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NBS TECHNICAL NOTE 981

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U.S. DEPARTMENT OF COMMERCE/ National Bureau of Standards

The Calibration of a Burn

^ Room for Fire Tests on

^

Furnishings

QC

100

.U5853

NO. 981

1978
NATIONAL BUREAU OF STANDARDS

The National Bureau of Standards' was established by an act of Congress March 3, 1901. The

Bureau's overall goal is to strengthen and advance the Nation's science and technology and

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and the Institute for Computer Sciences and Technology.

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The National Bureau of Standards was reorganized, effective April 9, 1978.
DEC 1 2 13rd

The Calibration of a Burn ,os-is:5

Room for Fire Tests on

^ '^'^' Furnishings ^^^X~

King-Mon Tu and

Vytenis Babrauskas

Center for Fire Research

National Engineering Laboratory

National Bureau of Standards

Washington, D.C. 20234

.< °^ oo.

U.S. DEPARTMENT OF COMMERCE, Juanita M. Kreps, Secretary

Dr. Sidney Harman, Under Secretary

Jordan J. Baruch, Assistant Secretary for Science and Technology

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Director

Issued December 1978
National Bureau of Standards Technical Note 981

Nat. Bur. Stand. (U.S.), Tech. Note 981, 59 pages (Dec. 1978) CODEN: NBTNAE

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1978

For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402

Stock No. 003-003-01999-2 Price $2.30

(Add 25 percent additional for other than U.S. mailing).
TABLE OF CONTENTS

Page

LIST OF FIGURES iv

LIST OF TABLES V

NOMENCLATURE vi

ABSTRACT 1

1. INTRODUCTION 1

2. EXPERIMENTAL ARRANGEMENT 2 2.1 Exterior Environment and Ventilation 2 2.2 Test Compartment 2 2.3 Instrumentation 3 2.4 The Gas Burner 4

3. EXPERIMENTS CONDUCTED 4 3.1 Experimental Plan 4 3.2 Results 4

4. MASS BALANCE 5 4.1 Thermocouple Radiation Correction 5 4.2 Measured Mass Flows 7 4.3 Theoretical Mass Flows 7 4.4 Plume Flow 9

5. HEAT LOSSES AND HEAT BALANCE 10

5.1 Convective Ceiling Heat Transfer 10

5.2 Wall and Ceiling Heat Losses 12

5.3 Wall Thermal Conductance 13

5.4 Heat Balance 14

6. EFFECT OF AFTER-BURNER ON BURN ROOM FIRE 16

7. DISCUSSION 16

8. SUM*4ARY 17

9. ACKNOWLEDGMENTS 18

10. REFERENCES ' 18

111
LIST OF TABLES

Page

Table 1. List of instrumentation 19

Table 2. Burn-room tests conducted 21

Table 3. Test data 22

Table 4. Mass flow for test 102 25

Table 5. Mass flow for test 104 26

Table 6. Mass flow for test 105 27

Table 7. Mass flow for test 106 28

Table 8. Mass flow for test 107 29

Table 9. Theoretical mass flows 30

Table 10. Plume flows , 30

Table 11. Ceiling heat transfer 31

Table 12. Heat losses through room surfaces 33

Table 13. Thermal resistance values 34

Table 14. Heat balance 35

Table 15. Influence of after-burner for test 101 conditions 36
LIST OF FIGURES

Page

Figure 1. Plan view of test facility 37

Figure 2. General view of room-corridor complex 38

Figure 3. Plan view of room-corridor complex 39

Figure 4. Elevation of room-corridor complex 40

Figure 5. Vertical temperature profiles for test 101 41

Figure 6. Vertical temperature profiles for test 102 42

Figure 7. Vertical temperature profiles for test 103 43

Figure 8. Vertical temperature profiles for test 104 44

Figure 9. Vertical temperature profiles for test 105 45

Figure 10. Vertical temperature profiles for test 106 46

Figure 11. Vertical temperature profiles for test 107 47

Figure 12. Vertical temperature profiles for test 108 48

Figure 13. Vertical temperature profiles for test 109 49

Figure 14. Vertical temperature profiles for test 110 50

Figure 15. Typical doorway velocity distribution 51
NOMENCLATURE

A Doon%^ay area (m^

)

C Discharge coefficient (-)

C Heat capacity (J/kg-K)

P

- J -/ d Diameter (m)

D Normalized thermal discontinuity height (-)

f Friction factor (-)

g Acceleration of gravity (m/s^)

Gr Grashof number (-)

h Enthalpy (J)

h Convective transfer coefficient (W/m^-K)

c Ah Heat of combustion (J/kg)

c H Room height (m.)

H Doorway height (m)

k Thermal conductivity (W/m-K)

k Entrainment coefficient (-) e L Distance (m)

m Mass (kg)

N Normalized neutral plane height (-)

Nu Nusselt number (-)

P Pressure (Pa)

Pr Prandtl number (-)

q Heat (J)

Q Plume heat flow (W)

r Radial distance (m)

R Thermal resistance (m^-K/^^J) ; ratio of upper to lower

gas space temperatures (-)

Re Reynolds number (-)

T Temperature (K, °C) u Velocity (m/s)

Z Thermal discontinuity height (m)

Z„ Neutral plane height (m)

vi
e Emissivity (-)

V Kinematic viscosity (m^/s)

p Density (kg/m^)

a Stef an-Boltzmann constant

Superscripts

Per unit time

" Per unit area

Subscripts

Convected

Fire gas

Indicated; inflow

Lower (cold) part

Outflow

Plume

Surface

Wall

Ambient

Vll

THE CALIBRATION OF A BURN ROOM FOR FIRE

TESTS ON FURNISHINGS,

King-Mon Tu and Vytenis Babrauskas

A series of ten tests, using a diffusion flame gas

burner as heat source, was conducted in a full-size room

designed for furnishings flammability tests. The gas

burner was used to release known heat rates and to permit

steady state measurements of energy and mass flow. The

gas burner fires simulated preflashover conditions, with

peak temperatures outside the burner plume of around

300°C. The measurements obtained were compared with

available theoretical room fire descriptions and published

heat transfer values. The results showed the importance

of a precise determination of the inflow and exhaust

velocities at the doorway. It was demonstrated that a large number of doorway velocity probes is required to

accurately obtain a room heat and mass balance. A calculational procedure was developed for analyzing the results

which should be useful for future analysis of furnishings

experiments.

Key words: Buoyant plumes; convection; fire tests;

flammability; furnishings; heat transfer; radiation.

1. INTRODUCTION

One of the objectives of the Program for Fire Control-Furnishings at the

National Bureau of Standards (NBS) is to measure the fire contribution of

interior furnishings involved in room fires and to evaluate their potential

hazards. Fire incidence data show that upholstered furniture and other furnishings are the major contributors to all fire deaths. Full-scale experiments

are necessary to identify the sequential process of fire development. For this

purpose, a burn room was constructed in which a wide variety of tests could

be conducted and instrumentation was installed to measure the appropriate

i physical and thermal changes. A gas burner was used as a heat source to

' characterize and calibrate the burn room for the full-scale experiments.

Temperatures, gas velocities, and heat fluxes were recorded during the tests.

The data obtained were analyzed in terms of available theory of room fires

to determine the usefulness and applicability of theoretical models.
A general methodology for analysis has also been developed in the course

of this study. Thus, the procedures outlined will be useful in making heat

and mass flow analyses for any full-size burn-room experiments, not just for

those in the present test room.

2. EXPERIMENTAL ARRANGEMENT

2.1 Exterior Environment and Ventilation

Tests were conducted in a room-corridor complex located inside the NBS

Fire Test Facility Building. The large building is 57 m (187 ft) long and

26.6 m (87 ft 4 in) wide, with a ceiling height of 11 m (36 ft) in the high

bay area over the test space. The general plan and section view are shown

in figures 1 and 2. The heat and smoke generated in the room-corridor complex

was ducted through an exhaust hood to an after-burner for smoke abatement

purposes. The air needed for combustion in the burn room entered the doorways

through the corridor. Air conditioning was provided in the laboratory building

to maintain an average ambient temperature of 20 to 25°C, with a relative

humidity of approximately 40% at the start of each test.

2 . 2 Test Compartment

The experiments were conducted in a full-scale burn room sized to represent a bedroom or small living room. An adjacent room along the corridor was provided for measuring and potentially controlling the flow of air. The burnroom-corridor complex is shown in figures 3 and 4. The length of the burn

room was 3.52 m (11.5 ft) . The adjacent room was 3.05 m (10 ft) long and the

corridor was 6.10 m (20 ft) in length. The rooms were 3.40 m (11 ft 2 in) wide

and the corridor was 2.44 ra (8 ft) wide; they all had the same ceiling height

of 2.44 m (8 ft) . An exhaust hood at the end of the corridor funneled the

exhaust products at low velocity to a stack containing an after-burner for

smoke abatement. Doorways 2.13 m (7 ft) high and 0.91 m (3 ft) wide separated

the burn room, the adjacent room, and the corridor. The rooms had a concrete

slab floor. Walls and ceilings were constructed of 16 mm (nominal 5/8 inch)

Type X gypsum wallboard applied on steel studs. All the surfaces of the rooms,

including the floors, were lined with 13 mm cement-asbestos board (Atlas

Asbestos Co. "Superbestos" ) . The cement-asbestos boards were staggered over

the gypsum wallboard to minimize air leaks and heat loss. All joints, both

gypsum and cement-asbestos, were spackled.

Certain commercial equipment and materials are identified in this report in

order to adequately specify the experimental procedure. In no case does such

identification imply recommendation or endorsement by the National Bureau of

Standards, nor does it imply that the material or equipment identified is

the best available for the purpose.

2 ;
2.3 Instrumentation

The room-corridor complex was instrumented with 86 thermocouples, six

bidirectional velocity probes, four radiometers, and four total heat flux

meters. Test data were recorded by a high speed digital data acquisition

system at the rate of one scan every 10 seconds. The locations of the instrumentation are given in table 1 and shown in figures 3 and 4.

Chromel-alumel (Type K) thermocouples of 18-gage (1.02 mm) wire were

used. Radiometers and total heat flux meters were Gardon-foil type water

cooled units. Bidirectional velocity probes were located in the doorway to

2 measure flows. This type of probe was developed by Heskestad [1] for obtaining accurate low-velocity flow measurements under fire conditions which can involve water condensation, soot deposition, and flow reversal. McCaffrey

and Heskestad [2] have provided calibration techniques for these probes. The

probes used were 12.7 mm in diameter, with construction details as given in

the above reference. The basic equation gives that

4

2^P/P = C(Re)

where AP = measured differential pressure,

p = gas density (obtained from thermocouple reading

adjacent to the probe and the use of the ideal gas law)

,

u = the gas velocity,

and C(Re) = is a constant which depends on the Reynolds number.

For Reynolds numbers in the range of interest the constant

can be approximately taken as C = 1.08 according to the

recommendation of McCaffrey and Heskestad.

Pressures were sensed with variable reluctance pressure transducers. The

velocity probes, together with their associated thermocouples, were initially

placed along the doorway centerline. After steady state was reached and center line values recorded, the probes were moved to make a horizontal traverse

of the doorway at 0.076 m intervals. Only half the doorway was traversed since

use was made of symmetry.

2 Numbers in brackets refer to the literature references listed at the end

of this paper.
I

2.4 The Gas Burner

A diffusion flame gas burner was used for this study. Since no primary

air was injected, a tall, yellowish flame, somewhat typical of furnishings

fires, was obtained. The burner measured 0.84 m by 0.51 m by 0.46 m high

and was placed on the floor in one of three positions — center, back wall,

or corner — shown in figure 3. The fuel used was natural gas. Gas flow was measured by the pressure drop across a calibrated orifice. A gas burner was chosen for this calibration work because of the ease of controlling and mea- ' suring the output of the burner. It is realized, of course, that a gas burner j does not model a real fire in that there is no feedback from the flame

increasing the rate of fuel liberation.

3 . EXPERIMENTS CONDUCTED

3.1 Experimental Plan

Ten experiments were conducted in the test room, varying the burner position and the fuel supply rate. A list of conditions studied is given in

table 2. The heat release rate was obtained by multiplying the gas flow rate

by the lower calorific value of the fuel gas, which averaged 34.2 MJ/m^

(normal temperature and pressure, NTP)

3 . 2 Results

Since no attempt was made to model realistic fire development rates with

the gas burner, only steady state results are presented. Readings were taken

when it was determined that steady state was reached, some 2-3 hours after

ignition. A constant temperature on the unexposed wall surfaces was used to

indicate steady state.

The measurements made are given in table 3. Vertical temperature profiles

at various locations, going from west to east are shown in figures 5 through

14. Within the room, air temperatures were measured in vertical groupings at

six locations: at the four corners, at the room center, and midway between

the center and a corner (the latter designated as "tree") . The channels

plotted are the following:

outer doorway -- 70, 71, 72, 73

outer-room center -- 67, 68, 69

burn-room doorway — 56, 57, 83, 58, 84, 59, 85, 60, 86, 61, 87, 62,

65, 63, 88

NW corner -- 55, 13, 14, 32, 15, 16, 33, 76

SW corner -- 51, 17, 18, 19, 20, 77

burn-room center — 46, 01, 02, 03, 04

tree -- 52, 21, 22, 23, 24, 25, 26, 27, 28, 29, 74

3 A Thoro-Mix Model U4-43 burner, manufactured by Thoro-Mix Power-Flame

Division, Parsons, Kansas, was found suitable for this purpose.

4
NE corner — 53, 09, 10, 11, 12

SE corner — 52, 05, 06, 07, 08

The profiles given in figures 5 through 14 are to be read with each labeled

ordinate as starting at a base line 0°C value.

With the exception of tests with the burner in the corner position, the

test geometry was nearly symmetrical about the east-west axis. The close

agreement for the NW-SW readings and also for the NE-SE ones bears this out.

It might be observed that in the general case the highest air temperatures

were recorded at about 0.1 m below the ceiling. This peak is best visible at

the tree location because of the closer thermocouple spacing there. The

ceiling temperature was generally lower than the peak by 10 to 40°C. In the

lower half of the room the measured temperatures were fairly uniform; the

readings at the floor surface, however, were higher than in the surrounding

air. This is not an error; in fact, it shows the effect of combined radiative

heating and convective cooling.

4. MASS BALANCE

In five experiments where a satisfactory record of doorway velocities was

obtained a mass balance for the burn room could be made. An analysis has been

made for tests 102, 104, 105, 106, and 107.

4.1 Thermocouple Radiation Correction

The air densities for the doorway flows are determined from measured

temperatures and the ideal gas law. The measured temperatures differ somewhat

from the actual temperatures because of radiation error. An attempt was made

to correct for this error.

The procedure used was as follows. Heat balance for the thermocouple

bead is

q" + q" = ^c ^r

The sum of convective and radiative transfer rates are equal to zero since

no heat is stored in steady state. The convective transfer can be expressed

as

^c = (I) ^^ [dl (^f - ^i)

where Nu = Nusselt number

k ^- conductivity of air (W/m-K)

d = bead diameter (m)

T_ = actual air temperature (K) T. = indicated thermocouple temperature (K)
The Nusselt number for airflow past spheres in the velocity range of interest

(Reynolds number <_ 250) is given by [3] :

Nu = 2.0+0.53 /Re

And the Reynolds number is

Re = ud

V

where u = velocity (m/s)

V = kinematic viscosity (m^/s)

For the present experiments the bead diameter can be taken as approximately twice the wire diameter, ord=2xl0 "m. The thermal conductivity

of air, which is temperature dependent, was taken as 0.03 W/m-K for the cold

air inflow and 0.04 W/m-K for the hot gas outflow. The kinematic viscosity

was taken as 0.2 x 10 m'^/s for the inflow and 0.5 x 10 m/s for the

outflow. Combining the above expressions gives

q" = (30 + 80 /u) AT (W/m^) inflow

(40+67 /u)AT (W/m^) outflow

where AT = T_ - T. is the correction term.

f 1 The radiative term can be expressed in a simplified way as follows. For

an environment at a uniform temperature

q = ea (T - T.

)

^r w 1

where T = the bounding surface temperature

Q a = Stefan-Boltzmann constant = 5.67 x 10 W/m^K'*

e = effective emissivity.

The emissivity of a metal varies widely, depending on the surface preparation.

Sooty fuels had been burned in the test room prior to the present test series.

It is therefore, reasonable to assume that the thermocouple surface will be

covered with soot and therefore e ~ 1. The wall emissivity is not well known,

but is fairly high. The effective emissivity has been set to 1 . , a simplification that is reasonable in the present circumstance.

The bounding surfaces viewed by the thermocouple basically consist of

the hot ceiling and the cool floor. Thus the radiation term becomes
k h 1+ U

. (T; - T^ + (T^ - T?)

(5" = 5.7 X 10"^ —^ i 5 i_ (w/m2) ^

2

where the subscripts t and b denote ceiling and floor, respectively. Combining

all terms gives

AT = ^'^ ^ ^Q"'°

(2T^ - t; - T^) inflow

1 + 2.7 y^

-1 =

"^-^ ^ ^°

(2t'^ - t!! - T^ outflow

i t b'

1 + 1.7 .^T

The results are given in tables 4 through 8. The corrected temperatures

for the outflow portion of the doorway averaged about 10 °C higher than measured (range: 3-29°C), while the inflow temperatures averaged about 20°C lower

than measured (range: 11-28°C). It can thus be seen that part of the reason

why the measured doorway temperature distribution is not square-edged, as might

be expected from theoretical consideration [4] , is because of the radiation

error. The corrected profile is not completely square-edged, however, even though the correction appears to slightly over-correct. (Ambient temperature

for this series of tests was approximately 20°C; those corrected inflow values

that are lower than 20°C can be presumed to be over-corrected.)

4.2 Measured Mass Flows

The computed mass flows are given in tables 4 through 8, where a record

of horizontal velocity distributions is also given. Figure 15 illustrates a typical velocity distribution. Readings are reported at five heights in the

doorway. Measurements from velocity probe 112 have not been used since it

appears that they were systematically depressed. The differences for the five

tests range between 7% and 25% of the mean, with a median of 8%. The cause

for the major deviation of 25% for test 107 is not obvious. In general, the

precision of mass flow measurements in this test series was limited by the

small niimber of velocity probes. It would be desirable in future tests to use at least a total of 10 probes. The thermocouple radiation corrections

did help to reduce the imbalance, but it is clear that two or three probes for

inflow or outflow are insufficient to provide a complete and accurate flow

mapping.

4.3 Theoretical Mass Flows

A theory for steady state flow through compartment openings has been

developed by Rockett [4] . The flow depends on the gas temperatures and opening dimensions and is calculable from Bernoulli's equation. The air in the
compartment away from the opening is assumed to be at ambient temperature

below a certain height, Z , and at a uniform elevated temperature above Z . The neutral (zero flow) plane at the opening is at a different height,

Z„, which must be greater than Z_. The flow is known when the Z„ is specified,

N D N '^ Conservation of mass relates heights Z and Z . In the present case fuel flow

is only « 0.3% of the doorway flow and can be neglected in comparison. The

governing relationship is then

-"^' - ^l-g)(l^§,fH

where N = Z^/H = normalized neutral plane height

D = Z /E = normalized thermal discontinuity height

H = doorway height (m)

R = T^/T, = ratio of absolute upper to lower gas temperatures

and the flow equation is

m =- c|p.A/H^/25( w _ f- ^1 • ii_ i[l-|])"' (l-N.V^

3 " D

where m = mass flow (kg/s)

C = discharge coefficient

P^ = ambient air density (kg/m^)

A = doorway area (m^)

g = acceleration of gravity (m/s^)

The flows in and out are approximately equal, differing only by the fuel flow

amount. To solve for flows from basic principles a third relationship would be

needed that gives either N or D. In the present series measured values of N are readily available for five of the experiments. A value of D can be calculated from them and checked for reasonableness. It is hard, however, in the

absence of measurement of N to deduce it from D. As is readily seen in

figures 4-14 the vertical temperature distributions, while definitely indicating hot upper and cold lower zones, are not sharp enough to accurately assign

a therTttal discontinuity height.

8
Values for R, N, D, and m/C are given in table 9. By dividing measured

flows by the theoretical lii/C a value for the discharge coefficient is computed.

The results show outflow coefficients C ranging from 0.58 to 0.75 and inflow O

-J ^ coefficients from 0.39 to 0.60. The average C is 0.66 and the average C,

discounting the 0.39 value due to poor mass balance, is 0.56. Literature

values [5] give for Re > 5000 (based on opening height), C si. c . '^ 0.68. The

present "^ C value of 0.66 agrees well, but the C. value is somewhat low. The

o 1 experiments on which the 0.6 8 recommended value was based were all done at

lower doorway Re numbers than the present room burns (Re - 4-6 x lO'*) . To

the extent that there was a measured difference, however, the experiments of

reference 5 did show C . < C . 1 o

4.4 Plume Flow

According to simple compartment fire theory [4] the gases from the hot

upper layer and the cold lower layer are assumed not to mix along their interface except at the source plume. It is assumed that under steady state con- ditions all of the compartment outflow has come in through the plume, and

therefore the outflow should equal the plume flow, at the height Z , where it

intercepts the hot gas layer. The plume flow equation, as given by Rockett [4],

is:

P f

P f

/ 4 ^ V5 / 5 (1-0)) 2 2\^^V ^d\ , a

5/2

- 1

where subscript f refers to the source (burner) conditions; w is a constant,

for the fuel and is equal to 0.091 for methane. The height Z_^ should properly

be corrected by subtracting the burner distance above the floor and adding a virtual source distance to account for finite burner mouth area. Since the

latter is not well known and since the corrections are of opposite sign,

neither correction has been applied. The equation can be solved for the only

unknown factor, k , the entrainment coefficient. The results are given in

table 10.

For those cases where the burner is located near a room boundary, a circularly symmetrical flow does not result and a modified analysis must be

made. When the burner is located against a wall, a construction using an image burner can be made. The wall situation represents one-half of the flow

that would result from a burner of twice the flow rate in a room double the

size. Thus, ih is obtained by inserting into the above equation an m^ equal

to twice the actual value and then multiplying the calculated m by 0.5. The

2/5 practical effect of this is that only the lii^ term is modified. The values

of k in table 10 have been calculated on this basis. A similar procedure,

using three image burners, is used for analyzing the corner position flows.

9
When the above procedure ^ is followed, the calculated k should be indee pendent of burner placement. From the results in table 10, it can be concluded

that a value of k = 0.56 is indicated by the data. Tests 102 and 106,

however, give differing results, for which no explanation is available. A

value of 0.56 is, of course, considerably higher than the k — 0.16 obtained

[6] when regions of a plume far away from the burner are considered. In a room fire it is generally not possible to be far enough above the burner for

the far region expressions to hold. McCaffrey and Rockett [7] have recently

examined in more detail the experimental verification of entrainment constants.

Instead of using the image burner technique they expressed the different

entrainment in wall and corner positions simply as part of an effective k .

5. HEAT LOSSES AND HEAT BALANCE

5.1 Convective Ceiling Heat Transfer

The test series was originally not designed with the objective of verifying ceiling heat transfer relationships. However, suitable ceiling heat flux

measurements were available for five tests. Table 11 lists the radiative

and total heat flux measurements taken at the center of the ceiling. The

convective component is obtained by subtraction. Since maximum gas temperatures were not measured in the immediate vicinity of the heat flux meters, a certain amount of extrapolation had to be performed. The peak gas temperature,

T^ , below the heat flux meters was assumed to be equal to the reading of TCOl | multiplied by the ratio of the reading at TC21 divided by the TC23 values. 1 (TC21 is located near the height of peak temperatures, while TC23 is at the same height as TCOl.) Ratios were taken using temperature rise values,

(T^ - T^) , with T^ = 20°C. The surface temperature of the heat flux gage is , equal to that of the cooling water, T = 15 °C, plus the average rise in foil

temperature, which was taken as 5°C, giving T = 20°C. Heat average coeffi- , cients were then calculated according to the relation ;

h ^c

C T, - T

f s

Measured values ranged from 6.1 to 24.6 W/m^-K.

Several references are available for empirical and theoretical ceiling

heat transfer coefficients. Alpert [8] has studied the ceiling flows for a situation where the walls are effectively very far away from the region of

interest. For that case, a nondimensional heat transfer coefficient can be

derived:

10
1/3

' T H ^ /

h = h

where Q is the plume heat flow. Alpert then gives the radial dependence of

* r - 5 9 h = 0.67 f 77 , valid outside the plume region.

The f is a friction factor and will most likely be in the range of 0.02 - 0.04 according to Alpert' s results. Values of f calculated from the heat

transfer coefficients in the present case are given in table 11 and range from

0.005 to 0.017.

Comparison can also be made with the direct measurements of Zukoski and

Kubota [9] who studied both the infinite ceiling and the wall-obstructed case. Zukoski reports his results as a band of values within which the infinite

ceiling measurements fell. The obstructed ceiling results fell near the lower

limit of the infinite ceiling measurements. Table 11 also shows a comparison

* between experimentally determined h and Zukoski 's values. The results from

test 104 show a significant disagreement with both Alpert 's and Zukoski 's findings. Since the ratio of the radiant to the convective fluxes is also

quite different for test 104 than for the four other tests, the discrepancy

may be attributable to instriiment malfunction in this case. The remaining

* four tests all show h values which fall right around Zukoski ' s lower limit.

c These data also agree well with Alpert 's equation, if it is taken that in the

obstructed ceiling case a value of f - 0.013 is appropriate.

Use of expressions for h based on plume flow knowledge would be difficult

in a room with realistic furnishings because neither the Q nor the r/H values

would be well defined. It would be much more useful in that case to use some expression that depends only on locally measureable quantities. An expression

can be derived that is dependent on H and T^, but not on Q, by using Alpert'

s

results for T^- as a function of Q. The resulting expression is

-0.44

he = '^i^1 ^(1) ny "'^' *^f'^'

where AT^ = T_ - T^. For a Gaussian ceiling jet profile the value of C,

would be 85. The present data are, instead, best fitted by C-, = 47.

It is also of some interest to compare the experimental results against

the simple relationship for turbulent heat transfer by natural convection to

a horizontal flat plate. Accepted literature values [10] are that

11
Nu = h L

ck

gL^AT

Tv2

- 0.14 (Gr Pr)^^3

where Gr =

And T is some average temperature for the problem. The gas viscosity v, conductivity k, and Prandtl number Pr are to be evaluated at T. The con- vective transfer coefficient is then

h = 0.14 k

c (

g Pr At\

v^ 7

/3

Calculations for flat plate h on the above basis are also shown in

c table 11. For tests 105-110 the experimental values average twice the litera- 1 ture values. Such a difference is not unexpected in view of the differences

between the velocity profiles in the ceiling jet, and in the flat plate

situations. Still, if an equation of this form might be useful in estimating

the ceiling fluxes, then the k and v factors can well be approximated by

power law expressions. When multiplied by 2.0 this gives

h - 162 T ^^3 AT

^'^ (W/m2-K)

c

This expression can then be used for approximate calculations. Although it is

cruder than Alpert's and Zukoski ' s expressions, it does not require the

knowledge of the distance r from the plume center.

5.2 Wall and Ceiling Heat Losses

In the steady state the heat transferred to the ceiling from the room fire

gases is equal to the heat conducted through the ceiling and is equal to the

heat leaving from the unexposed surface. The desired heat flux is, of course,

not what is measured by the total heat flux meter, since its surface temperature is '='20°C and is not the ceiling surface temperature.

Theoretically, the ceiling heat loss might be determined by using the

measurements on the exposed side. The radiative transfer would be the measured

incident flux minus reradiation at the surface temperature. The convective

term could be obtained by using measured temperatures and the best h value.

Practically, this procedure is not very useful since it would entail subtractinc

two large numbers to get a small difference. The desired heat flux can best

be evaluated by considering the conditions at the unexposed surface. The heat

leaving the unexposed surface can be expressed as

12
q = q + q ^w cw ^rw

-2/3 4/3 4 h ? = 0.081 T '^ AT / + ae WW(T - T ) (kW/m ) °°

The gypsum wallboard emissivity can be taken as £ — 0.9 for the temperatures of interest. To get average ceiling unexposed surface values, T can be w averaged over the readings for TC47, TC49, TC54, and TC81. The calculations

are given in table 12. According to these results the ceiling heat losses

ranged from 0.18 to 0.40 kW/m^ . A similar calculation can be made for the

wall losses. It is assumed that losses are non-negligible only through the

upper half of the walls. For the walls, T is taken as the average from the

readings of TC40 and TC44. In the vertical plate case [10], the constant in

the Nusselt number expression is 0.12, giving

-2/3 1/3 h - 0.069 T '^ AT ^ c

The resultant wall fluxes, which were of similar magnitude as the ceiling

fluxes have been multiplied by the effective wall area, 16.0 m^, to yield the

total wall losses. Total room surface losses — wall and ceiling — are added up and tabulated in table 12. These losses range from 3% to 6% of the

fuel heat release rate.

5.3 Wall Thermal Conductance

The wall (and ceiling) material in these tests consisted of two layers:

13 mm of cement-asbestos board on the inside and 16 mm of Type X gypsum wallboard on the outside of the room. The ambient temperature values for the

conductivities are taken as

Material K (W/m-K)

Cement-asbestos board 0.14

Gypsum wallboard 0.20

These conductivities are not strongly dependent on temperature. The total

thermal resistance, for the thickness used, is R = 0.17 m^-K/W.

This composite resistance should agree with the measured resistance,

which can be gotten as

T - T

R = -^ ^

^w

13
The average measured resistance is seen from the computations in table 13 to

be R = 0.74, leaving a net resistance of R = 0.74 - 0.17 = 0,57 m^-K/W

unaccounted for.

The above computation was based on the implicit assumption that thermal

contact between the two wall strata is perfect. Since no special pains were

taken to achieve a tight fit, however, it is likely that with repeated heatinginduced deformation some gaps could exist. It is of interest to calculate the

possible resistance that such a gap could introduce. The maximum gap thickness that can be expected is on the order of L = 2 mm. The thermal conductivity of air is k = 0.036 W/m-K at an average interface temperature of 428 K.

The actual gap conductance is the sum of the gas conductance plus the radiative

conductance

R R R

c r

= ^ + 4 eal^

= 18+15

R = 0.03 m2-K/W

Thus, contact resistance can account for up to 5% of the difference between

measured and calculated R values. The remaining discrepancy must be attributed i to either changed material properties with heating or to inapplicability of the

flat plate expressions for the external heat transfer.

5.4 Heat Balance

The heat balance can be written for the system consisting of the gas

within the room as follows:

h.in

- h ^ - q, =0

out ^loss

where h denotes enthalpy. Assumptions of steady state and negligible kinetic

energy have been included. The combination reaction is

1 kg fuel + r kg air — ^ (1+r) kg products

and Ah = h^ + rh - (l+r)h

c f a p

where f, a, and p denote fuel, air, and products, respectively, and all

enthalpy values are taken at a reference temperature of 298 K.

14
The heat balance becomes

m_Ah - m (h T^ - h ^nor^) "

f c

^i =0

P P/ f p,298K ^loss

It simplifies analysis considerably to assume that the heat capacity of

the products is the same as of air. Also, the heat capacity of air at 300°C

is only 1% different than at room temperature; thus it is useful to assume

that Ah . = C AT, with C being taken as 1.0 kJ/kq-K. Then air p P

Ij m^

f

Ah

c

- m

o (1.00) AT - q,loss =0

ij where m is the total outflow. The calorific value. Ah , to be used is the

o ' c

lower, or net, value which excludes the latent heat of water vaporization.

' This is most convenient since otherwise the h term could not oe simply represented with a constant C but would have to include a vaporization contribution,

ir AT can be computed on a flow-weighted basis at the doorway. The calculations

are given in table 14.

The wall surface losses were considered in section 5.2 and are also

included in table 14. The radiant losses through the doorway can be estimated

by the expression

q ^ a y (t'^ - t") AA.

1

where the summation is taken over temperature readings at the various heights

of the doorway.

The error in the heat balance is also shown in table 14. The range is

from 6.8 to 13.8%, with a mean of 10.5%. The errors consistently show that

the losses exceeded the heat gain. No allowance was made for incomplete

combustion losses. Incomplete combustion losses would further serve to

increase the disparity in the measurements. The dominant source of error is

presumed to be in the doorway velocity measurements. The poor agreement shows

that using two or three points to measure a distribution which, according to

theory, is expected to be parabolic, is quite insufficient. In future work

more vertical sampling positions should be provided to improve the accuracy.

It should be observed, however, that in a test of actual furnishings steady

state conditions will not exist. This means that a horizontal traversing of

the velocity probes is not readily feasible and, therefore, that greater

reliance will have to be placed on accuracy of the vertical distribution.

15
6. EFFECT OF AFTER-BURNER ON BURN ROOM FIRE

The test facility exhaust hood is equipped with a draft-inducing exhaust

blower and an after-burner for smoke abatement. Tests were conducted to determine if the induced flow due to after-burner operation had an effect on burnroom measurements. Repeat room fires were conducted for tests 101 and 110

with the after-burner on and off. The results for test 101 are given in

table 15; the results of test 110 were similar. The temperature rises with

the after-burner were, on the average, 7% lower than without. This difference

was judged not significant. Since the test burner flames were not smoky, and

since the effect of the after-burner on the temperature fields was small, and

in the interest of energy conservation (the after-burner consumed some ten | times more fuel than the test burner) all the tests reported in the previous

sections were conducted with the after-burner off.

7. DISCUSSION

The measuring of the room fire variables using a steady state gas burner

as fuel source represents idealized conditions for measurement. A room fire

fueled by furnishings will, by contrast, be strongly time dependent and poorly

characterized in its release rate. Yet the present series of tests has shown

numerous difficulties in accurate measurement and in theoretical analysis.

The most significant shortcoming was the small number of velocity measurement probes in the doorway. It is clear that two or three probes are insufficient for characterizing the inflow or the outflow, both of which are nonlinear functions of height. It is apparent that in future work a minimum

of 10 probes should be used, distributed about equally between inflow and outflow. The failure to obtain adequate mass and heat balances can be attributed

directly to the insufficiency of velocity sampling points.

Plume entrainment and ceiling heat transfer measurements are intrinsically more difficult to make than doorway flows. The agreements with theory

and literature values achieved for these measurements can be considered satisfactory. Doorway discharge coefficients determined were also as expected.

Heat transfer through the ceiling and upper wall surfaces could not be

satisfactorily compared with material property values and literature heat

transfer coefficients. This might be due to degraded material properties,

errors in surface temperature measurement, or inapplicability of the literature

heat transfer coefficients.

16
8 . SUMMARY

A series of detailed steady state measurements was taken in a furnishings

burn room fueled with a gas burner. These measurements were intended to be

used as a calibration for the constants and procedures used in analysis since

only with a controlled fuel source, such as a gas burner, can heat release

rates be adequately characterized.

The major observations were the following:

o A general calculational procedure for making heat and mass flow

balance in a test burn compartment has been evolved. The

procedures adopted are quite general and will be useful for

situations where steady state flows are to be determined

in a room with a vertical single ventilation opening and a single horizontal fuel source located in the lower half of

the room. For time-dependent flows only a minor extension is

needed in the analysis of wall losses.

o Agreement with room fire theories is good, generally within

the error bounds (—factor of 2) of the theories.

o Because of insufficient precision in the doorway velocity

measurements a satisfactory heat balance could not be obtained.

The doorway flow is the dominant loss term at steady state; thus

accuracy in determining wall losses and doorway radiation was

not limiting.

o A plume entrainment coefficient of 0.56 was calculated from the

data. This is in general agreement with other data showing high

entrainment coefficient in the source region of combusting plumes.

o Discharge coefficients were calculated which were quite close to

the literature value of 0.68 on outflow, but less on inflow.

o Doorway mass inflows and outflows showed an imbalance of about

8%, largely attributable to insufficient velocity probe positions.

o Good agreement was obtained for the measured ceiling heat transfer

compared with literature values.

o No agreement was obtained between wall loss calculations based on

(a) the measured unexposed surface temperatures, using standard

convective coefficient formulas, and (b) the wall material con- ductance and measured temperature drops. Several explanations

are possible, but a single cause was not reliably identified.

o Required thermocouple radiation corrections in the doorway were

about -10 °C for inflow, and about +20 °C for outflow temperatures

on the order of 300 °C. In the early stages of heating the inflow

correction would be more and the outflow correction less.

17
9 . ACKNOWLEDGMENTS

The authors would like to thank both Mr. R. Smith and Mr. T. Prather for

their assistance in the experimental work, and Mr. R. Smith for his assistance

in developing a computer program and reduction of experimental data.

10 . REFERENCES

[1] Heskestad, G. , Bidirectional flow tube for fire-induced vent flows,

The Large-scale Bedroom Fire Test, July 11, 1973, FMRC Serial 21011.4,

pp. 140-5, P. A. Croce and H. W. Emmons, eds . , Factory Mutual Research

Corp., Norwood (1974).

[2] McCaffrey, B. J. and Heskestad, G. , A robust bidirectional low-velocity

probe for flame and fire application. Combustion and Flame, Vol. 26,

125-7 (1976) .

[3] Knudsen, J. G. and Katz , D. L. , Fluid Dynamics and Heat Transfer, p. 511

(McGraw-Hill, New York, 1958).

[4] Rockett, J. A., Fire induced gas flow in an enclosure. Combustion

Science and Technology, Vol. 12, 165-175 (1976).

[5] Prahl, J. and Emmons, H. W. , Fire induced flow through an opening.

Combustion and Flame, Vol. 25, 369-385 (1975).

[6] Tamanini, F., An Improved Version of the k-e-g Model of Turbulence and

Its Application to Axisymmetric Forced and Buoyant Jets, Report 22360-4,

RC77-BT-4, Factory Mutual Research Corp., Norwood (1977).

[7] McCaffrey, B. J. and Rockett, J. A., Static pressure measurements of

enclosure fires, J. Research, Nat. Bur. Stand. (U.S.), Vol. 82, 107-117

(Sept. -Oct. 1977) .

[8] Alpert, R. L. , Fire Induced Turbulent Ceiling-Jet, FMRC Serial 19722-2,

Factory Mutual Research Corp., Norwood (19 71).

[9] Zukoski, E. E. and Kubota, T. , Experimental Study of Environment and

Heat Transfer in a Room Fire (Quarterly Progress Report, June 1, 1975 - September 1, 1975), NBS GCR 77-98, National Bureau of Standards,

Washington, D.C.

[10] Fishenden, M. and Saunders, 0. A., An Introduction to Heat Transfer

(Oxford University Press, Oxford, 1950).

18
Table 1 List of instrumentation

01

02

03

04

05

06

07

08

09

10

11

12

13

14

15

16

17

18

19

20

21

22

23

24

25

26

27

28

29

32

33

35

36

37

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

Thermocouples

Center of room,

Center of room,

Center of room, 1 Center of room, 2 SE corner of room

SE corner of room

SE corner of room

SE corner of room

NE corner of room

NE corner of room

NE corner of room

NE corner of room

NW corner of room

NW corner of room NW corner of room

NW corner of room

SW corner of room

SW corner of room

SW corner of room

SW corner of room

0.91 m from E wall,

0.91m from E wall,

0.91 m from E wall,

0.91m from E wall

,

0.91m from E wall

,

0.91m from E wall,

0.91m from E wall

,

0.91 m from E wall,

0.91m from E wall.

31 m from ceiling

92 m from ceiling

53 m from ceiling

14 m from ceiling

. 31 m from ceiling

0.92 m from ceiling

1.53 m from ceiling

2.14 m from ceiling

0.31 m from ceiling

0.92 m from ceiling

1.53 m from ceiling

2.14 m from ceiling

0.31 m from ceiling

0.92 m from ceiling

1.53 m from ceiling

1.83 m from ceiling

0.31 m from ceiling

0.92 m from ceiling

1.53 m from ceiling

2.14 m from ceiling

0.91 m from S wall,

0.91m from S wall,

0.91 m from S wall,

0.91 m from S wall,

0.91 m from S v/all,

0.91 m from S wall,

0.91 m from S wall,

0.91 m from S wall,

0.91 m from S wall.

0.08

0.10

0.31

0.61

0.92

22

52

83

13

m from m from m from m from m from

m from m from m from

m from

ceiling

ceiling

ceiling

ceiling

ceiling

ceiling

ceiling

ceiling

ceiling

On S wall, 2,

On S wall, 1,

On E wall, 1,

NW corner of room, 1.22 m from ceiling

NW corner of room, 2.13 m from ceiling

28 m from E wall, 1.83 m from ceiling

06 m from E wall, 0.61 m from ceiling

22 m from S wall, 1.83 m from ceiling

On rear wall surface, behind TC 37

On E wall, 1.22 m from S wall, 0.61 m from ceiling

On unexposed wall surface, behind TC 39

On N V7all, 1.22 m from E wall, 1.83 m from ceiling

On unexposed wall surface, behind TC 41

On N wall, 2.43 m from E V7all, 0.61 m from ceiling

On unexposed wall surface, behind TC 4

3

On ceiling, 1.70 m from S wall, 0.31 m from E wall

On ceiling, 1.70 m from S wall, 1.83 m from E wall

On unexposed ceiling surface, behind TC 46

On ceiling, 1.70 m from S wall, 2.74 m from E wall

On unexposed ceiling surface, behind TC 48

On ceiling, 1.70 m from S wall, 3.35 m from E wall

On ceiling, 0.91 m from S wall, 2.59 m from E wall

On ceiling, 0.91 m from S wall, 0.91 m from F wall

On ceiling, 2.49 m from S wall, 0.91 m from E wall

On unexposed ceiling surface, behind TC 53

On ceiling, 2.49 m from S wall, 2.59 m from E wall

At doorway centerline, 0.0 9 m below top

At doorway centerline, 0,

At doorway centerline, 0,

At doorway centerline,

At doorway centerline, 0. At doorway centerline, 1,

At doorway centerline, 1,

At doorway centerline, 1.

13 m below top

30 m below top

61 m below top

91 m below top

22 m below top

52 m below top

83 m below top

19
91 m from E wall

1 07 m from E wall

61 m from E wall

2 59 m from E wall

3. 05 m from E wall

Table 1. (continued)

Thermocouples

At doorway, 1.47 m from S wall, 1.52 m below top

Center of adjacent room, 0.91 m from ceiling

Center of adjacent room, 1.52 m from ceiling

Center of adjacent room, 2.13 m from ceiling

Adjacent room doorway centerline, . 30 m below top

Adjacent room doorway centerline, 0.91 m below top

Adjacent room doorway centerline, 1.52 m below top

Adjacent room doorway centerline, 2.13 m below top

On^floor, 0.91 m from S wall,

On floor, 2.33 m from S wall,

NW corner of room, on floor

SW corner of room., on floor

On floor, 1.70 m from S wall.

On floor, 1.70 m from S wall.

On floor, 1.70 m from S wall,

On unexposed ceiling surface, behind TC 45

Quick-response thermocouple, adjacent to TC 48

At velocity probe 113, 0.13 m below doorway top

At velocity probe 112, 0.30 m below doorway top

At velocity probe 111, 0.66 m below doorway top

At velocity probe 110, 1.07 m below doorway top

At velocity probe 109, 1.37 m below doorway top

At velocity probe 108, 1.91 m below doorway top

On unexposed ceiling surface, behind TC 90

Ceiling of adjacent room, 0,61 m W of test room

Floor of adjacent room, 0.61 m W of test room

Heat Flux Meters

100 Radiometer, facing East, in adjacent room, 0.91 m W of test room,

1.53 m from ceiling

101 Radiometer, facing East, on W wall, 0.61 m from S wall, 0.61 m from ceiling

103 Total heat flux meter, on ceiling, 1.70 m from S wall, 2.89 m

from E wall

104 Total heat flux meter, on ceiling, center of room

105 Radiometer, same location as heat flux meter 104

106 Radiometer, on floor, 1.70 m from S wall, 2.59 m from E wall

107 Total heat flux meter, same location as heat flux meter 106

114 Total heat flux meter, same location as heat flux meter 101

Velocity Probes

108 At doorway, 1.91 m below doorway top

109 At doorway, 1.37 m below doorway top

110 At doorway, 1.07 m below doorway top

111 At doorway, 0.66 m below doorway top

112 At doorway, 0.30 m below doorway top

113 At doorway, 0.13 m below doorway top

Channel

Number

65

67

68

69

70

71

72

73

74

75

76

77

78

79

80

81

82

83

84

85

86

87

88

89

90

91

20
Table 2. Burn-room tests conducted

Test No. er Position Heat Release Rate

(kW)

Center 164

Center 184

Center 203

Corner 164

Corner 184

Corner 203

Back 164

Back 184

Back 203

Back 228

101

102

103

104

105

106

107

108

109

110

21
Table 3. Test data (at steady state)

Channel Thermocouples (C)

Test Number

101 102 103 104 105 106 107 108 109 110

01 314 360 377 224 273 289 235 270 291 308

02 325 445 458 172 222 237 168 197 214 225

03 648 718 748 52 81 87 62 73 84 87

04 65 61 64 36 51 54 42 48 54 55

05 -- 271 288 241 290 315 271 313 337 337

06 250 265 281 211 262 281 233 268 289 306

07 81 87 92 51 77 84 69 83 100 107

08 61 29 27 22 30 29 27 26 31 29

09 238 263 280 261 322 349 260 299 324 347

10 234 253 270 239 300 320 229 260 282 298

11 63 68 72 70 98 106 55 65 77 79

12 56 62 66 56 79 87 50 58 70 72

13 252 272 287 218 272 291 230 259 280 295

14 242 257 273 201 250 265 212 241 263 276

15 92 98 101 59 91 100 67 78 94 99

16 70 78 82 50 69 77 57 66 78 83

17 237 259 276 190 237 253 217 246 267 282

18 250 266 284 199 248 265 222 253 274 292

19 82 87 94 55 83 92 65 77 91 97

20 64 69 75 23 64 69 27 55 67 72

21 264 288 306 235 287 308 264 303 330 348

22 273 299 318 238 291 313 — -- -- —

23 -- 276 293 226 275 296 235 269 290 305

24 247 267 283 202 258 276 219 250 272 285

25 — 245 265 184 232 247 204 234 256 273

26 158 141 158 113 163 177 132 160 182 193

27 75 82 86 62 93 103 80 96 111 120

28 80 86 92 49 68 72 69 81 92 97

29 70 75 81 42 60 64 58 70 80 87

32 169 159 178 118 169 180 100 125 143 153

33 57 64 66 40 55 57 43 50 60 61

35 64 71 74 39 60 64 46 53 62 64

36 226 242 257 190 234 252 229 263 287 300

37 100 96 102 57 82 92 145 173 194 206

38 31 26 25 20 25 24 25 26 28 28

39 46 234 248 197 248 266 203 234 260 273

40 53 50 50 40 60 62 41 47 55 55

41 58 105 112 93 130 144 85 101 120 126

42 37 33 32 25 33 33 32 34 38 37

43 220 252 269 198 247 265 211 240 261 275

44 63 58 58 41 56 57 48 53 58 58

45 242 253 267 234 282 305 306 352 378 406

46 323 379 416 234 295 314 240 276 298 314

47 44 88 86 31 56 57 35 41 53 48

48 286 -- — 204 -- — 212 245 264 276

49 62 66 66 46 61 63 51 52 58 55

50 242 259 277 166 213 228 177 204 223 237

51 250 274 293 184 234 250 204 232 253 267

52 254 265 282 207 252 271 247 284 308 328

53 263 280 291 275 337 364 260 296 320 343

22
Table 3. (continued)

Channel Thermocouples (C)

Test Number

101 102 103 104 105 106 107 108 109 110

54 40 38 39 30 38 37 35 36 39 40

55 282 303 321 214 274 292 216 247 268 282

56 248 257 274 197 249 266 210 238 255 272

57 262 278 297 211 260 278 231 263 283 300

58 249 -- — 208 — -- 227 257 279 294

59 229 248 264 198 250 268 219 245 268 281

60 109 103 115 70 110 124 70 84 95 103

61 61 86 93 34 83 91 40 44 53 62

62 44 41 43 28 39 42 32 36 41 41

63 41 38 41 28 37 37 33 35 39 38

65 — 41 43 29 39 40 33 36 41 41

67 126 111 128 48 118 124 49 55 63 68

68 42 41 42 28 43 43 34 38 42 42

69 33 29 29 20 31 29 23 27 27 27

70 30 26 26 20 28 27 23 24 24 25

71 29 27 26 25 28 27 29 30 31 31

72 28 24 24 19 26 25 22 23 24 25

73 26 23 22 18 25 23 21 21 22 22

74 107 105 113 64 90 100 111 137 ' 159 168

75 76 67 65 38 55 60 59 70 88 89

76 75 61 65 41 53 56 47 50 60 62

77 88 104 118 58 92 102 61 85 98 98

78 95 113 119 96 136 153 139 162 185 192

79 83 99 105 — 87 93 — — — —

80 75 65 78 34 60 63 41 46 52 55

81 52 52 52 44 58 57 53 59 66 67

82 254 225 235 130 180 192 136 152 167 171

83 253 272 291 208 257 273 226 257 280 292

84 245 259 274 -- 256 275 — — — —

85 224 227 235 177 234 249 180 202 245 243

86 58 69 70 33 60 80 43 44 60 59

87 46 44 43 35 40 40 41 47 55 56

88 39 53 43 28 37 38 33 36 39 41

89 188 42 43 — 44 44 — — — —

90 207 216 228 — 210 223 — — — —

91 53 32 32 32 32

Heat Flux Meters

(kW/ra2)

100 1.5 1.4 1.7 0.7 1.2 1.4 0.9 — -- 1.5

101 2.8 3.2 3.1 1.9 2.9 3.7 0.9 — — 5.1

103 8.2 10.4 11.7 6.4 5.1 6.2 6.8 — — 9.8

104 9.2 15.8 16.3 3.1 6.7 8.7 6.1 — — 7.6

105 11.8 3.1 3.7 1.8 1.4 1.8 2.0 -- — 3.2

106 2.2 2.9 3.3 1.3 2.0 2.4 1.5 — — 2.8

107 2.8 3.3 3.8 1.5 2.4 2.9 1.7 — — 3.1

114 — 5.4 6.4 2.0 2.9 3.4 4.3 — — 5.7

23
Table 3. (continued)

* Channel Velocity Probes (m/s)

Test Number

101 102 103 104 105 106 107 108 109 110

108 -- -0.90 -0.97 -0.75 -0.98 -1.05 -0.73 -- -- -0.88

109 - -0.53 -0 63 -0 42 -0 74 -1 01 -0 35 -0.50

110 — -0.40 -0 41 -0 41 -0 48 -0 28 -0. 20

111 1.70 1.89 2 00 1 40 2 25 2 31 1. 36

112 1.96 1.31 1 52 1. 34 1 81 1 77 1. 32

113 2.26 2.67 2 44 1 82 2 53 2 46 2. 05

-0.43

1.72

1.42

2.19

* Values at doorway centerline. See tables 4-8 for other values,

24
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29
Table 9, Theoretical mass flows

iH

rO -a T! U 0) ,—. a ^

H ^-- Sh m M en -p en P \ D \

^N

CJ U \ 0] cr- en -H CP M \ D^ (T3-E M fo-e ^

O'E ^ V — OJ —

Test (m) N D R

0) "

x;

Eh

f' c

o ?

102 1.14 0.54 0.45 1.89 1.56 1.02 0.65 0.88 0.56

104 1.14 0.54 0.44 1.68 1.54 1.15 0.75 0.93 0.60

105 1.13 0.53 0.42 1.86 1.61 1.05 0.65 0.91 0.57

106 1.02 0.48 0.30 1.93 1. 88 1.09 0.58 0.93 0.49

107 1.03 0.49 0.31 1.72 1. 80 1.17 0.65 0.71 (0.39)

Table 10. Plume flows

Burner

position (kg/s)

^D

Test

ft '/5 m^ k

e

102 Center 0.0035 273 9.20 0.26

104 Corner 0.0032 324 9.33 0.55

105 Corner 0.0035 280 8.59 0.56

106 Corner 0.0039 259 5.88 0.93

107 Back 0.0032 293 6.37 0.57

0.091

0^ = 0.68 kg/m3 at 15°C

30
Table 11, Ceiling heat transfer

11a. Experimental measurements

Flux meter read ings

*f T

s AT

c Test ^r '^total ^c hc (kW/m2) {kW/m2) (kW/m2) (°C) (°C) (K) (W/m2-K)

104 1.8 3.1 1.3 233 20 213 6.1

105 1.4 6.7 5.3 285 20 265 20.0

106 1.8 8.7 6.9 301 20 281 24.6

107 2.0 6.1 4.1 264 20 244 16. 8

110 3.2 7.6 4.4 351 20 331 13.3

lib. Comparison with Alpert 's theory

Test q- V3

(W-1/3 )

h*

c

(-)

r/H

(-)

f

measured

(-)

f Alpert

(-)

^1

(-)

104 0.0183 0.004 0.67 0.005 02 - 0.04 17

105 0.0176 0.013 0.67 0.015 02 - 0.04 51

106 0.0170 0.015 0.67 0.017 02 - 0.04 61

107 0.0183 0.011 0.58 0.012 02 - 0.04 42

110 0.0164 0.008 0.58 0.008 02 - 0.04 28

31
lie. Comparison with Zukoski's theory

h*

c h*

c Test measured Zukoski

(-) {-)

104 0.004 012 - 0.021

105 0.013 012 - 0.021

106 0.015 012 - 0.021

107 0.011 012 - 0.020

110 0.008 012 - 0.020

lid. Comparison with flat nlate values

"'c Test measured flat plate

{W/m2-K) (W/m^-K)

104 6.1 9.1

105 20.0 9.5

106 24.5 9.7

107 16.8 9. 6

110 13.3 10.1

32
O ; -p y-

(0 —

.

p E

o X

BO

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s:3o

u

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3 —

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= 3

3 E

: l-l \

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3 «

Eh —

3 e

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33
'able 13. Thermal resistance values

% "s

TwR

measured

R

calculated Difference

Test Surface (W/m2) (°C) (°C) (m2-K/W) (m2-K/W) (m^-K/W)

104 Ceiling 180 237 38 1.10 0.17 0.93

Walls 210 198 41 0.75 0.17 0.58

105 Ceiling 380 305 53 0.66 0.17 0.49

Walls 370 248 58 0.51 0.17 0.34

106 Ceiling 400 328 54 0.69 0.17 0.52

Walls 390 266 60 0.53 0.17 0.36

107 Ceiling 260 339 44 1.13 0.17 0.96

Walls 220 207 45 0.74 0.17 0.57

110 Ceiling 380 335 53 0.74 0.17 0.57

Walls 370 274 57 0.59 0.17 0.42

34
OC

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35
Table 15. Influence of after-burner for test 101 conditions

Temperature (°C) Temperature (°C) Channel without after-burner with after-burner

01 314 316

02 325 364

03 648 702

06 250 239

07 81 74

08 61 56

09 238 230

10 234 226

11 63 57

12 56 51

13 252 241

14 242 230

15 92 83

16 70 64

17 237 228

19 82 74 20 64 57 21 264 255

22 273 264

24 247 238

26 158

" 140

27 75 70

28 80 75

29 70 64

36 226 214

37 100 92

38 31 27

40 53 48

41 58 53

42 37 34

43 220 210

44 63 60

45 242 235

46 323 308

48 286 276

49 62 58

50 242 230

51 250 240

52 254 245

53 263 255

54 40 37

55 282 269

56 248 240

57 262 254

58 249 239

59 229 220

60 109 95

61 61 60

62 44 40

63 41 36

67 126 107

68 42 37

69 33 27

70 30 28

71 29 26

72 28 23

73 26 22

74 107 99

75 76 70

76 75 64

77 88 79

78 95 88

79 83 75

30 75 80 81 52 50

82 254 244

83 253 238

84 245 233

85 224 200

86 58 72

87 46 42

88 39 33

90 207 199

91 53 49

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Figure 15. Typical doorway velocity distribution

51
NBS.114A (REV. 7-73)

U.S. DEPT. OF COMM. BIBLIOGRAPHIC DATA

SHEET

1. PLBLIC ATION OR RFIPORT NO. NBS TN 981

2. Gov't Accession

No.

3. Recipient's Acces.'sion No.

4. TITLE AND SUBTITLE

THE CALIBRATION OF A BURN ROOM FOR FIRE TESTS ON

FURNISHINGS

5. Publication Date December 1978

6. Performing Organization Code

7. AUTHOR(S)

King-Mon Tu and Vytenis Babrauskas

8. Performing Organ. Report No.

9. PERFORMING ORGANIZATION NAME AND ADDRESS

NATIONAL BUREAU OF STANDARDS

DEPARTMENT OF COMMERCE

WASHINGTON, D.C. 20234

10. Project/Task/Work Unit No. 7527677

11. Contract /Grant No.

12. Sponsoring Organization Name and Complete Address (Street, City, Slate, ZIP)

Same as No . 9

13. Type of Report & Period CoveredFinal

14. Sponsoring Agency Code

15. SUPPLEMENTARY NOTES

16. .\BSTRACT (A 200-word or less (actual summary of most significant information. If document includes a significant

bibliography or literature survey, mention it here.) A series of ten tests, using a diffusion flame gas burner as heat source, was conducted in a full-size room designed for furnishings flammability tests.

The gas burner was used to release known heat rates and to permit steady state

measurements of energy and mass flow. The gas burner fires simulated preflashover conditions, with peak temperatures outside the burner plume of around 300°C

The measurements obtained were compared with available theoretical room fire

descriptions and published heat transfer values. The results showed the importance of a precise determination of the inflow and exhaust velocities at the

doorway. It was demonstrated that a large number of doorway velocity probes is

required to accurately obtain a room heat and mass balance. A calculational

procedure was developed for analyzing the results which should be useful for

future analysis of furnishings experiments.

17. KEY WORDS (six to twelve entries; alphabetical order; capitalize only the first letter of the first key word unless a proper name; separated by semicolons) Buoyant plumes; convectiou; fire tests; flammability;

furnishings; heat transfer; radiation.

18. AVAILABILITY [IT Unlimited

I For Official Distribution. Do Not Release to NTIS

I y Order From Sup. of Doc, U.S. Government Printing Office Washington, D.C. 20402, SD Stock No. SN003-003

I

I Order From National Technical Information Service (NTIS)

Springfield, Virginia 22151

19. SECURITY CLASS

(THIS REPORT)

UNCLASSIFIED

20. SECURITY CLASS

(THIS PAGE)

UNCLASSIFIED

21. NO. OF PAGES

59

22. Price

$ 2.30

USCOMM.DC 29042-P74

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