FROM.:TAYLOR CLAY FAX NO. :7046362413 San. 28 2009 04:41PM P1 

•1 • I •oo7 

Taylor Clay Products, Inc. 

P. O. Box 2128, Salisbury, North Carolina 28145-21•8 

185 Peeler Rd. •8147 Phone (704) 636-2411 

taylor•taylorclay.com Fax (704) 636-2413 

www, taylor¢lay.eom 

FAX 

RTZ Pages: 

Phone: 
FROM :TAYLOR CLAY :?046362413 Jan. 28 2009 04:41PM P2 

ENGINEERINQ CONSLILTANTS, INC., 

Blvd. Oharlotte, NO •8=69 |704) 5•8-1049 FAX (?04) -•98-1050 

August l 8, 2000 

Mr. H•oM Howard 

Plant Enginecr 

Taylor Clay Products Company 

Post Office Box 2128 

Salisbury, North Carolina 28145 

Stack Emission Testing Services 

Taylor Clay Product Company 

Salisbury, North CaroIina 

Trigon Project No. 046-00-076 

Dear Mr. Howard: 

Please find enolosed a copy of the "Summary of Results", field dam shoots, laboratory analysis, and the production data for thv hydrogen fluoridv (HF), and sulfur dioxido (SO2) testing conducted on July 11 & 12, 2000 at the Taylor Clay Products facility in Salisbury, North Carolina. Testing was conducted on the limestone scrubber exhaust for concentrations and ¢missions rates of I-IF and SO2. Three 3-hour sampling runs were conducted at the svrubb•r exhaust. 

Thank you for the opportunity to provide this servico to you. If there regm'ding are any questions the sampling procedures or data generated fi'om this project, please do not hesitate to contact me. 

RFC:mos 

Enclosures 

Sinc•ty, 

TRIGON ENGINEERING CONSULTANTS, INC. 

Robert F. Callahan 

Project Manager 

Air Monitoring Department 
FROM :TAYLOR CLAY FAX NO. :7@46362413 5an. 28 2009 04:41PM P3 

Run Number 

Date: 

0 

Pb•r 

EPA METHOD 26A 

Detorraination of Hydrogen Fluoride Emissions 

Taylor Clay Products 

Salisbury, North Carolina 

Limestone Scrubber Exhaust 

I 2 3 Avg 

07/11/00 07/12/00 07/12/00 

180.0 180.1 180.0 

29.12 29.15 29.18 29.15 

Net Time of T•st, minutes 

Barometric Pressure, in. Hg 

Pg 

Ps 

V• 

/Sl"O 

Vwc 

%Oi 

%CO• 

%CO 

M• 

Cp 

APS 

Ts 

V• 

A 

Static Pressure, in. Hg 

St•ck Pressure, Absolute, in. Hg 

Actual Meter Volume Sampled, cu. ft. 

Avg. Delta H, in. H20 

Avg. Gas Meter Temp., Dog. F 

Volume Sampled at Stand. Con&, cu. ft. 

Volume of Water Collscmd, rnl 

Volume of Water Vapor at St& Cond.,SCF 

Moisture Conmnt of Gas Stream 

Percent Moisture in Stack 

Mole Fraction of Dry Gas 

Percent Oxygen, Dry 

Percent Carbon Dioxide, Dry 

Percent Carbon Monoxide, Dry 

Mole. Wt. Stack Oas, Dry Basis, lb/lb mole 

Mole. Wt. Stack Gas, Wet Basis, Ib/lb mole 

Pitot Tube Constant 

Avg. Sqrt. Delta P, in. H20 

Avg. Staok Temp., Deg. F 

Avg. Sta•k Velooity, 

Area Stack, 

-0.019 -0.019 -0.019 -0.019 

29.I01 29.131 29.161 29.131 

168.02 161.82 165.82 •65.22 

2.55 2.38 2.48 2.47 

85,2 80.5 80.8 82.2 

159.39 154.93 158.87 157.73 

338.7 340.4 332.8 337.3 

15.95 16.03 15,67 15.88 

0.091 0.094. 0.090 0,092 

9.1 9,4 9.0 9.2 

0,909 0,906 0,910 0.908 

I6.63 16.64 17.02 16.76 

2.49 2.58 2.34 2.47 

0.00 0.00 0.00 0.00 

29.064 29.078 29.055 29.066 

28.057 28.040 28.063 28.053 

0.84 0.83 0.84 0.84 

0.463 0,477 0.468 0,469 

405.3 408.9 405.9 406.7 

34.3 34.9 34.6 34,6 

12,048 12,048 12.048 12,048 
FROM :TAYLOR CLAY FAX NO. :7046362413 Jan. 28 2009 04:42PM P4 

;;-:,• 

;L}" 

• 

•:•".. 

,.':...' 

22. 

•,.....: 

EPA M•THOD 26A 

.Determination of Hydrogen Fluoride Emissions 

Taylor" Clay Products 

Salisbury, Not• Carolina 

Limestone Scrubber Exhaust 

29,101 

159.4 

15,95 

0.091 

•lack Pressure, Absolute, in. Hg 

l• Pb,, + P• 

Volume Sampled at Stand. Cond., cu. ft. 

17.647 * VM * (Pb,, + AH / 13.6) 

Tu + 460 

Volume of Water Vapor at Std. Cond.,gCF 

Vwc 0.04709 * Vc 

Moisture Content of Gas Stream 

Vw• 

Vs• + Vwc 

l•eent Moisture in Stack 

100 * Vwc 

Vsvo + V• 

Mole Fraction of Dry Gas 

100 PMv 

I00 

Mole. Wt. Stack Gas, Dry Basis, lb/lb mole 

M• 0,44 * %CO• + 0.32 * %02+ 0.28 * (100 %COu %02) 

Mole. Wt. Stack Gas, Wet Basis, lb/Ib mole 

Ms Me * (1 Bw.) + 18.0 * B,•, -- 

Avg. Stack Velocity, ff/seo 

(Ts + 460) 

Vs 85.49 * Cp * APS * SQRT ............... 

(Ps * M,) 

Gas Volume Flow, Dry Std. Cond. CFM 

1058.82 * V.• * A * Ps * (I B,•) 

Ts + 460 

9.1 

0.909 

29.064 

28.057 

34,3 

13358 
FROM :TQYLOR CLR¥ FRX NO. :7046362413 San. 28 2@09 04:42PM P5 

EPA METHOD 26A 

Determination of Hydrogen Fluoride Emissions 

Taylor Clay Products 

Salisbury, North Carolina 

Limestone Scrabber Exhaust 

Gas Volume Flow, Dry Std. Cond. CFM 13358 13531 

Aotual Gas Volume Flow, CFM 24759 25237 

Gas Volume Flow, Wet Std. Cond., CFM 14694 I4931 

Sample Nozzle Diameter, inches 0.376 0.372 

13514 13467 

24982 24993 

14847 14824 

0.376 0,375 

A. Area of Nozzle, R • 0.00077 

I Percent Isokineti• 103.6 

:Hydrogen Fluoride Coneentratlon and Emission Rate 

Hydrogen Fluoride Catch, mg 149.8 

Hydrogen Fluoride Concentration, gr/dscf 0.0145 

Hydrogen Fluoride Concentration, gr/acf 0.0137 

Hydrogen Fltmride Emission Rate, lbs/hr 1.66 

i" 

0.00075 0.00077 0,00077 

101.5 102.1 102.4 

155.4 166.6 157.3 

0.0154 0.0161. 0.0154 

0.0148 0.0155 0.0147 

1.79 1.87 1.77 
FROM :TAYLOR CLAY FAX NO, :7046•6241• 5an. 28 2009 04:42PM P6 

SUMMARY OF RESULTS 

EPA METHOD 26A 

Determination of Hydrogma Fluoride Emissions 

Taylor Clay Products 

Salisbury, North Carolina 

Limestone Scrubber Exhaust 

i•.i! Signal Gas Volume Flow, CFM 

i';"• Vs * A * 60 

i!..'i•."• Volume Flow, Wet Std. Con&, CFM 

'?:•. Q,D* [1/(l-Bw,)] 

•" i' i:.•. 'i,,:.• of'Nozzle, f• 

0.0945 * (Ts + 460) * Vsvn 

Fluoride Concen•tion, •/dscf 

S•d•d Conditions) 

24759 

14694 

103.6 

0.0145 

0.0137 

1.66 
FROM :TRYLOR CLRY FRX NO. :7046362413 Zan, 28 2009 04:42PM P¥ 

Net Time of Test, minutes 

Barometric Pressure, in. Hg 

EPA METHOD 6C 

Determination of Sulfur Dioxide Emissions 

Taylor Clay Products 

Salisbury, North Carolina 

Limestone Scrubber Exhaust 

1 

07/11/00 

180.0 

29.12 

2 

07/12/00 

180.1 

29.15 

-0.019 

29,131 

161.82 

2.38 

80.5 

154.93 

340.4 

16.03 

0.094 

9.4 

0.906 

16.64 

2,58 

29.078 

28,040 

0.83 

0.477 

408.9 

34.9 

12.048 

%0= 

%C0• 

Ma 

Ms 

Cp 

APS 

A 

Static Pressure, in. Fig 

St/•ok Pressure, Absolute, in. Hg 

Actual Meter Volume Sampled, eu. ft. 

Avg. Delta I-I, in. I-lzO 

Avg. Gas Meter Temp., Deg. F 

Volume Sampled at Stand. Cond., eu. ft. 

Volume of Water Collected, ml 

Volume of Water Vapor at Std. Cond., SCF 

Moisture Content of Gas Stream 

Percent Moisture inGas Stream 

Mole. Fraction of Dry Gas 

Percent Oxygen, Dry 

Percent Carbon Dioxide, Dry 

Mole. Wt. Stack Gas, Dry Basis, llglb mole 

Mole. Wt. Stack Gas, Wet Basis, lb/lb mole 

Pitot Tube Constant 

Avg, Sqrt, Delta P, in. HaO 

Avg. Stack Temp., Deg. F 

Avg. Stack Velocity, R/see 

Area Stack, • 

-0.019 

29.101 

168.02 

2.55 

85,2 

159.39 

338.7 

15.95 

0.091 

9.1 

0.909 

16.63 

2.49 

29.064 

28.057 

0.84 

0.463 

405.3 

34.3 

12,048 

3 

07/12/00 

180.0 

29.18 

-0.019 

29.161 

165,82 

2.48 

80.8 

158.87 

332.8 

15,67 

0.090 

9.0 

0.910 

17.02 

2,34 

29.055 

28.063 

0.84 

0.468 

405.9 

34.6 

12.048 

Avg 

29.15 

-0.019 

29.131 

165.22 

2.47 

82.2 

157.73 

337.3 

15.88 

0.092 

9.2 

0.908 

16.76 

2.47 

29.066 

28,053 

0.84 

0.469 

406.7 

34.6 

12.048 
FROM :TAYLOR CLAY FAX NO. :7046362413 Jan. 28 2009 04:42PM P8 

EPA METI•, OD 6C 

Dotermination of Sulfur Dioxido Emissions 

Taylor Clay Produots 

Salisbury, North Carolina 

Limestone $¢rubbor Exhaust 

Qm Gas Volume Flow' Dry Std. Cond. CFM 

Q• Aotual Gas Volum© Flow, CFM 

Sulfur Dioxide Concentrations and Emission Rates 

Cm• SO• Concentration, ppm dry 

Cd SO2 Concentration, ibs/dsef 

CAw 802 Emission Rate, lbs/hr 

13358 13531 13514 13467 

24759 25237 24982 24993 

68.50 

0.000011 

9.11 

65.03 53.27 62.27 

0.000011 0.000009 0.000010 

8.76 7,17 8.35 
FROM :TAYLOR CLAY FAX NO. :7046•6241• San. 28 2009 04:4•PH Pg 

SOURCE DESCRIPTION 

Taylor Clay Products, hac. operates a brick manufactttring facility at 185 Peeler Road in Salisbury, North Carolina. The company has been .at, its current location for more than fifty years and has ff•ee natural gas-fired kilns that are utilized m drying product. A fourth kiln 

was recently built and brought on-line. Testing w•s conducted only on the new kilr• while burnin• a mixture of Petroleum coke and natural gas. 

Bdck Kiln #4 (ES-K4-rated at 16 mmBttVhr) utilize eomp_uter-eon_tro!!eaw_•,ab!e •,**,• *-•,,, 

draw flue gases from the tunnel to maintain a constant pressure in the firing zones. A limestone absorber treats the gases prior to exhausting to atmosphere through a baghouse and then a 26" round, vertical stack. Refer to the process sketch below. 

Absorber 

I. D. Yah Bagfilter 

w/ 2,800 

•q. ft. of 

filter area 

(CD-K4-2) 

Exhaus• ] St•ck 

The following table outlines process data tracked by STACLEAN employee Doug Ashbaugh. 

pro,,cess Data Summa Pa.ra, meter Run #1 •un #2 

Lime Inection Rate, gpm 

Temp. #1 inlet of Lime Injec.t!_o.n), F 

Temp. •2_. (Outlet of Lime Injection)• • 

Temp. #3 (Inlet of Baghouse), F 

Magnahelic (Duct pressure @ inlet to 

Lime Injection) in. H=O 

Baghouse Pressure Drop, in. H•O 

Fan Speed• Hz 

0.61 

327.7 

248.4 

249.1 

1 

3.72 

51.66 

0.62 

330.4 

251.7 

'2s0.s 

1.54 

3.71 

52.71 

R.,.u. n #3 

0.66 

327,3 

2•0.4 

248.4 

1 

3.68 

53.54 

Average0.63 

328.5 

Mr. Steven Rlankenbeker, Engineer for Taylor Clay was the facility liaison during emissions testing. Mr. Blankenbeker stated that during sampling the kiln was processing approximately 8,200 tons of green brick per hour (or 4,1 tons per hour) and that approximately 0.067 tons per 

hoar (1.6 tons per day) of peteoke was burned. 

ATC Project No. P-7132 Taylor Clay Kiln. ES-K4 Page 5 of 54 

52.64 

1.56 

3,70 

250.2 

249.$ 
FROM :TAYLOR CLAY FAX NO. :V046•6241• Jan. 28 2009 04:4•PM 

RESULTS SUMMARY 

SYSTEM Taylor Clay 

Lime Slurry System 

TEST DA TE 11/01/07 

PARAMETER R•l.Metsls R#2.Metals R#3.Metals A VERA QE 

GENERAL 

Q$• FLOW; ACFM 10,497 9,883 9,294 

Q STD DRY, FLOW $CFM 5,880 6,509 6,093 

%1 105.28 100.93 109.75 

9,891 

6,494 

QS, FLOW, ACFM 12,820 12,221 12,494 

Q STD DRY, PLOWSCFM 6,963 6,657 6,751 

%1 96.43 98.83 98.64 

12,512 

6,790 

Petcoke Firing Rata, ton•/hr 

Metals Emission Rate Summarv. 

PMRc (ibs/hr).As 1.31E-05 

Note: 1/2 of detection limit used for run• 2 and 3. 

Controlled Arsenic Emissions, Ib=/ton petcoke 

2.84E-06 2.61E-06 

0.067 

6.17E-06 

9.22E-05 

PMRc (Ib•/hr).Cd 4. t4E-06 1.82E•06 

Controlled Cadmium Emisalons• Iba/ton petcoke 

1.36E-05 2.44E-06 

3.64E-05 

PMR¢ (lt•thr)-Aa 1.07E-03 1.51E-03 1.34E-03 1.31E-03 

Uncontrolled Arsenic Emissions, Ibs/ton petcoke 

PMR•: (ib•hr).C.d 5.55E-06 7.34E-06 

Uncontrolled Cadmium Emissions, Ibs/ton petcoke 

7.79E-06 

1.95E-02 

6.90E-06 

1.03E-04 

Permitted Arsenic Emissions, Ibs/ton 6.58E-07 

Permitted Csdmlum Emissions, Ibs/•on 3.13E-06 

ATC Project No. P-7132 Taylor Clay Kiln E$-K4 Page 6 of 54 
FROM :TRYLOR CLRY FRX NO. :7046•6241• Jan. 28 2009 04:4•PM Pll 

SYSTEM 

TEST DATE 

PARAMETER 

RESULTS SUMMARY 

Taylor Clay 

Lime Slurry System 

11/01/07 

R#1.HCI/HF R#2.HCI/HF R#3-HCI/HF A VERA GE 

I le__j 

FLOW, ACFM 

O STD DRY, FLOW$CFM 

%1 

HCI/HF, .EmI•sion= 

PMRo (Ibs/hr)-HCl 

10,070 10,088 10,19t 

6,649 6,485 6,542 

102.13 100.55 103.34 

10,850 12,049 11,786 

5,954 6,471 6,357 

92.74 102.31 97,49 

2.83E-03 

Note: 1/2 of Run 2 ND used to celculate average 

PMRc (Ibs/hr).HF 4.481E-04 

Note: 1/2 of ND values used to calculate average 

PMRc (Ibs/hr).HCI 1,02E-01 

PMRc (Ibs/hr).HF 1,49E+00 

Destruction Efflclen.cv. % 

Hydrogen Chloride (HCI) 97=23% 

Hydrogen Fluoride (HI = ) 99.97% 

Reouired Destruct/onETflclencv..% 

7.38E-04 2,55E-03 

5.49E-04 4.981=-04 

1.05E.01 1.04E-01 

1.57E+00 1.23E+00 

99.30% 97.56% 

99.97% 99.96% 

10,116 

6•559 

11,562 

6,261 

2.04E-03 

4,•)8E-04 

1.04E-01 

t .43E÷00 

98,03% 

99,96% 

ATC Project No, P-7132 Taylor Clay Kiln ES-K4 Page 7 of 54 
FROM :TRYLOR CLAY FAX NO. :7046362413 San. 28 200• 04:44PM P12 

Results Summary of Gaseous Emissions Testing 

Client: 

Loc, atlon: 

Date: 

,•General Stack Parameters 

Run TimesTaylor Clay 

Salisbury, NC 

11101/07 

Lime Sorubbar Inlet 

Start 

End 

Sta•k Velocity, feet per second 

Aetual VolumetfiG Air Flow Rate, 

cubic feet per minute 

Stack moisture, percent 

Staek temperature, degrees F 

Standard Volumetri¢ Air Flow Rete, 

cubie feet per minute 

Oxygen Concentration, percent 

(corrected per 7e-5b) 

Carbon Dioxide concentration, percent 

(corrected per 7e-Sb) 

Measured Gase0u• Po!lutan • 

Sulfur Dioxide SO2, ppm vlv dry basls•correc=ted 

SO2, lbs/hr 

SO•, potential tons par year 

9:00 AM 

9:59 AM 

6.54 

429.3 

6,963 

17.21 

2.33 

332.02 

21.90 

95.92 

12:20 PM 

1:19 PM 

93.36 

12,221 

6.80 

424.2 

6,657 

16.68 

2.63 

339.96 

21.87 

95.79 

3:22 PM 

4:21 PM 

95.45 

12,494 

7.97 

420.3 

6,761 

16.58 

2.63 

341.62 

22.17 

97.10 

12,512 

7,10 

424,60 

6,790 

16.82 

2,63 

Averane 

337,87 

21,98 

96.27 

ATC Project No. P-7132 Taylor Clay Kiln ES-K4 Page 9 of 54 
FROM :TAYLOR CLAY FAX NO. :7046362413 3an. 28 2009 04:44PM 

Results Summary of Gaseous Emissions Testing 

Client:J Location:• 

Date: 

8our, ce: 

Parametem 

Taylor Clay 

Salisbury, NC 

11/01/07 

LIm•.$crubber Outlet 

9:00AM 

9:59 AM 

10:59 AM 

12:20 PM 

1:19 PM 

2:19 PM 

3:22 PM 

4:21 PM 

5:21 PM 

feet per second 45.52 45.60 46.07 

Air Flow Rate, 10,070 10,088 10,191 

45.73 

percent 

degrees F 

7.12 

266.4 

6,649 

Concent/'etion, percent 16.62 

7e-5b) 

eoncentretion, percent 2,68 

per 7e-Sb) 

Gaseous poli0tants 

v/v dry basts-corrected 215,22 

¢•s/hr 14.20 

potential tons per year 62,18 

Destruction/Removal Efficiency, % 35.18% 

9.37 

268.0 

6,485 

16,72 

2.54 

200.12 

12.87 

56.39 

41.13% 

9.72 

266.3 

6,542 

16.42 

2.66 

Run#3 

187.49 

12.17 

53.29 

45.12% 

8.74 

266,•}0 

6,S•9 

16.59 

2,63 

200,94 

13,08 

S7,29 

40.48% 

Removal Efficiency, % 

ATC Project No. P-7132 Taylor Clay Kiln ES-K4 Page 10 of 54 
FROM :TAYLOR CLAY FAX NO, :7046362413 Jan. 28 2009 04:45PM P14 

RESULTS, CONCLUSIONS AND COMMENTS 

Results from the destruction efficiency testing of the Lime Slurry Injection System are presented 

.• •he preceding test summaries. Additional information can be reviewed in the Caleulatlons and 

Aplxmdix sections of this report. 

Stack Profile-Inlet 

M¢•als Train 

.Slack velocities were measured at a mean 95.58 feet per second (Ft/s) with the metals sampling 

•nin. This yielded a mean actual volumetrle flow rate of 12,512 cubic feet per minute (acfrn). 

:Standardizing the volumetric flow for temperature, moisture and pressure yielded a mean value 

Of 6,790 cubic feet per minute (scfm). 

I•CH'IF Train 

.S•aek velocities were measured at a mean 88.33 feet per second (Ft/s) with the HCI/HF sampling 

•rain. This yielded a mean a6tual volumetric flow rate of 11,562 cubic feet per minute (acf_m). 

Startdardizing the volumetric flow for temperature, moisture and pressure yielded a mean value 

of 6,261 cubic feet per minute (scfm). 

_S•ck Pr•lrae-Outlet 

Metals Train 

Stack velocities were measured at a mean 44.71 feet per second (Ft/s) with the metals sampling 

train. This yielded a mean a•tual volumetric flow rate of 9,891 cubic feet per minute (aefm). 

Smndardizlng the volumetric flow for temperature, molsmre and pressure yielded a mean value 

of 6,494 cubic feet per minute (scfm). 

.FI.C1/HF Tr,•n 

Stack velocities were mcas•ed at a mean 45.73 feet per second (Ft/s) with the HCI/HF sampling 

L,-ain. This yielded a mean actual volumetric flow rate of I0,116 cubic feet per minute (acfm), 

Standardizing the volumetric flow for temperature, moisture and pressure yielded a mean value 

of 6,559 cubic feet per minute (scfm), 

Benzene Results 

Benzene mass rates were calculated utilizing the volumetric flow rates determined by the 

HC1/HF sampling trains for each loeatiort. Benzene was not detected on any sample, inlet or 

o•atlet. Therefore mass rates were calculated utilizing 1⁄2 of the detection limit of the an•alys{.s. 

.ATC Project No. P-7132 Taylor Clay Kiln ES-K4 Page 11 of 54 
FROM :TAYLOR CLAY FAX NO. :7046362413 Jan. 28 2009 04:45PM PI5 

RESULTS, CONCLUSIONS, AND COMMENTS 

(continued) 

yielded a mean benzene mass loading rate of <4,99e "•4 lbs/hr and a benzene emission rate of "•.220e • lbs/hr. Based on a petcoke usage rate of 0,07 tons/hour, the mean specific emission 

•¢•e of 7,77e "°3 lbs/hr is in compliance with the permitted allowable of 0.0303 lbs-benzene per i•: •n of petcoke burned. 

Hydrogen. chloride and hydrogen fluoride concentrations were detectably present in all inlet samples. The calculated mean mass loading rates were 1.43 lbs/hr of I-IF and 0,104 lbs/hr of HCI. HC1 concentrations were detectable on two oft.he three outlet samples. To calculate a 

mean estinaated emission rate, 1⁄2 of the detection limit was utilized for run two. This yielded 

mass HC1 emission rate of2,04e "°3 lbsMr yielding a removal efficiency of 98,03%, in corripliance with the required removal efficier•ey of 95%. 

Hydrogen fluoride concentrations were not detected in any of the outlet samples; therefore, emissions for each of the three runs were calculated utilizing 1⁄2 of the detection limit of HF, This yielded an estimated mass emission rate of4,98e -°• Ibs/hr and a removal efficiency of>99,96%, 

HF removal efficiency is also required to meet 95% as stipulated in the facility air permit. 

Metals Mass Rate•,, 

Arsenic and cadmium concentrations were determined on both the inlet/exhaust via US ]SPA 

method 29 sampling trains. Arsenic mass loading prior to the bagl•ouse was 1.3 le "°• lbs/hr. 

Arsenic was only detected ir• the outlet sample on run one; the arsenic mean mass emissions were 

calculated utilizing the mass rate of run one and the mass rates of runs two and three, which were 

calculated utilizing 1⁄2 the arsenic detection limit. The Kiln #4 arsenic emission rate of 6.16e "°6 

lbs/hr was slightly in excess oft he fuel-based emission standard of 6.5 8e -°7 ibs/hr. 

Cadmium inlet mass rates were a mean 6.90e "°• Ibs/hr compared to the exhaust rate of2,44e "°e 

lbs/b_r. Controlled emissions were less than the fuel-based emission standard of 3.13e -°e Ibsarsenic per hem', 

Sulfur Dioxide Mea•.urements 

Sulfur Dioxide (SO2) concentrations were measured continuously on the inle• and exhaust of the 

lime injection system. Inlet concentrations averaged 338 parts per million which yielded a mass 

loading rate of 21,98 lbs/hr and a potential uncontrolled emission of 96.3 tons per year. Exhaust 

concentrations averaged 200,94 parts per million yielding a controlled $O• emission rate of 13,08 

lbs/hr, The potential SO• emissions from. the #4 Kiln are projected at 57,29 tons. Removal 

effieiencies averaged 40.48%, less •an the permit-required efl'ieiency of 95%. 

ATC Project No, P-7132 Taylor Clay Kiln ES-K4 Page 12 of 54