r^-l^i^l

NisrUNITED STATES

DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS

AND TECHNOLOGY

NAT L INST. OF STAND & TECH R.I.C.

A111D3 7St,E7fi

NIST Technical Note 1344

MIST

PUBUCATIONS

J

Qc too

Orifice Meter Performance

Downstream of a Tube Bundle Flow

Conditioner, Elbows, and a Tee

Charles F. Sindt

Michael A. Lewis

James A. Brennan

Chemical Engineering Science Division

Center for Chemical Technology

National Measurement Laboratory

National Institute of Standards and Technology

Boulder, Colorado 80303-3328

Sponsored by

Gas Research Institute

8600 West Bryn Mawr Avenue

Chicago, Illinois 60631

\

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

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

Issued December 1 990
National Institute of Standards and Technology Teclinicai Note 1344

Natl. Inst. Stand. Technol., Tech. Note 1344, 74 pages (Dec. 1990)

CODEN:NTNOEF

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1990

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

Page

CROSS REFERENCE CHART xi

ABSTRACT 1 INTRODUCTION 1 EXPERIMENTAL PROGRAM 3 TEST RESULTS 4 Baseline Data 4 Flow Conditioner Location Tests 4 Inlet Disturbance Tests 6

CONCLUSIONS 7 RECOMMENDATIONS 8

REFERENCES 8

111
List of Figures

Page

Figure l.a Four-inch orifice meter, 4 6 pipe diameters of straight pipe

upstream 10

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

diameters 10

Figure l.c Four-inch orifice meter, 56-inch pipe diameters of straight

pipe upstream 10

Figure 2 . In-line tube bundle 11

Figure 3. Test configuration with two elbows in plane at 19 pipe

diameters from the orifice plate 11

Figure 4. Test configuration with a tee at 19 pipe diameters from the

orifice plate 12

Figure 5. Test configuration with two elbows out-of -plane at 19 pipe

diameters from the orifice plate 12

Figure 6. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate, baseline data 13

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

ratio orifice plate, baseline data 13

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

ratio orifice plate, baseline data 14

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

ratio orifice plate, baseline data 14

Figure 10. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate with the in-line tube bundle at 7 pipe

diameters 15

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

ratio orifice plate with the in-line tube bundle at 7 pipe

diameters 15

Figure 12. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate with the in-line tube bundle at 7 pipe

diameters 16

Figure 13. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate with the in-line tube bundle at 7 pipe

diameters 16

Figure 14. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate with the in-line tube bundle at 11 pipe

diameters 17

Figure 15. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate with the in-line tube bundle at 11 pipe

diameters 17

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

ratio orifice plate with the in-line tube bundle at 11 pipe

diameters 18

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

ratio orifice plate with the in-line tube bundle at 11 pipe

diameters 18

IV
List of Figures (continued)

Page

Figure 18. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate with the in-line tube bundle at 17 pipe

diameters 19

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

ratio orifice plate with the in-line tube bundle at 17 pipe

diameters 19

Figure 20. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate with the in-line tube bundle at 17 pipe

diameters 2 Figure 21. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate with the in-line tube bundle at 27 pipe

diameters 20

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

ratio orifice plate with the in-line tube bundle at 27 pipe

diameters 21

Figure 23. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate with the in-line tube bundle at 27 pipe

diameters 21

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

ratio orifice plate with the in-line tube bundle at 27 pipe

diameters and the 6-inch Sprenkle at 4 6 pipe diameters 22

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

ratio orifice plate with the in-line tube bundle at 27 pipe

diameters and the 6-inch Sprenkle at 4 6 pipe diameters 22

Figure 26. Percent change in the orifice discharge coefficient vs. flow

conditioner location for the 0.55 beta ratio orifice plate... 23

Figure 27. Percent change in the orifice discharge coefficient vs. flow

conditioner location for the 0.67 beta ratio orifice plate... 23

Figure 28. Percent change in the orifice discharge coefficient vs. flow

conditioner location for the 0.73 beta ratio orifice plate... 24

Figure 29. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate at 19 pipe diameters from two elbows in

plane 24

Figure 30. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate at 19 pipe diameters from two elbows in

plane 25

Figure 31. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate at 19 pipe diameters from two elbows in

plane 25

Figure 32. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate at 19 pipe diameters from two elbows in

plane 2 6 Figure 33. Percent change in the orifice discharge coefficient vs. beta

ratio for the orifice plate 19 diameters from two elbows in

plane 26

Figure 34. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 0.76 /im upstream pipe 27

V
List of Figures (continued)

Page

Figure 35. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 0.76 /im upstream pipe 27

Figure 36. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 0.76 /nm upstream pipe 28

Figure 37. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 0.76 iJ.m upstream pipe 28

Figure 38. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 3.8 ^m upstream pipe 29

Figure 39. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 3.8 /Ltro upstream pipe 29

Figure 40. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 3.8 iim upstream pipe 30

Figure 41. Discharge coefficient vs. Reynolds number for the 0.73 beta

ratio orifice plate at 19 pipe diameters from a tee and with

the 3.8 jum upstream pipe 30

Figure 42. Percent change in the orifice discharge coefficient vs. beta

ratio for the tee at 19 pipe diameters from the orifice

plate 31

Figure 43. Discharge coefficient vs. Reynolds number for the 0.43 beta

ratio orifice plate at 19 pipe diameters from two elbows outof-plane 31

Figure 44. Discharge coefficient vs. Reynolds number for the 0.55 beta

ratio orifice plate at 19 pipe diameters from two elbows outof-plane 32

Figure 45. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate at 19 pipe diameters from two elbows outof-plane 32

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

ratio orifice plate at 19 pipe diameters from two elbows outof-plane 33

Figure 47. Percent change in the orifice discharge coefficient vs. beta

ratio for two elbows out-of-plane at 19 pipe diameters from

the orifice plate 33

VI
List of Tables

Page

Table l.a. Measured and calculated quantities for the beta ratio of 0.43

with the 3.8 /xm upstream pipe and 4 6 pipe diameters of

straight pipe upstream of the orifice plate 34

Table l.b. Measured and calculated quantities for the beta ratio of 0.43

with the 6-inch Sprenkle 46 pipe diameters upstream of the

orifice plate 34

Table 2. a. Measured and calculated quantities for the beta ratio of 0.55

with the 3.8 jim upstream pipe and 46 pipe diameters of

straight pipe upstream of the orifice plate 35

Table 2.b. Measured and calculated quantities for the beta ratio of 0.55

with the 6-inch Sprenkle 46 pipe diameters upstream of the

orifice plate 35

Table 3. a. Measured and calculated quantities for the beta ratio of 0.67

with the 3.8 /xm upstream pipe and 4 6 pipe diameters of

straight pipe upstream of the orifice plate 36

Table 3.b. Measured and calculated quantities for the beta ratio of 0.67

with the 3.8 ^m upstream pipe and 56 pipe diameters of

straight pipe upstream of the orifice plate 36

Table 3.c. Measured and calculated quantities for the beta ratio of 0.67

with the 6-inch Sprenkle 46 pipe diameters upstream of the

orifice plate 36

Table 4. a. Measured and calculated quantities for the beta ratio of 0.73

with the 3.8 nm upstream pipe and 46 pipe diameters of

straight pipe upstream of the orifice plate 37

Table 4.b. Measured and calculated quantities for the beta ratio of 0.73

with the 3.8 /um upstream pipe and 56 pipe diameters of

straight pipe upstream of the orifice plate 37

Table 4.C. Measured and calculated quantities for the beta ratio of 0.73

with the 6-inch Sprenkle 46 pipe diameters upstream of the

orifice plate 37

Table 5. Measured and calculated quantities for the beta ratio of 0.43

with the in-line tube bundle at 7 pipe diameters upstream of

the orifice plate 38

Table 6. Measured and calculated quantities for the beta ratio of 0.55

with the in-line tube bundle at 7 pipe diameters upstream of

the orifice plate 38

Table 7. Measured and calculated quantities for the beta ratio of 0.67

with the in-line tube bundle at 7 pipe diameters upstream of

the orifice plate 39

Table 8. Measured and calculated quantities for the beta ratio of 0.73

with the in-line tube bundle at 7 pipe diameters upstream of

the orifice plate 39

Table 9. Measured and calculated quantities for the beta ratio of 0.43

with the in-line tube bundle at 11 pipe diameters upstream of

the orifice plate 40

Table 10. Measured and calculated quantities for the beta ratio of 0.55

with the in-line tube bundle at 11 pipe diameters upstream of

the orifice plate 40

VI
List of Tables (continued)

Page

Table 11. Measured and calculated quantities for the beta ratio of 0.67

with the in-line tube bundle at 11 pipe diameters upstream of

the orifice plate 41

Table 12. Measured and calculated quantities for the beta ratio of 0.73

with the in-line tube bundle at 11 pipe diameters upstream of

the orifice plate 41

Table 13. Measured and calculated quantities for the beta ratio of 0.55

with the in-line tube bundle at 17 pipe diameters upstream of

the orifice plate 42

Table 14. Measured and calculated quantities for the beta ratio of 0.67

with the in-line tube bundle at 17 pipe diameters upstream of

the orifice plate 42

Table 15. Measured and calculated quantities for the beta ratio of 0.73

with the in-line tube bundle at 17 pipe diameters upstream of

the orifice plate 43

Table 16. Measured and calculated quantities for the beta ratio of 0.55

with the in-line tube bundle at 27 pipe diameters upstream of

the orifice plate 43

Table 17. Measured and calculated quantities for the beta ratio of 0.67

with the in-line tube bundle at 27 pipe diameters upstream of

the orifice plate 44

Table 18. Measured and calculated quantities for the beta ratio of 0.73

with the in-line tube bundle at 27 pipe diameters upstream of

the orifice plate 45

Table 19. Measured and calculated quantities for the beta ratio of 0.67

with the in-line tube bundle at 27 pipe diameters upstream of

the orifice plate and with the 6-inch Sprenkle at 46 pipe

diameters upstream of the orifice plate 46

Table 20. Measured and calculated quantities for the beta ratio of 0.73

with the in-line tube bundle at 27 pipe diameters upstream of

the orifice plate and with the 6-inch Sprenkle at 46 pipe

diameters upstream of the orifice plate 46

Table 21. Measured and calculated quantities for the beta ratio of 0.43

with two elbows in plane at 19 pipe diameters upstream of the

orifice plate. 47

Table 22. Measured and calculated quantities for the beta ratio of 0.55

with two elbows in plane at 19 pipe diameters upstream of the

orifice plate 47

Table 23. Measured and calculated quantities for the beta ratio of 0.67

with two elbows in plane at 19 pipe diameters upstream of the

orifice plate 47

Table 24. Measured and calculated quantities for the beta ratio of 0.73

with two elbows in plane at 19 pipe diameters upstream of the

orifice plate 48

Table 25. Measured and calculated quantities for the beta ratio of 0.43

with two elbows in plane upstream of the in-line tube bundle

at 17 pipe diameters upstream of the orifice plate 48

Vlll
List of Tables (continued)

Page

Table 26. Measured and calculated quantities for the beta ratio of 0.55

with two elbows in plane upstream of the in-line tube bundle

at 17 pipe diameters upstream of the orifice plate 49

Table 27. Measured and calculated quantities for the beta ratio of 0.67

with two elbows in plane upstream of the in-line tube bundle

at 17 pipe diameters upstream of the orifice plate 49

Table 28. Measured and calculated quantities for the beta ratio of 0.73

with two elbows in plane upstream of the in-line tube bundle

at 17 pipe diameters upstream of the orifice plate 50

Table 29. Measured and calculated quantities for the beta ratio of 0.43

and the 0.7 6 /im upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 50

Table 30. Measured and calculated quantities for the beta ratio of 0.55

and the 0.76 /xm upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 51

Table 31. Measured and calculated quantities for the beta ratio of 0.67

and the 0.76 jum upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 51

Table 32. Measured and calculated quantities for the beta ratio of 0.73

and the 0.76 ^m upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 52

Table 33. Measured and calculated quantities for the beta ratio of 0.43

and the 0.7 6 fxm upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 52

Table 34. Measured and calculated quantities for the beta ratio of 0.55

and the 0.7 6 /xm upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 53

Table 35. Measured and calculated quantities for the beta ratio of 0.67

and the 0.7 6 /xm upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 53

Table 36. Measured and calculated quantities for the beta ratio of 0.73

and the 0.76 jiim upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 54

Table 37. Measured and calculated quantities for the beta ratio of 0.43

and the 3.8 /xm upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 54

Table 38. Measured and calculated quantities for the beta ratio of 0.55

and the 3.8 iJ,m upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 54

Table 39. Measured and calculated quantities for the beta ratio of 0.67

and the 3 . 8 /xm upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 55

Table 40. Measured and calculated quantities for the beta ratio of 0.73

and the 3 . 8 /xm upstream pipe with a tee at 19 pipe diameters

upstream of the orifice plate 55

IX
List of Tables (continued)

Page

Table 41. Measured and calculated quantities for the beta ratio of 0.43

and the 3.8 fim upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 55

Table 42. Measured and calculated quantities for the beta ratio of 0.55

and the 3.8 ^m upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 56

Table 43. Measured and calculated quantities for the beta ratio of 0.67

and the 3.8 /xm upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 56

Table 44. Measured and calculated quantities for the beta ratio of 0.73

and the 3.8 /im upstream pipe with a tee upstream of the inline tube bundle at 17 pipe diameters upstream of the orifice

plate 57

Table 45. Measured and calculated quantities for the beta ratio of 0.43

with two elbows out-of-plane at 19 pipe diameters upstream of

the orifice plate 57

Table 46. Measured and calculated quantities for the beta ratio of 0.55

with two elbows out-of-plane at 19 pipe diameters upstream of

the orifice plate 58

Table 47. Measured and calculated quantities for the beta ratio of 0.67

with two elbows out-of-plane at 19 pipe diameters upstream of

the orifice plate 58

Table 48. Measured and calculated quantities for the beta ratio of 0.73

with two elbows out-of-plane at 19 pipe diameters upstream of

the orifice plate 59

Table 49. Measured and calculated quantities for the beta ratio of 0.43

with two elbows out-of-plane and the in-line tube bundle at 17

pipe diameters upstream of the orifice plate 59

Table 50. Measured and calculated quantities for the beta ratio of 0.55

with two elbows out-of-plane and the in-line tube bundle at 17

pipe diameters upstream of the orifice plate 60

Table 51. Measured and calculated quantities for the beta ratio of 0.67

with two elbows out-of-plane and the in-line tube bundle at 17

pipe diameters upstream of the orifice plate 60

Table 52. Measured and calculated quantities for the beta ratio of 0.73

with two elbows out-of-plane and the in-line tube bundle at 17

pipe diameters upstream of the orifice plate 61
CROSS REFERENCE CHART

Beta Ratio

Fig.

No.

Table

No.

Test

0.43 0.55 0.67 0.73 Configuration

6 X la, lb Baseline

7 X 2a, 2b Baseline

8 X 3a, 3b, 3c Baseline

9 X 4a, 4b, 4c Baseline

10 X 5 Fig. la

11 X 6 Fig. la

12 X 7 Fig. la

13 X 8 Fig. la

14 X 9 Fig. la

15 X 10 Fig. la

16 X 11 Fig. la

17 X 12 Fig. la

18 X 13 Fig. la

19 X 14 Fig. la

20 X 15 Fig. la

21 X 16 Fig. la

22 X 17 Fig. la

23 X 18 Fig. la

24 X 19 Fig. lb

25 X 20 Fig. lb

26 X Summary

27 X Summary

28 X Summary

29 X 21, 25 Fig. 3 30 X 22, 26 Fig. 3 31 X 23, 27 Fig. 3 32 X 24, 28 Fig. 3 33 X X X X Summary Fig. 3

34 X 29, 33 Fig. 4 35 X 30, 34 Fig. 4 36 X 31, 35 Fig. 4 37 X 32, 36 Fig. 4 38 X 37, 41 Fig. 4 39 X 38, 42 Fig. 4 40 X 39, 43 Fig. 4 41 X 40, 44 Fig. 4 42 X X X X Summary Fig. 4

43 X 45, 49 Fig. 5 44 X 46, 50 Fig. 5 45 X 47, 51 Fig. 5

46 X 48, 52 Fig. 5

47 X X X X Summary Fig. 5

XI

Orifice Meter Performance Downstream of a Tube Bundle Flow

Conditioner, Elbows, and a Tee

Charles F, Sindt, Michael A. Lewis, and James A. Brennan

System pipe configurations can produce large flow disturbances

that significantly affect the accuracy of orifice meters. Flow

conditioners such as the tube bundle are frequently used to remove

the effect of upstream disturbances. The flow conditioner can also

influence measurement accuracy if improperly located relative to the

orifice plate in the orifice meter. Tests were conducted in a 3.8 /iim (150 /iin) Ra surface finish pipe with a tube bundle flow conditioner

located at four different positions upstream of an orifice plate.

The resulting orifice discharge coefficients are shown for the tube

bundle flow conditioner at each of the locations. Changes in the

orifice discharge coefficient for orifice plates downstream of three

flow disturbances consisting of elbows or a tee were measured. For

most of the configurations tested, installing a tube bundle flow

conditioner immediately downstream of the disturbances reduced these

changes in the discharge coefficient from as much as 2 percent to

less than 0.2 percent. Recommendations for future research needs are suggested.

Key words: discharge coefficient; flow conditioner; flow disturbances;

flow measurement; gas; orifice meter; tube bundle

INTRODUCTION

Most meter installations have some form of flow disturbance upstream of

the meter. The disturbance may be a valve, an elbow, a tee, a header, or other

piping elements. The parameters for acceptable orifice meter installations

downstream of a flow disturbance are specified in standards such as ANSI/API

2530[1] and ISO 5167[2]. These standards define the minimum upstream distances

between the orifice plate and the upstream disturbance in installations with no flow conditioner. For installations with a flow conditioner the standards

specify the minimum distance between the upstream disturbance and the flow

conditioner as well as the distance from the flow conditioner to the orifice

plate. These required distances from the orifice plate are functions of the

type of disturbance; the beta ratio; the type of pressure taps; and the

location of a flow conditioner, if used. Effects of the flow conditioner

location on the orifice meter in undisturbed flow have been measured and

reported [3, 4] . The work reported by Smith[3] included the effects of the

location on the orifice discharge coefficient when using flow conditioners such

as the Sprenkle, Zanker, and two types of tube bundles. A literature review of

flow conditioner effects is included in NIST Technical Note 1330[4]. That
report also covers the previous work performed at the National Institute of

Standards and Technology, Boulder, Colorado (NIST-B) that was sponsored by the

Gas Research Institute (GRI) , Chicago, Illinois. The test results reported in

Technical Note 1330 are for the tube bundle and the Sprenkle flow conditioner

in a 4-inch orifice meter with an upstream tube of 0.76 iim (30 Min) Ra surface

roughness. This surface roughness is smoother than that of most commercial

meters. Therefore, tests with the tube bundle were repeated using a meter with

an upstream tube surface roughness of 3.8 /im (150 /iin) . The test results

indicate the effect of the increased surface roughness in reducing the flow

conditioner influence was less than 0.3 percent with the flow conditioner

located at seven pipe diameters and was less than 0.1 percent in most other

cases.

If no flow conditioner is used, the ANSI/API 2530[1] standard requires a longer upstream straight pipe between the disturbance and the orifice plate

than it does if a flow conditioner is installed. For example, the distance

from two close-spaced, out-of-plane elbows to the orifice plate must be 35 pipe

diameters without a flow conditioner and 15 pipe diameters if a tube bundle

flow conditioner is used. However, for an orifice beta ratio of 0.75, this

standard specifies that a flow conditioner can be placed no closer than seven

pipe diameters upstream of the orifice plate. Tests reported here and by

others [3, 4] show that an in-line tube bundle located at seven pipe diameters

upstream of the orifice plate in a 4-inch orifice meter can decrease the

orifice discharge coefficient by as much as 1.2 percent. The location of the

flow conditioner that resulted in a much smaller change to the orifice

discharge coefficient depended on the beta ratio and was between 15 and 20 pipe

diameters upstream of the orifice plate. Depending on the type of disturbance,

this is more than the total length between the disturbance and the orifice

plate specified in the current standard[l]. Moving the flow conditioner to 15

pipe diameters upstream of the orifice plate and maintaining the specified

distance between the flow conditioner and the upstream disturbance would

require eight more pipe diameters of overall meter length, as the current

standard also specifies eight pipe diameters between the disturbance and the

flow conditioner outlet.

The potential requirement for increasing the overall length between an upstream disturbance and the orifice plate would be an impractical modification

to many existing installations. For this reason, a program to determine the

minimum practical length of pipe required between the disturbance and the flow

conditioner was conducted by NIST-B. The program included testing the effects

of three upstream disturbances: (1) two elbows in plane at 12 pipe diameters

apart, (2) a tee, and (3) two out-of-plane elbows butt-welded together. Both

the tee and the out-of-plane elbows were 12 diameters downstream of an elbow.

The test results indicate that an in-line tube bundle placed immediately

downstream of the disturbance and 17 pipe diameters upstream from the orifice

plate resulted in negligible flow measurement error with the tee and less than

0.2 percent error in most of the other cases.
EXPERIMENTAL PROGRAM

Three test configurations were used to produce the baseline orifice

discharge coefficients. The meter configuration for these tests included at

least 46 pipe diameters of straight upstream length and were composed of an approach section, an upstream section, and a downstream section, as shown in

figures la, lb, and Ic. The approach section was 34 pipe diameters long and

had an internal surface roughness of 2,3 /im (90 Aiin) Ra- The internal surface

roughness of the 11 pipe diameters long upstream section was 3.8 iim (150 Min)

Ra. The downstream section was 16 pipe diameters long. Four orifice beta

ratios of 0.43, 0.55, 0.67, and 0.73 were tested with and without a 6-inch

Sprenkle flow conditioner located at 4 6 pipe diameters upstream of the orifice

plate (the configurations shown in figures la and lb) . A few tests were conducted using the beta ratio plates of 0.67 and 0.73 with 56 pipe diameters

of straight pipe upstream of the orifice plate (configuration Ic)

.

The flow conditioner used for the tests was a 19-tube, circular pattern,

in-line unit, as illustrated in figure 2. This type of flow conditioner is

held in the pipe with a set screw positioned at the center of the tube bundle.

The set screw was located at the top of the horizontal meter tube. The flange

pressure taps were located at the 9 o'clock position looking in the direction

of flow.

The first objective of the test program was to determine the flow

conditioner location where the calculated orifice discharge coefficient was equivalent to the discharge coefficient at the baseline. Four flow conditioner

locations upstream of the orifice plate were selected. The closest was at seven pipe diameters because this is the minimum distance allowed[l] when using

a beta ratio of 0.75. The other locations were approximately 11, 17, and 27

pipe diameters. Data were taken using the meter with 46 pipe diameters of

straight upstream pipe (the configuration shown in figure la) and with four

orifice plates with beta ratios of 0.43, 0.55, 0.67, and 0.73. With the flow

conditioner at 27 pipe diameters and the beta ratios of 0.67 and 0.73, a second

test configuration used an oversized (6-inch) Sprenkle flow conditioner at 46

pipe diameters upstream of the orifice plate (the configuration shown in figure

lb).

The second objective of the program was to test configurations to

determine the minimum lengths required between the orifice plate, the tube

bundle, and the disturbance for maintaining accurate flow measurement. The

flow conditioner location tests reported here and those reported by McFaddin[4]

suggest that a distance of 15 to 2 pipe diameters is the best compromise for

the distance between the in-line tube bundle flow conditioner and the orifice

plate to prevent the flow conditioner from degrading the flow measurement.

Therefore, to keep the overall length to a minimum, the test plan started with

the flow conditioner located immediately downstream of the disturbances, which

were located 19 pipe diameters upstream of the orifice plate. The meter

approach section used for the flow conditioner location study was replaced with
a shorter section to obtain the 19 pipe diameters. The downstream flange of

this piece was pinned to the upstream section to ensure alignment. The

internal surface roughness of this piece was 0.76 iim (30 fxin) Ra. The flow

conditioner used for these tests was the same in-line, circular pattern, 19

tube unit used for the flow conditioner location study.

The first upstream disturbance test configuration used two long radius

elbows in plane which turned the same direction and were spaced 12 pipe

diameters apart. This configuration is shown in figure 3. The next test

configuration placed a tee 12 pipe diameters downstream of a long radius elbow

as is shown in figure 4. Figure 5 shows the third configuration, which

consisted of two out-of-plane long radius elbows butt-welded together and

spaced 12 pipe diameters downstream of a third long radius elbow.

Two upstream sections of different interior surface roughness were used in

the test program. The data for the two elbows in plane were taken using a 0.76

/im (30 /iin) Ra upstream section. A 3.8 nm (150 iJ.in) Ra upstream section was used with the two out-of-plane elbows. Both sections were used with the tee.

Flow was measured using all three configurations, with and without the flow

conditioner installed, and using orifice plates with beta ratios of 0.43, 0.55,

0.67, and 0.73.

TEST RESULTS

Baseline Data

The baseline data used for the 3.8 ixm (150 iiin) Ra upstream tube in the

three configurations shown by figure 1 are presented in tables la through 4c

for the four beta ratio plates. The plotted data are shown in figures 6

through 9. Data for each configuration are plotted with a different symbol so that it can be observed separately from the others; a straight line fitted to

all of the data is also shown on the plots.

The baseline data used for the 0.76 /xm (30 idin) Ra upstream tube were

taken from NIST Technical Note 1330 by McFaddin et al.[4]. The measured data

for each beta ratio plate using the two baseline configurations (tables Bl

through B8 of the referenced technical note) were combined and fitted with a straight line. These resulting curves serve as the baselines used in this

study.

Flow Conditioner Location Tests

The flow conditioner location tests using the 0.76 iim (30 ^J.iT\) Ra upstream

pipe were reported in NIST Technical Note 1330[4]. The flow conditioner

location tests reported here are for the 3.8 jim (150 /iin) Ra upstream pipe.

All of the tests on location of the flow conditioner were taken for the

configuration shown in figure la; that is, no flow conditioner at the elbow and

46 pipe diameters of straight pipe from the last elbow to the orifice plate,

with two exceptions. The two exceptional cases were with the flow conditioner

located at 27 pipe diameters with the two beta ratios of 0,67 and 0.73. With

these two beta ratios and the tube bundle at 27 pipe diameters, additional data
were taken in the configuration shown in figure lb. The data taken with the

flow conditioner located at 7 pipe diameters upstream of the orifice plate and

37 pipe diameters downstream from the elbow are presented in tables 5 through

8. The data for the four beta ratios are compared to the baseline in figures

10 through 13. Tables 9 through 12 contain the data for the four beta ratios

with the flow conditioner located at 11 pipe diameters; the discharge

coefficients are compared to the baseline in figures 14 through 17. The graphs

for the flow conditioner located at 17 pipe diameters upstream of the orifice

plate are shown in figures 18 through 20 and the data are in tables 13 through

15. No data were taken with the 0.4 3 beta ratio plate and the flow conditioner

located at 17 or 27 pipe diameters, because previous measurements [4] indicated

very little effect at these locations. Figures 21 through 23 and tables 16

through 18 present the data with the flow conditioner located at 27 pipe

diameters. The data for the in-line tube bundle located at 27 pipe diameters

with the 6-inch Sprenkle at 46 pipe diameters are given in tables 19 and 20 and

are shown in figures 24 and 25 for the two beta ratios of 0.67 and 0.73. In

these data there appears to be a difference which needs additional

investigation.

To calculate the differences in the orifice discharge coefficient, the

data at each flow conditioner location and beta ratio were fitted to a straight

line over the flow range tested. The percent difference at selected Reynolds

numbers was calculated as follows:

(C^ - Cjj) X 100

AC(%) = , (1)

where C^ is the calculated discharge coefficient for the test configuration and

Cjj is the calculated discharge coefficient for the baseline configuration.

Figures 26 through 28 show the difference in the orifice discharge

coefficient between the baseline and the configuration with the flow

conditioner at the four test locations when using the 3.8 /im (150 iiin) Ra and

0.76 lira (30 /iin) Ra upstream sections. Curves are shown for a pipe Reynolds

number of 1.6 x 10^ for the beta ratios of 0.55, 0.67, and 0.73.

For all beta ratios there is a difference of less than 0.2 percent in the

change of the orifice discharge coefficient between the two upstream pipes,

except when the flow conditioner is located at seven pipe diameters from the

orifice plate for the beta ratios of 0.55 and 0.67. Also, at a beta ratio of

0.73, the change in discharge coefficient with the flow conditioner at 11 and

27 pipe diameters is 0.3 percent between the smoother and the rougher upstream

pipe. But with the Sprenkle flow conditioner upstream of the meter run the

change in the discharge coefficient was within 0.2 percent of that with the

smoother upstream section. The location of the flow conditioner which

minimizes the shift in the orifice discharge coefficient is between 15 and 20
pipe diameters from the orifice plate for both of the upstream pipe roughnesses

tested.

As noted above, with the flow conditioner placed 27 pipe diameters

upstream of the 0.73 beta ratio orifice plate, there was a significant

difference in the discharge coefficient when the 6-inch Sprenkle was used at

the elbow and when it was not used. The data when the 6-inch Sprenkle was used

are in better agreement with the data using the 0.76 iJ,m Ra upstream pipe. More

data points were taken without the 6-inch Sprenkle to reduce the possibility

that one anomalous data set was causing the disagreement. There is some scatter in these data, but the scatter does not overlap the data taken when

using the 6-inch Sprenkle, so we conclude that the difference measured is

valid.

Inlet Disturbance Tests

Measurements were made with and without the flow conditioner installed for

each of the three disturbances. Data were taken with the two elbows in plane

using the 0.76 /xm (30 fJ-in) Ra upstream section. Data with no flow conditioner

are presented in tables 21 through 24 and the data with the in-line tube bundle

placed at the discharge of the second elbow are presented in tables 25 through

28. Figures 29 through 32 show the orifice discharge coefficient versus the

pipe Reynolds number. The difference between the calculated discharge

coefficients determined from the measurements with and without the flow

conditioner and the baseline meter is shown at a pipe Reynolds number of 1.25 x

10 in figure 33. With the two elbows in plane, the calculated discharge

coefficient was below the baseline for all beta ratios. With the 0.43 and 0.55

beta ratio plates, installing the flow conditioner did not improve the flow

measurement. With a beta ratio of 0.67 the flow conditioner almost restored

the orifice discharge coefficient to the baseline value and with a beta ratio

of 0.7 3 it reduced the shift from -0.7 percent to -0.2 percent.

Orifice discharge coefficients were determined using the 0.76 /xm (30 iiin) Ra and the 3.8 ^m (150 Min) Ra upstream pipes with the tee 19 pipe

diameters from the orifice plate. The data measured using the 0.76 jum (30 Min)

Ra upstream pipe with and without the flow conditioner are presented in tables

29 through 32 and tables 33 through 36, respectively. Figures 34 through 37

show plots of the data. Similar data for the 3.8 iJ,m (150 Min) upstream pipe

are given in tables 37 through 44 and figures 38 through 41. Figure 42 shows

the change in the orifice discharge coefficient versus the beta ratio at a Reynolds number of 1.25 x 10^ for both upstream pipes with the tee at 19 pipe

diameters.

The tee introduces very large fluctuations in the orifice differential

pressure; these fluctuations are accompanied by large errors in the flow

measurement, especially at the lower beta ratios. These pressure fluctuations

are apparently caused by a moving swirl produced by the tee, as measurements

made with a pitot tube reveal highly fluctuating stagnation pressures, which
indicate swirl. The tube bundle flow conditioner placed 17 pipe diameters

upstream of the orifice plate at the discharge of the tee restored the orifice

discharge coefficient to the baseline value over the Reynolds number range

tested, 0.5 x 10^ to 1.5 x 10 , except with the smooth pipe and the 0.73 beta

ratio orifice plate. For this configuration the shift was still less than 0.5

percent and was actually greater with the flow conditioner than for the

configuration without it. With the 3.8 ^im (150 fiin) Ra upstream pipe, the data

in figure 42 show a small positive change in the discharge coefficient with no flow conditioner. However, the curve in figure 4 2 with no flow conditioner is

deceptive because it does not show the scatter in the measured orifice

discharge coefficient that is apparent in figure 41. Therefore, the discharge

coefficient may not be predictable without the flow conditioner.

The two out-of-plane elbows butt-welded together were tested using the 3.8

/Ltm (150 jLtin) Ra upstream pipe. Data for this configuration without the flow

conditioner are in tables 45 through 48 and data for the configuration with the

flow conditioner at the exit of the second elbow are in tables 49 through 52.

Figures 43 through 46 show these data. The change in orifice discharge

coefficient versus the beta ratio at the Reynolds number of 1.25 x 10 is

presented in figure 47.

With the beta ratios of 0.43 and 0.55, use of the flow conditioner removed

nearly all of the shift of the orifice discharge coefficient produced by the

two elbows. The data taken with 0.43 beta ratio plate and the flow conditioner

show slightly less shift than was previously reported[5]. This is a result of our having taken additional data since that paper was written, and of a better

resolution of the conditioned coefficient value. Without a flow conditioner

the shift in the orifice discharge coefficient reversed sign between the beta

ratio of 0.67 and the beta ratio of 0.73, which is the response previously

observed with swirl present [ 6] . With the 0.67 beta ratio plate the flow

conditioner had no effect, but at a beta ratio of 0.73 the flow conditioner

almost restored the discharge coefficient to the baseline value.

CONCLUSIONS

Tests of the orifice meter at NIST-B show that the best compromise for the

location of the tube bundle in our 4-inch meter was 17 pipe diameters upstream

of the orifice plate, as this location produced the smallest average flow

measurement deviation for all beta ratios from the baseline measurement [4 ]

.

This was true for both roughnesses of upstream pipes (0.76 /xm and 3.8 ^m Ra) . Using the in-line tube bundle at 17 pipe diameters upstream of an orifice plate

also significantly reduced the shift in flow measurement caused by flow

disturbances immediately upstream. The test results reported here show that

placing the flow conditioner at the discharge of two out-of-plane elbows buttwelded together reduces the shift in the orifice discharge coefficient within

0.3 percent of the baseline installation as the worst case. When the flow

disturbance was a tee, the flow conditioner located at the discharge of the tee
removed most of the change in the orifice discharge coefficient, which was larger than 2.75 percent. The flow conditioner .located at the discharge of two

elbows in plane widely spaced was only helpful at the beta ratio of 0.67 and

higher where it did reduce the effect of the disturbance to less than 0.25

percent. However, at 0.43 and 0.55 beta ratio the shift from the baseline

discharge coefficient was less than 0.25 percent with or without the flow

conditioner.

RECOMMENDATIONS

This research was conducted with a 4-inch orifice meter, so the effect of

meter tube size was not measured and is unknown at this time. Some of the work

reported by others was conducted in larger sizes and did include tests with a 19-tube flow conditioner [ 3 ] . The effect of location of the flow conditioner

relative to the orifice plate and to upstream disturbances needs to be measured

in larger and smaller meter sizes.

The only flow conditioner used in our tests was the in-line tube bundle.

Tests using other flow conditioners have been reported[3 , 4 ] . These tests were limited in scope and did not evaluate the effectiveness of the flow conditioner

downstream of a disturbance. More extensive tests need to be conducted to

determine whether other types of flow conditioners located closer to the

orifice plate will remove the effects of disturbances when placed close to the

disturbance.

Tests should be run with flow conditioners close to the disturbance and

the disturbance closer to the orifice plate to determine if the overall length

can be further reduced to accommodate shorter field installations. Some of

this testing is included in the 1990 program.

REFERENCES

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

A.G.A Report No. 3 —ANSI/API 2530, Second Edition, American Gas

Association, Arlington, VA 22209 (September 1985)

.

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

tubes inserted in circular cross-section conduits running full.

International Standard ISO 5167, First Edition, International Organization

for Standardization (1980)

.

[3] Smith, D. J.M. , The effects of flow straighteners on orifice plates in good

flow conditions. International Conference on Flow Measurement in the Mid

80 's, June 9-12, 1986, National Engineering Laboratory, East Kilbride,

Glasgow, UK.

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

conditioners in a 4-inch orifice meter, NIST Technical Note 1330, National

Institute of Standards and Technology, Gaithersburg, MD (1989).
[5] Sindt, C.F., M.A. Lewis, J. A. Brennan, Orifice Meter Performance

Downstream From Elbows or a Tee, Proceedings of the 2nd International

Symposium on Fluid Flow Measurement, Calgary, Alberta, Canada (June 6-8,

1990)

.

[6] Brennan, J. A., S.E. McFaddin, and C.F. Sindt, 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)

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

straight pipe upstream.

Oversize Sprenkle

Flow Conditioner

Figure lb. Four-inch orifice meter, 6-inch Sprenkle at

46 pipe diameters.

Figure Ic. Four-inch orifice meter, 56 pipe diameters of

straight pipe upstream.

10
Figure 2. In-line tube bundle.

Orifice Plate

Long Radius Elbow

Figure 3. Test configuration with two elbows in plane

at 19 pipe diameters from the orifice plate,

11
Orifice Plate

Tee

Figure 4. Test configuration with a tee at 19

pipe diameters from the orifice plate.

Butt weid two

elbows In plane

Butt weld two elbows out of plane

Flow

Conditioner

Figure 5. Test configuration with two elbows out-ofplane at 19 pipe diameters from the orifice

plate.

12
0.62

/S = 0.43

3.8 ^m Ra

a

O 0.61

oo

0)bLU

eS g 0.60

CO

O D

OOOOO Baseline. Elbow at 46D

DDDDD Baseline. OS at 46D

Baseline, All Data

0.5< 0.6 1.0 1.4 Pipe Reynolds Number/10

Rgure 6.

1.8

Discharge coefficient vs. Reynolds number for the 0.4-3 beta

ratio orifice plate, baseline data.

0.62

/S = 0.55

3.8 fiTxi Ra

O 0.61

0)oo

a;

bt) ti

CD •g 0.60

to

CXXXX3 Baseline. Elbow at 46D aaaaa Baseline. OS at 46D

Baseline. All Data

0-5%.^

Figure 7.

0.6 1.0 1.4 Pipe Reynolds Number/10

1.8

Discharge coefficient vs. Reynolds nunnber for the 0.55 beta

ratio orifice plate, baseline data.

13
0.62

o 0.61

oo

u

eio

CO 0.60

0.5 %.

- /S == 0.67

- 3.8 /xm Ra

- ^

- O -—-^ ^%^^""^-'su^. O

_ ^^—^

- a

;

00000 Baseline,

OOOOO Baseline,

DDODD Baseline,

1 1

Elbow at 56D

Elbow at 46D

OS at 46D

All Data

1 1 1 1 0.6 1.0 1.4 1.8 Pipe Reynolds Number/ID

Rgure 8. Discharge coefficient vs. Reynolds number for the 0.67 beta

ratio orifice plate, baseline data.

0.61

O 0.60

0)oO

ag 0.59

OQ

0.5E

/S = 0.73

3.8 fim Ra

OOOOO Baseline, Elbow at 56D

OOOOO Baseline, Elbow at 46D nnnnn Baseline, OS at 46D

Baseline, All Data

_L 1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/ 10

Figure 9. Discharge coefficient vs. Reynolds number for the beta ratio orifice plate, baseline data. 0.73

14
0.62

o 0.61

0)ou

tm

as -g 0.60

CQ

0.5$

- /S = 0.43

-

3.8 fMva Ra

: r~

^

-

*

i J^^~^*

***** In-I.ine

1 1

Tube Bundle

1

at 7D

1 1 1 1 0.6 1.0 1.4 1.8 Pipe Re3niolds Number/ID

Figure 10. Discharge coefficient vs. Reynolds nunnber for the 0.43 beta ratio orifice plate with the in— line tube bundle at 7 pipe diameters.

0.62

"3 0.61

0)ou

V

u

a

•^ 0.60

GQ

0.5{

/S = 0.55

3.8 fim. Ra

**if:»f* In-line Tube Bundle at 7D

Baseline

J_ _L 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 1 1 . Discharge coefficient vs. Reynolds nunnber for the 0.55 beta ratio

orifice plate with the in-line tube bundle at 7 pipe diameters.

15
0.62

o 0.61

oO

v

cd -g 0.60

CO

0.5c

- jg = 0.67

- 3.8 /^m Ra

-

*

: »

**

*

- ***** In-line Tube Bundle at 7D

Baseline

1 1 > 1 1 1 1 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 12. Discharge coefficient vs. Reynolds nunnber for the 0.67 beta ratio orifice plate with the in— line tube bundle at 7 pipe diameters.

0.61

d

O 0.60

oo

0)

eS •^ 0.59 m

0.5{

- /9 = 0.73

- 3.8 /xm Sa

-

* ** j-< *

* * *

-

***** In-line Tube

RnspliTip

1

Bundle at 7D

1 1

1 ).8

Figure 13.

1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/10

Reynolds nunnber for the 0.73 beta ratio pipe

Discharge coefficient vs. orifice plate with the in -line tube bundle at 7 diameters.

16
0.62

C

0)o 0.61

•fH

<t-l K-i(Uoo

•^ 0.60 n

0.5%

- /? = 0.43

_

3.8 fjjn Ra

-

* *^^^^^^^--_* * -

*

-

***** In-line Tube Bundle at UD

- Tlnnplinp

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

Rgure 14. Discharge coefficient vs. Reynolds nunnber for the 0.43 beta ratio orifice plate with the in— line tube bundle at 1 1 pipe diameters.

0.62

0) 0.61

9iO

V

a

o

in 0.60

0.5£

/S = 0.55

3.8 fim. Ra

***** In-line Tube Bundle at IID

Baseline

*

0.6 1.0 1.4 1.8 Pipe Reynolds Number/ 10

Figure 15. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio

orifice plate with the in-line tube bundle at 1 1 pipe diameters.

17
0.62

o 0.61

o

0)U

a

0.60 -

0.5%_

- /S = 0.67

- 3.8 fjJD. Ra

-

*

-

*

*

*

: ***** In-line Tube Bundle at IID

-

1 1 1 1 1 1 2 0.6 1.0 1.4 l.l

Figure 16. Pipe Reynolds Number/lO"

Discharge coefficient vs. Reynolds nunnber for the 0.67 beta ratio

orifice plate with the in— line tube bundle at 1 1 pipe diameters.

0.61

0)O 0.60

ou

V

bt) u

aio

m

0.59 -

0.5%

/S = 0.73

3.8 nm Ra

i 1r

* * * * * *

***** In-line Tube Bundle at IID

Baseline

1 1 1 1 1.0 1.2 1.4 1.6 Pipe Rejmolds Number/10

1.8

Figure 17. Discharge coefficient vs. Reynolds nunnber for the 0.73 beta ratio orifice plate with the in— line tube bundle at 1 1 pipe diameters.

18
0.62

0)O 0.61

•iH

«4-( oo

cd -g 0.60

0.5{

/? = 0.55

3.B fjin Ra

***** In-line Tube Bundle at 17D

Baseline

1.2 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Rgure 18. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio orifice plate with the in-line tube bundle at 17 pipe dianneters.

0.62

HiV

"3 0.61

0)ou

u

a

•g 0.60 n

0.5{

/S = 0.67

3.8 fim Ra

***** In-line Tube Bundle at 17D

Baseline

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

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

orifice plate with the in-iine tube bundle at 17 pipe diameters.

19
0.62

<4-> d

O 0.61

o

(0 •g 0.60

go

0.5£

^ = 0.73

3.8 /xm Ra

***** In-line Tube Bundle at 17D

Baseline

1.8

Figure 20.

1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/lO

Discharge coefficient vs. Reynolds number for the 0.73 beta ratio

orifice plate with the in-line tube bundle at 17 pipe diameters.

0.62

"5 0.61

0)oo

0)

cd •g 0.60

03

0.5J

/8 = 0.55

3.8 fim Ra

***** In-Line Tube Bundle at 27D

Baseline

0.6 1.0 1.4 1.8 Pipe Reynolds Number/ 10

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

orifice plate with the in— line tube bundle at 27 pipe diameters.

20
0.62

a

o 0.61

0>ou

0)u

•g 0.60

00

0.5£

/S = 0.67

3.8 fiTO. Ra

*«*** In-line Tube Bundle at 27D. No OS

Baseline

_L 0.6 1.0 1.4 Pipe Reynolds Number/10°

1.6

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

orifice plate with the in-line tube bundle ot 27 pipe diameters.

0.62

d

9)U 0.61

ou

v

a

•^ 0.60

DQ

0.5{

- /S = 0.73

.

3.8 fim. Ra

-

«

-

- ^

h Iti-

*

*

*

**

- ***** In-I.ine Tube Bundle at 27D, No

Baseline

1 1 1

OS

1 1.0 1.2 1.4 1.6 Pipe Reynolds Number/10

1.8

Figure 23. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio orifice plate with the in— line tube bundle at 27 pipe diameters.

21
0.62

a

v

o 0.61

•i-t •m

0)OU

0)00

C0 '§ 0.60

CO

0.5J

/? = 0.67

3.8 /xm Ra

DDDnn In-line Tube Bundle at 27D, OS at Elbow

Baseline

0.6 1.0 1.4 1.8

Figure 24. Pipe Reynolds Number/ID

Discharge coefficient vs. Reynolds number for the 0.67 beta ratio

orifice plate with the in-line tube bundle at 27 pipe diameters and

the 6— inch Sprenkle at 46 pipe diameters.

0.62

O 0.61

oo

V

CDu

GO 0.60 -

0.5J

j8 = 0.73

3.8 fun Ra

° a ff " ig D

n

-

D

DDDnn In-line Tube Bundle at 27D, OS

1 1 1

at Elbow

1 ).6 1.0 1.2 1.4 1.6 l.B Pipe Reynolds Number/10

Figure 25. Discharge coefficient vs. Reynolds number for the 0.7J beta ratio

orifice plote with the in— line tube bundle at 27 pipe diameters and

the 6-inch Sprenkle at 46 pipe diameters.

22
2.0

o 1.5 h

•5 ^-^ "

0)

et£ 0.5

CI

ed ^ 0.0

o

-0.5

1.0 -

-1.5 -

-2.0

/? = 0.55

Reynolds No. = 1.6 z 10*

QOQQO 3.6 fj,m Ra Pipe

OOOOO 0.76 A^m Ra Pipe

O 10 20

Location (Pipe Diameters)

Rgure 26. Percent change in the orifice discharge coefficient vs. flow conditioner location for the 0.55 beta ratio orifice plate.

30

2.0

o 1.5 U

13 1.0

•fH

(D^ 0.5 a

cd ^ 0.0 o

^ -0.5

ti

0)D

(h -1.0

0) cu

-1.5

-2.0

_

/S = 0.67

-

Reynolds No. = 1.6 x 10*

-

-

- unauu 3.8 /xm Ra Pipe, OS at Elbow

QQOQD3.8 /zm Ra Pipe

00000 0.76 /im Ra Pipe

"

1 1 1 1 ) 10 20

Location (Pipe Diameters)

Figure 27. Percent change in the orifice discharge coefficient vs. flow conditioner location for the 0.67 beta ratio orifice plate.

30

23
2.0

Q 1.5

0)

ttO 0.5 ^ 0.0

tf -0.5

M

(U£-1.0

0) -1.5

-2.0

/? = 0.73

Reynolds No. = 1.6 x lO'

~ o

ODDDO 3.8 /mi Ra Pipe, OS at Elbow

QQOQO 3.8 fj-TO. Ra Pipe

00000 0.76 /xm Ra Pipe

Figure 28.

10 20

Location (Pipe Diameters)

Percent change in the orifice discharge coefficient vs. flow conditioner location for the 0.73 beta ratio orifice plate.

30

0.62

d

o 0.61

0)oo

o

CO 0.60

0-5%.

- /? = 0.43

- 0.76 /im Ra

-

^T""^-^—.g^

n r^^ ~_^__

- ^ °^

-

D

00000 Elbow at 19D

\

DDDDD In-line Tube Bundle at the Elbow

- Baseline

1 1 1 1 1 1 1 0.6 1.0 1.4 l.B Pipe Reynolds Number/lO

Figure 29. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio orifice plate at 19 pipe diameters from two elbows in plane.

24
0.62

a

4)O 0.61

0)ou

0)

CDo

09 0,60 -

0.5%

^ = 0.55

0.76 fim Ra

: »B

^ /~~~~^^~-~-~-j----

T00000 Elbow at 19D aaoaa In-line Tube Bundle at the Elbow I.I, 1 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Rgure 30. Discharge coefficient vs. Reynolds nunnber for the 0.55 beta ratio

orifice plate at 19 pipe diameters fronn two elbows in plane.

0.62

0)o 0.61

'C

0)o

0)ao 0.60 -

0.5£

/S = 0.67

0.76 fim Ra

D

B

a"

a

00000 Elbow at 19D

DDDDD In-line Tube Bundle at the Elbow

, 1 1 1 1 1 1 0.6 1.0 1.4 1.8 Pipe Reynolds Number/ 10

Figure 31. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio

orifice plate at 19 pipe diameters from two elbows in plane.

25
0.61

o 0.60

ou

V«

•g 0.59

to

0.5f

jff = 0.73

0.76 /xm Ra

00000 Elbow at 19D nnnna In-line Tube Bundle at the Elboir

Baseline

_L 1.0 Pipe

1.2 Reynolds1.4 1.6 1.8 Number/10*

Figure 32. Discharge coefficient vs. Reynolds nunnber for the 0.73 beta ratio orifice plate at 19 pipe diameters from two elbows in plane.

Q

2.0

1.5

1.0

bX) 0.5

0.0

tf -0.5

Q

Q)g-1.0

CD -1.5

-2.

ft.

Reynolds No. = 1.25 x lO' 0.76 fim Ra Pipe

UBUiln-Iine Tube Bundle at the Elbow

ODDnD No Flow Conditioner

_L 0.4 0.5 Beta

0.6 Ratio

0.7 0.8

Figure 33. Percent change in the orifice discharge coefficient vs. beta ratio for the orifice plate 19 diameters from two elbows in plane.

26
0.63

0.62 -

0.61 o

Qiwu

a

Q 0.60 h

0.5£

- /S = 0.43

- 0.76 fim Ra

_ A

-

^ A

A

A

A A

A

AA

A

- o

^

- AAAAA Tee at 19D, No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

I 1 1 1 1

-

1 r 0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Rgure 34. Discharge coefficient vs. Reynolds number for the 0.43 beta ratio

orifice plate at 19 pipe dianneters from a tee and with the 0.76 /zm

upstream pipe.

0.63

0.62

0.61

a;o

V

f1

o

CQ Q 0.60 -

0.5J

/S = 0.55

0.76 fun Ra

AAAAA Tee at 19D, No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

Baseline

[).2 0.6 1.0 1.4 l.B Pipe Rej^nolds Number/lO

Figure 35. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio

orifice plote at 19 pipe diameters from a tee and with the 0.76 ^m

upstream pipe.

27
0.62

d

0)O 0.61

ou

V

d

•§ 0.80

OS

/? = 0.67

0.76 /an Ra

o

o

AAAAATee at 19D, No Flow Conditioner

OCXXX3 In-line Tube Bundle at the Tee

Baseline

0-5%. _L _L 0.6 1.0 1.4 1.8

Rgure 36. Pipe Reynolds Number/10

Discharge coefficient vs. Reynolds number for the 0.67 beta ratio

orifice plate at 19 pipe diameters from a tee and with the 0.76 iu,m upstream pipe.

0.62

P = 0.73

0.76 fjjn Ra

O 0.61

0)o

Vu

CO •^ 0.80

09

AAAAA Tee at 19D, No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

Baseline

0.5%L _L J_ 1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/10

Figure 37. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio

orifice plate at 19 pipe diameters from a tee and with the 0.76 f^m upstream pipe.

28
0.63

C

O

ou

V

til) u

0.62

0.61

O 0.60

0.5{

A

A

A

/? = 0.43

3.8 /xm Ra

A

A

&

. AAAAA Tee at 19D, No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

Baseline

_L 0.6 1.0 1.4 1.8 Pipe Reynolds Number/lO

Rgure 38. Discharge coefficient vs. Reynolds nunnber for the 0.43 beta ratio orifice plate at 19 pipe diameters from o tee and with the 3.8 /xm

upstream pipe.

0.63

g 0.62 \-

0)o

0.61 -

0)u

cdo

QQ Q 0.60 h

0.5?

/8 = 0.55

3.8 /xm Ra

^

A

A A ^

" A

~^ 8~ —~^-—-^

AAAZiATee at 19D. No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

BasRiiTiR

1 1 1 1 1 1 1 2 0.6 1.0 1.4 l.f

Figure 39. Pipe Reynolds Number/ 10

Discharge coefficient vs. Reynolds number for the 0.55 beta ratio orifice plate at 19 pipe diameters from a tee ond with the 3.8 fim upstream pipe.

29
0.63

^0.62

O

ou 0.61

SO O 0.60

0.5%

/S = 0.67

3.B /zm Ra

AAAAA Tee at 19D, No Flow Conditioner

CXXXXD In-line Tube Bundle at the Tee

Baseline

J_ 0.6 1.0 1.4 1.6 Pipe Re3molds Number/lO'

Figure 40. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio

orifice plate at 19 pipe diameters from a tee and with the 3.8 fj,rr\ upstream pipe.

0.62

0.61 -

0)o" 0.60 h

0)

61) U

C0o

mQ 0.59 -

0.5E

- ^ = 0.73

- 3.8 fita Ra

. ^

. % ^^^-_^2___ A

- ^ %o &

8

- AAAAA Tee ® 19D, No Flow Conditioner

OOOOO In-line Tube Bundle at the Tee

"

1 1 1 1 1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/10

Figure 41. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio orifice plate at 19 pipe diameters from a tee and with the 3.8 fu,m upstream pipe.

30
^->

O

PL,

3.0

2.5

2.0

1.5

1.0

0.5 h

0.0

-0.5 -

-1.0 - H.

QQOQD3.8 pan Ra Pipe with Tube Bundle at the Tee

ClO^O^ 3.8 fjjn Ra Pipe with No Flow Conditioner

AAAAA 0.76 fj.m. Ra Pipe with Tube Bundle at the Tee

aODElD 0.76 fim Ra Pipe with No Flow Conditioner

0.4 0.5 Beta0.6 Ratio0.7 0.8

Figure 42. Percent change in the orifice discharge coefficient vs. beta ratio for the tee ot 19 pipe dianneters from the orifice plate.

0.62

0)o 0.61

0)ou

0)m

o

0.60 -

0.5J

- /S = 0.43

- 3.8 fan Ra

A

A

o—----^

o

A

A AA

A^

O

- °8

AAAAATwo Elbows at 19D

OOOOO In-line Tube Bundle at the Elbow

Baseline

1 1 1 1 1 1 ] 0.6 1.0 1.4 Pipe Reynolds Number/lO

1.8

Figure 43. Discharge coefficient vs. orifice plate at 19 pipe

Reynolds number for the 0.43 beta ratio diameters from two elbows out— of— plane.

31
0.62

d

O 0.61

4)O

«

h

a

•g 0.60

0.5%

- /S = 0.55

-

, 3.8 ^m Ra

- o A

A

O

A

A

A

O

A^

-

o

O o

- AAAAATwo Elbows at 19D

OOOOO In-line Tube Bundle at

1 1 1

the

1.

Elbow

1 0.6 1.0 1.4 1.8 Pipe Rejmolds Number/10

Figure 44. Discharge coefficient vs. Reynolds number for the 0.55 beta ratio

orifice plate at 19 pipe dianneters from two elbows out-of-plane.

0.62

4>O 0.61 Vou

«

u

"g 0.60

0.5%

- fi = 0.67

- 3.8 /xm Ra

- A

- o cu ° -X_J

- AAAAATwo Elbows at 19D

CXXOO In-line Tube Bundle at the Elbow

1 1 1 1 1 1 1

I

0.6 1.0 1.4 1.8 Pipe Reynolds Number/10

Figure 45. Discharge coefficient vs. Reynolds number for the 0.67 beta ratio orifice plate at 19 pipe diameters from two elbows out-of-plane.

32

1
0.61

a

o 0.60

ou

V

05 •^ 0.59

0-5%,

- /? =: 0.73

- 3.8 /jjn Ra

o&—

- .«^ % —

-

A^

&A

A

Q)

- AiiAAATwo Elbows at 19D

OOOOOln-Une Tube Bundle at the Elbow

1

1 1 1 1.0 1.2 1.4 1.6 1.8 Pipe Reynolds Number/lO

Figure 46. Discharge coefficient vs. Reynolds number for the 0.73 beta ratio orifice plate at 19 pipe diameters from two elbows out— of-plane.

2.0

P 1.5

fn 1.0 -

0)b£ 0.5 -

rC 0.0 O

tJ -0.5 h

2-i.oh

PL, -1.5 h

-2.(

Reynolds No. = 1.25 x lO'

3.8 pan Ra Pipe

vmaav In-line Tube Bundle at the Elbow

ODDIXi No Flow Conditoner

0.4 0.5 0.6 Beta Ratio

0.7 0.8

Figure 47. Percent change in the orifice discharge coefficient vs. beta ratio for two elbows out-of— plane at 19 pipe diameters from the orifice plate.

33
Table l.a. Measured and calculated quantities for the beta ratio of 0.43 with the 3.8 /xm upstream pipe and 46 pipe dieuseters of straight pipe upstream of the orifice plate.

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

Run ID Pressure Pressure Temperature Tempei:at' Density Dif Press Flow Rate Pipe Re No. (MPa) (K)

43050389- 1 3.7800 287,,89

43050389- 2 3.7730 287,.68 43050389- 3 4.0826 289,,35

43050389- 4 4.0496 289,,42

43050389- 5 3.8726 288,.72 43050389- 6 3.8703 288,,57

43050389- 7 3.9226 288,,92

43050389- 8 3.9166 288,,89

CY,

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

£>

44.57 48.332 1.9763 1.,3425 0,.6019 0.6036

44.52 47.914 1.9627 1.,3341 0,.6007 0.6023

47.89 4.956 0.6556 0..4422 0,.6033 0.6035

47.48 5.147 0.6670 0,.4500 0..6047 0.6048

45.52 25.059 1.4379 0,,9737 0.,6026 0.6035

45.52 24.745 1.4262 0,,9662 0,.6015 0.6023

46.08 13.378 1.0562 0..7144 0,.6026 0.6030

46.01 13.440 1.0575 0,.7154 0..6023 0.6027

Table l.b. Measured and calculated quantities for the beta ratio of 0.43 with the 6-inch

Sprenkle 46 pipe diameters upstream of the orifice plate.

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

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

43042390- 1 4.0545 289,,42

43042390- 2 4.0345 289.,60

43042390- 3 3.7342 287,,38

43042390- 4 3.7275 287,,50

43042390- 5 3.8085 287.,79

43042390- 6 3.8125 287,,68

43042390- 7 3.8129 287,,78

43042390- 8 3.8698 288,,23

43042390- 9 3.8671 288,,38

43042490- 1 3.7679 286,,72

43042490- 2 3.7624 286,,97

43042490- 3 4.0151 288,,16

43042490- 1 3.8144 287,,49

43042490- 2 3.8255 287,,54

43042490- 3 3.8918 288,,18

43042490- 4 3.8860 288,,18

43042490- 5 4.0122 288,,82

CY,

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

47.54 6.234 0.7369 0,,4971 0,.6067 0.6069

47.27 6.252 0.7358 0,,4963 0,.6068 0.6070

44.11 46.548 1.9198 1,,3064 0,.5989 0.6005

44.02 46.390 1.9132 1,,3016 0,.5986 0.6002

44.93 29.862 1.5498 1,,0526 0,.5988 0.5998

44.99 30.013 1.5593 1,,0594 0,.6005 0.6015

44.98 29.767 1.5562 1,,0570 0,.6019 0.6029

45.57 15.091 1.1156 0,,7564 0,.6025 0.6030

45.52 15.032 1.1138 0,,7549 0,.6031 0.6036

44.63 46.089 1.9272 1,,3130 0,.6008 0.6024

44.52 46.060 1.9207 1,,3079 0,.5997 0.6013

47.30 6.048 0.7198 0,.4873 0,.6031 0.6033

45.05 29.353 1.5422 1,.0482 0..6002 0.6012

45.17 29.485 1.5455 1,.0502 0.,5993 0.6003

45.84 14.839 1.1097 0,.7523 0,,6026 0.6031

45.77 14.712 1.1042 0..7486 0..6026 0.6031

47.15 6.368 0.7393 0.,4997 0..6046 0.6048 I

34
Table 2. a. Measured and calculated quantities for the beta ratio of 0.55 with the 3.8 fim upstream pipe and 46 pipe diameters of straight pipe upstream of the orifice plate.

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

44050389- 1 3.9783 288.92 46.73 7.180 1.3348 0.9023 6052 0.6054

44050389- 2 3.9954 288.93 46.93 7.133 1.3325 0.9005 6048 0.6050

44050389- 3 4.1054 289.42 48.14 2.970 0.8717 0.5877 6056 0.6057

44050389- 4 4.1067 289.48 48.14 3.001 0.8781 0.5919 6069 0.6070

44050389- 5 3.9190 288.29 46.15 12.697 1.7617 1.1936 6043 0.6047

44050389- 6 3.9139 288.38 46.07 12.602 1.7517 1.1866 6036 0.6040

44050389- 7 3.6938 287.39 43.64 23.047 2.2984 1.5647 6014 0.6022

44050389- 8 3.7305 288.04 43.96 20.645 2.1922 1.4895 6039 0.6046

44102589- 1 4.0569 288.14 47.80 2.615 0.8172 0.5530 6073 0.6074

44102589- 2 4.0527 288.17 47.75 2.655 0.8240 0.5576 6080 0.6081

44102589- 3 3.6886 286.78 43.67 21.201 2.2109 1.5075 6030 0.6037

44102589- 4 3.6864 286.16 43.75 20.941 2.1997 1.5022 6031 0.6038

44102589- 5 3.8298 286.97 45.32 13.694 1.8125 1.2333 6041 0.6045

44102589- 6 3.8242 287.17 45.22 13.871 1.8198 1.2377 6033 0.6037

44102589- 8 3.9145 287.55 46.22 8.107 1.4139 0.9597 6066 0.6068

44102589- 9 3.9151 287.47 46.25 8.137 1.4143 0.9601 6055 0.6058

Table 2.b. Measured and calculated quantities for the beta ratio of 0.55 with the 6-inch

Sprenkle 46 pipe diameters upstream of the orifice plate.

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^

44042390- 3 3.8806 287.53 45.83 13.214 1.7943 1.2185 6054 0.6058

44042390- 4 3.8832 287.56 45.85 13.197 1.7961 1.2196 6063 0.6067

44042390- 5 4.0500 288.70 47.62 3.082 0.8857 0.5985 6074 0.6075

44042390- 6 4.0414 288.83 47.49 3.108 0.8880 0.6000 6072 0.6073

44042390- 7 3.9393 288.25 46.39 7.295 1.3442 0.9106 6069 0.6071

44042490- 1 3.9007 287.86 46.01 7.574 1.3574 0.9208 6040 0.6042

44042490- 2 3.6656 287.06 43.36 21.887 2.2356 1.5237 6023 0.6030

44042490- 3 3.6605 287.11 43.29 21.948 2.2349 1.5232 6017 0.6025

35
Table 3. a. Measured and calculated quantities for the beta ratio of 0.67 with the 3.8 fim upstrean pipe and 46 pipe diameters of straigt)t pipe upstream of the orifice plate.

Pipe Diameter = 10.366 cm (4.081 in) , 3.8 |im Ra Orif ice Diameter = 6.9840 cm (2. 7496 in)

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

45050289- 1 3.7063 288.22 43.64 8.400 2.2188 1.5073 6025 0.6028

45050289- 2 3.7284 288.26 43.90 8.442 2.2311 1.5151 6026 0.6029

45050289- 3 3.8914 288.75 45.74 4.379 1.6407 1.1107 6029 0.6030

45050289- 4 3.8893 288.74 45.72 4.459 1.6554 1.1207 6030 0.6031

45050289- 5 3.8481 288.38 45.29 5.782 1.8756 1.2715 6027 0.6029

45050289- 6 3.8351 288.68 45.09 5.757 1.8681 1.2657 6030 0.6031

45050289- 7 3.9556 288.97 46.46 2.661 1.2961 0.8763 6063 0.6064

45050289- 8 3.9348 288.91 46.22 2.685 1.2986 0.8784 6063 0.6064

45082989- 1 3.8527 286.81 45.62 3.927 1.5577 1.0600 6053 0.6054

45082989- 2 3.8492 286.95 45.55 3.885 1.5436 1.0501 6035 0.6036

45082989- 3 3.6286 285.98 43.09 8.482 2.2184 1.5167 6034 0.6036

45082989- 4 3.7554 286.46 44.52 6.053 1.9008 1.2961 6022 0.6023

45082989- 5 3.7565 286.34 44.56 6.126 1.9130 1.3048 6022 0.6024

45082989- 6 3.9022 287.12 46.15 2.705 1.2995 0.8831 6050 0.6050

45082989- 7 3.8988 287.14 46.11 2.732 1.3035 0.8858 6041 0.6042

Table 3.b. Measured and calculated quantities for the beta ratio of 0.67 with the 3.8 /jb upstream pipe and 56 pipe diameters of straight pipe upstream of the orifice plate.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 nm 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')

45051790- 1 3.8566 287.26 45.59 5.782 1.8834 1.2801 6033 0.6035

45051790- 2 3.8560 287.39 45.56 5.770 1.8794 1.2770 6029 0.6030

45051790- 3 3.9672 287.74 46.81 2.570 1.2785 0.8668 6063 0.6064

45051790- 4 3.9717 287.86 46.85 2.571 1.2798 0.8674 6065 0.6066

45051790- 8 3.7262 286.62 44.15 8.688 2.2692 1.5472 6025 0.6027

45051790- 9 3.7241 286.76 44.10 8.697 2.2674 1.5455 6020 0.6023

45051790- 10 3.9226 287.57 46.32 4.063 1.5933 1.0813 6041 0.6042

45051790- 11 3.9208 287.48 46.31 4.082 1.5992 1.0856 6050 0.6051

45051790- 12 3.9713 287.87 46.84 2.395 1.2338 0.8363 6059 0.6060

Table 3.C. Measured and calculated quantities for the beta ratio of 0.67 with the 6-inch

Sprenkle 46 pipe diameters upstream of the orifice plate.

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

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

(MPa) (K)

45051690- 1 3.8949 287 20

45051690- 2 3.8986 287 16 45051690- 3 3.7136 286 82 45051690- 4 3.7138 286 42 45051690- 5 3.8244 286 79

45051690- 6 3.8342 286 73

45051690- 8 3.9429 287 61

45051690- 9 3.9468 287 61

CY,

(kg/m") (kPa) (kg/s) (-10°)

46.05 4 311 1 6360 1 1117 6039 0.6040

46.10 4 297 1 6330 1 1097 6034 0.6036

43.97 8 727 2 2705 1 5475 6027 0.6030

44.03 8 685 2 2607 1 5424 6011 0.6014

45.29 6 151 1 9358 1 3178 6032 0.6033

45.41 6 194 1 9460 1 3247 6034 0.6036

46.55 2 737 1 3135 8911 6052 0.6053

46.60 2 737 1 3138 8913 6051 0.6052

36
Table 4. a. Measured and calculated quantities for the beta ratio of 0.73 with the 3.8 /im upstream pipe and 46 pipe diameters of straight pipe upstream of the orifice plate.

Pipe Diameter = 10.366 cm (4.081 in), 3 . 8 /zm Ra

Run ID

Orifice Diameter = 7.6197 cm (2.9999 in)

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

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

46050289- 1 3 8813 288 41 45 68 3.212 1 7653 1962 0.6014 0.6014

46050289- 2 3 8562 288 50 45 37 3.183 1 7476 1843 0.6001 0.6002

46050289- 3 3 8915 288 63 45 76 2.707 1 6218 0982 0.6013 0.6014

46050289- 4 3 8966 288 50 45 84 2.706 1 6235 0997 0.6015 0,6016

46050289- 5 3 7055 287 41 43 77 5.631 2 2875 5570 0.6012 0,6013

46050289- 6 3 6874 287 51 43 54 5.584 2 2673 5433 0.6000 0,6001

46050289- 7 3 7804 288 06 44 55 4.424 2 0466 3897 0.6015 0,6016

46050289- 8 3 7795 288 21 44 51 4.456 2 0507 3919 0.6008 0,6009

Table 4,b, Measured and calculated quantities for the beta ratio of 0.73 with the 3.8 fjtm upstream pipe and 56 pipe diameters of straight pipe upstream of the orifice plate.

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 CYz (MPa) (K) (kg/m^*) (kPa) (kg/s) (-10^)

46051790- 1 3.9302 287.76 46,37 2.630 1.6115 1.0930 6022 0.6022

46051790- 2 3.9333 287.53 46,45 2.628 1.6112 1.0934 6018 0.6019

46051790- 3 3.7514 286.92 44,40 5.361 2.2409 1.5263 5993 0.5994

46051790- 4 3.7515 286,61 44,45 5.344 2.2392 1.5264 5995 0.5996

46051790- 5 3.8251 287,08 45,25 4.331 2.0346 1.3840 5998 0.5999

46051790- 6 3.8200 287,20 45,16 4.341 2.0346 1.3837 5995 0.5996

46051790- 7 3.8923 287,23 46.02 3.239 1.7779 1.2080 6009 0.6010

46051790- 8 3.8896 287.23 45.99 3.255 1.7814 1.2105 6009 0.6010

Table 4.c. Measured and calculated quantities for the beta ratio of 0.73 with the 6-inch

Sprenkle 46 pipe diameters upstream of the orifice plate.

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

46051690- 1 3.8589 287.08 45.64 3.392 1.8129 1.2327 6012 0.6013

46051690- 2 3.8578 287.07 45.64 3.394 1.8156 1.2346 6020 0.6021

46051690- 3 3.7876 286.74 44.86 4.418 2.0532 1.3985 6018 0.6019

46051690- 4 3.7873 286.81 44.84 4.426 2.0540 1.3988 6016 0.6017

46051690- 5 3.8948 287.23 46.05 2.661 1.6171 1.0987 6029 0.6030

46051690- 6 3.8940 287.16 46.05 2.666 1.6175 1.0992 6024 0.6025

46051690- 7 3.7039 287.08 43.80 5.526 2.2685 1.5454 6016 0.6018

46051690- 8 3.7029 286.66 43,86 5.497 2.2632 1.5434 6014 0.6015

37
Table 5. Measured and calculated quantities for the beta ratio of 0.43 with the in-line tube

bundle at 7 pipe diameters upstream of the orifice plate.

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

43050889- 1 3.9887 289.22 46.80 14.143 1.0945 0.7393 0.6026 0.6030

43050889- 2 3.9807 289.34 46.69 13.935 1.0821 0.7308 0.6009 0.6014

43050889- 3 3.9087 288.67 45.96 27.878 1.5140 1.0249 0.5986 0.5996

43050889- 4 3.9061 288.66 45.93 27.794 1.5132 1.0245 0.5994 0.6003

43050889- 5 4.1318 289.95 48.35 4.647 0.6376 0.4292 0.6029 0.6030

43050889- 6 4.1098 289.98 48.09 4.653 0.6357 0.4280 0.6024 0.6025

43050889- 7 3.8163 287.91 45.00 49.991 2.0104 1.3650 0.5992 0.6008

43050889- 8 3.8107 288.09 44.90 49.285 1.9966 1.3551 0.6000 0.6016

43050989- 1 3.8528 288.74 45.28 29.569 1.5463 1.0473 0.5980 0.5990

43050989- 2 3.8440 288.83 45.17 29.270 1.5384 1.0418 0.5988 0.5997

43050989- 3 3.9182 289.23 45.97 15.755 1.1403 0.7708 0.6001 0.6006

43050989- 4 3.9035 289.32 45.78 15.785 1.1399 0.7705 0.6005 0.6011

43050989- 1 4.1488 289.98 48.55 4.991 0.6615 0.4452 0.6023 0.6025

43050989- 2 4.1553 289.91 48.64 4.808 0.6509 0.4380 0.6033 0.6034

43050989- 3 3.8413 288.22 45.24 49.439 2.0069 1.3612 0.5999 0.6015

43050989- 4 3.8318 288.10 45.15 48.816 1.9912 1.3511 0.5996 0.6012

Table 6. Measured and calculated quantities for the beta ratio of 0.55 with the in-line tube

bundle at 7 pipe diameters upstream of the orifice plate.

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. c CYz (MPa) (K) (kg/m^) (kPa) (kg/s) (-10^)

44050489- 1 4.0638 289.32 47.67 3.259 0.9046 0.6103 .6030 0.6031

44050489- 2 4.0442 289.35 47.43 3.225 0.8998 0.6072 .6043 0.6044

44050489- 3 3.7285 287.47 44.03 21.404 2.2194 1.5101 6000 0.6006

44050489- 4 3.7413 288.09 44.08 21.366 2.2161 1.5053 5993 0.6000

44050489- 1 3.8806 288.44 45.67 13.234 1.7726 1.2011 5987 0.5991

44050489- 2 3.8687 287.96 45.61 13.106 1.7671 1.1989 6001 0.6005

44050489- 3 3.9339 288.64 46.26 7.699 1.3635 0.9229 6001 0.6003

44050489- 4 3.9429 288.64 46.37 7.745 1.3706 0.9275 6007 0.6009

44051189- 1 4.0865 289.33 47.93 2.951 0.8621 0.5815 6021 0.6022

44051189- 2 4.0636 289.37 47.66 2.934 0.8572 0.5783 6022 0.6023

44051189- 3 3.7074 287.64 43.75 21.906 2.2466 1.5283 6019 0.6026

44051189- 4 3.7122 287.84 43.78 22.253 2.2596 1.5363 6006 0.6013

44051189- 5 3.9513 288.62 46.47 7.807 1.3815 0.9349 6024 0.6026

44051189- 6 3.9460 288.50 46.43 7.948 1.3928 0.9429 6021 0.6024

44051189- 7 3.8817 288.48 45.67 13.020 1.7662 1.1966 6013 0.6017

44051189- 8 3.8871 288.35 45.76 12.979 1.7647 1.1959 6012 0.6016

44102589- 1 3.9315 287.49 46.44 7.558 1.3592 0.9225 6026 0.6028

44102589- 2 3.9366 287.59 46.48 7.566 1.3605 0.9231 6026 0.6028

44102589- 3 4.0574 288.21 47.80 2.714 0.8280 0.5602 6040 0.6041

44102589- 4 4.0543 288.17 47.77 2.731 0.8287 0.5607 6028 0.6029

44102589- 5 3.7032 286.83 43.84 20.826 2.1821 1.4875 0. 5994 0.6000

44102589- 6 3.6892 286.81 43.68 21.687 2.2220 1.5150 0, 5992 0.5999

44102589- 7 3.8272 287.03 45.28 14.041 1.8195 1.2378 0. 5991 0.5996

44102589- 8 3.8230 286.94 45.25 14.223 1.8344 1.2483 0. 6004 0.6008

38
Table 7. Measured and calculated quantities for the beta ratio of 0.67 with the in-line tube

bundle at 7 pipe diameters upstream of the orifice plate.

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

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

(MPa) (K)

45050889- 1 3 .8667 288 26

45050889- 2 3 .8592 288 27 45050889- 3 3 .9753 288 94

45050889- 4 3 .9624 288 98

45050889- 5 3 .9241 288 77 45050889- 6 3 .9355 288 74 45050889- 7 3 .7096 288 03 45050889- 8 3 ,7212 287 42 45050989- 1 4 0159 289 01

45050989- 2 3 9993 288 92 45050989- 3 3 9907 288 51 45050989- 4 3 9630 288 53 45050989- 5 3 8911 288 33 45050989- 6 3 8937 288 30

45050989- 7 3 7158 288 02 45050989- 8 3 7319 287 86

45042790- 1 3 8784 288 29 45042790- 2 3 8514 288 05

45042790- 3 3 7877 287 84

45042790- 4 3 7652 287 79 45042790- 5 3 6369 287. 47 45042790- 6 3 6277 287. 27 45042790- 7 3 8547 288. 32 45042790- 8 3 8321 288. 43 45042790- 9 3 8321 288. 22

Table 8. Me asured and calcu].at<

CY,

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

45.53 6.260 1.9529 1.3240 6015 0.6017

45.44 6.270 1.9488 1.3214 6004 0.6006

46.70 2.570 1.2671 0.8565 6016 0.6016

46.54 2.591 1.2721 0.8600 6026 0.6026

46.12 3.895 1.5512 1.0497 6020 0.6021

46.26 3.887 1.5491 1.0482 6008 0.6009

43.71 8.897 2.2712 1.5436 5988 0.5991

43.95 8.867 2.2758 1.5488 5994 0.5997

47.16 2.522 1.2623 0.8528 6019 0.6020

46.98 2.531 1.2589 0.8508 6004 0.6005

46.95 3.905 1.5651 1.0589 6012 0.6013

46.45 3.865 1.5484 1.0479 6000 0.6001

45.81 5.971 1.9026 1.2893 5983 0.5984

45.84 5.936 1.8992 1.2871 5987 0.5989

43.79 9.218 2.3120 1.5712 5984 0.5986

44.01 8.982 2.2872 1.5547 5982 0.5984

45.67 3.970 1.5521 1.0520 5995 0.5996

45.39 3.961 1.5471 1.0497 6001 0.6003

44.67 6.001 1.8842 1.2800 5985 0.5987

44.41 5.985 1.8785 1.2766 5992 0.5994

42.95 8.922 2.2489 1.5318 5974 0.5977

42.87 8.884 2.2450 1.5300 5982 0.5984

45.38 3.069 1.3566 0.9198 5980 0.5981

45.09 3.096 1.3606 0.9225 5990 0.5991

45.13 3.080 1.3613 0.9234 6005 0.6006

0.7 3 with the in-line tube

bundle at 7 pipe diameters upstream of the orifice plate.

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

46050489- 1 3.8230 288.32 45.01 4.378 2.0277 1.3753 .5960 0.5961

46050489- 2 3.8186 288.25 44.97 4.369 2.0198 1.3702 .5946 0.5947

46050489- 3 3.7091 287.74 43.76 5.609 2.2637 1.5395 5962 0.5963

46050489- 4 3.7214 287.05 44.02 5.579 2.2612 1.5402 5954 0.5955

46050489- 5 3.8595 288.24 45.45 3.559 1.8321 1.2423 5944 0.5945

46050489- 6 3.8439 288.33 45.25 3.602 1.8420 1.2489 5953 0.5954

46050489- 7 3.9015 288.48 45.91 2.640 1.5934 1.0793 5973 0.5973

46050489- 8 3.9039 288.53 45.92 2.659 1.5971 1.0816 5964 0.5964

46051189- 1 3.8889 288.66 45.73 2.638 1.5910 1.0773 5978 0.5978

46051189- 2 3.8862 288.65 45.70 2.626 1.5839 1.0726 5966 0.5967

46051189- 3 3.7989 288.26 44.73 4.432 2.0282 1.3762 5943 0.5944

46051189- 4 3.7958 288.51 44.65 4.415 2.0234 1.3721 5946 0.5947

46051189- 5 3.8400 288.18 45.23 3.541 1.8245 1.2376 5949 0.5950

46051189- 6 3.8389 288.02 45.25 3.564 1.8316 1.2429 5952 0.5952

46051189- 7 3.6573 287.43 43.31 5.872 2.2934 1.5617 5933 0.5935

46051189- 8 3.6806 287.58 43.45 5.856 2.2934 1.5609 5932 0.5934

46042690- 1 3.8636 287.94 45.55 2.474 1.5325 1.0399 5957 0.5958

46042690- 2 3.8479 288.11 45.34 2.466 1.5286 1.0370 5967 0.5967

46042690- 3 3.7401 287.42 44.18 4.266 1.9817 1.3483 5957 0.5958

46042690- 4 3.7325 287.35 44.10 4.263 1.9767 1.3452 5948 0.5949

46042690- 5 3.6320 287.44 42.89 5.664 2.2437 1.5285 5940 0.5941

46042690- 6 3.6274 286.92 42.92 5.629 2.2433 1.5302 5955 0.5956

46042690- 7 3.7699 287.55 44.51 3.321 1.7537 1.1924 5952 0.5953

46042690- 8 3.7612 287.29 44.45 3.356 1.7633 1.1998 0. 5957 0.5958

39
Table 9. Measured and calculated quantities for the beta ratio of 0.43 with the in-line tube

bundle at 11 pipe diameters upstream of the orifice plate.

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^

43052589- 1 4.0096 288.39 47.20 15.262 1.1465 0.7757 0..6050 0.6055

43052589- 2 4.0088 288.44 47.18 15.212 1.1421 0.7727 0,,6038 0.6043

43052589- 3 3.8380 287.80 45.27 47.747 1.9802 1.3445 0,,6021 0.6037

43052589- 4 3.8433 287.44 45.40 47.481 1.9743 1.3416 0.,6012 0.6028

43052589- 5 4.1497 289.02 48.74 4.835 0.6542 0.4412 0,,6039 0.6041

43052589- 6 4.1289 289.15 48.47 4.764 0.6470 0.4364 0.,6035 0.6037

43052589- 7 3.9517 287.94 46.59 28.663 1.5566 1.0551 0.,6028 0.6038

43052589- 8 3.9435 287.91 46.50 28.129 1.5406 1.0445 0,,6029 0.6038

Table 10. Measured and calculated quantities for the beta ratio of 0.55 with the in-line tube

bundle at 11 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 fim 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)

44052489- 1 3.,9832 288..24 44052489- 2 3,,9784 288..28 44052489- 3 3..9810 288,.24 44052489- 4 3,,7272 286..79 44052489- 5 3.,7377 287,.32 44052489- 6 3..8926 287..78 44052489- 7 3,.8759 287,.64 44052489- 8 4,.1092 288..64 44052489- 9 4,.1087 288,.77 44101989- 2 3..9477 287,.32 44101989- 3 3,.9466 287,.47 44101989- 4 3,.8598 287,.19 44101989- 5 3..8608 286,.94 44101989- 6 3..6777 286..15 44101989- 7 3,.6857 286..60 44101989- 8 4,.0805 287,.81 44101989- 9 4,.0775 287..89 44102489- 1 3,.8572 286..88 44102489- 2 3,.8561 287..18 44102489- 3 3,.7017 286,.67 44102489- 4 3,.7061 285..92 44102489- 8 4,.0027 287,.20 44102489- 9 4..0051 287,.38 44102489-:10 4..1207 287,.89

kg/m') (kPa) (kg/s) ( H-10^)

46.91 7.310 1.3511 0..9148 0,.6060 0.6062

46.85 7.263 1.3405 0,.9076 0,.6035 0.6037

46.89 7.254 1.3403 0..9075 0,.6036 0.6038

44.13 21.313 2.2155 1,.5099 0,.5996 0.6002

44.17 21.154 2.2154 1,.5077 0,,6015 0.6022

45.92 12.925 1.7695 1,,2007 0,.6031 0.6035

45.75 13.087 1.7802 1,,2086 0,.6041 0.6045

48.33 3.074 0.8887 0,.6002 0..6058 0.6059

48.30 3.096 0.8933 0,.6032 0,.6069 0.6070

46.66 7.849 1.3872 0,.9417 0,.6021 0.6023

46.62 7.857 1.3873 0,.9415 0,.6021 0.6023

45.64 13.214 1.7794 1,.2096 0,.6016 0.6020

45.69 13.104 1.7722 1,.2054 0,.6013 0.6017

43.65 21.788 2.2232 1,.5184 0..5983 0.5990

43.67 21.705 2.2251 1,.5179 0,,5998 0.6005

48.14 3.044 0.8798 0..5956 0,,6038 0.6039

48.09 3.096 0.8857 0,.5995 0,,6031 0.6031

45.66 13.577 1.8082 1..2301 0.,6030 0.6034

45.60 13.540 1.8057 1..2276 0.,6034 0.6038

43.85 21.367 2.2220 1,.5153 0.,6024 0.6031

44.03 21.217 2.2160 1.,5139 0.,6018 0.6025

47.33 7.358 1.3602 0.,9231 0.,6054 0.6056

47.33 7.353 1.3574 0.,9208 0.,6044 0.6046

48.60 2.741 0.8431 0,,5704 0,.6069 0.6070

40
Table 11. Measured and calculated quantities for the beta ratio of 0.67 with the in-line tube

bundle at 11 pipe diameters upstream of the orifice plate.

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 CYz

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

45052489- 1 3.7874 287.39 44.74 8.263 2.2280 1.5152 6025 0.6028

45052489- 2 3.7683 287.68 44.47 8.162 2.2088 1.5014 6029 0.6031

45052489- 3 4.0172 288.39 47.29 2.586 1.2887 0.8718 6061 0.6062

45052489- 4 4.0087 288.42 47.18 2.624 1.2929 0.8747 6043 0.6044

45052489- 5 3.9628 288.14 46.69 3.857 1.5584 1.0557 6040 0.6041

45052489- 6 3.9672 288.11 46.75 3.857 1.5586 1.0559 6037 0.6038

45052489- 7 3.8798 287.72 45.78 5.871 1.9003 1.2898 6028 0.6030

45052489- 8 3.8834 287.49 45.87 5.823 1.8971 1.2884 6037 0.6039

45072489- 1 3.9871 287.33 47.12 2.522 1.2682 0.8605 6051 0.6052

45072489- 2 4.0226 287.43 47.53 2.521 1.2720 0.8625 6044 0.6045

45072489- 3 3.8463 286.90 45.53 6.038 1.9219 1.3076 6030 0.6031

45072489- 4 3.8507 286.66 45.63 6.031 1.9164 1.3046 6008 0.6010

45072489- 5 3.7372 286.57 44.29 8.106 2.1920 1.4945 6016 0.6018

45072489- 6 3.7365 286.09 44.36 8.057 2.1870 1.4929 6015 0.6018

45072489- 7 3.9090 286.80 46.29 4.016 1.5808 1.0750 6031 0.6032

45072489- 8 3.9043 286.92 46.21 4.072 1.5938 1.0836 6043 0.6044

Table 12. Measured and calculated quantities for the beta ratio of 0.73 with the in-line tube

bundle at 11 pipe diameters upstream of the orifice plate.

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

Run ID Pressure Temperat

(MPa) (K)

46052589- 1 3.7105 286.86

46052589- 2 3.7188 287.33

46052589- 3 3.8089 287.67

46052589- 4 3.7943 287.57

46052589- 5 3.9144 287.98

46052589- 6 3.9089 287.88

46052589- 7 3.9019 287.78

46052589- 8 3.9033 287.89

46072589- 1 3.8473 286.89

46072589- 2 3.8393 286.82

46072589- 3 3.9396 287.08

46072589- 4 3.9211 287.13

46072589- 5 3.7126 285.96

46072589- 6 3.7172 286.52

46072589- 7 3.8722 286.99

46072589- 8 3.8511 286.82

CY,

(kg/m') (kPa) (kg/s) (-10'')

43.92 5.542 2 .2609 1 5409 5979 0.5981

43.94 5.527 2 .2588 1 .5376 5981 0.5982

44.95 4.438 2 0449 1 3894 5974 0.5975

44.80 4.431 2 0439 1 3892 5986 0.5987

46.15 2.628 1 .5966 1 0826 5983 0.5984

46.10 2.678 1 6088 1 0912 5975 0.5976

46.03 3.252 1 .7779 1 2063 5996 0.5996

46.03 3.256 1 .7779 1 2059 5993 0.5993

45.54 4.104 1 9855 1 3509 5993 0.5994

45.46 4.108 1 9844 1 3505 5992 0.5993

46.61 2.571 1 5891 1 0795 5991 0.5991

46.38 2.574 1 5908 1 0808 6008 0.6009

44.10 5.533 2 2689 1 5498 5993 0.5995

44.06 5.503 2 2621 1 5429 5995 0.5996

45.82 3.464 1 8355 1 2482 6012 0.6013

45.60 3.502 1 8402 1 2522 6009 0.6009

41
Table 13. Measured and calculated quantities for the beta ratio of 0.55 with the in-line tube

bundle at 17 pipe diameters upstream of the orifice plate.

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

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

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

44101989- 1 3.6757 286.76 43.53 21.248 2.2070 1.5052 0.,6023 0.6030

44101989- 3 3.8436 287.25 45.43 13.154 1.7775 1.2084 0,.6037 0.6041

44101989- 4 3.8400 287.06 45.43 13.255 1.7804 1.2110 0,.6024 0.6028

44101989- 5 3.6704 286.63 43.48 21.653 2.2286 1.5205 0,.6028 0.6035

44101989- 7 4.0868 288.06 48.17 3.071 0.8864 0.5997 0..6055 0.6056

44101989- 8 4.0899 288.14 48.19 3.083 0.8892 0.6014 0,.6060 0.6061

44101989- 9 3.9585 287.58 46.74 7.278 1.3435 0.9114 0..6050 0.6052

44101989-10 3.9545 287.62 46.68 7.253 1.3424 0.9105 0,.6059 0.6061

Table 14. Measured and calculated quantities for the beta ratio of 0.67 with the in-line tube

bundle at 17 pipe diameters upstream of the orifice plate.

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

45072689- 1 3.8993 287.16 46.11 4.096 1.6006 1.0877 0,.6058 0.6059

45072689- 2 3.8946 287.25 46.04 4.097 1.5997 1.0868 0,.6058 0.6059

45072689- 3 3.6755 286.52 43.56 8.737 2.2670 1.5470 0,.6043 0.6045

45072689- 4 3.6805 285.69 43.76 8.617 2.2567 1.5430 0,.6043 0.6046

45072689- 5 3.8170 286.82 45.19 6.127 1.9343 1.3168 0,.6045 0.6047

45072689- 6 3.7946 286.92 44.91 6.174 1.9361 1.3180 0,.6047 0.6048

45072689- 7 3.9248 287.42 46.37 2.764 1.3183 0.8950 0,.6057 0.6058

45072689- 8 3.9243 287.46 46.36 2.813 1.3311 0.9036 0,.6063 0.6063

45082289- 1 3.6154 286.06 42.92 8.656 2.2248 1.5210 0..6002 0.6004

45082289- 2 3.6117 285.70 42.94 8.497 2.2132 1.5145 0..6026 0.6028

45082289- 3 3.6171 285.66 43.01 8.459 2.2109 1.5130 0,.6028 0.6030

45082289- 4 3.7407 286.87 44.28 6.042 1.8983 1.2933 0,.6036 0.6037

45082289- 5 3.7265 286.38 44.19 6.055 1.8950 1.2928 0..6025 0.6027

45082289- 6 3.8754 287.06 45.85 2.611 1.2763 0.8677 0,.6068 0.6069

45082289- 7 3.8707 287.20 45.77 2.602 1.2700 0.8632 0.,6054 0.6055

45082289- 8 3.8198 287.10 45.18 3.952 1.5525 1.0561 0,,6043 0.6044

45082289- 9 3.8162 286.86 45.18 3.915 1.5461 1.0524 0,,6047 0.6048

42
Table 15. Measured and calculated quantities for the beta ratio of 0.7 3 with the in-line tube

bundle at 17 pipe diameters upstream of the orifice plate.

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

46072689- 1 3.8273 286.83 45.32 3.396 1.8070 1.2299 6011 0.6012

46072689- 2 3.8218 286.67 45.28 3.388 1.8035 1.2281 6009 0.6010

46072689- 3 3.6337 286.00 43.15 5.806 2.3016 1.5734 6000 0.6001

46072689- 4 3.6691 286.44 43.50 5.468 2.2437 1.5315 6003 0.6004

46072689- 5 3.7760 286.49 44.76 4.371 2.0326 1.3855 5996 0.5997

46072689- 6 3.7614 286.71 44.55 4.391 2.0366 1.3877 6009 0.6010

46072689- 7 3.8638 286.90 45.74 2.551 1.5778 1.0733 6028 0.6029

46072689- 8 3.8750 287.06 45.84 2.551 1.5805 1.0746 6031 0.6032

46082289- 1 3.8300 287.11 45.30 2.516 1.5616 1.0621 6037 0.6038

46082289- 2 3.8198 287.04 45.19 2.485 1.5504 1.0548 6037 0.6038

46082289- 3 3.5788 285.97 42.50 5.739 2.2756 1.5567 6012 0.6013

46082289- 4 3.5946 285.61 42.75 5.692 2.2683 1.5528 6000 0.6001

46082289- 5 3.7035 286.23 43.94 4.449 2.0368 1.3904 6011 0.6012

46082289- 6 3.6843 286.18 43.72 4.423 2.0223 1.3810 6000 0.6001

46082289- 7 3,7694 286.91 44.61 3.224 1.7426 1.1867 5996 0.5997

46082289- 8 3.7672 286.48 44.66 3.281 1.7636 1.2023 6012 0.6013

Table 16. Measured and calculated quantities for the beta ratio of 0.55 with the in-line tube

bundle at 27 pipe diameters upstream of the orifice plate.

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 CYz (MPa) (K) (kg/ra^) (kPa) (kg/s) (^10^)

44102489- 1 3.9072 287.54 46.14 8.013 1.3997 0.9502 6046 0.6048

44102489- 2 3.9055 287.62 46.10 7.995 1.3998 0.9501 6055 0.6058

44102489- 3 4.0438 288.28 47.62 2.675 0.8245 0.5578 6069 0.6070

44102489- 4 4.0421 288.36 47.59 2.676 0.8248 0.5579 6072 0.6073

44102489- 5 3.6710 286.98 43.43 20.908 2.1859 1.4900 6020 0.6027

44102489- 6 3.6650 286.02 43.52 21.535 2.2233 1.5193 6027 0.6034

44102489- 7 3.8026 287.12 44.97 14.145 1.8302 1.2452 6025 0.6029

44102489- 8 3.8016 287.13 44.96 14.307 1.8417 1.2530 6029 0.6034

43
Table 17. Measured and calculated quantities for the beta ratio of 0.67 with the in-line tube

bundle at 27 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.366> cm (4.081 in) , 3.8 /xm Ra Ori.fice Diameter = 6.9840 cm (2. 7496 in)

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

45082389- 1 3.8480 287.38 45.47 4.057 1.5900 1.0805 0,.6089 0.6090

45082389- 2 3.8431 287.23 45.43 4.044 1.5837 1.0767 0,.6077 0.6078

45082389- 3 3.9101 287.56 46.17 2.595 1.2845 0.8719 0,.6104 0.6105

45082389- 4 3.9101 287.62 46.16 2.601 1.2837 0.8713 0,.6093 0.6094

45082389- 5 3.7781 286.79 44.74 5.773 1.8743 1.2766 0,.6066 0.6067

45082389- 6 3.7706 286.68 44.67 5.724 1.8622 1.2688 0,.6057 0.6059

45082389- 7 3.6175 285.75 43.00 8.774 2.2581 1.5449 0,.6046 0.6048

45082389- 8 3.6184 286.24 42.93 8.655 2.2402 1.5308 0,.6043 0.6046

45082889- 1 3.8280 286.62 45.36 6.090 1.9431 1.3232 0,.6080 0.6082

45082889- 2 3.8296 286.66 45.37 6.091 1.9377 1.3194 0,.6062 0.6064

45082889- 3 3.8324 286.67 45.40 6.075 1.9355 1.3179 0,.6061 0.6063

45082889- 4 3.9537 287.17 46.76 2.662 1.3044 0.8858 0,.6082 0.6083

45082889- 5 3.9607 287.32 46.81 2.694 1.3175 0.8942 0..6102 0.6103

45082889- 6 3.9698 287.34 46.92 2.696 1.3193 0.8954 0,.6102 0.6102

45082889- 7 3.6977 286.55 43.82 8.602 2.2593 1.5412 0,.6051 0.6054

45082889- 8 3.6988 286.49 43.84 8.545 2.2493 1.5346 0,.6043 0.6045

45082889- 9 3.8997 286.94 46.16 4.202 1.6233 1.1037 0..6063 0.6064

45082889-:10 3.8857 286.67 46.04 4.283 1.6372 1.1140 0..6064 0.6065

45102389- 1 3.6379 286.59 43.10 8.557 2.2401 1.5291 0,.6065 0.6068

45102389- 2 3.6406 286.45 43.16 8.504 2.2300 1.5227 0..6053 0.6056

45102389- 3 3.7612 287.24 44.46 6.235 1.9408 1.3207 0,.6062 0.6064

45102389- 4 3.7676 287.13 44.55 6.304 1.9556 1.3310 0.,6068 0.6070

45102389- 5 3.9030 287.24 46.14 2.918 1.3585 0.9229 0.,6090 0.6091

45102389- 7 3.8742 287.05 45.84 4.011 1.5854 1.0779 0,,6082 0.6083

45102389- 8 3.8776 287.21 45.85 3.976 1.5774 1.0720 0.,6077 0.6078

45050990- 2 3.8393 287.94 45.26 4.020 1.5765 1.0700 0,,6079 0.6080

45050990- 3 3.8652 287.83 45.59 4.023 1.5800 1.0723 0,,6068 0.6069

45050990- 4 3.8727 287.87 45.67 2.582 1.2714 0.8627 0.,6090 0.6091

45050990- 5 3.8604 287.98 45.51 2.610 1.2743 0.8646 0,,6082 0.6083

45050990- 6 3.6417 286.97 43.08 8.396 2.2065 1.5047 0,,6033 0.6035

45050990- 7 3.6364 287.14 43.00 8.332 2.1974 1.4979 0.,6037 0.6039

45050990- 8 3.7273 287.68 43.98 6.249 1.9283 1.3114 0.,6049 0.6050

45050990- 9 3.7341 287.48 44.10 6.338 1.9455 1.3235 0.,6052 0.6054

44
Table 18. Measured and calculated quantities for the beta ratio of 0.73 with the in-line tube

bundle at 27 pipe diameters upstream of the orifice plate.

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

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

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

46082389- 1 3.7923 286.98 44.87 3.358 1.7904 .2187 0,.6019 0.6020

46082389- 2 3.7834 286.97 44.77 3.325 1.7820 .2132 0,.6027 0.6027

46082389- 3 3.7269 287.02 44.09 4.211 1.9838 .3513 0..6007 0.6008

46082389- 4 3.7298 286.92 44.14 4.208 1.9855 .3527 0.,6011 0.6012

46082389- 5 3.6366 286.52 43.10 5.507 2.2482 .5349 0.,6021 0.6023

46082389- 6 3.6317 285.58 43.20 5.411 2.2301 .5261 0.,6019 0.6020

46082389- 7 3.8364 287.09 45.38 2.678 1.6121 .0964 0,,6034 0.6035

46082389- 8 3.8470 287.07 45.51 2.706 1.6236 .1042 0.,6037 0.6038

46082889- 1 3.6363 286.31 43.13 5.579 2.2515 .5379 0.,5989 0.5990

46082889- 2 3.6451 285.50 43.37 5.530 2.2512 .5406 0,,5998 0.5999

46082889- 3 3.7459 286.70 44.37 4.373 2.0302 .3836 0.,6014 0.6015

46082889- 4 3.7334 286.33 44.28 4.363 2.0213 .3790 0.,6000 0.6001

46082889- 5 3.8513 286.84 45.60 2.735 1.6281 .1078 0.,6017 0.6018

46082889- 6 3.8816 286.62 46.00 2.568 1.5834 .0776 0,,6012 0.6013

46082889- 7 3.8538 286.92 45.62 3.265 1.7781 .2096 0,,6013 0.6014

46082889- 8 3.8657 286.63 45.81 3.255 1.7813 .2125 0,,6020 0.6021

46102389- 1 3.7216 286.97 44.03 4.297 2.0050 .3660 0,,6014 0.6015

46102389- 2 3.7252 287.10 44.06 4.302 2.0046 .3652 0.,6008 0.6009

46102389- 3 3.6368 285.91 43.20 5.345 2.2125 ,5128 0.,6008 0.6009

46102389- 4 3.6425 285.69 43.31 5.297 2.2104 .5120 0.,6022 0.6023

46102389- 5 3.8257 287.22 45.23 2.704 1.6116 .0959 0.,6014 0.6015

46102389- 6 3.8305 287.09 45.31 2.761 1.6323 ,1103 0.,6022 0.6023

46102389- 7 3.7895 287.11 44.82 3.445 1.8158 .2357 0.,6030 0.6031

46102389- 8 3.7921 287.32 44.81 3.439 1.8074 ,2293 0.,6008 0.6009

46050990- 1 3.8222 287.76 45.10 3.279 1.7757 ,2060 0.,6025 0.6026

46050990- 2 3.8318 287.44 45.26 3.280 1.7797 ,2095 0,,6027 0.6028

46050990- 3 3.7434 287.58 44.19 4.236 1.9987 ,3593 0.,6028 0.6029

46050990- 4 3.7553 287.53 44.34 4.241 2.0028 ,3620 0.,6026 0.6027

46050990- 5 3.8291 287.88 45.15 2.583 1.5781 ,0714 0.,6029 0.6030

46050990- 6 3.8819 287.74 45.80 2.588 1.5974 ,0842 0.,6054 0.6055

46050990- 7 3.9078 287.73 46.11 2.585 1.6022 ,0871 0.,6055 0.6056

46050990- 8 3.6670 286.78 43.42 5.398 2.2349 ,5242 0..6023 0.6025

46050990- 9 3.6610 287.41 43.24 5.394 2.2324 ,5203 0..6031 0.6033

45
Table 19. Measured and calculated quantities for the beta ratio of 0.67 with the in-line tube

bundle at 27 pipe diameters upstream of the orifice plate and with the 6-inch

Sprenkle at 46 pipe diameters upstream of the orifice plate.

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 CYz (MPa) (K) (kg/ra^) (kPa) (kg/s) (-10^)

45050890- 1 3.7890 287.76 44.70 5.996 1.9009 1.2915 0..6038 0.6040

45050890- 2 3.7821 287.83 44.61 5.987 1.9010 1.2915 0,.6050 0.6052

45050890- 3 3.7789 287.79 44.58 5.996 1.8949 1.2875 0..6028 0.6029

45050890- 4 3.8801 288.46 45.66 2.610 1.2689 0.8597 0..6046 0.6047

45050890- 5 3.8762 288.46 45.61 2.641 1.2748 0.8638 0..6041 0.6042

45050890- 6 3.8263 288.05 45.09 4.166 1.5954 1.0827 0..6054 0.6055

45050890- 7 3.8261 287.98 45.10 4.161 1.5941 1.0820 0,.6052 0.6053

45050890- 8 3.6327 287.70 42.86 8.835 2.2584 1.5375 0..6035 0.6037

45050890- 9 3.6298 287.59 42.84 8.824 2.2552 1.5358 0,.6031 0.6034

45050890- 10 3.7731 287.40 44.57 5.899 1.8819 1.2800 0..6036 0.6037

45050890- 11 3.8201 287.88 45.05 3.981 1.5557 1.0563 0,.6042 0.6043

45050890- 12 3.8589 288.25 45.44 2.690 1.2859 0.8719 0..6049 0.6050

45051090- 1 3.7964 287.77 44.78 6.103 1.9197 1.3042 0..6039 0.6040

45051090- 2 3.7912 287.36 44.79 6.087 1.9190 1.3050 0,,6043 0.6045

45051090- 3 3.8666 287.86 45.60 4.028 1.5705 1.0658 0..6027 0.6028

45051090- 4 3.8629 287.73 45.58 4.041 1.5776 1.0710 0,.6046 0.6047

45051090- 5 3.8973 288.19 45.91 2.566 1.2626 0.8559 0.,6051 0.6052

45051090- 6 3.8951 287.93 45.93 2.560 1.2624 0.8563 0.,6056 0.6056

45051090- 7 3.6815 287.44 43.48 8.156 2.1882 1.4898 0.,6042 0.6045

45051090- 8 3.6804 287.63 43.44 8.135 2.1816 1.4846 0.,6035 0.6037

Table 20. Measured and calculated quantities for the beta ratio of 0.73 with the in-line tube

bundle at 27 pipe diameters upstream of the orifice plate and with the 6-inch

Sprenkle at 46 pipe diameters upstream of the orifice plate.

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

46050890- 1 3.7422 287.56 44.18 5.215 2.2312 1.5176 0,.6065 0.6067

46050890- 2 3.7359 287.83 44.06 5.209 2.2253 1.5126 0,.6061 0.6062

46050890- 3 3.8573 287.63 45.53 3.292 1.7986 1.2214 0,.6062 0.6063

46050890- 4 3.8517 287.59 45.47 3.286 1.7960 1.2198 0,.6063 0.6063

46050890- 5 3.8862 287.82 45.84 2.432 1.5517 1.0529 0..6065 0.6065

46050890- 6 3.8862 287.80 45.84 2.423 1.5450 1.0484 0..6049 0.6049

46050890- 7 3.7858 287.43 44.72 4.055 1.9703 1.3398 0,.6037 0.6038

46050890- 8 3.7826 287.26 44.71 4.045 1.9687 1.3393 0,.6041 0.6042

46050890- 9 3.7550 287.55 44.33 4.062 1.9640 1.3356 0.,6039 0.6040

46050890- 10 3.6428 287.49 43.01 5.413 2.2337 1.5212 0.,6040 0.6041

46051090- 1 3.8300 287.93 45.15 2.642 1.6008 1.0867 0.,6048 0.6049

46051090- 2 3.8235 287.66 45.13 2.640 1.5993 1.0864 0.,6046 0.6047

46051090- 3 3.7236 287.67 43.94 4.246 1.9988 1.3594 0.,6038 0.6039

46051090- 4 3.7139 286.93 43.95 4.227 1.9934 1.3583 0.,6035 0.6036

46051090- 5 3.6383 287.48 42.96 5.376 2.2175 1.5104 0.,6020 0.6022

46051090- 6 3.6353 286.79 43.04 5.323 2.2119 1.5091 0.,6029 0.6031

46051090- 7 3.7541 287.27 44.37 3.394 1.7969 1.2228 0.,6042 0.6043

46051090- 8 3.7511 287.54 44.29 3.424 1.8037 1.2267 0. 6044 0.6045

46
Table 21. Measured and calculated quantities for the beta ratio of 0.43 with two elbows in

plane at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 ^m Ra Orifice Diameter = 4.4445 cm (1.7498 in)

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

43021087- 1 3.9541 289 .05 43021087- 2 3.9463 289 68 43021087- 3 3.8360 288 33 43021087- 4 3.8318 290 09

43021087- 5 4.1393 287 40

43021087- 6 4.1466 286 32 43021187- 1 3.9837 288 05

43021187- 2 3.9852 287 96

43021187- 3 3.9022 287 02

43021187- 4 3.9016 288 97

43021187- 5 3.9022 287 94

43021187- 6 4.1994 287 81

43021187- 7 4.1933 287 88

cy. (kg/m") (kPa) (kg/s) (-10°)

46.43 29 067 1 5602 1 0545 6009 6018

46.22 28 782 1 5469 1 0440 6000 6009

45.16 49 987 2 0078 1 3612 5971 5988

44.81 49 840 1 9986 1 3494 5976 5992

48.92 5 722 7141 4835 6047 6049

49.21 5 567 7045 4782 6032 6034

46.95 29 802 1 5906 1 0773 6016 6025

46.99 29 690 1 5870 1 0751 6011 6021

46.17 49 647 2 0328 1 3815 6000 6017

45.82 49 836 2 0257 1 3702 5990 6006

46.01 49 529 2 0243 1 3727 5993 6009

49.55 6 916 7879 5326 6030 6033

49.47 6 905 7862 5314 6027 6029

Table 22. Measured and calculated quantities for the beta ratio of 0.55 with two elbows in

plane at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 /im Ra Orifice Diameter = 5.7137 cm (2.2495 in)

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

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

44021087- 1 3.9580 288.59 46.55 10.774 1.6232 1.0983 6020 0.6023

44021087- 2 3.9547 289.36 46.38 10.754 1.6157 1.0912 6009 0.6012

44021087- 3 4.1127 286.87 48.70 2.713 0.8364 0.5672 6048 0.6049

44021087- 4 4.1100 289.40 48.20 2.741 0.8323 0.5610 6017 0.6018

44021087- 5 4.1186 288.52 48.46 2.728 0.8380 0.5660 6058 0.6058

44021087- 6 3.7519 287.17 44.36 22.943 2.3033 1.5676 5993 0.6000

44021087- 7 3.7503 286.27 44.50 22.677 2.2952 1.5655 5998 0.6005

Table 23. Measured and calculated quantities for the beta ratio of 0.67 with two elbows in

plane at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 fim Ra Orifice Diameter 6.9840 cm (2.7496 in)

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

45021187- 1 3.9490 288.06 46.54 4.835 1.7365 1.1765 5021 0.6022

45021187- 2 3.9497 287.27 46.69 4.818 1.7337 1.1768 6012 0.6013

45021187- 3 3.7722 289.22 44.25 9.077 2.3136 1.5664 6003 0.6005

45021187- 4 3.7701 288.72 44.31 9.002 2.3094 1.5655 6013 0.6015

45021187- 5 4.0190 286.44 47.67 2.537 1.2765 0.8675 6039 0.6039

45021187- 6 4.0215 288.59 47.30 2.556 1.2755 0.8624 6034 0.6035

47
Table 24. Measured and calculated quantities for the beta ratio of 0.73 with two elbows in

plane at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 fxm Ra Orifice Diameter = 7.6177 cm (2.9991 in)

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

46021087- 1 3.9764 289.81

46021087- 2 3.9694 289.12

46021087- 3 3.7516 290.65

46021087- 4 3.7645 287.29

46021087- 5 3.9227 287.33

46021087- 6 3.9173 288.59

46021187- 1 3.9841 288.97

46021187- 2 3.9803 288.29

46021187- 3 3.9136 288.68

46021187- 4 3.8951 288.35

46021187- 5 3.7627 286.09

46021187- 6 3.7578 289.94

CY,

(kg/m-') (kPa) (kg/s) (-10°)

46 55 2 765 1 6452 1 1097 5988 0.5989

46 59 2 747 1 6421 1 1095 5995 0.5996

43 78 5 879 2 3122 1 5605 5951 0.5953

44 49 5 797 2 3178 1 5768 5960 0.5961

46 36 3 766 1 9133 1 2990 5980 0.5981

46 07 3 776 1 9091 1 2923 5978 0.5979

46 79 2 504 1 5742 1 0638 6006 0.6007

46 87 2 481 1 5667 1 0605 6000 0.6001

46 01 3 798 1 9141 1 2955 5980 0.5981

45 85 3 767 1 9036 1 2897 5982 0.5983

44 67 5 776 2 3161 1 5802 5955 0.5956

43 97 5 808 2 3041 1 5575 5954 0.5955

Table 25. Measured and calculated quantities for the beta ratio of 0.43 with two elbows in

plane upstream of the in-line tube bundle at 17 pipe diameters upstream of the

orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 /im Ra Orifice Diameter = 4.4445 cm (1.7498 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. c 0^2 (MPa) (K) (kg/m^) (kPa) (kg/s) (-10')

43081088- 1 4.0643 289.19 47.70 4.953 0.6542 0.4414 6030 0.6032

43081088- 2 4.0575 289.59 47.54 4.553 0.6265 0.4224 6033 0.6035

43081088- 3 3.8781 288.41 45.64 27.928 1.5149 1.0263 6003 0.6013

43081088- 4 3.8728 288.39 45.58 27.520 1.5021 1.0178 6001 0.6010

43081088- 5 3.7566 287.93 44.29 49.221 1.9764 1.3424 5982 0.5998

430,81088- 6 3.7658 287.82 44.41 48.795 1.9729 1.3403 5989 0.6005

43081088- 7 3.9682 288.61 46.67 13.236 1.0574 0.7152 6024 0.6029

43081088- 8 3.9615 288.62 46.59 13.451 1.0632 0.7192 6014 0.6018

43081188- 1 3.9179 288.42 46.11 13.177 1.0484 0.7099 6023 0.6027

43081188- 2 3.9221 288.34 46.17 13.316 1.0556 0.7149 6028 0.6032

43081188- 3 3.8326 287.57 45.25 27.826 1.5068 1.0234 6008 0.6017

43081188- 4 3.8302 287.56 45.22 27.684 1.4957 1.0160 5981 0.5990

43081188- 5 4.0144 289.21 47.11 5.034 0.6571 0.4436 6046 0.6047

43081188- 6 4.0068 289.26 47.01 5.006 0.6548 0.4421 6048 0.6050

43081188- 7 3.7162 287.22 43.93 47.211 1.9347 1.3171 6004 0.6020

43081188- 8 3.7172 287.24 43.94 46.765 1.9224 1.3085 5993 0.6010

48
Table 26. Measured and calculated quantities for the beta ratio of 0.55 with two elbows in

plane upstream of the in-line tube bundle at 17 pipe diameters upstream of the

orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 /jm Ra Orifice Diameter = 5.7137 cm (2.2495 in)

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

44080588- 1 3.9360 288.64 46.29 7.528 1.3561 0.9176 6036 0.6038

44080588- 2 3.9197 288.62 46.10 7.509 1.3489 0.9129 6023 0.6025

44080588- 3 3.8229 287.73 45.11 14.587 1.8550 1.2596 6005 0.6010

44080588- 4 3.8331 288.07 45.17 14.476 1.8470 1.2530 5998 0.6003

44080588- 5 4.0801 289.26 47.87 3.105 0.8899 0.6002 6066 0.6067

44080588- 6 4.0762 289.31 47.82 3.117 0.8919 0.6015 6072 0.6072

44080588- 7 3.6799 287.47 43.46 21.505 2.2143 1.5071 6013 0.6020

44080588- 8 3.6828 287.43 43.50 21.345 2.2041 1.5003 6005 0.6012

44081088- 1 3.8108 287.23 45.05 14.763 1.8614 1.2656 5994 0.5998

44081088- 2 3.8082 287.09 45.04 14.672 1.8546 1.2615 5991 0.5996

44081088- 3 4.0090 288.55 47.16 3.151 0.8873 0.6000 6048 0.6049

44081088- 4 3.9990 288.77 47.00 3.176 0.8912 0.6024 6061 0.6062

44081088- 5 3.9437 287.97 46.50 7.387 1.3448 0.9113 6028 0.6031

44081088- 6 3.9205 287.84 46.24 7.320 1.3358 0.9058 6032 0.6034

44081088- 7 3.6887 286.90 43.66 21.804 2.2257 1.5168 5988 0.5995

44081088- 8 3.6972 286.15 43.88 21.675 2.2252 1.5191 5989 0.5996

Table 27. Measured and calculated quantities for the beta ratio of 0.67 with two elbows in

plane upstream of the in-line tube bundle at 17 pipe diameters upstream of the

orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 urn Ra Orifice Diameter = 6.9840 cm (2.7496 in)

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

45080488- 1 3.6952 286 31 45080488- 2 3.7109 285 65 45080488- 3 3.8975 287 22 45080488- 4 3.8782 286 94

45080488- 5 3.8162 286 81

45080488- 6 3.8225 287 26

45080488- 7 3.9735 287 71 45080488- 8 3.9955 287 69

45081188- 1 3.7987 286 26

45081188- 2 3.7829 287 12 45081188- 3 3.6026 286 48

45081188- 4 3.6244 285 89 45081188- 5 3.7179 289 22 45081188- 6 3.7273 290 12 45081188- 7 3.8391 289 79 45081188- 8 3.8476 289 26

CY,

(kg/m") (kPa) (kg/s) (-10°)

43 83 8 849 2 2848 1 .5592 6034 0.6036

44 13 8 665 2 2627 1 5463 6018 0.6020

46 08 4 724 1 7116 1 1627 6035 0.6036

45 90 4 750 1 7090 1 1619 6020 0.6022

45 19 6 557 1 9989 1 3605 6040 0.6042

45 18 6 605 2 0079 1 3650 6045 0.6047

46 89 2 591 1 2840 8703 6059 0.6060

47 16 2 588 1 2884 8731 6067 0.6068

45 07 5 025 1 7461 1 1903 6035 0.6036

44 74 5 021 1 7361 1 1812 6025 0.6027

42 70 9 010 2 2655 1 5471 6007 0.6009

43 06 8 379 2 2011 1 5049 6027 0.6029

43 61 6 478 1 9461 1 3183 6022 0.6023

43 58 6 527 1 9525 1 3197 0. 6021 0.6023

44 94 2 957 1 3419 9065 0. 6055 0.6056

45 14 2 987 1 3484 9120 0. 6040 0.6041

49
Table 28. Measured and calculated quantities for the beta ratio of 0.73 with two elbows in

plane upstream of the in-line tube bundle at 17 pipe diameters upstream of the

orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 /im Ra Orifice Diameter = 7.6177 cm (2.9991 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. c CYz

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

46080488- 1 3.8567 288.08 45.45 3.692 1.8890 1.2811 0..6023 0.6024

46080488- 2 3.8671 287.89 45.60 3.715 1.8926 1.2839 0,.6006 0.6007

46080488- 3 3.8653 288.19 45.53 3.705 1.8917 1.2824 0..6015 0.6016

46080488- 4 3.8015 287.58 44.88 4.761 2.1233 1.4427 0,.5999 0.6000

46080488- 5 3.8094 287.58 44.97 4.788 2.1319 1.4484 0..6000 0.6001

46080488- 6 3.7308 287.52 44.05 5.569 2.2721 1.5453 0,.5991 0.5992

46080488- 7 3.7278 287.54 44.01 5.564 2.2688 1.5430 0,.5988 0.5989

46080488- 8 3.9166 288.09 46.15 2.701 1.6309 1.1052 0..6034 0.6034

46080488- 9 3.9087 288.03 46.07 2.723 1.6341 1.1077 0..6026 0.6027

46080588- 1 3.8357 287.94 45.22 3.625 1.8587 1.2613 0..5996 0.5997

46080588- 2 3.8378 288.22 45.20 3.624 1.8575 1.2596 0,.5994 0.5995

46080588- 3 3.6591 287.01 43.29 5.903 2.3203 1.5814 0..5995 0.5996

46080588- 4 3.6699 284.11 43.90 5.839 2.3213 1.5932 0..5989 0.5990

46080588- 5 3.9005 288.13 45.96 2.636 1.6054 1.0881 0,.6025 0.6026

46080588- 6 3.8956 288.03 45,92 2.637 1.6016 1.0858 0..6012 0.6012

46080588- 7 3.7808 287.50 44.65 4.596 2.0814 1.4148 0,.6001 0.6002

46080588- 8 3.7825 287.48 44.67 4.575 2.0782 1.4127 0,.6004 0.6005

Table 29. Measured and calculated quantities for the beta ratio of 0.43 and the 0.76 pm

upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 /im Ra Orifice Diameter = 4.4445 cm (1.7498 in)

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

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

43100588- 1 3.9279 288.25 46.26 26.697 1.5089 1.0221 0..6078 0.6086

43100588- 2 3.9026 287.88 46.02 29.580 1.5927 1.0801 0..6110 0.6120

43100588- 3 3.8980 287.96 45.96 29.674 1.5867 1.0759 0..6081 0.6091

43100588- 4 4.0854 289.08 47.97 5.401 0.6987 0.4715 0..6153 0.6155

43100588- 5 4.0738 289.18 47.81 5.510 0.7051 0.4757 0..6158 0.6160

43100588- 6 3.9908 288.54 46.95 13.193 1.0800 0.7305 0,.6148 0.6152

43100588- 7 3.9733 288.77 46.70 12.884 1.0644 0.7197 0..6147 0.6152

43100588- 8 3.7803 287.68 44.61 48.108 2.0013 1.3598 0..6108 0.6125

43100588- 9 3.7772 286.84 44.72 49.814 2.0394 1.3886 0,.6109 0.6126

43100688- 1 4.0994 289.13 48.12 5.107 0.6864 0.4630 0..6208 0.6210

43100688- 2 4.1055 289.12 48.20 5.450 0.7061 0.4762 0.,6176 0.6178

43100688- 3 3.9286 287.67 46.37 27.260 1.5501 1.0514 0.,6172 0.6181

43100688- 4 3.9102 287.67 46.15 26.839 1.5222 1.0327 0.,6122 0.6131

43100688- 5 3.8158 287.37 45.09 49.032 2.0400 1.3866 0.,6134 0.6151

43100588- 6 3.7966 287.03 44.92 48.752 2.0190 1.3737 0.,6099 0.6116

43100688- 7 3.9703 288.00 46.80 14.361 1.1277 0.7639 0.,6162 0.6167

43100688- 8 3.9600 288.22 46.64 14.628 1.1362 0.7694 0. 6162 0.6167

50
Table 30. Measured and calculated quantities for the beta ratio of 0.55 and the 0.76 /im upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 ^m Ra Orifice Diameter = 5.7137 cm (2.2495 in)

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

44093088- 1 3.7151 287.48 43.87 20.428 2.1925 1.4916 6081 0.6088

44093088- 2 3.7228 286.83 44.07 20.429 2.1920 1.4935 6066 0.6072

44093088- 3 3.8282 287.98 45.13 14.793 1.8842 1.2786 6057 0.6061

44093088- 4 3.8423 288.04 45.28 14.982 1.9004 1.2891 6060 0.5065

44093088- 5 4.0261 288.70 47.34 3.390 0.9260 0.6258 6075 0.5076

44093088- 6 4.0416 288.84 47.49 3.398 0.9370 0.6329 6131 0.5132

44093088- 7 4.0754 288.91 47.88 3.444 0.9397 0.6344 6082 0.5083

44093088- 8 3.9293 288.21 46.28 8.334 1.4442 0.9783 6111 0.5113

44093088- 9 3.9430 288.32 46.42 8.227 1.4370 0.9730 6110 0.5112

44100688- 1 3.9499 288.01 46.56 8.060 1.4242 0.9650 6109 0.6111

44100688- 2 3.9434 288.03 46.48 8.096 1.4191 0.9515 6078 0.6081

44100688- 3 3.8760 287.62 45.75 13.919 1.8422 1.2504 5064 0.6058

44100688- 4 3.8617 287.70 45.57 13.688 1.8334 1.2445 5098 0.6102

44100688- 5 3.7357 286.68 44.25 20.868 2.2299 1.5196 5093 0.6100

44100688- 6 3.7420 287.23 44.23 21.001 2.2286 1.5166 5072 0.6079

44100688- 7 4.0509 288.25 47.71 3.773 0.9851 0.5663 6103 0.5104

44100688- 8 4.0373 288.48 47.51 3.836 0.9945 0.6723 6123 0.6124

Table 31. Measured and calculated quantities for the beta ratio of 0.67 and the 0.76 /im upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.358 cm (4.082 in), 0.76 fim Ra Orifice Diameter = 6.9840 cm (2.7496 in)

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

45100588- 1 3.8289 287.35 45.24 6.233 1.9568 1.3299 6062 0.6063

45100588- 2 3.8158 287.82 45.02 6.243 1.9421 1.3186 6026 0.6028

45100588- 3 3.9237 287.94 46.26 3.971 1.5778 1.0695 6056 0.6057

45100588- 4 3.9154 287.98 46.16 3.994 1.5820 1.0724 6062 0.5053

45100588- 5 3.7385 287.32 44.18 8.449 2.2460 1.5282 6047 0.5049

45100588- 6 3.7225 287.06 44.03 8.391 2.2286 1.5176 5031 0.6033

45100588- 7 3.9755 288.13 45.86 2.797 1.3298 0.9004 6043 0.5044

45100588- 8 3.9458 288.13 45.49 2.807 1.3276 0.8993 6045 0.5047

45100588- 9 3.8334 287.85 45.21 6.304 1.9666 1.3349 6060 0.5052

45101188- 1 3.8473 287.55 45.43 5.868 1.9075 1.2954 6078 0.5079

45101188- 2 3.8249 287.59 45.15 5.764 1.8862 1.2812 6082 0.5084

45101188- 3 3.7143 287.27 43.90 8.562 2.2553 1.5358 6053 0.5055

45101188- 4 3.7206 287.27 43.97 8.545 2.2524 1.5331 6044 0.6046

45101188- 5 3.8786 287.79 45.76 4.721 1.7138 1.1628 5065 0.5057

45101188- 5 3.8663 287.83 45.50 4.748 1.7213 1.1580 6085 0.6087

45101188- 7 3.9319 287.92 45.35 2.912 1.3600 0.9219 5090 0.6091

45101188- 8 3.9372 288.15 46.38 2.940 1.3624 0.9229 0. 6070 0.6071

51
Table 32. Measured and calculated quan-tities for the beta ratio of 0.73 and the 0.76 ^m

upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 ftm Ra Orifice Diameter = 7.6177 cm (2.9991 in)

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

46092988- 1 3.8509 286.30 45.69 3.492 1.8392 1.2528 6015 0.6016

46092988- 2 3.8733 286.44 45.93 3.473 1.8392 1.2520 6016 0.6017

46092988- 3 3.7325 288.02 43.99 5.335 2.2266 1.5125 6004 0.6005

46092988- 4 3.7442 288.12 44.11 5.322 2.2285 1.5132 6008 0.6009

46092988- 5 3.9706 288.44 46.73 2.719 1.6381 1.1085 6004 0.6005

46092988- 6 3.9396 288.85 46.29 2.737 1.6422 1.1106 6027 0.6028

46092988- 7 3.9590 288.88 46.51 2.742 1.6487 1.1146 6030 0.6031

46092988- 8 3.8433 288.08 45.29 3.913 1.9377 1.3143 6013 0.6014

46092988- 9 3.8555 287.70 45.50 3.891 1.9286 1.3092 5988 0.5989

46092988- 10 3.8447 288.53 45.22 3.868 1.9197 1.3007 5995 0.5996

46101188- 1 3.7072 286.95 43.87 5.418 2.2368 1.5239 5994 0.5995

46101188- 2 3.7199 287.34 43.95 5.432 2.2388 1.5235 5985 0.5986

46101188- 3 3.8890 287.69 45.90 2.693 1.6166 1.0969 6007 0.6007

46101188- 4 3.8716 287.63 45.70 2.707 1.6169 1.0976 6005 0.6006

46101188- 5 3.7695 287.45 44.52 4.632 2.0857 1.4181 5999 0.6000

46101188- 6 3.7681 287.12 44.56 4.647 2.0832 1.4176 5980 0.5981

46101188- 7 3.8436 287.51 45.39 3.396 1.8032 1.2248 5999 0.6000

46101188- 8 3.8359 287.56 45.29 3.352 1.7936 1.2183 6014 0.6015

Table 33. Measured and calculated quantities for the beta ratio of 0.43 and the 0.76 /xm upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 ^m Ra Orifice Diameter = 4.4445 cm (1.7498 in)

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe Re No. c 0^2 (MPa) (K) (kg/m^) (kPa) (kg/s) (-10^)

43100488- 1 3.8024 287.17 44.96 46.401 1.9375 1.3177 5995 0.6011

43100488- 2 3.8088 287.37 45.00 45.974 1.9291 1.3113 5994 0.6010

43100488- 3 4.1297 289.02 48.50 5.218 0.6778 0.4572 6037 0.6039

43100488- 4 4.0922 289.22 48.02 5.356 0.6838 0.4612 6040 0.6042

43100488- 5 3.9206 288.11 46.20 27.642 1.5236 1.0324 6033 0.6042

43100488- 6 3.9044 287.70 46.08 28.390 1.5365 1.0424 6010 0.6020

43100488- 7 3.9743 288.34 46.79 13.626 1.0749 0.7275 6028 0.6032

43100488- 8 3.9671 288.50 46.68 13.532 1.0689 0.7232 6022 0.6027

43101288- 1 3.9094 288.63 45.97 13.727 1.0685 0.7233 6023 0.6027

43101288- 2 3.8934 288.56 45.80 13.507 1.0574 0.7160 6020 0.6024

43101288- 3 3.9934 289.28 46.85 5.427 0.6808 0.4596 6049 0.6051

43101288- 4 3.9990 289.44 46.88 5.672 0.6961 0.4697 6048 0.6049

43101288- 5 3.8401 288.04 45.26 28.652 1.5345 1.0410 6029 0.6038

43101288- 6 3.8262 287.83 45.13 28.212 1.5183 1.0306 6020 0.6030

43101288- 7 3.7318 287.59 44.05 49.558 1.9893 1.3527 6016 0.6033

43101288- 8 3.7348 287.61 44.08 49.225 1.9809 1.3469 6009 0.6026

52
Table 34. Measured and calculated quantities for the beta ratio of 0.55 and the 0.76 fim upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 nm Ra Orifice Diameter = 5.7137 cm (2.2495 in)

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

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

44100388- 1 3.9846 288.50 46.88 7.156 1 3294 0.8993 0.6029 0.6032

44100388- 2 4.0186 288.20 47.34 7.187 1 3384 0.9057 0.6028 0.6030

44100388- 3 4.0927 288.84 48.10 3.221 9027 0.6094 0.6027 0.6028

44100388- 4 4.0731 288.95 47.85 3.120 8892 0.6003 0.6047 0.6048

44100388- 5 3.8836 287.75 45.82 14.440 1 8630 1.2641 0.6014 0.6019

44100388- 6 3.8822 287.76 45.80 14.345 1 8528 1.2571 0.6002 0.6007

44100388- 7 3.7434 287.21 44.25 21.129 2 2150 1.5074 0.6013 0.6020

44100388- 8 3.7561 287.63 44.33 21.076 2 2105 1.5026 0.6003 0.6010

44101288- 1 3.6847 287.49 43.51 21.869 2 2226 1.5126 0.5981 0.5988

44101288- 2 3.6931 286.54 43.77 21.598 2 2281 1.5197 0.6016 0.6023

44101288- 3 3.8718 288.28 45.59 7.739 1 3604 0,9220 0.6016 0.6019

44101288- 4 3.8585 288.25 45.44 7.735 1 3549 0.9185 0.6004 0.6006

44101288- 5 3.7575 287.83 44.32 14.797 1 8457 1.2539 0.5985 0.5990

44101288- 6 3.7683 287.96 44.42 14.760 1 8502 1.2565 0.6000 0.6005

44101288- 7 3.9532 288.82 46.46 3.638 9409 0.6362 0.6013 0.6015

44101288- 8 3.9550 288.97 46.45 3.728 9547 0.6453 0.6028 0.6029

Table 35. Measured and calculated quantities for the beta ratio of 0.67 and the 0.76 ^m

upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 ^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/m^) (kPa) (kg/s) (-10^

45100488- 1 3.9629 288.59 46.61 2.685 1.2979 0.8780 6035 0.6036

45100488- 2 3.9686 288.51 46.69 2.695 1.3022 0.8810 6039 0.6040

45100488- 3 3.9387 288.23 46.39 4.152 1.6048 1.0869 6015 0.6016

45100488- 4 3.9308 288.26 46.29 4.116 1.5980 1.0823 6021 0.6022

45100488- 5 3.7341 287.52 44.09 8.725 2.2603 1.5372 5993 0.5996

45100488- 6 3.7350 287.48 44.11 8.734 2.2585 1.5361 5984 0.5987

45100488- 7 3.8491 287.48 45.46 6.306 1.9581 1.3300 6015 0.6017

45100488- 8 3.8499 287.46 45.47 6.304 1.9562 1.3288 6009 0.6011

45101188- 1 3.8548 287.83 45.47 6.048 1.9219 1.3043 6028 0.6030

45101188- 2 3.8349 287.59 45.27 5.957 1.9015 1.2914 6022 0.6024

45101188- 3 3.8987 287.97 45.96 4.443 1.6612 1.1263 6047 0.6048

45101188- 4 3.9006 287.91 46.00 4.472 1.6641 1.1284 6035 0.6036

45101188- 5 3.9457 287.94 46.52 2.893 1.3492 0.9144 6050 0.6051

45101188- 6 3.9389 287.99 46.43 2.904 1.3487 0.9140 6042 0.6043

45101188- 7 3.7345 286.61 44.25 8.548 2.2489 1.5328 6014 0.6016

45101188- 8 3.7390 287.02 44.23 8.531 2.2470 1.5299 6016 0.6018

53
Table 36. Measured and calculated quantities for the beta ratio of 0.73 and the 0.76 /in upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

Pipe Diameter = 10.368 cm (4.082 in), 0.76 nm Ra Orifice Diameter = 7.6177 cm (2.9991 in)

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

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

46092988- 1 3.8250 289.08 44,,90 4.355 2,.0245 1.3702 0.5979 0.5980

46092988- 2 3.8346 289.00 45.,03 4.357 2..0265 1.3716 0.5975 0.5976

46092988- 3 3.6653 287.42 43,,29 6.080 2,.3472 1.5980 0.5975 0.5977

46092988- 4 3.7420 282.53 45,,05 5.216 2,.2141 1.5242 0.5966 0.5968

46092988- 5 3.8651 286.09 45,,90 3.664 1,.8807 1.2815 0.5990 0.5991

46092988- 6 3.8500 286.02 45,,73 3.698 1..8888 1.2874 0.5999 0.6000

46092988- 7 3.9441 286.71 46,,73 2.522 1,.5765 1.0716 0.5999 0.6000

46092988- 8 3.9013 286.47 46,,26 2.524 1..5679 1.0669 0.5993 0.5994

46100388- 1 3.9411 288.34 46,,40 2.558 1..5892 1.0760 0.6025 0.6026

46100388- 2 3.9710 288.43 46,,73 2.558 1,.5934 1.0782 0.6019 0.6020

46100388- 3 3.8312 287.38 45,,27 4.335 2,.0380 1.3849 0.6009 0.6010

46100388- 4 3.8322 287.86 45,,19 4.292 2..0236 1.3735 0.6001 0.6002

46100388- 5 3.7233 286.58 44,,12 5.832 2,.3267 1.5862 0.5991 0.5992

46100388- 6 3.7243 286.74 44,,11 5.773 2,.3126 1.5760 0.5985 0.5987

46100388- 7 3.8549 288.10 45,,42 3.874 1,.9214 1.3031 0.5983 0.5984

46100388- 8 3.8420 287.81 45,,32 3.910 1..9293 1.3095 0.5986 0.5987

Table 37. Measured and calculated quantities for the beta ratio of 0.43 and the 3.8 nm

upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

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 CYz

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

43091389- 1 3.7488 286.49 44.44 48.485 2.0213 1.3782 0..6158 0.6175

43091389- 2 3.7474 286.50 44.42 48.513 2.0191 1.3767 0..6151 0.6168

43091389- 3 4.1024 287.62 48.44 5.198 0.6942 0.4700 0,,6204 0.6205

43091389- 4 4.1238 287.76 48.67 4.973 0.6885 0.4659 0,,6275 0.6277

43091389- 5 3.9223 286.68 46.47 27.165 1.5593 1.0605 0..6215 0.6224

43091389- 6 3.9238 286.83 46.46 26.758 1.5420 1.0483 0,,6194 0.6203

43091389- 7 3.9894 287.22 47.17 15.005 1.1683 0.7929 0,,6224 0.6229

43091389- 8 3.9860 287.10 47.15 15.085 1.1716 0.7954 0,,6225 0.6230

43091389- 9 4.1303 287.97 48.70 5.109 0.6942 0.4695 0,.6241 0.6243

Table 38. Measured and calculated quantities for the beta ratio of 0.55 and the 3.8 ;xm upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

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 CYz (MPa) (K) (kg/m') (kPa) (kg/s) (-10')

44091389- 1 3.9463 287.12 46.68 7.076 1.3470 0.9149 0,.6158 0.6161

44091389- 2 3.9472 287.43 46.63 7.071 1.3408 0.9100 0,.6135 0.6137

44091389- 3 3.8476 286.84 45.55 13.389 1.8124 1.2333 0,,6094 0.6099

44091389- 4 3.8444 287.03 45.48 13.169 1.8065 1.2287 0,,6130 0.6134

44091389- 5 3.6688 285.98 43.57 21.697 2.2677 1.5496 0.,6122 0.6129

44091389- 6 3.6684 285.92 43.58 21.613 2.2662 1.5489 0.,6130 0.6137

44091389- 7 4.0559 287.41 47.93 3.013 0.8932 0.6054 0,,6177 0.6178

44091389- 8 4.0596 287.38 47.97 3.099 0.9071 0.6149 0.,6182 0.6183

54
Table 39. Measured and calculated quantities for the beta ratio of 0.67 and the 3.8 /xm upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.365 cm (4.081 in), 3.8 pm Ra Orifice Diameter = 6.9840 cm (2.7496 in)

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

45091289- 1 3.8879 286..62 45091289- 2 3.8840 286..72 45091289- 3 3.8042 286.,16

45091289- 4 3.8020 285.,99

45091289- 5 3.6507 285.,70

45091289- 6 3.5807 285.,77

45091289- 7 3.9308 285.,83

45091289- 8 3.9361 286.,69

CY,

(kg/m") (kPa) (kg/s) (-10°)

46.,07 4,,330 1.6510 1.1235 0,,6081 0.6082

46.,01 4,,262 1.6363 1.1133 0.,5079 0.6080

45.,15 6,,202 1.9611 1.3374 0.,5095 0.6097

45.,16 6,,204 1.9583 1.3360 0.,5085 0.6087

43.,52 8.,751 2.2780 1.5579 0.,5067 0.6070

43.,75 8.,399 2.2402 1.5314 0.,5078 0.6081

46.,55 2.,691 1.3116 0.8916 0.,5097 0.6098

46.,63 2.,734 1.3331 0.9065 0.,5142 0.6143

Table 40. Measured and calculated quantities for the beta ratio of 0.73 and the 3.8 /xm upstream pipe with a tee at 19 pipe diameters upstream of the orifice plate.

Pipe Diameter = 10.365 cm (4.081 in), 3.8 /jm Ra Orifice Diameter = 7.6197 cm (2.9999 in)

Run ID Pressure Temperat

(MPa) (K)

46091289- 1 3.8813 286.29

45091289- 2 3.8793 286.65

46091289- 3 3.7645 285.87

46091289- 4 3.7665 285.58

46091289- 5 3.6634 286.04

46091289- 6 3.6649 284.86

46091289- 7 3.8255 285.05

46091289- 8 3.8222 285.08

CY,

(kg/m') (kPa) (kg/s) (-10°)

45,,05 2.,651 1..6277 1.1085 0,.6068 0.6069

45..96 2,,587 1..6234 1.1047 0.,6028 0.6029

44..73 4,,244 2,.0231 1.3813 0,,5059 0.6060

44,.54 4.,324 2,.0177 1.3752 0.,5994 0.5995

43,.50 5,,480 2,,2508 1.5380 0.,5015 0.6017

43,,72 5.,442 2..2431 1.5372 0.,6002 0.6004

45.,43 3.,364 1.,7967 1.2253 0.,5999 0.6000

45.,39 3.,375 1,,7987 1.2265 0.,5998 0.5999

Table 41. Measured and calculated quantities for the beta ratio of 0.43 and the 3.8 /im upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

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

43101789- 1 3.9388 287.12 45.59 15.607 1.1464 0.7787 0,.6021 0.5027

43101789- 2 3.9254 287.36 45.39 15.602 1.1427 0.7759 0..6016 0.6021

43101789- 3 3.8559 287.07 45.75 28.278 1.5319 1.0416 0.,5028 0.6038

43101789- 4 3.8636 286.86 45.74 28.013 1.5227 1.0359 0.,6021 0.6030

43101789- 5 4.0759 287.92 48.08 5.158 0.6589 0.4527 0.,6020 0.6021

43101789- 5 4.0787 287.98 48.09 5.546 0.5969 0.4715 0.,6048 0.6050

43101789- 7 3.7534 286.32 44.52 46.197 1.9308 1.3170 0.,6019 0.6035

43101789- 8 3.7506 285.78 44.58 45.644 1.9189 1.3105 0.,5014 0.6030

55
Table 42. Measured and calculated quantities for the beta ratio of 0.55 and the 3.8 /im upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

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

Run ID

Orifice Diameter = 5.7142 cm (2.2497 in)

Pressure Temperature Density Dif Press Flow Rate Pipe Re No C CY,

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

44101789- 1 4..0423 287.61 47,,73 2,.839 0.8491 0,.5754 0,.6060 0,.6061

44101789- 2 4..0610 287.77 47,,92 2,.878 0.8576 0,.5808 0,,6067 0,.6068

44101789- 3 3..6704 285.56 43,.66 21,.415 2.2241 1,.5214 0,,6037 0,.6044

44101789- 4 3..6712 286.07 43,.59 21..327 2.2161 1,.5140 0,,6032 0,.6039 44101789- 5 3,.8043 286.76 45,,06 14,.151 1.8350 1,.2496 0,.6034 0,.6038

44101789- 6 3..8045 286.21 45,.15 14,.241 1.8422 1,.2561 0,.6032 0,.6036

44101789- 8 3..9105 286.72 46,.32 8,.026 1.4023 0,.9538 0,.6040 0,.6043

44101789- 9 3,.9107 286.90 46,.29 8..044 1.4047 0,.9550 0,,6046 0,,6048

Table 43. Measured and calculated quantities for the beta ratio of 0.67 and the 3.8 /xm upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

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 cYz (MPa) (K) (kg/m^ (kPa) (kg/s) (-MO^)

45090789- 1 3.8565 287.47 45.55 3.990 1.5660 1.0639 0,,6042 0.6043

45090789- 2 3.8613 287.28 45.64 3.964 1.5618 1.0615 0,,6039 0.6040

45090789- 3 3.6233 285.81 43.06 8.907 2.2600 1.5459 0,.6001 0.6004

45090789- 4 3.6317 286.25 43.08 8.887 2.2552 1.5407 0,,5993 0.5996

45090789- 5 3.7656 286.99 44.55 6.247 1.9319 1.3154 0,,6022 0.6024

45090789- 6 3.7707 287.22 44.58 6.329 1.9445 1.3232 0,,6021 0.6022

45090789- 7 3.9221 287.56 46.31 2.580 1.2732 0.8641 0,.6059 0.6059

450,90789- 8 3.9244 287.50 46.35 2.611 1.2777 0.8673 0,.6042 0.6042

45090889- 1 3.6742 286.67 43.52 8.781 2.2622 1.5432 0,,6017 0.6020

45090889- 2 3.6829 285.56 43.81 8.726 2.2606 1.5462 0,,6013 0.6015

45090889- 3 3.8907 287.09 46.02 4.259 1.6245 1.1042 0,,6035 0.6036

45090889- 4 3.8898 287.02 46.03 4.344 1.6414 1.1159 0,,6038 0.6039

45090889- 5 3.8260 286.92 45.28 5.991 1.9119 1.3011 0,,6037 0.6038

45090889- 6 3.8273 286.88 45.31 5.976 1.9114 1.3008 0..6041 0.6043

45090889- 7 3.9535 287.09 46.77 2.596 1.2839 0.8720 0..6061 0.6062

45090889- 8 3.9550 287.52 46.71 2.625 1.2866 0.8729 0..6044 0.6045

56
Table 44. Measured and calculated quantities for the beta ratio of 0.73 and the 3 . 8 ;iin upstream pipe with a tee upstream of the in-line tube bundle at 17 pipe diameters

upstream of the orifice plate.

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

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

46090789- 1 3.6572 286.58 43.33 5.561 2.2604 1.5426 0.,6008 0.6009

46090789- 2 3.6575 284.98 43.61 5.519 2.2560 1.5456 0,,6001 0.6002

46090789- 3 3.8134 286.63 45.18 3.404 1.8085 1.2317 0.,6017 0.6018

46090789- 4 3.8139 286.63 45.19 3.494 1.8286 1.2455 0.,6005 0.6006

46090789- 5 3.7594 286.82 44.51 4.294 2.0174 1.3743 0,,6022 0.6023

46090789- 6 3.7576 286.49 44.54 4.281 2.0105 1.3707 0.,6008 0.6009

46090789- 7 3.8672 287.12 45.74 2.644 1.6075 1.0929 0.,6032 0.6032

46090789- 8 3.8688 287.12 45.76 2.695 1.6215 1.1024 0.,6026 0.6027

46090889- 1 3.8871 286.95 46.01 3.174 1.7645 1.1998 0.,6026 0.6026

46090889- 2 3.8789 287.01 45.90 3.321 1.7954 1.2207 0.,6001 0.6001

46090889- 3 3.6821 286.59 43.63 5.592 2.2599 1.5418 0.,5970 0.5971

46090889- 4 3.6904 286.63 43.72 5.572 2.2613 1.5424 0.,5978 0.5979

46090889- 5 3.7733 286.48 44.73 4.408 2.0358 1.3877 0.,5982 0.5983

46090889- 6 3.7691 286.94 44.60 4.457 2.0494 1.3955 0.,5997 0.5998

46090889- 7 3.8957 287.25 46.05 2.655 1.6120 1.0952 0,,6016 0.6016

46090889- 8 3.8951 287.12 46.07 2.676 1.6189 1.1002 0.,6017 0.6017

Table 45. Measured and calculated quantities for the beta ratio of 0.43 with two elbows outof-plane at 19 pipe diameters upstream of the orifice plate.

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 CYz

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

41,110189- 1 3.9490 287.81 46.59 14.982 1.1306 0.7666 0..6062 0.6067

43110189- 2 3.9498 287.99 46.56 15.000 1.1288 0.7651 0.,6050 0.6055

43110189- 3 3.8836 287.57 45.85 28.639 1.5466 1.0501 0,,6040 0.6050

43110189- 4 3.8871 287.39 45.93 28.506 1.5471 1.0509 0,,6052 0.6061

43110189- 5 4.0530 288.44 47.70 5.796 0.7126 0.4819 0,,6074 0.6076

43110189- 6 4.0554 288.47 47.73 5.468 0.6940 0.4692 0,,6089 0.6090

43110189- 7 3.7643 287.05 44.53 49.293 2.0015 1.3626 0.,6039 0.6056

43110189- 8 3.7701 286.69 44.66 48.683 1.9886 1.3549 0.,6029 0.6046

43110889- 1 3.9798 288.44 46.84 5.092 0.6607 0.4471 0,.6064 0.6066

43110889- 2 3.9879 288.58 46.91 5.441 0.6864 0.4643 0,.6089 0.6091

43110889- 3 3.6999 287.32 43.72 48.049 1.9574 1.3328 0..6038 0.6054

43110889- 4 3.7102 286.88 43.91 47.353 1.9435 1.3245 0.,6025 0.6042

43110889- 5 3.8784 287.75 45.76 16.207 1.1626 0.7891 0.,6046 0.6052

43110889- 6 3.8826 287.94 45.78 16.420 1.1718 0.7949 0.,6053 0.6059

43110889- 7 3.8260 287.36 45.21 28.996 1.5486 1.0527 0.,6053 0.6063

43110889- 8 3.8223 287.12 45.21 29.205 1.5524 1.0560 0.,6047 0.6057

57
Table 46. Measured and calculated quantities for the beta ratio of 0.55 with two elbows outof-plane at 19 pipe diameters upstream of the orifice plate.

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

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

(MPa) (K)

44103189- 1 3.7401 287..36 44103189- 2 3.7437 286,.75 44103189- 3 4.0953 288..13 44103189- 4 4.0933 288..23 44103189- 5 3.9782 287..66 44103189- 6 3.9742 287,.66 44103189- 7 3.8812 287,,60

44103189- 8 3.8842 287,,31

44110889- 1 3.7571 287,.78 44110889- 2 3.7576 287,.39 44110889- 3 3.8520 287,.88 44110889- 4 3.8515 287,.91 44110889- 5 3.9626 288,.41 44110889- 6 3.9637 288,.45 44110889- 7 3.6313 287,.18 44110889- 8 3.6152 286,.96

CY,

kg,'ra^) (kPa) (kg/s) (-10^)

^

44,.19 21.489 2.2564 1.5354 0,.6077 0,.6084

44,.33 21.323 2.2524 1.5349 0,.6080 0,.6087

48,.26 2.442 0.7984 0.5400 0,,6110 0,.6111

48,.22 2.467 0.8022 0.5425 0,,6112 0,.6113

46,.96 7.009 1.3327 0.9037 0,.6101 0,.6103

46,.91 6.961 1.3259 0.8991 0,.6095 0,.6097

45,.82 13.389 1.8132 1.2310 0,.6078 0,.6082

45,.91 13.284 1.8127 1.2316 0,.6095 0,.6099

44..32 14.115 1.8277 1.2422 0,.6067 0,.6072

44,.39 14.089 1.8276 1.2433 0,.6067 0,.6072

45,.43 7.472 1.3477 0.9147 0,.6075 0,.6078

45,.42 7.484 1.3500 0.9162 0,.6082 0,,6084

46,.64 2.726 0.8277 0.5603 0,.6099 0,,6100

46,.65 2.755 0.8323 0.5634 0,.6099 0,.6100

42,.93 21.271 2.2067 1.5042 0,.6060 0,.6067

42,.77 22.221 2.2525 1.5365 0,.6063 0,.6071

Table 47. Measured and calculated quantities for the beta ratio of 0.67 with two elbows outof-plane at 19 pipe diameters upstream of the orifice plate.

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 CYz

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

45103189- 2 3.8506 287.57 45.46 6.198 1.9532 1.3267 0,.6051 0.6053

45103189- 3 3.7344 287.16 44.15 8.548 2.2613 1.5396 0,.6052 0.6055

45103189- 4 3.7377 287.38 44.16 8.534 2.2602 1.5379 0..6054 0.6057

45103189- 5 3.9336 287.41 46.48 4.012 1.5891 1.0787 0,.6053 0.6054

45103189- 6 3.9383 287.53 46.51 4.064 1.6025 1.0874 0,.6063 0.6064

45103189- 7 3.9857 287.58 47.06 2.738 1.3303 0.9021 0,.6096 0.6097

45103189- 8 3.9839 287.47 47.06 2.742 1.3250 0.8988 0,.6067 0.6068

45103189- 9 3.9838 287.57 47.04 2.735 1.3227 0.8970 0,.6065 0.6066

45110789- 1 3.9470 287.57 46.60 2.666 1.2978 0.8805 0..6057 0.6058

45110789- 2 3.9481 287.85 46.57 2.650 1.2945 0.8776 0,.6061 0.6062

45110789- 3 3.9053 287.44 46.13 4.190 1.6137 1.0957 0,.6037 0.6038

45110789- 4 3.9062 287.19 46.19 4.170 1.6126 1.0956 0,.6044 0.6045

45110789- 5 3.7066 286.54 43.93 8.639 2.2631 1.5437 0,.6041 0.6044

45110789- 6 3.7079 286.62 43.93 8.613 2.2532 1.5366 0,.6024 0.6026

45110789- 7 3.8287 287.39 45.23 6.045 1.9180 1.3037 0,,6032 0.6034

45110789- 8 3.8258 287.23 45.23 6.080 1.9245 1.3087 0..6036 0.6037

58
Table 48. Measured and calculated quantities for the beta ratio of 0.73 with two elbows out- of-plane at 19 pipe diameters upstream of the orifice plate.

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

46110189- 2 3.7977 287.08 44.92 4.320 2.0158 1.3717 5971 0.5972

46110189- 3 3.8031 287.07 44.99 4.329 2.0159 1.3717 5961 0.5962

46110189- 4 3.7250 287.28 44.02 5.448 2.2438 1.5274 5978 0.5979

46110189- 5 3.7064 287.38 43.79 5.423 2.2252 1.5148 5958 0.5960

46110189- 6 3.8931 287.41 46.00 2.644 1.6019 1.0879 5995 0.5995

46110189- 7 3.8935 287.58 45.97 2.684 1.6116 1.0941 5987 0.5988

46110189- 8 3.8613 287.40 45.62 3.222 1.7540 1.1917 5970 0.5971

46110189- 9 3.8605 287.50 45.59 3.218 1.7537 1.1912 5975 0.5975

46110789- 1 3.8671 287.31 45.71 3.323 1.7854 1.2133 5978 0.5979

46110789- 2 3.8669 287.46 45.68 3.328 1.7840 1.2118 5971 0.5972

46110789- 3 3.9077 287.47 46.16 2.606 1.5943 1.0824 5999 0.6000

46110789- 4 3.9082 287.53 46.15 2.604 1.5892 1.0788 5983 0.5983

46110789- 5 3.6990 287.26 43.72 5.719 2.2853 1.5562 5964 0.5965

46110789- 6 3.6992 287.18 43.73 5.696 2.2834 1.5553 5969 0.5971

46110789- 7 3.7905 287.31 44.80 4.464 2.0468 1.3922 5973 0.5974

46110789- 8 3.7925 286.87 44.89 4.477 2.0526 1.3976 5975 0.5976

Table 49. Measured and calculated quantities for the beta ratio of 0.43 with two elbows outof-plane and the in-line tube bundle at 17 pipe diameters upstream of the orifice

plate.

Pipe Diameter = 10.366 cm (4.081 in), 3.8 /zm 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')

43110289- 1 3.7763 286.88 44.70 49.001 1.9787 1.3475 .5977 0.5993

43110289- 2 3.7839 287.13 44.75 48.863 1.9789 1.3467 5982 0.5999

43110289- 3 3.9573 287.58 46.73 16.504 1.1804 0.8007 6020 0.6025

43110289- 4 3.9688 287.78 46.83 15.409 1.1412 0.7737 6017 0.6022

43110289- 5 3.9197 287.48 46.30 27.937 1.5297 1.0384 6020 0.6029

43110289- 6 3.9134 287.35 46.25 29.827 1.5764 1.0705 6007 0.6017

43110289- 7 3.7978 287.28 44.89 48.903 1.9872 1.3516 5996 0.6012

43110289- 8 3.8013 286.79 45.01 48.586 1.9794 1.3478 5983 0.6000

43110289- 9 4.0947 288.30 48.22 6.260 0.7416 0.5014 6049 0.6051

43110289- 10 4.0927 288.43 48.17 6.176 0.7378 0.4987 6062 0.6064

43110989- 1 3.8604 287.78 45.54 28.526 1.5285 1.0375 6002 0.6011

43110989- 2 3.8622 287.90 45.54 28.435 1.5264 1.0358 6003 0.6013

43110989- 3 3.9277 288.13 46.28 13.987 1.0811 0.7326 6019 0.6023

43110989- 4 3.9307 288.02 46.33 13.891 1.0793 0.7316 6026 0.6031

43110989- 5 3.7539 287.31 44.36 46.761 1.9285 1.3123 5986 0.6002

43110989- 6 3.7417 287.52 44.18 49.075 1.9747 1.3432 5994 0.6011

43110989- 7 4.0238 288.53 47.34 5.913 0.7128 0.4821 6038 0.6040

43110989- 8 4.0216 288.66 47.29 5.817 0.7056 0.4770 6029 0.6031

43030890- 1 3.9133 287.82 46.16 15.431 1.1340 0.7692 6018 0.6023

43030890- 2 3.9451 288.06 46.50 15.274 1.1320 0.7671 6016 0.6021

43030890- 3 3.8148 287.59 45.04 29.851 1.5564 1.0576 0. 6007 0.6017

43030890- 4 3.8207 287.52 45.12 29.764 1.5539 1.0560 0. 6001 0.6011

43030890- 5 4.0598 288.67 47.74 5.199 0.6732 0.4549 0. 6055 0.6057

43030890- 6 4.0704 288.86 47.83 4.872 0.6519 0,4403 0. 6053 0.6054

43030890- 7 3.6912 287.32 43.62 48.076 1.9461 1.3252 0. 6008 0.6024

43030890- 8 3.6920 287.18 43.65 47.327 1.9275 1.3129 0. 5995 0.6011

59
Table 50. Measured and calculated quantities for the beta ratio of 0.55 with two elbows out- of-plane and the in-line tube bundle at 17 pipe diameters upstream of the orifice

plate.

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

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

44110389- 1 3,.8921 287..31 44110389- 2 3,.8908 287..32 44110389- 3 3,.9769 287,.91 44110389- 4 3,.9770 287..75 44110389- 5 4,.0796 288..32 44110389- 6 4,.0829 288,.31 44110389- 7 3,.7410 286,.37 44110389- 8 3,.7430 286,.43 44110989- 1 3..9097 288,.02 44110989- 2 3,.9126 287,.98 44110989- 3 4..0170 288,.37 44110989- 4 4,.0172 288,.42 44110989- 5 3,.6796 286,.74 44110989- 6 3,.6834 287,.14 44110989- 8 3..8123 287,.05 44110989- 9 3..8296 287,.53

CY,

kg;^m^) (kPa) (kg/s) (-10')

46,.00 13.189 1.7879 1.2146 0,,6027 0,.6031

45,.98 13.164 1.7889 1.2152 0,.6037 0,.6041

46,.90 7.346 1.3505 0.9152 0.,6043 0,.6045

46,.93 7.317 1.3492 0.9147 0..6048 0,.6050

48,.04 2.833 0.8534 0.5770 0,.6078 0,.6079

48,.08 2.854 0.8565 0.5791 0.,6074 0,.6075

44,.37 21.020 2.2142 1.5104 0..6018 0,.6024

44,.38 20.829 2.2110 1.5079 0..6036 0,.6042

46,.09 7.226 1.3301 0.9019 0,.6054 0,.6056

46,.13 7.083 1.3198 0.8949 0..6064 0,.6066

47,.29 2.794 0.8419 0.5696 0,,6086 0,.6086

47,.28 2.717 0.8316 0.5625 0,,6096 0,.6096

43,.57 21.468 2.2253 1.5176 0..6038 0,.6045

43,.55 21.344 2.2165 1.5101 0,.6033 0,.6040

45,.10 14.124 1.8393 1.2515 0..6051 0,.6055

45,.22 12.749 1.7474 1.1873 0,.6043 0,.6047

Table 51. Measured and calculated quantities for the beta ratio of 0.67 with two elbows out- of-plane and the in-line tube bundle at 17 pipe diameters upstream of the orifice

plate .

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

45110389- 1 3.9838 287.89 46.98 2.689 1.3098 0.8876 0,.6061 0.6062

45110389- 2 3.9865 287.50 47.09 2.680 1.3094 0.8881 0,.6063 0.6063

45110389- 3 3.9350 287.49 46.48 4.273 1.6428 1.1149 0,.6063 0.6064

45110389- 4 3.9356 287.36 46.51 4.261 1.6410 1.1141 0,.6063 0.6064

45110389- 5 3.7344 286.46 44.27 8.596 2.2657 1.5452 0,.6040 0.6042

45110389- 6 3.7356 286.18 44.34 8.540 2.2570 1.5404 0,,6032 0.6034

45110389- 7 3.8631 287.02 45.71 5.950 1.9182 1.3044 0,,6049 0.6051

45110389- 8 3.8559 286.90 45.64 5.946 1.9163 1.3036 0,,6049 0.6051

45110389- 9 3.9267 287.29 46.41 4.246 1.6350 1.1103 0,.6058 0.6059

45112189- 1 3.8843 287.48 45.88 4.019 1.5861 1.0772 0,.6075 0.6076

45112189- 2 3.8822 287.82 45.79 4.024 1.5812 1.0729 0,,6058 0.6059

45112189- 3 3.6701 287.23 43.38 8.863 2.2748 1.5498 0,.6033 0.6035

45112189- 4 3.6724 287.27 43.40 8.809 2.2663 1.5437 0..6027 0.6029

45112189- 5 3.7969 287.34 44.86 5.962 1.8996 1.2918 0..6041 0.6042

45112189- 6 3.7976 287.53 44.84 5.997 1.9014 1.2925 0.,6030 0.6032

45112189- 7 3.9212 287.98 46.23 2.272 1.1960 0.8109 0..6071 0.6071

45112189- 8 3.9141 288.02 46.14 2.626 1.2841 0.8706 0.,6068 0.6069

60
Table 52. Measured and calculated quantities for the beta ratio of 0.73 with two elbows out- of-plaue and the in-line tube bundle at 17 pipe diameters upstream of the orifice

plate.

Pipe Diameter = 10.356 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 CYz

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

46110689- 1 3.8702 287.00 45.80 4.082 1.9889 1.3525 0..6002 0.6003

46110689- 2 3.8685 286.83 45.80 4.063 1.9836 1.3494 0,,6000 0.6001

46110689- 3 3.9608 287.22 46.83 2.585 1.6042 1.0892 0,,6017 0.6017

46110689- 4 3.9603 287.38 46.80 2.597 1.6061 1.0900 0,,6013 0.6013

46110689- 5 3.7512 287.00 44.38 5.507 2.2758 1.5498 0,,6007 0.6008

46110689- 6 3.7488 286.93 44.36 5.515 2.2734 1.5485 0.,5997 0.5998

46110689- 7 3.8996 286.93 46.16 3.486 1.8484 1.2568 0.,6013 0.6014

46110689- 8 3.8937 286.91 46.09 3.512 1.8524 1.2595 0.,6007 0.6008

46112189- 1 3.8759 287.53 45.77 2.681 1.6180 1.0988 0.,6028 0.6028

46112189- 2 3.8689 288.03 45.60 2.664 1.6071 1.0901 0.,6017 0.6018

46112189- 3 3.6721 287.24 43.40 5.550 2.2592 1.5390 0,,6006 0.6007

46112189- 4 3.6712 287.29 43.38 5.554 2.2586 1.5384 0,,6004 0.6005

46112189- 5 3.8128 287.14 45.09 3.457 1.8154 1.2349 0,,6000 0.6001

46112189- 6 3.8145 287.79 45.00 3.499 1.8230 1.2381 0.,5994 0.5995

46112189- 7 3.7624 287.08 44.50 4.294 2.0082 1.3671 0.,5995 0.5996

46112189- 8 3.7652 286.91 44.56 4.265 2.0037 1.3646 0.,5997 0.5998

46030890- 1 3.6220 286.36 42.95 5.432 2.2165 1.5141 0.,5987 0.5989

46030890- 2 3.6220 287.12 42.83 5.428 2.2126 1.5087 0.,5988 0.5989

46030890- 3 3.7798 287.59 44.62 3.358 1.7744 1.2062 0.,5982 0.5983

46030890- 4 3.7838 287.42 44.70 3.389 1.7888 1.2164 0..5998 0.5998

46030890- 5 3.7774 287.59 44.59 3.389 1.7862 1.2143 0..5995 0.5996

46030890- 6 3.7727 287.22 44,60 3.359 1.7759 1.2084 0..5988 0.5988

61
BL-114A

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

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

BIBLIOGRAPHIC DATA SHEET

PUBUCATION OR REPORT NUMBER NIST TN 1344

PERFORMING ORGANIZATION REPORT NUMBER

3. PUBUCATION DATE

TITLE AND SUBTITLE Orifice Meter Performance Downstream of a Tube Bundle Flow Conditioner, Elbows,

and a Tee

5. AUTHOR(S)

Charles F. Sindt, Michael A. Lewis, and James A. Brennan

6. PERFORMING ORGANIZATION (IF JOINT OR OTHER THAN NIST, SEE INSTRUCTIONS)

U.S. DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

BOULDER, COLORADO 80303-3328

CONTRACT/GRANT NUMBER 5088-271-1680

8. TYPE OF REPORT AND PERIOD COVERED TOPICAL, 1989

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

8600 West Bryn Mawr Avenue

Chicago, Illinois 60631

10. SUPPLEMENTARY NOTES

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

LITERATURE SURVEY, MENTION IT HERE.)

System pipe configurations can produce large flow disturbances that significantly

affect the accuracy of orifice meters. Flow conditioners such as the tube bundle

are frequently used to remove the effect of upstream disturbances. The flow conditioner

can also influence measurement accuracy if improperly located relative to the orifice

plate in the orifice meter. Tests were conducted in a 3.8 ym (150 pin) Ra surface

finish pipe with a tube bundle flow conditioner located at four different positions

upstream of an orifice plate. The resulting orifice discharge coefficients are shown for the tube bundle flow conditioner at each of the locations. Changes in

the orifice discharge coefficient for orifice plates downstream of three flow disturbances

consisting of elbows or a tee were measured. For most of the configurations tested,

installing a tube bundle flow conditioner immediately downstream of the disturbances

reduced these changes in the discharge coefficient from as much as 2 percent to

less than 0.2 percent. Recommendations for future research needs are suggested.

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

discharge coefficient; flow conditioner; flow disturbances; flow measurement; gas;

orifice meter; tube bundle

13. AVAILABIUTY UNUMITED

FOR OFFICIAL DISTRIBUTION. DO NOT RELEASE TO NATIONAL TECHNICAL INFORMATION SERVICE (NTIS). X

X

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

74

15. PRICE

ELECTRONIC FORM

•irV.S. GOVERNMENT PRINTING OFFICE: 1991 - S74-0I9/45033


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