the coking properties of coal at elevated pressures. - Argonne ...

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interchange systems and/or components. The original system has been expanded to include NO and Hydrocarbon measurements at the furnace outlet and CO measurement at in-bed znd freeboard locations. Table 1 Tabulation of Gas Sampling System Details Tank Fan Calibration Gases SO2, CO. 02, NO. C02. Air, and ti2 Instrument Air System 60 - 100 PSig (2 - 3 SCFM) G4S SAMPLE SYSTEMS SO2. CO. 02, NO,. and C02 Analyzers Hydrocarbon Analyzer C m n Tank Farm Commn lnstrwnt Air Supply Separate Sample Probes Separate Filter-Cyclone Assemblies Separate Heated Sample Lines Separate Filter-Pump Systems lnstrumnt Air to Pump Control Switch Cooling Water to Probes GAS SAMPLING SOURCE Approximate Source Gas Temperature Sample Gas Temperature @ Probe Discharge Sample Gas Temperature in Sample Line Sample Gas Temperature @ Pump Inlet Sample Gas Temperature After Analyzers Sample Gas Flow Fran Source Sample Gas to 02 Analyzers Instrument Air to 02 Analyzers Sample Gas to SO2. CO. and C02 Analyzers Sample Gas to NO, Analyzers Instrument Air to NOx Analyzers Recorder "A" Gas Printout Recorder "B" Gas Printout Furnace Outlet Probe Yes Yes Yes Yes Yes Yes Yes Yes 10 psig @ 1200 cclminute 20 gph maximum Stack (Furnace Out) ~ 900'F 31 0°F 300'F 180°F hbient (80OF) 5 literslminute 250 cclminute 10 psig 1000 cclminute 1200 cclminute 35 psig SO2. CO. 02, and to2 Mobile Probe Yes 110 Yes Yes Yes Yes Yes Yes 10 psig B 1200 cclminute 20 gph nmximum "In-Bed" and Freeboard 165OOF 310'F 300'F 180°F Ambient (80'F) 5 literslminute 250 cclminute 10 psig 1000 cclminute 1200 cclminute 35 psig SO2. CO, 02, and NOx I
GAS SAMPLING WITH ORIGINAL PROBE-FILTER ASSEMBLIES Furnace Outlet Gas Sample Location The gas analysis from the furnace outlet is used in performance calculations and additionally to set and control the facility test conditions. This system must operate on a continuous basis. Figures 4 and 5, respectively, show the probe installation in the furnace outlet duct and the original probe-filter assembly. The water-cooled probe has an open-ended, concentric quartz tube for sample flow. In turn, the tube is connected to an in-line particulate filter assembly (glass cyclone collectorfdrop out bottle and frit-fiberglass filter unit) through which the gas sample flows enroute to the heated sample line. The particulate filter assembly, located in an electrically-heated cyclone oven (size - 9-1/2 inches square x 21-1/2 inches long), is maintained at 30OOF. At normal operating conditions (no dust recycle), the particulate filter assembly had to be changed twice during each 24-hour operating period. Freeboard Sample Locations The mobile gas sampling system and probe installation shown in Figure 6 are used to traverse the freeboard at the locations previously shown in Figure 2. A typical traverse at one location would include taking gas samples at 12 or 13 points across the width of the facility. A complete traverse, conducted with the drive mechanism on either "hand mode" or "automatic mode", requires from 60 to 90 minutes to complete. Except for the difference in length, the furnace outlet and mobile probe-filter assemblies are identical. In-Bed Sampling Locations The in-bed gas sampling probe installation, shown in Figure 7, is used for traversing in the fluidized bed. The original in-bed probe-filter assembly is shown in Figure 8. The filters are 3/4 inches in diameter x 1-3/4 inches long with a pore size of approximately 1 micron. The ceramic collar is cemented to the filter at a position that is 1/4 inch away from the open end. The collar is clamped in the probe head at a location that presents an active filter flow area of approximately 2 square inches. Typically, the ceramic filter had to be cleaned (nitrogen back-purged) at 15- to 20-minute intervals. GAS SAMPLING PROBLEMS The original gas sampling probes operated satisfactory and allowed accurate gas concentration measurements during no dust recycle test conditions. However, operation of the 6' x 6' AFBC unit has shifted to the use of dust recycle to improve performance. Uust loadings as high as 10,000 lb/hr have been run at temperatures up to 1750'F and at gas velocities of about 100 ftfsec. The high dust recycle increased the particulates that were entrained in the gas samples. This condition necessitated frequent filter changes, caused problems with glassware breakage due to increased handling, and required more frequent nitrogen back-purging of the in-bed filter. Problems associated with gas sampling at the furnace outlet, freeboard, and in-bed locations are discussed in the following paragraphs. 211
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I / The Coking Properties of Coal a
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Procedure : Hand picked lunips of c
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Apparatus: The equipment for this t
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the total pressure on the swelling
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A comparison of the results obtaine
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was used, however, general trends a
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1 D 13 3 G
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Table 8 L_ Effect os FaeO Compo.lrl
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i-l SPARE SAblPLE Plortlc 209 Figur
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- z c 100,000 50,000 10,000 0 n 5,0
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Flnure 9 SWELLltlG PROPERTIES OF PI
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Fi ure 13 EFFECT OF TOTAL PRESSQRE,
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TABLE 1. OPERATING CONDITIONS Opera
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1. . 2. 3. 4. 5. 6. 7. 8. 9. REFERE
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Figure 4. SCANNING ELECTRON MICROGR
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Turkgodan et al. (18) studied the p
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Materidl balance on packed bed Boun
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These phenomena iiiay be described
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Walker, P. L., Rusinko, F., and Aus
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-""I- *I,".. I Dlrf".,on Co.1flcl.n
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After a variable residence time, th
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Changes in Char Chemistry The infra
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20. 21. 22. 23. 24. 25. 26. 27. 28.
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0s-a 00-a OS'S 00-E os-2 00-2 02.1
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COAL PYROLYSIS AT HIGH TEMPERATURES
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actions, decreasing the secondary c
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01 40 60 TI MEISeC) 80 100 120 140
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Reaction Temperature OC In-situ Ini
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and the gas velocity is often repre
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The mathematical model developed he
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si sio Fraction of solid species i
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Table 2. Differential Equations Mod
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1 60 I I RUN KE-5 50 T.1121K(1557'F
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to condense excess steam, the press
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conversion-time data.* The integrat
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catalyzed and uncatalyzed runs were
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CATALYTIC EFFECTS OF ALKALI METAL S
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%me thermogravimetric measurements
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than in steam. Figure 9 shows data
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C - C02 REACTION C - H20 REACTION L
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1. 2. 3. 4. 5. 6. 7. 8. 9. 10. 11.
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n 'm L u. t m - L 84
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i 5360-096bw \ KINETICS OF POTASSIU
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t 5360-096pj There is an interactio
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1 I > \ i I 5360-096bw bed data. Be
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I 1. I 5360-096bw ranging from atmo
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uY.ku ICHlMAlIC OF MINI-FLUID BE0 R
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800-12-1133 -9 FIGURE IO CALCULATED
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Mexico coal. Table 1 shows an analy
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', Complete results from all runs c
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I the methanol down to atmospheric
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TABLE 3 -----______________________
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\ "I N z 107 c. . 0 0
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I. INTRODUCTION DIRECT METHANATION
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The catalyst development program fo
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Preparing process flow diagrams and
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\ \ i 1. 2,000 4,000 6,000 8,000 10
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(JMS-OlBM-2). The mass spectra were
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I I Fairbridge, R.W. (ed.) 1972, En
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v- W V z d 3 z m 4 ? P m W c3 W m N
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e. \ I , W 2 m 4 t- CI 99-79 noooo
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L Table I: Compositions of High Tem
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\ " \ I For all three coals, the pr
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4 , 1024 1024 3a 3b J Mineral Parti
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The Determination of Mineral Distri
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pyrite crystals in framboids locate
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FIG. 1. TEM MICROGRAPH OF A HIGH VO
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\ \ FIG. 5. SEM MICROGRAPH SHOWING
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\ , species. In fact, combustion ex
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1, It is possible to make a reasona
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\ i SURFACE AND BULK ENRICHMENT OF
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I Coal Ash Sintering Model and the
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5 carried out such sintering measur
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I this ash and other bituminous coa
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forming propensity. However, none o
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t I 153
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CENTRAL ELECTRICIN RESEARCH LABORAT
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157 18 I I a I
Page 159 and 160: temperature, sulfur species concent
Page 161 and 162: The facility is fired with coal usi
Page 163 and 164: Tests have been carried out to dete
Page 165 and 166: under which conditions sulfur speci
Page 167 and 168: I TITANIUM L Corn AS A TRACER FOR D
Page 169 and 170: E 6 i i h \ 1 1 \ on the XRF is cau
Page 171 and 172: \ ? CONCLUSIONS Titanium can accura
Page 173 and 174: NY) m * oa
Page 175 and 176: GFETC constructed a 0.2 square mete
Page 177 and 178: \: Stage 3. Sulfated ash-cemented a
Page 179 and 180: I FIG. 1. Initial ash coating on qu
Page 181 and 182: FIG 9. Limestone bed material alter
Page 183 and 184: (4) Since the operating temperature
Page 185 and 186: I I maximum particle diameter leavi
Page 187 and 188: ! suspension chambers and cyclone f
Page 189 and 190: Pilot Plant of a Coal Fired Fluidiz
Page 191 and 192: After the fiscal year 1982, the fol
Page 193 and 194: MBC CBC Fig. 1 Boiler Structure 193
Page 195 and 196: \ i Table 2. Coal Properties Planne
Page 197 and 198: -2- more than 3 years, since 1977.
Page 199 and 200: , I B. 2 which temporarily raised t
Page 201 and 202: -6- abrasion rate at the bottom of
Page 203 and 204: \if F3.3 - Particulate Circulation
Page 205 and 206: \' I/O. analog 1/13. industrial I/O
Page 207 and 208: ACQUISITION DATA UNIT < I L- J (T)
Page 209: SAMPLING SYSTEM FOR FLUIDIZED BED A
Page 213 and 214: Remove the quartz tube (gas sample
Page 215 and 216: ' ' The modifications have been com
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Page 219 and 220: With regard to the similarity parti
Page 221 and 222: i \ ' 2.2. soz Emission and NOx Emi
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Page 225 and 226: Figure 9: Sulphur captLTre as 0 fun
Page 227 and 228: P SUMMARY OF TESTS Testing complete
Page 229 and 230: I Table 1 Comparison of Sulfur Capt
Page 231 and 232: , NITROGEN OXIDE REDUCTION Single-S
Page 233 and 234: 0 The addition of air at the 96-inc
Page 235 and 236: m- Y i? 4: BO n 8 c Y l0- Bo- I I I
Page 237 and 238: E! w 2 z e Y 100 - 3 t 5 80- 0, 40
Page 239 and 240: 0 f 0.so o'm: 0.300 0.zo - - A 5m 4
Page 241 and 242: &e- -A \ \ \ : ERCENT OVERBED AIR I
Page 243 and 244: PARTICLE ENTRAINMENT AND NITRIC OXI
Page 245 and 246: i 1' 1 ! I. i Chaung (15) showed th
Page 247 and 248: The maximum height that a large par
Page 249 and 250: 3.0 Nitric Oxide Reduction in the F
Page 251 and 252: assumed to be identical to that of
Page 253 and 254: Nomenclature A *t cD ‘NO $3 _ _ _
Page 255 and 256: TABLE 2. OPERATING CONDITIONS AND E
Page 257 and 258: i 1 \ ', References 1. 2. ( 3. 1 4.
Page 259 and 260: \ ” Y) I 259
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t I 100 - - I I ] , I , I , I 'ii 9
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Feeding of the carbonaceous materia
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! Table 2 Proximate and ultimate an
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lb, , --pp---p-- 4 p? CHAR 1 Tu-IWO
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I CHAR Y Y /I TIME O i ' ' ' ' 1 '
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could not be assumed constant. Thus
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\ greatly acknowledged. Literature
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constructed and operated to demonst
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The experimental procedure for the
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atmospheric pressure fluidized bed
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1' TABLE 2 Screen Analysis of Sand
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n RECORDER I Ill I ’ NO. NOX THER
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\ 285 Y 0 I- 5 B 5 3 m "9 E5 3 uz 0
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CHAR1 TOC 0.85 M3/k 600 0 700 V 750
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f Durin all the experimental runs t
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Assuming that large coal particles
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i 7 -_ 0 m\o --n 0 W i 293 a\o 0
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The influence of particle size dist
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all the initial values of x for whi
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\ - + 1) x. = 1 bL/n YO Defining di
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$ m. 1 Results and Discussion Evalu
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kl k2 k' KC KD m m. m P N P R R g t
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UNBURNT FRACTION UNBURNT FRACTION m
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