The estimated annualized costs for SCR systems on the eight model plants are shown in Table 6-15. These include operating labor and maintenance costs, capital recovery, gas reheating, ammonia reagent, and catalyst replacement costs. The individual operating costs were obtained by appropriately scaling the vendor provided operating costs19,20 to the model plants. The total annualized costs ranged <strong>from</strong> $2.5 million/yr for the small long dry kiln to $7.2 million for the large precalciner kiln. 6-50
TABLE 6-15. ANNUALIZED COSTS FOR SCR Total annualized costs Capital recovery ($/yr) Taxes insurance admin. ($/yr) Catalyst costs ($/yr) Energy and fuel costs (103 $/yr) Maintenance and overhead costs ($/yr) Ammonia reagent costs ($/yr) Operating labor costs ($/yr) <strong>NOx</strong> emissions (lb/hr) Kiln capacity (tons clinker/ hr) Kiln type 3 (10 $/yr) Model no. 30 290 30,400 287,000 48,700 468 326,000 511,000 1,680,000 3,350 1 Long wet 50 490 30,400 485,000 48,700 779 544,000 694,000 2,280,000 4,860 2 Long wet 25 220 30,000 218,000 48,700 304 212,000 395,000 1,300,000 2,510 3 Long dry 6-51 40 340 30,400 337,000 48,700 487 339,000 523,000 1,720,000 3,490 4 Long dry 40 240 30,400 238,000 48,700 421 293,000 480,000 1,580,000 3,090 5 Preheater 70 410 30,400 406,000 48,700 736 513,000 571,000 2,210,000 4,610 6 Preheater 100 340 30,400 337,000 48,700 930 649,000 772,000 2,540,000 5,300 7 Precalciner 150 510 30,400 505,000 48,700 1,400 974,000 985,000 3,240,000 7,180 8 Precalciner
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EPA-453/R-94-004 ALTERNATIVE CONTRO
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ALTERNATIVE CONTROL TECHNOLOGY DOCU
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Chapter Page 4.1 MECHANISMS OF NO F
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TABLE OF CONTENTS (con.) Chapter Pa
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LIST OF TABLES Number Page 2-1 UNCO
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CHAPTER 1 INTRODUCTION Congress, in
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CHAPTER 2 SUMMARY This chapter pres
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2.2 NO EMISSION CONTROL TECHNOLOGIE
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TABLE 2-2. ACHIEVABLE NO REDUCTIONS
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TABLE 2-4. CAPITAL AND ANNUAL COSTS
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TABLE 2-5. COST EFFECTIVENESS OF NO
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eductions ranged from 470 tons/year
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CHAPTER 3 INDUSTRY DESCRIPTION 3.1
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Type II. Moderate-heat-of-hardening
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3 a TABLE 3-2. UNITED STATES CEMENT
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Figure 3-1. U.S. Portland cement pl
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Table 3-3. (con.) Rank Clinker 3 (1
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5 cement processes: wet process and
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Figure 3-3. New technology in dry-p
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substantial levels of silica and al
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are achieved by clinker coolers of
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126,000 to 963,000 tons/year with a
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such as crushing and grinding opera
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4.1.1 Thermal NO Formation x Therma
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temperatures are on the order of 16
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4-6
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expected to produce more fuel NO th
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introduce a large proportion of com
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will also mean a somewhat lower sec
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ILC systems: In these systems, the
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which indicates an average and the
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4-18
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Uncontrolled NO x emissions Plant c
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from 2 to 9 lb/ton of clinker, and
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Capacity Heat in NO x emissions Met
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TABLE 4-3. (con.) Capacity Heat in
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TABLE 4-3. (con.) Capacity Heat in
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TABLE 4-3. (con.) Capacity Heat in
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in estimating uncontrolled and cont
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13. Letter from Sheridan, S.E., to
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44. Chemecology Corporation Source.
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73. Letter and attachments from Smi
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NO control approaches applicable to
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5.1.2.2 Kiln Fuel Changing the prim
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oxygen content of the primary air m
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tend to recirculate hot combustion
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e about 15 to 38 percent depending
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combustion system shown in Figure 5
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5-14
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Figure 5-3. Schematic of hazardous
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5-18
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higher than typical cement kiln flu
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window is in the middle of a kiln.
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Figure 5-4. Application of the sele
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in Section 5.1.2 is usually difficu
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5.4 REFERENCES 1. Helmuth, R.A., F.
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