.08 46.43 6.219 1.2376 0.8409 0.6050 0.6052

072591- 7 3.9218 287.09 46.39 6.218 1.2336 0.8382 0.6033 0.6035

072591- 8 3.7483 286.95 44.36 19.616 2.1350 1.4542 0.6008 0.6014

072591- 9 3.7512 285.69 44.61 19.416 2.1272 1.4532 0.6000 0.6006

072691 -1 3.9348 287.29 46.51 6.022 1.2180 0.8271 0.6046 0.6047

072691- 2 3.9393 287.03 46.61 6.026 1.2246 0.8320 0.6069 0.6071 072691 - 3 3.9648 287.58 46.81 3.532 0.9377 0.6360 0.6058 0.6059

072691 - 4 3.9626 287.51 46.80 3.536 0.9411 0.6385 0.6078 0.6079

072691- 5 3.8683 287.11 45.75 12.723 1.7508 1.1903 0.6025 0.6029

072691 - 6 3.8670 286.63 45.82 12.626 1.7531 1.1933 0.6052 0.6056

072691- 7 3.9348 286.81 46.60 6.586 1.2817 0.8713 0.6077 0.6079

072691- 8 3.7520 286.27 44.52 20.394 2.1805 1.4875 0.6006 0.6013

072691- 9 3.7536 286.50 44.50 20.279 2.1831 1.4884 0.6032 0.6039

Table 23. Measured and calculated quantities for 0.55 beta ratio, elbow at 34D, III at 150, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (.kg/n?) (kPa) (kg/s) (/10^)

CY,

072991- 1 3.8220 287.48 45.14 13.035 1.7599 1.1960 0.6024 0.6028

072991- 2 3.8188 286.74 45.23 13.039 1.7548 1.1948 0.6000 0.6004

072991 - 3 3.7234 286.94 44.06 20.167 2.1591 1.4711 0.6012 0.6018

072991- 4 3.7159 285.38 44.24 19.767 2.1350 1.4603 0.5993 0.5999

072991 - 5 3.8884 287.13 45.99 6.930 1.2985 0.8826 0.6041 0.6044

072991- 6 3.8874 287.30 45.95 6.990 1.3051 0.8867 0.6049 0.6051 072991- 7 3.9110 288.38 46.04 3.533 0.9290 0.6294 0.6051 0.6053

072991- 8 3.9094 288.34 46.02 3.534 0.9297 0.6299 0.6056 0.6057

072991- 9 3.8284 287.86 45.15 12.502 1.7214 1.1688 0.6016 0.6020

073091- 1 3.7438 286.11 44.45 20.492 2.1864 1.4923 0.6013 0.6019

073091- 2 3.7443 287.69 44.18 20.499 2.1815 1.4832 0.6016 0.6023

073091- 3 3.8469 287.06 45.51 13.145 1.7755 1.2075 0.6027 0.6032

073091- 4 3.8467 288.19 45.31 13.218 1.7803 1.2075 0.6040 0.6044

073091- 5 3.9275 288.26 46.25 6.145 1.2268 0.8312 0.6044 0.6046

073091- 6 3.9272 287.88 46.32 6.183 1.2340 0.8368 0.6057 0.6059

073091- 7 3.9482 288.42 46.47 3.182 0.8885 0.6016 0.6071 0.6072

073091- 8 3.9546 288.74 46.49 3.174 0.8873 0.6003 0.6070 0.6071 073091- 9 3.9536 288.44 46.53 3.183 0.8893 0.6021 0.6072 0.6073

073091- 10 3.9383 288.21 46.39 6.018 1.2171 0.8245 0.6050 0.6052

073091- 11 3.9334 288.08 46.35 6.013 1.2155 0.8238 0.6047 0.6049

073091- 12 3.8491 287.44 45.47 13.184 1.7762 1.2069 0.6024 0.6028

073091- 13 3.9488 288.45 46.47 3.433 0.9205 0.6232 0.6055 0.6056

073091- 14 3.9811 288.17 46.90 5.931 1.2140 0.8221 0.6046 0.6048

43
Table 24. Measured and calculated quantities for 0.55 beta ratio, elbow at 3AD, IT1 at 150, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 mm Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(HPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

072991- 1 3.8220 287.48 45.14 13.011 1.7599 1.1960 0.6030 0.6034

072991- 2 3.8188 286.74 45.23 13.015 1.7548 1.1948 0.6005 0.6009

072991- 3 3.7234 286.94 44.06 20.162 2.1591 1.4711 0.6012 0.6019

072991- 4 3.7159 285.38 44.24 19.755 2.1350 1 .4603 0.5994 0.6001 072991- 5 3.8884 287.13 45.99 6.912 1.2985 0.8826 0.6050 0.6052

072991- 6 3.8874 287.30 45.95 6.973 1.3051 0.8867 0.6056 0.6058

072991- 7 3.9110 288.38 46.04 3.522 0.9290 0.6294 0.6061 0.6062

072991- 8 3.9094 288.34 46.02 3.524 0.9297 0.6299 0.6064 0.6065

072991- 9 3.8284 287.86 45.15 12.490 1.7214 1.1688 0.6019 0.6023

073091- 1 3.7438 286.11 44.45 20.486 2.1864 1.4923 0.6014 0.6020

073091- 2 3.7443 287.69 44.18 20.482 2.1815 1.4832 0.6018 0.6025

073091- 3 3.8469 287.06 45.51 13.144 1.7755 1.2075 0.6028 0.6032

073091- 4 3.8467 288.19 45.31 13.232 1.7803 1.2075 0.6037 0.6041 073091- 5 3.9275 288.26 46.25 6.146 1.2268 0.8312 0.6044 0.6046

073091- 6 3.9272 287.88 46.32 6.186 1.2340 0.8368 0.6055 0.6057

073091- 7 3.9482 288.42 46.47 3.194 0.8885 0.6016 0.6060 0.6061 073091- 8 3.9546 288.74 46.49 3.183 0.8873 0.6003 0.6061 0.6062

073091- 9 3.9536 288.44 46.53 3.189 0.8893 0.6021 0.6066 0.6067

073091- 10 3.9383 288.21 46.39 6.020 1.2171 0.8245 0.6049 0.6051 073091- 11 3.9334 288.08 46.35 6.018 1.2155 0.8238 0.6044 0.6046

073091 - 12 3.8491 287.44 45.47 13.185 1.7762 1.2069 0.6023 0.6027

073091- 13 3.9488 288.45 46.47 3.439 0.9205 0.6232 0.6049 0.6050

073091- 14 3.9811 288.17 46.90 5.925 1.2140 0.8221 0.6049 0.6051

Table 25. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, ITl at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density

(MPa) (K) (kg/m^)

Dif Press Flow Rate Pipe Re No. (kPa) (kg/s) (/10^)

061091- 1 3.8994 285.73 46.37 5.725 1.8954 1.2924 0.6050 0.6052

061091- 2 3.9053 285.46 46.49 5.662 1.8841 1.2855 0.6040 0.6041 061091- 3 3.9588 285.79 47.07 4.032 1.6009 1.0907 0.6044 0.6045

061091- 4 3.9579 285.33 47.14 4.040 1.6048 1.0946 0.6049 0.6050

061091- 5 3.8218 284.81 45.61 7.698 2.1710 1.4851 0.6026 0.6028

061091- 6 3.8203 284.46 45.65 7.533 2.1594 1.4784 0.6036 0.6038

061091- 7 3.9842 285.64 47.40 2.556 1.2790 0.8714 0.6044 0.6045 061091- 8 3.9832 285.49 47.41 2.577 1.2876 0.8776 0.6059 0.6060

071291- 1 3.9400 283.83 47.20 4.019 1.6024 1.0972 0.6052 0.6053

071291- 2 3.9390 283.81 47.19 4.006 1.5998 1.0954 0.6052 0.6053 071291- 3 3.8007 283.44 45.59 7.975 2.2124 1.5189 0.6034 0.6037

071291- 4 3.8001 283.33 45.60 7.844 2.1863 1.5013 0.6012 0.6014

071291- 5 3.8696 283.80 46.36 6.037 1.9423 1.3311 0.6039 0.6040

071291- 6 3.8698 284.01 46.32 6.036 1.9392 1.3283 0.6032 0.6033

071291- 7 3.9698 284.19 47.49 2.539 1.2808 0.8759 0.6067 0.6068

071291- 9 3.9628 285.16 47.23 2.606 1.2962 0.8844 0.6078 0.6078

071291- 10 3.8094 283.52 45.68 7.592 2.1613 1.4833 0.6036 0.6038

071291- 11 3.8123 283.87 45.66 7.473 2.1418 1.4686 0.6030 0.6032

Table 26. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, ITl at 15D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /xm Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

CY,

061091- 1 3.8994 285.73 46.37 5.740 1.8954 1.2924 0.6043 0.6044

061091- 2 3.9053 285.46 46.49 5.677 1.8841 1.2855 0.6032 0.6033

061091- 3 3.9588 285.79 47.07 4.044 1.6009 1.0907 0.6036 0.6037

061091- 4 3.9579 285.33 47.14 4.053 1.6048 1.0946 0.6039 0.6040

061091- 5 3.8218 284.81 45.61 7.727 2.1710 1.4851 0.6014 0.6016

061091- 6 3.8203 284.46 45.65 7.615 2.1594 1.4784 0.6023 0.6025

061091- 7 3.9842 285.64 47.40 2.556 1.2790 0.8714 0.6045 0.6045 061091- 8 3.9832 285.49 47.41 2.574 1.2876 0.8776 0.6063 0.6064

071291- 1 3.9400 283.83 47.20 4.027 1.6024 1.0972 0.6046 0.6047

071291- 2 3.9390 283.81 47.19 4.017 1.5998 1.0954 0.6044 0.6045

071291- 3 3.8007 283.44 45.59 7.997 2.2124 1.5189 0.6026 0.6028

071291- 4 3.8001 283.33 45.60 7.861 2.1863 1.5013 0.6005 0.6007

071291- 5 3.8696 283.80 46.36 6.050 1.9423 1.3311 0.6032 0.6034

071291- 6 3.8698 284.01 46.32 6.052 1.9392 1.3283 0.6024 0.6025

071291- 7 3.9698 284.19 47.49 2.540 1.2808 0.8759 0.6067 0.6067

071291- 9 3.9628 285.16 47.23 2.608 1.2962 0.8844 0.6075 0.6076

071291- 10 3.8094 283.52 45.68 7.621 2.1613 1.4833 0.6024 0.6026

071291- 11 3.8123 283.87 45.66 7.495 2.1418 1.4686 0.6022 0.6024

44
Table 27. Measured and calculated quantities for 0.67 beta ratio, elbow at 22D, IT1 at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 6.98A0 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

072591- 1 3.8877 286.76 46.05 4.146 1.6035 1.0908 0.6036 0.6037

072591- 2 3.9216 286.48 46.50 4.156 1.6197 1.1021 0.6060 0.6061 072591 - 3 3.7507 287.27 44.33 7.823 2.1533 1.4654 0.6013 0.6015

072591- 4 3.7488 286.73 44.40 7.775 2.1530 1.4672 0.6026 0.6028

072591- 5 3.9178 286.79 46.40 2.593 1.2762 0.8678 0.6052 0.6053

072591- 6 3.9184 287.49 46.28 2.618 1.2817 0.8701 0.6057 0.6057

072591- 7 3.8245 286.78 45.29 6.028 1.9124 1.3019 0.6019 0.6021 072591- 8 3.8467 286.31 45.64 6.012 1.9219 1.3095 0.6035 0.6036

072591- 9 3.8854 286.58 46.05 4.218 1.6211 1.1033 0.6050 0.6051 072691- 1 3.7971 286.34 45.04 5.967 1.8980 1.2938 0.6021 0.6023

072691- 2 3.8007 286.86 44.99 5.932 1.8889 1.2860 0.6013 0.6015 072691- 3 3.7223 286.81 44.07 8.082 2.1803 1.4859 0.6008 0.6010

072691- 4 3.7263 286.14 44.23 8.031 2.1732 1.4834 0.5996 0.5998

072691- 5 3.7288 287.16 44.09 8.128 2.1845 1.4874 0.6001 0.6003

072691 - 6 3.8553 287.13 45.59 4.217 1.6101 1.0948 0.6039 0.6040

072691 - 7 3.8560 286.65 45.69 4.230 1.6119 1.0972 0.6031 0.6032

072691- 8 3.9193 287.34 46.32 2.511 1.2561 0.8529 0.6058 0.6059

072691 - 9 3.9206 287.21 46.36 2.517 1.2565 0.8535 0.6050 0.6051

Table 28. Measured and calculated quantities for 0.67 beta ratio, elbow at 22D, ITl at 15D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2 (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

072591- 1 3.8877 286.76 46.05 4.146 1.6035 1.0908 0.6037 0.6038

072591- 2 3.9216 286.48 46.50 4.154 1.6197 1.1021 0.6062 0.6063

072591- 3 3.7507 287.27 44.33 7.795 2.1533 1.4654 0.6024 0.6026

072591- 4 3.7488 286.73 44.40 7.736 2.1530 1.4672 0.6041 0.6043

072591- 5 3.9178 286.79 46.40 2.582 1.2762 0.8678 0.6064 0.6065 072591- 6 3.9184 287.49 46.28 2.609 1.2817 0.8701 0.6067 0.6068

072591- 7 3.8245 286.78 45.29 6.010 1.9124 1.3019 0.6028 0.6030

072591- 8 3.8467 286.31 45.64 6.001 1.9219 1.3095 0.6040 0.6042

072591- 9 3.8854 286.58 46.05 4.215 1.6211 1.1033 0.6052 0.6053

072691 -

1 3.7971 286.34 45.04 5.949 1.8980 1.2938 0.6030 0.6032

072691- 2 3.8007 286.86 44.99 5.922 1.8889 1.2860 0.6018 0.6020

072691- 3 3.7223 286.81 44.07 8.054 2.1803 1.4859 0.6018 0.6020

072691- 4 3.7263 286.14 44.23 8.000 2.1732 1.4834 0.6008 0.6010

072691- 5 3.7288 287.16 44.09 8.098 2.1845 1.4874 0.6012 0.6014

072691- 6 3.8553 287.13 45.59 4.214 1.6101 1.0948 0.6042 0.6043

072691- 7 3.8560 286.65 45.69 4.224 1.6119 1.0972 0.6035 0.6036

072691- 8 3.9193 287.34 46.32 2.512 1.2561 0.8529 0.6057 0.6058

072691- 9 3.9206 287.21 46.36 2.513 1.2565 0.8535 0.6055 0.6056

Table 29. Measured and calculated quantities for 0.67 beta ratio, elbow at 34D, ITl at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter - 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

072991- 1 072991- 2 072991- 3 072991- 4 072991- 5 072991- 6 072991- 7 072991- 8 073091- 1 073091- 2 073091- 3 073091- 4 073091- 5 073091- 6 073091- 7 073091- 8

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s)

3.7765 3.7763

3.7165

3.7173 3.8602

3.8613

3.8933

3.8968

9310 9308

9799

9781 7873

7874 8313

8299

287.06

287.34

287.12 286.97

287.31 287.53 287.77

287.89

287.29

287.43

288.01 287.69

287.48

286.74 287.76

286.82

44.67

44.62

43.95 43.98

45.62 45.60

45.93

45.95 46.47

46.44

46.91 46.95 44.73 44.86

45.20

45.35

6.360 1.9522 6.353 1.9478

8.071 2.1792

8.034 2.1743 4.280 1.6230

4.311 1.6217 2.566 1.2620

2.581 1.2648

4.044 1.5937 4.040 1.5896 2.503 1.2637

2.504 1 . 2667

7.566 2.1298

7.491 2.1272 6.149 1.9317

6.134 1.9344

(/lO^)

^

1.3289 0.6023 0.6025

1.3249 0.6016 0.6018

1.4842 0.6017 0.6019

1.4814 0.6015 0.6017

1.1030 0.6041 0.6042

1.1015 0.6016 0.6017

0.8563 0.6047 0.6047

0.8580 0.6041 0.6041 1.0822 0.6047 0.6048

1.0791 0.6036 0.6037

0.8561 0.6066 0.6067

0.8588 0.6077 0.6077

1.4480 0.6020 0.6022

1.4489 0.6035 0.6037

1.3118 0.6025 0.6027

1.3167 0.6032 0.6034

45
Table 30. Measured and calculated quantities for 0.67 beta ratio, elbow at 34D, IT1 at 15D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m'') (kPa) (kg/s) (/10^)

072991- 1 3.7765 287.06 44.67 6.363 1.9522 1.3289 0.6022 0.6024

072991 - 2 3.7763 287.34 44.62 6.350 1.9478 1.3249 0.6018 0.6020

072991- 3 3.7165 287.12 43.95 8.060 2.1792 1.4842 0.6021 0.6023

072991- 4 3.7173 286.97 43.98 8.019 2.1743 1.4814 0.6020 0.6023

072991- 5 3.8602 287.31 45.62 4.274 1.6230 1.1030 0.6045 0.6046

072991- 6 3.8613 287.53 45.60 4.301 1.6217 1.1015 0.6023 0.6024

072991- 7 3.8933 287.77 45.93 2.555 1.2620 0.8563 0.6060 0.6060

072991- 8 3.8968 287.89 45.95 2.577 1.2648 0.8580 0.6046 0.6046

073091- 1 3.9310 287.29 46.47 4.052 1.5937 1.0822 0.6041 0.6042

073091- 2 3.9308 287.43 46.44 4.046 1.5896 1.0791 0.6031 0.6032

073091- 3 3.9799 288.01 46.91 2.502 1.2637 0.8561 0.6067 0.6067

073091- 4 3.9781 287.69 46.95 2.501 1.2667 0.8588 0.6080 0.6081 073091- 5 3.7873 287.48 44.73 7.559 2.1298 1.4480 0.6023 0.6025

073091- 6 3.7874 286.74 44.86 7.484 2.1272 1.4489 0.6038 0.6040

073091- 7 3.8313 287.76 45.20 6.151 1.9317 1.3118 0.6024 0.6026

073091- 8 3.8299 286.82 45.35 6.137 1.9344 1.3167 0.6031 0.6032

Table 31. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, IT! at 13D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m-^) (kPa) (kg/s) (/10^)

£,

071691- 1 3.7838 282.86 45.49 19.550 2.1599 1.4852 0.6012 0.6018

071691- 2 3.7848 283.51 45.39 19.359 2.1537 1.4786 0.6031 0.6037

071691- 3 3.9499 285.86 46.95 5.997 1.2210 0.8318 0.6045 0.6046

071691- 4 3.9501 285.03 47.10 5.939 1.2196 0.8325 0.6058 0.6059

071691- 5 3.8711 284.31 46.29 13.623 1.8216 1.2469 0.6024 0.6028

071691- 6 3.8695 283.91 46.34 13.499 1.8203 1.2472 0.6044 0.6048

071691- 7 4.0330 291.56 46.91 2.892 0.8517 0.5717 0.6074 0.6075

071691- 8 4.0237 292.47 46.64 2.916 0.8529 0.5714 0.6075 0.6076

071791- 1 3.8811 275.77 48.01 12.728 1.7942 1.2543 0.6029 0.6033

071791- 2 3.8811 273.04 48.55 12.573 1.7943 1.2630 0.6033 0.6037

071791- 3 3.9679 273.11 49.63 5.712 1.2254 0.8614 0.6048 0.6050

071791- 4 3.9706 273.04 49.67 5.738 1.2282 0.8635 0.6046 0.6038

071991- 1 3.7712 285.76 44.83 19.723 2.1497 1.4680 0.6000 0.6007

071991- 2 3.7650 285.47 44.81 19.518 2.1321 1.4571 0.5984 0.5990

071991- 3 3.9233 287.73 46.29 3.075 0.8693 0.5897 0.6054 0.6055

Table 32. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, ITl at 13D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 5.7142 cm (2.2497 in)

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

£>

071691- 1 3.7838 282.86 45.49 19.565 2.1599 1.4852 0.6010 0.6016

071691- 2 3.7848 283.51 45.39 19.364 2.1537 1.4786 0.6030 0.6036

071691- 3 3.9499 285.86 46.95 5.998 1.2210 0.8318 0.6044 0.6046

071691- 4 3.9501 285.03 47.10 5.942 1.2196 0.8325 0.6056 0.6058

071691- 5 3.8711 284.31 46.29 13.627 1.8216 1.2469 0.6023 0.6027

071691- 6 3.8695 283.91 46.34 13.514 1.8203 1.2472 0.6040 0.6044

071691- 7 4.0330 291.56 46.91 2.893 0.8517 0.5717 0.6073 0.6074

071691- 8 4.0237 292.47 46.64 2.914 0.8529 0.5714 0.6077 0.6078

071791- 1 3.8811 275.77 48.01 12.724 1.7942 1.2543 0.6030 0.6034

071791- 2 3.8811 273.04 48.55 12.587 1.7943 1.2630 0.6030 0.6034

071791- 3 3.9679 273.11 49.63 5.711 1.2254 0.8614 0.6049 0.6051 071791- 4 3.9706 273.04 49.67 5.737 1.2282 0.8635 0.6046 0.6048

071991- 1 3.7712 285.76 44.83 19.739 2.1497 1.4680 0.5998 0.6004

071991- 2 3.7650 285.47 44.81 19.530 2.1321 1.4571 0.5983 0.5989

071991- 3 3.9233 287.73 46.29 3.086 0.8693 0.5897 0.6044 0.6045

46
Table 33. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, IT1 at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ;im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

CY,

072391- 1 3.9063 286.82 46.26 13.674 1.8188 1.2369 0.6005 0.6009

072391- 2 3.9033 287.25 46.14 13.517 1.8144 1.2326 0.6032 0.6036

072391- 3 3.9852 287.08 47.15 6.335 1.2543 0.8516 0.6028 0.6030

072391- 4 3.9845 286.71 47.21 6.323 1.2594 0.8559 0.6055 0.6057

072391 - 5 3.8042 286.56 45.09 19.971 2.1674 1.4766 0.5995 0.6001 072391 - 6 3.8020 287.11 44.97 20.009 2.1716 1.4776 0.6009 0.6015

072391- 7 4.0061 287.21 47.37 3.086 0.8794 0.5967 0.6043 0.6044

072391- 8 4.0072 287.91 47.26 3.109 0.8814 0.5971 0.6041 0.6042

072391 - 9 4.0060 287.64 47.29 3.106 0.8820 0.5979 0.6046 0.6047

072491- 1 3.9210 287.82 46.25 6.193 1.2293 0.8338 0.6033 0.6035

072491- 2 3.9224 287.60 46.31 6.179 1.2273 0.8328 0.6026 0.6028

072491 - 3 3.7411 287.09 44.24 20.053 2.1509 1.4646 0.5993 0.6000

072491- 4 3.7414 286.71 44.31 19.793 2.1345 1.4548 0.5982 0.5988

072491- 5 3.8331 287.61 45.25 13.652 1 . 7969 1.2207 0.6003 0.6007

072491 - 6 3.8327 286.79 45.39 13.631 1 . 7978 1.2237 0.6001 0.6005

072491 - 7 3.9360 287.72 46.45 3.420 0.9157 0.6211 0.6036 0.6037

072491- 8 3.9381 287.89 46.44 3.417 0.9146 0.6201 0.6032 0.6033

Table 34. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, ITl at IID, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

072391 -

1 3.9063 286.82 46.26 13.698 1.8188 1.2369 0.5999 0.6004

072391 - 2 3.9033 287.25 46.14 13.535 1.8144 1.2326 0.6028 0.6032

072391- 3 3.9852 287.08 47.15 6.345 1.2543 0.8516 0.6024 0.6025

072391 - 4 3.9845 286.71 47.21 6.333 1.2594 0.8559 0.6050 0.6052

072391 - 5 3.8042 286.56 45.09 20.008 2.1674 1.4766 0.5990 0.5996

072391- 6 3.8020 287.11 44.97 20.036 2.1716 1.4776 0.6005 0.6011 072391- 7 4.0061 287.21 47.37 3.089 0.8794 0.5967 0.6040 0.6041 072391- 8 4.0072 287.91 47.26 3.120 0.8814 0.5971 0.6030 0.6031

072391 - 9 4.0060 287.64 47.29 3.117 0.8820 0.5979 0.6036 0.6037

072491- 1 3.9210 287.82 46.25 6.206 1.2293 0.8338 0.6027 0.6029

072491- 2 3.9224 287.60 46.31 6.195 1.2273 0.8328 0.6019 0.6020

072491- 3 3.7411 287.09 44.24 20.075 2.1509 1.4646 0.5990 0.5996

072491- 4 3.7414 286.71 44.31 19.824 2.1345 1.4548 0.5977 0.5984

072491- 5 3.8331 287.61 45.25 13.668 1 . 7969 1.2207 0.5999 0.6003

072491- 6 3.8327 286.79 45.39 13.650 1.7978 1.2237 0.5997 0.6001 072491 - 7 3.9360 287.72 46.45 3.427 0.9157 0.6211 0.6030 0.6031 072491 - 8 3.9381 287.89 46.44 3.423 0.9146 0.6201 0.6026 0.6028

Table 35. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, ITl at 13D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 lim Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)CY,

071691- 1 3.9484 283.22 47.42 2.569 1.2860 0.8817 0.6061 0.6062

071691- 2 3.9491 282.41 47.57 2.561 1.2868 0.8841 0.6065 0.6066

071691- 3 3.7710 279.56 45.93 8.125 2.2355 1.5502 0.6019 0.6021 071691- 4 3.7719 279.43 45.97 8.011 2.2156 1.5368 0.6006 0.6008

071691- 5 3.8468 280.76 46.64 6.240 1.9759 1.3647 0.6025 0.6026

071691- 6 3.8449 280.47 46.67 6.236 1.9710 1.3624 0.6010 0.6012

071691- 7 3.9100 284.31 46.75 4.159 1.6184 1.1073 0.6037 0.6038

071691- 8 3.9117 282.09 47.18 4.128 1.6162 1.1117 0.6025 0.6026

071991- 1 3.9300 287.20 46.47 4.147 1.6091 1.0929 0.6028 0.6029

071991- 2 3.9300 287.03 46.50 4.147 1.6099 1.0939 0.6030 0.6031 071991- 3 3.8639 285.99 45.90 5.977 1.9151 1.3056 0.6014 0.6015 071991- 4 3.8650 286.45 45.83 5.950 1.9096 1.3004 0.6014 0.6016

071991- 5 3.9687 287.03 46.96 2.649 1.2962 0.8803 0.6045 0.6046

071991- 6 3.9659 286.87 46.95 2.661 1.3074 0.8883 0.6084 0.6085

071991- 7 4.0010 286.89 47.37 2.681 1.3178 0.8950 0.6083 0.6084

071991- 8 3.7974 285.15 45.25 7.781 2.1688 1.4828 0.6011 0.6013

071991- 9 3.7961 286.49 45.00 7.706 2.1585 1.4709 0.6028 0.6030

071991- 10 3.9299 286.43 46.61 3.920 1.5743 1.0713 0.6058 0.6059

071991- 1 3.9849 286.83 47.19 2.690 1.3115 0.8910 0.6055 0.6056

071991- 2 3.9506 286.00 46.93 4.103 1.6095 1.0961 0.6033 0.6034 071991- 3 3.8746 286.96 45.86 6.204 1.9497 1.3259 0.6011 0.6013 071991- 4 3.8075 286.11 45.21 7.960 2.1925 1.4953 0.6010 0.6013

47
Table 36. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, IT1 at 13D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 6.98A0 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

^

071691- 1 3.9484 283.22 47.42 2.573 1.2860 0.8817 0.6057 0.6057

071691- 2 3.9491 282.41 47.57 2.565 1.2868 0.8841 0.6060 0.6060

071691- 3 3.7710 279.56 45.93 8.135 2.2355 1.5502 0.6015 0.6018

071691- 4 3.7719 279.43 45.97 8.022 2.2156 1.5368 0.6001 0.6004

071691- 5 3.8468 280.76 46.64 6.241 1.9759 1.3637 0.6024 0.6026

071691- 6 3.8449 280.47 46.67 6.237 1.9710 1.3624 0.6009 0.6011 071691- 7 3.9100 284.31 46.75 4.166 1.6184 1.1073 0.6032 0.6033

071691- 8 3.9117 282.09 47.18 4.135 1.6162 1.1117 0.6019 0.6020

071991- 1 3.9300 287.20 46.47 4.169 1.6091 1.0929 0.6013 0.6014

071991- 2 3.9300 287.03 46.50 4.170 1.6099 1.0939 0.6013 0.6014

071991- 3 3.8639 285.99 45.90 5.997 1.9151 1.3056 0.6003 0.6005

071991- 4 3.8650 286.45 45.83 5.971 1.9096 1.3004 0.6004 0.6005

071991- 5 3.9687 287.03 46.96 2.660 1.2962 0.8803 0.6032 0.6033

071991- 6 3.9659 286.87 46.95 2.679 1.3074 0.8883 0.6064 0.6064

071991- 7 4.0010 286.89 47.37 2.697 1.3178 0.8950 0.6065 0.6065 071991- 8 3.7974 285.15 45.25 7.815 2.1688 1.4828 0.5998 0.6000

071991- 9 3.7961 286.49 45.00 7.733 2.1585 1.4709 0.6017 0.6019

071991- 10 3.9299 286.43 46.61 3.952 1.5743 1.0713 0.6033 0.6034 071991- 1 3.9849 286.83 47.19 2.706 1.3115 0.8910 0.6037 0.6037

071991- 2 3.9506 286.00 46.93 4.134 1.6095 1.0961 0.6010 0.6011 071991- 3 3.8746 286.96 45.86 6.233 1.9497 1.3259 0.5998 0.5999

071991- 4 3.8075 286.11 45.21 7.976 2.1925 1.4953 0.6004 0.6007

Table 37. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, IT1 at IID, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

072391- 1 3.9610 286.66 46.94 4.080 1.6008 1.0883 0.6017 0.6018

072391- 2 3.9615 286.36 46.99 4.051 1.5981 1.0872 0.6024 0.6025

072391- 3 3.8311 285.81 45.54 7.915 2.1895 1.4940 0.5997 0.5999

072391- 4 3.8305 285.38 45.61 7.743 2.1665 1.4798 0.5996 0.5998

072391 - 5 3.9883 287.39 47.13 2.681 1.3025 0.8836 0.6027 0.6027

072391- 6 3.9889 287.07 47.19 2.716 1.3126 0.8911 0.6031 0.6032

072391- 7 3.8875 286.75 46.05 6.100 1.9348 1.3163 0.6004 0.6006

072391 - 8 3.8890 287.32 45.96 6.073 1.9282 1.3099 0.6002 0.6004

072491 -

1 3.8199 286.80 45.23 6.156 1.9272 1.3119 0.6006 0.6008

072491- 2 3.8211 287.22 45.18 6.131 1.9191 1.3051 0.5997 0.5999

072491 - 3 3.7459 287.12 44.30 8.062 2.1810 1.4849 0.6002 0.6004

072491- 4 3.7472 285.42 44.60 7.994 2.1765 1.4879 0.5994 0.5996

072491- 5 3.8835 287.27 45.91 4.143 1.5969 1.0850 0.6022 0.6023

072491- 6 3.8825 287.09 45.92 4.159 1.5974 1.0858 0.6011 0.6012

072491- 7 3.9218 287.43 46.33 2.679 1.2946 0.8789 0.6044 0.6045

072491- 8 3.9202 287.25 46.34 2.682 1.2936 0.8786 0.6036 0.6036

Table 38. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, IT1 at 11D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /tm Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Ra' (MPa) (K) (kg/m^) (kPa) (kg/s)

072391 - 1 3.9610 286.66 46.94 4.101 1.6008

072391- 2 3.9615 286.36 46.99 4.078 1.5981 072391- 3 3.8311 285.81 45.54 7.941 2.1895

072391- 4 3.8305 285.38 45.61 7.772 2.1665

072391- 5 3.9883 287.39 47.13 2.690 1.3025 072391- 6 3.9889 287.07 47.19 2.726 1.3126

072391 - 7 3.8875 286.75 46.05 6.134 1.9348 072391- 8 3.8890 287.32 45.96 6.098 1.9282 072491- 1 3.8199 286.80 45.23 6.180 1.9272 072491- 2 3.8211 287.22 45.18 6.147 1.9191 072491- 3 3.7459 287.12 44.30 8.091 2.1810

072491- 4 3.7472 285.42 44.60 8.012 2.1765

072491- 5 3.8835 287.27 45.91 4.159 1.5969

072491- 6 3.8825 287.09 45.92 4.174 1.5974 072491- 7 3.9218 287.43 46.33 2.686 1.2946 072491- 8 3.9202 287.25 46.34 2.685 1 . 2936

Pipe Re No. (/lO^)CY,

1 .0883 0.6001 0.6002

1 .0872 0.6004 0.6005

1 .4940 0.5988 0.5990

1 .4798 0.5985 0.5987

.8836 0.6018 0.6018

.8911 0.6020 0.6021

1 .3163 0.5987 0.5989

1 .3099 0.5990 0.5991

1 .3119 0.5994 0.5996

1 .3051 0.5989 0.5991

1 .4849 0.5991 0.5993

1 .4879 0.5987 0.5989

1 .0850 0.6011 0.6012

1 .0858 0.6001 0.6002

.8789 0.6036 0.6037

.8786 0.6032 0.6032

48
Table 39. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, IT1 at 15D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. a.

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

&

061191- 1 3.9426 284.94 47.03 3.327 1.8218 1.2440 0.6010 0.6011 061191- 2 3.9490 285.55 46.99 3.331 1.8254 1.2445 0.6020 0.6021 061191- 3 3.8258 284.89 45.64 5.098 2.2208 1.5188 0.6008 0.6009

061191- 4 3.8240 284.62 45.66 5.050 2.2098 1.5123 0.6005 0.6006

061191- 5 3.9577 286.21 46.98 2.649 1.6316 1.1105 0.6035 0.6036

061191- 6 3.9721 286.09 47.17 2.684 1.6404 1.1166 0.6016 0.6017

061191- 7 3.8723 284.21 46.32 4.201 2.0359 1.3938 0.6023 0.6024

061191- 8 3.8693 285.29 46.09 4.197 2.0312 1.3870 0.6027 0.6028

071291- 1 3.9033 284.87 46.57 3.194 1.7843 1.2192 0.6037 0.6038

071291- 2 3.9041 284.52 46.64 3.173 1.7795 1.2169 0.6036 0.6037

071291- 3 3.8311 283.82 45.89 4.462 2.0868 1.4308 0.6017 0.6019

071291- 4 3.8347 282.87 46.11 4.396 2.0760 1.4266 0.6018 0.6019

071291- 5 3.9286 283.34 47.16 2.582 1.6152 1.1074 0.6041 0.6041 071291- 6 3.9295 283.71 47.10 2.600 1.6188 1.1089 0.6037 0.6038

071291- 7 3.7868 282.64 45.57 5.133 2.2307 1.5347 0.6019 0.6020

071291- 8 3.7929 281.91 45.77 5.025 2.2172 1.5281 0.6033 0.6034

Table 40. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, ITl at 15D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density

(MPa)

061191- 1 3.9426

061191- 2 3.9490

061191- 3 3.8258

061191- 4 3.8240

061191- 5 3.9577

061191- 6 3.9721 061191- 7 3.8723

061191- 8 3.8693

071291- 1 3.9033

071291- 2 3.9041 071291- 3 3.8311 071291- 4 3.8347

071291- 5 3.9286

071291- 6 3.9295

071291- 7 3.7868

071291- 8 3.7929

(K)

284.94

285.55 284.89

284.62

286.21 286.09

284.21 285.29 284.87

284.52

283.82 282.87

283.34

283.71 282.64

281.91

(kg/m-")

47.03 46.99

45.64 45.66

46.98 47.17

46.32 46.09 46.57

46.64 45.89

46.11 47.16

47.10 45.57

45.77

f Press Flow Rate Pipe Re No. C CY2

(kPa) (kg/s) (/lO^)

3.348 1.8218 1.2440 0.5991 0.5992 3.346 1.8254 1.2445 0.6007 0.6008

5.126 2.2208 1.5188 0.5991 . 5993 5.074 2.2098 1.5123 0.5991 0.5992 2.656 1.6316 1.1105 0.6028 0.6028

2.691 1.6404 1.1166 0.6008 0.6009

4.220 2.0359 1.3938 0.6010 0.6011 4.219 2.0312 1.3870 0.6011 0.6012 3.207 1.7843 1.2192 0.6026 0.6026

3.185 1.7795 1.2169 0.6025 0.6026

4.471 2.0868 1.4306 0.6012 0.6013 4.409 2.0760 1.4266 0.6009 0.6010

2.585 1.6152 1.1074 0.6038 0.6039

2.606 1.6188 1.1089 0.6030 0.6031 5.154 2.2307 1.5347 0.6006 0.6008

5.051 2.2172 1.5281 0.6018 0.6019

Table 41. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, ITl at 13D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

^

071691- 1 3.9361 283.42 47.23 2.640 1.6313 1.1181 0.6029 0.6030

071691- 2 3.9337 283.18 47.24 2.637 1.6283 1.1168 0.6021 0.6021 071691- 3 3.8412 283.31 46.11 4.274 2.0434 1.4027 0.6007 0.6008

071691- 4 3.8379 282.21 46.26 4.175 2.0177 1.3888 0.5992 0.5993

071691- 5 3.8849 283.63 46.57 3.339 1.8194 1.2472 0.6021 0.6022

071691- 6 3.8838 283.77 46.54 3.359 1 .8202 1.2473 0.6008 0.6009

071691- 7 3.7856 282.40 45.60 5.134 2.2261 1.5325 0.6004 0.6005 071691- 8 3.7818 282.46 45.54 5.074 2.2054 1.5181 0.5987 0.5988

071991- 1 3.9617 286.83 46.91 2.545 1.5920 1.0818 0.6012 0.6012

071991- 2 3.9605 286.52 46.95 2.537 1.5939 1.0840 0.6026 0.6026

071991- 3 3.9227 286.16 46.57 3.163 1.7669 1.2032 0.6008 0.6008

071991- 4 3.9226 285.94 46.61 3.152 1.7660 1.2032 0.6013 0.6014

071991- 5 3.8690 285.91 45.97 4.131 2.0023 1.3653 0.5996 0.5997

071991- 6 3.8684 285.43 46.05 4.104 1.9982 1.3641 0.5998 . 5999

071991- 7 3.8014 285.74 45.20 5.259 2.2356 1.5262 0.5983 0.5984

071991- 8 3.8050 285.11 45.35 5.168 2.2269 1.5225 0.6002 0.6003

49
Table 42. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, IT1 at 13D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID

071691- 1 071691- 2 071691- 3 071691- 4 071691- 5 071691- 6 071691- 7 071691- 8 071991- 1 071991- 2 071991- 3 071991- 4 071991- 5 071991- 6 071991- 7 071991- 8

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C (MPa)

3.9361 3.9337

3.8412 3.8379

3.8849

3.8838

3.7856

.7818 .9617

.9605 .9227

.9226 3.8690

3.8684

3.8014

3.8050

(K)

283.42 283.18

283.31

282.21 283.63

283.77

282.40

282.46

286.83 286.52 286.16

285.94

285.91 285.43

285.74

285 . 1

(kgV)

47.23

47.24

46.11 46.26 46.57

46.54 45.60

45.54

46.91 46.95 46.57

46.61 45.97

46.05 45.20

45.35

(kPa) (kg/s)

2.647 1.6313 2.643 1.6283 4.294 2.0434

4.191 2.0177

3.353 1.8194 3.373 1.8202 5.143 2.2261 5.090 2.2054 2.569 1.5920 2.560 1.5939

3.195 1.7669 3.183 1.7660 4.170 2.0023

4.141 1.9982 5.288 2.2356

5.200 2.2269

1.1181 1.1168

1.4027

1.3888

1.2472 1.2473

1.5325

1.5181 1.0818

1.0840

1.2032

1.2032

1.3653

1.3641 1.5262

1.5225

0.6022

0.6014

0.5993

0.5980 0.6009

0.5996

0.5999

0.5978

. 5984 0.5999

0.5978

0.5983 0.5968

0.5971 0.5967

0.5984

CY,

0.6022

0.6014

0.5994

0.5981 0.6009

0.5997

0.6000 0.5979

0.5984 0.6000 0.5979

0.5984 0.5969

0.5972 0.5968

0.5985

Table 43. Measured and calculated quantities for 0.73 beta ratio, elbow at 170, IT1 at 11D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 (im Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID

072391- 1 072391- 2 072391- 3 072391- 4 072391- 5 072391- 6 072391- 7 072391- S

072491- 1 072491- 4 072491- 5 072491- 7 072491- 8 072491- 9 072491- 10 072491- 11 072491- 12 072491- 13 072491- 14 072491 15 072491- 16

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C (MPa)

3.9142 3.9147

3.9619

3.9609

3.8260

3.8243

3.8671 3.8664 3.8602

3.8563

3.8962

3.7605 3.7602 3.7969

3.7978 3.7939

3.7918

3.8789

3.8889 3.8597

3.8555

(K)

286.87

286.78

286.39

287.48

285.72 287.16

286.46

285.70 287.38

287.32

287.44 286.68

287.02 286.96

287.39

285.99

286.82

287.14 287.14

287.11 286.71

(kg/m'')

46.34 46.36

46.99

46.79

45.49

45.22 45.85 45.98

45.61 45.58

46.02

44.55 44.48

44.93 44.87

45.06 44.89

45.87

45.99

45.65 45.67

(kPa) (kg/s)

3.412 1.8232 3.399 1.8291 2.544 1.5847

2.554 1.5886 4.987 2.1783 4.977 2.1788 4.228 2.0153 4.219 2.0260 3.307 1.7841 3.265 1.7773 2.547 1.5746

4.981 2.1581 4.977 2.1644

4.325 2.0206

4.318 2.0274 4.297 2.0201 4.303 2.0181 2.622 1.5958 2.648 1.6035

3.251 1.7701 3.221 1 . 7648

1.2395 1.2438

1.0780 1.0778 1.4867

1.4819

1.3723

1.3821 1.2123 1.2079

1.0693 1.4706 1.4737

1.3754 1.3786

1.3783

1.3742 1.0847

1.0898

1.2035 1.2012

0.5983

0.6012

0.5981 0.5997

0.5968

0.5992

0.5973

0.6002

0.5994

0.6013 0.6002

0.5978

0.6002

0.5981 0.6010

0.5990

0.5991 0.6005 0.5996

0.5996

0.6004

CY,

0.5983

0.6013

0.5982 0.5997

0.5969

0.5994 0.5973

0.6003

0.5995 0.6013

0.6002

0.5980

0.6003

0.5982

0.6011

0.5991 0.5992

0.6005 0.5996

0.5997

0.6005

Table 44. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, IT1 at 11D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 inn Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (tC) (kg/m^) (kPa) (kg/s) (/10^)

072391- 1 3.9142 286.87 46.34 3.439 1.8232 1.2395 0.5959 0.5960

072391 - 2 3.9147 286.78 46.36 3.421 1.8291 1.2438 0.5993 0.5994

072391 3 3.9619 286.39 46.99 2.555 1.5847 1.0780 0.5968 0.5968

072391- 4 3.9609 287.48 46.79 2.571 1.5886 1.0778 0.5977 0.5978

072391- 5 3.8260 285 . 72 45.49 5.014 2.1783 1 .4867 0.5951 0.5952

072391- 6 3.8243 287.16 45.22 5.012 2.1788 1.4819 0.5972 0.5973

072391 - 7 3.8671 286.46 45.85 4.252 2.0153 1.3723 0.5956 0.5957

072391- 8 3.8664 285 . 70 45.98 4.246 2.0260 1.3821 0.5983 0.5984

072491- 1 3.8602 287.38 45.61 3.325 1.7841 1.2123 0.5978 0.5979

072491- 4 3.8563 287.32 45.58 3.282 1.7773 1.2079 0.5997 0.5998

072491- 5 3.8962 287.44 46.02 2.555 1.5746 1.0693 0.5992 0.5992

072491- 7 3.7605 286.68 44.55 4.999 2.1581 1.4706 0.5967 0.5968

072491- 8 3.7602 287.02 44.48 4.996 2.1644 1.4737 0.5990 0.5992

072491 9 3.7969 286.96 44.93 4.340 2.0206 1.3754 0.5971 0.5972

072491 10 3.7978 287.39 44.87 4.338 2.0274 1.3786 0.5996 0.5997

072491 11 3.7939 285.99 45.06 4.316 2.0201 1.3783 0.5977 0.5978

072491 12 3.7918 286.82 44.89 4.320 2.0181 1.3742 0.5979 0.5980

072491 13 3.8789 287.14 45.87 2.627 1.5958 1.0847 0.5999 0.6000

072491- 14 3.8889 287.14 45.99 2.655 1.6035 1.0898 0.5988 0.5988

072491 15 3.8597 287.11 45.65 3.267 1.7701 1.2035 0.5981 0.5982

072491 16 3.8555 286.71 45.67 3.237 1.7648 1.2012 0.5990 0.5990

50
Table 45. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

061291- 1 3.9029 285.23 46.50 13.355 1.8076 1.2340 0.6023 0.6027

061291- 2 3.9027 285.16 46.51 13.318 1.8068 1.2337 0.6028 0.6032

061291- 1 4.0063 286.69 47.47 2.971 0.8641 0.5871 0.6046 0.6047

061291- 2 4.0045 286.68 47.45 2.954 0.8615 0.5853 0.6046 0.6047

061291- 3 3.7715 285.14 44.94 21.547 2.2565 1.5433 0.6018 0.6025 061291- 4 3.7732 284.75 45.03 21.277 2.2446 1.5366 0.6019 0.6025 061291- 5 3.9631 285.37 47.20 6.598 1.2812 0.8737 0.6031 0.6033

061291- 6 3.9593 285.54 47.12 6.773 1.2974 . 8844 0.6033 0.6035

061291- 7 3.9717 286.17 47.15 6.754 1.3024 0.8864 0.6062 0.6064

061291- 8 3.7987 285.12 45.27 6.030 1.2000 0.8205 0.6033 0.6035

061291- 9 3.9574 286.07 47.00 2.854 0.8433 0.5741 0.6049 0.6050

061391- 1 4.0134 285.75 47.73 6.254 1.2548 0.8544 0.6033 0.6035 061391- 2 4.0135 285.72 47.74 6.259 1.2563 0.8555 0.6037 0.6039

061391- 4 3.7819 286.11 44.90 19.599 2.1435 1.4623 0.5998 0.6004

061391- 5 3.7838 285.02 45.11 19.490 2.1445 1.4669 0.6003 0.6009

061391- 6 3.8766 285.73 46.10 13.151 1.7839 1.2168 0.6016 0.6020

061391- 7 3.8738 285.46 46.11 13.174 1.7846 1.2181 0.6012 0.6016

061391- 8 4.0172 286.41 47.65 3.097 0.8852 0.6018 0.6055 0.6056

061391- 9 4.0267 286.73 47.70 3.096 0.8867 0.6023 0.6062 0.6063

Table 46. Measured and calculated quantities for 0.55 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 iim Orifice Diameter = 5.7142 cm (2.2497 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

061291- 1 3.9029 285.23 46.50 13.347 1.8076 1.2340 0.6025 0.6029

061291- 2 3.9027 285.16 46.51 13.317 1.8068 1.2337 0.6028 0.6032

061291- 1 4.0063 286.69 47.47 2.966 0.8641 0.5871 0.6051 0.6052

061291- 2 4.0045 286.68 47.45 2.948 0.8615 0.5853 0.6053 0.6054

061291- 3 3.7715 285.14 44.94 21.548 2.2565 1.5433 0.6018 0.6025

061291- 4 3.7732 284.75 45.03 21.271 2.2446 1.5366 0.6020 0.6026

061291- 5 3.9631 285.37 47.20 6.582 1.2812 0.8737 0.6038 0.6040

061291- 6 3.9593 285.54 47.12 6.767 1.2974 0.8844 0.6036 0.6038

061291- 7 3.9717 286.17 47.15 6.740 1.3024 0.8864 0.6068 0.6070

061291- 8 3.7987 285.12 45.27 6.017 1.2000 0.8205 0.6039 0.6041 061291- 9 3.9574 286.07 47.00 2.846 0.8433 0.5741 0.6057 0.6058

061391- 1 4.0134 285.75 47.73 6.250 1.2548 0.8544 0.6035 0.6037

061391- 2 4.0135 285.72 47.74 6.257 1.2563 0.8555 0.6039 0.6041 061391- 4 3.7819 286.11 44.90 19.590 2.1435 1.4623 0.5999 0.6005 061391- 5 3.7838 285.02 45.11 19.484 2.1445 1.4669 0.6004 0.6010 061391- 6 3.8766 285.73 46.10 13.147 1.7839 1.2168 0.6017 0.6021 061391- 7 3.8738 285.46 46.11 13.174 1 . 7846 1.2181 0.6012 0.6017

061391- 8 4.0172 286.41 47.65 3.106 0.8852 0.6018 0.6046 0.6047

061391- 9 4.0267 286.73 47.70 3.102 0.8867 0.6023 0.6057 0.6057

Table 47. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

t061291- 1 3.9659 285.31 47.24 4.185 1.6306 1.1121 0.6032 0.6033 061291- 2 3.9601 285.38 47.16 4.204 1.6313 1.1125 0.6026 0.6027

061291- 4 3.8851 284.42 46.43 6.157 1.9513 1.3350 0.6003 0.6004

061291- 5 3.8798 284.31 46.39 6.135 1.9476 1.3330 0.6005 0.6006

061291- 6 3.9863 285.58 47.43 2.695 1.3127 0.8945 0.6039 0.6040

061291- 7 3.9839 285.48 47.42 2.722 1.3176 0.8980 0.6032 0.6032

061291- 8 3.8242 285.03 45.59 7.601 2.1451 1.4666 0.5993 0.5995

061291- 9 3.8076 285.48 45.32 8.010 2.1973 1.5009 0.5998 0.6000

51
Table 48. Measured and calculated quantities for 0.67 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /im Orifice Diameter = 6.9840 cm (2.7496 in)

Run ID Pressure Temperature Dens it; (MPa) (K) (kg/m^

061291- 1 3.9659 285.31 47.24

061291- 2 3.9601 285.38 47.16

061291- 4 3.8851 284.42 46.43

061291- 5 3.8798 284.31 46.39

061291- 6 3.9863 285.58 47.43

061291- 7 3.9839 285.48 47.42

061291- 8 3.8242 285.03 45.59

061291- 9 3.8076 285.48 45.32

Dif Press Flow Rate Pipe Re No. (kPa) (kg/s)

4.174 1.6306 4.195 1.6313 6.139 1.9513

6.121 1.9476 2.688 1.3127 2.713 1.3176

7.571 2.1451 7.983 2.1973

CY, (/lO^)

£.

1.1121 0.6040 0.6041 1.1125 0.6033 0.6034

1.3350 0.6011 0.6013

1.3330 0.6011 0.6013

0.8945 0.6047 0.6048

0.8980 0.6042 0.6043

1.4666 0.6004 0.6006

1.5009 0.6008 0.6010

Table 49. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position A.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ]im Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2 (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

061191- 1 3.8651 286.21 45.88 4.247 2.0269 1.3811 0.5992 0.5993

061191- 2 3.8629 286.13 45.86 4.196 2.0134 1.3722 0.5989 0.5990

061191- 3 3.9410 285.74 46.86 2.661 1.6228 1.1059 0.5997 0.5998

061191- 4 3.9411 285.79 46.86 2.689 1.6329 1.1127 0.6004 0.6004

061191- 5 3.8105 285.98 45.26 5.232 2.2357 1.5252 0.5995 0.5996

061191- 6 3.7969 285.36 45.21 5.144 2.2088 1.5094 0.5977 0.5978

061191- 7 3.8986 285.60 46.38 3.351 1.8078 1.2331 0.5984 0.5985

061191- 8 3.8980 285.71 46.36 3.377 1.8158 1.2382 0.5989 0.5990

061191- 9 3.7909 284.24 45.33 5.142 2.2144 1.5174 0.5985 0.5986

Table 50. Measured and calculated quantities for 0.73 beta ratio, elbow at 17D, Zanker at 16D, flange taps at position C.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 am Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

£.

061191- 1 3.8651 286.21 45.88 4.226 2.0269 1.3811 0.6007 0.6008

061191- 2 3.8629 286.13 45.86 4.177 2.0134 1.3722 0.6003 0.6004

061191- 3 3.9410 285.74 46.86 2.647 1.6228 1.1059 0.6012 0.6013

061191- 4 3.9411 285.79 46.86 2.672 1.6329 1.1127 0.6022 0.6023

061191- 5 3.8105 285.98 45.26 5.218 2.2357 1.5252 0.6003 0.6004

061191- 6 3.7969 285.36 45.21 5.120 2.2088 1.5094 0.5991 0.5992

061191- 7 3.8986 285.60 46.38 3.343 1.8078 1.2331 0.5991 0.5992

061191- 8 3.8980 285.71 46.36 3.363 1.8158 1.2382 0.6001 0.6002

061191- 9 3.7909 284.24 45.33 5.119 2.2144 1.5174 0.5998 0.6000

Table 51. Measured and calculated quantities for 0.54 beta ratio, oversize Sprenkle at 44D, flange taps at position A.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 >tm Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)CY,

102291- 1 4.0411 288.49 47.55 9.902 0.3955 0.5280 0.6062 0.6065

102291- 2 4.0408 288.46 47.56 9.892 0.3948 0.5271 0.6055 0.6058

102291- 3 3.9806 288.07 46.91 57.814 0.9567 1.2795 0.6095 0.6113

102291- 4 3.9776 288.01 46.89 58.333 0.9602 1.2844 0.6092 0.6110

102291- 5 3.8349 287.46 45.30 42.171 0.7989 1.0719 0.6069 0.6083

102291- 6 3.8357 287.61 45.28 41.913 0.7965 1.0683 0.6071 0.6084

102291- 7 3.8922 287.96 45.89 25.402 0.6229 0.8341 0.6063 0.6071 102291- 9 3.8088 287.29 45.02 59.325 0.9461 1.2703 0.6073 0.6092

102291- 10 3.8110 287.63 44.98 58.740 0.9420 1.2638 0.6080 0.6098

102391- 1 3.8399 288.17 45.23 57.929 0.9332 1.2499 0.6048 0.6067

102391- 2 3.8380 288.21 45.20 61.285 0.9610 1.2870 0.6057 0.6076

102391- 3 3.8202 287.96 45.04 21.472 0.5662 0.7589 0.6052 0.6059

102391- 4 3.8211 288.07 45.03 21.640 0.5685 0.7617 0.6053 0.6060

102391- 5 3.7783 287.87 44.56 36.953 0.7398 0.9922 0.6055 0.6067

102391- 6 3.7778 287.36 44.64 36.838 0.7394 0.9929 0.6056 0.6068

102391- 7 3.8908 288.34 45.80 10.219 0.3937 0.5267 0.6052 0.6055

102391- 8 3.8940 288.34 45.84 10.198 0.3936 0.5266 0.6054 0.6057

52
Table 52. Measured and calculated quantities for 0.54 beta ratio, oversize Sprenkle at 44D, flange taps at position

Pipe Diameter = 5.250 cm (2.067 in), 4.1 iim Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Oif Press Flow Rate Pipe Re No. C (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)CY,

102291- 1 4.0411 288.49 47.55 9.901 0.3955 0.5280 0.6062 0.6065

102291- 2 4.0408 288.46 47.56 9.888 0.3948 0.5271 0.6056 0.6059

102291- 3 3.9806 288.07 46.91 57.775 0.9567 1.2795 0.6097 0.6115

102291- 4 3.9776 288.01 46.89 58.312 0.9602 1.2844 0.6093 0.6111

102291- 5 3.8349 287.46 45.30 42.185 0.7989 1.0719 0.6068 0.6082

102291- 6 3.8357 287.61 45.28 41.917 0.7965 1.0683 0.6071 0.6084

102291- 7 3.8922 287.96 45.89 25.407 0.6229 0.8341 0.6062 0.6070

102291- 9 3.8088 287.29 45.02 59.301 0.9461 1.2703 0.6074 0.6094

102291- 10 3.8110 287.63 44.98 58.723 0.9420 1.2638 0.6081 0.6099

102391- 1 3.8399 288.17 45.23 57.905 0.9332 1.2499 0.6050 0.6068

102391- 2 3.8380 288.21 45.20 61.254 0.9610 1.2870 0.6058 0.6078

102391- 3 3.8202 287.96 45.04 21.471 0.5662 0.7589 0.6052 0.6059

102391- 4 3.8211 288.07 45.03 21.637 0.5685 0.7617 0.6053 0.6060

102391- 5 3.7783 287.87 44.56 36.959 0.7398 0.9922 0.6055 0.6067

102391- 6 3.7778 287.36 44.64 36.853 0.7394 0.9929 0.6054 0.6066

102391- 7 3.8908 288.34 45.80 10.219 0.3937 0.5267 0.6052 0.6055

102391- 8 3.8940 288.34 45.84 10.198 0.3936 0.5266 0.6054 0.6057

Table 53. Measured and calculated quantities for 0.54 beta ratio, oversize Sprenkle at 44D, flange taps at position C.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 iim Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

i.

102291- 1 4.0411 288.49 47.55 9.910 0.3955 0.5280 0.6060 0.6063

102291- 2 4.0408 288.46 47.56 9.900 0.3948 0.5271 0.6052 0.6055

102291- 3 3.9806 288.07 46.91 57.788 0.9567 1.2795 0.6097 0.6115

102291- 4 3.9776 288.01 46.89 58.324 0.9602 1.2844 0.6092 0.6110

102291- 5 3.8349 287.46 45.30 42.196 0.7989 1.0719 0.6068 0.6081 102291- 6 3.8357 287.61 45.28 41.925 0.7965 1.0683 0.6070 0.6083

102291- 7 3.8922 287.96 45.89 25.413 0.6229 0.8341 0.6062 0.6070

102291- 9 3.8088 287.29 45.02 59.302 0.9461 1.2703 0.6074 0.6093

102291- 10 3.8110 287.63 44.98 58.704 0.9420 1.2638 0.6081 0.6100

102391- 1 3.8399 288.17 45.23 57.868 0.9332 1.2499 0.6051 0.6070

102391- 2 3.8380 288.21 45.20 61.216 0.9610 1.2870 0.6060 0.6079

102391- 3 3.8202 287.96 45.04 21.471 0.5662 0.7589 0.6053 0.6059

102391- 4 3.8211 288.07 45.03 21.645 0.5685 0.7617 0.6052 0.6059

102391- 5 3.7783 287.87 44.56 36.965 0.7398 0.9922 0.6054 0.6066

102391- 6 3.7778 287.36 44.64 36.843 0.7394 0.9929 0.6055 0.6067

102391- 7 3.8908 288.34 45.80 10.227 0.3937 0.5267 0.6049 0.6053

102391- 8 3.8940 288.34 45.84 10.206 0.3936 0.5266 0.6052 0.6055

Table 54. Measured and calculated quantities for 0.54 beta ratio, oversize Sprenkle at 44D, flange taps at position D.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 /im Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density

(MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

102291- 4.0411 288.49 47.55 9.917 0.3955 0.5280 0.6057 0.6060

102291- 4.0408 288.46 47.56 9.908 0.3948 0.5271 0.6050 0.6053

102291- 3.9806 288.07 46.91 57.818 0.9567 1.2795 0.6095 0.6113

102291- 3.9776 288.01 46.89 58.354 0.9602 1.2844 0.6091 0.6109

102291- 3.8349 287.46 45.30 42.224 0.7989 1.0719 0.6066 0.6079

102291- 3.8357 287.61 45.28 41.953 0.7965 1.0683 0.6068 0.6081 102291- 3.8922 287.96 45.89 25.432 0.6229 0.8341 0.6059 0.6067

102291- 3.8088 287.29 45.02 59.346 0.9461 1.2703 0.6072 0.6091 102291- 10 3.8110 287.63 44.98 58.750 0.9420 1.2638 0.6079 0.6098

102391- 3.8399 288.17 45.23 57.918 0.9332 1.2499 0.6049 0.6067

102391- 3.8380 288.21 45.20 61.279 0.9610 1.2870 0.6057 0.6076

102391- 3.8202 287.96 45.04 21.491 0.5662 0.7589 0.6050 0.6057

102391- 3.8211 288.07 45.03 21.660 0.5685 0.7617 0.6050 0.6057

102391- 3.7783 287.87 44.56 36.988 0.7398 0.9922 0.6052 0.6064

102391- 6 3.7778 287.36 44.64 36.877 0.7394 0.9929 0.6052 0.6064

102391- 7 3.8908 288.34 45.80 10.232 0.3937 0.5267 0.6048 0.6051

102391- 8 3.8940 288.34 45.84 10.210 0.3936 0.5266 0.6051 0.6054

53
Table 55. Measured and calculated quantities for 0.67 beta ratio, oversize Sprenkle at 440, flange taps at position A.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 /im Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Densi ty Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

102291- 1 4.0092 288.08 47.25 26.154 1.0296 1.3764 0.6121 0.6128

102291- 2 4.0107 288.44 47.20 26.124 1.0279 1.3729 0.6118 0.6125

102291- 3 3.9643 287.64 46.80 41.964 1.2958 1.7351 0.6107 0.6118

102291- 4 3.9550 287.43 46.73 41.820 1.2949 1.7350 0.6118 0.6130

102291- 5 3.9851 287.89 47.00 8.767 0.5903 0.7898 0.6083 0.6085

102291- 6 3.9861 288.10 46.97 8.802 0.5925 0.7922 0.6094 0.6096

102291- 7 3.9008 287.76 46.02 58.379 1.5125 2.0262 0.6089 0.6105

102291- 8 3.9037 287.47 46.11 57.784 1.5088 2.0226 0.6100 0.6116

102391- 1 3.8741 288.10 45.65 8.706 0.5797 0.7762 0.6082 0.6084

102391- 2 3.8741 288.21 45.63 8.683 0.5790 0.7751 0.6084 0.6086

102391- 3 3.8386 287.61 45.31 36.721 1.1933 1.6004 0.6111 0.6121

102391- 4 3.8411 288.02 45.27 36.148 1.1831 1.5851 0.6109 0.6119

102391- 5 3.8202 287.66 45.09 18.329 0.8373 1.1230 0.6089 0.6094

102391- 6 3.8200 287.37 45.14 18.391 0.8385 1.1255 0.6085 0.6090

102391- 7 3.7803 287.77 44.60 57.248 1.4757 1.9798 0.6095 0.6111

102391- 8 3.7858 287.42 44.72 56.793 1.4715 1.9757 0.6094 0.6110

Table 56. Measured and calculated quantities for 0.67 beta ratio, oversize Sprenkle at 44D, flange taps at position

Pipe Diameter = 5.250 cm (2.067 in), 4.1 /im Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

£.

102291- 1 4.0092 288.08 47.25 26.156 1.0296 1.3764 0.6121 0.6128

102291- 2 4.0107 288.44 47.20 26.127 1.0279 1.3729 0.6117 0.6124

102291- 3 3.9643 287.64 46.80 41.955 1.2958 1.7351 0.6108 0.6119

102291- 4 3.9550 287.43 46.73 41.838 1.2949 1.7350 0.6117 0.6128

102291- 5 3.9851 287.89 47.00 8.762 0.5903 0.7898 0.6085 0.6087

102291- 6 3.9861 288.10 46.97 8.795 0.5925 0.7922 0.6097 0.6099

102291- 7 3.9008 287.76 46.02 58.352 1.5125 2.0262 0.6091 0.6107

102291- 8 3.9037 287.47 46.11 57.765 1.5088 2.0226 0.6101 0.6117

102391- 1 3.8741 288.10 45.65 8.678 0.5797 0.7762 0.6092 0.6094

102391- 2 3.8741 288.21 45.63 8.657 0.5790 0.7751 0.6093 0.6096

102391- 3 3.8386 287.61 45.31 36.646 1.1933 1.6004 0.6117 0.6127

102391- 4 3.8411 288.02 45.27 36.085 1.1831 1.5851 0.6115 0.6125

102391- 5 3.8202 287.66 45.09 18.289 0.8373 1.1230 0.6096 0.6101

102391- 6 3.8200 287.37 45.14 18.345 0.8385 1.1255 0.6092 0.6098

102391- 7 3.7803 287.77 44.60 57.105 1.4757 1.9798 0.6103 0.6119

102391- 8 3.7858 287.42 44.72 56.667 1.4715 1.9757 0.6100 0.6116

Table 57. Measured and calculated quantities for 0.67 beta ratio, oversize Sprenkle at 44D, flange taps at position C.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 ^m Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

£,

102291- 1 4.0092 288.08 47.25 26.181 1.0296 1.3764 0.6118 0.6125

102291- 2 4.0107 288.44 47.20 26.150 1.0279 1.3729 0.6115 0.6122

102291- 3 3.9643 287.64 46.80 42.007 1.2958 1.7351 0.6104 0.6115

102291- 4 3.9550 287.43 46.73 41.866 1 . 2949 1.7350 0.6115 0.6126

102291- 5 3.9851 287.89 47.00 8.781 0.5903 0.7898 0.6078 0.6080

102291- 6 3.9861 288.10 46.97 8.816 0.5925 0.7922 0.6089 0.6092

102291- 7 3.9008 287.76 46.02 58.377 1.5125 2.0262 0.6090 0.6106

102291- 8 3.9037 287.47 46.11 57.784 1.5088 2.0226 0.6100 0.6116

102391- 1 3.8741 288.10 45.65 8.701 0.5797 0.7762 0.6083 0.6086

102391- 2 3.8741 288.21 45.63 8.679 0.5790 0.7751 0.6085 0.6088

102391- 3 3.8386 287.61 45.31 36.674 1.1933 1.6004 0.6115 0.6125

102391- 4 3.8411 288.02 45.27 36.120 1.1831 1.5851 0.6112 0.6122

102391- 5 3.8202 287.66 45.09 18.307 0.8373 1.1230 0.6093 0.6098

102391- 6 3.8200 287.37 45.14 18.374 0.8385 1.1255 0.6088 0.6093

102391- 7 3.7803 287.77 44.60 57.125 1.4757 1.9798 0.6102 0.6118

102391- 8 3.7858 287.42 44.72 56.696 1.4715 1.9757 0.6099 0.6115

54
Table 58. Measured and calculated quantities for 0.67 beta ratio, oversize Sprenkle at 44D, flange taps at position D.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 iim Orifice Diameter = 3.4933 cm (1.3753 in)

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

£.

102291- 1 4.0092 288.08 47.25 26.216 1.0296 1.3764 0.6114 0.6121 102291- 2 4.0107 288.44 47.20 26.189 1.0279 1.3729 0.6110 0.6117

102291- 3 3.9643 287.64 46.80 42.046 1.2958 1.7351 0.6101 0.6112

102291- 4 3.9550 287.43 46.73 41.905 1.2949 1.7350 0.6112 0.6123

102291- 5 3.9851 287.89 47.00 8.790 0.5903 0.7898 0.6075 0.6077

102291- 6 3.9861 288.10 46.97 8.827 0.5925 0.7922 0.6086 0.6088

102291- 7 3.9008 287.76 46.02 58.415 1.5125 2.0262 0.6088 0.6104

102291- 8 3.9037 287.47 46.11 57.816 1.5088 2.0226 0.6098 0.6114

102391- 1 3.8741 288.10 45.65 8.732 0.5797 0.7762 0.6073 0.6075

102391- 2 3.8741 288.21 45.63 8.712 0.5790 0.7751 0.6074 0.6076

102391- 3 3.8386 287.61 45.31 36.803 1.1933 1.6004 0.6104 0.6114

102391- 4 3.8411 288.02 45.27 36.231 1.1831 1.5851 0.6102 0.6112

102391- 5 3.8202 287.66 45.09 18.372 0.8373 1.1230 0.6082 0.6087

102391- 6 3.8200 287.37 45.14 18.442 0.8385 1.1255 0.6076 0.6082

102391- 7 3.7803 287.77 44.60 57.329 1.4757 1.9798 0.6091 0.6107

102391- 8 3.7858 287.42 44.72 56.879 1.4715 1.9757 0.6089 0.6105

Table 59. Measured and calculated quantities for 0.54 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position A.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 ton Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(MPa) (K) (kg/m-^) (kPa) (kg/s) (/lO^)

102491- 1 3.9350 288.14 46.36 59.145 0.9580 1.2816 0.6069 . 6088

102591- 1 3.9477 288.22 46.50 59.985 0.9637 1 . 2889 0.6054 0.6072

102591- 2 3.8904 287.26 45.99 36.137 0.7427 0.9963 0.6051 0.6062

102591- 3 3.8904 287.77 45.90 36.213 0.7428 0.9952 0.6051 0.6062

102591- 4 3.9546 287.81 46.65 9.921 0.3912 0.5236 0.6047 0.6050

102591- 5 3.9542 287.93 46.63 10.018 0.3929 0.5257 0.6046 0.6049

102591- 6 3.9357 287.91 46.41 21.463 0.5745 . 7690 0.6050 0.6057

102591- 7 3.9352 287.65 46.45 21.482 0.5750 0.7701 0.6050 0.6057

102591- 1 3.9145 287.44 46.24 21.428 0.5726 0.7675 0.6046 0.6053

102591- 2 3.9135 287.49 46.22 21.527 0.5736 0.7689 0.6045 0.6052

102591- 3 3.8688 287.87 45.63 35.913 0.7372 0.9878 0.6049 0.6060

102591- 4 3.8697 287.61 45.68 35.630 0.7348 0.9851 0.6049 0.6061

102591- 5 3.9648 287.88 46.76 10.276 0.3987 0.5336 0.6050 0.6053

102591- 6 3.9657 287.91 46.77 10.348 0.3998 0.5350 0.6045 0.6049

102591- 7 3.9101 287.64 46.16 61.584 0.9777 1.3100 0.6084 0.6103

102591- 8 3.9092 287.59 46.15 60.250 0.9671 1.2960 0.6084 0.6103

Table 60. Measured and calculated quantities for 0.54 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position

Pipe Diameter = 5.250 cm (2.067 in), 4.1 /im Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Densi ty Dif Press Flow Ra Pipe Re No. C CY, (MPa) (K) (kg/m^) (kPa) (kg/s)

102491- 1 3.9350 288.14 46.36 59.135 0.9580

102591- 1 3.9477 288.22 46.50 60.023 0.9637

102591- 2 3.8904 287.26 45.99 36.168 0.7427

102591- 3 3.8904 287.77 45.90 36.244 0.7428

102591- 4 3.9546 287.81 46.65 9.923 0.3912

102591- 5 3.9542 287.93 46.63 10.023 0.3929

102591- 6 3.9357 287.91 46.41 21.474 0.5745

102591- 7 3.9352 287.65 46.45 21.492 0.5750

102591- 1 3.9145 287.44 46.24 21.438 0.5726

102591- 2 3.9135 287.49 46.22 21.527 0.5736

102591- 3 3.8688 287.87 45.63 35.937 0.7372

102591- 4 3.8697 287.61 45.68 35.653 0.7348

102591- 5 3.9648 287.88 46.76 10.279 0.3987

102591- 6 3.9657 287.91 46.77 10.351 0.3998

102591- 7 3.9101 287.64 46.16 61.614 0.9777

102591- 8 3.9092 287.59 46.15 60.267 0.9671

1.2816 0.6070 0.6088

1 . 2889 0.6052 0.6070

0.9963 0.6048 0.6060

0.9952 0.6049 0.6060

0.5236 0.6046 0.6050

0.5257 0.6044 0.6047

0.7690 0.6049 0.6055

0.7701 0.6049 0.6055

0.7675 0.6045 0.6051 0.7689 0.6045 0.6052

0.9878 0.6047 0.6058

0.9851 0.6047 0.6059

0.5336 0.6049 0.6052

0.5350 0.6044 0.6048

1.3100 0.6082 0.6101

1.2960 0.6083 0.6102

55
Table 61. Measured and calculated quantities for 0.54 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position C.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 iim Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(HPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

102491- 1 3.9350 288.14 46.36 59.177 0.9580 1.2816 0.6068 0.6086

102591- 1 3.9477 288.22 46.50 60.025 0.9637 1.2889 0.6052 0.6070

102591- 2 3.8904 287.26 45.99 36.195 0.7427 0.9963 0.6046 0.6057

102591- 3 3.8904 287.77 45.90 36.263 0.7428 0.9952 0.6047 0.6058

102591- i, 3.9546 287.81 46.65 9.930 0.3912 0.5236 0.6045 0.6048

102591- 5 3.9542 287.93 46.63 10.029 0.3929 0.5257 0.6043 0.6046

102591- 6 3.9357 287.91 46.41 21.494 0.5745 0.7690 0.6046 0.6052

102591- 7 3.9352 287.65 46.45 21.508 0.5750 0.7701 0.6047 0.6053

102591- 1 3.9145 287.44 46.24 21.465 0.5726 0.7675 0.6041 0.6047

102591- 2 3.9135 287.49 46.22 21.549 0.5736 0.7689 0.6042 0.6049

102591- 3 3.8688 287.87 45.63 35.972 0.7372 0.9878 0.6044 0.6055

102591- 4 3.8697 287.61 45.68 35.698 0.7348 0.9851 0.6044 0.6055

102591- 5 3.9648 287.88 46.76 10.284 0.3987 0.5336 0.6047 0.6050

102591- 6 3.9657 287.91 46.77 10.357 0.3998 0.5350 0.6043 0.6046

102591- 7 3.9101 287.64 46.16 61.622 0.9777 1.3100 0.6082 0.6101 102591- 8 3.9092 287.59 46.15 60.304 0.9671 1.2960 0.6082 0.6100

Table 62. Measured and calculated quantities for 0.54 beta ratio plate, elbow at 170, 1T3 at 12D, flange taps at position D.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 ^m Orifice Diameter = 2.8588 cm (1.1255 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

^

102491- 1 3.9350 288.14 46.36 59.223 0.9580 1.2816 0.6065 0.6084

102591- 1 3.9477 288.22 46.50 60.086 0.9637 1.2889 0.6049 0.6067

102591- 2 3.8904 287.26 45.99 36.228 0.7427 0.9963 0.6043 0.6055

102591- 3 3.8904 287.77 45.90 36.312 0.7428 0.9952 0.6043 0.6054

102591- 4 3.9546 287.81 46.65 9.940 0.3912 0.5236 0.6041 0.6044

102591- 5 3.9542 287.93 46.63 10.038 0.3929 0.5257 0.6040 0.6043

102591- 6 3.9357 287.91 46.41 21.519 0.5745 0.7690 0.6042 0.6049

102591- 7 3.9352 287.65 46.45 21.542 0.5750 0.7701 0.6042 0.6048

102591- 1 3.9145 287.44 46.24 21.485 0.5726 0.7675 0.6038 0.6045

102591- 2 3.9135 287.49 46.22 21.575 0.5736 0.7689 0.6038 0.6045

102591- 3 3.8688 287.87 45.63 36.001 0.7372 0.9878 0.6042 0.6053

102591- 4 3.8697 287.61 45.68 35.715 0.7348 0.9851 0.6042 0.6053

102591- 5 3.9648 287.88 46.76 10.295 0.3987 0.5336 0.6044 0.6047

102591- 6 3.9657 287.91 46.77 10.366 0.3998 0.5350 0.6040 0.6043

102591- 7 3.9101 287.64 46.16 61.676 0.9777 1.3100 0.6079 0.6098

102591- 8 3.9092 287.59 46.15 60.354 0.9671 1.2960 0.6079 0.6098

Table 63. Measured and calculated quantities for 0.67 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position A.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 lim Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

^

102491- 1 3.9912 287.76 47.09 35.236 1.1883 1.5902 0.6094 0.6104

102491- 2 3.9950 287.31 47.22 35.130 1.1874 1.5907 0.6091 0.6101

102491- 3 3.9362 287.06 46.57 20.026 0.8905 1.1944 0.6096 0.6101

102491- 4 3.9359 287.33 46.52 20.124 0.8923 1.1961 0.6097 0.6102

102491- 5 3.9348 286.57 46.64 57.319 1.5061 2.0226 0.6080 0.6095

102491- 6 3.9333 286.74 46.59 56.961 1.4991 2.0124 0.6073 0.6089

102491- 7 4.0203 287.45 47.50 7.453 0.5467 0.7318 0.6078 0.6080

102491- 8 4.0211 287.63 47.47 7.556 0.5507 0.7369 0.6082 0.6084

102591- 1 3.9039 287.24 46.15 19.677 0.8765 1.1756 0.6080 0.6086

102591- 2 3.9042 287.22 46.16 19.598 0.8747 1.1733 0.6080 0.6085

102591- 3 3.9213 287.27 46.35 8.915 0.5903 0.7916 0.6074 0.6076

102591- 4 3.9224 287.53 46.32 8.987 0.5928 0.7943 0.6077 0.6079

102591- 5 3.9318 287.31 46.47 36.972 1.2117 1.6244 0.6107 0.6117

102591- 6 3.9245 287.80 46.30 36.855 1.2063 1.6154 0.6100 0.6111

102591- 7 3.8669 287.71 45.63 59.624 1.5214 2.0393 0.6087 0.6103

102591- 8 3.8642 287.43 45.65 59.118 1.5137 2.0304 0.6081 0.6097

56
Table 64. Measured and calculated quantities for 0.67 beta ratio plate, elbow at 170, IT3 at 12D, flange taps at positic

Pipe Diameter = 5.250 cm (2.067 in), 4.1 (im Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C CY2

(HPa) (K) (kg/m'^) (kPa) (kg/s) (/10^)

102491- 1 3.9912 287.76 47.09 35.215 1.1883 1.5902 0.6096 0.6106

102491- 2 3.9950 287.31 47.22 35.106 1.1874 1.5907 0.6093 0.6103

102491- 3 3.9362 287.06 46.57 20.013 0.8905 1.1944 0.6098 0.6103

102491- 4 3.9359 287.33 46.52 20.100 0.8923 1.1961 0.6100 0.6106

102491- 5 3.9348 286.57 46.64 57.264 1.5061 2.0226 0.6082 0.6098

102491- 6 3.9333 286.74 46.59 56.922 1.4991 2.0124 0.6075 0.6091

102491- 7 4.0203 287.45 47.50 7.432 0.5467 0.7318 0.6086 0.6088

102491- 8 4.0211 287.63 47.47 7.533 0.5507 0.7369 0.6091 0.6093

102591- 1 3.9039 287.24 46.15 19.682 0.8765 1.1756 0.6079 0.6085

102591- 2 3.9042 287.22 46.16 19.601 0.8747 1.1733 0.6080 0.6085

102591- 3 3.9213 287.27 46.35 8.901 0.5903 0.7916 0.6079 0.6081

102591- 4 3.9224 287.53 46.32 8.976 0.5928 0.7943 0.6080 0.6083

102591- 5 3.9318 287.31 46.47 36.989 1.2117 1.6244 0.6105 0.6115

102591- 6 3.9245 287.80 46.30 36.864 1.2063 1.6154 0.6100 0.6110

102591- 7 3.8669 287.71 45.63 59.600 1.5214 2.0393 0.6088 0.6104

102591- 8 3.8642 287.43 45.65 59.099 1.5137 2.0304 0.6082 0.6098

Table 65. Measured and calculated quantities f-or 0.67 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position C.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 fun Orifice Diameter = 3.4933 cm (1.3753 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. CY, (MPa) (K) (kg/m^) (kPa) (kg/s) (/10^)

t.

102491- 1 3.9912 287.76 47.09 35.337 1.1883 1.5902 0.6086 0.6095

102491- 2 3.9950 287.31 47.22 35.218 1.1874 1.5907 0.6083 0.6093

102491- 3 3.9362 287.06 46.57 20.085 0.8905 1.1944 0.6087 0.6093

102491- 4 3.9359 287.33 46.52 20.172 0.8923 1.1961 0.6090 0.6095

102491- 5 3.9348 286.57 46.64 57.411 1.5061 2.0226 0.6075 0.6090

102491- 6 3.9333 286.74 46.59 57.048 1.4991 2.0124 0.6069 0.6084

102491- 7 4.0203 287.45 47.50 7.473 0.5467 0.7318 0.6069 0.6071

102491- 8 4.0211 287.63 47.47 7.578 0.5507 0.7369 0.6073 0.6075

102591- 1 3.9039 287.24 46.15 19.720 0.8765 1.1756 0.6074 0.6079

102591- 2 3.9042 287.22 46.16 19.647 0.8747 1.1733 0.6072 0.6078

102591- 3 3.9213 287.27 46.35 8.926 0.5903 0.7916 0.6070 0.6072

102591- 4 3.9224 287.53 46.32 9.000 0.5928 . 7943 0.6072 0.6075

102591- 5 3.9318 287.31 46.47 37.053 1.2117 1.6244 0.6100 0.6110

102591- 6 3.9245 287.80 46.30 36.941 1.2063 1.6154 0.6093 0.6103

102591- 7 3.8669 287.71 45.63 59.742 1.5214 2.0393 0.6081 0.6097

102591- 8 3.8642 287.43 45.65 59.213 1.5137 2.0304 0.6076 0.6092

Table 66. Measured and calculated quantities for 0.67 beta ratio plate, elbow at 17D, IT3 at 12D, flange taps at position D.

Pipe Diameter = 5.250 cm (2.067 in), 4.1 (un Orifice Diameter = 3.4933 cm (1.3753 in)

Pressure Temperature Density Dif Press Flow Rate Pipe Re No. (MPa) (K) (kg/m^) (kPa) (kg/s) (/lO^)

102491- 1 3.9912 287.76 47.09 35.417 1.1883 1.5902 0.6079 0.6088

102491- 2 3.9950 287.31 47.22 35.299 1.1874 1.5907 0.6076 0.6086

102491- 3 3.9362 287.06 46.57 20.134 0.8905 1.1944 0.6080 0.6085

102491- 4 3.9359 287.33 46.52 20.222 0.8923 1.1961 0.6082 0.6088

102491- 5 3.9348 286.57 46.64 57.539 1.5061 2.0226 0.6068 0.6083

102491- 6 3.9333 286.74 46.59 57.176 1.4991 2.0124 0.6062 0.6077

102491- 7 4.0203 287.45 47.50 7.487 0.5467 0.7318 0.6064 0.6066

102491- 8 4.0211 287.63 47.47 7.593 0.5507 0.7369 0.6067 0.6069

102591- 1 3.9039 287.24 46.15 19.768 0.8765 1.1756 0.6066 0.6072

102591- 2 3.9042 287.22 46.16 19.689 0.8747 1.1733 0.6066 0.6071

102591- 3 3.9213 287.27 46.35 8.951 0.5903 0.7916 0.6062 0.6064

102591- 4 3.9224 287.53 46.32 9.026 0.5928 0.7943 0.6063 0.6066

102591- 5 3.9318 287.31 46.47 37.136 1.2117 1.6244 0.6093 0.6103

102591- 6 3.9245 287.80 46.30 37.024 1.2063 1.6154 0.6086 0.6097

102591- 7 3.8669 287.71 45.63 59.843 1.5214 2.0393 0.6075 0.6092

102591- 8 3.8642 287.43 45.65 59.338 1.5137 2.0304 0.6069 0.6086

57

*U.S. GOVERNMENT PRINTING OFFICE: 1993-77A-025/690A6



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