NisrUNITED STATES

DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS

AND TECHNOLOGY

NATU INST. OF STANO & TECH RT.C.

A111D3 7bDSbD

NIST

PUBLICATIONS

NIST Technical Note 1352

^3b

The Effects of Flow Conditioners and

Tap Location on Orifice Flowmeter

Performance

Jennifer L. Scott

Charles F. Sindt

Michael A. Lewis

James A. Brennan

Chemical Engineering Division

Chemical Science and Technology Laboratory

National Institute of Standards and Technology

Boulder, Colorado 80303-3328

\ s

^'S^TES O^

'^/

U.S. DEPARTMENT OF COMMERCE, Robert A. Mosbacher, Secretary

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY, John W. Lyons, Director

Issued October 1991
National Institute of Standards and Technology Technical Note 1352

Natl. Inst. Stand. Technol., Tech. Note 1352, 72 pages (Oct. 1991)

CODEN:NTNOEF

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1991

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

PAGE

ACKNOWLEDGEMENTS iv

CROSS-REFERENCE CHART V

LIST OF FIGURES vi

LIST OF TABLES X

ABSTRACT 1 INTRODUCTION 1 EXPERIMENTAL PROGRAM 3 TEST RESULTS 5 Alternate Flow Conditioners 5 In-line vs. Flanged Tube Bundle Flow Conditioners 6 Pressure Tap Location 7 Other Tube Bundle Flow Conditioners 8 CONCLUSIONS AND RECOMMENDATIONS 8 REFERENCES 10

111
ACKHOWLEDOEMEMTS

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

Chicago, Illinois, under GRI dbntract No. 5088-271-1680. This report is also

cited as GRI Report Number GRI-91/0229. 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)

.

IV
CROSS-REFERENCE CHART

Figure

No.

Beta Ratio Flow

Cond.

Table

No.

Test

Conf ig

Tap Location**

0.43 0.55 0.67 0.73 3:00 6:00 9:00 12:00

6 X ZAN 2 FIG. 3 X

7 X ZAN 3 FIG. 3 X

8 X ZAN 4 FIG. 3 X

9 X ZAN 5 FIG. 3 X

10 X X X X ZAN SUMM. FIG. 3 X

11 X ETl 6 FIG. 3 X

12 X ETl 7 FIG. 3 X

13 X ETl 8 FIG. 3 X

14 X ETl 9 FIG. 3 X

15 X X X X ETl SUMM. FIG. 3 X

16 X FT6 10 FIG. 3 X

17 X FT6 11 FIG. 3 X

18 X FT6 12 FIG. 3 X

19 X FT6 13 FIG. 3 X

20 X X X

• X FT6 SUMM. FIG. 3 X

21 X FTl 14 FIG. 3 X

22 X FTl 15 FIG. 3 X

23 X FTl 16 FIG. 3 X

24 X FTl 17 FIG. 3 X

25 X X X X FTl SUMM. FIG. 3 X

26 X FTl 18 FIG. 4 X

27 X FTl 19 FIG. 4 X

28 X FTl 20 FIG. 4 X

29 X FTl 21 FIG. 4 X

30 X X X X FTl SUMM. FIG. 4 X

31 X ITl 22 FIG. 4 X

32 X ITl 23 FIG. 4 X

33 X ITl 24 FIG. 4 X

34 X ITl 25 FIG. 4 X

35 X X X X ITl SUMM. FIG. 4 X

36 X 26,27 FIG. 4 X X

37 X 28,29 FIG. 4 X X

38 X 30,31 FIG. 4 X X

39 X 32,33 FIG. 4 X X

40 X ITl 34,35 FIG. 4 X X

41 X ITl 36,37 FIG. 4 X X

42 X ITl 38,39 FIG. 4 X X

43 X ITl 40,41 FIG. 4 X X

44 X FT2 42,43 FIG. 4 X X

45 X FT2 44,45 FIG. 4 X X

46 X FT4 46,47 FIG. 4 X X

47 X FT4 48,49 FIG. 4 X X

*See Table 1 for details

**As seen when looking downstream
LIST OF FIGURES

PAGE

Figure 1. In-line, tube bundle flow conditioner. 11

Figure 2a. Zanker flow conditioner. 11

Figure 2b. Etoile flow conditioner. 12

Figure 2c. Flanged, 7 tube bundle flow conditioner. 12

Figure 2d. Flanged, 19 tube bundle flow conditioner (round) . 13

Figure 2e. Flanged, 19 tube bundle flow conditioner (hexagonal). 13

Figure 3 . Test configuration with a tee 19 pipe diameters upstream of 14

the orifice plate.

Figure 4. Test conf igiiration with a tee 17 pipe diameters upstream of 14

the orifice plate.

Figure 5a. Four-inch orifice meter, 56 pipe diameters of straight pipe. 15

Figure 5b. Four-inch orifice meter, 6-inch Sprenkle at 46 pipe 15

diameters.

Figure 5c. Four-inch orifice meter, 4 6 pipe diameters of straight pipe. 15

Figure 6. Discharge coefficient vs. Reynolds number for the 0.4 3 beta 16

ratio plate with a tee at 19D and a Zanker flow conditioner

at lOD.

Figure 7. Discharge coefficient vs. Reynolds number for the 0.55 beta 16

ratio plate with a tee at 19D and a Zanker flow conditioner

at lOD.

Figure 8. Discharge coefficient vs. Reynolds number for the 0.67 beta 17

ratio plate with a tee at 19D and a Zanker flow conditioner

at lOD.

Figure 9. Discharge coefficient vs. Reynolds number for the 0.73 beta 17

ratio plate with a tee at 19D and a Zanker flow conditioner

at lOD.

Figure 10. Percent change in discharge coefficient vs. beta ratio with 18

a Zanker flow conditioner at lOD and a tee at 19D.

Figure 11. Discharge coefficient vs. Reynolds number for the 0.43 beta 18

ratio plate with a tee at 19D and an etoile flow conditioner

at IID.

Figure 12. Discharge coefficient vs. Reynolds number for the 0.55 beta 19

ratio plate with a tee at 19D and an etoile flow conditioner

at IID.

Figure 13. Discharge coefficient vs. Reynolds number for the 0.67 beta 19

ratio plate with a tee at 19D and an etoile flow conditioner

at IID.

Figure 14. Discharge coefficient vs. Reynolds number for the 0.73 beta 2 ratio plate with a tee at 19D and an etoile flow conditioner

at llD.
LIST OF FIGURES (continued)

PAGE

Figure 15. Percent change in discharge coefficient vs. beta ratio with 2 an etoile flow conditioner at IID and a tee at 19D.

Figure 16. Discharge coefficient vs. Reynolds number for the 0.4 3 beta 21

ratio plate with a tee at 19D and a flanged, 7 tube bundle

flow conditioner at IID.

Figure 17. Discharge coefficient vs. Reynolds number for the 0.55 beta 21

ratio plate with a tee at 19D and a flanged, 7 tube bundle

flow conditioner at IID.

Figure 18. Discharge coefficient vs. Reynolds number for the 0.67 beta 22

ratio plate with a tee at 19D and a flanged, 7 tube bundle

flow conditioner at IID.

Figure 19. Discharge coefficient vs. Reynolds number for the 0.73 beta 22

ratio plate with a tee at 19D and a flanged, 7 tube bundle

flow conditioner at IID.

Figure 20. Percent change in discharge coefficient vs. beta ratio with 23

a flanged, 7 tube flow conditioner at IID and a tee at 19D.

Figure 21. Discharge coefficient vs. Reynolds number for the 0.4 3 beta 2 3 ratio plate with a tee at 19D and a flanged, 19 tube bundle

flow conditioner at IID.

Figure 22. Discharge coefficient vs. Reynolds number for the 0.55 beta 24

ratio plate with a tee at 19D and a flanged, 19 tube bundle

flow conditioner at IID.

Figure 23. Discharge coefficient vs. Reynolds number for the 0.67 beta 24

ratio plate with a tee at 19D and a flanged, 19 tube bundle

flow conditioner at IID.

Figure 24. Discharge coefficient vs. Reynolds number for the 0.73 beta 25

ratio plate with a tee at 19D and a flanged, 19 tube bundle

flow conditioner at IID.

Figure 25. Percent change in discharge coefficient vs. beta ratio with 25

a flanged, 19 tube flow conditioner at IID and a tee at 19D.

Figure 26. Discharge coefficient vs. Reynolds number for the 0.43 beta 26

ratio plate with a tee at 17D and a flanged, 19 tube bundle

flow conditioner at the outlet of the tee.

Figure 27. Discharge coefficient vs. Reynolds number for the 0.55 beta 26

ratio plate with a tee at 17D and a flanged, 19 tube bundle

flow conditioner at the outlet of the tee.

Figure 28. Discharge coefficient vs. Reynolds number for the 0.67 beta 27

ratio plate with a tee at 17D and a flanged, 19 tube bundle

flow conditioner at the outlet of the tee.

Figure 29. Discharge coefficient vs. Reynolds number for the 0.73 beta 27

ratio plate with a tee at 17D and a flanged, 19 tube bundle

flow conditioner at the outlet of the tee.

Figure 30. Percent change in discharge coefficient vs. beta ratio with 28

a tee at 17D and a flanged, 19 tube bundle flow conditioner

at the outlet of the tee.
LIST OF FIGURES (continued)

Figure 31.

Figure 32.

Figure 33.

Figure 34.

Figure 35.

Figure 36.

Figure 37.

Figure 38.

Figure 39.

Figure 40.

Figure 41.

Figure 42.

Figure 43.

Figure 44.

PAGE

Discharge coefficient vs. Reynolds nuinber for the 0.43 beta 28

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

flow conditioner at the outlet of the tee.

Discharge coefficient vs. Reynolds number for the 0.55 beta

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

flow conditioner at the outlet of the tee.

Discharge coefficient vs. Reynolds nuinber for the 0.73 beta

ratio plate with a tee at 17D, no flow conditioner, and

flange pressure taps at 3 and 9 o'clock.

Discharge coefficient vs. Reynolds nuinber for the 0.73 beta

ratio plate with a tee at 17D, a flanged, 19 tube bundle flow

conditioner (hex) at the tee outlet, and flange pressure taps

at 3 and 9 o'clock.

29

Discharge coefficient vs. Reynolds nuinber for the 0.67 beta 29

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

flow conditioner at the outlet of the tee.

Discharge coefficient vs. Reynolds nuinber for the 0.73 beta 30

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

flow conditioner at the outlet of the tee.

Percent change in discharge coefficient vs. beta ratio with 3 a tee at 17D and an in-line, 19 tube bundle flow conditioner

at the outlet of the tee.

31

Discharge coefficient vs. Reynolds nuinber for the 0.73 beta 31

ratio plate with a tee at 17D, no flow conditioner, and

flange pressure taps at 6 and 12 o'clock.

Discharge coefficient vs. Reynolds nuinber for the 0.43 beta 3 2 ratio plate with a tee at 17D, no flow conditioner, and

flange pressure taps at 3 and 9 o'clock.

Discharge coefficient vs. Reynolds nuinber for the 0.4 3 beta 3 2 ratio plate with a tee at 17D, no flow conditioner, and

flange pressure taps at 6 and 12 o'clock.

Discharge coefficient vs. Reynolds number for the 0.7 3 beta 3 3 ratio plate with a tee at 17D, an in-line, 19 tube bundle

flow conditioner at the tee outlet, and flange pressure taps

at 3 and 9 o'clock.

Discharge coefficient vs. Reynolds number for the 0.73 beta 33

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

flow conditioner at the tee outlet, and flange pressure taps

at 6 and 12 o'clockDischarge coefficient vs. Reynolds nuinber for the 0.43 beta 34

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

flow conditioner at the tee outlet, and flange pressure taps

at 3 and 9 o'clock.

Discharge coefficient vs. Reynolds number for the 0.43 beta 34

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

flow conditioner at the tee outlet, and flange pressure taps

at 6 and 12 o'clock.

35
LIST OF FIGURES (continued)

PAGE

Figure 45. Discharge coefficient vs. Reynolds number for the 0.4 3 beta

ratio plate with a tee at 17D, a flanged, 19 tube bundle flow

conditioner (hex) at the tee outlet, and flange pressure taps

at 3 and 9 o'clock.

35

Figure 46. Discharge coefficient vs. Reynolds number for the 0.73 beta 36

ratio plate with a tee at 17D, a flanged, 19 tube bundle flow

conditioner (round) at the tee outlet, and flange pressure

taps at 3 and 9 o'clock.

Figure 47. Discharge coefficient vs. Reynolds number for the 0.43 beta 36

ratio plate with a tee at 17D, a flanged, 19 tube bundle flow

conditioner (round) at the tee outlet, and flange pressure

taps at 3 and 9 o'clock.
LIST OF TABLES

PAGE

Table 1. Flow conditioner codes, descriptions, and measurements. 3 Table 2. Measured and calculated quantities for 0.4 3 beta ratio, tee 37

at 19D, ZAN at lOD.

Table 3. Measured and calculated quantities for 0.55 beta ratio, tee 37

at 19D, ZAN at lOD.

Table 4. Measured and calculated quantities for 0.67 beta ratio, tee 38

at 19D, ZAN at lOD.

Table 5. Measured and calculated quantities for 0.73 beta ratio, tee 38

at 19D, ZAN at lOD.

Table 6. Measured and calculated quantities for 0.4 3 beta ratio, tee 39

at 19D, ETl at IID.

Table 7. Measured and calculated quantities for 0.55 beta ratio, tee 39

at 19D, ETl at IID.

Table 8. Measured and calculated quantities for 0.67 beta ratio, tee 40

at 19D, ETl at IID.

Table 9. Measured and calculated quantities for 0.73 beta ratio, tee 40

at 19D, ETl at IID.

Table 10. Measured and calculated quantities for 0.43 beta ratio, tee 41

at 19D, FT6 at IID.

Table 11. Measured and calculated quantities for 0.55 beta ratio, tee 41

at 19D, FT6 at IID.

Table 12. Measured and calculated quantities for 0.67 beta ratio, tee 42

at 19D, FT6 at IID.

Table 13. Measured and calculated quantities for 0.73 beta ratio, tee 42

at 19D, FT6 at IID.

Table 14. Measured and calculated quantities for 0.43 beta ratio, tee 43

at 19D, FTl at IID.

Table 15. Measured and calculated quantities for 0.55 beta ratio, tee 43

at 19D, FTl at IID.

Table 16. Measured and calculated quantities for 0.67 beta ratio, tee 44

at 19D, FTl at IID.

Table 17. Measured and calculated quantities for 0.73 beta ratio, tee 44

at 19D, FTl at IID.

Table 18. Measured and calculated quantities for 0.43 beta ratio, tee 45

at 17D, FTl at 15D.

Table 19. Measured and calculated quantities for 0.55 beta ratio, tee 45

at 17D, FTl at 15D.

Table 20. Measured and calculated quantities for 0.67 beta ratio, tee 46

at 17D, FTl at 15D.

Table 21. Measured and calculated quantities for 0.73 beta ratio, tee 46

at 17D, FTl at 15D.
LIST OF TABLES (continued)

Table 22.

Table 23.

Table 24.

Table 25.

Table 26.

Table 27.

Table 28.

Table 29.

Table 30.

Table 31.

Table 32.

Table 33.

Table 34.

Table 35.

Table 36.

Table 37.

Table 38.

Table 39.

Table 40.

Table 41.

Table 42.

Measured and calculated quantities for 0.4 3 beta ratio

at 17D, ITl at 15D.

Measured and calculated quantities for 0.55 beta ratio

at 17D, ITl at 15D.

Measured and calculated quantities for 0.67 beta ratio

at 17D, ITl at 15D.

Measured and calculated quantities for 0.73 beta ratio

at 17D, ITl at 15D.

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

Measured and calculated quantities for 0. at 17D, no flow conditioner, flange taps

,73 beta ratio

at 3:00.

,73 beta ratio

at 9:00.

,73 beta ratio

at 6:00.

,73 beta ratio

at 12:00.

.43 beta ratio

at 3:00.

,43 beta ratio

at 9:00.

,43 beta ratio

at 6:00.

,43 beta ratio

at 12:00.

Measured and calculated quantities for 0.73 beta ratio

at 17D, ITl at 15D, flange taps at 3:00.

Measured and calculated quantities for 0,

at 17D, ITl at 15D, flange taps at 9:00.

Measured and calculated quantities for 0. at 17D, ITl at 15D, flange taps at 6:00.

Measured and calculated quantities for 0. at 17D, ITl at 15D, flange taps at 12:00.

Measured and calculated quantities for 0. at 17D, ITl at 15D, flange taps at 3:00.

73 beta ratio

73 beta ratio

73 beta ratio

4 3 beta ratio

Measured and calculated quantities for 0.43 beta ratio

at 17D, ITl at 15D, flange taps at 9:00.

Measured and calculated quantities for 0.4 3 beta ratio

at 17D, ITl at 15D, flange taps at 6:00.

Measured and calculated quantities for 0.43 beta ratio

at 17D, ITl at 15D, flange taps at 12:00.

Measured and calculated quantities for 0.73 beta ratio

at 17D, FT2 at 15D, flange taps at 3:00.

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

tee

PAGE

47

47

48

48

48

49

49

49

50

50

50

51

51

51

52

52

52

53

53

53

54

XI
LIST OF TABLES (continued)

Table 43. Measured and calculated quantities

at 17D, FT2 at 15D, flange taps at

Table 44. Measured and calculated quantities

at 17D, FT2 at 15D, flange taps at

Table 45. Measured and calculated quantities

at 17D, FT2 at 15D, flange taps at

Table 46. Measured and calculated quantities

at 17D, FT4 at 15D, flange taps at

Table 47. Measured and calculated quantities

at 17D, FT4 at 15D, flange taps at

Table 48. Measured and calculated quantities

at 17D, FT4 at 15D, flange taps at

Table 49. Measured and calculated quantities

at 17D, FT4 at 15D, flange taps at

PAGE

for 0,.73 beta ratio. tee 54

9:00.

for 0..43 beta ratio, tee 55

3:00.

for 0,.43 beta ratio. tee 55

9:00.

for 0.,73 beta ratio. tee 56

3:00.

for 0,,73 beta ratio. tee 56

9:00.

for 0.,43 beta ratio. tee 57

3:00.

for 0..43 beta ratio. tee 57

9:00.

Xll
THE EFFECTS OF FLOW CONDITIONERS AND TAP LOCATION

ON ORIFICE FLOWMETER PERFORMANCE

ABSTRACT

Current research is being conducted to provide information which will be used to improve

the existing industry standards for proper installation of orifice meters. This research includes

experimental investigation of a Zanker, an etoile, and several tube bundle flow conditioners at various positions relative to the orifice plate. Also included are the effects of pressure tap

location, both with and without flow conditioning, as reflected in determination of discharge

coefficients

.

Of the flow conditioners tested at approximately 11 pipe diameters upstream of the orifice

plate, the Zanker flow conditioner resulted in discharge coefficients most similar to baseline

values. There was only a slight difference in orifice meter performance when a flanged or an inline tube bundle flow conditioner was used at the tested location upstream of the orifice plate.

The effect of pressure tap location was found to be significant with the 0.73 beta ratio plate.

Recommendations for future research, as a result of these findings, are included.

Key words: discharge coefficient; etoile; flow conditioner; flow disturbance; flow measurement;

gas; orifice flowmeter; tap location; tube bundle; Zanker

INTRODUCTION

In recent years, much research has been devoted to improving flow

measurement accuracy of the orifice flowmeter. Various piping configurations

upstream of the orifice flowmeter can induce swirl in the flow that causes a shift in discharge coefficient [1,2,3]. Using a flow conditioner upstream of the

meter can remove swirl [4, 5], but the proper location of the flow conditioner

relative to the orifice plate remains a question. The locations are specified

in the standards such as AGA Report No. 3, ANSI/API 2530[6], and ISO 5167[7];

however, the guidelines provided in these standards do not adequately address

this problem. Work has been done to determine both the type of flow conditioner

and its location relative to the orifice plate that will result in discharge

coefficients similar to baseline values[3 , 8-12] . Most recent work completed at the National Institute of Standards and

Technology, Boulder, Colorado (NIST-B) , has been done using an in-line flow

conditioner with 19 concentric tubes (figure 1). The published results [11,12]

indicate that for flow conditions in this facility, a good location of the inline tube bundle for all beta ratios tested is between 13 and 17 pipe diameters

upstream of the orifice plate. The beta ratio of an orifice plate is the ratio

between the orifice diameter and the inner diameter of the meter tube. If placed

closer to the orifice plate, the flow conditioner caused a negative shift in the

discharge coefficient. Research was conducted at NIST-B with various piping

configurations upstream of the flow conditioner. When the in-line tube bundle
is located 17 pipe diameters upstream of the orifice plate, the measured

discharge coefficient is within 0.3% of the baseline discharge coefficient at the same Reynolds number for all beta ratios tested. This result was consistent

regardless of whether the flow conditioner was preceded by a long, straight,

upstream section or a disturbance such as a tee or two, out-of-plane elbows

located 19 pipe diameters upstream of the orifice plate. The question was raised

that perhaps a different type of flow conditioner would produce similar or better

results. For that reason, the following four alternate flow conditioners were

tested: a Zanker; an etoile; a flanged, 7 tube bundle; and a flanged, 19 tube

bundle of similar construction to the in-line, 19 tube bundle. These flow

conditioners are illustrated in figures 2a through 2d. Because previous work had

determined that an upstream tee resulted in the greatest shift in the discharge

coefficient [11] , the tee was placed 19 pipe diameters upstream of the orifice

plate for the testing of the four flow conditioners (figure 3)

.

Another objective of this research was to determine the difference in

orifice meter performance when using either the flanged or the in-line, 19 tube

bundle flow conditioner. Prior to conducting these tests, the system

configuration was modified so that the distance between the tee and the orifice

plate was reduced to 17 pipe diameters (figure 4) . This configuration more accurately reflects the minimum allowable overall distance between the

disturbance and the orifice plate as specified by AGA Report No. 3, ANSI/API

2530 [6] when a flow conditioner is used (for a beta ratio of 0.75 and a partially

closed valve disturbance) . The flow conditioners were placed directly downstream

of the disturbance because it was previously determined that this was an acceptable location for the in-line tube bundle in this system[ll].

The next aim of the research conducted at NIST-B was to determine the

effect, if any, of pressure tap location (flange taps) on determining the orifice

discharge coefficient. These tests were conducted with and without an in-line

tube bundle flow conditioner located directly downstream of the tee, as shown in

figure 4. In addition, concern had been expressed that flow conditioners of the

same basic type could be significantly different from one to another. Using the same configuration, tests were conducted using two other flanged, 19 tube bundle

flow conditioners, one with a hexagonal pattern, figure 2e, and the other a round

pattern with tubes of slightly larger diameter. Table 1 lists all the flow

conditioners and their salient features.
Table 1. Flow conditioner codes, descriptions, and measurements.

Identi- Name Number Pattern: Dimension mm (in)

fication Tubes/

Blades

In-line (I)

Flanged (F)

Length OD Tube ID

ITl tube 19 round-I 254 97 15

bundle (10) (3.8) (0.6)

FTl tube 19 round-F 254 95 15

bundle (10) (3.7) (0.6)

FT2 tube 19 hex-F 254 95 16

bundle (10) (3.7) (0.64)

FT4 tube 19 round-F 254 101 18

bundle (10) (4) (0.7)

FT6 tube 7 round-F 340 100 32

bundle (13.4) (3.9) (1.3)

ETl etoile 8 star-F 311

(12.3)

102

(4)

ZAN Z anker 32 perf. plate 108 102

holes with

honeycomb-F

(4.3) (4)

EXPERIMENTAL PROGRAM

The facility at NIST-B is a 100 mm (4 inch) nitrogen gravimetric system with

an operating pressure of about 4 MPa (580 psia) . The orifice flowmeter consists

of three sections: approach, upstream, and downstream. Two approach pieces were used during the course of this research. One approach section used is 8 pipe

diameters in length and has an internal surface roughness of 0.76 |im (30 iJ.in) Ra,

the absolute mean deviation value of the surface finish measurement. This piping

configuration is shown in figure 3. The other approach section is 6 pipe

diameters in length with an internal surface roughness of 2.5 /Ltm (100 /iin) Ra and

was used as shown in figure 4. The upstream section, 11 pipe diameters long, has

a surface roughness of 3.8 nm (150 ixin) Ra. The downstream section is 16 pipe

diameters in length. All sections were pinned at the flanges to insure proper

alignment.

The 4 inch orifice discharge coefficient baseline values used for

comparison in this report were described in detail by Sindt et al.[ll]. In

brief, for each of the beta ratios of 0.43, 0.55, 0.67, and 0.73, data were obtained in at least two baseline configurations. For these baseline

configurations, the orifice plate was preceded by either 56 pipe diameters of

straight pipe, figure 5a, an oversized Sprenkle flow conditioner and 46 diameters

of straight pipe, figure 5b, or 46 diameters of straight pipe, figure 5c. All

meter tube configurations included the 3.8 urn (150 ^in) Ra upstream section.

These data were fitted to a curve which relates orifice discharge coefficient to
pipe Reynolds number for each beta ratio. The same fitting routine was used for

all subsequent experimental data.

Portions of this research include complete data sets. A typical data set

contains at least four data points, taken at each of four flow rates, for all

four beta ratios. For each beta ratio, half of the data were taken on one day

and the other half on another to include the effects of any daily variability.

For each data point, the pressure drop across the orifice plate was measured at

the flange pressure taps located at the 9 o'clock position, as viewed from

upstream (figure 3) . The flow rates used extended over a pipe Reynolds number

range of 0.5-1.5 x 10*^. The data sets for the other portions of the research in this report include

data points obtained when using only the largest and smallest beta ratios.

Because the configuration and flow conditioner (in-line tube bundle) used for the

tap location tests had been investigated thoroughly in previous work [11], we decided to limit this testing to the 0.43 and 0.73 beta ratio plates with two

data points at each flow rate. The flow rates using these two plates covered the

entire pipe Reynolds number range. The use of these two orifice plates was also

deemed sufficient for tests to determine the effect of variations in the

dimensions of the flanged, 19 tube bundle flow conditioner, but four data points were obtained at each flow rate.

The percentage of the shift in orifice meter discharge coefficients caused

by either upstream piping configurations or flow conditioners at selected

Reynolds numbers was computed as follows:

(C,-Ch)xlOO (1) q, '

where C^ is the discharge coefficient that was experimentally determined with the

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

various test configurations.

The first tests involved alternate flow conditioners, and a complete data

set was taken for each flow conditioner. A complete data set is defined as four

data points taken at each of four flow rates, for all four orifice plate beta

ratios. The data sets were taken over a two-day period to include the effects

of daily variability. The tee was located 19 pipe diameters upstream of the

orifice plate as shown in figure 3. AGA Report No. 3, ANSI/API 2530 [6] specifies

that the minimum allowable distance between the flow conditioner and the orifice

plate is approximately 7 pipe diameters with a 0.75 beta ratio orifice plate.

Tests at this facility and others [3 ,8-11] have shown that placing the flow

conditioner 7 pipe diameters upstream of the orifice plate results in a negative

shift of the discharge coefficient for a variety of working fluids and meter

sizes. In an effort to find a better location, the initial tests of the

alternate flow conditioners were conducted with the downstream end of the flow

conditioner located 11 pipe diameters upstream of the orifice plate. An

exception was the Zanker flow conditioner, figure 2a. Because of its design, the
flange must be on the upstream side; therefore, the distance between the outlet

of the Zanker flow conditioner and the orifice plate was 10 pipe diameters.

Because these tests showed a consistent negative shift of the discharge

coefficients with the use of each of the flow conditioners, no tests were conducted with the flow conditioners located closer to the orifice plate.

For the second portion of the research, the tee was located 17 pipe

diameters upstream of the orifice plate (figure 4) . This was accomplished by

installing the shorter approach section of the flowmeter. A complete set of data was gathered using the flanged, round pattern, 19 tube flow conditioner [FTl]

,

and the in-line, 19 tube flow conditioner [ITl], figures 1 and 2d. For these

tests, the flow conditioner was placed at the outlet of the tee so that its

downstream end was 15 pipe diameters upstream of the orifice plate.

The piping configuration shown in figure 4 was used in the pressure tap

location study. For these tests the discharge coefficients were determined both

with and without the in-line, 19 tube flow conditioner located at the tee outlet.

Because the configuration and flow conditioner (ITl) used for the tap location

tests had been previously investigated[ll] , a reduced data set was taken. Only

the 0.43 and 0.73 beta ratio orifice plates were used, and only two data points were taken at each flow rate. The pressure drop across the orifice plate was measured at four locations: 12, 3, 6, and 9 o'clock, as viewed from upstream of

the orifice.

Because these tests indicated a pressure tap location influence, subsequent

tests were modified to include the determination of the discharge coefficients

at the 3 o'clock tap location in addition to those from the 9 o'clock tap

location. With measurements at the two tap locations and the same piping

configuration (figure 4) , two other flanged, 19 tube bundle flow conditioners of

slightly different design [FT2, FT4] were located at the tee outlet and tests were conducted with the 0.43 and 0.73 beta ratio orifice plates.

To complement the flow measurement work being done with various flow

conditioners, a pitot-static probe was used to characterize the velocity profiles

downstream of each flow conditioner. For these measurements, the orifice plate

was removed and the probe apparatus was located in its place. The velocity

profile work was preliminary; however, a general description of the profiles are mentioned in this report.

TEST RESULTS

Alternate Flow Conditioners;

Data for the Zanker flow conditioner are shown in tables 2-5. Figures 6-9

show the orifice discharge coefficients at various pipe Reynolds numbers for each

of the beta ratios. For a pipe Reynolds number of 1.25 x 10*, the difference

between the discharge coefficients calculated from the measured data and that of

the baseline is shown in figure 10. Using the Zanker flow conditioner lOD

upstream of the orifice plate results in discharge coefficients within -0.15% of

baseline for each beta ratio.
Data taken with the etoile flow conditioner located IID upstream of the

orifice plate are recorded in tables 6-9 and the discharge coefficients are shown

in figures 11-14. The shift in discharge coefficient is shown in figure 15. The

discharge coefficients are at least 0.25% below baseline values for all beta

ratios tested.

Tables 10-13 contain the data taken while using the flanged, 7 tube bundle

[FT6] located at IID, and the discharge coefficient data are displayed in figures

16-19. The percent shift in discharge coefficient when using this flow

conditioner is shown in figure 20. Once again, the discharge coefficients with

this flow conditioner were lower than baseline values for all beta ratios tested.

The last flow conditioner tested at the IID upstream location was the

flanged, 19 tube bundle [FTl] and the data are in tables 14-17. Figures 21-24

and figure 2 5 display the discharge coefficient data and the percent shift in

discharge coefficient, respectively. With this flow conditioner, the discharge

coefficient with the 0.4 3 beta ratio is similar to the baseline value, but there

was a negative shift with the larger beta ratios.

In summary, when a tee disturbance is located 17 pipe diameters upstream of

the orifice plate, placing any of the four flow conditioners about 11 pipe

diameters upstream of the orifice plate returns the discharge coefficient within

-0.5% of the baseline value, at a pipe Reynolds number of 1.25 x 10*.

Velocity profiles were measured downstream of these flow conditioners at the

orifice meter location and the results were somewhat varied. All were symmetric,

but those downstream of the tube bundle and etoile flow conditioners were

flatter, while the profiles downstream of the Zanker flow conditioner were slightly more peaked than a theoretical reference turbulent velocity profile at an equivalent Reynolds number.

In-line vs. Flanged Tube Bundle Flow Conditioners;

The data taken with the flanged, 19 tube bundle flow conditioner [FTl]

located 15 pipe diameters (15D) upstream of the orifice plate are recorded in

tables 18-21 and are illustrated in figures 26-29. The percent differences

between these discharge coefficients and the baseline values are shown in figure

30. Tables 2 2-25 contain the data taken when the in-line tube bundle was located

15 pipe diameters upstream of the orifice plate. The data are plotted in figures

31-3 4 and figure 3 5 shows the percent change in discharge coefficient from

baseline.

The discharge coefficients with the flanged flow conditioner were slightly

above baseline except for the 0.55 beta ratio plate. The largest shift in

discharge coefficient occurred with the 0.67 beta ratio plate, but it was only

about +0.25%. The results for the in-line flow conditioner were marginally

better. The largest shift was -0.2% which occurred with the 0.55 beta ratio

plate. Though the velocity profiles in the plane of the orifice plate were asymmetric, placing either of these flow conditioners 15 pipe diameters upstream

of the orifice plate resulted in discharge coefficients close to baseline values.
Pressure Tap Location;

Only the 0.4 3 and 0.7 3 beta ratio plates were used for the pressure tap

location testing. Data were taken simultaneously at the 3 and 9 o'clock

positions, as were the data for the 6 and 12 o'clock positions. Therefore, the

3 and 9 o'clock discharge coefficient data will be plotted together, as will the

6 and 12 o'clock data.

Tables 26-29 contain the data taken at each of the pressure taps with a 0.73

beta ratio orifice plate installed and no flow conditioner. Figures 36 and 37

show the discharge coefficients computed at each location. Tables 30-33 list the

data obtained at the four tap locations while using the 0.4 3 beta ratio plate and no flow conditioner. The plots of the discharge coefficients are shown in

figures 38 and 39.

As expected, the discharge coefficients for the 0.7 3 beta ratio plate

shifted away from the baseline because no flow conditioner was installed. The

effect of tap location was significant, especially at the 6 and 12 o'clock

positions (figure 37). At a pipe Reynolds number of 1.1 x 10^, the discharge

coefficient from the 6 o'clock position showed a +0.7% shift from baseline, while

the coefficient for the 12 o'clock position showed a -0.36% shift from baseline.

Figures 38 and 39 indicate that the shift from baseline when using the 0.4 3 beta

ratio orifice plate without a flow conditioner was very substantial, however

there was little difference between results for different pressure tap locations.

The in-line tube bundle was installed at the outlet of the tee and the tests

to determine pressure tap location effects were repeated. The data for the 0.73

beta ratio plate are in tables 34-37 and are plotted in figures 40 and 41.

Tables 38-41 contain the data for the 0.43 beta ratio plate, and figures 42 and

43 show those data.

The discharge coefficients for the 0.43 beta ratio plate resulted in values

similar to baseline as shown previously in figure 31 for this piping

configuration and flow conditioner location. The discharge coefficients at the

6 and 12 o'clock positions indicated a slight downward shift; however, all points

are within the scatter shown in figure 31. No dependence on tap location was observed for these specific tests.

The discharge coefficients for the 0.73 beta ratio plate with the flow

conditioner installed showed a tap location dependency. The discharge

coefficients were near baseline values at the 9 and 6 o'clock tap locations as previously seen with this configuration in figure 34. The discharge coefficients

at the 3 and 12 o'clock positions, however, were below baseline. At a pipe

Reynolds number of 1.1 x 10*, the difference between the discharge coefficients

at the 3 and the 9 o'clock positions was about 0.75% (figure 40). The disparity

between discharge coefficients at the various tap locations for the 0.73 beta

ratio plate seemed as great when the flow conditioner was installed as when it was not. Because of the apparent influence of tap location on discharge

coefficient for the 0.73 beta ratio plate, determination of the discharge
coefficient at the 3 o'clock position was added to the test plan for subsequent

research work.

Other Tube Bundle Flow Conditioners;

Two flanged, 19 tube bundle flow conditioners, one with a hexagonal tube

pattern [FT2] and one with a round concentric pattern [FT4] were placed at the

outlet of the tee disturbance which was located 17 pipe diameters upstream of the

orifice plate. The round pattern conditioner had tubes of larger diameter,

thinner walls, and rougher surface finish than those in the flow conditioners

referred to previously in this paper.

Data taken with the hexagonal -pattern flow conditioner and the 0.73 beta

ratio orifice plate are located in tables 42 and 43 and are plotted in figure 44.

Data for the 0.4 3 beta ratio and the same flow conditioner are in tables 44 and

45 and are displayed in figure 45.

Data obtained when using the round-pattern flow conditioner and the 0.73 and

0.43 beta ratio orifice plates are found in tables 46-49. Data for the 0.73 beta

ratio are displayed in figure 46 and those for the 0.43 beta ratio are in figure

47.

Figure 45 indicates that for the 0.4 3 beta ratio plate the hexagonal-pattern

flow conditioner resulted in discharge coefficients similar to baseline values.

Figure 47 shows that the discharge coefficients using the round-pattern flow

conditioner with the 0.43 beta ratio plate are shifted slightly downward. In both

cases, pressure tap location had very little impact on the discharge coefficient.

This is not the case with the 0.73 beta ratio plate. Figure 44 shows that

when the hexagonal-pattern flow conditioner was used, the discharge coefficients

using the 9 o'clock taps were slightly higher than baseline value, while those

using the 3 o'clock taps fell nearly 1.0% lower.

Using the round-pattern flow conditioner yielded similar results. The 9 o'clock tap location yielded slightly higher discharge coefficients than

baseline, and the discharge coefficients at the 3 o'clock tap location were lower

than baseline and showed more data scatter.

CONCLDSIONS AND RECOMMENDATIONS

Previous work at this facility showed that a tee disturbance upstream of the

orifice plate resulted in a larger shift in discharge coefficient than either a single- or double-elbow disturbance at the same location[ll] . Additional work

is needed to determine whether the same is true for other upstream disturbances

such as valves and reducers.

With a tee installed 19 pipe diameters upstream of the orifice plate and the

various flow conditioners located 10 to 11 pipe diameters upstream of the orifice

plate, discharge coefficients were within -0.5% of the baseline value for all

beta ratios tested. The Zanker flow conditioner produced somewhat better results

than the others; discharge coefficients were within -0.2% of baseline values for

all beta ratios.

8
Should these results prompt additional interest in the Zanker flow

conditioner, future research could include several possibilities. The Zanker

flow conditioner could be tested in other line sizes and at different locations

relative to the orifice plate. Because the velocity profile downstream of the

Zanker flow conditioner is quite distinctive from those downstream of other flow

conditioners, pressure tap location tests should also be included.

The tee was installed 17 pipe diameters upstream of the orifice plate, and

comparative data were taken with a flanged, 19 tube bundle [FTl] and an in-line,

19 tube bundle flow conditioner [ITl] placed directly downstream of the tee. The

discharge coefficients with the flanged tube bundle flow conditioner were higher

than baseline except when the 0.55 beta ratio plate was used. The largest shift

in coefficient, +0.25%, occurred when the 0.67 beta ratio plate was used. When

the in-line flow conditioner was used, all discharge coefficients were at or slightly below baseline value. The largest error, -0.2%, occurred when the 0.55

beta ratio plate was used. Figures 3 and 3 5 would indicate that the in-line

flow conditioner performed slightly better in this test configuration.

Discharge coefficients were computed using the pressure differential across

the flange taps at 3, 6, 9, and 12 o'clock for the 0.43 and 0.73 beta ratio

orifice plates. These tests were conducted with the tee located 17 pipe

diameters upstream of the orifice plate, with no flow conditioner and with an inline tube bundle flow conditioner placed directly downstream of the tee. When

the 0.4 3 beta ratio plate was used, the computed discharge coefficient showed no dependence upon pressure tap location. When the 0.73 beta ratio plate was used,

there was a dependence on pressure tap location both with and without a flow

conditioner (figures 40, 41, 44, 46).

The results for various types of flanged, 19 tube bundle flow conditioners

were beta ratio dependent. When the 0.43 beta ratio plate was used, installing

the hexagonal-pattern flow conditioner [FT2] at the outlet of the tee resulted

in discharge coefficients similar to baseline values. When the round-pattern

tube bundle, with larger rougher tubes [FT4], was placed at the tee outlet, the

computed discharge coefficient showed a -0.3% shift from baseline. Because of

the obvious dependence of pressure tap location when using the 0.73 beta ratio

plate, it is difficult to deteirmine the performance characteristics of these flow

conditioners when this orifice plate is used. If we consider the discharge

coefficients at the 9 o'clock tap location, the flow conditioners performed

comparably.

The results from the pressure tap location study, including the flow

conditioner comparison work, were very compelling. Future work should include

additional measurement of pressure tap location effects when the system is in a baseline piping configuration (figures 5a, 5b, 5c), particularly with larger beta

ratio orifice plates. It would also be interesting to examine the relationship

between flow conditioner position and tap location.
REFERENCES

[I] Brennan, J.A. , S.E. McFaddin, C.F. Sindt, and K.M. Kothari, The influence

of swirling flow on orifice and turbine flowmeter performance. Flow

Measurement and Instrumentation, Vol. 1, No. 1, Butterworth Scientific Ltd.,

Burry Street, Guildford, Surrey, UK (Oct. 1989)

[2] Morrison, G.L., R.E. DeOtte, M. Moen, K.R. Hall, and J.C. Holste, Beta

ratio, swirl, and Reynolds number dependence of wall pressure in orifice

flowmeters. Second International Symposium on Fluid Flow Measurement,

Calgary, Alberta, Canada, (June 6-8, 1990).

[3] Mattingly, G.E., and T.T. Yeh, Summary Report of NIST's Industry-Government

Consortium Research Program on Flowmeter Installation Effects with Emphasis

on Research Period Nov. 1988-May 1989. Nat. Inst. Stand. Tech. (U.S.)

NISTIR 4310; 1989.

[4] Kinghorn, F.C., A. McHugh and W.D. Dyet, The use of etoile flow

straighteners with orifice plates in swirling flow, American Society of

Mechanical Engineers Winter Annual Meeting, Paper 79-WA/FM-7 (1979) . [5] Sprenkle, R.E. and N.S. Courtright, Straightening vanes for flow

measurement, Mechanical Engineering, 71-73 (Feb. 1958) . [6] Orifice metering of natural gas and other related hydrocarbon fluids,

ANSI/API 2530, Second Edition, American Gas Association, Arlington, VA 22209

(Sept. 1985)

[7] 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)

[8] Sattary, J.A., EEC orifice plate programme-installation effects.

Installation Effects on Flow Metering, National Engineering Laboratory, East

Kilbride, Glasgow (Oct. 22, 1990).

[9] Morrow, T.B., R.J. McKee, and J.T. Park, Upstream installation requirements

for accurate orifice measurements. Second International Symposium on Fluid

Flow Measurement, Calgary, Alberta, Canada (June 6-8, 1990).

[10] Zanker, K.J., The development of a flow straightener for use with orifice

flowmeters in disturbed flow. Paper D-2 , Symposium of Flow Measurement,

Scotland (1969)

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

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

Stand. Tech. (U.S.) Tech. Note 1344; 1990.

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

conditioners in a 4-inch orifice meter. Nat Inst. Stand. Tech. (U.S.) Tech.

Note 1330; 1989.

10
Figure 1. In-line, tube bundle flow conditioner.

Figure 2a. Zanker flow conditioner,

11
Figure 2b. Etoile flow conditioner.

Figure 2c. Flanged, 7 tube bundle flow conditioner.

12
Figure 2d. Flanged, 19 tube bundle flow

conditioner (round)

.

Figure 2e. Flanged, 19 tube bundle flow

conditioner (hexagonal)

.

13
Orifice Plate

Tee

Figure 3. Test configuration with a tee 19 pipe

diameters upstream of the orifice plate.

Tee

Figure 4. Test configuration with a tee 17 pipe

diameters upstream of the orifice plate,

14
Figure 5a. Four-inch orifice meter, 56 pipe diameters of

straight pipe.

Figure 5b. Four-inch orifice meter, 6-inch Sprenkle at

4 6 pipe diameters.

Figure 5c. Four-inch orifice meter, 46 pipe diameters of

straight pipe

.

15
0.62

O 0.61

0)oo

0)a

-g 0.60

0.5J

-

- /S = 0.43

- Flow Conditioner: ZAN

- *

- *

. *---*

- *. ,.. **

"*---.

*

*

- Baseline

- ««««« Tee at 19D, flow conditioner at lOD (Table 2)

1 1 1 1 1 1 1 .2 0.6 1.0 1.4 1.8

0.62

o 0.61

O

o

"^ 0.60

.5%

Pipe Reynolds Number/10

Figure 6. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 19D and a Zanker flow conditioner at lOD.

-

- /3 = 0.55

- Flow Conditioner: ZAN

- 7

_

*

- Baseline **

Tee at 19D, flow conditioner at lOD (Table 3)

1 1 1 1 1 2 0.6 1.0 1.4 1. 8

Pipe Reynolds Number/ 10

Figure 7. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate vidth a tee at 19D and a Zanker flow conditioner at lOD.

16
0.62

O 0.61

ou

a

-g 0.60

0.5£

-

- /S = 0.67

- Flow Conditioner: ZAN

- — * "-*-

* "«

-

Baseline

- • *•** Tee at 19D,

1

flow conditioner at lOD (Table 4)

1 1 1.6

0.62

o 0.61

o

CJ

a;u

CO -g 0.60

0.5J

1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 8. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 19D and a Zanker flow conditioner at lOD.

-

- /S = 0.73

-

Flow Conditioner: ZAN

-

*

-

* ;. ,

1 ' %

**

*

- Baseline ***** Tee at 19D.

1

flow conditioner ill. at lOD (Table 5)

1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 9. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 19D and a Zanker flow conditioner at lOD.

17
1.0

a

aA 0.0

a

0)ou

0)

-1.0

Pipe Reynolds No. = 1.25 x lO' Flow Conditioner: ZAN

Q- — — — — —D— _ — -a — __ -Q

0.3 0.4 —

r

0.5 0.6 Beta Ratio

0.7

Figure 10. Percent change in discharge coefficient vs. beta ratio with a Zanker flow conditioner at lOD and a tee at 19D,

0.62

o 0.61

0)oo

beu

CO •% 0.60

0.5 % 0.6 1.0 1.4 Pipe Reynolds Number/lO

0.8

-

- /S = 0.43

-

Flow Conditioner ETl

1

1

1

1

11

---

* * *

* * •

* %

*

Baselin

Tee at

1

19D. flow

1

conditioner

1

at IID (Table 6)

1 1 1 i.e

Figure 11. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 19D and an etoile flow conditioner at IID.

18
0.62

O 0.61

0)oo

<u

lao u

as -§ 0.60

to

0.5£

/3 = 0.55

Flow Conditioner: ETl

i * *

Baseline ***** Tee at 19D. How conditioner at IID (Table 7)

0.6 1.0 1.4 Pipe Reynolds Number/10*

1.8

Figure 12. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate with a tee at 19D and an etoile flow conditioner at IID.

0.62

o 0.61

0)oo

0)

•^ 0.60 m

.5%

)8 = 0.67

Flow Conditioner: ETl

**

*

*

Baseline Tee at 19D, flow condtioner at UD (Table 8)

1.0 1.4 Pipe Reynolds Number/10

1.8

Figure 13. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 19D and an etoile flow conditioner at IID.

19
0.62

a

O 0.61

0)oo

a>u

CO -^ 0.60

(n

0.5{

-

- /3 = 0.73

-

Flow Conditioner: ETl

;<t

-

** *

* *^ * *f -

- Baseline

Tee at 19D, flow conditioner at IID (Table 9)

1 1 1 1 1 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 14. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 19D and an etoile flow conditioner at IID.

1.0

a

(0 A 0.0

u

a.

-1.0

Pipe Reynolds No. = 1.25 x 10 Flow Conditioner: ETl

D- — __ —

O' — D0.3 0.4 —I

1 r0.5 0.6 Beta Ratio

I 0.7 0,8

Figure 15. Percent change in discharge coefficient vs. beta ratio with an

etoile flow conditioner at IID and a tee at 19D.

20
0.62

C

0) *0 0.61

ou

0)

b(

CO -^ 0.60

CO a

0.5

%,

/S = 0.43

Flow Conditioner: FT6

•iT-

*

Baseline

*«** Tee at 19D. flow conditioner at IID (Table 10)

0.6 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 16. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 19D and a flanged, 7 tube bundle flow

conditioner at IID.

0.62

o 0.61

ou

lac u

CO ^ 0.60

0.5 %

/S = 0.55

Flow Conditioner: FT6

Baseline **

Tee at 19D, flow conditioner at IID (Table 11)

0.6 1.0 1.4 1.6 Pipe Reynolds Number/lO

Figure 17. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate with a tee at 19D and a flanged, 7 tube bundle flow

conditioner at UD.

21
0.62

G

0)o 0.61

0)ou

0)

^ 0.60

•5%

-

- /? = 0.67

- Flow Conditioner: FT6

- 4

_

*

* » * .* * — *

- Baseline ***** Tee at 19D. flow conditioner at IID (Table 12)

1 . 1 1

0.62

C

"o 0.61

0)o

c_>

C0 •^ 0.60

0.5 %

1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 18. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 19D and a flanged, 7 tube bundle flow

conditioner at IID.

/3 = 0.73

Flow Conditioner: FT6

Baseline ***** Tee at 19D, flow conditioner at IID (Table 13)

1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 19. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 19D and a flanged, 7 tube bundle flow

conditioner at IID.

22
u

0)

tlfl d

o

d

o

ft

OJ a,

l.U

Pipe Reynolds No. = 1.25 x 10* Flow Conditioner: FT6

u.u

— —o- — "~" -a

1.0 -

1 1 1 1 1 1 1 1 ' 0.3 0.4 0.5Beta

0.6 Ratio0.7 0.8

Figure 20. Percent change in discharge coefficient vs. beta ratio with a

flanged, 7 tube flow conditioner at IID and a tee at 19D.

0.62

ao 0.61

v

oo

V

-^ 0.60 w

0.5J

-

- /9 = 0.43

- Flow Conditioner: FTl

- *

-

- "- *

_ t ^.

- *

- Baseline Tee at 19D, flow conditioner at IID (Table 14)

1 1 1 t 1 1 1 2 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 21. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 19D and a flanged, 19 tube bundle flow

conditioner at IID.

23
0.62

C

0)O 0.61

0)oo

a

-^ 0.60

0.51

-

- /S = 0.55

- Flow Conditioner: FTl

- *'""----.-

- *• ""---. ^ _

- t

""^""-^^^

- *

* **

- *

- Baseline *« Tee at 19D. flow conditioner at IID (Table 15)

1 1 1 1 1 1 , 0.6 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 22. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate with a tee at 19D and a flanged, 19 tube bundle flow

conditioner at IID.

0.62

o 0.61

0)oo

a>

03 "g 0.60 m

0.5%

-

- /3 = 0.67

- Flow Conditioner: FTl

- *

*

•

*

- Baseline ***

Tee at 19D,

1

flow conditioner at IID (Table 16)

1 1 1 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 23. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 19D and a flanged, 19 tube bundle flow

conditioner at IID.

24
0.62

O 0.61

O

u

0)

CO •^ 0.60 m

0.5 %

-

- /3 = 0.73

-

Flow Conditioner: FTl

- "^' • •• .-

- *Baseline

Tee at 19D, flow condtioner at IID {Table 17)

1 1 1 1.0 1.4 1.6 Pipe Reynolds Number/10

Figure 24. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 19D and a flanged, 19 tube bundle flow

conditioner at IID.

1.0

a;a

CO j3 0.0

a

o

u

0)

-1.0

Pipe Reynolds No. = 1.25 x 10 Flow Conditioner: FTl

Q- __ — D ^'

0.3 0.4 —

r

0.5 0.6 Beta Ratio

0.7 0.8

Figure 25. Percent change in discharge coefficient vs. beta ratio with a

flanged, 19 tube flow conditioner at IID and a tee at 19D.

25
0.62

*0 0.61

ou

0)

CD •^ 0.60

tn

0.5£

-

- /S = 0.43

- Flow Conditioner: FTl

'

*

- *

« -,,_ * 4-. *

1 •

-

"*--.

- Baseline ***** Tee at 17D. flow conditioner at 15D (Table 18)

1 . 1 . 1 1

0.62

'o 0.61

a;oU

CO •§ 0.60

CO

0.5{

0.6 1.0 1.4 1.8 Pipe Reynolds Number/ 10

Figure 26. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D and a flanged, 19 tube bundle flow

conditioner at the outlet of the tee.

-

-. /5 = 0.55

. Flow Conditioner: FTl

- %

-

*

*

i -

-

Baseline

- ***** Tee at 17D,

1 1

flow conditioner I.I. at 15D (Table 19)

0.6 1.0 1.4 1.6 Pipe Reynolds Number/10

Figure 27. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate with a tee at 17D and a flanged, 19 tube bundle flow

conditioner at the outlet of the tee.

26
0.62

0) "S 0.61

QiOO

9)60

-g 0.60

en

•H

-

- /3 = 0.67

- Flow Conditioner: FTl

-

*

-

1 $

*

---

<f *

'

Baseline ***** Tee at 17D,

1

flow conditioner at 15D

1 1

(Taible 20)

1 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 28. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 17D and a flanged, 19 tube bundle flow

conditioner at the outlet of the tee.

0.62

a

O 0.61

0)OU

0)tau

CO •^ 0.60 m

0.5J

-

- /3 = 0.73

-

Flow Conditioner: FTl

- ^^..x .

V 'v

- Baseline ***** Tee at 17D.

1

flow conditioner at 15D (Table 21)

1 1.0 1.4 1.6 Pipe Reynolds Number/lO

Figure 29. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D and a flanged, 19 tube bundle flow

conditioner at the outlet of the tee.

27
1.0

u

0)a

aA 0.0 u

C

0)o

0) cu

-1.0

Pipe Reynolds No. = 1.25 x 10

Flow Conditioner: FTl

B.

y^ ^

0.3 0.4 0.5 0.6 Beta Ratio

0.7 0.8

Figure 30. Percent change in discharge coefficient vs. beta ratio with a tee at 17D and a flanged, 19 tube bundle flow conditioner at the outlet of

the tee.

0.62

o 0.61

0)oo

a

•% 0.60

0]

0.5£

/? = 0.43

Flow Conditioner: ITl

*

*

Baseline ***** Tee at 17D. flow conditioner at 15D (Table 22)

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 31. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D and an in-line, 19 tube bundle flow

conditioner at the outlet of the tee.

28
0.62

a

'o 0.61

oo

9)h

a

•^ 0.60

CO

0.5 %

-

- /3 = 0.55

- Flow Conditioner: ITl

- *

*

* v

-

* *

- Baseline ***** Tee at 17D,

1 1

flow conditioner at 15D (Table 23)

I 1 1 1 1

0.62

G

o 0.61

0)oo

0)a

•^ 0.60

0.5J

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 32. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio plate with a tee at 17D and an in-line, 19 tube bundle flow

conditioner at the outlet of the tee.

-

- /S = 0.67

-

Flow Conditioner: ITl

- * : %...

-

* % , vv

- Baseline ***** Tee at 17D,

1

flow conditioner at 15D (Table 24)

1 1 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 33. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio plate with a tee at 17D and an in-line, 19 tube bundle flow

conditioner at the outlet of the tee.

29
0.62

'o 0.61

ou

(30

-^ 0.60

!0

0.5J

-

- /3 = 0.73

-

Flow Conditioner: ITl

- »* #-* T,^ *...

»

- Baseline ***** Tee at 17D,

1 1,1. flow conditioner at 15D (Table 25)

1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 34. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D and an in-line, 19 tube bundle flow

conditioner at the outlet of the tee.

1.0

^ 0.5

0)a

CO

-C5 0.0 o

a

u

CU -0.5

-1.0

Pipe Reynolds No. = 1.25 x 10

Flow Conditioner: ITl

— Q'

0.3 0.4 0.5 0.6 Beta Ratio

0.7 O.B

Figure 35. Percent change in discharge coefficient vs. beta ratio with a tee at 17D and an in-line, 19 tube bundle flow conditioner at the outlet of

the tee.

30
0.62

a

O 0.61

9iOO

0)cm

"^ 0.60 m

0.5£

(.6

0.62

o 0.61

4)OO

0)

o

0.60 -

0.5J

1.6

/S = 0.73

Flow Conditioner: NONE

(P

** i

Baseline

00000 Tee at 17D. Tap at 3 O'Clock (Table 26)

****Tee at 17D, Tap at 9 O'Clock (Table 27)

1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 36. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, no flow conditioner, and flange pressure

taps at 3 and 9 o'clock.

-

/S = 0.73

Flow Conditioner: NONE

t

A

A A

A

: * * *

Baseline

AAAAATee at 17D. Tap at 6 O'Clock (Table 26)

AAAAATee at 17D. Tap at 12 O'Clock (Table 29)

1 . 1 1 1.0 1.4 1.6 Pipe Reynolds Number/10

Figure 37. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, no flow conditioner, and flange pressure

taps at 6 and 12 o'clock.

31
l/.OC

- * /S = 0.43

*i 9

c 9

0)o 0.61 - * %

0)oo

CO)

~ ,. Flow Conditioner: NONE

»4 **"---.

(0 ~"~--.,_

•g 0.60 ""------,_ m•r4 _ o

Baseline

OOOOOTee * at 17D. Tap at 3 O'Clock (Table 30) Tee at 17D, Tap at 9 O'Clock (Table 31) n <;q 1 1 1 1 1 1 1 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 38. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, no flow conditioner, and flange pressure

taps at 3 and 9 o'clock.

0.62

'o 0.61

0)o

bXl u

•^ 0.60

CO

0.5£

1.2

/S = 0.43

Flow Conditioner: NONE

Baseline

Tee at 17D. Tap at 6 O'Clock (Table 32)

AAAAATee at 17D, Tap at 12 O'Clock (Table 33)

0.6 1.0 1.4 1.8 Pipe Reynolds Nunriber/lO

Figure 39. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, no flow conditioner, and flange pressure

taps at 6 and 12 o'clock.

I

32
0.62

3 0.61

ou

V

etc a

•^ 0.60 m

0.5£

0.62

o 0.61 -

9iOU

a>

es •^ 0.60

0.5 %.

/S = 0.73

Flow Conditioner: ITl

O

O O

O

O

O

Baseline

00000 Tee at 17D. Tee at 17D,

O

O

FC

FC

at 15D, Tap at

at 15D, Tap at

3 O'clock (Table 34)

9 O'clock (Table 35)

_L 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 40. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, an in-line, 19 tube bundle flow conditioner

at the tee outlet, and flange pressure taps at 3 and 9 o'clock.

/S = 0.73

Flow Conditioner: ITl

A

A

A

&

Baseline Tee at 17D. FC at 15D. Tap at 6 O'Clock (Table 36)

AAAAATee at 17D. FC at 15D. Tap at 12 O'Clock (Table 37)

1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 41. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, an in-line, 19 tube bundle flow conditioner

at the tee outlet, and flange pressure taps at 6 and 12 o'clock.

33
0.62

0.5 %

fjc

- V

"S 0.61 -

•p4

i«-i

(<-i - <DO

o

0) ""-*--.- ^ e

CO -g 0.60 -

(0

•1.^ a

Baseline

.5 = 0.43

Flow Conditioner: ITl

4.

4-

OOOOOTee at 17D, FC at 15D. Tap at 3 O'Clock (Table 38) Tee at 17D, FC at 15D, Tap at 9 O'Clock (Table 39)

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 42. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, an in-line, 19 tube bundle flow conditioner

at the tee outlet, and flange pressure taps at 3 and 9 o'clock.

0.62

o 0.61

0)ou

0)

C0 -g 0.60

(0

0.5J

1.2

/S = 0.43

Flow Conditioner: ITl

A

|"

i

Baseline

AAAAATee at 17D, FC at 15D. Tap at 6 O'Clock (Table 40)

AAAAA Tee at 17D. FC at 15D. Tap at 12 O'Clock (Table 41)

J_ 0.6 1.0 1.4 1.8 Pipe Reynolds Number/lO

Figure 43. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, an in-line, 19 tube bundle flow conditioner

at the tee outlet, and flange pressure taps at 6 and 12 o'clock.

34 i
0.62

"3 0.61

ou

(d -^ 0.60 m

0.5%

/3 = 0.73

Flow Conditioner: FT2

* *

* o

COo 8

Baseline o OOOOOTee at 17D, FC at 15D. Tap at 3 O'Clock TTable

Tee at 17D, FC at 15D. Tap at 9 O'Clock (Table 43«{

1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 44. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, a flanged, 19 tube bundle flow conditioner

(hex) at the tee outlet, and flange pressure taps at 3 and 9

o'clock.

0.62

a

9) 'o 0.61

0)oo

a>bOh

C0 ^

CJm

0.60 -

0.5J

-

- /? = 0.43

- Flow Conditioner: FT2

*o

--er^-...

O "

6

-- ----. -.1

-

Baseline

CXXXXDTee at 17D,

*>ic>ti** Tee at 17D,

1

FC

FC

1

at

at

15D,

15D. Tap at Tap at

1

3

g O'clockO'clock

1

(Table

Table

44)

45)

1

Figure 45.

0.6 1.0 1.4 1.8 Pipe Reynolds Number/ 10

Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, a flanged, 19 tube bundle flow conditioner

(hex) at the tee outlet, and flange pressure taps at 3 and 9

o'clock.

35
U.06

-

- jg = 0.73

c

3 0.61

iso

-

Flow Conditioner: FT4

a

•^ 0.60 n•iH

- > i

s

o o

° ft 8 ^

* "1

n iio

-

Baseline

OOOOOTee at 17D. **

Tee at 17D,

FC

FC

o

at 15D, tap

at 15D. Up

at

at

o

o

3 o 9

1

o

clock (Table 46)

clock (Table 47)

1 0.6

Figure 46.

1.0 1.4 1.8 Pipe Reynolds Number/lO

Discharge coefficient vs. Reynolds number for the 0.73 beta ratio plate with a tee at 17D, a flanged, 19 tube bundle flow conditioner

(round) at the tee outlet, and flange pressure taps at 3 and 9

o'clock.

0.62

o 0.61

oV

C0 •^ 0.60 -

01

0.5

/? = 0.43

Flow Conditioner: FT4

O

. * 6% %

o d

Q

Baseline

OOOOOTee at 17D, FC at 15D, tap at 3 o'clock (Table 48) ***** Tee at 17D. FC at 15D. tap at 9 o'clock (Table 49)

%.2

Figure 47.

0.6

_L 1.0_L 1.4 Pipe Reynolds Number/10°

Discharge coefficient vs. Reynolds number for the 0.43 beta ratio plate with a tee at 17D, a flanged, 19 tube bundle flow conditioner

(round) at the tee outlet, and flange pressure taps at 3 and 9

o'clock.

36

J
Table 2. Measured and calculated quantities for 0.43 beta ratio, tee at 19D, ZAN at lOD.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 fim Ra Orifice Diameter = 4.4437 cm (1.7495 in)

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

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

43031490- 1 3.8857 287.94 45.81 16.365 1.1629 0.7888 0.6015 0.6020

43031490- 2 3.8745 288.01 45.67 16.624 1.1690 0.7929 0.6008 0.6014

43031490- 3 3.7976 287.50 44.85 29.730 1.5496 1.0534 0.6006 0.6016

43031490- 4 3.7904 287.62 44.74 29.585 1.5419 1.0480 0.5997 0.6007

43031490- 5 4.0065 288.57 47.13 5.550 0.6909 0.4673 0.6054 0.6056

43031490- 6 3.9981 288.69 47.01 5.588 0.6954 0.4702 0.6080 0.6082

43031490- 7 3.6474 287.06 43.14 46.633 1.9048 1.2985 0.6004 0.6020

43031490- 8 3.6495 287.39 43.11 45.868 1.8819 1.2818 0.5983 0.5999

43031690- 1 3.6170 287.31 42.74 47.683 1.9156 1.3056 0.5998 0.6015

43031690- 2 3.6149 286.66 42.82 46.854 1.8930 1.2922 0.5974 0.5991

43031690- 3 3.9582 288.30 46.61 5.841 0.7017 0.4752 0.6027 0.6029

43031690- 4 3.9959 288.50 47.02 6.020 0.7179 0.4857 0.6047 0.6049

43031690- 6 3.7876 287.48 44.73 27.745 1.4959 1.0170 0.6010 0.6019

43031690- 8 3.8533 287.93 45.43 15.154 1.1154 0.7569 0.6021 0.6026

43031690- 9 3.8483 287.96 45.37 15.071 1.1120 0.7547 0.6023 0.6028

Table 3. Measured and calculated quantities for 0.55 beta ratio, tee at 19D, ZAN at lOD.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra 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/m3) (kPa) (kg/s) (^106)

44031390- 1 3.8773 287.91 45.72 7.004 1.3011 0.8827 0.6039 0.6041

44031390- 2 3.8687 287.88 45.62 6.935 1.2923 0.8769 0.6034 0.6037

44031390- 3 3.9877 288.42 46.93 2.950 0.8596 0.5817 0.6070 0.6070

44031390- 4 4.0170 288.50 47.26 2.976 0.8677 0.5869 0.6078 0.6079

44031390- 5 3.5659 286.29 42.29 21.672 2.1991 1.5034 0.6028 0.6035

44031390- 7 3.7334 287.19 44.14 12.863 1.7310 1.1785 0.6032 0.6036

44031390- 8 3.7147 287.41 43.88 12.889 1.7245 1.1737 0.6021 0.6025

44031590- 1 3.7087 287.29 43.83 13.199 1.7480 1.1901 0.6034 0.6038

44031590- 2 3.7049 287.24 43.79 13.124 1.7424 1.1865 0.6035 0.6039

44031590- 3 3.5461 286.33 42.05 21.652 2.1939 1.5001 0.6034 0.6041

44031590- 4 3.9395 287.88 46.46 2.936 0.8523 0.5779 0.6062 0.6063

44031590- 5 3.9399 288.15 46.42 3.024 0.8651 0.5861 0.6066 0.6066

44031590- 6 3.8087 287.76 44.93 7.329 1.3212 0.8974 0.6047 0.6049

44031590- 7 3.8032 287.82 44.86 7.226 1.3087 0.8889 0.6037 0.6039

44031590- 8 3.5464 286.13 42.09 20.828 2.1536 1.4733 0.6037 . 6044

37
Table 4. Measured and calculated quantities for 0.67 beta ratio, tee at 19D, ZAN at lOD.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 ^m Ra 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/m3) (kPa) (kg/s) (+106)

45031490- 2 3.6803 287.37 43.48 5.692 1.8242 1.2422 0.6030 0.6032

45031490- 3 3.6728 287.35 43.39 5.707 1.8228 1.2414 0.6024 0.6026

45031490- 4 3.7979 287.58 44.84 2.783 1.3010 0.8843 0.6058 0.6059

45031490- 5 3.7915 287.47 44.78 2.838 1.3113 0.8916 0.6051 0.6052

45031490- 6 3.7415 287.34 44.21 4.102 1.5636 1.0640 0.6040 0.6041

45031490- 7 3.7425 287.20 44.24 4.061 1.5570 1.0599 0.6042 0.6043

45031590- 1 3.5935 287.17 42.48 8.687 2.2221 1.5154 0.6015 0.6017

45031590- 2 3.5951 286.99 42.53 8.600 2.2151 1.5113 0.6023 0.6025

45031690- 1 3.8122 287.91 44.95 3.885 1.5309 1.0395 0.6025 0.6026

45031690- 2 3.8061 287.67 44.92 3.846 1.5248 1.0360 0.6034 0.6035

45031690- 3 3.8422 287.94 45.30 2.700 1.2854 0.8724 0.6045 0.6046

45031690- 4 3.8389 287.83 45.28 2.709 1.2853 0.8726 0.6037 0.6038

45031690- 5 3.6830 287.57 43.48 6.052 1.8772 1.2776 0.6019 0.6020

45031690- 6 3.6801 287.13 43.51 5.978 1.8691 1.2735 0.6027 0.6029

45031690- 7 3.5660 286.72 42.23 8.187 2.1519 1.4696 0.6018 0.6021

45031690- 8 3.5700 286.54 42.30 8.153 2 . 1484 1.4679 0.6016 0.6018

Table 5. Measured and calculated quantities for 0.73 beta ratio, tee at 19D, ZAN at 100.

Pipe Diameter -= 10.366 cm (4.081 in), 3.8 fim Ra Orifice Diameter - 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46031390- 1 3.6679 287.11 43.37 3.987 1.9226 1.3102 0.6033 0.6034

46031390- 2 3.6426 286.69 43.14 4.292 1.9833 1.3534 0.6014 0.6015

46031390- 4 3.7371 287.27 44.17 2.783 1.6173 1.1009 0.6020 0.6021

46031390- 5 3.7015 287.26 43.75 3.279 1.7475 1.1900 0.6021 0.6021

46031390- 6 3.7003 287.24 43.74 3.271 1.7426 1.1867 0.6013 0.6013

46031490- 1 3.6166 286.99 42.78 5.461 2.2193 1.5138 0.5991 0.5992

46031490- 2 3.6209 286.74 42.88 5.438 2.2218 1.5163 0.6004 0.6005

46031590- 1 3.7704 287.48 44.53 3.309 1.7685 1.2026 0.6012 0.6013

46031590- 2 3.7521 287.41 44.32 3.293 1.7591 1.1968 0.6008 0.6009

46031590- 3 3.8031 287.66 44.89 2.595 1.5701 1.0669 0.6003 . 6004

46031590- 4 3.7981 287.76 44.81 2.608 1.5711 1.0674 0.5998 0.5999

46031590- 5 3.5599 286.63 42.17 5.432 2.2047 1.5062 0.6010 0.6012

46031590- 6 3.5680 286.45 42.29 5.401 2.1998 1.5033 0.6006 0.6007

46031590- 7 3.6898 287.12 43.63 4.067 1.9364 1.3193 0.5999 0.6000

46031590- 8 3.6710 287.51 43.35 4.057 1.9282 1.3127 0.6000 0.6001

38

J
Table 6. Measured and calculated quantities for 0.43 beta ratio, tee at 19D, ETl at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 urn Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kg/m3) (kPa) (kg/s) (+10^)

43041090- 1 3.7005 286.86 43.80 46.321 1.9037 1.2976 0.5975 0.5991

43041090- 2 3.6796 286.63 43.59 48.265 1.9416 1.3245 0.5983 0.6000

43041090- 3 3.9763 288.14 46.85 6.684 0.7515 0.5090 0.6018 0.6020

43041090- 4 3.9657 288.31 46.69 7.159 0.7758 0.5253 0.6013 0.6015

43041090- 5 3.7961 287.64 44.81 27.827 1.4968 1.0172 0.6000 0.6009

43041090- 6 3.7937 287.38 44.82 27.424 1.4859 1.0104 0.5998 0.6008

43041090- 7 3.8510 287.76 45.43 14.944 1.1067 0.7514 0.6016 0.6021

43041090- 8 3.8488 287.87 45.39 14.904 1.1015 0.7477 0.5998 0.6003

43041190- 1 3.7730 287.41 44.57 28.249 1.4987 1.0193 0.5978 0.5987

43041190- 2 3.7700 287.46 44.53 28.182 1.4964 1.0176 0.5978 0.5988

43041190- 3 3.6499 287.32 43.12 47.354 1.9090 1.3005 0.5971 0.5988

43041190- 4 3.6528 287.27 43.17 47.205 1.9040 1.2972 0.5962 0.5979

43041190- 5 3.9554 288.49 46.54 5.542 0.6780 0.4589 0.5984 0.5986

43041190- 6 3.9483 288.37 46.48 6.433 0.7297 0.4941 0.5983 0.5985

43041190- 7 3.8844 287.93 45.80 13.721 1.0635 0.7215 0.6009 0.6014

43041190- 8 3.8764 287.96 45.70 13.523 1.0525 0.7140 0.5997 0.6001

Table 7. Measured and calculated quantities for 0.55 beta ratio, tee at 19D, ETl at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /jm Ra 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/m3) (kPa) (kg/s) (+10^)

44041090- 1 3.7852 287.62 44.68 13.226 1.7591 1.1956 0.6008 0.6012

44041090- 2 3.7798 287.33 44.66 13.152 1.7534 1.1927 0.6007 0.6011

44041090- 1 3.9564 288.38 46.57 3.225 0.8926 0.6043 0.6051 0.6052

44041090- 2 3.9612 288.40 46.62 3.259 0.8967 0.6070 0.6043 . 6044

44041090- 3 3.6493 286.47 43.26 21.401 2.2026 1.5037 0.6008 0.6015

44041090- 4 3.6568 286.52 43.34 21.339 2.1989 1.5009 0.6001 0.6008

44041090- 5 3.8693 287.38 45.72 7.652 1.3552 0.9207 0.6018 0.6020

44041090- 6 3.8640 287.54 45.63 7.648 1.3542 0.9197 0.6021 0.6023

44041190- 1 3.9210 288.12 46.20 2.828 0.8329 0.5645 0.6054 0.6055

44041190- 2 3.9291 288.31 46.26 2.808 0.8318 0.5635 0.6064 0.6064

44041190- 3 3.6690 286.63 43.47 21.127 2.1986 1.5000 0.6021 0.6028

44041190- 4 3.6655 286.28 43.48 20.960 2.1879 1.4941 0.6015 0.6022

44041190- 5 3.7863 287.03 44.79 13.805 1.7986 1.2242 0.6005 0.6010

44041190- 6 3.7759 287.58 44.57 13.886 1.8024 1.2253 0.6015 0.6019

44041190- 7 3.8867 287.35 45.93 7.746 1.3678 0.9292 0.6023 0.6026

44041190- 8 3.8518 287.65 45.46 7.786 1.3674 0.9286 0.6036 0.6039

39
Table 8. Measured and calculated quantities for 0.67 beta ratio, tee at 19D, ETl at IID.

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

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

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

45040990- 1 3.6336 287.01 42.98 9.091 2.2805 1.5552 0.5999 0.6001

45040990- 2 3.6436 287.15 43.08 9.085 2.2802 1.5542 0.5994 0.5996

45040990- 3 3.7484 286.98 44.35 6.528 1.9622 1.3363 0.5997 0.5999

45040990- 4 3.7423 287.01 44.27 6.559 1.9677 1.3401 0.6005 0.6007

45040990- 5 3.8755 287.66 45.74 2.647 1.2761 0.8663 0.6033 0.6034

45040990- 6 3.8716 287.54 45.72 2.669 1.2773 0.8675 0.6016 0.6017

45040990- 7 3.8176 287.29 45.12 4.231 1.6019 1.0892 0.6030 0.6032

45040990- 8 3.8123 287.34 45.05 4.228 1.6002 1.0880 0.6031 0.6032

45041190- 1 3.7165 287.07 43.96 6.167 1.9037 1.2967 0.6013 0.6015

45041190- 2 3.7150 286.89 43.97 6.143 1.9021 1.2962 0.6019 0.6021

45041190- 3 3.8014 287.23 44.94 4.028 1.5587 1.0602 0.6026 0.6027

45041190- 4 3.7933 287.06 44.87 4.036 1.5599 1.0616 0.6029 0.6030

45041190- 5 3.8345 287.55 45.28 2.634 1.2647 0.8593 0.6024 0.6025

45041190- 6 3.8340 287.44 45.29 2.620 1.2656 0.8601 0.6045 0.6045

45041190- 7 3.5935 286.73 42.55 8.643 2.2140 1.5116 0.6003 0.6006

45041190- 8 3.5932 286.47 42.59 8.567 2.2059 1.5069 0.6005 0.6008

Table 9. Measured and calculated quantities for 0.73 beta ratio, tee at 19D, ETl at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra 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/m3) (kPa) (kg/s) (+10^)

46040990- 1 3.6970 286.73 43.78 4.278 1.9891 1.3563 0.5997 0.5998

46040990- 2 3.6938 286.80 43.73 4.267 1.9822 1.3514 0.5987 0.5988

46040990- 3 3.6020 286.67 42.66 5.445 2.2103 1.5091 0.5984 0.5985

46040990- 4 3.6028 286.62 42.68 5.443 2.2146 1.5122 0.5995 0.5997

46040990- 5 3.7941 287.29 44.84 2.459 1.5292 1.0401 0.6010 0.6010

46040990- 6 3.7878 287.31 44.77 2.491 1.5391 1.0468 0.6015 0.6016

46040990- 7 3.7439 287.29 44.25 3.187 1.7264 1.1749 0.5999 0.6000

46040990- 8 3.7435 287.11 44.27 3.173 1.7191 1.1705 0.5985 0.5986

46041090- 1 3.6967 287.29 43.69 3.988 1.9176 1.3058 0.5995 0.5996

46041090- 2 3.6824 287.33 43.51 4.116 1.9427 1.3230 0.5990 0.5991

46041090- 3 3.7301 287.28 44.08 3.338 1.7656 1.2018 0.6006 0.6007

46041090- 4 3.7296 287.37 44.06 3.361 1.7685 1.2035 0.5997 0.5998

46041090- 5 3.6353 286.91 43.02 5.494 2.2342 1.5239 0.5996 0.5998

46041090- 6 3.6327 286.08 43.12 5.480 2.2287 1.5233 0.5982 0.5984

46041090- 7 3.8207 287.36 45.15 2.540 1.5614 1.0615 0.6018 0.6018

46041090- 8 3.8165 287.35 45.10 2.563 1.5651 1.0641 0.6008 0.6008

I

40
Table 10. Measured and calculated quantities for 0.43 beta ratio, tee at 19D, FT6 at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

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

43040490- 1 3.9202 288.78 46.07 15.562 1.1400 0.7714 0.6030 0.6035

43040490- 2 3.9179 288.87 46.03 15.551 1.1386 0.7703 0.6027 0.6032

43040490- 3 3.8499 288.28 45.33 28.436 1.5254 1.0344 0.6013 0.6022

43040490- 4 3.8436 287.95 45.31 28.176 1.5182 1.0304 0.6013 0.6023

43040490- 5 3.9928 289.24 46.85 7.698 0.8095 0.5467 0.6040 0.6043

43040490- 6 3.9895 289.22 46.81 7.427 0.7947 0.5367 0.6039 0.6041

43040490- 7 3.6983 287.34 43.70 48.180 1.9487 1.3268 0.6003 0.6020

43040490- 8 3.6959 287.51 43.64 47.390 1.9268 1.3114 0.5990 0.6006

43040690- 1 3.6344 288.18 42.80 51.709 1.9862 1.3506 0.5966 0.5984

43040690- 2 3.6675 288.32 43.17 49.523 1.9590 1.3311 0.5988 0.6006

43040690- 3 3.6737 287.91 43.31 49.784 1.9672 1.3379 0.5988 0.6005

43040690- 4 3.9817 289.37 46.69 5.962 0.7108 0.4799 0.6039 0.6041

43040690- 5 3.9720 289.51 46.55 6.135 0.7206 0.4865 0.6043 0.6045

43040690- 6 3.7861 288.39 44.56 28.747 1.5143 1.0273 0.5988 0.5997

43040690- 7 3.7952 288.41 44.66 28.285 1.5028 1.0193 0.5984 0.5993

43040690- 8 3.8718 288:91 45.48 14.799 1.0956 0.7416 0.5981 0.5986

43040690- 9 3.8829 288.90 45.61 14.805 1.1003 0.7447 0.5997 0.6002

43040690- 10 3.8756 288.24 45.64 14.671 1.0978 0.7443 0.6009 0.6014

43040690- 11 3.8760 288.09 45.67 14.649 1.0974 0.7442 0.6009 0.6014

43040690- 12 3.8058 287.31 44.98 28.830 1.5233 1.0359 0.5987 0.5996

Table 11. Measured and calculated quantities for 0.55 beta ratio, tee at 19D, FT6 at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 urn Ra Orifice Diameter = 5.7142 cm (2.2497 in)

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

CY2

44040490- 1 3.8411 288.36 45.21 7.493 1.3362 0.9059 0.6029 0.6031

44040490- 2 3.8358 288.38 45.15 7.509 1.3340 0.9045 0.6018 0.6020

44040490- 3 3.9519 289.04 46.40 3.043 0.8664 0.5857 0.6057 0.6058

44040490- 4 3.9501 289.24 46.34 3.067 0.8713 0.5887 0.6071 0.6072

44040490- 5 3.7015 287.36 43.73 21.918 2.2472 1.5299 0.6024 0.6031

44040490- 6 3.6953 287.71 43.60 21.726 2.2306 1.5174 0.6015 0.6022

44040490- 7 3.8416 288.10 45.26 13.121 1.7686 1.1999 0.6026 0.6030

44040490- 8 3.8318 287.74 45.21 13.168 1.7699 1.2019 0.6023 0.6027

44040590- 1 3.8760 288.47 45.61 7.491 1.3424 0.9096 0.6033 0.6035

44040590- 2 3.8742 288.44 45.59 7.480 1.3378 0.9065 0.6017 0.6019

44040590- 3 3.9917 289.14 46.85 2.946 0.8540 0.5769 0.6039 0.6040

44040590- 4 3.9881 289.17 46.81 2.961 0.8592 0.5804 0.6063 0.6064

44040590- 5 3.6380 287.69 42.92 21.004 2.1799 1.4840 0.6025 0.6032

44040590- 6 3.6376 287.71 42.92 20.895 2.1715 1.4782 0.6018 0.6025

44040590- 7 3.7630 288.15 44.33 13.335 1.7598 1.1949 0.6010 0.6014

44040590- 8 3.7578 288.03 44.29 13.379 1.7653 1.1990 0.6021 0.6025

41
Table 12. Measured and calculated quantities for 0.67 beta ratio, tee at 19D, FT6 at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 pm Ra Orifice Diameter - 6.9840 cm (2.7496 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

45040590- 1 3.9254 288.63 46.16 3.379 1.4470 0.9794 0.6026 0.6027

45040590- 2 3.9217 288.69 46.11 3.365 1.4416 0.9757 0.6020 0.6021

45040590- 3 3.9413 288.85 46.31 2.635 1.2828 0.8677 0.6041 0.6041

45040590- 4 3.9365 288.78 46.27 2.629 1.2792 0.8655 0.6033 0.6033

45040590- 5 3.8126 288.06 44.93 5.943 1.8864 1.2804 0.6004 0.6005

45040590- 6 3.8065 288.21 44.83 5.941 1.8835 1.2781 0.6002 0.6004

45040590- 7 3.6688 287.50 43.32 8.788 2.2494 1.5315 0.5995 0.5997

45040590- 8 3.6687 287.98 43.24 8.789 2.2498 1.5299 0.6001 0.6003

45040690- 1 3.6497 286.54 43.25 8.533 2.2267 1.5199 0.6027 0.6030

45040690- 2 3.6442 287.23 43.07 8.519 2.2173 1.5110 0.6019 0.6022

45040690- 3 3.7510 287.08 44.36 5.968 1.8872 1.2849 0.6032 0.6033

45040690- 4 3.7418 287.27 44.22 5.964 1.8827 1.2814 0.6029 0.6031

45040690- 5 3.8599 287.79 45.54 2.623 1.2726 0.8638 0.6058 0.6059

45040690- 6 3.8547 287.83 45.47 2.628 1.2715 0.8630 0.6051 0.6052

45040690- 7 3.8076 287.42 44.98 4.088 1.5729 1.0693 0.6033 0.6034

45040690- 8 3.8048 287.48 44.94 4.070 1.5670 1.0652 0.6027 0.6028

Table 13. Me asured and1 calculated quantities for 0.73 beta ratio, tee at 19D , FT6 at IID.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^m Ra 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/m3) (kPa) (kg/s) (+10^)

46040590- 1 3.7797 288.37 44.48 4.105 1.9600 1.3299 0.5984 0.5985

46040590- 2 3.7778 288.04 44.52 4.096 1.9600 1.3309 0.5989 0.5990

46040590- 3 3.6619 287.81 43.19 5.691 2.2752 1.5480 0.5988 0.5989

46040590- 4 3.6615 288.04 43.14 5.682 2.2721 1.5450 0.5987 0.5989

46040590- 5 3.8540 288.12 45.41 2.782 1.6334 1.1079 0.5997 0.5998

46040590- 6 3.8538 288.40 45.36 2.811 1.6403 1.1119 0.5995 0.5996

46040590- 7 3.8144 288.25 44.92 3.429 1.8012 1.2219 0.5989 0.5990

46040590- 8 3.8116 288.23 44.89 3.427 1.8006 1.2216 0.5991 0.5991

46040690- 1 3.6445 287.96 42.96 5.707 2.2695 1.5438 0.5980 0.5982

46040690- 2 3.6407 287.73 42.95 5.689 2.2663 1.5426 0.5982 0.5983

46040690- 3 3.7849 288.47 44.53 3.455 1.8021 1.2224 0.5995 0.5996

46040690- 4 3.7783 288.11 44.51 3.461 1.8035 1.2244 0.5996 0.5997

46040690- 5 3.8165 288.33 44.93 2.699 1.6048 1.0885 0.6014 0.6014

46040690- 6 3.8120 288.38 44.86 2.708 1.6041 1.0879 0.6006 0.6006

46040690- 8 3.7097 288.47 43.64 4.091 1.9415 1.3180 0.5995 0.5996

42
Table 14. Measured and calculated quantities for 0.43 beta ratio, tee at 19D, FTl at IID.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 pm Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

43032090- 1 3.7557 287.21 44.40 49.445 1.9830 1.3497 0.5983 0.5999

43032090- 2 3.7503 286.84 44.40 48.996 1.9786 1.3479 0.5997 0.6014

43032090- 3 4.0411 288.54 47.54 6.415 0.7462 0.5045 0.6055 0.6057

43032090- 4 4.0217 288.69 47.29 6.610 0.7575 0.5121 0.6072 0.6074

43032090- 5 3.8411 287.93 45.29 28.370 1.5266 1.0361 0.6028 0.6037

43032090- 6 3.8345 287.63 45.26 27.942 1.5117 1.0269 0.6016 0.6026

43032090- 7 3.8891 288.21 45.81 15.112 1.1229 0.7612 0.6045 0.6050

43032090- 8 3.8799 287.99 45.74 14.992 1.1167 0.7575 0.6040 0.6045

43032390- 1 3.8628 288.22 45.49 15.325 1.1194 0.7591 0.6005 0.6010

43032390- 2 3.8607 288.26 45.46 15.341 1.1201 0.7595 0.6007 0.6012

43032390- 3 3.8016 287.81 44.84 27.774 1.4978 1.0174 0.6007 0.6016

43032390- 4 3.8007 287.66 44.86 27.706 1.4942 1.0153 0.5999 0.6008

43032390- 5 3.9679 288.74 46.64 6.540 0.7428 0.5024 0.6028 0.6030

43032390- 6 3.9855 288.96 46.81 6.080 0.7210 0.4873 0.6057 0.6059

43032390- 7 3.7221 287.61 43.93 48.715 1.9676 1.3384 0.6012 0.6029

43032390- 8 3.7152 287.49 43.87 48.189 1.9514 1.3279 0.5999 0.6016

Table 15. Measured and calculated quantities for 0.55 beta ratio. tee at 19D , FTl at IID.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 ^lm Ra Orifice Diameter •= 5.7142 cm (2.2497 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (4-106)

44032290- 1 3.8919 288.93 45.71 3.082 0.8668 0.5865 0.6067 0.6068

44032290- 1 3.8398 287.86 45.28 13.024 1.7570 1.1928 0.6007 0.6011

44032290- 2 3.8315 287.73 45.21 12.990 1.7541 1.1913 0.6010 0.6014

44032290- 3 3.6579 287.84 43.13 21.944 2.2176 1.5087 0.5982 0.5989

44032290- 4 3.6589 287.64 43.18 21.889 2.2218 1.5123 0.5997 0.6004

44032290- 5 4 . 0044 288.75 47.07 3.146 0.8858 0.5989 0.6048 0.6049

44032290- 6 3.9990 288.87 46.99 3.185 0.8935 0.6039 0.6068 0.6069

44032290- 7 3.9921 289.03 46.88 3.163 0.8896 0.6011 0.6070 0.6071

44032290- 8 3.8724 288.28 45.60 7.023 1.2981 0.8800 0.6025 0.6027

44032290- 9 3.8637 288.49 45.46 6.901 1.2851 0.8708 0.6026 0.6028

44032690- 1 3.7603 288.13 44.30 13.290 1.7580 1.1938 0.6016 0.6020

44032690- 2 3.7567 287.91 44.29 13.215 1.7540 1.1918 0.6019 0.6023

44032690- 3 3.6282 287.49 42.84 22.118 2.2355 1.5228 0.6027 0.6034

44032690- 4 3.6311 287.64 42.85 22.034 2.2294 1.5180 0.6021 0.6028

44032690- 5 3.9233 288.75 46.12 3.304 0.8991 0.6084 0.6051 0.6052

44032690- 6 3.9273 288.89 46.14 3.343 0.9046 0.6119 0.6050 0.6051

44032690- 7 3.8704 288.43 45.55 7.506 1.3444 0.9110 0.6039 0.6041

44032690- 8 3.8314 288.41 45.09 7.441 1.3314 0.9028 0.6037 0.6040

43
Table 16. Measured and calculated quantities for 0.67 beta ratio, tee at 19D, FTl at IID.

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

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

45032090- 1 3.8194 287.73 45.06 3.898 1.5401 1.0461 0.6044 0.6045

45032090- 2 3.8124 287.69 44.99 3.862 1.5364 1.0438 0.6063 0.6064

45032090- 3 3.8490 288.06 45.36 2.504 1.2392 0.8408 0.6049 0.6050

45032090- 4 3.8479 288.07 45.34 2.476 1.2323 0.8360 0.6049 0.6050

45032090- 5 3.7246 287.48 43.99 5.834 1.8574 1.2638 0.6030 0.6032

45032090- 6 3.7237 287.47 43.98 5.817 1.8530 1.2608 0.6025 0.6027

45032090- 7 3.7153 287.48 43.87 8.470 2.2345 1.5205 0.6027 0.6030

45032090- 8 3.6954 287.17 43.69 8.419 2.2191 1.5115 0.6017 0.6019

45032390- 1 3.8844 288.31 45.73 3.941 1.5569 1.0552 0.6032 0.6033

45032390- 2 3.8780 288.10 45.69 3.931 1.5575 1.0562 . 6044 0.6045

45032390- 3 3.9097 288.22 46.05 2.689 1.2921 0.8756 0.6039 0.6040

45032390- 4 3.8958 288.29 45.87 2.680 1.2866 0.8720 0.6036 0.6037

45032390- 5 3.7657 287.52 44.47 5.992 1.8892 1.2847 0.6020 0.6021

45032390- 6 3.7588 287.42 44.40 5.990 1.8865 1.2833 0.6016 0.6018

45032390- 7 3.6328 287.29 42.93 8.765 2.2394 1.5261 0.6003 0.6006

45032390- 8 3.6348 287.23 42.96 8.717 2.2371 1.5247 0.6011 0.6014

Table 17. Measured andI calculated iquantities for 0.73 beta ratio, tee at 19D , FTl at IID.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46032290- 1 3.7570 287.96 44.29 3.437 1.7930 1.2181 0.5997 0.5998

46032290- 2 3.7495 287.65 44.25 3.405 1.7885 1.2160 0.6013 0.6014

46032290- 3 3.7929 287.97 44.71 2.700 1.6004 1.0867 0.6011 0.6012

46032290- 4 3.7828 287.86 44.61 2.700 1.5955 1.0839 0.6000 0.6001

46032290- 5 3.6519 287.02 43.20 5.645 2.2765 1.5520 0.6015 0.6016

46032290- 6 3.6478 287.42 43.08 5.621 2.2650 1.5428 0.6006 0.6007

46032290- 7 3.7789 287.68 44.59 4.089 1.9690 1.3382 0.6017 0.6018

46032290- 8 3.7563 287.88 44.29 4.107 1.9638 1.3344 0.6008 0.6009

46032690- 1 3.8089 287.91 44.91 3.267 1.7607 1.1956 0.5998 0.5999

46032690- 2 3.8015 287.94 44.82 3.264 1.7583 1.1940 0.6000 0.6000

46032690- 3 3.8362 288.47 45.14 2.608 1.5784 1.0700 0.6003 0.6004

46032690- 4 3.8343 288.28 45.15 2.605 1.5778 1.0701 0.6004 0.6005

46032690- 5 3.6355 287.94 42.85 5.606 2.2504 1.5311 0.5990 0.5992

46032690- 6 3.6360 287.78 42.88 5.601 2.2491 1.5308 0.5987 0.5989

46032690- 7 3.7201 287.77 43.88 4.390 2.0162 1.3710 0.5994 0.5995

46032690- 8 3.7158 287.48 43.88 4.397 2.0187 1.3737 0.5997 0.5998

44
Table 18. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, FTl at 15D.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 /jm Ra Orifice Diameter = 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+106)

43090590- 1 4.0485 286.02 48.10 14.913 1.1393 0.7749 0.6026 0.6031

43090590- 2 4.0502 285.89 48.14 14.870 1.1391 0.7750 0.6031 0.6035

43090590- 3 3.9885 285.54 47.47 28.413 1.5575 1.0614 0.6003 0.6012

43090590- 4 3.9869 285.59 47.44 28.449 1.5588 1.0621 0.6006 0.6015

43090590- 5 4.1335 286.73 48.97 6.366 0.7573 0.5137 0.6079 0.6081

43090590- 6 3.9063 285.07 46.57 48.677 2.0294 1.3859 0.6026 0.6042

43090590- 7 3.8702 285.26 46.11 48.602 2.0181 1.3782 0.6027 0.6043

43090690- 1 3.8228 287.56 45.14 48.052 1.9787 1.3445 0.6007 0.6023

43090690- 2 3.8247 288.17 45.05 47.610 1.9638 1.3324 0.5994 0.6010

43090690- 3 3.9263 288.26 46.24 29.151 1.5600 1.0569 0.6013 0.6023

43090690- 4 3.9098 288.06 46.08 29.283 1.5603 1.0578 0.6011 0.6021

43090690- 5 3.9620 288.66 46.59 15.093 1.1286 0.7636 0.6028 0.6033

43090690- 6 3.9917 288.52 46.96 15.181 1.1373 0.7695 0.6033 0.6038

43090790- 1 4.0740 288.52 47.94 6.937 0.7783 0.5260 0.6048 0.6051

43090790- 2 4.0609 288.58 47.77 6.631 0.7618 0.5149 0.6067 0.6069

43090790- 3 4.0635 288 . 5.7 47.80 6.842 0.7732 0.5226 0.6059 0.6062

Table 19. Measured and calculated quantities for 0.55 beta ratio, tee at 17D, FTl at 15D.

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

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

44083090- 1 3.9774 285.36 47.37 5.976 1.2255 0.8356 0.6051 0.6053

44083090- 2 3.9786 285.23 47.41 5.974 1.2252 0.8356 0.6048 0.6050

44083090- 3 4.0921 286.27 48.57 2.679 0.8367 0.5684 0.6095 0.6096

44083090- 1 3.8027 285.02 45.34 21.138 2.2499 1.5386 0.6032 0.6039

44083090- 2 3.8005 285.60 45.21 21.181 2.2483 1.5354 0.6030 0.6037

44083090- 3 3.9259 285.62 46.71 13.864 1.8509 1.2620 0.6040 0.6044

44083090- 4 3.9366 285.76 46.81 13.932 1.8581 1.2663 0.6042 0.6046

44083090- 5 4.0981 286.92 48.52 2.592 0.8228 0.5581 0.6097 0.6098

44090790- 1 3.8980 287.58 46.02 13.157 1.7841 1.2111 0.6020 0.6024

44090790- 2 3.8965 286.91 46.13 13.132 1.7853 1.2139 0.6023 0.6027

44090790- 3 3.7878 287.29 44.77 21.145 2.2300 1.5168 0.6015 0.6022

44090790- 4 3.7998 286.75 45.00 21.126 2.2348 1.5219 0.6015 0.6022

44090790- 5 3.9845 288.07 46.96 3.016 0.8649 0.5858 0.6038 0.6039

44090790- 6 3.9853 288.18 46.95 2.816 0.8383 0.5677 0.6057 0.6058

44090790- 7 3.9571 287.36 46.76 7.786 1.3870 0.9414 0.6037 0.6039

44090790- 8 3.9552 287.53 46.71 7.817 1.3876 0.9414 0.6031 0.6034

45
Table 20. Measured and calculated quantities for 0.67 beta ratio, tee at 17D, FTl at 15D.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 6.9840 cm (2.7496 In)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

45083190- 1 3.7629 285.61 44.76 8.544 2.2667 1.5486 0.6028 0.6030

45083190- 2 3.7660 285.08 44.89 8.473 2.2597 1.5458 0.6026 0.6028

45083190- 3 3.8656 285.44 46.02 6.149 1.9529 1.3331 0.6038 . 6040

45083190- 4 3.8651 285.25 46.04 6.203 1.9628 1.3405 0.6041 0.6042

45083190- 5 4.0080 286.13 47.59 2.632 1.3074 0.8895 0.6077 0.6078

45083190- 6 4.0061 286.14 47.57 2.667 1.3190 0.8973 0.6091 0.6092

45090590- 1 3.9770 285.04 47.42 4.171 1.6421 1.1205 0.6073 0.6074

45090590- 2 3.9687 285.27 47.28 4.195 1.6452 1.1221 0.6076 0.6077

45090590- 3 3.9997 285.55 47.60 2.616 1.3028 0.8877 0.6074 0.6075

45090590- 4 4.0017 285.65 47.61 2.640 1.3079 0.8909 0.6070 0.6071

45090590- 5 3.9105 285.30 46.58 5.714 1.8977 1.2951 0.6050 0.6052

45090590- 6 3.9090 284.83 46.65 5.693 1.8956 1.2953 0.6050 0.6052

45090590- 7 3.8240 284.46 45.69 8.074 2.2274 1.5249 0.6031 0.6033

45090590- 8 3.8202 284.37 45.66 8.027 2.2239 1.5230 0.6041 0.6043

Table 21. Meiasured and calculated quantities for 0.73 beta ratio, tee at 17D , FTl at 15D.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+106)

46083090- 1 3.8723 284.64 46.24 4.196 2.0247 1.3847 0.5998 0.5999

46083090- 2 3.8671 284.94 46.12 4.180 2.0243 1.3835 0.6016 0.6017

46083090- 3 3.7650 284.04 45.06 5.489 2.2868 1.5683 0.6000 0.6001

46083090- 4 3.7693 283.88 45.14 5.492 2.2883 1.5699 0.5997 0.5998

46083090- 5 3.9461 284.74 47.11 2.680 1.6430 1.1224 0.6034 0.6035

46083090- 6 3.9410 284.60 47.07 2.666 1.6377 1.1192 0.6034 0.6034

46083090- 7 3.9144 284.35 46.80 3.207 1.7897 1.2242 0.6029 0.6030

46083090- 8 3.9095 284.94 46.63 3.217 1.7824 1.2175 0.6006 0.6007

46090690- 1 3.9071 287.74 46.10 3.255 1.7874 1.2127 0.6021 0.6021

46090690- 2 3.9064 287.78 46.09 3.256 1.7857 1.2115 0.6015 0.6016

46090690- 3 3.9454 288.28 46.46 2.504 1.5739 1.0660 0.6022 0.6022

46090690- 4 3.9405 288.22 46.41 2.528 1.5819 1.0716 0.6026 0.6027

46090690- 5 3.7902 287.39 44.78 5.368 2.2577 1.5353 0.6009 0.6010

46090690- 6 3.7904 288.14 44.65 5.357 2.2498 1.5271 0.6002 0.6003

46090690- 7 3 . 8443 287.94 45.32 4.392 2.0565 1.3957 0.6014 0.6016

46090690- 8 3.8426 287.76 45.34 4.403 2.0594 1.3983 0.6014 0.6016

46
Table 22. Measured and calculated quantities for 0.A3 beta ratio, tee at 17D, ITl at 15D.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 /im Ra Or Lfice Diameter - 4.4437 cm (1. 7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

43110990- 1 3.9287 284.91 46.87 28.068 1.5388 1.0510 0.6005 0.6015

43110990- 2 3.9277 284.36 46.96 28.028 1.5374 1.0515 0.5999 0.6008

43110990- 3 4.0621 286.02 48.26 6.744 0.7660 0.5209 0.6019 0.6021

43110990- 4 4.0532 286.01 48.15 6.139 0.7329 0.4985 0.6042 0.6044

43110990- 5 3.9898 285.21 47.54 14.802 1.1307 0.7711 0.6038 0.6043

43110990- 6 3.9846 285.12 47.50 14.591 1.1211 0.7648 0.6032 0.6037

43110990- 7 3.8516 284.07 46.09 45.730 1.9494 1.3354 0.6004 0.6019

43110990- 8 3.8435 283.87 46.03 45.593 1.9474 1.3348 0.6011 0.6026

43111490- 1 3.9614 288.47 46.61 15.220 1.1309 0.7655 0.6013 0.6018

43111490- 2 3.9590 288.95 46.50 15.328 1.1331 0.7661 0.6011 0.6016

43111490- 3 3.8285 287.52 45.21 48.133 1.9794 1.3450 0.5999 0.6015

43111490- 4 3.8269 287.83 45.14 47.951 1.9729 1.3396 0.5995 0.6011

43111490- 5 3.9129 288.48 46.04 28.755 1.5437 1.0454 0.6004 0.6014

43111490- 6 3.9106 288.47 46.01 29.176 1.5567 1.0543 0.6013 0.6022

43111490- 7 4.0643 289.64 47.61 6.689 0.7610 0.5130 0.6043 0.6045

43111490- 8 4.0608 289.43 47.61 6.414 0.7467 0.5037 0.6056 0.6058

Table 23. Me asured and calculated quantitie s for 0.55 beta ratio, tee at 17D , ITl at 15D.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 pm Ra 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/m3) (kPa) (kg/s) (+10^)

44111390- 1 3.8153 284.52 45.58 20.080 2.1881 1.4980 0.6004 0.6010

44111390- 2 3.8134 284.15 45.62 19.944 2.1804 1.4941 0.6000 0.6007

44111390- 3 3.9062 284.26 46.72 13.324 1.8104 1.2388 0.6026 0.6030

44111390- 4 3.9026 284.40 46.65 13.458 1.8133 1.2404 0.6010 0.6014

44111390- 1 4.1360 285.86 49.17 3.083 0.8944 0.6079 0.6036 0.6036

44111390- 2 4.1523 286.18 49.30 3.109 0.9025 0.6128 0.6057 0.6058

44111390- 3 4.0820 285.59 48.58 5.770 1.2191 0.8297 0.6049 0.6051

44111390- 4 4.0810 285.62 48.56 5.684 1.2104 0.8237 0.6052 0.6054

44111590- 1 3.9260 287.91 46.30 13.481 1.8164 1.2316 0.6037 0.6041

44111590- 2 3.9255 288.43 46.20 13.495 1.8144 1.2288 0.6033 0.6038

44111590- 3 3.9971 288.60 47.01 6.004 1.2228 0.8271 0.6046 0.6048

44111590- 4 3.9960 288.76 46.97 6.022 1.2237 0.8274 . 6044 0.6045

44111590- 5 3.8193 287.58 45.09 20.759 2.2207 1.5089 0.6024 0.6031

44111590- 6 3.8169 287.42 45.09 20.639 2.2134 1.5046 0.6022 0.6028

44111590- 7 4.0757 289.56 47.77 3.213 0.9029 0.6087 0.6055 0.6056

44111590- 8 4.0756 289.23 47.82 3.220 0.9033 0.6095 0.6048 0.6049

47
Table 24. Measured and calculated quantities for 0.67 beta ratio, tee at 17D, ITl at 15D.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 ^lm Ra 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/m3) (kPa) (kg/s) (4-10^)

45110990- 1 3.7988 284.01 45.47 8.197 2.2413 1.5366 0.6038 0.6040

45110990- 2 3.7930 284.21 45.36 8.248 2.2385 1.5340 0.6018 0.6021

45110990- 3 3.9592 284.56 47.30 2.651 1.2998 0.8882 0.6039 0.6040

45110990- 4 3.9614 284.66 47.31 2.665 1.3035 0.8904 0.6038 0.6039

45110990- 5 3.8768 284.57 46.31 5.899 1.9186 1.3123 0.6037 0.6039

45110990- 6 3.8742 284.99 46.20 5.891 1.9165 1.3096 0.6042 0.6044

45110990- 7 3.9346 284.59 47.00 3.927 1.5782 1.0786 0.6042 0.6043

45110990- 8 3.9298 284.84 46.89 3.932 1.5753 1.0761 0.6034 0.6035

45111490- 1 3.8784 289.27 45.50 6.039 1.9182 1.2972 0.6018 0.6020

45111490- 2 3.8747 287.70 45.73 5.986 1.9132 1.2987 0.6014 0.6015

45111490- 3 3.9654 288.67 46.63 2.583 1.2702 0.8593 0.6020 0.6021

45111490- 4 3.9648 288.43 46.66 2.585 1.2762 0.8638 0.6043 0.6044

45111490- 5 3.9340 288.31 46.32 4.115 1.5976 1.0822 0.6018 0.6019

45111490- 6 3.9326 288.40 46.29 4.103 1.5954 1.0805 0.6021 0.6022

45111490- 7 3.7960 288.09 44.73 8.211 2.2183 1.5059 0.6019 0.6021

45111490- 8 3.7977 288.61 44.66 8.226 2.2181 1.5038 0.6018 0.6020

Table 25. Meiasured and calculated quantities for 0.73 beta ratio, tee at 17D , ITl at 15D.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 pm Ra Orifice Diameter = 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46111390- 1 4.0551 284.88 48.39 2.534 1.6166 1.1025 0.6025 0.6026

46111390- 2 4.0445 284.53 48.33 2.540 1.6156 1.1029 0.6018 0.6019

46111390- 3 3.8676 284.19 46.26 5.147 2.2484 1.5395 0.6012 0.6014

46111390- 4 3.8660 285.33 46.04 5.170 2.2453 1.5331 0.6005 0.6006

46111390- 5 3.9772 284.19 47.58 3.232 1.8096 1.2374 0.6022 0.6023

46111390- 6 3.9740 284.13 47.55 3.259 1.8125 1.2396 0.6008 0.6009

46111390- 7 3.9289 284.00 47.04 4.159 2.0394 1.3960 0.6017 0.6018

46111390- 8 3.9288 284.01 47.03 4.146 2.0335 1.3919 0.6009 0.6010

46111590- 1 3.9531 288.17 46.57 3.253 1.7947 1.2158 0.6016 0.6017

46111590- 2 3.9488 288.08 46.54 3.245 1.7900 1.2129 0.6011 0.6012

46111590- 3 3.9811 288.95 46.76 2.529 1.5850 1.0714 0.6014 0.6015

46111590- 4 3.9830 288.84 46.80 2.530 1.5870 1.0730 0.6018 0.6018

46111590- 5 3.8412 288.06 45.27 5.145 2.2171 1.5043 0.5994 0.5995

46111590- 6 3.8399 288.07 45.25 5.147 2.2178 1.5048 0.5996 0.5997

46111590- 7 3.9000 288.50 45.88 4.140 2.0059 1.3586 0.6005 0.6006

46111590- 8 3.9006 288.57 45.88 4.137 2.0058 1.3584 0.6007 0.6008

Table 26. Measured and calculated quantities for 0.73 beta ratio,, tee at 17D, no fl<3W conditioner, flange taps at 3:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra Orifice Diameter - 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46112790- 1 3.9172 287.36 46.29 4.210 2.0345 1.3815 0.6014 0.6015

46112790- 2 3.9159 286.91 46.36 4.186 2.0286 1.3791 0.6010 0.6011

46112790- 3 3.9606 286.89 46.89 3.198 1.7858 1.2134 0.6020 0.6020

46112790- 4 3.9555 287.93 46.64 3.216 1.7819 1.2078 0.6005 0.6005

46112790- 5 3.8455 286.67 45.56 5.101 2.2176 1.5097 0.6003 0.6004

46112790- 6 3.8440 287.33 45.43 5.110 2.2201 1.5090 0.6014 0.6015

46112790- 7 3.9790 287.51 46.99 2.603 1.6176 1.0972 0.6036 0.6037

46112790- 8 3.9782 286.97 47.08 2.653 1.6357 1.1110 0.6041 0.6042

48
Table 27. Measured and calculated quantities for 0.73 beta ratio,

conditioner, flange taps at 9:00. tee at 17D, no flow

Pipe Diameter - 10.366 cm (4.081 in), 3.8 ^m Ra Orifice Diameter = 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46112790- 1 3.9172 287.36 46.29 4.203 2.0345 1.3815 0.6019 0.6020

46112790- 2 3.9159 286.91 46.36 4.156 2.0286 1.3791 0.6032 0.6033

46112790- 3 3.9606 286.89 46.89 3.190 1.7858 1.2134 0.6026 0.6026

46112790- 4 3.9555 287.93 46.64 3.214 1.7819 1.2078 0.6006 0.6007

46112790- 5 3.8455 286.67 45.56 5.088 2.2176 1.5097 0.6011 0.6012

46112790- 6 3 . 8440 287.33 45.43 5.099 2.2201 1.5090 0.6020 0.6021

46112790- 7 3.9790 287.51 46.99 2.611 1.6176 1.0972 0.6027 0.6027

46112790- 8 3.9782 286.97 47.08 2.666 1.6357 1.1110 0.6025 0.6026

Table 28. Measured and calculated quantities for 0.73 beta ratio tee at 17D, no fl DW conditioner, flange taps at 6:00.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 /jm Ra Orifice Diameter = 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46120490- 1 3.9617 285.98 47.07 3.387 1.8481 1.2585 0.6041 0.6042

46120490- 2 3.9593 287.15 46.83 3.421 1.8490 1.2556 0.6030 0.6030

46120490- 3 3.8316 286.91 45.35 5.566 2.3168 1.5765 0.6018 0.6019

46120490- 4 3.8295 286.48 45.40 5.597 2.3180 1.5790 0.6000 0.6002

46120490- 5 3.9090 286.19 46.40 4.350 2.0750 1.4132 0.6027 0.6028

46120490- 6 3.9053 286.54 46.29 4.348 2.0721 1.4100 0.6027 0.6028

46120490- 7 4.0006 286.57 47.42 2.562 1.6169 1.0989 0.6056 0.6056

46120490- 8 3.9918 286.22 47.38 2.558 1.6166 1.0998 0.6062 0.6062

Table 29. Measured and calculated quantities for 0.73 beta ratio tee at 17D, no fl 3W conditioner, flange taps at 12:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra 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/m3) (kPa) (kg/s) (^-10^)

46120490- 1 3.9617 285.98 47.07 3.447 1.8481 1.2585 0.5988 0.5989

46120490- 2 3.9593 287.15 46.83 3.474 1.8490 1.2556 0.5983 0.5984

46120490- 3 3.8316 286.91 45.35 5.653 2.3168 1.5765 0.5970 0.5972

46120490- 4 3.8295 286.48 45.40 5.645 2.3180 1.5790 0.5974 0.5976

46120490- 5 3.9090 286.19 46.40 4.411 2.0750 1.4132 0.5985 0.5986

46120490- 6 3.9053 286.54 46.29 4.417 2.0721 1.4100 0.5979 0.5980

46120490- 7 4.0006 286.57 47.42 2.613 1.6169 1.0989 0.5994 0.5995

46120490- 8 3.9918 286.22 47.38 2.613 1.6166 1.0998 0.5996 0.5996

49
Table 30. Measured and calculated quantities for

conditioner, flange taps at 3:00.

0.43 beta ratio, tee at 17D, no flow

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kg/m3) (kPa) (kg/s) (-1-106)

43112790- 1 3.9812 287.04 47.11 29.315 1.6045 1.0895 0.6113 0.6123

43112790- 2 3.9772 287.53 46.97 29.499 1.6014 1.0862 0.6090 0.6100

43112790- 3 4.1255 288.38 48.57 6.280 0.7596 0.5132 0.6167 0.6169

43112790- 4 4.1537 288.63 48.85 6.283 0.7616 0.5141 0.6164 0.6166

43112790- 5 3.8955 286.67 46.15 45.593 1.9728 1.3422 0.6083 0.6098

43112790- 6 3.8906 287.56 45.94 45.434 1.9666 1.3352 0.6089 0.6104

43112790- 7 4.0189 287.79 47.42 15.335 1.1674 0.7909 0.6135 0.6140

43112790- 8 4.0155 287.55 47.42 15.382 1.1671 0.7912 0.6123 0.6128

Table 31. Measured and calculated quantities for 0.43 beta ratio , tee at 17D, no fl(3W conditioner , flange taps at 9 : 00

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (-HO^)

43112790- 1 3.9812 287.04 47.11 29.327 1.6045 1.0895 0.6112 0.6121

43112790- 2 3.9772 287.53 46.97 29.486 1.6014 1.0862 0.6092 0.6101

43112790- 3 4.1255 288.38 48.57 6.282 0.7596 0.5132 0.6166 0.6168

43112790- 4 4.1537 288.63 48.85 6.283 0.7616 0.5141 0.6164 0.6166

43112790- 5 3.8955 286.67 46.15 45.616 1.9728 1.3422 0.6081 0.6096

43112790- 6 3.8906 287.56 45.94 45.461 1.9666 1.3352 0.6087 0.6102

43112790- 7 4.0189 287.79 47.42 15.353 1.1674 0.7909 0.6131 0.6136

43112790- 8 4.0155 287.55 47.42 15.396 1.1671 0.7912 0.6120 0.6125

Table 32. Measured and calculated quantities for 0.43 beta ratio , tee at 17D, no fl(3W conditioner, flange taps at 6:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 ^m Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) i+10^)

43120490- 1 3.8886 286.35 46.13 45.781 1.9770 1.3462 0.6085 0.6100

43120490- 2 3.8876 286.29 46.13 45.402 1.9698 1.3415 0.6088 0.6104

43120490- 3 3.9799 286.57 47.18 27.772 1.5550 1.0571 0.6082 0.6091

43120490- 4 3.9716 286.04 47.17 27.604 1.5561 1.0594 0.6106 0.6116

43120490- 5 4.1009 287.24 48.49 6.593 0.7764 0.5262 0.6158 0.6160

43120490- 6 4.1020 287.35 48.48 6.859 0.7890 0.5346 0.6134 0.6136

43120490- 7 4.0290 286.74 47.73 14.395 1.1288 0.7666 0.6101 0.6106

43120490- 8 4.0244 286.73 47.68 14.154 1.1212 0.7615 0.6116 0.6121

50
Table 33. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, no flow

conditioner, flange taps at 12:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 pm Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

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

43120490- 1 3.8886 286.35 46.13 45.695 1.9770 1.3462 0.6091 0.6106

43120490- 2 3.8876 286.29 46.13 45.236 1.9698 1.3415 0.6100 0.6116

43120490- 3 3.9799 286.57 47.18 27.752 1.5550 1.0571 0.6085 0.6094

43120490- 4 3.9716 286.04 47.17 27.518 1.5561 1.0594 0.6117 0.6126

43120490- 5 4.1009 287.24 48.49 6.576 0.7764 0.5262 0.6166 0.6168

43120490- 6 4.1020 287.35 48.48 6.847 0.7890 0.5346 0.6140 0.6142

43120490- 7 4.0290 286.74 47.73 14.395 1.1288 0.7666 0.6102 0.6106

43120490- 8 4.0244 286.73 47.68 14.128 1.1212 0.7615 0.6122 0.6127

Table 34. Measured and calculated quantities for 0.73 beta ratio tee at 17D, ITl at 15D,

flange taps at 3:00.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 ^m Ra Ori fice Diameter - 7.6197 cm (2. 9999 in)

Run ID Pressure Temperature Density Dif Pre ss Flow Rate Pipe Re No C CY2

(MPa) (K) (kgV) (kPa) (kg/s) (+106)

46112890- 1 3.9797 287.74 46.96 3.246 1.7855 1.2104 0.5968 0.5968

46112890- 2 3.9757 287.83 46.90 3.270 1.7939 1.2159 0.5978 0.5978

46112890- 3 3.8676 286.51 45.85 5.162 2.2247 1.5147 0.5967 0.5968

46112890- 4 3.8602 286.87 45.70 5.173 2.2183 1.5091 0.5953 0.5954

46112890- 5 3.9219 287.37 46.34 4.205 2.0216 1.3726 0.5975 0.5976

46112890- 6 3.9200 287.34 46.33 4.203 2.0162 1.3691 0.5962 0.5963

46112890- 7 3.9965 287.46 47.21 2.572 1.5988 1.0844 0.5988 0.5988

46112890- 8 3.9958 287.86 47.13 2.597 1.6010 1.0848 0.5972 0.5973

Table 35. Measured and calculated quantities for .73 beta ratio tee at 17D, ITl at 15D,

flange taps at 9 : 00

.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 ^m Ra 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/m3) (kPa) (kg/s) (-s-lO^)

46112890- 1 3.9797 287.74 46.96 3.206 1.7855 1.2104 0.6004 0.6005

46112890- 2 3.9757 287.83 46.90 3.237 1.7939 1.2159 0.6008 0.6008

46112890- 3 3.8676 286.51 45.85 5.094 2.2247 1.5147 0.6007 0.6008

46112890- 4 3.8602 286.87 45.70 5.093 2.2183 1.5091 0.6000 0.6001

46112890- 5 3.9219 287.37 46.34 4.160 2.0216 1.3726 0.6007 0.6008

46112890- 6 3.9200 287.34 46.33 4.145 2.0162 1.3691 0.6004 0.6005

46112890- 7 3.9965 287.46 47.21 2.537 1.5988 1.0844 0.6028 0.6029

46112890- 8 3.9958 287.86 47.13 2.556 1.6010 1.0848 0.6020 0.6020

51
Table 36. Measured and calculated quantities for 0.73 beta ratio, tee at 17D, ITl at 15D,

flange taps at 6:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 ^m Ra 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/m3) (kPa) (kg/s) (+10^)

46120390- 1 4.0003 285.97 47.53 2.483 1.5882 1.0810 6033 0.6034

46120390- 2 4.0208 286.63 47.65 2.486 1.5894 1.0798 6027 0.6028

46120390- 3 3.9179 286.01 46.54 4.045 2.0001 1.3626 6015 0.6016

46120390- 4 3.9118 286.31 46.41 4.041 1.9947 1.3580 6010 0.6011

46120390- 5 3.8176 285.68 45.40 5.516 2.3018 1.5713 6002 0.6003

46120390- 6 3.8194 285.48 45.46 5.513 2.3025 1.5725 6002 0.6003

46120390- 7 3.9414 286.77 46.68 3.326 1.8138 1.2331 6007 0.6008

46120390- 8 3.9321 286.01 46.71 3.338 1.8197 1.2395 6014 0.6014

Table 37. Measured and calculated quantities for 0.73 beta ratio tee at 17D, ITl at 15D,

flange taps at 12:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra 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/m3) (kPa) (kg/s) (+10^)

46120390- 1 4.0003 285.97 47.53 2.508 1.5882 1.0810 6003 0.6003

46120390- 2 4.0208 286.63 47.65 2.508 1.5894 1.0798 5999 0.6000

46120390- 3 3.9179 286.01 46.54 4.080 2.0001 1.3626 5989 0.5990

46120390- 4 3.9118 286.31 46.41 4.078 1.9947 1.3580 5982 0.5983

46120390- 5 3.8176 285.68 45.40 5.573 2.3018 1.5713 5971 0.5972

46120390- 6 3.8194 285.48 45.46 5.561 2.3025 1.5725 5976 0.5977

46120390- 7 3.9414 286.77 46.68 3.350 1.8138 1.2331 5985 0.5986

46120390- 8 3.9321 286.01 46.71 3.361 1.8197 1.2395 5993 0.5994

Table 38. Measured and calculated quantities for 0.43 beta ratio tee at 17D, ITl at 15D,

flange taps at 3 : 00

Pipe Diameter - 10.366 cm (4.081 in), 3.8 fim Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

43112890- 1 3.9791 287.31 47.03 28.346 1.5530 1.0539 0.6020 0.6029

43112890- 2 3.9739 287.96 46.86 28.415 1.5477 1.0487 0.6003 0.6013

43112890- 3 3.8783 286.93 45.90 48.332 1.9966 1.3578 0.5993 0.6009

43112890- 4 3.8804 287.13 45.89 48.042 1.9914 1.3536 0.5996 0.6012

43112890- 5 4.0925 288.39 48.18 6.626 0.7595 0.5134 0.6024 0.6027

43112890- 6 4.0897 288.51 48.12 7.447 0.8063 . 5449 0.6036 0.6038

43112890- 7 4.0239 287.84 47.47 14.152 1.1037 0.7476 0.6032 0.6036

43112890- 8 4.0232 288.07 47.42 14.057 1.0989 . 7440 0.6029 0.6034

52
Table 39. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, ITl at 15D,

flange taps at 9:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra Orifice Diameter = 4.4437 cm (1.7495 in)

Run ID Pressure

(MPa)

Temperature

(K)

Density Dif Press (kgV) (kPa)Flow Rate

(kg/s)

Pipe Re

(+10^) No • c CY2

43112890- 1 3.9791 287.31 47.03 28.326 1.5530 1.0539 6022 0.6031

43112890- 2 3.9739 287.96 46.86 28.411 1.5477 1.0487 6004 0.6013

43112890- 3 3.8783 286.93 45.90 48.260 1.9966 1.3578 5997 0.6013

43112890- 4 3.8804 287.13 45.89 47.983 1.9914 1.3536 6000 0.6016

43112890- 5 4.0925 288.39 48.18 6.622 0.7595 0.5134 6026 0.6029

43112890- 6 4.0897 288.51 48.12 7.436 0.8063 0.5449 6041 0.6043

43112890- 7 4.0239 287.84 47.47 14.129 1.1037 0.7476 6037 0.6041

43112890- 8 4.0232 288.07 47.42 14.049 1.0989 0.7440 6031 0.6035

Table 40. Measured and calculated quantities for 0.43 beta ratio tee at 17D, ITl at 15D,

flange taps at 6:00.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 /im Ra Orifice Diameter = 4.4437 cm (1.7495 in)

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

(MPa) (K) (kg/m3) (kPa) (kg/s) (+10^)

43120390- 1 4.0310 286.91 47.72 15.041 1.1394 0.7735 6024 0.6029

43120390- 2 4.0293 287.01 47.68 14.917 1.1333 0.7692 6019 0.6024

43120390- 3 3.8857 285.62 46.22 49.134 2.0175 1.3763 5985 0.6001

43120390- 4 3.8824 286.01 46.12 48.806 2.0058 1.3671 5977 0.5993

43120390- 5 3.9698 285.96 47.17 29.555 1.5843 1.0788 6005 0.6015

43120390- 6 3.9699 286.23 47.12 29.838 1.5890 1.0813 5998 0.6008

43120390- 7 4.1137 287.53 48.59 6.494 0.7548 0.5111 6022 0.6024

43120390- 8 4.1116 287.71 48.53 6.320 0.7458 0.5048 6036 0.6038

Table 41. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, ITl at 15D,

flange taps at 12:00.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 /im Ra

Run ID

Orifice Diameter

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

4.4437 cm (1.7495 in)

C CY2

43120390- 1 4.0310 286.91 47 72 15.063 1.1394 0.7735 0.6020 0.6025

43120390- 2 4.0293 287.01 47 68 14.941 1.1333 0.7692 0.6014 0.6019

43120390- 3 3.8857 285.62 46 22 49.171 2.0175 1.3763 0.5983 0.5999

43120390- 4 3.8824 286.01 46 12 48.878 2.0058 1.3671 0.5973 0.5989

43120390- 5 3.9698 285.96 47 17 29.576 1.5843 1.0788 0.6003 0.6013

43120390- 6 3.9699 286.23 47 12 29.869 1.5890 1.0813 0.5995 0.6004

43120390- 7 4.1137 287.53 48 59 6.499 0.7548 0.5111 0.6020 0.6022

43120390- 8 4.1116 287.71 48 53 6.335 0.7458 0.5048 0.6029 0.6031

53
Table 42. Measured and calculated quantities for 0.73 beta ratio, tee at 17D, FT2 at 15D,

flange taps at 3:00.

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 pm Ra Orifice Diameter - 7.6197 cm (2.9999 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

46120790- 1 46120790- 2 46120790

46120790

46120790

46120790

46120790

46120790

46121090

46121090

46121090

46121090

46121090

46121090

46121090

46121090

3.9697

3.9684

3.8637

3.8591

3.9862

3.9864

3.9173

3.9088

3.8433

3.8346

3.8933

3.8936

3.9704

3.9686

3.9413

3.9409

286.84

286.79

286.97

287.05

286.86

286.53

285.79

287.17

286.22

286.24

285.84

285.70

286.38

286.36

286.07

286.11

47.00

47.00

45.72

45.65

47.20

47.26

46.57

46.22

45.61

45.51

46.28

46.30

47.10

47.08

46.81

46.80

300

292

336

315

693

714

278

297

278

278

305

306

2.587

2.606

3.196

3.200

1.7985

1.7951

2.2491

2.2467

1.6335

1.6371

2.0378

2.0347

2 . 2444

2.2403

2.0400

2.0412

1.6026

1.6052

1.7710

1.7713

1.2220

1.2198

1.5297

1.5278

1.1097

1.1130

1.3891

1.3824

1.5296

1.5269

1.3907

1.3920

1.0901

1.0920

1.2060

1.2061

0.5959

0.5956

0.5941

0.5951

0.5979

0.5965

0.5958

0.5957

0.5969

0.5964

0.5964

0.5965

0.5992

0.5981

0.5976

0.5974

0.5959

0.5956

0.5943

0.5952

0.5980

0.5966

,5959

,5958

,5970

,5966

,5965

0.5966

0.5992

0.5982

0.5976

0.5975

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

flange taps at 9:00. tee at 17D, FT2 at 150,

Pipe Diameter - 10.366 cm (4.081 in), 3 . 8 ^ni Ra 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/m3) (kPa) (kg/s) (+106)

46120790- 1 3.9697 286.84 47.00 3.227 1.7985 1.2220 0.6026 0.6027

46120790- 2 3.9684 286.79 47.00 3.229 1.7951 1.2198 0.6013 0.6013

46120790- 3 3.8637 286.97 45.72 5.236 2.2491 1.5297 0.5998 0.5999

46120790- 4 3.8591 287.05 45.65 5.205 2.2467 1.5278 0.6013 0.6015

46120790- 5 3.9862 286.86 47.20 2.647 1.6335 1.1097 0.6031 0.6031

46120790- 6 3.9864 286.53 47.26 2.665 1.6371 1.1130 0.6019 0.6020

46120790- 7 3.9173 285.79 46.57 4.189 2.0378 1.3891 0.6021 0.6022

46120790- 8 3.9088 287.17 46.22 4.215 2.0347 1.3824 0.6015 0.6016

46121090- 1 3.8433 286.22 45.61 5.165 2 . 2444 1.5296 0.6034 0.6035

46121090- 2 3.8346 286.24 45.51 5.170 2.2403 1.5269 0.6027 0.6028

46121090- 3 3.8933 285.84 46.28 4.213 2 . 0400 1.3907 0.6029 0.6030

46121090- 4 3.8936 285.70 46.30 4.211 2.0412 1.3920 0.6032 0.6033

46121090- 5 3.9704 286.38 47.10 2.539 1.6026 1.0901 0.6048 0.6048

46121090- 6 3.9686 286.36 47.08 2.547 1.6052 1.0920 0.6049 0.6050

46121090- 7 3.9413 286.07 46.81 3.135 1.7710 1.2060 0.6034 0.6034

46121090- 8 3.9409 286.11 46.80 3.130 1.7713 1.2061 0.6039 0.6040

54

J
Table 44. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, FT2 at 15D,

flange taps a* 3:00.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /jm Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

43120790- 2 3.9686 286.14 47.12 28.588 1.5613 1.0627 0.6021 0.6030

43120790- 3 4.0128 287.18 47.46 14.478 1.1177 0.7585 0.6040 0.6045

43120790- 4 4.0098 287.11 47.43 14.457 1.1124 0.7550 0.6017 0.6022

43120790- 5 3.8814 285.48 46.20 46.320 1.9642 1.3404 0.6004 0.6019

43120790- 6 3.8782 285.43 46.17 46.085 1.9575 1.3361 0.6001 0.6016

43120790- 7 3.9590 285.78 47.07 29.194 1.5726 1.0714 0.6004 0.6014

43120790- 8 4.0983 287.59 48.39 6.118 0.7330 0.4964 0.6038 0.6040

43120790- 9 4.0982 287.72 48.37 6.812 0.7723 0.5228 0.6029 0.6031

43120790- 1 3.9388 286.18 46.76 34.066 1.6937 1.1531 0.6005 0.6016

43120790- 2 4.0136 287.26 47.45 10.476 0.9478 0.6430 0.6023 0.6026

43121090- 1 4.0376 286.95 47.79 15.224 1 . 1447 0.7769 0.6011 0.6016

43121090- 2 4.0371 287.22 47.74 15.216 1.1457 0.7771 0.6021 0.6026

43121090- 3 3.8989 285.40 46.42 47.242 1.9810 1.3519 0.5981 0.5997

43121090- 4 3.8760 285.58 46.12 47.026 1.9699 1.3441 0.5981 0.5996

43121090- 5 4.1107 287.29 48.60 7.011 0.7862 0.5327 0.6037 0.6039

43121090- 6 4.1109 287.57 48.55 6.769 0.7752 0.5249 0.6060 0.6063

43121090- 7 3.9767 286.40 47.17 27.367 1.5275 1.0389 0.6018 0.6027

43121090- 8 3.9779 286.42 47.18 27.212 1.5197 1.0335 0.6003 0.6012

Table 45. Measured and calculated quantities for 0.43 beta ratio , tee at 17D, FT2 at 15D,

flange taps at 9:00.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 /im Ra Orifice Diameter -= 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+10^)

43120790- 2 3.9686 286.14 47.12 28.534 1.5613 1.0627 0.6027 0.6036

43120790- 3 4.0128 287.18 47.46 14.462 1.1177 0.7585 . 6044 0.6048

43120790- 4 4.0098 287.11 47.43 14.433 1.1124 0.7550 0.6022 0.6027

43120790- 5 3.8814 285.48 46.20 46.219 1.9642 1.3404 0.6010 0.6026

43120790- 6 3.8782 285.43 46.17 45.958 1.9575 1.3361 0.6009 0.6024

43120790- 7 3.9590 285.78 47.07 29.145 1.5726 1.0714 0.6009 0.6019

43120790- 8 4.0983 287.59 48.39 6.107 0.7330 0.4964 0.6043 0.6045

43120790- 9 4.0982 287.72 48.37 6.802 0.7723 0.5228 0.6034 0.6036

43121090- 1 4.0376 286.95 47.79 15.204 1.1447 0.7769 0.6015 0.6020

43121090- 2 4.0371 287.22 47.74 15.189 1.1457 0.7771 0.6027 0.6032

43121090- 3 3.8989 285.40 46.42 47.100 1.9810 1.3519 0.5990 0.6006

43121090- 4 3.8760 285.58 46.12 46.892 1.9699 1.3441 0.5989 0.6005

43121090- 5 4.1107 287.29 48.60 6.993 0.7862 0.5327 0.6044 0.6047

43121090- 6 4.1109 287.57 48.55 6.751 0.7752 0.5249 0.6069 0.6071

43121090- 7 3.9767 286.40 47.17 27.322 1.5275 1.0389 0.6023 0.6032

43121090- 8 3.9779 286.42 47.18 27.163 1.5197 1.0335 0.6009 0.6018

55
Table 46. Measured and calculated quantities for 0.73 beta ratio, tee at 17D, FT4 at 15D,

flange taps at 3:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 fim Ra Orifice Diameter

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. C (MPa) (K) (kg/m3) (kPa) (kg/s) (-s-lO^)

7.6197 cm (2.9999 in)

CY2

46121290- 1 3.8673 284.96 46.12 5.085 2.2103 1.5106 0.5956 0.5957

46121290- 2 3.8676 285.45 46.04 5.061 2.2004 1.5020 0.5948 0.5949

46121290- 3 3.9576 285.49 47.11 3.213 1.7831 1.2157 0.5981 0.5982

46121290- 4 3.9557 286.93 46.82 3.241 1.7789 1.2086 0.5959 0.5960

46121290- 5 3.9879 286.06 47.36 2.527 1.5852 1.0789 0.5979 0.5980

46121290- 6 3.9894 286.03 47.39 2.531 1.5856 1.0792 0.5975 0.5975

46121290- 7 3.9268 286.94 46.48 4.232 2.0252 1.3764 0.5959 0.5960

46121290- 8 3.9093 286.24 46.40 4.227 2.0195 1.3752 0.5950 0.5951

46040891- 1 3.9301 286.66 46.57 4.120 2.0056 1.3640 0.5975 0.5976

46040891- 2 3.9093 285.44 46.54 4.089 1.9958 1.3617 0.5970 0.5971

46040891- 3 3.8350 286.77 45.42 5.121 2.2026 1.4993 0.5959 0.5961

46040891- 4 3.8384 285.73 45.64 5.080 2.1994 1.5009 0.5960 0.5962

46040891- 5 3.9675 285.83 47.16 2.545 1.5903 1.0832 0.5990 0.5991

46040891- 6 3.9688 286.47 47.06 2.578 1.6014 1.0891 0.5999 0.6000

46040891- 7 3.9373 285.98 46.78 3.216 1.7798 1.2123 0.5988 0.5989

46040891- 8 3.9360 286.45 46.68 3.226 1.7812 1.2119 0.5990 0.5991

46040891- 9 3.9357 286.44 46.67 3.216 1.7811 1.2119 0.5999 0.6000

Table 47. Measured and calculated quantities for 0..73 beta ratio, tee at 17D, FT4 at 15D,

flange taps at 9:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 ^m Ra 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/m3) (kPa) (kg/s) (+10^)

46121290- 1 3.8673 284.96 46.12 4.974 2.2103 1.5106 0.6021 0.6023

46121290- 2 3.8676 285.45 46.04 4.955 2.2004 1.5020 0.6011 0.6013

46121290- 3 3.9576 285.49 47.11 3.151 1.7831 1.2157 0.6040 0.6041

46121290- 4 3.9557 286.93 46.82 3.177 1.7789 1.2086 0.6019 0.6019

46121290- 5 3.9879 286.06 47.36 2.486 1.5852 1.0789 0.6029 0.6030

46121290- 6 3.9894 286.03 47.39 2.491 1.5856 1.0792 0.6022 0.6023

46121290- 7 3.9268 286.94 46.48 4.157 2.0252 1.3764 0.6012 0.6013

46121290- 8 3.9093 286.24 46.40 4.135 2.0195 1.3752 0.6017 0.6018

46040891- 1 3.9301 286.66 46.57 4.075 2.0056 1.3640 0.6008 0.6009

46040891- 2 3.9093 285.44 46.54 4.038 1.9958 1.3617 0.6008 0.6009

46040891- 3 3.8350 286.77 45.42 5.053 2.2026 1.4993 0.5999 0.6001

46040891- 4 3.8384 285.73 45.64 5.010 2.1994 1.5009 0.6002 0.6003

46040891- 5 3.9675 285.83 47.16 2.524 1.5903 1.0832 0.6014 0.6015

46040891- 6 3.9688 286.47 47.06 2.556 1.6014 1.0891 0.6026 0.6026

46040891- 7 3.9373 285.98 46.78 3.178 1.7798 1.2123 0.6023 0.6024

46040891- 8 3.9360 286.45 46.68 3.183 1.7812 1.2119 0.6030 0.6030

46040891- 9 3.9357 286.44 46.67 3.184 1.7811 1.2119 0.6029 0.6030

56
Table 48. Measured and calculated quantities for 0.43 beta ratio, tee at 17D, FT4 at 15D,

flange taps at 3:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

(MPa) (K) (kgV) (kPa) (kg/s) (+106)

43121190- 1 4.0143 286.67 47.57 14.503 1.1157 0.7580 0.6017 0.6022

43121190- 2 4.0102 286.73 47.51 14.503 1.1157 0.7579 0.6021 0.6026

43121190- 3 3.8728 286.71 45.88 47.474 1.9741 1.3433 0.5981 0.5996

43121190- 4 3.8744 286.64 45.91 47.286 1.9717 1.3419 0.5983 0.5999

43121190- 5 3.9596 285.75 47.08 28.324 1.5469 1.0540 0.5996 0.6005

43121190- 6 3.9578 286.13 46.99 28.630 1.5539 1.0578 0.5996 0.6005

43121190- 7 4.0911 287.53 48.32 7.198 0.7958 0.5390 0.6047 0.6050

43121190- 8 4.0984 287.48 48.42 7.161 0.7966 0.5396 0.6064 0.6066

43121290- 1 3.9839 286.51 47.24 28.345 1.5462 1.0513 0.5981 0.5990

43121290- 2 3.9812 286.64 47.18 28.353 1.5482 1.0523 0.5991 0.6000

43121290- 3 4.1404 287.42 48.93 6.197 0.7400 0.5011 0.6024 0.6026

43121290- 4 4.1158 287.61 48.60 7.438 0.8078 0.5469 0.6022 0.6024

43121290- 5 3.8808 285.34 46.21 46.971 1.9675 1.3432 0.5971 0.5987

43121290- 6 3.8858 286.48 46.07 47.028 1.9664 1.3386 0.5973 0.5988

43121290- 7 4.0210 286.42 47.69 15.232 1.1439 0.7775 0.6011 0.6016

43121290- 8 4.0181 286:61 47.62 15.268 1 . 1440 0.7773 0.6010 0.6015

Table 49. Measured and calculated quantities for 0.43 beta ratio tee at 17D, FT4 at 15D,

flange taps at 9:00.

Pipe Diameter - 10.366 cm (4.081 in), 3.8 /im Ra Orifice Diameter - 4.4437 cm (1.7495 in)

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

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

43121190- 1 4.0143 286.67 47.57 14.538 1.1157 0.7580 0.6010 0.6014

43121190- 2 4.0102 286.73 47.51 14.540 1.1157 0.7579 0.6013 0.6018

43121190- 3 3.8728 286.71 45.88 47.358 1.9741 1.3433 0.5988 0.6004

43121190- 4 3.8744 286.64 45.91 47.209 1.9717 1.3419 0.5988 0.6004

43121190- 5 3.9596 285.75 47.08 28.307 1.5469 1.0540 0.5997 0.6007

43121190- 6 3.9578 286.13 46.99 28.619 1.5539 1.0578 0.5997 0.6007

43121190- 7 4.0911 287.53 48.32 7.235 0.7958 0.5390 0.6032 0.6034

43121190- 8 4.0984 287.48 48.42 7.195 0.7966 0.5396 0.6049 0.6051

43121290- 1 3.9839 286.51 47.24 28.280 1.5462 1.0513 0.5988 0.5997

43121290- 2 3.9812 286.64 47.18 28.278 1.5482 1.0523 0.5999 0.6008

43121290- 3 4.1404 287.42 48.93 6.187 0.7400 0.5011 0.6029 0.6031

43121290- 4 4.1158 287.61 48.60 7.418 0.8078 0.5469 0.6030 0.6033

43121290- 5 3.8808 285.34 46.21 46.818 1.9675 1.3432 0.5981 0.5996

43121290- 6 3.8858 286.48 46.07 46.888 1.9664 1.3386 0.5982 0.5997

43121290- 7 4.0210 286.42 47.69 15.200 1.1439 0.7775 0.6018 0.6023

43121290- 8 4.0181 286.61 47.62 15.241 1 . 1440 0.7773 0.6015 0.6020

57

BL-114A

(5-90) U.S. DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

BIBLIOGRAPHIC DATA SHEET

1. PUBUCATION OR REPORT NUMBER

NIST TN 1352

2. PERFORMING ORQANIZATION REPORT NUMBER B91-0281

3. PUBUCATION DATE

4. TITLE AND SUBTITLE The Effects of Flow Conditioners and Tap Location on Orifice Flo\^7meter Performance

5. AUTHOR(S)

J.L. Scott, C.F. Sindt, M.A. Lewis and J. A. Brennan

6. PERPORMINQ ORQANIZATION (IF JOINT OR OTHER THAN NIST, SEE INSTRUCTIONS)

U.S. DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

BOULDER, COLORADO 80303-3328

7. CONTRACT/GRANT NUMBER

5088-271-1680

8. TYPE OF REPORT AND PERIOD COVERED

Tech. Note 02/90 - 12/90

9. SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (STREET, CITY, STATE, ZIP) Gas Research Institute

8600 West Bryn Mawr Avenue

Chicago, IL 60631-3564

10. SUPPLEMENTARY NOTES

This publication is also referenced as Gas Research Institute Report Number GRI-91-0229.

11. ABSTRACT (A 200-WORO OR LESS FACTUAL SUMMARY OF MOST SIGNIFICANT INFORMATION. IF DOCUMENT INCLUDES A SIGNIFICANT BIBUOGRAPHY OR

UTERATURE SURVEY, MENTION IT HERE.) Current research is being conducted to provide information which will be used to improve the

existing industry standards for proper installation of orifice meters. This research

includes experimental investigation of a Zanker, an etoile, and several tube bundle flow

conditioners at various positions relative to the orifice plate. Also included are the

effects of pressure tap location, both with and without flow conditioning, as reflected in

determination of discharge coefficients.

Of the flow conditioners tested at approximately 11 pipe diameters upstream of the orifice

plate, the Zanker flow conditioner resulted in discharge coefficients most similar to

baseline values. There was only a slight difference in orifice meter performance when a flanged or an in-line tube bundle flow conditioner was used at the tested location upstream

of the orifice plate. The effect of pressure tap location was found to be significant with

the 0.73 beta ratio plate. Recommendations for future research, as a result of these

findings, are included.

12. KEY WORDS (6 TO 12 ENTRIES; ALPHABETICAL ORDER; CAPITAUZE ONLY PROPER NAMES; AND SEPARATE KEY WORDS BY SEMICOLONS)

discharge coefficient; etoile; flow conditioner; flow disturbance; flow measurement; gas;

orifice flowmeter; tap location; tube bundle; Zanker

13. AVAILABIUTY UNUMITED

FOR OFFICIAL DISTRIBUTION. DO NOT RELEASE TO NATIONAL TECHNICAL INFORMATION SERVICE (NTIS). ORDER FROM SUPERINTENDENT OF DOCUMENTS, U.S. GOVERNMENT PRINTING OFFICE, WASHINGTON, DC 20402. ORDER FROM NATIONAL TECHNICAL INFORMATION SERVICE (NTIS), SPRINGFIELD. VA 22161.

14. NUMBER OF PRINTED PAGES

72

IS. PRICE

ELECTRONIC FORM

'^U.S. GOVERNMENT PRINTING OmCE: 1991 - 673-591/65007

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