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- 199 -
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CUMULATIVE SOLIDS AND SULPHUR BALANCES
A comprehensive solids and sulphur balance check was made for
all runs. Where silicon carbide was involved, both spent lime and
silicon carbide balances were checked. The sulphur, spent lime,
and silicon carbide recovery was in the region of 85-90$* 90$, and
95-100$ respectively.
An illustration of the approach used in the cumulative solids
and sulphur balances is given in Tables D.XII to D.XIV, based on data
for sulphation run no. 10.
- 200 -
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- 203 -
-------
APPENDIX E
PILOT PLANT MODIFICATIONS
Page
Modifications prior to Run 8 205
General
Gasifier
The bottom P.O. injector
Gasifier lid
Regenerator
Cyclones
Cyclone drains and fines return
Steam
Duct and burner
Various
Modifications prior to Run 9 208
Gasifier
Gasifier lid
Regenerator
Cyclones and fines return
Steam/Nitrogen
Various
Pre-run explosion repairs
- 204 -
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PILOT PLANT MODIFICATIONS
To extend the range of operating conditions (e.g. higher bed velocity,
deeper bed, etc.) considerable modifications were carried out before runs
8 and 9« Moreover, runs 5* 6 and 7 had pinpointed several areas of
unreliability of the peripheral equipment while our growing experience
had pointed to several potential improvements.
Modifications prior to Run 8
General -
The monolith block was raised 10" (25 cm) to improve access to the plenums
and to allow more up and down movement to the bottom injector. An extra
36 inches (91 cm) of refractory was added to the top of the monolith block
to allow an operation with deeper beds without flooding the cyclones with
stone.
Gasifier -
2
The gasifier bed area was reduced from 4.50 sq. ft. (0.42 m ) to 3.28 sq. ft.
(0.30 m ) by the addition of 5 sleeving blocks in the right hand side of the
gasifier cavity. The blocks were keyed to each other and held back by
stainless steel bars through the right hand gasifier wall. The second
block from the bottom was cast from C1850 refractory while the remainder were
cast in C1600: this arrangement served as a comparison of the relative
merits of the two refractories. The addition of the blocks reduced the
internal dimensions of the gasifier cavity to 17.5 inches x 27 inches &4,5 cm
x 68.5 cm) at the bottom and 19.5 inches x 28 inches (49.5 cm x 71 cm) in
the parallel portion from the original dimensions of 17-5 inches x 37 inches
(*4,5 cm x 94 cm) and 19.5 inches x 39 inches (49.5 cm x 99 cm) respectively.
As a consequence of this change of dimension: the gasifier thermocouples were
lengthened and relocated (they passed through the sleeving blocks) in order to
measure temperatures at the same depths as in the previous runs, the right
hand fuel oil injector was blanked off and the air distributor was fitted with
24 nozzles instead of 32 used previously. The air nozzles were of the same
design as used in runs 6 and 7 but the orifices were bored out to give a cold
air flow of 260 s.f.c.m. at 10 inches,w.g. (440 m'/h at 2.5 kPa) instead of
350 s.c.f.m. at 15 inches w.g. (590 rrr/h at 3.75 kPa) in the run 7
configuration. These changes were a compromise solution to provide reasonable
performance at both 4 and 6 ft/sec. (1.22 to 1.83 m/sec.) bed velocity and at
both high and low bed depths. The position of the fines return to the
gasifier was changed to inject fines into the gasifier to regenerator
transfer pocket; the fines return duct was lined with a f" T.D. silicon
carbide pipe and nitrogen was used to transfer the fines.
- 205 -
-------
The bottom P.O. injector -
The bottom fuel oil injector was placed centrally in the bottom of the
gasifier bed and had six horizontal holes, '/64" dia. (2.8 mm) equally
spread around the circumference at the hot end and could be moved up and
down about 20 inches (6l cm). The bottom injector was piped in to take
oil or kerosene from one, two or three pumps and in addition, the oil to it
could be by-passed through a Kemix mixer which could also be fed with up to
45 I.gal./hr (204 litres/hr) of warm water. This arrangement was intended
to try water (in an oil/water emulsion form) as a process temperature
moderator and to compare it with flue gas recycle.
Gasifier lid -
The gasifier lid was modified to fit the new gasifier geometry. It was
also provided with 5 new penetrations: four of these were for 1 /l6" (27
mm) Firebird Blue tubes, with their bottom ends sealed and 1" deep x l80°
cut-outs in their sides, for injecting air under the lid, and the fifth one
for inserting a silicon carbide sample tube, through a nitrogen purged lock
chamber, into the gasifier top space to determine the rate of deposition of
carbon at the cyclone entry.
Regenerator -
The top 36" of the regenerator was cast in ClS^O refractory, it was
also made wider i.e. 11" for 17" (28 cm for 4 3 cm) to reduce the fines removal
from the regenerator. The regenerator distributor was modified to
include a stainless steel coned top with a central drain coming out through
the bottom of the regenerator air pipe, to facilitate easy removal of the
regenerator bed.
Cyclones -
In raising the gasifier top level 36" (91 cm) an opportunity was taken to re-
cast the gasifier cyclones in Durax C1850 high alumina refractory. The
design of the cyclones themselves remained identical but the cyclone inlets
were siamesed and provided with trumpet bell inlets. Because the gasifier
cavity had been partly closed off, the cyclone entries (being symmetrically
arranged in the original wall) were offset to one side. The cyclone drains
were both arranged straight through with no internal connections to transfer
passages. The seals were effected by lining the relevant parts of the cyclone
drain legs with 2" I.D. (5 cm) silicon carbide pipes.
Cyclone drains and fines return -
Both cyclones were drained externally with no internal connections. Since
the pneumatic logic control systems caused many problems during the previous
test run, they were replaced by two electro-pneumatic control systems in which
- 206 -
-------
the sequencing was done by electric timers and pressure switches which,
in turn, caused solenoid valves to trip and pressurise the appropriate
actuator connections. The only portions of the pneumatic logic which
were retained were the two knife oscillators: these were arrangements of
five pneumatic miniature valves which provided a pulsed 80 psig (55^ kPa)
output when energised by a steady 80 psig input. The actual arrangement
of the cyclone drain and fines return system were as follows: the
vertical cyclone drain leg terminated at the lower end in a if inch (38 mm)
plug valve with a double acting air cylinder activator. Below the plug
valve was a conical pressure vessel (fitted with a chunk trap) at the
bottom of which was the fines off-take pipe fitted with gas knife
connections. The if inch (jS mm) fines off-take pipe led vertically up to
well above the top of the gasifier where it terminated in a if inch (J58 mm)
ball valve with graphite seats and a double acting air activator. This
terminated the solids lift system. Downstream of the ball valve the two
pipes (from the two cyclone drains) discharged into an inclined hopper which
fed an elutriator. Pines from the top of the elutriator passed to a bag
filter while the coarser material passed down through a plug valve and
a flow limiting restrictor to an injector into the gasifier. The plug valve
was air activated and set to open when the head of solids above it exceeded
an adjustable pre-set height.
Steam -
Steam was connected, through a meter, to the plenum and also to a 2 inch
(50 mm) pipe in the upper part of the left hand wall of the gasifier.
Injection of steam into the plenum was intended to allow a comparison of
steam, as a gasifier temperature moderator, with recycled flue gas and with
water in the fuel oil/water emulsion. Provision of steam injection into the
upper part of the gasifier was for an attempt on an on-stream steam/air burn
out of carbon deposited in the cyclone inlets and cyclones.
Duct and burner -
The cyclone off-take and gas duct was of the same basic design as used
previously with swept bends and Durax C1600 refractory lining enclosed with
calcium silicate slab insulation within a square steel casing. The actual
geometry was modified to conform with the changes in configuration of the unit.
The burner premix section has been shortened by 2 inches (50 mm) also to
conform with the changes in the geometry of the unit.
Vari ous -
The shooter which was used to test the effect of shooting stone at cyclone
inlets was removed from the unit. A high water level alarm was
installed on the flue gas recycle scrubber.
A provision was made to inject a controlled and measured rate of SO
- 207 -
-------
into various parts of the plant to check out the sampling systems.
Modifications prior to Run 9
Gasifier -
The top sleeving block was removed and the second one down was recast with
the top sloping at 45°. The top part of the gasifier cavity was thus
expanded back to its original width of 39 inches (99 cm) and cyclone inlets
were once again symmetrically disposed in the gasifier back wall.
Gasifier lid -
The gasifier lid was re-cast to conform with the dimensions of the top of
the gasifier cavity. It was fitted with 6 air injectors (of the same type
as in run 8) capable of injecting a total of 53 s.c.f.m. (1500 litres/min)
of air just under the gasifier lid. The actual air flow was measured with
a low pressure drop rotameter.
Regenerator -
The regenerator design remained the same as in run 8.
Cyclones and fines return -
The cyclones remained unchanged but the fines return system had several small
but important modifications: at the bottom of the cyclone drain two valves
were installed in series (a butterfly valve and a plug valve) both 1-| inches
(38 mm), with a vent controlled by a -| inch (12 mm) valve between them. All
three were pneumatically operated. The operating sequence was: the butterfly
valve closed, then after a few seconds' delay the plug valve closed and the
pressurisation sequence started to transfer the fines, then the plug valve and
the vent valve opened, the vent valve shut and, last, after a few seconds'
delay, the butterfly valve open. This sequence was intended to ensure a good
seal at the bottom of the cyclone during the fines transfer, actuation of the
plug valve with no solids load and avoidance of intermittent puffs of gas in
the cyclone drain. The unreliable pneumatic knife pulsers were replaced by
electric pulse generators and solenoid valves. At the bottom of the
elutriator the flow limiting restrictor was replaced by a pulsed solids flow
controller in which the downward flow of solids was prevented by a flat plate
and initiated by pulses of nitrogen directed across the plate.
Steam/nitrogen -
Steam connections to the plenum and side of the gasifier were retained for
this run and, in addition, nitrogen was connected to the 2 inch (50 mm)
steam pipe in the upper part of the left hand side of the gasifier. This
- 208 -
-------
connection, in conjunction with the large volume of air injection through
the lid allowed another attempt on an on-stream steam/air or nitrogen/air
burn-out of carbon. An addition of a small bleed of nitrogen to the
plenum and the above provisions made it possible to attempt slumped bed
burn-outs using steam/air, nitrogen/air or flue gas/air and without
sulphating the gasifier bed.
Various -
The Kemix mixer for providing an emulsion of fuel oil and water was
disconnected for this run.
Sight glasses were installed over the cyclone offtakes and over the
gasifier.
Provisions were made for the injection of S0? and H_S into the gasifier.
Boiler gas sampling probe was installed in parallel with the existing
sampling system and a refrigerator was installed to cool the sample rapidly
and to condense out the water so that a dry gas sample was pumped to the
analysers in the control room.
Pre-run explosion repairs -
Just before the start of Run 9 a propane/air explosion inside the gasifier
blew off the lid and caused some minor damage to the refractory. The lid
was repaired with Durax C1600 refractory and the gasifier refractory
cracks were sealed with Sairset. None of the unit modifications or main
features were affected.
- 209 -
-------
APPENDIX F
CAPS RUN 8
Operational Log, Inspection & Dfta
Page
Summary of Operational Log, Run 8 2D1
Inspection, Run 8 218
Figures F-l to F-l? 223
Table I Temperatures and Feed Rates 234
Table II Gas Flow Rates 246
Table III Pressures 2^8
Table IV Desulphurisation Performance 270
Table V Gas Compositions 282
Table VT Sulphur and Stone Cumulative Balance 297
Table VII Solids Removed (Raw Data) 312
Table VIII Solids Removed (Analysis for Total Carbon) 322
Table IX Solids Removed (Analysis for Sulphate Sulphur) 32*
Table X Solids Removed (Analysis for Total Sulphur) 326
Table XI Sieve Analyses : Gasifier, Regenerator & Elutriator 32°
Fig. F-l8 Chronological Plot of Unit Performance 33T
Fig. F-l9 Chronological Plot of Gas Space Pressure 339
- 210 -
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SUMMARY OF OPERATIONAL LOG, RUN 8
25.5.74 to 30.5.74 (Unit Warm Up)
Warm up of the unit started at 16.00 on 25.5.74. and initially
the temperature was held around 100°C for six hours to allow new
concrete to gently dry out. Thereafter the temperature was raised
progressively by about 10°C per hour until 500°C, held at this
temperature for six hours, and then increased again at the same rate.
Kerosine was added at 06.00 on 29-5.74. and limestone addition
began at 19-35. This was switched over to fuel oil combustion some
thirty minutes before gasification at 02.55 on 31.5.74.
Throughout the period of warm up the usual minor teething
problems occurred, in particular several start-up burner flame outs
due to condensation of water on the flame fire-eye. This
highlighted the need for Np purges to the fire-eyes to prevent
condensation.
31.5.74 (Day 1 of Gasification)
Successful start-up on gasification leading to only a few minor
problems relating to the cyclone drain system and a leak in the
gasif ier lid.
Main effort of the day was concentrated on ensuring correct
calibration and operation of the analytical equipment. The flue
gas C02 meter was found to be unreliable, and the regenerator S02
meter initially appeared to need recalibration but was later found to
be faulty and replaced.
The R.H. cyclone fines return system gave some problems during
the day, but these were ironed out by the evening.
1.6.74 (Day 2)
More teething problems were encountered on the second day of
gasification. Particularly troublesome were the cyclone drain
systems which continually blocked throughout the day. The problem
- 211 -
-------
seemed to be that with relatively deep beds (-^-90-100 cm) and high
fluidising velocities (^l.J m/sec.) a large amount of material was
carried over into the cyclones and the fines return system failed to
cope. '
Some problems with the Wostoff SC>2 meter and regenerator/gasifier
A P control valve were overcome, and leaks in the propane line to
warm-up burner were identified and cured.
2.6.74 (Day 3)
Initially the system was operated at high bed velocity
(-«~1.4 m/sec.) and molar stone feed rate, but bed depth could not be
maintained and it was evident that a lot of fines was going over to
the back of the boiler. Bed depth stabilised at about 75 cm. The
fines return systems were overworked and prone to failure.
The desired condition of high bed velocity and a deep bed seemed
unattainable and attempts were made to build bed depth at lower bed
velocities.
3.6.74 (Day 4)
Early in the day a flow check of the fines return system was
carried out. At a mean cyclone temperature of approximately 410°C
about 42 kg/hour of material was calculated to be circulating.
Another day of continual problems from the fines return system.
4.6.74 (Day 3)
A comparatively quiet morning was interrupted by a power failure
at 09.12 which caused automatic shutdown of the unit. Gasification
recommenced at 09-53.
In all an uneventful day with much less trouble from the fines
return system. Generally the performance of the unit in terms of
% SRE seemed worse than in previous runs. Major differences in
operation identified were:-
• Low stone feed.
• High regenerator air rate
- 212 -
-------
• Higher gasifier temperature
It was decided to return to a molar stone feed rate and reduce
gasifier temperature.
5.6.74 (Day 6)
Repairs to the cyclone drain control equipment were carried
out and the stone feed system was cleaned out. The improved
performance of the stone vibrator after cleaning resulted in a short
period of extremely high stone addition (Ca/S mole ratio—-15). This
was reflected in a drop in gasifier temperature. Pilot flame failure
occurred due to a dirty fire-eye.
Poor regenerator performance was experienced throughout the day.
A low regenerator air rate was set and a high C0? and low SCL off
gas was obtained. Poor 0_ utilisation in the regenerator was
improved by deepening the Bed.
6.6.74 (Day 7)
Quiet morning with the unit operating well until the RH cyclone
blocked and the pilot flame failed more or less simultaneously.
A silicone carbide probe was inserted in gasifier lid tapping
(weight 104 grams), removed after four hours and found to be partly
covered with a layer of carbon (weight of carbon ^\,1.2g) which readily
flaked off. The object of the test was to try to measure the rate
of iay down of coke above the bed, but some of the carbon had obviously
been removed while extracting the probe, and this method was deemed
unsatisfactory.
Tests with steam injection to the plenum air were started at
16.56 and continued till shortly after midnight. The flue gas rate
was decreased to compensate for the drop in gasifier temperature.
The immediate effect of steam injection was a considerable drop in
desulphurising performance.
7.6.74 (Day 8)
Usual problems of cyclone, stone feed hopper and regenerator
sampling line blockages. Otherwise uneventful.
- 213 -
-------
8.6.74 (Day 9)
The stone feed system was particularly troublesome on this day
with fine material blocking the vibrator. At one stage a large
amount of this fine material was added to the gasifier causing a drop
in gasifier temperature by 25°C and a considerable improvement in
% SHE. More problems were experienced with the fine control system
hardware.
The gas space pressure was now high, and a steam/air burn out
was attempted by injecting above the bed while still gasifying. After
several hours no obvious benefit was indicated by this approach and a
switch was made to the conventional sulphation and slumped bed decoke.
9.6.74 (Day 10)
After the sulphation and slumped bed decoke the unit was
re-started on kerosine at 07-00 to raise bed temperature. The cyclone
chunk traps were drained and large pieces of coke removed. The boiler
was inspected and several rows of tubes were found to be solidly blocked
with deposits, and these were removed.
Later the KH cyclone drain activator became faulty causing a
blockage in the system. This was replaced and the unit shut down
to rod out the cyclones and again clean the chunk traps.
Further troubles with the cyclone drain system were ironed out
and gasification was started at 22.00.
10.6.74 (Day 11)
At 07.30 the fuel supply was switched to a new tank and this
apparently caused a pressure rise in the centre fuel pump sufficient
to activate the relief valve starving the unit of fuel. Bed
temperature increased rapidly followed by flame out and an emergency
shut down.
At this point contact with the fuel storage depot revealed that
a leak in a steam coil had caused their fuel delivery to us to be
heavily contaminated with water. A quick analysis of the fuel supply
indicated that about 10 wt.$ water contamination was present. Later
analysis indicated more than 25 wt.$ contamination.
- 214 -
-------
11.6.74 (Day 12)
At 00.30 an attempt to gasify failed due to the re-occurrence
of high pressure on centre fuel pump. A switch to the LH fuel pump
resulted in a successful start-up on gasification at 02.00.
More evidence of water contamination came from the fact that a
high oxygen content in the flue gas was obtained while operating at
an apparently high fuel rate. Furthermore copious amounts of water
vapour was coming from the stack. The carbon level on the stone
was also low due to the presence of water. Indeed a gasifier bed
sample taken at this time showed the stone almost completely white.
Poor regenerator performance was evident throughout this period.
Detailed analysis of the fuel oil used over the period
indicated nearly 28 wt.$ water contamination. A change to another
supply tank was made which reduced the contamination level to 10 wt.
12.6.74 (Day
A switch to another supply tank at 02.45 resulted in an increase
in flue gas oxygen level, and indicated this new supply was also
heavily water contaminated.
This time it was obvious that water contamination had a
considerably adverse effect on desulphurising performance. Meanwhile
arrangements were in hand to obtain fuel supplies free from water
contamination .
13.6.74 (Day 14)
Throughout the last few days periodic checks on fuel water
content were made and the levels were progressively reduced. At
06.00 the water level was 6.4 wt.$.
14.6.74 (Day 15)
Some problems with fines return system and stone feed hopper.
Otherwise uneventful day with a much improved desulphurising
performance due to lower water level in the fuel.
- 215 -
-------
15.6.74 (Day 16)
A short test on the rate of stone circulation to cyclones gave
a figure of 111 kg/hour for a mean cyclone temperature of about
500°C. More trouble with the RH cyclone drain actuator necessitated
manual operation. Desulphurising performance was poor at this point
(06.29) and it was decided until conditions were more stable to
revert to gasification with wet fuel (*Jo.Q wt.$ H20) to save the
limited supply of dry fuel oil (0.2 wt.$ HgO) available.
At 12.05 a switch to dry fuel oil was made and this gave only
a slight improvement in flue gas SOg levels.
At 22.50 the performance of the regenerator deteriorated showing
high levels of COp and low levels of SOp. Attempts to improve the
situation were unsuccessful.
16.6.7^ (Day 1?)
The poor performance of the regenerator continued throughout
the day. The regenerator C02 meter went off scale while the SOp
meter read zero. A possible explanation was that operating
conditions in the gasifier were too rich and reductions in the fuel
oil rate eventually cured the problem later in the day.
At 18.00 a thunderstorm caused two brief shut downs due to
lightening strikes on the power lines, but in each case start-up was
almost immediate.
17.6.74 (Day 18)
Trouble with cyclone drain valves dominated the day.
At 21.00 a heavy fuel oil leak was detected on the underside of
the unit at several points. A possible explanation was a leak into
the space between the refractory and the bottom steel casing.
18.6.74 (Day 19)
A system to inject SOp into the air supply to the burner was
set up and tests were started to confirm the reliability of the
analytical sampling systems. Several of these tests were carried out
throughout the day.
- 216 -
-------
At the end of the day preparations were made for a sulphation
and slumped bed decoke.
19.6.74 (Day 20)
After the decoke the unit was restarted on kerosine combustion
at 04.00. Several further SOp injection tests were carried out and
it was concluded that 81$ of tne SOo injected was picked up by the
flue gas sampling system. The most likely position where losses
could occur was concluded to be at the sampling filter.
At 06.20 the unit was shutdown to allow the boiler to be
inspected and cleaned. A large amount of material was removed.
After a false start due to a leaking fuel pump start-up on
kerosine combustion was achieved at 18.30.
20.6.74 (Day 21)
The initial attempt to gasify at 04.15 was unsuccessful because
trace heating on the fuel line had been switched off resulting in a
build-up of pressure on the line. A successful start-up on gasifica-
tion was achieved at 05.20. Initially high flue gas S02 readings
were obtained until the sulphate levels on the stone were reduced.
Further SOp injection tests were carried out during the day.
21.6.74 (Day 22)
More tests on S02 injection were carried out during the day.
This time injections into the bifurcated duct,the regenerator upper
space tapping and the boiler were all tried out.
Before completion of the test run a short trial measuring the
effect on performance of moving the bottom fuel injector up through
the bed, effectively changing the bed depth was carried out.
- 217 -
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INSPECTION, RUN 8
Gaslfier and Regenerator Refractory
The unit was shut down and inerted with nitrogen at the end of
the run without bed sulphation or carbon burn out so that the cyclone
and duct deposits could be examined.
The gasifier was generally in good condition with carbon
deposits on all faces. In the lower area the carbon was hard and
polished where it had been in contact with the fluid bed. At the
top, particularly around the cyclone entries the carbon was bonded
to the refractory to form a thicker layer with a granular surface
finish.
The additional lift of refractory installed prior to Run 8
showed some cracks which in general formed a continuation of the
cracks which were present in the original gasifier refractory.
The refractory blocks which were inserted into the gasifier
to reduce the bed area were free of cracks and in excellent
condition. Carbon was deposited in the gaps between these blocks,
and the gasifier wall. The head of the bolt retaining one of the
blocks to the wall was sheared from the shank, probably due to
distortion of the outer mild steel casing of the gasifier which could
have induced very large tensile forces.
The gasifier lid refractory which had carbon deposited on the
exposed faces was in good condition and free from cracks. The
transfer passage to the regenerator was unobstructed, but the return
line to the gasifier contained some hard agglomerated material
bonded to the refractory on the rear face of the transfer section.
However, it is unlikely that this obstruction was sufficient to
restrict the flow of material. The burnerquarl was undamaged and
free from the agglomerates which have been observed in earlier runs.
The regenerator bore was quite clear in the middle and upper
section, but two agglomerates had formed between the distributor and
the transfer passage from the gasifier. Figure F-l shows the
regenerator bore viewed from the underside after the removal of the
distributor. The two agglomerates were not bonded together and this
- 218 -
-------
suggests that they were formed at different times, probably during
the emergency shut downs which occurred during the run. The shut
down control system did not cut off the total air supply to the
regenerator, and there was probably enough oxygen to react locally
with defLuidised material thus raising its temperature and allowing
formation of the sticky CaS/CaO/CASCL eutectic.
The regenerator refractory did not show any significant
deterioration in the lower lifts which have been extensively cracked
from earlier test runs. The upper lift which was added for this run
appeared to be in good condition. The outlet bore from the top of
the regenerator was quite clean, unlike earlier runs when
irregular hard fused deposits had formed in this bore.
Gasifier and Regenerator Penetrations
The thermocouples, drain tubes and pressure tappings were in
good condition with light carbon and lime deposits on those areas
exposed to the bed material. The ends of the angled bed pressure
tapping tubes were cut in a vertical plane before installation on
this run whereas in earlier runs they had been cut on a horizontal
plane. This change has prevented obstructions in the regenerator
bottom tapping which were always a problem in earlier runs.
The tip of the left hand fuel injector was burnt away leaving
the open bore of the 18 mm tube flush with the wall. This would have
given a poor fuel distribution and probably accounts for the heavy
fuel oil seepage observed underneath the unit. The right hand fuel
injector and vertical fuel injector in the distributor were in good
condition.
The silicon carbide tube, which was installed through the
refractory sleeving blocks to project towards the material transfer
port was clear and undamaged.
Cyclones
Figure F-2 shows the entry ducts to the cyclones after the test
run. The right hand duct had significantly less carbon deposited on
one sidewall. This may have resulted from the greater quantity of
fine material which entered the cyclone as indicated by the higher
- 219 -
-------
operating temperature in the transfer vessel which drained the right
hand cyclone. The cyclone fines return system injected the fines
into the right hand side of the bed immediately below this cyclone
entry, and so may have resulted in a heavier fines loading on that
portion of the bed and gas space. The deposits in the entries were
firmly attached to the refractory and the irregular surface profile
was most marked on the left hand entry wall of the left hand cyclone.
The cyclone entries were very clear compared with previous operations,
although the gasification period since the previous burn out was fairly
short, at approximately 39 hours. This does show that the carbon
burn out procedures were very effective in removing the carbon-lime
deposits.
The bores of the cyclones were generally clean apart from the
left hand (Figure F-J) cyclone which had a small build up of material
where the entry blended with the bore. The drain of the left hand
cyclone was partially obstructed at the base of the cyclone (Figure
F-3) by a layer of carbon and lime. This obstruction would not have
prevented the cyclone draining, although the efficiency of operation
could be slightly reduced. The drain of the right hand cyclone
(Figure F-4) was quite clear.
The cyclone outlet tubes both had deposits of flakey carbon
and lime on their external faces (Figures F-5 and F-6). There was
a small area on each tube immediately opposite the entry duct where
the deposit was smooth due to the impingement of the fine material.
Figures F-7 and F-8 show that these are as on the left and right hand
tubes respectively. The deposited layer had fallen away when the
left hand tube was removed from the unit.
Gasifier and Regenerator Distributors
The gasifier distributor was in good condition with a hard layer
of lime deposited immediately below the nozzles in the defluidised
zone. The stainless steel nozzles were undamaged, but 15$ were
totally obstructed with lime particles with a further 3$ partially
obstructed.
The defluidised material on the distributor was impregnated with
oil (Figure F-9) around the centre injector which had been retracted
to the lowest position as the last test before the shut down. In
- 220 -
-------
addition the lower portion of the defluidised material at the left
hand side of the distributor was also impregnated with oil which had
come from the damaged left hand fuel injector. The two nozzles in
this area were coated with oil which had run back into the plenum
from the damaged injector. There was also a considerable quantity
of bed material in the plenum indicating that 5- 2 ram dia. holes with
this distributor design and bed particle size will permit material to
fall back under some conditions.
The regenerator distributor was partially covered by the
agglomerate and 7 of the 16 holes were obstructed, Figure F-10. The
upper cone section on the distributor top was a modification introduced
to eliminate the static bed which could form immediately above the
distributor. This modification apparently did not help fluidisation
and possibly contributed to the formation of the agglomerate.
Bed Material
The gasifier was shut down without sulphation and the sulphided
bed was found to be free from agglomerates apart from three carbon-
lime deposits shown in Figure F-ll. The larger deposit was found
near the centre of the bed and just below the slumped surface, and it
seems probable that it had formed around the open end of the burnt
fuel injector when there was bad fuel distribution. The source of
the two smaller particles is unknown.
The regenerator bed was free flowing apart from the presence of
the two large agglomerates. These would have adversely affected the
fluidisation of the bed.
Bifurcated Duct
The new bifurcated duct necessary because of the additional
height of the gasifier included two additional right angled bends to
bring the hot gas back to the burner. The construction of the gas
duct was the same as in previous runs, with refractory enclosed by
insulation and sealed with a mild steel cladding. The refractory was
in excellent condition without signs of cracking or spalling. The
bore of the duct was generally coated with carbon about 3 n™ thick,
but at the right angled corners there were additional deposits,
- 221 -
-------
particularly on the inside of the bends with local thickness up to
18 mm. These additional deposits extended for lengths between 5
and 15 cms along the pipe near the curved section.
Premix Section
Figure F-12 shows the up-stream side of the premix section with
a carbon layer up to 6 mm thick generally uniform about the
circumference with one piece which broke away during the removal of
the section. Figure F-13 shows the down-stream section with the
outer air annulus through which the first stage air is admitted.
Some deposits of limestone can be seen in the air annulus section
where material has been thrown out of the gas stream.
Figure F-l4 shows the premix section after the removal of the
carbon and lime showing some local deterioration in the inner tube,
and also in the outer air shroud. It is likely that this deterioration
in the material arose from high temperatures associated with local
carbon burning.
Figure F-15 shows the up-stream side of the burner which is
joined to the premix section. Deposits of lime with some carbon
can be seen on the lower portion, and there is a general deposit of
carbon on the conical duct leading into the burner gas discharge
orifice. Figure F-16 shows the discharge orifice with the inner
annulus through which the second stage air is admitted, and the outer
annulus through which the final combustion air is passed. The
steelwork on the burner was generally in good condition, apart
from one small hole around a weld joint, Figure F-17. The thermocouple
inserted into the burner throat had burnt away, presumably during a
burn out with the associated high surface temperatures.
- 222 -
-------
Fig F-l Regenerator Bore after Distributor has been Removed
Fig F-2 Gasifier Cyclone Entry Ducts
- 223 -
-------
Fig F-3 View of Left Hand Cyclone
Fig F-4 View of Right Hand Cyclone
- 224 -
-------
Fig F-5 Left Hand Cyclone Outlet Tubes
- 225 -
-------
Fig F-6 Right Hand Cyclone Outlet Tubes
- 226 -
-------
Fig F-7 Left Hand Cyclone Outlet Tube (second view)
- 227 -
-------
Fig F-8 Right Hand Cyclone Outlet Tube (second view)
- 228 -
-------
Fig F-9 Overhead View of Gasifier Distributor
Fig F-1O View of Regenerator Distributor
- 229 -
-------
Fig F-ll Carbon/Lime Deposits Found in Gasifier
Fig F-12 Up-stream Side of Main Burner Premix Section
- 230 -
-------
Fig F-13 Main Burner Downstream Section
Fig F-14 Main Burner Premix Section after Removal of Carbon and Lime
- 231 -
-------
Fig F-15 Up-Stream Side of Main Burner (joined to the premix section)
Fig F-16 Main Burner Discharge Orifice
- 232 -
-------
Fig F-17 Main Burner Steelwork (showing small hole in weld joint)
233 -
-------
RUN 8:
APPENDIX pi TABLE
TEMPERATURES AND FEED RATES
PAGE 1 OF 12
DAY.HOUR TEMPERATURE, DEO. C.
OASIFIER REGEN. RECYCLE
FEED RATE KG/HR
OIL STONE
.0330
.0430
.0530
.0630
.0730
. 0 830
.0930
. 1030
. 1 130
. 1230
. 1 330
. 1430
. 1 530
. 1630
. 1 730
. 1830
. 1 930
.2030
.PI 30
.2230
.2330
P. 00 30
2 . 0 1 30
2.0230
P. 0330
2.0430
2.0530
2.0630
2.0730
2.0830
2.0930
2. 1030
2 . 11 30
2. 1230
2. 1330
2. 1430
2. 1530
2 . 1 630
2 . 1 730
2. 1830
858.
858.
878.
892.
891.
900.
891.
877.
865.
870.
896.
898.
891.
880.
874.
872.
870.
853.
870.
880.
883.
887.
888.
87R.
860.
859.
872.
872.
874.
890.
880.
879.
864.
890.
900.
906.
877.
888.
889.
884.
970.
1032.
1040.
1050.
1050.
1048.
1052.
998.
1028.
1058.
1058.
1059.
1053.
1060.
1053.
1050.
1055.
1061 .
1062.
1062.
1062.
1060.
1060.
1058.
1058.
1058.
1058.
1058.
1058.
1059.
1059.
1059.
1058.
1055.
1058.
1059.
1051 .
1031 .
1058.
1059.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
56.
55.
54.
54.
53.
53.
53.
53.
53.
52.
49.
49.
49.
49.
49.
49.
50.
53.
52.
54.
54.
142.0
14?. 0
142.8
142.0
142.8
141.6
142.8
142.8
142.0
144.0
144.0
142.0
141.6
143.6
136.2
145.7
141.6
142.4
141.6
140.8
140.8
144.0
1 40 . 8
135.4
131.3
128.0
133.8
133.3
134.2
135.0
137.0
137.9
137.0
137.9
139.5
139. 1
137.0
132.5
137.5
137.5
9.1
20.4
25.9
24.5
24.0
22.7
22.7
29.0
32.2
29.0
36.7
28.6
28. I
34.9
38.6
39.0
41.7
29.0
29.0
24.5
24.0
23. 1
26.3
27.2
34.5
43.5
37.6
29.5
27.2
22.7
26.8
24.9
31.8
26.8
18. 1
28. 1
38. 1
29.0
28.6
24.9
- 234 -
-------
HUN 8:
APPENDIX Ft TABLE I.
TEMPERATURES AND FEED RATES PAGE
2 OF 12
DAY. HOUR TEMPERATURE, DEO. C.
OASIFIER REGEN. RECYCLE
FEED RATE KO/HR
OIL STONE
2. 1930
2.2030 .
2 . 2 1 30
2.2230
2.2330
3.0030
3 . 0 I 30
3.0230
3.0330
3.0430
3.0530
3 . 0 630
3.0730
3.0830
3.0930
3. 1030
3. 1 130
3. 1230
3. 1330
3. M30
3. 1530
3. 1630
3. 1730
3. 1830
3.1930 .
3.2030
3.2130
3.2230
3.2330
4.0030
4.0130
4.0230
4.0330
4.0430
4.0530
4 . 0 630
4.0730
4.0830
4.0930
4. 1030
898.
879.
862.
899.
888.
907.
902.
912.
898.
889.
890.
885.
890.
885.
895.
868.
872.
862.
870.
877.
870.
866.
891 .
892.
878.
872.
880.
888.
888. •
896.
891.
878.
871.
892.
880.
886.
875.
872.
892.
898.
1059.
1044.
1058.
1056.
1050.
1053.
1056.
1058.
1058.
1051 .
1058.
1055.
1058.
1060.
1061.
1058.
1059.
1059.
1058.
1059.
1059.
1059.
1058.
1058.
1058.
1058.
1058.
1058.
1058.
1057.
1057.
1055.
1055.
1056.
1056.
1055.
1056.
1058.
1058.
1058.
54.
61.
61.
57.
56.
57.
57.
61.
62.
62.
63.
64.
64.
65.
65.
62.
61.
61.
60.
60.
60.
59.
59.
59.
61.
61.
61.
61.
60.
55.
56.
56.
56.
54.
55.
54.
59.
57.
57.
57.
137.0
137.5
137.0
136.2
132. 1
142.0
151.9
158.4
163.8
168.7
168. 3
168.3
168.7
169. 1
169. 1
154.3
145.7
146.5
145.7
149.8
142.4
145.7
138.3
156.8
143.2
141.6
146. 1
149.8
141.6
144.9
144.9
145.3
145.3
143.6
142.4
142.8
144.5
139. 1
143.2
140.8
24.9
14.5
17.2
51.3
54.0
?3.6
3.2
9.5
9.5
5.9
4. 1
4. 1
9.5
8.2
10.4
1 1.8
7.7
1 1.3
22.2
32.7
27.2
32.2
24.5
27.2
36.3
34.0
37.2
30.4
37.6
6.8
29.5
24.5
39.9
40.4
40.8
16.3
1 1.8
18. 1
23. 1
8.6
- 235 -
-------
RUN 8:
DAY.HOUR
4
4
4
4
4
4,
4
4
4
4
4
4
4
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
6
6
, 1 1 30
, 1230
, 1330
, 1 430
, 1530
, 1630
, 1 730
, 1 830
, 1930
,2030
,2130
,2230
,2330
,0030
,0130
.0230
,0330
,0430
,0530
,0630
,0730
.0830
,0930
. 1030
, 1 1 30
. 1230
. 1 330
. 1430
. 1 530
. 1 630
. 1 730
, 1830
, 1930
.2030
.2130
.2230
.2330
.0030
. 0 1 30
6.0230
APPEND
TEMPERATURES AND
IX ps TABLE
FEFrD HATES
TEMPERATURE, DEG. C.
GASIFIER
898.
902.
892.
89V).
885.
900.
885.
886.
880.
882.
889.
895.
893.
899.
892.
892.
896.
893.
890.
891 .
898.
893.
900.
900.
886.
900 .
890.
878.
880.
886.
896.
920.
921.
903.
909.
900 .
906.
91H.
REGEN.
1058.
1060.
1060.
1060.
1058.
1045.
1050.
1050.
1048.
1048.
1048.
1048.
1049.
1051.
1052.
1053.
1051 .
1052.
1050.
1055.
1052.
1055.
MISSED
MISSED
1054.
1058.
1054.
1052.
1045.
1050.
1050.
1052.
1055.
1055.
1052.
1050.
1048.
1051.
1049.
1049.
RECYCLE
57.
60.
60.
60.
60.
60.
60.
60.
60.
60.
50.
58.
58.
58.
58.
56.
55.
53.
54.
54.
55.
54.
DATA READING
DATA READING
64.
70.
70.
70.
70.
70.
70.
68.
70.
62.
65.
58.
59.
59.
59.
58.
I.
PAGE 3
FEED RATE
OIL
142.0
142.8
140.8
145.3
142.4
142.8
140.8
145.3
142.8
143.2
142.4
143.2
143.2
143.6
143.2
143.6
142.4
143.6
142.8
143.6
143.2
143.6
144.9
146. 1
144.9
144.5
144.5
144.5
144.5
142.8
134.2
133.8
132.9
133.8
133.3
133.8
132.9
133.3
OF 1 2
KG/HR
STONE
7.7
6.8
1 .3
4.5
4. 1
2.7
4. 1
7.7
15.9
14. 1
15.9
15.0
1 1 .8
12.7
14.5
3.6
10.9
12.7
14.5
13.6
10.0
1 1.3
S.0
1 1.H
9.5
8.2
6.8
0.4
1 .8
10.4
8.2
6.8
6.4
9.5
11.3
10.4
10.9
5.9
- 236 -
-------
HUN 8:
AFPFNDIX F: TABLE
TEMPERATURES AND FEED RATES
PAGE 4 OF 12
DAY.HOUR TEMPERATURE, DEO. C.
GASIFIER RFGEN. RECYCLE
FEED RATF KG/HR
OIL STONE
6.0330
6.0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6. 1 130
6. 1230
6. 1330
6. 1430
6. 1530
6. 1630
6. 1730
6. 1830
6. 1930
6.2030
6.2130
6.2230
6.2330
7.0030
7.01 30
7.0230
7.0330
7.0430 .
7.0530
7.0630
7 . 0 730
7.0830
7.0930
7. 1030
7. 1 130 .
7. 1230
7. 1330
7. 1430
7. 1530
7 . 1 630
7. 1730
7 . 1 830
906.
882.
894.
887.
888.
892.
889.
902.
889.
888.
882.
885.
890.
900.
904.
894.
892.
883.
880.
876.
872.
876.
886.
883.
882.
879.
886.
888.
892.
900.
91 1.
878.
878.
878.
891.
881 .
873.
878.
868.
899.
1048.
1051 .
1 050 .
1052.
1052.
1040.
1045.
1058.
1058.
1058.
1058.
1060.
1060.
1060.
1060.
1060.
1058.
1062.
1061 .
1059.
1058.
1056.
1058.
1056.
1058.
1057.
1060.
1060.
1058.
1061 .
1059.
1060.
1060.
1060.
1058.
1060.
1060.
1060.
1059.
1060.
59.
59.
58.
63.
60.
61.
62.
62.
62.
62.
60.
60.
62.
62.
62.
62.
62.
62.
62.
61.
59.
58.
59.
59.
55.
53.
53.
53.
52.
53.
57.
62.
62.
62.
62.
62.
63.
66.
67.
63.
133.3
133.3
133.8
133.8
133.8
132.9
133.3
134.2
135.0
135.8
139. 1
129.2
134.2
133.3
134.2
135.0
133.8
133.8
134.2
134.6
134.2
133.8
134.2
134.6
134.2
133.8
134.2
134.6
133.8
133.8
134.2
134.2
134.2
131.7
136.6
134.2
133.8
133.8
133.8
133.8
8.2
29.0
5.9
1 .8
1.3
2.7
4.1
4.5
1.3
1.8
0.9
9. 1
7.7
10.9
12.7
5.0
8.6
10.9
10.0
10.0
15.0
15.4
13.6
16.3
15.9
13.6
10.9
10.9
10.9
1 1.3
12.7
12.2
15.4
9.5
7.7
7.7
10.9
1 1.3
13.6
15.4
- 237 -
-------
RUN Hi
APPENDIX F: TARLF I.
TEMPERATURES AND FEED HATES PAGE
5 OF 12
DAY.HOUR TEMPERATURE, DEC. C.
GASIFIFR REOEN. RECYCLE
FEED RATE KG/HR
OIL STONE
7 . 1 930
7.2(230
7.2130
7.2230
7.2330
8.0030
8.0130
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8.0930
8. 1030
8. 1 130
8. 1230
8. 1330
8. 1430
8. 1530
8. 1630
8. 1730
8. 1830
8. 1930
8.2030
8.2130
8.2230
8.2330
9.0030
9.01 30
9.0230
9.0330
9.0430
9.0530
9.0630
9.0730
9.0830
9.0930
9. 1030
896.
898.
885.
883.
897.
889.
888.
885.
883.
884.
890.
886.
886.
885.
877.
886.
892.
898.
902.
900.
900.
900.
888.
898.
906.
B98.
895.
889.
891 .
891.
889.
890.
888.
878.
882.
869.
868.
871.
871.
886.
1060.
1060.
1060.
1058.
1059.
1058.
1059.
1059.
1061 .
1061 .
1059.
1057.
1057.
1058.
1058.
1056.
1058.
1058.
1058.
1060.
1060.
1060.
1060.
1060.
1060.
1059.
1059.
1058.
1059.
1058.
1056.
1058.
1059.
1058.
1056.
1056.
1058.
1058.
1058.
1056.
63.
63.
63.
63.
63.
63.
63.
63.
63.
63.
63.
63.
63.
64.
66.
68.
68.
68.
68.
68.
68.
68.
68.
68.
70.
71.
70.
70.
69.
69.
68.
68.
69.
70.
71.
71.
70.
71.
70.
70.
134.2
133.8
134.2
133.8
135.0
133.8
1 31 .3
138.3
131 .7
134.2
134.2
135.0
132.5
133.8
134.2
134.2
133.3
134.2
133.8
133.8
133.8
133.8
134.2
133.8
133.8
133.8
133.8
133.8
133.8
133.8
133.3
133.8
133.8
133.8
133.8
133.8
133.8
133.8
133.8
133.8
14. 1
1 1 .8
12.7
8.6
10.4
12.7
1 1 .8
12.2
11.8
12.7
12.7
1 1 .3
9.5
9.5
5.9
3.6
8.6
5.0
5.9
7.7
1 .8
1 1 .3
10.0
9.5
9.5
11.3
10.9
1 1 .8
9. 1
7.7
7.7
7.7
4. 1
15.0
10.0
10.4
10.4
1 4.5
5.4
8.6
- 238 -
-------
APPENDIX Pi TABLE I.
HUN 8: TEMPERATURES AND FEED RATES PAGE
6 OF 12
DAY.HOUR TEMPERATURE, DEG. C.
GASIFIER REGEN. RECYCLE
9. 1 130
9. 1230
9. 1330
9. 1430
9. 1530
9. .1630
9. 1 730
9.1830 .
9. 1930
9.2030
9 . 2 1 30
9.2230
SHUT
10.2230
10.2330
.0030
.0130
.0230
.0330
.0430
.0530
1.0630
1.0730
SHUT
12.0330
12.0430
12.0530
12.0630
12.0730
12.0830
12.0930
12.1030
12.1 130
12. 1230
892.
887.
899.
889.
885.
890.
889.
879.
880.
882.
878.
858.
DOWN AT
888.
880.
880.
880.
885.
897.
908.
894.
892.
892.
DOWN AT
900.
920.
900.
900.
918.
912.s
912.
900.
880.
890.
1058.
1058.
1058.
1058.
1058.
1060.
1058.
1057. .
1056.
1058.
1058.
1057.
9.2230 FOR
980.
1030.
1040.
1032.
1051.
1045.
1054.
1052.
1054.
1054.
1 1.0730 FOR
930.
950.
970.
1000.
1000.
1010.
1010.
1032.
1020.
1034.
71.
72.
71.
71.
71.
70.
70.
71.
71.
72.
71.
69.
23 HOURS
62.
62.
62.
62.
62.
62.
62.
62.
62.
62.
19 HOURS
63.
65.
63.
65.
65.
65.
57.
50.
50.
49.
134.2
133.8
134.2
134.6
133.3
133.8
133.8
134.2
133.8
134.2
134.2
133.3
144.0
144.0
150.6
151.9
153. 1
153.5
153.9
154.7
155.6
1 16.9
127. 1
128.6
128.9
131. 1
135.7
137.3
137.0
137.6
138.8
137.9
FEED RATE KG/HR
OIL STONE
2.7
6.4
1 1.3
10.0
15.4
13.2
5.0
12.2
15.0
1 1.
9,
9.1
15.9
13.?
14.5
18. 1
18.6
1 1.8
9.1
8.6
10.4
10.4
10.0
1 1.8
15.0
1 1.8
8.2
8.6
12.2
13.2
30.4
16.3
- 239 -
-------
RUN 8:
APPENDIX Pi TABLE I.
TEMPERATURES AND FEED RATES PAGE
7 OF 12
DAY.HOUR TEMPERATURE, DEC. C.
GASIFIER REGEN. RECYCLE
FEED RATE KG/HH
OIL STONE
12. 1330
12. 1430
12. 1530
12.1 630
12. 1730
12. 1830
12. 1930
12.2030
12.2130
12.2230
12.2330
13.0030
1 3 . 0 1 30
13.0230
13.0330
13.0430 .
13.0530
13.0630
13.0730
13.0830
13.0930
13. 1030
13.1 1 30
13. 1230
13. 1330
13. 1430
13. 1530
13.1 630
13. 1 730
13.1 830
13. 1930
13.2030
13.2130
13.2230
13.2330
14.0030
1 4 . 0 1 30
14.0230
14.0330
14.0430
890.
850.
865.
875.
878.
882.
871.
871.
875.
880.
880.
895.
895.
874.
880.
875.
870.
867.
870.
872.
876.
870.
890.
890.
889.
880.
890.
888.
880.
882.
890.
875.
890.
892.
891.
879.
883.
884.
880.
880.
1034.
990.
995.
1038.
1038.
1040.
1041 .
1047.
1038.
1033.
1033.
1045.
1048.
1038.
1040.
1033.
1030.
1030.
1035.
1030.
1025.
1034.
1038.
1048.
1058.
1053.
1058;
1052.
1052.
1052.
1051.
1049.
1050.
1054.
1052.
1052.
1052.
1050.
1052.
1054.
49.
59.
55.
60.
55.
55.
52.
52.
52.
52.
52.
50.
50.
50.
50.
50.
50.
50.
46.
45.
44.
45.
45.
45.
45.
46.
47.
48.
48.
40.
42.
40.
40.
38.
38.
38.
33.
33.
32.
32.
138.2
137.6
139.1
137.3
168. 1
157.6
149.7
149.4
149.4
149.0
149.0
152.7
149.4
149.0
144.8
161.3
164.4
157.7
161.6
160.9
162.0
163.0
1 60 . 2
162.0
162.0
162.0
162.3
161.6
162.0
162.7
162.0
161.7
160.6
161.7
162.0
177.7
170.3
169.5
167.9
169. 1
14.1
22.2
24.0
20.9
23.6
21.3
26.8
20.0
25.4
18.6
14. 1
14. 1
18.6
20. 4
15.4
17.7
17.7
1 7.7
1 6.8
1 3.2
8.2
20.4
24.9
22.7
24.9
14.5
20.9
22.2
23.6
21 .3
19.5
26.3
20.9
22.7
23. 1
20.9
20.0
21 .3
26.8
2 1 .8
- 240 -
-------
APPENDIX F: TABLE I.
HUN 8: TEMPERATURES AND FEED RATES PAGE
8 OF 12
DAY. HOUR
14.0530
14.0630
14.0730
14.0830
14.0930
14. 1030
14. 1 130
14.1230 ,
14. 1330
14. 1430
14. 1530
14. 1630
14.1730 .
14. 1830
14. 1930
14.2030
14.2130
14.2230
14.2330
15.0030
1 5 . 0 1 30
15.0230
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
15.0930
15. 1030
15. 1 130
15. 1230
15. 1330
15. 1430
15. 1530
15. 1630
15.1 730
15. 1830
15. 1930
15.2030
TEMPERATURE, DEC. C.
GASIFIER
890.
889.
889.
890.
886.
880.
879.
879.
880.
881.
880.
880.
879.
889.
890.
901.
894.
885.
892.
885.
886.
890.
895.
886.
887.
896.
892.
890.
889.
882.
870.
879.
881.
885.
873.
872.
872.
875.
878.
891.
REGEN.
1052.
1052.
1050.
1052.
1053.
1051.
1052.
1052.
1051.
1052.
1052.
1052.
1052.
1052.
1052.
1051.
1052.
1052.
1052.
1055.
1054.
1052.
1052.
1053.
1053.
1054.
1053.
1053.
1051 .
1050.
1050.
1052.
1049.
1051 .
1051 .
1050.
1053.
1054.
1059.
1059.
RECYCLE
32.
32.
32.
32.
30.
31.
31.
31.
31.
31.
31.
31.
31.
32.
32.
32.
32.
32.
32.
32.
32.
32.
32.
31.
31.
31.
31.
31.
31.
29.
29.
29.
28.
30.
31.
31.
31.
32.
32.
32.
FEED RATE KG/HR
OIL
169. 1
1 69. 9
168.7
168.3
168.3
168.7
167.5
168.7
167.5
166.8
166.4
167.5
167.9
167.5
168.3
167.9
167.9
167.2
169.2
169.6
170.0
170.0
169.6
169.2
170.0
170.4
169.2
169.6
169.2
170.0
168.8
168.8
169.2
168.0
168.0
164. 1
162.2
161.8
161.4
161.0
STONE
20.0
19.1
19.5
18.6
17.2
19.5
24.0
21.8
23. 1
18. 1
23. 1
24.9
23.6
22.7
20.9
23. 1
23.6
24.9
20.9
20.9
26.8
19.5
27.2
26.3
24.0
15.9
23. 1
21.8
14.5
20.9
19. 1
25.9
20.9
17.7
21.3
24.0
27.7
21.8
2k. 2
20.0
- 241 -
-------
RUN 8:
APPENDIX FI TABLE
TEMPERATURES AND FEED RATES
PAGE 9 OF 12
DAY.HOUR
TEMPERATURE, DFG. C.
GASIFIER REGFN. RECYCLE
FEED RATE KO/HR
OIL STONE
15.2130
15.2230
15.2330
16.0030
16.0 130
16.0230
16.0330
1 6.W430
16.0530
16.0630
16.0730
16.0830
16.0930
16. 1030
16. 1 130
16. 1230
16. 1330
16. 1430
16. 1530
16. 1630
16. 1730
16. 1830
1 6. 1930
1 6. 2030
1 6.2 1 30
16.2230
16.2330
17.0030
17.0 130
17.0230
17.0330
17.0430
17.0530
17.0630
17.0730
17.0830
17.0930
1 7 . 1 0 30
17.1 130
17. 1230
893.
890.
890.
900.
894.
886.
879.
884.
890.
898.
898.
892.
917.
881.
880.
891.
890.
b98.
908.
922.
919.
923.
920.
915.
91 1.
896.
885.
878.
879.
881.
885.
891.
889.
892.
898.
882.
871.
902.
912.
899.
1060.
1059.
1058.
1055.
1053.
1052.
1055.
1052.
1055.
1054.
1054.
1052.
1052.
1048.
1050.
1050.
1050.
1055.
1056.
1062.
1058.
1055.
1045.
1040.
1050.
1050.
1 050 .
1041 .
1050.
1048.
1044.
1042.
1043.
1040.
1035.
1043.
1050.
1043.
1060.
1066.
33.
33.
33.
33.
33.
33.
34.
34.
33.
32.
31.
30.
45.
35.
62.
65.
63.
52.
48.
45.
44.
44.
44.
40.
39.
37.
35.
32.
33.
32.
32.
32.
32.
31.
30.
50.
65.
65.
60.
60.
161 .4
160.6
161 .4
161 .8
162.6
167.2
165.7
163.7
178.3
178.3
180.8
166.8
159.2
157.3
157.3
165.8
167.4
164. 1
165.4
114.3
141.5
146.0
151 .4
158.4
164.5
160.0
158.0
156.7
157. 1
158.0
157. 1
157.5
157.2
157.6
158. 1
156.8
149.0
142.4
1 40 . 4
135.8
20.9
22.7
J—j *-,
1 .2
1 5.9
26.6
24.0
26.3
20.4
22.7
1 9.^
16.8
19.5
13.6
12.7
15.4
20.0
19. 1
20 . 9
1 8.6
1—7 *•»
7.2-
9. 1
1A 1
4. 1
1 8.6
16.8
14.5
1 6.8
27.2
24.0
2-7 —7
/.7
2 1 .3
25.9
1 6.8
19.1
20.0
1A 4
4. 1
16.8
20.^
16.3
16.3
, 17.7
- 242 -
-------
RUN 8;
DAY.HOUR
17
17
17
17
17
17
17
17
17
17
17
18
18
18
18
18
18
18
18
Ib
18
18
18
18
18
18
18
18
18
18
18
18
18
18
18
19
19
19
19
. 1330
. M30
, 1530
. 1630
, 1730
, 1830
. 1 930
.2030
. 2 1 30
,2230
.2330
.0030
. 0 1 30
.0230
.0330
,0430
,0530
,0630
,0730
,0830
,0930
, 1030
, 1 130
, 1230
, 1330
, 1430
, 1530
, 1 630
, 1 730
, 1 830
, 1930
,2030
,2130
,??30
,2330
,0030
, 0 1 30
,0230
,0330
19.0430
APPENDIX P : TABLE
TEMPFRATUHES AND FEED RATFS
TEMPERATURE, DEO. C.
GASI FIER
890.
890.
910.
900.
920.
912.
898 .
905.
891.
898.
804.
891.
899.
89?.
885.
907.
893.
899.
904.
900.
894.
899.
903.
91?.
920.
925.
916.
930.
91?.
910.
899.
907.
907.
898.
91 1.
888.
889.
874.
REGEN. RECYCLE
1049. 60.
1073. 58.
1060. 50.
1056. 55.
1060. 40.
MISSED DATA READING
MISSED DATA HEADING
104?. 35.
1052. 35.
1058. 36.
1063. 36.
1052. 37.
1059. 35.
1056. 33.
1056. 31.
1050. 31.
105?. 32.
1049. 31.
1052. 32.
1055. 33.
1050. 33.
1058. 34.
1055. 35.
1060. 35.
1062. 35.
1062. 35.
1052. 35.
1062. 40.
1059. 35.
1063. 35.
1040. 45.
1060. 35.
1060. 41.
1056. 41.
1055. 58.
1058. 31.
1055. 31.
1049. ?8.
1039. 29.
1050. 29.
I.
PAG
FEED
OIL
141.2
151. 1
149.0
148.2
147.8
149.0
155.0
147. 1
1 40 . 1
1 40 . 1
140.6
M4.3
144.7
143.8
141 .4
139.7
138.9
139.6
139.6
143.3
145.3
145.3
137. 1
135.0
135.9
139.6
145.3
144.5
142.0
141.6
139.6
139.6
140.0
140.4
140.4
139.6
140.4
140.0
10 OF 12
RATE
KG/HR
STONE
23
18
17
?3. 1
8.2
15.
14.
26,
13,
17,
21.
10.
16.
17.
21.
16.
18,
16.
15,
18.
20.
24,
24.
?3,
20.
24,
18.
25.
26.
6
1
2
13.6
19. h
15.0
25.9
19. 1
16.3
0
5
3
2
2
8
9
3
2
8
8
1
8
0
6
5
4
9
R
6
4
9
1
9
3
31.8
- 243 -
-------
HUN 8:
APPENDIX Pi TABLE I.
TEMPERATURES AND FEED RATES PAGE
I 1 OF 12
DAY.HOUR ThMPFRATURE, DEC. C.
GASIFIER REGEN. RECYCLE
FEFD RATE KG/MR
OIL STONE
19.0530
19.0630
19.0730
19.0830
19.0930
19. 16330
19. 11 30
19. 1?30
19. 1330
19. 1430
19. 1530
19.1 630
19. 1730
898.
899.
898.
894.
897.
900.
900.
898.
909.
890.
900.
900.
920.
1048.
1057.
1054.
1055.
1055.
1056.
1055.
1052.
1055.
1050.
1052.
1052.
1088.
30.
30.
31.
31.
30.
29.
30.
30.
30.
30.
30.
30.
30.
137. 1
135.5
136.3
135.9
141 .2
134.2
133.8
134.6
135.5
135.0
135.0
135.5
133.0
20.0
20. 4
20.9
16.8
24.5
24.9
26.3
25.9
13.6
10.9
10.0
8.2
7.7
SHUT DOWN AT 19.1730 FOR 36 HOURS
21 .0630
21.0730
21 .0830
21 .0930'
21 . 1030
21.1 1 30
? 1 . 1 230
21 . 1330
21. 1430
21 . 1530
21 . 1630
21.1 730
2 1 . 1 830
21.1 930
21 .2030
2 1 . 2 1 30
21.2230
21 .2330
22.0030
22.0130
22.0230
22.0330
22.0430
910.
900.
901.
908.
906.
901 .
905.
910.
91 1.
918.
914.
918.
917.
915.
930.
937.
932.
925.
922.
912.
91 1 .
914.
918.
1005.
1042.
• 1059.
1060.
1058.
1060.-
•1058. '
1060.
1058.
1058.
1059.
1059.
1059.
1080.
1056.
1048.
1061 .
1061 .
1065.
1062.
1062.
1062.
1060.
25.
25.
25.
30.
30.
30.
31.
32..
34.
36.
36.
36.
35.
36.
36.
36.
36.
36.
36.
36.
35.
35.
34.
151.9
152.7
150.2
155.6
153.5
153. 1
153. 1
152.7
153. 1
153.5
152.7
153.5
153. 1
153. 1
146.9
144.0
148.2
152.7
152.7
152.9
157.3
158.9
158.0
18.6
1 V . 9
10.4
9.5
1t5.9
15.0
1 3.6
9.S
9.5
12.2
13.6
1 3.6
12.2
1 5.4
15.9
11.3
11.8
1 3.6
18.6
18.6
1 6.3
1 5.4
12.7
- 244 -
-------
RUN 8
APPENDIX Pi TABLE I.
TEMPERATURES AND FRED RATES PAGE
12 OF 1?
DAY. HOUR
TEMPERATURE, DFG. C.
OASIFIER RFGEN
22.0530
22.0630
22.0730
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1330
22. 1430
22. 1530
22. 1630
910.
912.
91 1.
912.
913.
903.
895.
889.
890.
902.
91 1.
1064.
1061 .
1059.
1066.
1060.
1071.
1059.
1060.
106 1 .
1062.
M I SSED
1062.
. RECYCLE
34.
34.
33.
33.
33.
32.
32.
33.
32.
0.
DATA READING
33.
FEED RATE KG/HR
OIL STONE
159.3 12.2
159.3
159.3
158.5
158.5
159.3
158.5
158.5
158.9
158.5
5.0
4. 1
0.9
7.7
3.6
7.2
6.3
5.4
5.9
158.9 11.8
- 245 -
-------
APPENDIX B TABLE II.
RUN 8: GAS FLOW RATES
PAGE 1 OF 12
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
1.0330
.0430
.0530
.0630
.0730
.0830
.0930
. 1030
. 1 130
. 1?30
. 1330
. 1430
. 1530
. 1630
. 1730
. 1830
. 1930
.2030
.2130
.2230
.2330
5.0030
? . 0 1 30
2.0230
3.0330
3.0430
3.0530
3.0630
?.0730
2.0830
3.0930
3. 1030
3.1 130
3. 1230
3 . 1 330
3. 1430
3. 1530
3. 1630
3. 1730
3 . 1 830
299.
316.
333.
342.
351.
385.
377.
386.
391.
391.
417.
416.
416.
416.
416.
416.
416.
418.
410.
419.
410.
402.
410.
376.
359.
359.
376.
376.
393.
393.
393.
392.
392.
400.
4(7)0.
417.
409.
400.
413.
404.
87.
87.
57.
57.
57.
57.
57.
57.
57.
57.
72.
71.
68.
61 .
61.
59.
46.
44.
46.
47.
49.
39.
50.
42.
46.
47.
39.
37.
37.
41 .
41 .
34.
49.
52.
49.
43.
47.
57.
57.
57.
4.6
4.6
4.7
4.7
4.7
4.7
4.6
4.6
4.6
4.6
4.6
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.6
4.6
4.6
4.7
4.7
4.9
4.9
4.9
4.9
4.9
29.8
30.3
24.4
25.6
31.3
30.5
28.4
31 .0
26.8
26.4
31.9
31.9
32.0
30.8
28.2
26.0
31 .9
29.8
29. 1
28.6
28.6
29.2
27.9
33.6
34.8
30.8
32.0
32.7
30.7
30.8
34.8
30. 1
29.3
28.9
31 .7
32.9
31.9
32. 1
30 . 0
34.6
1.7
1 .8
2.1
1.5
.7
1.7
2.1
1.5
.8
.0
.8
.2
.6
.4
.7
. 7
. 1
.6
. 1
1.5
1.5
.5
.5
. 6
.6
. 5
. 6
. 7
.6
• -5
.3
.6
.7
1.4
1.5
1.4
1.5
1.5
1.4
1.6
.37
.46
.21
.25
.53
.48
.42
.45
.30
.28
.57
.54
.55
.50
.39
.28
.53
.46
.41
.40
.40
.42
.37
.63
.69
.50
.56
.60
.50
.50
.68
.47
.44
.40
.54
.59
.54
.53
.46
.68
- 246 -
-------
PAGE 2 OF 12
DAY.HOUR
GAS
GASIFIFR
AIR FLUF GAS
RATES M3/HR RF.GFN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
2. 1930
2.2030
2.2130
2.2230
2.2330
3.0030
3.0130
3.0230
3.0330
3.0430
3.0530
3.0630
3.0730
3.0830
3.0930
3. 1030
3. 1 130
3. 1230
3.1330
3. 1430
3. 1530
3. 1630
3. 1730
3. 1830
3. 1930
3.2030
3 . 2 1 30
3.2230
3.2330
4.0030
4 . 0 1 30
4.0230
4.0330
4.0430
4.0530
4.0630
4.0730
4.0830
A. 0930
4. 1030
401.
375.
392.
427.
410.
429.
428.
^27.
461.
461.
461.
461.
461.
453.
420.
325.
333.
342.
359.
376.
376.
384.
392.
393.
393.
393.
393.
394.
376.
376.
376.
393.
394.
394.
402.
402.
402.
402.
402.
402.
57.
127.
107.
87.
88.
88.
88.
88.
166.
186.
186.
206.
225.
225.
206.
146.
157.
137.
1 17.
108.
108.
108.
98.
98.
9b.
88.
88.
88.
88.
67.
67.
67.
67.
67.
67.
67.
67.
67.
57.
57.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
31 .8
30.8
29.7
28.2
28.6
30.7
31.5
30.9
29.3
29. 1
29. 1
28.5
31.3
32.2
33.7
34.0
30 . 6
33. 1
31.9
31.3
28.9
29.0
31 .6
30.3
29.8
30.9
30.6
31 . 1
30.4
30.7
30.5
30.4
30. 1
29.2
29.2
29.0
31 .2
30.3
30.9
30.7
1.6
1.5
1.2
1.6
1.5
1.5
1 .5
1.8
1.5
1.3
1 .5
1.5
1.5
1.6
1.8
2.0
2.0
1 .9
2.0
1.9
2.0
1.6
1 .8
1.8
1.7
1.7
1.6
1.8
1.9
1.9
1.9
1.6
1.5
1 .8
1.5
1.5
1.6
1.9
1.4
1.6
.55
.48
.43
.38
.38
.48
.52
.50
.41
.38
.40
. 36
.50
.54
.62
.66
.50
.61
.56
.53
.43
.41
.54
.47
.45
.51
.49
.52
.49
.50
.40
.A7
.46
.43
.42
.41
.51
. 4Q
.49
.4^
- 247 -
-------
APPFND1X Pi TABLE II.
RUN 8: GAS FLOW RATFS
PAGF 3 OF 12
PAY.HOUR
HAS
GASIFIER
AIR FLUF. HAS
RATES M3/HR KEGEN.
PILOT HEOFNERATOH VELOCITY
PROPANE AIR NITROGEN M/SHC
A. 1 130
4. 1230
4. 1330
4. 1430
4. 1530
4. 1630
4. 1730
4 . 1 830
4 . 1 930
4.2030
4.21 30
4.P230
4.2330
5.0030
5 . 0 | 30
5.0230
5.0330
5.0430
5.0530
5.0630
5.0730
5.0830
5.0930
5. 1030
5 . 1 1 30
5. 1230
5. 1330
5. 1430
5. 1530
5. 1630
5. 1730
5 . 1 830
5 . 1 930
5.2030
5.2130
5.2230
5.2330
6.0030
6.0 130
6.0230
402.
401 .
399 .
398.
397.
389.
390.
390.
390.
389.
389.
372.
372.
372.
372.
372.
372.
372.
372.
372.
372.
372.
375.
393.
393.
393.
375.
355.
355.
364.
364.
407.
372.
372.
372.
372.
372.
372.
55.
57.
57.
57.
57.
57.
57.
57.
57.
57.
76.
57.
73.
73.
77.
76.
77.
58.
57.
65.
60.
50.
MISSED
M I SSED
57.
88.
88.
44.
32.
48.
42.
50.
48.
51 .
68.
67.
57.
. 57.
57.
67.
4.9
4.9
4.9
4.9
4.9
4.9
4.5
4.5
4.5
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.5
DATA
DATA
4.5
4.5
4.5
4.5
4.5
4.4
4.4
4.5
4.4
4.5
4.5
4.5
4.5
4.5
4.5
4.5
33.0
36.2
34.4
34.8
34.0
32.9
32.8
30. 1
28.9
29.6
30.2
28.2
30 . 9
31.7
30.5
27.9
31 .4
29.8
29.2
29. 1
28.0
28.0
READING
READING
30 . 0
32.0
33.2
33.5
34.8
35. 1
35. 1
34.9
34.2
34.8
34.6
34.4
34.5
34.6
33.8
34.0
1.8
2.0
1.9
1.9
1.0
2.0
2.4
1.7
1.6
1 .8
2.2
.4
.6
.5
.4
.6
.6
.6
.5
.5
.4
.9
1 .9
1 .8
2.1
2.7
2.3
1 .9
1.6
1.9
2.0
2.0
1.8
1.9
1 .7
1.9
1 .6
1.9
.61
.76
.68
.70
.62
.60
.62
.46
.40
.44
.49
.36
.49
.52
.47
.36
.52
.45
.41
.41
.^5
.38
.46
.56
.62
.66
.69
.70
.68
.69
.67
.70
.67
.67
.66
.68
.63
1 .65
- 248 -
-------
APPENDIX P« TABLE II.
RUN Ui GAS FLOW RATES
PAGF 4 OF 12
DAY.HOUR
G A S
GASIFIER
AIR FLUF GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
6.0330
6.0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6. 1 130
6. 1230
6. 1330
6. 1430
6. 1530
6. 1630
6. 1730
6. 1830
6. 1930
6.2030
6.2130
6.2230
6.2330
7.0030
7.0130
7.0230
7.0330
7.0430
7.0530
7.0630
7.0730
7.0830
7.0930
7. 1030
7. 1 130
7. 1230
7. 1330
7. 1430
7. 1530
7 . 1 630
'/ . 1 730
7. 1830
364.
364.
364.
364.
364.
364.
355.
355.
355.
355.
343.
351.
351.
351.
351.
351.
351.
352.
352.
353.
353.
353.
353.
353.
353.
353.
354.
354.
354.
355.
355.
329.
338.
338.
320.
320.
320.
320.
354.
354.
87.
87.
87.
88.
88.
88.
88.
68.
68.
68.
68.
68.
68.
68.
75.
68.
68.
68.
68.
68.
68.
69.
68.
68.
68.
68.
68.
68.
68.
68.
68.
67.
88.
88.
67.
87.
87.
108.
55.
18.
4.5
4.5
4.5
4.5
4.5
4.5
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.5
4.5
4.5
4.5
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.5
4.5
4.4
4.4
4.4
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
33.3
33. 1
33.0
33.0
32.2
33.0
28.2
25.2
25.9
25.4
26. 1
25.5
25.9
25.8
26.8
26.4
26.4
25.9
25.7
26.2
27.4
27.3
27.4
27.5
26.7
26.8
27.2
26.4
31.0
25.5
29.6
29.9
29.6
29.5
30.3
30.2
29.9
30. 1
28.7
29.6
1.7
1.6
1.6
1.6
1.5
2.4
2.3
1 .8
1.8
.8
.6
.7
.8
.8
.9
.8
.8
.9
2.3
.7
.6
1.9
1.5
2.0
1.6
1.6
1.7
1.7
2.0
1.7
1.9
2.5
1.9
.7
.6
2.0
.7
.5
.7 1
1 .8
.61
.60
.59
.59
.56
.6?
.40
.25
.29
.26
.28
.26
.28
.28
.33
.31
.30
.29
.30
.29
.34
.35
.34
.36
.31
.31
.34
.30
.53
.26
.46
.49
.45
.44
.48
.49
.46
.46
.41
.45
- 249 -
-------
APPENDIX Fs TABLF II.
RUN 8: GAS. FLOW RATES
PAGE 5 OF 12
DAY.HOUR
GAS
GASIFIFR
AIR FLUH GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
7. 1930
7.2030
7 . ? 1 30
7.2230
7 . 2330
8.0030
8.0130
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8.0930
8. 1030
8. 1 130
8. 1230
8. 1330
8. 1430
8. 1530
8 . 1 630
8. 1730
8. 1830
8. 1930
8.2030
8.2130
8.2230
8.2330
9.0030
9.0130
9.0230
9.0330
9.0430
9.0530
9.0630
9.0730
9.0830
9.0930
9. 1030
328.
337.
329.
329.
329.
338.
338.
338.
338.
337.
337.
329.
320.
328.
328.
337.
337.
337.
336.
1 12.
1 12.
337.
337.
337.
337.
337.
337.
320.
329.
330.
321.
330.
321.
321.
321.
321.
330.
330.
329.
329.
16.
13.
0.
0.
8.
87.
97.
97.
97.
97.
97.
107.
107.
107.
108.
109.
109.
99.
99.
99.
99.
99.
109.
99.
139.
139.
129.
129.
129.
129.
1 18.
1 18.
129.
129.
1 18.
1 18.
109.
109.
109.
109.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
30.8
30.5
30.7
30.3
31.0
28.3
28.4
30.7
29.0
29.0
20.8
30.7
29.3
29.5
29.2
29.3
29.2
29.3
29.6
31.4
31 .4
31.4
30.8
29.9
35.8
34. 1
33.4
34.2
26.7
29.6
29.2
29.4
29.6
29.4
29.8
28.9
30. 1
29.0
29.2
29.5
1 .9
1 .8
2.0
1.9
1.9
1.7
1.7
1.7
1 .7
1.6
1.7
1.9
1 .6
1.7
1.5
1.7
1.5
1.7
1.6
1.7
1.7
1.7
1 .5
1 .8
1 .6
1.8
2.1
1 .8
1 .8
1 .8
1 .7
1.7
1.7
1.8
1.7
1.8
1 .7
2.3
1.0
1 .9
1.52
1 .50
1.52
1 .40
1 .52
1 .38
1. 39
1 . 50
1 .42
1 .41
1 .45
1 .50
1.42
1 .44
1 .42
1 .43
1.42
1 .43
1 .44
1 .53
1 .53
1 .53
1 .49
1 .46
1 .72
1 .65
1 .63
1 .65
1 .31
1 .44
1 .42
1 .43
1 .44
1 .43
1 .45
1 .41
1 .46
1 .44
1 .30
1 .44
- 250 -
-------
APPENDIX Pi TABLE II.
RUN 8: GAS FLOW RATES
PACK 6 OF 12
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR RFGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SFC
9 . 1 1 30
9. 1230
9. 1330
9. 1430
9. 1530
9. 1630
9. 1730
9. 1830
9. 1930
9.2030
9.2130
9.2230
SHUT
0.2230
0.2330
.05030
.0130
.0230
.0330
.0430
1 .0530
1 .0630
1 .0730
SHUT
12.0330
12.0430
12.0530
12.0630
12.0730
12.0830
12.0930
12. 1030
12. 1 130
12. 1230
328.
320.
320. '
320.
312.
312.
312.
303.
294.
303.
286.
285.
DOWN AT
358.
375.
375.
372.
372.
389.
389.
389.
376.
376.
DOWN AT
370.
334.
335.
368.
352.
334.
370.
370.
370.
353.
109.
109.
109.
109.
109.
109.
109.
109.
98.
98.
98.
98.
9.2230
128.
108.
88.
88.
88.
68.
68.
109.
88.
88.
1 .0730
30.
81 .
83.
86.
27.
40.
39.
33.
26.
24.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
FOR 23
4.5
4.5
4.5
4.5
4.5
4.4
4.4
4.4
4.4
4.4
FOR 1 9
4.4
4.4
4.4
4.4
4.5
4.5
4.5
4.5
4.5
4.5
29.3
30.4
29.9
28.3
27.8
28.9
25.6
25.0
27.7
26.3
28.6
28.6
HOURS
24.2
24.2
24.3
24. 1
23.5
27.8
28.7
30. 1
30.0
29.3
HOURS
26.7
27.4
28.0
24.2
26.3
29.8
26.2
25.3
24.6
26.8
1.5
1.7
1 .8
1.8
1.5
1.7
2. 1
1.5
1 .8
1.5
1 .8
1.7
.8
, 1
1 .9
1.5
1.6
1.9
2.3
1.9
2.0
2.2
2.0
2.2
2.0
2.3
1.9
2.5
2.4
2.0
1.6
1.6
1 .41
1.48
1 .46
,38
,34
,40
,26
,21
,34
,26
1 .37
1.36
. 13
.19
.20
. 16
.16
.36
.43
.47
.47
.45
.26
.30
. 18
.25
.44
.28
.24
. 18
.29
- 251 -
-------
APPENDIX P: TABLE II.
RUN 8: GAS FLOW HATES
PAGE 7 OF 12
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SF.C
12. 1330
1?. 1430
12. 1530
12. 1630
12. 1730
12. 1830
12. 1930
12.2030
1 2 . 2 1 30
12.2230
12.2330
13.0030
1 3 . 0 1 30
13.0230
13.0330
13.0430
13.0530
13.0630
13.0730
13.0830
13.0930
13. 1030
13. 1 130
13. 1230
13. 1330
13. 1430
13. 1530
13. 1630
13. 1730
13. 1830
13. 1930
13.2030
13.2130
13.2230
13.2330
14.0030
1 4 . 0 1 30
14.0230
14.0330
14.0430
353.
353.
353.
353.
353.
353.
353.
353.
353.
353.
353.
370.
370.
353.
353.
353.
353.
353.
353.
353.
353.
353.
353.
370.
371.
370.
370.
387.
386.
387.
38b.
388.
389.
389.
389.
389.
389.
389.
398.
399.
24.
50.
48.
34.
29.
22.
37.
33.
34.
31 .
31 .
27.
28.
44.
15.
21 .
17.
22.
21.
21.
21.
21 .
17.
17.
18.
15.
15.
13.
13.
13.
8.
8.
8.
5.
10.
10.
1 1.
5.
5.
5.
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.4
4.4
4.6
. 4.6
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
26.9
26.3
25.7
26.5
27.5
26.3
25.9
25.5
25.2
26.0
26.2
32.5
37.4
34.4
34.7
33.2
31.7
34.4
32.2
31 .6
31 .0
31.2
30.7
30.9
31 . 1
31.2 '
30.9
30.5
30.6
30.5
30.8
30.6
30.4
30.2
29.6
30.5
30.6
30.8
30.3
30.8
1.9 1
1.6 1
1.6 1
1.5
1.7
1 .6
1.5
1.6
1.5
1 .6
1 .7
1.7
2.0
1 .9
1.8
1 .9
1 .9
2. 1
3.5
2.7
2.5
1 .9
1 .7
1.7
1 .7
1 .6
1 .7
1 .7
1 .7
1.7
1.7
1.7
1 .6
1.8
1 .5
1 .5
1.8
1 .5
1 .5
1 .8
.31
.23
.21
.28
. 33
.27
.25
.24
.22
.25
.26
.56
.80
.65
.66
.59
.51
.65
1 .62
1 .55
1 .50
1 .50
1 .47
1 .49
1.51
1.51
.50
.47
. 48
.48
.49
.48
.46
.47
.43
1 .47
1 .49
1 .48
1 .46
1 .50
- 252 -
-------
APPENDIX P: TABLE II.
RUN til GAS FLOW RATES
PAGE 8 OF 12
DAY.HOUR
G A S
GASIFIER
AIR FLUE GAS
RATES M3/HR
PILOT REGENERATOR
PROPANE AIR NITROGEN
14.0530
M.0630
14.0730
14.0830
14.0930
14. 1030
1 4 . 1 1 30
14. 1230
14. 1330
14. 1430
14. 1530
14. 1630
14. 1730
14. 1830
14. 1930
14.2030
1 4 . 2 1 30
14.2230
14.2330
IS. 00 30
15.0130
15.0230
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
IS. 0930
15. 1030
15. 1 130
15. 1230
15. 1330
15. 1430
15. 1530
15. 1630
15. 1730
15. 1830
15. 1930
15.2030
397.
406.
406.
406.
389.
388.
388.
388.
388.
387.
388.
388.
405.
407.
407.
407.
408.
398.
390.
398.
407.
407.
407.
408.
406.
405.
387.
405.
405.
405.
387.
387.
387.
386.
385.
385.
386.
386.
404.
404.
5.
5.
5.
5.
5.
2.
2.
2.
2.
2.
2.
2.
2.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
1 1.
1 1.
1 1 .
10.
10.
10.
10.
10.
10.
1 1.
1 1.
8.
8.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
5.0
5.0
5.0
5.0
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
5.0
5.0
5.0
5.0
5.0
4.9
4.9
30.6
31.1
30.8
30.3
30.2
29.9
29.5
29.3
29.5
29.2
29.4
30.4
30.6
31 .3
31.0
31 .9
33. 1
33.6
32.8
34.2
37.0
38.9
39.7
39.1
39.7
39.8
39.8
39.0
38.0
37.7
36.6
35.3
34.8
33.8
32.3
30.7
29.8
30.3
30.6
30.5
.6
.4
.5
.5
.6
.5
. 4
. 5
. 5
. 5
. 5
.5
.5
1.6
1.6
1.7
1.8
1.9
1.8
2.2
1.8
2.5
2.2
1.8
1.8
1.8
2.2
1.9
.7
.8
.6
.6
.6
.5
.4
.3
.3
.3
.3
.4
.48
1.49
.48
.46
.46
.44
.42
.41
.42
.40
.41
.46
.47
.50
.49
.53
.60
.62
.59
.67
.78
.89
.92
.88
.90
.91
.92
.88
.81
.80
.75
.69
.66
.61
.54
.46
.43
.45
.47
.47
- 253 -
-------
APPENDIX F: TARLF II.
HUN 8: GAS FLOW RATES
PAGE 9 OF 12
DAY.HOUR
GAS
GASIFIFR
AIR FLUH GAS
RATES M3/HR RFGFN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/5EC
15.21 30
15.2230
15.2330
16.0030
1 6 . 0 1 30
16.0230
16.^330
16.0430
16.0530
16.0630
16.0730
16.0830
16.0930
16. 1030
1 6 . 1 1 30
16. 1230
16. 1330
16. M30
1 6 . 1 b 30
16. 1630
16. 1730
16.1 830
16. 1930
16.2030
1 6 . 2 1 30
16.2230
16.2330
17.0030
17.01 30
17.0230
17.0330
17.0430
17.0530
17.0630
17.0730
1 7.0830
1 /.0930
1 /. 1030
17.1 130
17. 1230
40 4 .
405.
405.
405 .
405.
405.
404.
404.
404.
404.
404.
404.
404.
404.
404.
404.
421.
360.
369.
404.
404.
404.
404.
404.
404.
352.
352.
352.
352.
369.
352.
352.
337.
337.
354.
371 .
372.
371.
37 1.
371.
8.
8.
8.
8.
8.
11 .
1 .
1 .
0.
1 .
1 .
2.
2.
88.
88.
91 .
63.
8.
13.
13.
13.
13.
13.
8.
5.
12.
9.
10.
10.
15.
5. '
15.
14.
14.
17.
13.
27.
59.
57.
52.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.5
30.5
31.5
31.0
32.0
32.6
34.4
31.3
29.6
31.7
32.8
32.2
30.3
30 . 1
32.0
33.7
32.0
31 .3
35.3
36.4
36.7
38 . 1
37.0
34.6
32.8
31.3
35.8
33.4 ;
26.3
29.0
27.9
33.4 ;
33.7 ;
30.0
28.5
34. 1
37.5
31.9
34.5
33.5
30 . 7
.4
.5 1
.^ 1
.5 1
.2 1
.8
.5
.8 1
.9 1
.6 1
.4
.6
.5
.5 1
.4
.4
.4
.5
.5
.7
.9
.8
.8
.6
.7
.7
>.0
.5
.5
.9
?.4
?.7
.5
1 .6
2.4
1.7
.5
1.3
2.5
P.0
.47
.52
.50
.54
.5'i
.66
.51
.14
.^4
.58
.54
.46
.44
.51
.60
.52
.49
.69
. 75
.77
.84
. 7R
.66
.S6
.51
.72
.63
.27
.40
.37
.63
.65
.43
.36
1 . 65
1.77
1 .52
1 .62
1 .64
1 .50
- 254 -
-------
APPENDIX F» TABLE II.
RUN 8: GAS FLOW RATES
PAGE 10 OF 12
DAY.HOUR
GAS
GASIFIER
AIR FLUF GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
17. 1330
17. 1430
17. 1530
17. 1630
17. 1730
17. 1830
17. 1930
17.2030
17.2130
17.2230
17.2330
18.0030
18.0 130
18.0230
18.0330
18.0430
18.0530
18.0 630
18.0730
18.0830
18.0930
18. 1030
18.1 1 30
18. 1230
18. 1330
18. 1430
18. 1530
18. 1630
18.1 730
Ib. 1830
18. 1930
18.2030
18.2130
18.2230
18.2330
19.0030
19.0130
19.0230
19.0330
19.0430
371.
370.
405.
370.
370.
371.
371.
388.
371.
371.
371.
371.
371.
371.
371.
371.
371.
371.
371.
372.
372.
372.
354.
354.
355.
355.
372.
372.
372.
372.
372.
514.
372.
372.
372.
372.
372.
372.
50.
42.
17.
16.
17.
MISSED
MISSED
15.
15.
17.
17.
23.
22.
19.
19.
16.
16.
20.
16.
17.
17.
16.
16.
16.
16.
15.
15.
12.
15.
15.
12.
15.
12.
12.
14.
15.
16.
16.
15.
16.
4.5
4.5
4.5
4.5
4.5
DATA
DATA
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
4.5
35.6
38.2
37.4
37.5
37.5
READING
READING
38.8
28.2
32.2
36.5
36.7
35.8
35.7
35.8
35.4
28.9
36.4
35.5
35.2
43.9
25.2
28.3
28.0
37.0
39.0
39.8
38.9
38. 1
36.0
36.8
36.6
37. 1
36.8
37.0
34.2
37.0
36.5
36.7
35.7
2.3
1.7
2. 1
1.5
2.1
2.5
2.2
2.0
1.7
1.5
1.5.
1 .6
1 .8
1.8
1.5
1.2
.9
1.7
1.5
1.4
1.3
1.4
1.5
1.4
1.6
1.6
1.5
1.7
2.7
3. 1
2.3
.6
.9
.7
2.0
.5
.5
1.5
.72
.84
.81
.78
.81
.86
.38
.57
.76
.74
.71
.70
.72
.69
.39
.72
.71
.68
>.06
.21
.35
.34
.76
.85
.87
.85
.80
.71
.77
.81
.80
.75
.77
.63
.77
.72
.71
.68
- 255 -
-------
APPENDIX F* TABLE II.
RUN 8* GAa FLOW HATES
PAGE 11 OF 12
DAY.HOUR
AIR
19.0530
19.0630
19.0730
19.0830
19.0930
19. 1030
19. 1 130
19. 1230
19. 1330
19. 1430
19. 1530
19. 1630
19. 1730
SHUT
21.0630
21.0730
21 .0830
21 .0930
21. 1030
21. 1 130
21. 1230
21 . 1330
21 . 1430
21 . 1530
21. 1630
21. 1730
21.1 830
2 1 . 1 930
21 .2030
21 .2130
21 .2230
21.2330
22.0030
22.0130
22.0230
22.0330
22.0430
372.
372.
355.
372.
372.
355.
354.
372.
337.
320.
320.
303.
389.
DOWN AT
370.
369.
369.
369.
371.
354.
353.
370.
354.
371.
371.
371.
354.
354.
388.
388.
389.
389.
391.
391.
391.
391.
391.
GAS
IER
UE GAS
16.
17.
15.
17.
17.
22.
15.
16.
14.
61.
67.
57.
61.
9. 1730
10.
10.
10.
16.
16.
10.
20.
18.
15.
19.
18.
18.
18.
18.
21.
14.
14.
14.
13.
14.
13.
13.
13.
RAT
PILOT
PROPANE
4.5
4.5
4.5
4.5
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
FOR 36
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
E S M.
REG:
AIR
35. 1
34.5
31.6
33.0
32.6
33.0
32.4
33.4
32.4
32.8
32.8
32.7
35.8
HOURS
31. 1
35.0
33.4
33.6
33.0
31.5
32.5
32.8
35. 1
35.4
35.7
35.7
35.7
34.7
38. 1
38.9
35.9
39.0
35.2
38.5
35.9
36. 1
35.7
M3/HR
NERATOR
NITROGEN
1.5
1.2
1.4
1.6
1.8
.8
.8
2.4
.6
.8
.8
.6
.8
,8
,3
,2
.4
.2
.5
,8
,2
,5
.2
1.2
1.2
1.4
1.8
2.2.
2.2
1.7
5.5
1.7
1.7
1.7
1.7
1.6
REGEN.
VELOCITY
M/SEC
.65
.62
.49
.57
.56
.59
.55
.62
.54
.56
.57
.55
.74
1.47
1 .66
61
,63
,59
,54
,59
,58
,70
,70
,71
,71
.72
,72
,86
1 .89
1.74
2.06
1.71
1 .86
1.74
1.75
1.72
- 256 -
-------
APPENDIX F« TABLE II.
RUN 8: GAS FLOW RATES
PAGE 12 OF 12
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
22.
22.
22.
22.
22.
22.
22.
22.
22.
22.
22.
0530
0630
0730
0830
0930
1030
1 130
1230
1330
1430
1530
391 .
391.
390.
390.
390.
397.
397.
362.
379.
379.
13.
13.
13.
13.
8.
7.
10.
9.
7.
10.
MISSED
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
DATA
34.
36.
35.
35.
34.
32.
30.
30.
30.
29.
READING
1
5
6
3
9
3
2
3
2
5
1
1
1
2
1
1
1
1
1
1
•
•
•
•
•
•
*
•
•
•
7
7
7
0
6
7
r~
5
5
5
•
•
•
•
•
•
•
*
•
•
66
77
72
73
70
59
47
48
47
43
22.1630
379.
0. 4.9 31.5
1.5
1 .53
- 257 -
-------
APPENDIX Pi TABLE III.
RUN 8: PBESSUHES PAGE
1 OF 12
GASIFIFR P. KILOPASCALS
DAY. HOUR
.0330
1 .0430
1 .0530
.0630
.0730
.0830
.0930
. 1030
. 1 130
. 1230
. 1330
. 1430
. 1530
. 1630
. 1 730
. 1830
. 1930
.2030
.2130
.2230
.2330
2.0030
2 . 0 1 30
2.0230
2.0330
2.0430
2.0530
2.0630
2.0730
2.0830
2.0930
2. 1030
2. 1 130
2.1230
2. 1330
2. 1430
2. 1530
2. 1630
2. 1730
2. 1830
GAS
SPACE
2.2
2.3
2.4
2.2
2.2
2.2
2.1
2. 1
2. 1
2.2
2.3
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.6
2.5
2.3
2.2
2.2
2.5
2.4
2.2
2.2
2.2
2.2
2.2
2.2
2.5
2.5
2.5
2.4
2.5
2.5
DISTRIB.
D.P.
1 .9
2.0
2. 1
2. 1
2.2
2.1
2.2
2. 1
2.2
2. 1
2.2
2.2
2. 1
2.1
2. 1
2. 1
2. 1
2.1
2.0
2.1
2.1
2. 1
2.2
1 .9
1.9
1 .9
1 .9
1 .9
2.0
1.9
1.9
1.9
2.2
2.2
2. 1
2. 1
2.5
2.5
2.5
2.5
BED
D.P.
5.4
5.6
5.8
6.1
6.3
6.5
6.5
7.3
7.2
7.5
7.6
7.7
7.8
8.0
8.2
9.0
9.0
9.2
9.2
9.2
9.2
9.3
9.2
'9.3
9.8
9.8
9.6
9.5
9.8
9.5
9.7
9.8
10.1
10.0
9.2
9.3
9.3
9.1
8.8
8.8
GASIFIFR
BED
SP. GR.
1.00
1.00
1.00
0.95
1.00
1 .00
1 .00
.00
0.98
0.95
1 .00
0.95
0.98
1.00
0.96
.00
.00
.00
.00
.00
.00
1 .00
1 .00
1 .02
1 .02
1 .05
1 .00
1 .00
0.97
0.97
1 .00
1 .02
1.02
.00
1 .00
0.98
0.98
1 .00
1 .00
1.02
REOEN.
BED
D.P.
4.7
4.7
5.4
5.5
6.5
7.0
7.0
7.0
7.0
7.0
6.5
7.0
7.2
7.5
8.0
7.5
8.0
8.7
7.5
8.0
8.7
8.5
8.0
7.5
8.7
8.2
8.7
8.7
9.2
9.2
9.0
8.7
9.0
8.7
8.2
8.5
8.7
8.7
8.5
8.0
- 258 -
-------
APPENDIX » TARLF III.
RUN 8: PRESSURES PAGE
2 OF 12
OASIFIER P. KILOPASCALS
DAY. HOUR
2. 1930
2.2030
2 . 2 1 30
2.2230
2.2330
3.0030
3 . 0 1 30
3.0230
3.0330
3.0430
3.0530
3.0630
3.0730
3.0830
3 . 0 930
3. 1030
3. 1 130
3. 1230
3.1330
3. 1430
3. 1530
3. 1630
3. 1730
3. 1830
3. 1930
3.2030
3.2130
3.2230
3.2330
4.0030
4.0130
4.0230
4.0330
4.0430
4.0530
4.0630
4.0730
4.0830
4.0930
4. 1030
GAS
SPACE
2.7
2.8
2.8
2.9
2.9
2.9
3.1
3.5
4. 1
4.2
4. 1
4.4
4.2
4.6
4.2
3.5
3.5
3.4
3.4
3.4
3.2
3. 1
3.2
3.2
3.2
3.
3.
3.
3.
3.
3.
3.0
3.0
2.9
2.9
2.9
2.9
3.0
3.0
3.0
DISTRIB.
D.P.
2.5
2.7
2.7
3.2
3.0
2.9
3.1
3.1
4.7
4.5
4.7
4.7
5.0
5.0
4.2
3.0
3.0
2.7
2.7
2.7
2.6
2.6
2.7
2.7
2.7
2.6
2.6
2.9
2.6
2.7
2.6
2.6
2.6
2.7
2.7
2.7
2.7
2.7
2.6
2.6
BED
D.P.
8.7
8.5
8.2
8.5
8.5
8.3
7.7
7.8
7.5
7.2
7.3
7.3
7.1
6.7
6.0
6.0
5.7
6.0
6.2
6.6
6.8
7.2
7.3
7.3
7.3
7.6
7.6
7.6
7.7
7.8
8.0
8. 1
8. 1
8.3
8.6
9. 1
8.7
8.6
8.7
8.5
OASIFIER
BFD
SP. GR.
1.02
0.98
0.92
0.97
0.97
1.03
0.95
1.00
0.97
1.05
0.97
1.05
0.93
0.95
0.95
0.98
1.00
0.98
1.00
1 .00
1.02
1 .00
1.00
0.98
1.00
1.00
1.00
0.95
1 .00
1.00
1.00
1 .00
1.00
0.95
0.97
0.95
0.95
1.00
1 .00
1.00
REGEN.
BFD
D.P.
8.2
8.5
7.5
7.5
8.5
7.7
7.5
7.5
8.5
7.5
7.5
7.5
7.0
7.0
6.0
5.0
5.5
6.0
6.0
6.2
6.7
7.2
7.2
7.0
7.2
7.0
7.0
6.5
7.0
7.5
7.5
7.0
7.5
7.5
8.0
8.5
7.5
8.0
7.5
7.0
- 259 -
-------
APPENDIX & TABLE III.
RUN 8* PRESSURES PAGE
3 OF 12
GASIFIER P. KILOPASCALS GASIFIER
DAY. HOUR
4 . 1 ] 30
4. 1230
4. 1330
4. 1430
4. 1530
4. 1630
4. 1730
4. 1830
4. 1930
4.2030
4.2130
4.2230
4.2330
5.0030
5.0130
5.0230
5.0330
5.0430
5.0530
5.0630
5.0730
5.0830
5.0930
5. 1030
5 . 11 30
5. 1230
5. 1330
5. 1430
5. 1530
5. 1630
5. 1730
5. 1830
5. 1930
5.2030
5.2130
5.2230
5. 2330
6.0030
6.0130
6.0230
GAS
SPACE
3.0
3. 1
3.1
3.0
3.0
3.1
2.9
2.9
2.8
2.9
2.7
2.9
3.0
2.9
2.9
2.9
2.9
2.7
2.9
2.9
2.9
2.7
3.0
3.4
3. 1
3.2
3.0
3.0
3.1
3.0
2.9
2.9
2.9
2.9
2.7
2.6
2.5
2.6
DISTRIB
D.P.
2.6
2.7
2.7
2.7
2.7
2.7
2.7
2.6
2.6
2.6
2.6
2.6
2.6
2.7
2.7
2.7
2.7
2.2
2.2
2.2
2.2
2.0
MISSED
M I SSED
2.2
2.5
2.4
2.5
2.2
2.2
2.2
2.2
2.2
2.5
2.2
2.2
2.2
2.2
2.0
2.0
RED
D.P.
8.2
8. 1
8.4
8.4
8.7
8.5
8.5
8.7
8.7
8.7
8.b
9.0
9.0
9.1
9.1
9.2
9.3
9.5
9.5
9.5
9.3
9.5
DATA READING
DATA READING
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.3
9.3
9.3
9.2
9.2
9.5
9.7
9.7
9.5
BED
SP. OR.
1.00
1 .00
1.00
1 .00
1 .05
1.05
1. 10
1 . 10
1. 10
. 15
1. 15
1.20
1. 10
1 . 10
1. 10
1. 10
I. 15
0.90
0.90
0.90
0.90
1 .00
0.95
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
0.90
1.00
1.00
.00
REGEN .
BED
D.P.
6.5
6.2
6.2
6.2
6.2
7.2
8.2
8.2
b.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.5
9.5
9.5
9.5
9.5
9.5
9.5
9.0
9.5
9.5
9.5
9.5
9.5
9.5
9.5
9.5
9.5
9.5
- 260 -
-------
APPENDIX F» TABLF III.
RUN 81 PRESSURES PAGE
4 OF 12
DAY. HOUR
6.0330
6.0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6 . 1 1 30
6. 1230
6. 1330
6. 1430
6. 1530
6. 1630
6. 1730
6. 1830
6. 1930
6.2030
6.2130
6.2230
6.2330
7.0030
7.0130
7.0230
7.0330
7.0430
7.0530
7.0630
7.0730
7.0830
7.0930
7. 1030
7 . 1 1 30
7. 1230
7. 1330
7. 1430
7. 1530
7. 1630
7 . 1 730
7. 1830
GASIFIER P. KILOPASCALS GASIFIER
GAS D I STRIP. BED BED
SPACE D.P. D.P. SP. GR.
2.6 2.5 9.6 0.90
2.7
2.6
2.6
2.6
2.5
2.6
2.9
2.6
2.7
2.7
2.7
2.7
2.9
2.9
3.0
3.0
3.0
2.6
2.7
2.7
2.7
2.7
2.7
2.6
2.9
2.7
2.7
2.6
2.7
2.9
3. 1
3.0
2.9
2.9
2.9
3.0
3.0
2.6
2.6
2.2
2.5
2.0
2.2
2.2
2. 1
2.0
2.1
2.0
2.0
2.0
2.0
2.0
2.0
2.2
2.0
2.0
2.0
2.0
2.1
2.2
2.2
2.2
2. 1
2.2
2.2
2.2
2.2
2.2
2.2
2.5
2.4
2.5
2.4
2.5
2.5
2.5
2.1
2. 1
9.6 0 . 95
9.7 1.00
9.8 1.00
10.0
10.0
9.7
9.2
9.7
9.7
9.7
9.7
9.7
9.3
9.2
9.2
9.2
9.5
9.3
9.5
9.5
9.5
9.5
.00
.00
.00
.00
.00
.00
.00
.00
.05
.05
. 10
.00
.00
.00
.00
.00
.00
. 10
.00
9.5 1.00
9.5 0.90
9.5 0.90
9.5 0.90
9.3 1.00
9.5 1.00
9.1 1.00
9.1 1 . 00
9.1 1.00
9.2 0.95
9.2 0.95
9.1 1.00
9.0 1.00
9.0 1.00
9.0 1.00
9.1 1.00
9.1 0.95
RFGEN
RFD
D.P.
9.5
9.5
9.5
9.5
9.5
9.5
9.5
9.5
10.0
10.0
10.0
10.0
10.0
9.3
9.2
9.2
9.2
10.0
10.0
9.5
10.0
10.0
9.2
9.7
9.5
9.2
9.5
10.0
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
- 261 -
-------
'PAGE 5 OF 12
GASIFIER P. KILOPASCALS
DAY. HOUR
7. 1930
7.2030
7.2130
7.2230
7.2330
8.0030
8.0130
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8.0930
8. 1030
8. 1 130
8. 1230
8. 1330
8. 1430
8. 1530
8. 1630
8. 1730
8. 1830
8 . 1 930
8.2030
8.2130
8.2230
8.2330
9.0030
9.0130
9.0230
9.0330
9.0430
9.0530
9.0630
9.0730
9.0830
9.0930
9. 1030
GAS
SPACE
2.6
2.6
2.7
2.7
2.9
3.2
3.2
3.4
3.1
3. 1
3.?
3.2
3.2
3. 1
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.1
3.4
3.6
3.6
3.5
3.6
3.5
3.6
3.6
3.6
3.5
3.5
3.5
3.4
3.4
3.3
3.5
DISTRIB.
D.P.
2.0
2.0
1.9
1.9
2.1
2.5
2.5
2.4
2.4
2.5
2.5
2.5
2.4
2.5
2.6
2.6
2.5
2.5
2.4
2.4
2.4
2.4
2.4
2.5
2.9
3.0
3.0
2.7
2.8
2.7
2.8
2.6
2.7
2.6
2.6
2.6
2.5
2.5
2.6
2.4
BED
D.P.
9.0
9.1
9.2
9.2
9.2
9. 1
9.2
-9.2
9.2
9.3
9.2
9.3
9.3
9.2
9.2
9.2
9. 1
9.0
9.0
9.0
9.0
9.0
9.0
9.0
7.8
7.5
7.5
7.7
7.7
7.5
7.5
7.5
7.5
7.7
7.6
7.6
7.7
7.7
7.6
7.6
GASIFIER
BED
SP. GR.
0.92
0.91
0.89
0.86
0.88
0.99
0.96
1 .00
0.98
1 .00
0.98
1 .00
1 .00
0.85
0.98
0.94
0.97
1 .00
1.02
1.00
1 .00
0.98
0.98
1.00
0.97
0.97
0.98
0.98
.00
.00
.00
.00
.00
0.98
1.00
1 .00
1.00
1.00
0.96
0.97
HEGEN
RED
D.P.
8.7
8.7
8.7
8.7
9.0
8.7
9.2
9.2
9.2
9.5
9.0
9.2
9.0
9.0
8.7
8.7
8.7
8.7
9.0
8.7
8.7
8.7
9.0
9.0
7.5
7.2
6.7
6.5
7.0
7.2
7.2
6.7
6.5
6.5
6.5
6.7
6.7
6.7
7.0
7.0
- 262 -
-------
APPENDIX Ft TABLE III.
RUN 8: PRESSURES PAGE
SHUT DOWN AT 9.2230 FOR 23 HOURS
SHUT DOWN AT 11.0730 FOR 19 HOURS
6 OF 1?
DAY. HOUR
9. 1 130
9. 1230
9. 1330
9. 1430
9. 1530
9. 1630
9.1730
9. 1830
9. 1 930
9.2030
9.2130
9.2230
GASIFIER P. KILOPASCALS
GAS DISTRIB. BED
SPACE
3.5
3.5
3.6
3.7
3.9
3.9
4.0
4.0
4.2
4.5
5.2
6.2
D.P.
2.5
2.4
2.4
2.4
2.4
2.2
2.2
2.2
2.2
2.2
2.1
2.0
D.P.
7.5
6.7
6. 1
6.1
5.2
5.4
5.4
5.5
5.5
5.5
5.5
5.7
GASIFIER
BED
SP. GR.
1 .00
1 .00
0.97
1 .02
0.98
1 .00
1 .00
1.05
0.95
1.00
0.97
1.00
REGEN
BFD
D.P.
7.2
7.0
• • V.J
5.5
5. 5
5.0
5 7
_y • r
5.7
6.0
5.0
5.0
5.0
5.0
0.2230
0.2330
.0030
.0130
.0230
.0330
.0430
.0530
.0630
1.0730
2.7
2.7
2.6
2.6
2.7
2.7
2.9
3.0
3. 1
3.1
3.0
2.9
2.7
2.6
2.6
2.6
2.6
2.6
3.0
3.0
6.8
7.2
7.2
7.5
7.6
7.7
7.6
7.5
7.5
7.5
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
7 8
f • \~s
8.0
8.0
8.0
8.0
7.5
7. 5
7.5
7.5
7.5
12.0330
12.0430
12.0530
12.0630
12.0730
12.0830
12.0930
12. 1030
1 2 . 1 1 30
12. 1230
2.7
3.0
2.7
2.7
2.7
2.5
2.5
2.7
2.5
2.7
2.2
2.7
2.2
2. 1
2.1
2.2
2.5
2.2
2.2
2. 1
7.2
7.0
7.0
7.0
7.0
6.8
7.0
7.2
7.5
7.5
1 .00
.00
.00
.00
.00
.00
.00
. 10
.00
. 10
9.0
8. 7
8.7
8.7
8. 7
8. ?
V-1 • f .
7.5
7.5
i • *
7.5
7.5
- 263 -
-------
DAY.HOUR
12.
12.
12.
12.
12.
12.
12.
12.
12.
12.
12.
13.
13.
13.
13,
13.
13.
13.
13,
13.
13,
13.
13.
13,
13.
13,
13,
13.
13,
13.
13,
13.
13,
13,
13,
14,
14,
14,
14,
1330
1430
1530
1630
1730
1830
1930
2030
2130
2230
2330
0030
0130
0230
0330
0430
0530
0630
0730
0830
0930
1030
1 130
1230
1330
1430
1530
1630
1730
1830
1930
2030
2130
2230
2330
0030
0130
0230
,0330
APPENDIX Pi TABLE III.
RUN 8i PRESSURES PAGE
GASIFIER P. KILOPASCALS
GAS DISTRIB. BED
SPACE D.P. D.P.
7 OF 12
14.0430
2.6
2.6
2.6
2.6
3.0
2.9
2.9
2.9
3.0
3.0
3.0
3. 1
3.
3.
3.
3.
3.
3.
3.
3.
3.
3,
3,
3.2
3.2
3.2
3.4
3.4
3.2
3.2
3.2
3.2
3.2
3. 1
3. 1
3. 1
3. 1
3. 1
3. 1
3.1
2.1
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.1
2.1
2,
2,
2,
2
2
0
0
0
2.0
2.0
0
1
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.1
2.4
2.2
2. 1
2. 1
2.2
2.2
7.7
8.0
8.0
8.5
8.5
8.5
8.7
8.7
9.1
8.7
8.7
8.7
8.7
8.8
9.0
8.7
8.5
8.7
8.5
8.6
8.6
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.8
8.8
8.8
8.8
8.8
8.8
9.0
GASIFIFR
BED
SP. OR.
1.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
0.98
0.-95
1.00
1 .00
1.00
1 .00
0.98
0.98
1 .00
.00
.00
.00
.00
.00
.00
.00
.00
.00
0.97
REGEN.
BED
D.P.
7.5
7.5
7.5
9.0
9.0
8.7
8.0
8.2
8.2
8.2
8.2
6.2
7.5
8.5
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
9.0
9.0
9.0
9.0
8.7
8.7
8.7
8.7
- 264 -
-------
APPENDIX Pi TABLE III.
RUN 8: PRESSURES PAGE
8 OF 12
OASIFIER P. KILO PASCALS
DAY. HOUR
14.0530
14.0630
14.0730
14.0830
14.0930
14. 1030
14. 1 130
14. 1230
14. 1330
14. 1430
14. 1530
14. 1630
14; 1730
14. 1830
14. 1930
14.2030
14.2130
14.2230
14.2330
15.0030
15.0130
15.0230
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
15.0930
15. 1030
15. 1 130
15. 1230
15. 1330
15. 1430
15. 1530
15. 1630
15. 1730
15. 1830
1 5 . 1 930
15.2030
GAS
SPACE
3.1
3. 1
3.1
3. 1
3.2
3.4
3.4
3.5
3.5
3.5
3.5
3.5
3.5
3.5
3.7
3.8
3.2
3.2
3.4
3.4
3.4
3.4
3.4
3.4
3.4
3.4
3.4
3.4
3.6
3.4
3.4
3.5
3.5
3.5
3.4
3.4
3.5
3.5
3.5
3.5
DISTRIB.
D.P.
2.2
2.2
2.2
2.2
2.4
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.5
2.2
2.4
2.4
2.2
2. 1
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
2.
2.
2.
2.
2.
2.
2.
2.2
BED
D.P.
8.8
8.7
8.7
8.7
8.7
8.8
8.7
8.7
8.7
8.7
9.0
9.0
9.0
9.0
9.0
9.0
8.7
8.7
8.6
8.6
8.7
8.6
8.7
8.7
8.7
8.6
8.6
8.7
8.7
8.7
8.7
9.0
9.2
9.3
9.5
9.7
10.0
9.8
10.2
10. 1
OASIFIER
RED
SP. GR.
1.00
1.00
1.00
1.00
0.98
0.98
1.00
1.00
1 .00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
1.05
1.00
1 .00
1.03
.00
.00
.00
.00
.00
.00
.02
0.95
0.95
.00e>
1.00
1.00
1.00
1.00
1.00
REGEN
RED
D.P.
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
b.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
9.0
9.0
9.2
9.5
9.7
10.0
10.0
10.2
10.2
- 265 -
-------
APPENDIX F: TABLE III.
RUN 8» PRESSURES PAGE
9 OF 12
GAS1FIER P. KILOPASCALS GASIFIER
DAY. HOUR
15.2130
15.2230
15.2330
16.0030
16.0130
16.0230
16.0330
16.0430
16.0530
16.0630
16.W730
16.0830
16.0930
16. 1030
16. 1 130
16.1230
16. 1330
16. 1430
16. 1530
16. 1630
16. 1730
16. 1830
16. 1930
16.2030
16.2130
16.2230
16.2330
17.0030
17.0130
17.0230
17.0330
17.0430
17.0530
17.0630
17.0730
17.0830 '
17.0930
17. 1030
17. 1 130
17. 1230
GAS
SPACE
3.2
3.2
3.2
3.2
3.4
3.4
3.2
3.4
3.4
3.4
3.5
3.5
4.1
4.1
4.0
4. 1
4.1
3.4
3.1
3.2
3.2
3.4
3.4
3.7
3.4
3.1
3.0
3.0
3.0
3.0
3.2
3.5
3.5
3.5
3.5
3.9
4.4
4.4
4.4
4.1
DISTRIB.
D.P.
2. 1
2.2
2.1
2.2
2.2
2.2
2.1
2. 1
2.1
2.1
2. 1
2. 1
2.2
2.7
2.7
2.7
2.7
2.0
2.0
2.0
2.0
2.2
2.2
2.2
2.2
2.0
2.0
1.5
1.7
2.0
2.0
2.0
1 .9
1.9
2.0
2.1
2.5
2.2
2.4
2.4
RED BED
D.P. SP. GR.
9.8 0 . 97
10.0 0.97
10.0 1.00
9.8 0.95
9.8 0.97
9.7
10.0
-9.8
10.0
10,0
10.0
10.0 Q
10.0
9.5
9.5
9.2
9.2
9.3
9.5
9.3
9.3
9.3
.00
.00
.00
.00
.00
.00
5.95
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
9.3 1 . 00
9.3 1.00
9.5 1.00
9.2 1 . 00
9.7 1.00
10.0 0.90
10.2 0.90
10.2 .00
10.5 .00
10.2 .00
10.2 .00
10.0 .00
10.0 .00
10.1 .00
10.0 .00
9.7 .00
9.6 .00
•9.8 .00
REGEN
BED
D.P.
10.5
10.0
10.0
10.0
10.0
10.0
10.5
10.5
10.0
10.0
10.0
10.0
10.0
7.5
8.7
8.7
8.7
8.7
7.5
8.7
9.5
9.2
9.2
9.2
9.7
7.5
8.7
8.7
8.2
9.2
10.5
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
- 266 -
-------
APPENDIX P.I TABLE III.
RUN 8: PRESSURES PAGE
10 OF 12
DAY. HOUR
17,, 1330
17. 1430
17. 1530
17. 1630
17. 1730
17. 1830
17. 1930
17.2030
17.2130
17.2230
17.2330
18.0030
18.0130
18.0230
18.0330
18.0430
18.0530
18.0630
18.0730
18.0830
18.0930
18. 1030
18. 1 130
18. 1230
18. 1330
18. 1430
18. 1530
18. 1630
18. 1730
18. 1830
18. 1930
18.2030
18.2130
18.2230
18.2330
19.0030
19.0130
19.0230
19.0330
19.0430
GASIFIl
GAS
SPACE
4. 1
4.2
4. 1
4. 1
4.2
4.5
4.2
3.9
3.7
3.9
3.9
3.9
3.7
3.7
3.7
3.4
3.6
3.7
4.1
4.4
4.4
4.4
4.4
4.4
4.4
4.4
4.5
4.9
4.6
4.6
4.5
4.2
4.5
4.6
4.6
4.6
4.5
4.5
ER P. KI
DISTRI
D.P.
2.2
2.2
2.1
2.1
2.1
MISSED
MISSED
2.0
2.2
2.0
2.0
1 .9
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.1
2.2
2.0
2.0
2.0
2.0
2.0
1.9
1.7
2.0
1.7
1.7
LOPASCALS
B. BED
D.P.
9.6
10.0
9.7
10.0
10.0
DATA READI
DATA READI
9.3
9.5
9.6
9.7
9.6
9.7
10.0
10.1
10.0
10.2
10.5
10.5
10.5
10.0
10.2
10.1
10. 1
10.2
10.2
10.0
9.5
9.2
9.1
8.7
8.7
8.8
9.0
8.7
8.7
8.8
9.2
9.6
9.7
GASIFIER
BED
SP. GR.
.00
.00
.00
.00
.00
NG
NG
1 .00
0.95
1.00
0.90
0.90
0.90
0.90
1 .00
0.90
0.90
0.90
0.95
0.85
.00
.00
.00
.00
.00
1.00
1.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.05
.00
REGEN.
BFD
D.P.
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.0
8.2
8.7
10.0
9.2
8.7
8.7
8.0
8.7
10.5
10.0
10.0
8.7
«.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
8.7
7.5
8.0
8.7
- 267 -
-------
APPENDIXF* TABLE
RUN 8» PRESSURES
III.
PAGE II OF 12
DAY.HOUR
GASIFIER
GAS
SPACE
19.0530
19.0630
19.0730
19.0830
19.0930
19. ,1030
1 9 . 1 1 30
19. 1230
19. 1330
19. 1430
19. 1530
19. 1630
19.1730
SHUT
21.0630
21.0730
21.0830
21.0 930
21. 1030
2 1 . 1 1 30
21. 1230
21. 1330
21. 1430
21 . 1530
2 1 . 1 630
21 . 1730
21.1 830
21. 1930
21.2030
21.2130
21.2230
21.2330
22.0030
22.0130
22.0230
22.0330
22.0430
4.6
4.7
4.7
4.5
4.5
4.4
4.9
4.7
4.6
4.6
4.5
4.6
5.2
DOWN AT
2.5
2.5
2.5
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.5
2.6
2.6
2.6
2.7
3.0
3.0
3.0
3.0
3.0
R P. KILOPASCALS GASIFIER
DISTRIB.
D.P.
1.7
2.0
2.0
2.0
2.1
2.0
2.0
2. 1
2.0
2.0
2.0
2.0
2.2
9. 1730 FOR
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.4
2.5
2.4
2.6
2.6
2.7
2.7
3.0
3.0
3.0
2.9
2.9
- 268
BED BED
D.P. SP. GR.
10.0 1.00
10.1 1.00
10.1 1.05
10.2 0.90
10.5 .00
10.7 .00
10.7 .00
10.8 .00
10.7 .00
10.7 .05
11.1 .05
10.9 .00
10.9 .05
36 HOURS
9.6
9.5
9.5
9.3
9.2
9.2
9.3
9.3
9.5
9.5
9.3
9.3
^.3
9.3
9.5
9.5
9.5
9.5
9.5
9.5
9.3
9.3
9.3
.00
.00
.00
.00
.00
.05
.05
.05
.05
.05
.05
.05
.05
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
_
REGEN.
RFD
D.P.
8.7
8.7
8.7
8.7
10.0
10.5
1£.0
10.0
9.5
10.0
10.5
10.5
10.5
1 1.2
9.2
9.0
8.0
9.0
10.0
8.7
1v5.0
8.0
9.5
8.0
8.0
9.0
9.5
8.7
8.5
8.2
8.2
8.2
8.2
8.5
8.5
8.5
-------
DAY.HOUR
APPENDIX Pi TABLE III.
RUN 8* PRESSURES PAGE 12 OF 1?
GASIFIER P. KILOPASCALS GASIFIER REGEN.
GAS DISTRIB. BED BED BFD
SPACE D.P. D.P. SP. GR. D.P.
22.0530
22.0630
22.0730
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1330
22. 1430
22. 1530
22. 1630
3.0
3.0
3.0
3.0
2.6
2.5
2.5
2.5
2.6
3. 1
2.5
3.0
2.9
2.9
3.0
3.0
2.7
2.7
2.7
2.7
2.7
MISSED
2.6
9.3
9.2
9.3
9.3
9.3
9.2
9.2
9.2
9.2
9.2
DATA READING
9.2
.00
.00
.00
.00
.00
.00
.05
.05
.00
.00
.00
8.5
8.5
8.7
8.7
8.7
8.7
8.7
8.7
0.
0.
0.
- 269 -
-------
RUN 8:
APPENDIX F: TABLE IV.
DESULPHURISATION PERFORMANCE PAGE
1 OF 12
DAY. HOUR
.0330
.0430
.0530
.0630
.0730
.0830
.0930
. 1030
.1 130
.1230
.1330
. 1430
. 1530
. 1630
. 1 730
. 1830
. 1930
.2030
.2130
1.2230
1 .2330
2.0030
2.0,130
2.0230
2.0330
2.0430
2.0530
2.0630
2.0730
2.0830
2.0930
2. 1030
2.1 130
2.1230
2.1330
2. 1430
2. 1530
2. 1630
2.1730
2 . 1 830
SULPHUR GAS
REMOVAL VEL.
% M/S
68.4
71.6
77.6
79.3 1
81.2
82.3
80.9
81.7
84.6
85.2
85.3
86.5
86.5
87.4
87.8
87.9
88.3
87.9
87. >9
87.8
87.7
88.2
88. 1
87.5
89. 1
88.9
88.6
89. 1
&9.4
89.3
89.4
89.9
89.6
89.8
89.4
88.2
88.3
85.5
83.0
82.3
.45
.5t
.48
.53
.56
.70
.65
.67
.67
.68
.87
.87
.84
.79
.79
.78
.72
.68
.70
.75
.73
.65
.73
.56
.50
.50
.54
.53
.61
.64
.62
.59
.64
.72
.72
,7$
.70
.73
. 7b
.75
G-BED
DEPTH
CENTIM
54.
57.
59.
65.
64.
66.
66.
74.
75.
80.
77.
82.
81.
81.
87.
91.
91 .
93.
93.
93.
93.
95.
93.
93.
98.
95.
97.
96.
103.
99.
99 .
98.
100.
101.
93.
97.
97.
92.
90.
88.
AIR/
FUEL
% ST.
20.7
21.8
22.3
23.0
23.3
25.5
24.7
25.3
25.8
25.4
27.2
27.5
27.5
27.0
28.5
26.7
27.4
27.4
27.0
27.8
27.2
26. 1
27.3
26. 1
25.7
26.4
26.5
26.4
27.4
27.3
26.9
26.6
26.9
27.2
26.9
28.0
27.9
28.3
28. 1
27.6
CAO/S
RATIO
MOL.
0.83
1 .87
2.36
2.25
2. 19
2.08
2.07
2.65
2.95
2.62
3.32
2.62
2.59
3.16
3.68
3.48
3.84
2.65
. 2.67
2.26
2.22
2.09
2.43
2.62
3.42
4.43
3.66
2.88
2.64
2. 19
2.54
2.35
3.02
2.53
1.69
2.63
3.62
2.85
2.71
2.36
% CAS
TO CAO
19.8
42.0
52.4
56.7
53.1
48.7
46.3
42.8
32.0
36.7
32.1
32.1
31.2
28.2
29.4
25.6
59.2
62.2
76.8
89.9
82.9
85. 1
95.8
95.0
86. 1
108.9
104.5
64.7
86.5
87.2
89.7
10,1.8
66.5
70.8
59.9
59.2
50. 1
50.1
41.1
46.6
RE GEN.
S OUT %
OF FFD
19.0
44.9
49.5
58.4
59.9
61.7
48.7
35.2
29.8
32.2
38.4
40.4
37.0
28.6
28.1
20.5
62.9
54.4
68.5
83.4
88.7
90.8
08.3
28.6
17.4
18.4
12.3
98.9
93.2
107.4
121.0
105.8
66.7
73.7
80.2
84.4
66. 1
71.1
52.6
68.6
- 270 -
-------
RUN 8:
APPENDIX F: TABLE IV.
DESULPHURISATION PERFORMANCE PAGE
2 OF 12
DAY. HOUR
2. 1930
2.2030
2 . 2 1 30
2.2230
2.2330
3.0030
3 . 0 1 30
3.0230
3.0330
3.0430
3.0530
3.0630
3.0730
3.0830
3 . 0 930
3. 1030
3. 1 130
3.1230
3. 1330
3. 1430
3. 1530
3. 1630
3. 1730
3 . 1 830
3. 1930
3.2030
3.2130
3.2230
3.2330
4.0030
4 . 0 1 30
4.0230
4.0330
4.0-430
4.0530
4.0630
4.0730
4.0830
4.0930
4. 1030
SULPHUR GAS
REMOVAL VEL.
% M/S
79.0 •'(*
81.6 .93
84.8 .bV
83.7 .98
81.5 .b9
82.6 2.00
82.7 1.9b
81.3 2.00
82.4 2.43
78.3 2.51
74.3 2.51
71.9 2.5Q
68.4 2.70
64.2 2.65
54.4 2.48
57.6
66.9
67.0
70.6
75.2
77.6
78.4
79.6
76.7
76.6
77.7
79. 1
77.5
80.2
83.4
85. 1
84.7
83.5
84.8
86.4
86.5
, 84.9
82.9
83.4
83.4
.81
.89
.W3
.bl
.84
.b3
.86
.07
.89
.87
.81
.83
.b4
.78
.68
.68
.73
.72
.75
.76
.78
.76
.75
.75
.75
G-BED
DEPTH
CENTIM
8/.
88.
91.
89.
89.
82.
82.
80.
78.
70.
77.
71.
77.
72.
64.
62.
58.
62.
63.
67.
68.
73.
74.
76.
74.
77.
77.
81.
78.
80.
81.
82.
82.
89.
90.
97.
93.
87.
88.
86.
AIR/
FUEL
% ST.
27.5
26. 1
27.2
29.7
29.5
28.4
26.4
25.6
26.9
26.3
26.4
26.4
26.4
25.8
24.2
20.8
22.7
22.9
24.0
24.3
25.6
25.6
27.4
24.3
26.5
26.5
25.6
25.0
25.4
24.6
24.6
25.5
25.5
25. -9
26.7
26.7
26.2
27.2
26.4
26.8
CAO/S REGEN.
RATIO % CAS S OUT %
MOL. TO CAO
2.37
1.37
1 .64
4.90
5.32
2. 16
1 . 13
1 .60
1.55
1 .22
1 .0-9
1.09
0.73
0.63
0.80
0.99
0.69
1 .01
1.99
2.84
2.49
2.88
2.31
2.26
3.30
3. 13
3.31
2.64
3.46
0.61
2.65
2. 19
3.58
3.66
3.73
1.49
1 .06
1 .70
2. 10
0.80
51.1
55.5
55.8
42.6
39.0
43.5
37.8
34.9
54. 1
47.1
47.1
56.8
48.7
65.4
56.2
56.5
56.9
53.9
53.2
57.3
59.2
51.4
52.2
56.8
55.4
57.5
56.0
61 .0
58.0
64.5
64.6
57.9
55.8
58.0
47.2
46.6
62.0
63.8
63.4
62.6
OF FED
70.7
75.8
60.9
51.5
49.0
56.6
46.3
39.9
58.8
48.7
49. 1
60.6
54.5
80.8
70.9
75.4
72.7
72.4
69.9
69.4
68.5
59. 1
72.4
67.6
66.3
72. 1
66.6
75.4
73.3
81.6
81.8
67.6
65.7
69.3
55.8
54.4
75.?
78.8
78.6
78.4
- 271 -
-------
RUN 8»
APPENDIX Pi TABLE IV.
DESULPHURISATION PERFORMANCE PAOE
3 OF 12
DAY. HOUR
4 . 1 1 30
4. 1230
4. 1330
4. 1430
4.1530
4. 1630
4 . 1 730
4 . 1 830
4. 1930
4.2030
4.2130
4.2230
4.2330
5.0030
5.0130
5.0230
5.0330
5.0430
5.0530
5.0630
5.0730
5.0830
5.0930
5. 1030
5. 11 30
5. 1230
5. 1330
5. 1430
5. 1530
5. 1630
5.1730
5 . 1 830
5 . 1 930
5.2030
,5.2130 -
5.2230
5.2330
6.0030
.6.0130
6.0230
SULPHUR GAS
REMOVAL VEL.
% M/S
81.9
79.5
79.0
78.7
78.7
79.0
78.3
79. 1
79.8
80.0
81.0
80.6
81.7
82.0
82.6
82.7
82. 1
82.7
82.8
83. 1
82.7
82.5
.75
.76
.73
.73
.72
.72
.6b
.70
.68
.68
.76
.64
.70
.72
.72
.70
.72
.64
.62
.65
.66
.59
77. 1
78.0
76.3
76.5
77.5
77.7
78.0
78.3
79.9
77.4
76. 1
75.5
78. 1
78.0
79.3
.67
.89
.87
.67
.54
.53
.50
.58
.59
.78
.73
.70
.65
.65
1 .65
78.7 1.72
CT-BED
DEPTH
AIR/ CAO/S
FUEL RATIO 3
REGEN.
<, CAS S OUT %
CENTIM % ST. MOL. TO CAO
83.
82.
85.
85.
84.
82.
78.
80.
80.
77.
78.
76.
83.
84.
84.
85.
82.
107.
107.
107.
105.
96.
M I SSED
MISSED
96.
91 .
91 .
91.
91.
91.
91.
95.
95.
95.
93.
93.
107.
99.
99.
96.
26.6
26.4
26.6
25.8
26.2
25.6
26.0
25.2
25.6
25.5
25.8
24.5
24.5
24.4
24.5
24.5
24.8
24.4
24.6
24.4
24.4
24.3
DATA READ
0.71
0.62
1.05
.30
.29
.16
.30
.58
.45
.28
.45
.36
.07
.15
1 .32
1.23
0.9,9
,1.15
•1.32
1 .23
0.91
1 .03
ING
63.0
60.8
64.9
63.7
55.0
61.5
61.5
70.3
75.6
83.0
70.8
74.6
61 .5
68.5
68.5
69.9
79.9
71.4
71.8
60.6
72.4
76.4
OF FED
83.9
88.6
90.9
86.4
73. 1
78.7
80.3
78.0
81 .2
84.7
81 . 1
70.7
66.9
75.7
72.9
69.5
93.9
78.4
75. 1
66.3
74.0
79.6
DATA READING
24.4
25.2
25.5
25.4
24.2
23.0
23.0
23.9
25.3
28.5
26.4
26.2
26.2
26.2
26.3
26.3
0.45
1 .05
0.86
0.74
0.61
0.94
1.06
0.95
0.79
0.66
0.62
0.93
1.11
.1.02
1.07
0.58
66.8
61.6
59. 1
65.7
64.7
63.2
66.9
62.5
55.0
52.0
49.5
51.4
48.7
49.2
50.3
50.6
78.2
76.5
75.7
86.6
83.8
78.3
78.4
76.3
75.9
76.6
75.3
11. &
72.0
72.7
71.1
72. 1
- 272 -
-------
APPENDIX pi TABLE IV.
HUN 81 DESULPHURISATION PERFORMANCE PAGE
4 OF 12
DAY. HOUR
6.0330
A. 0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6 . 1 1 30
6. 1230
6. 1330
6. 1430
6. 1530
6. 1630
6. 1730
6 . 1 830
6. 1930
6.2030
6.2130
6.2230
6.2330
7.0030
7 . 0 1 30
7.0230
7.0330
7.0430
7.0530
7.0630
7.0730
7.0830
7.0930
7. 1030
7 . 1 1 30
7. 1230
7. 1330
7. 1430
7. 1530.
7 . 1 630
7. 1730
7 . 1 830
SULPHUR GAS
REMOVAL VEL.
% M/S
76.8 1.76
76.2 1.72
79.0
78.4
78.4
77. '9
77.8
77.3
77.7
79.3
79.3
79.4
~/9.7
79.6
78.3
78.4
78.4
77.5
78.1
78.9
1.73
1 .75
1.75
1 .75
1 .72
1 .64
1 .6?
1 .62
1 .56
1.59
1,61
1.62
1 .67
1.61
1 .61
1 .59
1.59
1 .59
79.4 1.59
79.5 1.59
80.3
81.2
82.2
81.8
82.6
82.8 1
82. 1
81.7
79.7
77.2
78. 1
78.5
79. 1
79.9
79.9
76.7
71.2
68.5
.61
.61
.59
.58
.59
.59
.61
.62
.64
.50
.62
.62
.50
.56
.56
.67
.54
.40
G-BED
DEPTH
CENTIM
108.
102.
99.
100.
101.
101.
99.
93.
99.
99.
99.
99.
94.
90.
85.
93.
93.
96.
95.
96.
96.
87.
96.
96.
107.
107.
107.
95.
96.
92.
92.
92.
98.
98.
92.
91.
91.
91.
92.
97.
AIR/
FUEL
% ST.
25.8
25.8
25.7
25.7
25.8
25.9
25.3
25. 1
24.9
24.5
23.2
25.7
24.7
24.8
24.7
24.6
24.8
24.8
24.7
24.7
24.8
25.0
25.0
P4.8
24.9
25.0
25.0
25.0
24.9
24.8
24.9
23.2
23.7
24.2
22. 1
22.6
22.4
22.4
24.7
24.6
CAO/S
RATIO
MOL.
0.80
2.83
0.57
1 . 15
1 . 10
1.24
1.37
0.44
1.09
1 . 13
1 .02
0.91
0.75
1.06
1.23
0.48
0.84
1 .06
0.97
0.96
. .45
.50
.32
.58
.54
.32
1.06
1.05
1.06
1. 10
1.23
1 . 19
1.50
0.94
0.73
0.75
1 .06
1 . 10
1 .32
1 .50
% CAS
TO CAO
45.6
46.6
45.2
46.7
51.3
58.6
69.3
68.5
78.9
75.5
69.4
86.7
77.3
73.3
64.2
67.0
66.0
76.2
43.9
77. &
79.0
72.5
67.9
65.8
64.8
70.2
57.1
74.5
61 .9
71.3
65.4
59.4
54.9
58.0
64.6
51 .3
56.7
58.5
51.0
49.8
HEGEN.
S OUT %
OF FED
64.4
65.3
63.5
63.6
67. 5
77.5
77.2
72.2
77.0
72.5
65.5
75.8
71 .2
72.6
69. 1
70.7
70.9
79.3
47.4
79.3
78.8
78.4
76.5
73. 1
70.3
71.7
62.5
75.4
77.2
76.6
82.6
74.8
67.3
69. 1
78.3
64.4
66.5
72.9
60.8
66.3
- 273 -
-------
RUN Ht
APPENDIX 5? TAPLF IV.
DESULPHURISATION PERFORMANCE PAOF
5 OF 12
DAY. HOUR
7 . I 930
7.2030
7.? 130
7.2230
7.2330
8.0030
8 . 0 1 30
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8.0930
8. 030
8. 130
8. 230
8. 330
8. 430
8. 530
8. 630
8. 730
u. 830
8. 930
8.2030
8 . 2 1 30
8.2230
8.2330
9.0030
9.0130
9.0230
9.0330
9.0430
9.0530
9.0630
9.0730
9.0830
9.0930
9. 1030
SULPHUR
REMOVAL
%
63.8
74.5
74.0
73.6
72.6
68.8
72.2
76.5
75.9
76.7
76.0
76.7
75.9
71.4
70.8
70.4
70. 1
70.0
69.8
68.6
67. 1
65.4
69.7
71.4
69.9
64.7
6?.0
63.5
58.0
61.8
61 .4
62. 1
61.3
63.9
65.5
66.6
68.2
69.5
68. 1
67.9
GAS
VEL.
M/S
1 .29
.33
.22
.22
.26
.64
.68
.67
.67
.67
.68
1 .68
1 .65
.68
./0
.75
.76
.72
1.73
0.8.9
0.8.9
1.73
1 .76
.72
.^3
.90
.86
.79
.83
.83
.73
.76
1 .78
1 .78"
./2
1.70
.70
1 .70
.70
.73
G-BED
DEPTH
CENTIM
99.
101 .
105.
109.
106.
93.
97.
93.
95.
95.
95.
95.
95.
1 10.
•95.
99.
95.
91.
89.
9] .
91 .
93.
93.
91.
82.
78.
77.
80.
78.
76.
76.
76.
76.
80.
77.
77.
78.
78.
80.
79.
AIR/
FUEL
% ST.
22.7
23.4
22.8
22.8
22.7
24. 1
24.6
23.3
24.5
24.0
24. 1
23.3
23. 1
23.4
23.3
23.9
24. 1
23.8
23.8
23.8
23.8
23.9
23.9
24.0
24.2
24.2
24. 1
23.0
23.6
23.7
23. 1
23.7
23. 1
22.9
22.8
22.9
23.3
23.3
23.2
23.3
CAO/S
RATIO
MOL.
1.36
1.15
1.23
0.84
.01
.24
. 17
. 15
.17
.23
.23
.09
0.94
0.93
0.57
0.35
0.84
0.^8
0.57
0.75
0. 18
1 .10
0.97
0.93
0.93
1 . 10
1 .06
1 . 15
0.88
0.75
0.75
0.75
0.40
1 .46
0.97
1.02
1 .02
1.41
0.53
0.84
°A CAS
TO CAO
46.3
46.7
47.5
49.8
47.4
36.2
46.9
46.7
49.5
51.0
54.3
48.5
52.5
50.4
50.4
60.9
57.7
52.6
51.2
52.0
52.0
48.8
45. 1
54.5
42.6
42.2
38.9
39.5
44.2
46.2
42.0
42.1
42.4
47.5
45.7
44. ]
49.6
46.5
47.8
53.5
REGEN.
S OUT %
OF FFD
64.0
63.7
64.6
64.4
64.4
43.6
56.3
55.8
57.9
57.0
65.3
57.8
62.7
58.2
57.2
68.0
66.9
62.3
62.5
66.4
66.7
61.3
54.8
64. 1
62.8
60. 1
54.3
57.3
49.9
57.5
52. 1
52.2
52.8
57.0
57.5
52.0
59.0
55.3
57.7
65.2
- 274 -
-------
APPENDIX E« TABLE IV.
RUN 8: DESULPHURISATION PERFORMANCE PAGE 6 OF 12
DAY. HOUR
9. 1 130
9. 1230
9. 1330
9. 1430
9. J530
9. 1630
9.1730
9. 1830
9 . 1 930
9.2030
9.2.130
9.2230
SULPHUR GAS
REMOVAL VEL.
% M/S
64.7
60.6
61.0
61.2
61.0
59.8
59.7
56.4
62.9
63. 1
61.9
.72
.68
.70
.68
.64
.65
.65
.61
.51
.54
.47
63.3 1.44
G-BED
DEPTH
CENTIM
76.
68.
64.
61 .
54.
54.
54.
53.
58.
55.
57.
58.
AIR/
FUEL
% ST.
23.2
22.6
22.6
22.5
22.2
22. 1
22. 1
21.5
20.8
21.4
20.2
20.3
CAO/S
RATIO 5
REGEN.
6 CAS S OUT %
MOL. ' TO CAO
0.26
0.62
.1.10
0.96
1.51
1.28
0.49
1. 19
1 .46
1 . 10
0.88
0.89
52.6
45.5
42.1
44.2
40.5
42.0
48. 1
41 .5
50.3
44. 1
43.5
45.2
OF FED
61.8
54.7
53.0
50.6
45.2
51. 1
51.1
42.3
54.6
46.8
49.3
47.9
SHUT DOWN AT 9.2230 FOR 23 HOURS
10.2230
10.2330
1 1.0030
1
1
*
1
*
1
.0.130
.0230
.0330
.0430
.0530
.0630
.0730
-
75. 1
73.4
73.4
76.8
78.0
76.3
75.8
.90
.86
.78
.76
.76
.76
.78
.93
74.8 1.79
71.0 1.Q8
69.
73.
73.
76.
77.
78.
77,.
76.
76.
76.
24.4
25.0
23.7
23.3
23.. 1
23.9
23.9
23.9
22.9
30.5
1 .43
1..19
.1.25
1.55
1.58
1.00
0.77
0.72
0.87
1 . 16
3.0
32.1
43.9
44.2
46.8
65.0
69. 1
66.6
6.7.5
68.3
2.8
31.8
42.2
40.9
40.3
61.2
68. 1
65.7
67.3
88.0
12.0330
12.0430
12.0530
12.0630
12.0730
12.0830
12.0930
12.1030
12. I 130
1 2. 1230
SHUT DOWN AT 11.0730 FOR 19 HOURS
14.8
14.7
23.7
36.3
38.9
.75
.87
.86
.0V
.70
.70
.83
.76
.72
.65
73.
71 .
71.
71 .
71 .
69.
71.
66.
76.
69.
27.5
25.3
25.3
27.2
24.4
23.0
25.6
25.4
25.0
24.0
1.02
1. 19
1.51
1.17
0.78
0.82
1. 16
1.24
2.85
1 .54
—
—
-
—
18.3.
6. 1
1 1.2
—
-
13.0
0.
0.
0.
0.
21.5
7.2
12. 1
0.
0.
14.3
- 275 -
-------
HUN 8:
APPENDIX p,i TABLE IV.
DESULPI1URISATION PERFORMANCE PAGE
7 OF 12
DAY. HOUR
12.1 330
12. 1430
12. 1530
12. 1630
12. 1730
12. 1830
12. 1930
12.2030
1 2 . 2 1 30
12.2230
12.2330
13.0030
13.0130
13.0230
13.0330
13.0430
13.0530
13.0630
13.0730
13.0830
13.0930
13. 1030
13. 1 130
13. 1230
13. 1330
13. 1430
13. 1530
1 3 . 1 630
13. 1730
13. 1830
13. 1930
13.2030
.1 3 . 2 1 30
13.2230
13.2330
14.0030
1 4 . 0 1 30
14.0230
14.0330
14.0430
SULPHUR GAS G-BED
REMOVAL VEL. DEPTH
% M/S
40.8
41. 1
22.2
30.6
32.9
58.6
72.5
,76.8
78.3
79.2
80.2
81.0
bl.8
81.6
77.0
66.2
63. 1
61.8
61. 1
59.4
58. 1
58.0
60.6
59. 1
59.0
61. 1
60.0
61.1
63. 1
64. 1
64.8
65.5
.65
.72
.72
.68
.50
.48
.51
.50
.51
.50
.50
.58
.5b
.54
.48
.51
.50
.51
.51
.51
.51
.51
.51
.59
.59
.56
.bb
.62
.61
.62
.62
.59
66.1 1.61
66.7 t.61
67.5 .64
70.5 .53
75.8 .53
78.5 .5,
79.5 .53
79.9 1.53
CENTIM
78.
81.
81 .
86.
86.
86.
88.
88.
92.
88.
88.
88.
88.
90.
91 .
88.
66.
88.
86.
87.
87.
90.
93.
88.
88.
88.
88.
90.
90.
88.
88.
88.
88.
90.
90.
90.
90.
90.
90.
94.
AIR/
FUEL
% ST.
23.9
24.2
23.9
24. 1
19.8
20.9
22. 1
22. 1
22.2
22.2
22.2
22.7
23.2
22.3
22.7
20.4
20.0
20.9
20.4
20.5
20.4
20.2
20.6
21 .3
21 .4
21 .3
21 .2
22.3
22.2
22. 1
22.3
22.3
22.5
22.3
22.3
20.3
21.3
21.3
22.0
21.9
CAO/S
RATIO 2
REGEN.
'•> CAS S OUT %
MOL. TO CAO
1.32
2. 10
2.25
1.98
1.83
1.76
2.33
1.74
2.21
1.62
1.23
1.20
.1.62
1.78
1 .39
1 .43
1 .40
1 .46
1.35
1.06
0.66
1 .63
2.03
1.82
2.00
1. 17
1.67
1.79
1 .90
1.71
1.57
2. 12
1.69
1.83
1.86
1.53
1 .53
1.64
2.07
1.68
13. 1
-
-
23.5
29.7
10.2
46.7
50.8
57.0
64.2
72.7
75.6
58. 1
53.4
40.7
43. 1
45.3
42.0
55.5
50.4
46.9
38.6
44.4
40.1
28.8
35.4
39.0
37.5
34.5
39.9
41 .6
39.9
43.1
40.4
39.8
51.7
54.7
54.7
56.7
57.8
OF FFD
14.6
0.
0.
25.3
28.4
10.0
44.8
48.3
50. 1
56.5
56.7
64.0
72. 1
61.3
56.3
54.5
54.9
57.6
71.5
64. 1
5#. 1
46.5
54.0
47.9
32.9
42.7
46.0
43.7
39.9
47.2
49.8
47.5
51 .4
47.4
45.7
48.3
54.9
54.9
54.7
56.0
- 276 -
-------
APPENDIX Ft TABLE IV.
RUN 81 DESULPHURISATION PERFORMANCE PAGE
8 OF 12
DAY.HOUH
14.0530
14.0630
14.0730
14.0830
14.0930
14. 1030
14.1 130
14. J230
14. 1330
14. 1430
M. 1530
14. 1630
14. 1730
14. 1830
14. 1930
14.2030
.14.2130
14.2230
14.2330
15.0030
15.0130
15.0230
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
15.0 930
15. 1030
15.1 130
15. 1230
15. 1330
15. 1430
15. 1530
15. 1630
1 5 . 1 730
15. 1830
15. 1930
15.2030
SULPHUR OAS
REMOVAL VEL.
% M/S
80.8
80.5
80. 1
79.6
79.6
79.4
79.5
79.2
78.6
78.9
80.0
77.9
77.2
78.7
78.9
78.3
77.3
78.6
78. 1
78.3
79.6
80.4
82.2 1
81.9
81.7
82.0
82. 1
80.0
77.7
76.9
75.3
75.7
76.3
76.2
77.3
78.5
79.5
81.2
81.6
82.2
.54
.58
.58
.58
.51
.48
.48
.48
.4«
.48
.48
.48
.54
.5b
.S8
.59
.59
.54
.51
• b4
.58
U58
.59
• ^
.58
,58
.51
.59
.59
,58
.50
.51
.51
.51
.50
.50
.50
,50
.56
.58
G-BED
DEPTH
CENTIM
90.
88.
88.
88.
90.
92.
88.
88.
88.
88.
91.
91.
91.
91.
, 91 .
91 .
88.
88.
87.,
87.
88.
83.
88.
88.
86.
87.
87.
88.
88.
88.
88.
89.
98.
100.
96.
99.
101 .
100.
104.
102.
AIR/ CAO/S
FUEL RATIO
% ST. MOL.
21 .8 . .54
22.2 .46
22.3
22.4
21.5
21.4
21.5
21.4
21.5
21.6
21.6
21.5
22.4
22.5
22.5
22.5
22.5
22. 1
21 .4
21.8
22.2 ;
22.2
22.3 I
22.4 i
22.2
22. 1
21 .3
22.2
22.2
22. 1
21 .3
21 .3
21 .2
21 .4
21 .3 1
21 .8 1
22. 1 2
22.2 1
23.3 1
23.3 1
.50
.44
.33
.50
.87
.68
.80
.42
.81
.94
.83
.76
.61
.79
.83
.94
.60
.60
>.05
.49
>.09
>.02
.84
.21
.78
.67
. 12
.60
.47
.99
.60
.37
.65
.91
.22
.75
.79
.61
% CAS
TO CAO
61 .9
60.9
6,1 .7
63.2
68.2
70.0
68. 1
67.2
67.7
70.9
66.5
65.8
69.9
60.4
64.8
64. 1
61 .8
60.9
60.9
61 .4
5-9.8
58.6
55.1
52.0
54.4
54.0
52.8
45. 1
54. 1
55.3
56.3
57.9
52.8
55.9
57.5
54.7
64.4
59.5
58.6
60.7
REGEN.
S OUT %
OF FED
59.6
59.7
60.0
59.3
61 .8
61 .2
60.3
61.3
62. 1
64. 1
62. 1
61 .8
64.6
62.7
68. 1
73.7
70.5
69.7
67.5
67.0
70.8
73.2
68.9
64.7
68.0
68.3
66.7
55.0
63.6
63.0
59.7
61.5
56. 1
•rS VX • 1
57.2
54.7
50.9
56.7
57.0
57.6
63.4
- 277 -
-------
RUN 81
APPENDIX P 5 TABLE IV.
DESULPMUHISATION PERFORMANCE PAGE
9 OF 12
SULPHUR GAS
DAY.HOUR REMOVAL VEL.
% M/S
G-RED AIR/ CAO/S REGEN.
DEPTH FUEL RATIO % CAS S OUT %
CENTIM % ST. MOL. TO CAO OF FFD
15.2130
15.2230
15.2330
16.0030
1 6 . 0 1 30
16.0230
16.0330
16.0430
16.0530
16.0630
16.0730
16.0830
16.0930
16. 1030
16. 1 130
16.1230
16. 1330
16. 1430
16. 1530
16. 1630
16. 1730
16. 1830
1 6 . 1 930
16.2030
16.2130
16.2230
16.2330
17.0030
17.0130
17.0230
17.0330
17.0430
17.0530
17.0630
IV. 0730
17.0830
1 7 . 0 930
17. 1030
1 7 . 1 1 30
17. 1230
82.7 1.59
81.8 1.58
80.7 .58
80.6 .S9
80.2 .59
77.8 .59
79.8 .56
80.3 .59
79.2 .54
68.5 .56
73.6 _.l,i>.6
73.5 .61
80.4 .62
81.3 .92
77.9 .00
77.5 .89
79.7 .&3
80.2 t.45
83.1 1.45
86.4 ' .59
84.6 .59
82.5 .59
83.0 .59
81.8 .56
80.4 .54
80.8 - .37
79.1 .34
78.0 .34
79.3 .34
79.9 f.44
81.1 1.37
82.4 1.37
83.4 |.3i
83.4 .31
82.1 .39
80.5 .40
84.9 .47
88.6 .64
89.9 .64
92.4 1.50
103.
104.
101 .
105.
103.
^9.
101 .
100.
101 .
101 .
101 .
106.
101 .
96.
96.
93.
93.
95.
96.
95.
95.
95.
95.
95.
96.
93.
99.
1 12.
1 15.
104.
106.
104.
104.
101 .
101.
102.
101 .
99.
97.
100.
23.3
23.4 1
23.3
23.3 1
23.2 ^
22.5 1
22.7 I
23.0 1
21.1 1
21.1 1
20.8
22.6
23.6
24.4
24.4
23.2
23.7
21 .0
20.8
32.9
26.5 Q
25.7
24.8
23.7
22.8
20.5
20.7 ;
20.9 ;
20.9 ;
21 .8
20.9
20.8
19.9
19.9
20.9
22. 1
23.3
24.7
25. 1
25.7
.68
.84
.39
.28
?. 14
.87
>.07
.62
.66
.42
.21
.52
. 1 1
.05
.28
.57
.48
.65
.46
.96
5.83
.25
.60
.38
.15
.36
>.24
?.00
?.29
1 .76
2.14
1.39
1.58
.65
. 16
.39
.78
.49
.51
.69
60.8
53.5
55.6
56.2
55.2
56.3
63.5
62.3
101.8
-
—
-
68.2
79.4
65.3
65.5
66.6
106.5
89. 1
74.7
73.6
66.5
64.0
66.9
77.2
82.5
10. 1
-
—
—
-
-
-
-
-
-
-
-
33.0
93.4
65.0
58.9
61.8
63.7
63.4
62.6
65.6
58.3
67.3
0.
•0.
0.
36.7
77.6
78.5
74.5
65.5
71.0
87.5
133.7
96.9
91.7
75.6
67.0
69. 1
53.6
7.4
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
20.3
1 14.7
- 278 -
-------
APPENDIX Ft TABLE IV.
RUN 8* DESULPHURISATION PERFORMANCE PAGE 10 OF 12
DAY. HOUR
17. 1330
17. 1430
17.1530
17.1 630
17.1730
17.1830
17.1930
17.2030
17.2130
17.2230
17.2330
18.0030
18.0130
18.0230
18.0330
18.0430
18.0530
18.0630
18.0730
18.0830 .
18.0930
18. 1030
18. 1 130
18. 1230
18. 1330
18. 1430
18. 1530
18. 1630
18. 1730
18. 1830
18. 1930
18.2030
18.2130
18.2230
18.2330
19.0030
19.0130
19.0230
19.0330
19.0430
SULPHUR GAS
REMOVAL VEL.
% M/S
92. 1 .58
90.2 .54
90.0 .58
89.9 .44
89.7 .47
89.4 .45
89.4 .44
88.2 .53
87.5 .45
86.6 .48
85.9 .47
85.3 .45
85.0 .47
84.8 .44
85.8 .44
86.9 .48
86.9 .45
87.0 t.45
88.6 1.45
87.6 I
85.5 J
b5.8
85.7
87.5
R7.9
88.7
87.3
86. 1
85.3
84.0
85.6
86.6
85.8
86.2
86.0
86.4
87.0
86.8
.45
.44
.45
.39
.39
.40
.39
.47
.48
.44
.45
.42
.97
.44
.44
.45
.44
.44
.42
G-RED
DEPTH
AIR/ CAO/S
FUEL RATIO
CENTIM % ST. MOL.
97.
101.
99.
101.
101 .
M I SSED
MISSED
95.
10.1 .
97.
1 10.
108.
1 10.
1 12.
102.
1 12.
1 15.
1 18.
1 12.
125.
101.
104.
102.
102.
104.
104.
101 .
96.
93.
92.
88.
88.
90.
91.
88.
88.
90.
93.
93.
99.
24.6
23.0
25.3
23.3
23.4
DATA READ I
DATA READ I
23.2
22.3
24.6
24.7
24.8
24.7
24.0
23.9
24.0
24.5
24.8
24. '9
24.8
24.8
24.2
23.8
23.8
24. 1
24.5
24.4
23.7
23.9
24.0
24.4
24.5
24.9
34.3
24.8
24.7
24.7
24.8
24.7
24.8
2. 17
1.56
1.51
2.03
0.72
NG
NG
1.19
1 .64
,1.32
2.40
.77
.51
.80
.35
.31
2.42
1.23
1.61
2.03
1 .02
.48
.54
.95
.59
.75
.61
.40
1 .67
1.76
1.87
2.29
2.28
2.20
1 .90
2.31
1.68
2.41
2.44
2.95
REGEN.
% CAS S OUT %
TO CAO
'98.5
100.2
98.1
86.5
90.9
80.4
1 10.7
1 13.4
85.7
82.6
73.6
81.0
85.2
99. 1
28.4
91.8
106. I
84.3
89.3
80.2
107.5
7.1.9
100.8
85.3
71.2
63.9
60.2
67.9
56.9
70.0
75.8
75.7
77.0
58.5
64.6
65.9
91.3
85.2
OF FFD
106.0
1 1 1.0
108.2
104.9
I 19.6
96.2
79.2
77.0
94.5
89. 1
85.5
84.2
80.5
78.9
27.6
73.3
88.2
91.6
121.2
60.6
73.4
39.5
82.7
86.5
88.8
83.4
70.0
87.5
73. 1
81.2
80. 1
78.0
76.5
65.0
77. 1
73.0
73.4
68.2
- 279 -
-------
HUN Rt
APPENDIX pi TABLE IV.
DESULPHURISATION PERFORMANCE PAGE 11 OF 12
DAY. HOUR
19.0530 .
19.0630 ,
19.0730
19.0830
19.0930
19. 1030
19. 11 30
1 9 . 1 230
19.1 330
19. 1430
19. 1530
19. 1630
19. 1730
SULPHUR GAS
REMOVAL VEL.
% M/S
87.0 1.45
87.3 f.45
88.8
89.6
89.4
89.7
9.1.2
90.2
88.8
88.7
88.3
88.0
86.8
.37
.44
.45
.42
.37
.44
.33
.45
.50
.39
.73
G-BED
DEPTH
CENTIM
101 .
102.
97.
1 15.
106.
109.
109.
1 10.
109.
104.
107.
111.
106.
AIR/
FUEL
% ST.
25.3
25.7
24.3
25.6
24.6
24.7
24.7
25.7
23.2
22.4
22.4
21 . 1
27.7
CAO/S
RATIO
REGEN.
% CAS S OUT %
MOL. TO CAO
1 .89
1 .96
1 .99
1.61
2.26
2.42
2.56
2.50
1.31
1 .05
0.96
0.78
0.75
83.8
81.7
66.6
107.8
83.3
76.4
100.6
92.3
90.7
14. 1
14. 1
7.1
40.3
OF FED
63.5
65.2
65.2
80.8
55.5
53.4
80.0
82.4
57.9
b.8
8.8
4.4
29.6
SHUT DOWN AT 19.1730 FOR 36 HOURS
21.0630
21.0730
21 .0830
?1 .0930
21 . 1030
2 1 . 1 1 30
2 1 . 1 230
21.1 330
21.1 430
21 . 1530
21.1 630
2 1 . 1 730
21.1 830
21 . 1930
21.2030
2 1 . 2 1 30
21 .2230
21 .2330
22.0030
22.0130
22.0230
22.0330
22.0430
27.2
67.0
74.4
74. 1
72.9
71.7
70.4
74. 1
72.9
73.6
74.0
74.3
74.4
74.5
74.3
79.6
78.0
76.5
77.8
77.2
76.4
76.9
.45 "
.44
.44
.48
.48
.39
.44
.545
.42
.51
.50
.51
.44
.44
.59
.58
.56
.56
.56
.56
.56
.56
77.9 1.58
97.
96.
•96.
95.
93.
89.
90.
90.
91 .
91 .
90.
90.
90.
95.
96.
96.
96.
96.
96.
96.
95.
95.
95.
22.7 1.59
22.5 0.93
22. '9 0.90
22.1 0.80
22.5 0.92
21.5 1.35
21.6 1 . 16
22.6 0.81
21.5 0.81
22.5
22.7
22.5
21 .5
21.6
24.7
25. 1
24.4
23.7
23.8
23.8
23.2
.04
. 16
.15
.04
.31
.41
.02
.04
.16
.59
.58
.35
22.9 1.26
22.9 1.04
36.0
61.2
84.7
78.7
74.6
82.3
99.8
98.7
107.4
91 .7
104.4
102.5
100.2
90.6
70.5
85.9
70.2
84.4
79.9
67. 1
63.2
60.5
58.2
42.2
85.2
83.0
86.8
87.3
83.5
87.2
93.5
76.3
64.8
76.7
73.6
71.6
60.0
50.8
82.9
81.4
101.9
88.0
88.3
79.5
74.3
68.7
- 280 -
-------
RUN 8*
APPENDIX P: TABLE IV.
DESULPHURISATION PERFORMANCE PAGE
12 OF 12
SULPHUR
DAY
22.
22.
22.
22.
22.
22.
22.
22.
22.
22.
22.
22.
.HOUR
0530
0630
0730
0830
0930
1030
1 130
1230
1330
1430
1530
1630
REMOVAL
%
16.
76.
76.
75.
73.
71.
72.
74.
76.
75.
-
8
8
3
5
8
6
7
9
3
1
GAS
VEL.
M/S
.56
.56
.56
.56
.54
.54
.56
.42
.47
.48
1 .47
G-BED
DEPTH
CENTIM
95.
93.
95.
95.
95.
93.
89.
89.
93.
93.
MISSED
93.
AI
R/
FUEL
%
22
22
22
22
22
23
23
21
22
22
DATA
22
ST.
.9
.9
.7
.9
.9
. 1
.3
.2
.2
.2
CAO/S
RATIO
MOL.
1.
1.
1 .
0.
0.
1 .
1.
1.
1.
1.
00
22
15
89
63
1 1
42
34
26
30
% CAS
TO CAO
53.5
64.6
59.6
70.7
63. 1
65.6
52.5
59.3
53.4
66.7
HEGEN.
S OUT %
OF FED
60.9
80.2
70.8
77.8
72.9
75.4
57.4
60.7
60.8
7J.1
READING
. 1
0.
97
55.3
67.4
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-------
APPENDIX F: TABLE V.
RUN 8: GAS COMPOSITIONS
FLUE GAS
DAY.HOUR 02 C02 VOL % SOP
% ANAL CALC PPM
PP.0930 2.5 15.0 13.9 370.
PP.1030 1.9 15.0 14.3 415.
PP. 1 130 P. 1 1 5.0 14.2 397.
PP..1230 2.1 15.3 14.2 364.
2P.1330 2.1 15.0 14.3 346.
REGENERATOR GAS
02 COP SOP
0.50
0.40
0.40
0*40
0.40
4.1 6.2
3.1 7.0
2.5 5.8
3.7 6.0
1.9 6.2
PAGE R OF R
GASIFIER INLET GAS
02 VOL % CO? VOL %
ANAL CALC ANAL CALC
20.7 20.7
20.7 20.7
20.6 20.6
20.6 20.6
20.7 20.7
0.
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APPENDIX F: TABLE VI.
RUN R: SULPHUR AND STONE CUMULATIVE BALANCE. PAGE 8 OF
DAY. HOUR
??
PP
PR
P?
PP
.0930
. 1030
. 1 130
• 1230
. 1 330
48
49
49
49
49
T
0
K
IN
.908
.033
. 157
.28?.
. 406
1
1
1
1
1
T A L
I L
FLUE
1 .345
1 .380
1.414
1 .445
1 .475
S U L
0 M 0
REGEN
30.809
30.903
30.974
31 .050
31 . 126
P H U
L S
FINES
4.923
4.926
4.935
4.940
4.960
R
EQUIVALENT BURNT STONE
KILOGRAMS
IN-OUT
1 .831
1 .824
1 .833
1 .847
1 .846
FEED
4476. 6
4484. 7
4 49 5 . 0
4504.7
4513.8
REMOVED
3165.0
3166.5
31 71 .3
31 73.5
3183. 1
IN-OUT
1 3 1 1 • A
1318.?
1323. 7
1331.1
1330. 7
- 311 -
-------
APPENDIX F: TABLE VII PAGE 1 OF 10
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUR GAS'R REGEN REGEN ELUTR BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSE
1.0700
1 . 1 U5
1.1445
1 . 1 630
0 . 1 1 80
1.2300
2.0300
2.0130
2.0500
2.0745
2.0815
2. 1045
2.1 145
2. 1400
2. 1445
?. 1450
2. 1800
2.2025
2.2040
2.2350
3.0030
3.0045
3.0050
3.0420
3.070W
3.0800
3. 1200
3. 1400
3. 1545
3.2040
3.2350
4.0005
4 . 0 1 20
4.0415
4.0645
4. 07 SCI
n.C',850
4. IK 35
4. 1200
4. U0M
- _ - _
- 6.12
- 14.63
— — — _
- ' - 8.85 0.
_ _ — _
4.76 - - 5.44
3.63
- 2.27
2.04 14.97 - 45.36
1.13 -
- 0.91
— — — _
- _ _ _
- 0.91
— — _ —
2.95 - 0.91
_ - _ _
- 0.91
d.68 1.36
2.72 -
2.72
— _ _ _
- 1.59
3.63 2.72
- 1.59
1.36
— _ - _
_ - _ -
- 0.23
_ — _ _
1.81 4.08 - 0.68
_ — — _
- 0.23
0.23
1.13
2.27 2.72
_ — _ —
- 0.45
0.45
—
0.
0.
-
3.63
—
0.45
—
0.45
0.68
—
—
—
—
1.59
—
10.89
—
1 0 . 89
30.84
—
-
-
41.73
—
32.66
19.96
—
6.35
31.75
-
36.74
—
16.33
—
14.06
—
—
14.51
-
5.44
3.63
2.72
—
-
—
8. 16
—
6.12
5.67
—
4.99
-
-
7.26
-
7.26
-
5.44
9.53
-
-
-
10.89
-
1 1.79
7.26
-
4.08
10.89
-
8.62
—
4.54
-
6.35
-
-
4.76
—
-
9.30
-
2.49
0.55
14.06
-
-
-
—
—
-
3.63
4.99
~
7.26
—
8. 16
-
-
—
—
5.44
—
1.81
—
—
10.43
-
—
2.49
-
1 1 .79
18.60
-
_
-
34. -72
-
-
- 312 -
-------
APPENDIX P: TABLE VII PAGE 2 Qp 1Q
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUR GAS'R RFGEN RHGEN ELUTR BOILER POILER FIUTR
CYCLONE FINES RACK FLUE COARSF
4.1500 - 0.68 - 2.61
4.1600 - 0.34 5.44
4.1700 , - - 0.68
4.1800 - - - 0.57 -
4.1900 - - 0.79
4.2000 1.59 1.59 1.70 9.07 3.63 - 1.91
4.2200 - 2.09 -
4.2300 - - - 2.45 -
5.0000 - 2.38 7.26 3.86 2.49
5.0100 2.27 2.27 - 2.04 -
5.0200 - - - 2.49 -
5.0300 - - - 1.70 -
5.0400 - - 2.18 4.08 3.18
5.0500 - 2.27 -
5.0600 - - - 0.9] _
5.0700 - - - 1.81 -
5.0800 - 3.40 2.95 1.36
5.0800 - - - - 2.95 1.36 -
5.0900 - - - 1.81 -
5.1100 - - - 9.30 2.72 1.81
5.1200 - - - 4.20-
5.1300 - - - 6.12 -
5.1400 - 3.40 -
5.1500 1.36 1.36 - 0.91 2.72 2.95
5.1600 - - 0.45
5.1700 - - 0.11
5.1800 - - - 0.11 -
5.1900 - 0.23 1.59 1.81
5.1930 - - 0.57
b.2100 - - - 0.54
5.2200 - 0.34 -
5.2300 - ' - - 0.34 -
6.0005 - 0.34 2.72 3.40
6.0100 - - 0.34
6.0200 2.72 1.81 - 0.45 0.91 1.70 3.63
6.0400 - - - 0.79 2.27
6.0600 1.81 - - 1.13 - - 17.op_
6.0800 - 1.81 - 0.68
6.1015 -----_ 4.76
6.1115 - - - - - - 4. t-,/i
- 313 -
-------
APPENDIX F: TABLE VII PAGE 5 OF 10
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUK GAS'K REGEN REGEN ELUTR BOILER BOILER ELUTH
CYCLONE FINES RACK FLUE COARSF
6.1200 1.36 1.36 - - - 6.35
6. 12 IS - - - - - - 4.76
6.1230 - - - - - - 4.54
6.1315 ______ 4.76
6.1415 ------ 4.76
6.1515 ______ 13.4/1
6.1615 - - - - - - 4.76
6.1715 -____- 5.22
6.1800 1.36 1.36 0. 1.36 4.08 4.99
6.1815 - - - - - 0.
6.1915 ------ 6.12
6.2015 - - - - - - 6.12
6.2115 ------ 4.^4
6.2215 ------ 4.54
6.2315 ------ 4.54
7.0000 1.81 1.81 - 1.13 3.86 4.54
7.0015 - - - - - - 4.54
7.0115 ------ 4.M
7.0215 - - - - - - 4.54
7.0315 - - - - - - 4.^4
7.0415 ______ 4.54
7.0515 - - - - - . - 4.54
7.0615 1.81 4.31 - 1.59 4.08 5.22 4.54
7.0715 - - - - - - 4.5*
7.0815 - - - - - - 4.54
7.0915 - 1.59 5.44 5.90 4.5*
7.1015 __-_-_ 4.54
7.1115 - - - - - - 4.5*
7.1215 2.49 2.04 - - - - 4.54
7.1315 - - - - - - 4.54
7.1405 - 0.91 7.71 1.81
7.1415 - - - - - - 4.5*
7.1515 - - - - - - 4.5*
7.1615 - - - - - - ^-54
7.1715 - - - - - - 4.54
7.1 HI 5 1.5Q 3.18 - - - - 4.54
7.1850 - - - 1.13 5.44 2.27
7.1915 - - - - - - 4 •u^
7.2015 - - - - - - ^.54
7.2145 - - - 1.13
- 314 -
-------
APPENDIX F: TABLE VII
PAGE 4 OP 10
SOLIDS REMOVED DURING HUN 8, KG. (RAW DATA)
DAY.IIOUk GAS'R HEGEN RFGEN ELUTH BOILER BOILFR EMITR
CYCLONE FINES RACK FLUE COARSF
4.54
4.54
4.54
7.21 15
7.2215
7.2315
7.2350
8.0030
8.0130
8.0230
8.^330
8.0430
8.0510
8.0530
8.0600
8.0630
8.0730
8.0830
8.0930
8. 1030
8. 1115
8. 1 1 30
8. 1300
8. 1330
8. 1640
8. 1800
8. 1842
8. 1845
8. 1847
8. 1850
8. 1910
8. 1915
8. 1918
8. 1920
8. 1955
6.2000
8.2026
8.2140
8.2230
8.2330
9.0005
9.0030
9.0130
—
—
—
2.72
—
—
—
—
—
—
—
3.63
-
—
—
—
-
—
-
_
2.27
-
1 .81
6. TO
5.67
5.44
7.71
6.80
5.90
5.90
9.07
5.90
7.71
—
—
—
-
0.
_
—
2.72
4.99
4.54
4.54
3.63
2.04
1.59
0.
0.23 4.54 5.22
1.59 5.67
2.49 2.27
4.R4
4.^4
4.54
4.54
4.54
1 1 .79
4.54
4.54
4.54
4.54
4.54
1.59
4.54
4.54
4 .54
1.59 1.36
0.23 1.36 1.13
1.36 2.27
2.04
4.54
4.^4
4.54
4.54
3. 63
- 315 -
-------
APPENDIX P: TABLE VII
SOLIDS REMOVED DURING RUN 8, KG.
PAGE
(RAW DATA)
5 OF 10
HAY. HOUR OAS'R REGEN
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
9
10
11
0230
0330
U430
0530
0600
0630
0730
0830
0930
1030
1130
1135
1147
M50
1155
1? 30
1305
1309
1312
1315
1330
1430
1515
1517
1520
1523
1526
1530
1630
1730
1750
1830
1930
.2030
2130
2230
.2315
2359
0300
REGEN ELUTR BOILER
CYCLONE FINES BACK
4.08 3.63
1.13 2.27 2.72
BOILER FLIJTR
FLUE COARSE
- 4.54
- 4.54
- 4.54
4.54
0.68
3.63 1.36
1.81
-
2.49
J 1.0600
6.35
6.35
6.35
6.80
-
7.71
6.35
7.71
6.35
8.62
8.62
R. 62
8.62
2.27 2.27
2.04 2.95
1.36 1.36
6.35 -
1.36 -
0.23
1.13 1.13
1.36
0.68
1.36
0.23
0.23
8.62
6.12
5.9(3
3.63
4.54
4.54
4.54
4.54
4.54
4.51
4.54
4.51
4.54
4.54
4.54
4.54
/l. 54
4.54
4.54
4.54
1.36
-------
APPENDIX F: TABIE VII PAGE 6 OF 10
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUR GAS'R RFGEN
13.2359
M.0100
W:GEN ELUTR
CYCLONE FINES
R01LER
BACK
1 1.0645
12.0430
12.0525
12.060(0
12. 1200
12. 1500
12. 1600
12.1 700
12. 1800
12. 1805
12.1 900
12.2000
12.21 00
12.2200
12.2300
13.0000
13.0100
13.0200
13.0400
13.0500
13.0600
13.0700
13.0800
13.0900
13. 1000
13. 1 100
13. 1200
13. 1300
13. 1400
13. 1500
13. 1600
13. 1700
13. 1800
13. 1900
13.2000
13.2100
13.2200
13.2300
1.36
9.30
4.54
1.36 1.36
1.81 1.81
_ _
— _
_ _
— _
— —
_ —
_ _
_ _
_ _
— —
1.36 1.36
_ _
— _
_ _
_ _
1.81 1.81
_ —
_ _
_ _
_ _
_ _
_ _
— _
2.49 6.35
— —
_ _
— _
2.49 0.91
— _
_ _
— —
w _
2.04 2.04
POILHR ELUTP
FLUE COARSF
A. 31
1 .36
0.73
0.91
1.59
1. 13
0.91 0.91
5.90
1 .81
1.13 5.44
1.36 1.36 3.63
1.13 2.72
0.91 0.91 5.44
5.90
1.13
4.54
4.54
9.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
y.07
9.07
4.54
9.07
9.07
9.07
9.07
9.07
9.07
'•;.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
9.07
0.68 1.81 3.18 9,
9.07
- 317 -
-------
AFFENDIX F: TABLE VII
PAGE ? OP 10
SOLIDS REMOVED DURING RUN 8, KG. (HAW DATA)
DAY. HOUR OAS'R REGEN RfcGEN ELUTR BOILER BOILER FLUTR
CYCLONE FINES HACK FLUE COARSE
14.0255
14.0300
14.0400
14.0500
1 4 . 0600
14.0615
14.0700
14.0800
U.0900
14. 1000
1 4 . 1 1 00
14. 1200
14. 130*0
14. 1400
M . 1500
14. 1600
14. 1700
14.1 800
14. 1900
1 4 . 2000
14.2100
14.2200
14.2300
1 5 . 0000
1 5 . 0 1 00
15.0200
15.0300
15.0400
15.0500
15.0600
15.0700
15.0900
15.1 000
15.1200
15. 1800
15.1 900
15.2000
15.21 00
15.2300
— —
_ _
— -
— —
2.72 2.49
- -
— —
— —
— —
— _
_ _
0.91 0.91
— —
— —
— —
— —
— -
0.91 0.91
- -
— -
- _
— —
- -
6.35 6.35
_ —
— —
— -
- -
- -
2.27 2.27
— —
— -
— ' -
2.27 2.27
2.27 2.27
— —
_ _
— —
— —
0.91
0.91
.36 1.36
1 .36
1.36
1.36
1.81
0.45 0.45
0.45
0.9
1.13 3.18
4.08
6.80
9.07
3.86
9.0 7
9.07
9.07
9.07
9.07
3.63
9.07
9.07
9.07
9.07
0.07
6.35 9.07
9.07
9.07
9.07
9.07
9.07
4.38 0.
13.61
13.61
13.61
9.07
9.07
6.80 9.07
9.07
9.07
9.07
9.07
9.07
8.62 9.07
9.07
9.07
0.07
8.16 0.91
14.51
9.07
9.07
9.07
9.07
- 318 -
-------
APPENDIX P: TABLE VII
SOLIDS REMOVED DURING RUN 8, KG. (RAW
PAGE 8 OF 10
DATA)
UAY.IIOUH GAS'H
15.2359
16.0100
16.0145
16.0300
16.0500
16.0600
16.0650
16.0700
16.0745
16.0800
16.0900
16.1000
16.I 100
16.1200
16. 1300
16.1400
16.1500
16.1600
16.1700
16.1800
16.1900
16.2000
16.2030
16.2100
16.2200
16.2215
16.2359
17.0300
17.0400
17.0500
17.0600
17.0700
17.0800
17.0830
17.0900
17.1000
17.1100
17.1200
17.1300
17.1500
.81
1.81
1.81
2.72
1.81
1.81
REGEN RFGEN ELUTH
CYCLONE FINES
BOILER POILER ELUTR
RACK FLUE COARSF
2.27 2.27
1.81
1.36
1.36
1.81
1.81
1.81
16.56 13.38
1.81
1.81
2.27 7.71 6.80 9.07
- 0.07
18.60
- 9.07
- ' 9.07
- 9.07
3.63 12.47 12.25
- 9.07
0.91 - - 0.91
- ' 9.07
- 9.07
- 9.07
- 9.07
1.13 6.80 4.99 9.07
- 9.07
- 9.07
- 9.07
- 9.07
7.71
1.81 4.08 3.18 0.91
- 9.07
- 9.07
1.36 1.36
1.27
0.91
9.07
9.07
9.07
0.68
5.22 0.91
9.07
9.07
9.07
5.03 9.07
9.07
9.07
9.07
9.07
5.44
5.44 4.54
6.80
6.80
- 319 -
-------
APPENDIX F: TABT£ VII PAGE 9 OF 10
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUR OAS'H REGEN REGEN ELUTR BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSE
17. 1600
17.1700
J 7 . 1 80(3
17.1900
17.2000
17.2100
17.2359
18.0600
18.0700
18.0800
18.0900
18. 1000
18. 1200
18. 1300
18.1400
18. 1500
18.1600
18.1700
18.1730
18.1800
18.1900
18.1910
18.2000
18.2100
18.2200
18.2300
18.2359
19.0100
19.0600
19.0945
19. 1200
19. 1700
19. 1805
19.2200
20.0900
20.2010
20.2200
20.2359
21.0730
—
-
—
-
-
—
1.81
1.81
—
-
—
—
1.81
—
—
-
—
-
45.36
—
1.81
1.81
-
-
—
—
1 .81
-
13. 15
-
4.54
—
1.36
—
-
—
-
0.91
1.81
-
-
-
0.45
-
-
0.
0.
—
-
—
-
1.81
-
-
-
-
—
-
-
2.72
-
-
-
—
-
1.81
-
1.81
—
2.72
-
1.36
-
-
-
-
-
-
—
-
0.91
—
-
-
1.81
2.72
-
-
—
-
t.81
—
-
-
—
—
- -
— -
7.71 6.35
3.63
— —
— —
2.04 4.99
9.75
- -
- -
- -
— —
4.99 4.54
- -
— —
- -
-. -
— —
6.80
6.80
6.80
—
4.54
6.80
—
4.54
4.54
4.54
4.54
9.07
9.07
9.07
6.80
9.07
9.07
9.07
3.18 3.63 3.63
25.85
6.58
262.63
6.80
9.07
-
—
1.13
-
4.99
21.77
7.26
7.26
-
_
6.35
—
9.53
4.08
3.18
3. 18
-
—
2.72
-
7.94
9.53
4.08
3.63
8.25
9.07
9.07
^9.07
9.07
9.07
9.07
0.91
-
0.91
-
21.0830
17.24
4.54
4.54
- 320 -
-------
21
21
21
21
21
21
21
21,
21,
21,
21,
21,
21.
22.
22.
22.
22.
22.
22.
22.
22.
22
22
22
22
22
22
22
23
0.68 0.68 15.42
2.27 0.91
0.45 2.27
9.07
2.27 2.27
APPENDIX P: TABLE VII PAGE 10 Op 10
SOLIDS REMOVED DURING RUN 8, KG. (RAW DATA)
DAY.HOUR GAS'R REGEN REGEN ELUTH BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSE
21.0930
21.1130 2.27 1.81
21.1145
.1230
.1330
. 1430
. 1530
. 1630
,1730
, 1800
, 1830
,1930
,2025
,2030
,2230
2300
0001 1.59 1.59
0030
0 1 30
0230
0330
0430
0530
0600 2.04
22.0630
22.0730
0830
1030
1 200
1300
1830
1900
2000 - - 0.00
0000
0.23 1.13 11.34
1.36 0.91 6.80
1.81
2.27 2.27
425.02 29.94
4.54
4.54
0.91
9.07
0.91
0.9!
26.76
5.44
1.81
0.23
22.68
4.54
4.54
0.91
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
0.91
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
4.54
0.
10.
45
43
0.45
- 321 -
-------
APPENDIX P: TABLE VIII PACE 1 OP 2
ANALYSIS OF SOLIDS REMOVED DURING HUN 8
TOTAL CARBON Wl*
DAY.HOUR GAS'R RFGFN REOEN ELUTR BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSE
1 . 1K00
2 . 0000
2.0800
2. 1800
3.0100
3.0700
3. 1800
4.0010
4.0315
4.0645
4.0900
4.2C;00
4.2359
5.0600
5. 1 100
5 . 1 5010
5.2100
6.C200
6.0600
6.0800
6. 1200
6. 1800
6.2359
7.0600
7. 1200
7. 1345
7 . M 1 5
7. 1800
7.2350
8.0600
8 . 1 300
8. 1800
S/.0005
9.06i)0
y. 1 130
y. 1320
-------
APPENDIX F: TABLE VIII PAGE 2 OF 2
ANALYSIS OF SOLIDS REMOVED DURING HUN 8
TOTAL CARBON WT*
DAY.HOUR GAS'R REOEN REGEN ELUTR BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSE
1 1 . 0600
12.0600
12. 1200
12.235V
13.0600
13. 1300
13.1 800
13. 1300
14.0600
14. 1200
14. 1800
14.23I?9
15.0600
15. 1200
15. 1800
15.2359
16.0700
16. 1200
16. 1800
17.0600
17. 1200
17. 1800
18.0001
18.0600
18. 1200
Iti. 1800
19.0001
19.0600
19. 1200
19. 1805
20.0630
2 .0630
2 . 1 1 00
2 . 1 200
2 . 1457
2 .2025
22.0001
22.0600
22. 1200
22. 1600
22.2000
0.20
0.
0.
0. 1 1
0.
0.
0.
0.
0.
0.13
0.03
0.
0.
0. 14
0.07
0.04
1 .84
0. 17
0.21
3.58
1.21
-
0.
0.75
0.58
0.39
0.07
0. 15
0.41
1.25
-
0.
0.50
-
0.89
0.66
0.25
0.89
0.06
0.J0
0. 11
0.02
0.
0.01
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.04
0.
0.
0 . 02
0.44
—
0.
0.
0.
0.
0.
0.
—
0. 10
-
—
0.
-
0.05
0.02
0.
—
—
0.
0.
10.32
0.76
1 .91
4.99
14.80
12.32
17.87
16.96
15.61
15.61
0.21 3.54
0.
10.06 0.04
0.02
0.79
0.
0.07
0.50
0.50
-
1.43
-
-
—
-
-
—
—
2.17
-
—
1 .98
-
—
-
—
_
5.91
1.93
—
—
—
-
—
0.22
0.22
0.
0.03
0.
0. 15
0.51
0.39
0.26
0.88
0.71
0.83
0.73
2.47
0.41
1.32
5.27
1 .63
2.52
2.49
0.88
0.
1 .94
0 . 66
2. 12
3.18
2.90
9.76
9.76
1.72
0.85
1 .58
0.22
2.54
0.97
0.97
- 323 -
-------
APPENDIX P: TABLE IX PAGE 1 OF 2
ANALYSIS OF SOLIDS REMOVED DURING RUN 8
SULPHATE SULPHUR WT.^
DAY.HOUR GAS'R REGEN REGEN ELUTR BOILER BOILER FLHTR
CYCLONE FINES BACK FLUE COARSE
1 1.0600
12.0600
12. 1200
12.2359
13.0600
13. 1300
13. 1800
13.2320
14.0600
14. 1200
14.1 800
14.2359
15.0600
15. 1200
15. 1800
15.2359
16.0700
16. 1200
16. 1800
1 7 . 0000
17.0600
17. 1200
17.1800
18.0000
18.0600
18. 1200
18. 1800
19.0000
19.0600
19. 1200
19. 1800
20.0630
21.0630
21 . 1 100
21.1 200
21.1457
21.2025
22.0000
22.0600
22. 1200
0. 18
0.89
0.28
0. 14
0.16
0. 15
0.15
0. 13
0.20
0.16
0. 15
0.14
0. 13
0. 13
0. 17
0.14
0.12
0. 1 1
0.11
0.11
0.12
0.09
—
W. 11
0. 15
0. 18
0. 10
0.14
0.10
0.95
0.07
-
2.05
0.15
-
0. 10
0.09
0.08
0 . 08
0. 1 1
1.00
2.14
2.64
0.59
.26
.50
.40
.50
.04
0.92
.14
.31
0.85
.15
.60
.33
0.09
1 .38
0.60
0. 1 1
0.08
0. 18
-
0.35
0.34
0.99
0.57
0.72
0.32
—
0.07
-
-
1.08
—
0.29
0. 18
0.68
—
-
0.90
1.19
1*65
0.95
0.93
-
-
-
—
—
—
0.77
-
—
0.71
—
—
-
—
—
0.41
0.37
—
-
^
—
—
—
2.03 3.08
2.77 5.66
1.37 4.45
2.21 2.79
- -
— —
- -
— —
— —
— —
- _
1.33 3.51
- -
— —
1.06 2.59
— —
— —
— —
_ _
— -
•» —
1.67 2.83
2.24
- -
— _
2.25
— —
— —
—
—
0.4^
0.26
0.51
0.41
0.44
0.45
0.33
0.44
0.25
0.33
0.40
0.16
0.28
0. 16
0.20
0.25
0.13
0.15
0. 17
0.50
0.57
0.20
0.23
0.21
0 . 20
0. 19
2.00
1.17
5.34
1.91
4.98
2.58
1.14
0.72
0.37
0.31
0. AV
- 324 -
-------
APPENDIX F: TABLE DC PAGE 2 OF 2
ANALYSIS OF SOLIDS REMOVED DURING RUN 8
SULPHATE SULPHUR WT.%
DAY.HOUR GAS'R REGEN RHGEN ELUTR BOILER BOILER ELUTR
CYCLONE FINES BACK FLUE COARSF
1 . 1 800
2.0000
2.0800
2. 1800
3.0)00
3.0700
3. 1800
4.0010
4.0315
4.0645
4.0900
4.2000
4.2359
5.0600
5. 1 100
5. 1500
5 . 2 1 00
6.0200
6.0600
6.0800
6. 1200
6. 1800
6.2359
7.0600
7. 1200
7. 1345
7. 1415
7. 1800
7.2350
8.0600
8. 1300
8 . 1 800
9.0000
9.0600
9. 1 130
9. 1320
9. 1745
10.0030
10. 1500
10.2359
22. 1600
22.2000
0.22
0. 17
0.45
0. 14
0. 1 1
0. 13
0. 1 1
0. 14
-
—
0. 10
0. 10
0. 13
0. 14
—
0. 12
0. 1 1
0. 17
0. 16
-
—
0. 16
0. 14
—
0. 12
—
-
0. 15
0.20
0.24
0.23
0. 17
0.23
0.23
-
0.24
0.20
2.68
—
0.31
0. 12
0. 12
-
.17
.37
-
.37
.42
.20
.06
-
-
1.30
1.00
1 .36
0.98
-
1.01
1.28
1.39
-
1.63
-
1.35
1.06
-
1.25
-
-
1.35
1.28
1.34
1.20
1.33
1. 17
1 .44
-
1 .26
1.24
-
-
2.36
1.23
1 .23
3.16
4.44
0.65
0.51
1.06
0.53
0.56
0.56
0.49
0.59
1.03
2.02
1 .05
2. 1 1
1.90
1.62
0.49 0.97 2.22
2.26
3.22
2.33
2.50
2.33
2.34
3.10
3.46
3.35
3.45
4.44
1.13
0.82
0.82
3. 13
3.29
1 .54
1.54
4.70
2.54
2.54
0.26
0. 18
0.25
0.35
0.34
0.23
0.47 1.11 1.62 0.30
0.42 -
0.46 2.10 2.27 0.20
0.39 2.02 2.5?
0.38 1.66 2.38 0.25
0.41 1.91 2.44 W.21
0.32
0.20
0.28
0.33
0.4?
0.34
0.50
0.42
0.54
0.49
0.18
- 325 -
-------
DAY.HOUR
APPENDIX F: TABLE X PAGE 1
ANALYSIS OF SOLIDS REMOVED DURING RUN 8
TOTAL SULPHUR WT.#
GAS'R REGEN REGEN ELUTR BOILER BOILER
CYCLONE FINES BACK FLUE
2.0000
2.0800
2.1800
3.0100
3.0700
3.1800
4.0010
4.0315
4.0645
4.0900
4.2000
4.2359
5.0600
5.1100
5.1500
5.2100
6.0200
6.0600
6.0800
6.1200
6.1800
6.2359
7.0600
7.1200
7.1345
7.1415
7.1800
7.2350
8.0600
8.1300
8.1800
9.0000
9.0600
9.1130
9.1320
9.1745
10.0030
10.1500
10.2359
11.0600
4.31
4.37
3.82
3-74
3.76
4.38
3.37
3.17
-
-
3.85
3-72
3.90
4.40
-
4.46
4.14
4.21
4.26
_
4.24
4.91
-
5.20
-
-
4.41
4.36
4.56
5.18
4.76
4.40
4.96
-
4.27
4.21
4.23
-
4.95
5.58
_
2.57
2.53
—
2.80
3.18
2.22
2.29
-
-
2.11
2.70
2.87
2.95
-
3. 33
3.15
3-37
-
3.30
3-38
3.50
-
3.52
-
-
3.43
3.24
3.46
2.88
3.54
3.62
3.87
-
3.61
3.40
-
-
3.65
4.22
6.97
6.30
4.96
4.65
3.89
4.49
6.17
5.20
3.52
5.29
6.79
4.04
6.15
4.03 2.79
4.72 2.64 2.39
4.85 3-27 2.22
3.18
5.34
3-95
3.71
3.82
3.69
4.21
3.47
3-91
4.57
4.47
4.57
3.65
4.11
5.04
2.95
3.48
3.85
5.18
3-45
3.85
3.62
4.74
OF 2
ELUTR
COARSE
3.75
3-72
3-91
3-85
5.18
3.88
3-79
3.80
5-19
0.53
4.36
6.11
5-33
5,
3.
5.
5.
5.
09
74
49
39
5-17
6.02
5.48
4.16
- 326 -
-------
DAY.HOUR
APPENDIX F: TABLE X PAGE 2 OF 2
ANALYSIS OP SOLIDS REMOVED DURING RUN 8
TOTAL SULPHUR WT.#
GAS'R REGEN REGEN ELUTR BOILER BOILER ELUTR
CYCLONE PINES BACK FLUE COARSE
12.0600
12.1200
12.2359
13.0600
13.1300
13.1800
13.2320
14.0600
14.1200
14.1800
14.2359
15.0600
15.1200
15.1800
15.2359
16.0700
16.1200
16.1800
17.0000
17.0600
17.1200
17.1800
18.0000
18.0600
18.1200
18.1800
19.0000
19.0600
19.1200
19.1800
20.0630
21.0630
21.1100
21.1200
21.1457
21.2025
22.0000
22.0600
22.1200
22.1600
3.06
2.58
4.28
4.12
3.58
3.65
3.57
4.21
4.56
4.73
4.35
4.17
4.56
4.45
5.56
5-87
7.56
6.68
7.14
8.59
12.28
-
8.10
8.31
8.65
8.01
7.50
7-32
7.05
8.71
-
7.04
7.42
-
7.15
7.71
7-73
7-37
6.52
6.41
2.70
3.12
2.94
3-50
3.08
2.63
2.71
3.04
3.33
3-33
3-72
3-38
3.41
4.00
4.13
5.82
5.53
5.38
6.76
8.72
8.44
-
7.66
7-19
7.83
7.23
6.31
5.67
-
7-58
-
-
4.83
_
6.13
7-51
6.50
-
_
5.89
10.50
8.01 4.12
4.. 97 4.25
5.74 4.41
4.05
3.90 5.81
5.48
3.27
3.92
3.44
4.55
3.46
3.28
6,
4.
4.
5-
5-
5.
5.
69
49
83
18
38
58
19
5.11
88
90
26
4.94
,56
.13
,79
.94
,97
7.34
6.52
.68
,86
-97
,81
.54
,19
5.02
6.73
—
4.89
-
_
5.46
-
_
4.76
-
-
5.18
5.82
_
3.82
-
_
4.00
6.98
6.90
5.81
5.75
6.71
7.83
- 327 -
-------
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DAY, HOUR
FIG. F-18.
- 337 -
-------
CAFB RUN 8.(contd)
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- 338 -
-------
GASIFIER TOP SPACE PRESSURE RUN 8
to
6
5
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APPENDIX G
CAFB RUN 9
OPERATIONAL LOG, INSPECTION AND DATA
PAGE
Pre-run Explosion in Gasifier Unit.
Operational LOK. 347
Inspection 357
Inspection, Figures Gl-22 360
Data Table I Temperatures and Feed Rates. 376
II Gas Flow Rate. 392
III Pressures. 4o8
IV Desulphurisation Performance. 424
V Gas Composition. 440
VI Sulphur and Stone Cumulative Balance. 461
VII Analysis of Solids, Total Sulphur. 482
VIII Analysis of Solids, Sulphate Sulphur. 485
IX Analysis of Solids, Total Carbon. 488
X Solids Removed. 491
XI Gasifier Bed Particle Distribution. 498
XII Regenerator Bed Particle Distribution. 503
XIII Elutriator Coarse Particle Distribution. 507
XIV Stone Feed Particle Distribution. 510
XV Trace Element Analysis by Neutron Activation. 512
XVI Spark-Source Mass Spectrometric Analysis. 51^
Figure G-23 Chronological Plot of Unit Performance. 528
Figure G-24 Chronological Plot of Gas Space Pressure. 531
- 340 -
-------
APPENDIX G
CAFB RUN 9
PRE-RUN EXPLOSION IN GASIFIER UNIT
On the morning of 22nd October 197^» an explosion occurred in
the gasifier during attempts to check out and set up the start-up
burner in the preparation for Run 9« Extensive damage to the unit
occurred which delayed the start of the run by about two weeks.
FiguresG-1 andOr-2shows the damage done to the gasifier lid which was
completely lifted by the explosion, whereas FiguresG-3 andG-4 show the
large cracks in the gasifier refractory. Damage to the cyclones also
occurred as shown in Figures G-5 andGWj.
An inquiry was convened to find out the cause of the
explosion, and various action points identified to prevent a
re-occurrence. A detailed description of the events leading up to
the explosion, and recommendations for future procedures is contained
in a file note written by the investigating committee and is incorporated
in this Appendix,
- 341 -
-------
APPENDIX G
CAPS GASIFIER EXPLOSION - 22nd OCTOBER 1974
WHAT HAPPENED
After usual calibration checks of flowmeters the pilot flame of
the gasifier was lit and established, and then main flame light-up
attempted, unsuccessfully.
Air purging was maintained for about 10 minutes, passing about
30 volumes of air through the gasifier, and then re-lighting was
attempted.
After the pilot was established, the main burner light-up was
attempted, and appeared to have been established, but with a rather
yellow flame. When the gas flow was reduced to increase air/fuel
ratio and rectify flame yellowing there was an immediate explosion
which lifted the 350 Ib. gasifier lid, cracked the refractory walls
and moved the cyclone off-takes.
The operators reacted calmly, confirming that nobody was hurt,
and making safe by cutting off the gas supply to the building. Their
early concern was on how quickly could the problem be solved so that
the run might proceed as planned.
Damage caused by the incident will be rectified by 4th November,
though the effectiveness of the repair of the refractory lining can
only be assessed when the gasifier is next heated up.
ANALYSIS OF EVENTS
All operators had been following standard operating instructions,
The control settings of the flow meters were re-checked and
found to be correct for the propane gas, but somewhat different from
the pre-explosion records for air. This may be due to disturbance
by the explosion since manometer fluid was found in the lines.
However, the gas air mixture would still have been flammable, both
before and after the adjustment which initiated the explosion
(stoichiometric air : fuel ratios being 1.5 : 1 and 2.3:1
respectively).
- 342 -
-------
It was also found that the fire eye controller was set to retain
a pilot flame throughout operation, and not to shut down the pilot
flame once the main flame was established. The controller can see
flames, but not distinguish between pilot flame and main flame. This
was as the result of a considered decision sometime ago to minimise
shut-downs due to transitory flame failure.
It was, therefore, concluded that:
(a) The pilot flame did not ignite the main flame.
(b)
(c)
The fire eye controller did not recognise that the main
flame had not been established, and so allowed flammable
gas mixture to fill the gasifier.
Disturbance of the gas flows caused ignition to occur
from the pilot which led to explosion.
These conclusions are the only ones we could reach which would
explain the facts, but we do not have positive evidence.
ACTION PROPOSED WITH CAFB GASIFIER
The actions proposed are:
1. Modify fire eye controller to cut out the
pilot flame 5 seconds after the main gas is
admitted (so allowing the fire eye to detect
presence or absence of the main flame).
2. As a back-up to the pilot solenoid a manual
pilot isolating valve will be installed.
3. An MSA gas detector will be installed in the
pit and connected to an alarm.
4. Install alternative valve in Stordy Hauck
burner gas piping to make it fully
controllable for use with propane, since
although it was supplied against
specification for propane, it has been found
that the main gas supply pipe and valve is
sized for towns gas, of which five times the
volume is required.
ACTION
Done
Done
GLJ/RD
Temporary
modification
for this run:
change after-
wards
- 343 -
-------
ACTION
5. Re-site solenoid valve nearer to burner. GLJ before
this run if
possible
6. Check that the CAFB gasifier warm up system Done
complies with the Code of Practice
recommendations of the Gas Council which was
issued after the CAFB system was designed, or
that safety hazards are not caused by
discrepancies from the code.
7. Provide better proof of air flow to the gas GLJ after
burner by replacing the pressure switch in this run
the air line connected to the fire eye by an
orifice flowmeter connected to the fire eye.
8. Provide for cleaning the fire eye sight glasses Done
more frequently.
9. Ensure two men present at all times during Done
gasifier warm up.
10. Incorporate appropriately all of the above GLJ in
actions in a revised set of written operating hand
instructions.
11. Give a training session to the operators GLJ in
incorporating these changes. hand
IMPLICATION WITH CAFB BOILER
The CAFB boiler is different from conventional boilers in that
the fuel gas is of unknown and changing composition at the time of
light-up.
Just prior to light-up the boiler is being purged by passage of
inert gas from stoichiometric combustion in the gasifier. For
light-up of the boiler additional fuel oil is passed into the
fluidised bed of the gasifier causing a combination of:
(a) direct vaporisation of volatiles.
- 344 -
-------
(b) cracking with formation of further volatiles and
deposits of carbon.
(c) burning of carbon deposits in lower parts of the bed to
generate further combustible gas.
These processes take place at different rates, and although it
takes about 6 minutes for the gas to reach maximum richness, it is very
difficult to estimate exactly when the gas entering the boiler reaches
flammable limits, though best estimates of composition and experience
on light-up put it at about 6 seconds. The significance of this is
that only about 3 seconds flow of flammable gas should be allowed
without successful ignition, before aborting the operation to avoid
explosion hazard, but the start of the 3 seconds is not known within
_+2 seconds. In practice, it has taken less than 10 seconds between
when the fuel oil pumps to the gasifier have been switched on and
there has been ignition in the boiler.
The recent incident involved explosion of about 1,000 Btu's of
gas in the gasifier. The boiler when full would contain approximately
6,000 Btu's of gas.
ACTION PROPOSED WITH CAFB BOII£R ACTION
1. Modify the instructions to allow maximum In hand
9 seconds to prove the main flame on the
boiler before aborting (before next run).
2. During start-up there should be no personnel In hand
in the hall, and nobody should be allowed to
approach the back door of the boiler until the
main flame has been proved. The sliding doors
at the back of the boiler should be open, and
nobody should be allowed to approach the
neighbourhood of these doors from the outside.
3. Ensure that any recommendations for safe GLJ after
operation arising from operation of the CAFB this run
pilot plant should be fed into the EPA
programme.
- 345 -
-------
SITE-WIDE ACTION ACTION
1. Check on all burners at ERCA to confirm that RD
a main flame failure will result in a positive
automatic shutdown.
All actions "in hand" will be completed before start-up.
R. Deval G. L. Johnes R. H. Vickers
RHV/MMM
1.11.74.
- 346 -
-------
APPENDIX G
CAFB RUN 9
OPERATIONAL LOG
4.11.74. to 8.5.74. (Unit Warm Up)
Warm up of the unit started at 15.00 on 4.11.74., and the
temperature was progressively raised by about 12°C per hour. At a
unit temperature slightly in excess of 500°C, carbon in the cyclones
and ducts laid down from the previous run caught fire and the
temperatures in that region rose rapidly. Sparks of glowing carbon
were clearly visible through the sight glass at the back of the
boiler. The burn-out lasted for approximately one hour after which
temperatures dropped to normal.
At 18.15 on 6.11.74., kerosine was introduced (unit temperature
»A. 700°C), and the propane progressively backed off. Stone addition
started at midnight on the same day initially using bed material
recovered from the previous run. Several minor leaks in the cyclone
ducts and gasifier lid were sealed with Sairset fireclay.
A switch to fuel oil combustion was made at 13.20 on 8.11.74.
prior to gasification at 19.00.
Throughout the period of warm up the usual minor teething
problems again occurred. The warm up propane burner was again subject
to frequent flame outs due to condensation of water in the fire eyes
until Np purges were fitted.
8.11.74. (Day 1 of Gasification)
Approximately two hours after initial start-up on gasification
the automatic shutdown system was activated by an electrical fault in
the 12 volt supply to the pulsers and alarm relays. In the absence
of fuel oil, runaway regeneration of the bed material occurred
resulting in a rapid rise in bed temperature to levels in excess of
1,000°C. To halt the temperature rise the bed was slumped.
9.11.74. (Day 2)
Shortly after midnight the gasifier plenum air was restarted and
- 347 -
-------
the bed material initially warmed up on kerosine combustion before
transferring to heavy fuel oil combustion. Gasification recommenced
at 01.35.
At 06.00, the flue gas analysis sampling line was replaced by a
new sampling line using a porous silumanite probe inserted into the
boiler flame. It was hoped this new sampling method would avoid the
problems associated with S02 pick up by the glass wool filter in the
old system. No change in the flue gas analysis was observed on
change over to the new system.
Throughout the day trouble was experienced with the fines return
system.
10.11.74. (Day ?)
Shortly after midnight a high gasifier lid pressure was observed
(yw6 kilopascals) and both the air flow and fuel flows were reduced to
alleviate this while preparing to attempt an on-line decoke. However,
at 01.40 a main flame failure caused a change in plans and instead
sulphation followed by slumped bed decoke was carried out.
Before the decoke was carried out the new flue gas sampling probe
was partially withdrawn to allow a clear view of the gasifier to burner
duct. Unfortunately during this operation the silumanite sheath
became detached from the Firebird white tube and dropped off inside the
boiler. The old sampling system was restored while a replacement
sheath was found.
Throughout the day the bed material was maintained at gasification
temperatures by periodically operating on kerosine combustion.
Meanwhile various repair and maintenance jobs were carried out including
a boiler clean out.
11.11.74. (Day 4)
Gasification was restarted at 01.10 and continued till 10.05 when
an electrical fault caused a brief shutdown of one hour duration.
Minor problems encountered were regenerator sampling line and
stone feed blockages. The bottom fuel injector also blocked.
- 348 -
-------
A new silumanite probe was fitted and the new flue gas
sampling method resumed.
12.11.74. (Day 5)
Problems with the fines return system re-occurred throughout
the day. High stone feed rates were used to increase bed depth and
this resulted in the need to periodically clean the feed hopper system
to remove fine material which caused blockages.
At 19.55. air was introduced below the gasifier lid to try to
minimise the rate of pressure rise due to lay down of coke. The rate
of air injection was progressively increased to 1,250 litres/minute,
while the burner premix _air was reduced to compensate.
13.11.7^. (Day 6)
Early in the day the flue gas sampling system was replaced
because the silumanite probe became blocked. This new system was
obviously not an improvement and was discarded for the rest of the
run.
At 21.40 a main flame failure occurred for no apparent reason.
14.11.74. (Day 7)
Gasification restarted at 00.30 after the fuel injection pumps
were flushed with hot oil to reduce the initial pressure build-up.
After a period of several days trying to raise the bed level, it
became evident that the stone feed material was too fine and most of
the feed was not being retained by the bed. A change was made to a
coarser fraction of stone.
During the earlier shutdown period the air to the lid was shut
off and this was re-introduced at the same rate at 10.30.
15.11.74. (Day 8)
An uneventful day, but the high gas space pressure necessitated
a shutdown for a slumped bed decoke at 22.30. This was carried out
without prior sulphation.
- 349 -
-------
16.11.?^. (Day 9)
After a successful decoke, gasification was resumed at 02.30 and
unlike previous occasions when sulphation was carried out,
desulphurization was immediate.
At 03.30, the pressurisation unit for the boiler failed and
activated the automatic shutdown sequence. The motor on the
autovalve controlling the water flow to the cooling tower failed in
the closed position resulting in all the cooling water being fed to the
cooling tower irrespective of the boiler water temperature.
Gasification restarted at 05.50 and proceeded until 21.15, when
loss of pressure in the pressurisation unit again caused a shutdown.
At 21.50 a restart was attempted, but failed to get ignition even
after twenty seconds. A second attempt was also abortive, this time
attributed to the presence of cold fuel in the fuel line. However,
after two more abortive attempts a fire valve in the fuel line was
found to be closed.
17.11.74. (Day 10)
Gasification began again at 01.55. The experiment of air
injection to the lid was continued.
A few minor problems occurred throughout the day, but on the
whole a good day's gasification.
18.11.71. (Day 11)
A restriction in the gasifier to regenerator transfer line
resulted in a period of poor regenerator performance. A high bed
depth in the regenerator could not be maintained, and difficulty was
experienced in keeping the regenerator temperature below 1,075°C. The
transfer line was rodded out and regenerator performance improved.
A desulphurising performance of 85$ was considered poor at a bed
depth of ^vllO cms, and it was decided to test conditions with high
levels of bed carbon. One theory put forward for the poor
performance was that the air to the lid may be causing some
regeneration of the stone above the bed. This was tested by
switching off the air, but the flue gas S02 levels remained constant,
and therefore the air to the lid was restored.
- 350 -
-------
19.11.74. (Day 12)
Sulphur removal efficiency had levelled out at 85$, and attempts
to improve this value by increasing bed carbon levels had failed.
The unit was now operated at low Ca/S mole feed ratios to assess the
effect of this variable. Operation in this way continued throughout
the day.
20.11.74. (Day 1?)
Gasification continued smoothly until 12.02 when a high gasifier
lid pressure necessitated a shutdown and burn-out.
At 21.00 gasification was resumed, and immediately both cyclone
drain systems were found to be inoperative due to cyclone blockage
as a result of the burn-out. Both systems were rodded out and a
large amount of carbonaceous material removed.
21.11.74. (Day 14)
The back of the boiler was cleaned out shortly after midnight,
and about 350 kg of stone removed.
Problems with cyclone blockages and control of regenerator
temperature featured throughout the day. Low Ca/S molar feed rates
were continued.
22.11.74. (Day 15)
The unit was performing well but the gasifier lid pressure was
high and steam/air injection above the bed was tried for a period of
three hours to try to decoke the system.
This approach was unsuccessful and the unit was shutdown at
16.50 to carry out a steam/air slumped bed decoke.
Gasification was restarted at 22.50 and once more both cyclones
were found to be blocked from the debris accumulated during the decoke.
23.11.74. (Day 16)
The initial problems with blocked cyclones was finally resolved
and conditions were set up to test high bed velocities (./vl.5 m/s). A
- 351 -
-------
limiting factor in this study was the high distributor pressure drop
due to lime build up below the distributor.
At 15.45, a main flame failure occurred. The oil pressure in
the main fuel pump was showing zero, although apparently the main
supply tank was far from empty. However, a switch to an alternative
supply tank resulted in a successful restart at 16.50.
Conditions were set up to test the effect of air/fuel ratio at
high bed velocities.
At 22.15, steady drops of oil were discovered leaking from the
bottom of the unit and a can was positioned to collect it.
24.11.74. (Day 17)
A main flame failure occurred at 00.^0 and the fire eyes were
checked and cleaned, and gasification restarted at 01.10.
At 12.50 tests involving I^S injection into the middle of the
gasifier bed through a central tapping were carried out. This was
continued till 14.45 after which gasifier and regenerator stone samples
were taken for analysis. The test was repeated at 19.16 for thirty
minutes. Throughout both test periods no change in flue gas SOg levels
was noted indicating complete absorption of HpS sulphur by the bed.
A similar test with SOg injection was carried out at 20.07 for
thirty minutes duration, and again complete absorption of the sulphur
from the additive was obtained.
25.11.74. (Day 18)
The unit was deliberately run under fuel rich conditions (A/F
•f^ 21$) to test sulphur removal efficiency at high carbon levels on the
bed limestone. This led to high COg levels and low SOg levels in the
regenerator tail gas.
Later conditions were established with air/fuel ratio around
2.6%, and regenerator performance was restored. The unit was operating
at a high gasifier lid pressure (^\_ 6 kilopascals).
- 352 -
-------
26.11.74. (Day 19)
At 01.00 a main flame failure occurred, but a restart was made
after ten minutes. However, both cyclones were blocked.
At 14.15 an electrical power failure produced a fifteen minutes
shutdown.
27.11.74. (Day 20)
The stone feed to the gasifier was changed from BCR 1359 to
Aragortite. The sulphur removal performance seemed to improve with the
new stone, but, the flue gas sampling line required frequent attention
due Lo blockage by a fine white powder. Furthermore difficulty was
experienced in maintaining bed depth despite a high stone feed addition
(Ca/S 1.5 m). This indicated rapid attrition in the bed and a large
amount of material lost to the boiler as fines.
At 21.15 the high gasifier lid pressure necessitated a shutdown
for a slump bed decoke.
28.11.74. (Day 21)
Gasification was restarted at 04.30 and again cyclone blockage
problems were encountered. A main flame failure occurred at 09-30,
and gasification was again resumed at 12.05- BCR 1359 was used
instead of Aragonite as the stone feed.
Another flame failure occurred at 15-30 without apparent reason,
and gasification was restarted at 20.20. While in the process of
cleaning the cyclone drain system the central fuel injector, which
had been blocked and not in use for sometime, suddenly burned out and
hot bed material escaped from the unit onto the pit floor. The unit
was shutdown and the injector blanked off.
29.11.74. (Day 22)
After a number of abortive start-up attempts, gasification finally
got underway at 08.00.
Once stable conditions were established the fuel supply was
gradually reduced in order to increase bed temperature and explore the
- 353 -
-------
off eel of this variable on sulphur removal efficiency.
30.11.74. (Day
The flue gas SOp level remained fairly constant with increasing
bed temperature until 980° C when the level increased.
At 11.50 the regenerator temperature was operated at 1,130°C
without any apparent ill effects.
1.12.74. (Day 24)
Early tests with high regenerator temperatures 1,100-1, 200° C,
and high regenerator C02 and lower S02 tail gases were completed by
09.00, and the regenerated temperature was restored to a more normal
level (**» 1,060°C).
Attempts to increase bed depth above -*-110 cm were thwarted by
cyclone blockages due to the high stone circulation at deeper beds.
2.12.74. (Day 25)
Throughout the morning problems with cyclone blockages occurred
arid at 17.55 the unit was shutdown prior to a slump bed burn-out.
Gasification restarted at 22.00.
3.12.74. (Day 26)
Early in the day the unit was lined out at a high air/fuel ratio
(^28%), but progressive blockage of the gasifier distribution resulted
in a reduction in air supply and fuel rich conditions in the gasifier.
In order to clean out the distributor the bed was partially
drained, the unit shutdown and the remaining bed sulphated.
Approximately 40 kg of material was removed from below the distributor.
The regenerator distributor was similarly cleaned out and the
unit restarted at 20.35-
4.12.74. (Day 27)
To maintain a good circulation of fines in the system, the unit
was operated at a high stone feed with alternate supplies of sieved
- 354 -
-------
.'iiul unt.ievcd utone.
The effect of thiophene injection was tested at 19.36 by
introducing the liquid into the bed through a central tapping.
3.12.74. (Day 28)
Experiments with air injection into the gasifier upper manometer
tapping were carried out at various times throughout the day. It
soon became clear that the blast of air was breaking up the stone and
generating fine material. Evidence for this came from the increase
in the cyclone drain temperatures. Also evident was an improvement
in sulpnur removal efficiency which persisted even when the stone feed
was reduced to zero.
Unfortunately, prolonged testing under these conditions was
curtailed by the distributor again progressively blocking up causing
a drop in bed velocity, and the need to shutdown before a loss in
fluidisation occurred.
6.12.74. (Day 29)
At 00.20 the unit was shutdown and sulphation began. After this
was completed the bed was slumped and the underside of the distributor
cleaned out. Approximately 30 kg of stone was removed.
Flue gas and air was then introduced above the bed to decoke the
system.
Gasification was restarted at 22.15.
7.12.74. (Day 30)
Initially the unit was operated at high bed velocity (1.5 m/sec.)
and a shallow bed (-^75 cm), but the sulphur removal efficiency was low
and consequently the bed velocity was reduced, the stone feed rate
increased in order to raise bed depth, and the air jet restored to the
middle of the bed. Almost immediately % SRE improved.
Throughout the day the effect of bed depth was explored by
progressively withdrawing bed material and studying performance.
- 355 -
-------
An attempt to control the circulation of fines by injecting
steam above the bed proved unsuccessful.
8.12.74. (Day
Instead of steam injection above the bed, Np injection was tried
but this too had no effect on performance.
Various attempts to improve performance by increasing the fines
circulation rate were carried out, culminating in the use of Aragonite
stone.
A good % SHE performance was obtained with Aragonite stone, but
it soon became obvious that this performance was artificially good
because of Aragonite contaminating the sampling filter.
9.12.7^. (Day 32)
At 09.30 the gasifier top space pressure was high and, therefore,
it was decided to shutdown the unit and carry out a slumped bed decoke.
- 356 -
-------
APPENDIX G
CAFB RUN 9
INSPECTION
Gasifier and Regenerator Refractory
At the end of Run 9i a slumped bed decoke was carried out, and
hence the state of the unit on subsequent inspection reflects the
efficiency of this procedure. Figures G-7, G-8, & G-9 show various views
of the gasifier unit after stripdown. This shows the remarkably
clean condition of the refractory walls and also that the sealing material
In the cracks from the pre-run explosion was still intact.
However, close inspection indicated the Sairset sealing material
had become friable, loose and obviously far from leak tight.
Presumably, during gasification the cracks were effectively sealed by
carbon laid down from the process, and this would account for the
observation of some leakage immediately after a slumped bed decoke
which disappeared after several hours operation.
The view of the gasifier bed material (FigureG-9)shows a piece
of asbestos rope and odd fragments of carbon which dropped on the bed
during the removal operation. Otherwise the bed was generally free
of agglomerates and homogeneous throughout its depth.
A notable exception to this was a large lump of fused limestone
of the general shape of the transfer line 'post box1 which was resting
on the plenum immediately below the 'post box'. This may have been
formed during the run when the transfer line was rodded out after an
operational malfunction tripped the Np supply and caused air to be
supplied to the injectors for a brief period.
The regenerator bore was generally clean, but oil markings on
the wall coincided with the height of the steel floor of the unit
suggesting the point of seepage of fuel oil from the gasifier. At the
top of the regenerator, where the bore diameter was restricted, material
was laid down causing a partial blockage.
- 357 -
-------
Gasifier and Regenerator Distributors
Some difficulty was experienced in removing the gasifier
distributor during the dismantling process. This was probably a
result of the tarry material surrounding the distributor. FigureG-10
gives a side view of the distributor showing the extensive seepage of
oil. The condition of the distributor air nozzles is shown in
Figure G—11. Approximately a third of the air nozzles were blocked or
partially blocked, and there was some evidence of oil seepage downwards
through two of them.
The aperture between the bottom plate and the regenerator
distributor was completely filled with tarry material. Figure G-12 gives
a view of the regenerator distributor which was in a reasonably good
condition with only one blocked air hole.
Gasifier and Regenerator Penetrations
The fuel injector projecting through the distributor at the
bottom of the gasifier was burnt off at the fuel outlet holes and also
12" below this point. One of the side injectors was also burnt
away. The gasifier thermocouples had distorted outer metal sheaths
and some burnt surface damage.
All three regenerator thermocouples had fractured ends, although
this may have resulted from falling material during the removal of the
distributor. The regenerator outlet refractory block housed inside
flexible bellows was fractured into two and the bellows also showed
some damage.
Gasifier/Regenerator Transfer Line Agitators and Injectors
The left hand agitator was distorted, and the angled outlet hole
partially blocked. The right hand agitator was also distorted, but
clear. Both injector holes were clear.
Gasifier Outlet to Cyclones
Figures G-12>&Grl4 show two views of the outlet from the gasifier
to the cyclones.
Some deposits in the zone between the two outlet ducts is clearly
shown, but the passages themselves are remarkably clean.
- 358 -
-------
Oasifler Cyclones
Photographs of the condition of the cyclones are given in
Figures GKL5-G~l8« The refractory walls appear to be reasonably clean,
but evidence for the extent of carbon laid down prior to the slump
bed decoke comes from the large flakes of carbon visible at the
bottom of the cyclone. This material was probably responsible for
the cyclone drain blockages experienced on restart after a slump bed
decoke.
The silicon carbide tubes shown in Figures G-J.7, and G-18 were
covered with white flaky material. Figure G-18 clearer shows the
refractory block; which carries the silicon carbon tube of the right
hand cyclone, was fractured into two pieces. However, the refractory
block which was located inside the flexible bellows was intact despite
having to be Jointed with Sairset prior to the run.
Main Burner
The central steel tube of the burner had two cracks
approximately 1" in length, and also the edge of tube was burnt away.
Figures G-l^& G-20 show this clearly.
Boiler
Figure Q-I1 gives a general view of the back of the boiler with
the door open. This shows a sizeable quantity of lime particles,
some of which were quite coarse indicating that the cyclones had not
been very effective over part of the operational period. The entries
into the first tube pass were coated, and in some cases completely
blocked by a thick layer of lime deposit. Figure G-22 shows a close-up
view of the fire tube leading down to the burner at the far end.
Approximately 195 kgs (4}2 Ibs.) of material was removed from
the boiler back end, 75 kgs (165 Ibs.) from the boiler front plenum
and a further 59 kgs (1^0 Ibs.) from the boiler furnace tubes.
- 359 -
-------
Fig. G-l Gasifier Lid Damage after Pre-run Explosion
Fig. G-2 Gasifier Lid Damage after Pre-run Explosion (second
view)
- 360 -
-------
Fig. G-3 Vlew of Rectory Cracks after Pre-run Explosion
- 361 -
-------
Fig. G-4 View of Refractory Cracks after Pre-run Explosion (second view)
- 362 -
-------
Fig. G-5 Damage to Cyclones after Pre-run Explosion
- 363 -
-------
Fig. G-6 Damage to Cyclones after Pre-run Explosion
- 364 -
-------
Fig. G-7 View of Gasifier after stripdown
- 365 -
-------
Fig. G-8 View of Gasifier after Strlpdown
- 366 -
-------
Fig. G-9 View of Gasifier after Stripdown
Fig. G-10 Side View of Gasifier Distributor
- 367 -
-------
Fig. G-ll Condition of Gasifier Distributor Air Nozzles
Fig. G-12 View of Regenerator Distributor
- 368 -
-------
Fig. G-13 View of Cyclone Entry Ducts
Fig. G-14 View of Left Hand Cyclone Entry Duct.
- 369 -
-------
Fig G-15 View of Left Hand Cyclone
Fig G-16 View of Right Hand Cyclone
- 370 -
-------
Fig G-17 View of Left Hand Cyclone Offtake Tube
- 371 -
-------
Fig G-18 View of Right Hand Cyclone Offtake Tube
- 372 -
-------
Fig G-19 View of Main Burner Central Steel Tube
Fig G-2O View of Main Burner Central Steel Tube
- 373 -
-------
Fig G-21 General View of Back of Boiler
- 374 -
-------
Fig G-22 Close up view of Boiler Fire Tube
- 375 -
-------
RUN 9:
APPENDIX. G, TABLE I.
TEMPERATURES AND FEED RATES PAGE
1 OF 16
A
1
1
1
Y.HOUR
• 1930
• 2030
.2130
TEMPERATURE* DEC. C.
GASIFIER REGEN. RECYCLE
920.
930.
928.
1030*
1008.
980.
0.
0.
0.
FEED
OIL
1
1
1
58.
67.
65.
RATE KG/HR
STONE
1
1
1
2.
2.
4.
3
3
5
1 . 1930
1 .2030
1 .2130
SHUT
2.0230
2.0330
2.0430
2.0530
2.0630
2.0730
2.0830
2.0930
2. 1030
2. 1 130
2. 1230
2. 1330
2. 1430
2.1530
2. 1630
2. 1730
2. 1830
2. 1930
2.2030
2.2130
2.2230
2.2330
SHUT
4.0430
4.0530
4.0630
4.0730
4.0830
4.0930
4. 1030
920.
930.
928.
DOWN AT
958.
951.
935.
903.
8R9.
8R5.
900.
920.
927.
925.
923.
910.
890.
880.
895.
880.
904.
895.
870.
900.
900.
900.
DOWN AT
885.
875.
875.
905.
905.
890.
1.2130 FOR
1000.
1005.
990.
975.
965.
950.
970.
1020.
1052.
1050.
1058.
1055.
1055.
1050*
1048*
1040.
1042.
1045.
1045.
1050.
1055.
1055.
4 HOURS
50.
50.
50.
50.
50.
50.
45.
38.
35.
35.
40.
40.
40.
40.
38*
38.
36.
36.
32.
32.
30.
30.
2.2330 FOR 28 HOURS
940.
990.
1040.
1040.
1035.
1038.
55.
53.
50.
50.
49.
45.
147.
163-
133.
194.
151.
161 <
169.
168.
173-
182.
184.
183.
187.
4
8
4
7
9
0
6
0
7
0
0
2
7
188.5
188.
188.
182.
186.
184.
179.
186.
185.
156.0
156.0
156.0
155.2
156.4
156.0
0.
18. 1
26.3
24.5
22.2
25.4
3.6
2.7
3.2
3.6
3.6
4.5
4-5
13.2
12.2
26.8
17.7
12.2
31 «B
13.2
11.3
14. 1
3.6
12.2
19. 1
29.9
15.9
29.0
MISSED DATA READING
- 376 -
-------
RUN 9:
APPENDIX Or TABLE I.
TEMPERATURES AND FEED RATES PAGE
? OE 1
AY. HO UK
A. \ P30
A* 1330
4. 1 430
4. 1 530
4. 1 630
4. 1 730
4. 1830
4. 1930
4.P030
4. PI 30
4. PP30
/'•P330
5. 00 30
5.01 30
5.0P30
5.0330
5. 0430
5.0530
5.0630
'•..01730
5.0R30
5.0930
5. 030
5. 130
5. P30
5. 330
5. /30
5. 530
5. 630
S. 730
5. 830
5. 930
5.P030
5. PI 30
S.PP30
5.P330
6. 0030
6 .01 30
6. 0230
A. 03 30
TEMPERATURE* DEP. C. EEFD RATE KG/HR
GASI El ER
9 18.
896.
R90.
903.
903.
89P.
888.
880.
884.
905.
9 1 5.
905.
9P0.
920.
9P0.
9P0.
910.
CM 0 .
890.
905.
900.
896.
89 1 .
89 1 .
900.
900.
909.
908.
896.
885.
905.
900.
880.
905.
900.
9 1 5.
895.
900.
905.
905.
REGEN.
1013.
10PR.
1036.
1040.
104P.
1045.
1048.
1046.
104R.
1050.
1050.
1050.
1050.
1070.
1065.
1075.
1040.
1040.
1045.
1045.
1 040 .
1042.
1039.
1 040 .
1055.
1040.
1045.
1050.
1046.
1042.
1042.
1042.
1040.
1040.
1 040 .
1040.
1040.
1045.
1040.
1 0^0 .
RECYCLE OIL
60. 147. R
58. 139.6
58. 140.0
62. 141.?
58. 140.4
60. 1 40 . 4
58. 140.R
60 . 1 40 .8
62. 1 40. 4
62. 14?. 4
60. 138.7
60. 141 .?
60. 1 44. 1
60. 140.R
60. 135.8
58. 14P.4
58 . 1 39 . 6
58 . 1 39 . 6
58 . 140.4
55. 141.6
55. 137. 1
58. 141 .?
58 • 1 40 . 4
60 • 140.4
60.
60.
65.
62.
62.
60.
60.
62.
62.
62.
60.
60.
60.
62.
62.
6P.
35 .R
40. 4
40 . 0
4PI.R
40. 4
40.0
40.8
40. 4
41 .?
44.9
36.3
40.8
40.4
40 .8
40. 4
40. 4
STONE
1 1 .8
14.5
1 7.P
6.4
3.6
5.4
PP.7
3P.2
33.6
P3.6
9. 1
30. 4
1 4. 5
P5.4
18. 1
18.6
25.9
1 1 .8
29. 5
PI .3
19. 5
24.0
1 5.0
P4.0
PP. 7
P5.4
P5. 4
1 5.9
17.2
P0.9
IP. 2
P0.0
31 .8
44.9
36.3
1 r< . 6
43. 1
33. 1
39. 5
39.9
- 377 -
-------
RUN 9:
APPENDIX G* TABLE I.
TEMPERATURES AND FF D RATES PAGE
3 OE 16
AY. HOUR
6.0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6.1130
6. 230
6. 330
6. 430
6. 530
6. 630
6. 730
6. 830
6. 930
6.2030
TEMPERATURE*
GASIFIER REGEN
885.
R90.
880.
900.
890.
905.
905.
890.
883.
910.
908.
875.
900.
900.
040.
040.
040.
040.
040 .
040 .
040 .
078.
01 5.
040 .
030.
040 .
040.
070.
880. 900.
880. 920.
880. 1000.
DEG. C. FEED RATE
RECYCLE OIL
60.
62.
62.
60.
60.
60.
60.
60.
60.
60.
60.
60.
60.
60.
60.
58.
52.
40. 4
40.4
42.8
37.9
40.4
39. 1
39. 1
42.4
40.8
47.4
40.4
40.4
37.9
47.0
41 .2
36.7
36. 7
KG/HR
STONE
41.3
45. R
49.0
44.9
54. 4
42.2
45. R
38. 1
62. 1
46.3
51 .3
30.8
22.2
33. 1
22.2
0.
0.
SHUT DOWN AT 6-2030 FOR
4 HOURS
7.0130
7.0230
7.0330
7.0430
7.0530
7.0630
7.0730
7.0830
7.0930
7. 1030
7. 1 130
7. 1230
7. 1 330
7. 1 430
7. 1 530
7. 1630
7. 1 730
7. 1830
7. 1930
850.
920.
935.
935.
914.
912.
900.
896.
905.
905.
908.
9 10.
902.
890.
915.
865.
860.
870.
860.
1050.
1055.
1060.
1045.
1043.
1042.
1042.
1042.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
40.
38.
38.
38.
38.
35.
35.
35.
35.
35.
35.
35.
35.
35.
35.
35.
35.
32.
32.
168.4
167. 5
165.9
166.3
166.3
166.3
166.3
166.3
172. 1
161.8
164.7
168.8
164.3
167. 1
165. 5
168.0
157.3
155.2
151 .9
0.
0.9
1 1 .8
2.7
9. 1
2.7
2.7
7. 7
1 5.0
6.8
5.4
5.9
12.7
17.2
74. 4
57.2
53. 1
46.3
30. R
- 378 -
-------
APPENDIX G: TABLE I.
RUN 9: TEMPERATURES AND FEF-D RATES PAGE
4 OF 16
DAY. HOUR
7.2030
7.21 3fl
7.2230
7.2330
8.0030
8 .0130
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8 .0930
8. 1030
8. 130
8. 230
8. 330
8 . 430
8. 530
8. 630
8. 730
8. 830
8. 930
8.2030
8.2130
TEMPERATURE* DEC. C.
GASIFIER
880.
900.
9 10.
9 10.
910.
9 12.
910.
905.
910.
905.
905.
907.
903.
903.
903.
888.
895.
890.
888.
888.
893.
905.
890.
895.
900.
896.
REGEN.
1042.
1043.
1043.
1042.
1042.
1042.
1043.
1043.
1042.
1042.
1042.
1040.
1040.
1040.
1040.
1038.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
RECYCLE
32.
32.
32.
35.
0.
0.
0.
0.
0.
0.
0.
0.
30.
30.
30.
30.
30.
30.
30.
30.
30.
30.
30.
30.
30.
0.
FEED RATE KG/HR
OIL
149.8
156.4
1 52.3
147.8
151 .9
150. 7
156.0
1 58. 1
1 58. 1
158. 1
1 58. 1
161.4
1 56.4
161.4
162.6
1 55.2
1 50.7
169.2
161.0
1 59.7
1 58.9
1 59.3
162.2
157.7
160. 5
160. 1
STONE
68. 5
19.5
19.1
19.5
20.9
17.7
16.8
20. 0
13.6
1 4. 5
17.7
17.7
20. 4
14.1
1 6.8
28 . 1
26.3
24. 5
27.2
18.6
22. 7
1 7. 7
23. 6
23.1
18.1
21 .3
SHUT DOWN AT 8.2130 FOR 8 HOURS
9.0630
9 .0730
9 .0830
9.0930
9. 1030
9. 1 130
9. 1230
9. 1330
9 . 1 430
9. 1 530
890.
900.
920.
910.
910.
910.
9 12.
9 10.
910.
908.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1040.
1045.
1055.
0.
0.
0.
30.
30.
30.
30.
0.
30.
30.
160. 1
160. 1
160.5
1 59.7
1 59.7
1 59. 7
1 59. 7
161.4
1 59.3
160. 5
10.4
10.9
7.3
14.1
•21 .8
13.6
1 3. 6
19. 1
22.2
30.4
- 379 -
-------
RUN 9:
APPENDIX G . TABLE I.
TEMPERATURES AND FEr-D RATES PAGE
5 OF 16
A
9
9
9
9
9
Y.HOIJR
. 1630
. 1730
. 1830
.1930
. 2030
TEMPERATURE* DEG. GI-
GA SI
91
9 1
9 1
90
91
FIER
5.
5.
0.
5.
0.
REGEN.
1
1
1
1
1
055.
055.
048.
050.
049.
RECYCLE
30.
30.
30.
30.
30.
FEED RATE KG/H
1
1
1
1
1
OIL
61.
56.
55.
55.
71.
R
STONE
0
8
2
2
2
23.
15.
21 .
23.
20.
6
4
8
6
9
9. 1630
9. 1730
9. 1830
9. 1930
9.2030
SHUT
10.0230
10.0330
10.0430
10.053PI
10.0630
10.0730
10.0830
10.0930
10. 1030
10. 1 130
10. 1230
10.1330
10. 1430
10. 1530
10. 1630
10. 1 730
10. 1830
10. 1930
10.2030
10.2130
10.2230
10.2330
1 .0030
1 .0130
1 .0230
1 .0330
1 .0430
1 .0530
1 .0630
1 .0730
1 .0830
915.
9 15.
9 10.
905.
910.
DOWN AT
860.
911.
911.
901 .
903.
906.
904.
9 10.
903.
905.
905.
903.
903-
903.
900.
900.
900.
910.
902.
903.
905.
900.
892.
903.
904.
906.
907.
902.
907.
902.
911.
9.2030 FOR 5 HOURS
920.
1045.
1043.
1044.
1044.
1054.
1050.
1075.
1080.
1070.
1060.
1065.
1061 .
1055.
1050.
1055.
1055.
1055.
1055.
1055.
1056.
1070.
1075.
1080.
1066.
1050.
1048.
1049.
1050.
1070.
1068.
30.
30.
30.
30-
0.
0.
20.
30.
30.
30.
30.
30.
30.
30.
30.
30-
30.
30.
30.
30-
30.
30.
30.
30.
30.
30.
30.
30.
30.
30.
36.
1 58.
158.
158.
158.
159.
159.
158.
160.
1 56.
158.
158.
160.
157.
161.
156.
156«
163.
1 57.
158.
163-
1 58.
1 58.
158.
157.
158.
158.
158.
157.
158.
157.
157,
9
9
9
9
3
3
9
5
0
9
1
1
3
4
8
4
4
3
.5
.4
. 1
. 1
. 1
,7
.5
.9
. 5
,3
.5
, 7
, 7
6.4
6.8
8.6
19.
27.
1 1 •
24.
17.
17.
1
.7
.8
.9
.2
, 7
18. 1
17.7
J 5.4
17.7
1 4. 5
15.4
19. 1
16. 3
1 1 .3
10.0
19. 1
14. 1
15.0
24.9
16.8
14. 5
13.6
15.9
14. 1
IB. 4
27.7
14. 5
- 380 -
-------
RUN 9:
APPENDIX G: TABLE I.
TEMPERATURES AND FE> 0 RATES PAGE
6 OF 16
DAY. HOUR
1 .0930
1 .1030
1 . 1 1 30
1 .1330
1 . 1330
1 .1430
1 • 1 530
1 . 1630
1 . 1 730
1 .1830
1 .1930
1 .2030
1 .2130
1 .2230
1 .2330
12.0030
12.0130
12.0230
1 2.0330
12.0430
12.0530
12.0630
12.0730
1 2.0830
12.0930
12. 030
12. 130
12. 230
12. 330
12. 430
12. 530
12. 630
12. 730
12. 830
12. 930
12.2030
12.2130
12.2230
12.2330
1 3.0030
TEMPERATURE* DEC. C.
GASIFIER
908.
900.
915.
9 12.
912.
908.
903.
902.
899.
902.
905.
9 10.
9 18.
9 19.
926.
909.
900.
905.
899.
902.
9 0.
9 4.
9 5.
9 9.
9 5.
920.
920.
925.
923.
9 18.
916.
9 15.
9 18.
920.
920.
925.
925.
915.
915.
9 13.
REGEN.
1062.
1052.
1053.
1045.
1048.
1040.
1042.
1040.
1040.
1040.
1049.
1049 .
1041 .
1046.
1051 .
1072.
1054.
1051 .
1053.
1059.
1068.
1054.
1060.
1060.
1060.
1060.
1070.
1065.
1062.
1055.
1040.
1055.
1050.
1050.
1050.
1050.
1050.
1050.
1050.
1052.
RECYCLE
38.
38.
38.
38.
37.
38.
38.
38.
38.
38.
38.
38.
0.
32.
32.
31 .
30.
30.
30.
30.
30.
30.
30.
30.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
42.
42.
35.
23.
FEED RATE KG/HR
OIL
1 59. 3
158.5
1 58.5
1 58. 5
1 59 . 3
154. 4
158. 5
1 54. 4
1 54.0
1 58. 5
1 58 . 9
158.9
152.7
158.9
158. 5
152. 7
141.2
137.5
142.0
141.2
141.6
141.6
141.2
41 .6
41 . 6
41 . 6
40.8
43. 3
43. 3
45. 7
46.6
47. 4
47.0
47. 4
47.8
47.8
49.0
47.8
46.6
49.0
STONE
21.3
16.3
19. 1
18. 1
13.6
6.R
6.3
6.3
20. PI
6.3
7.7
7. 7
7.2
3.6
0.0
1 7.2
21 .8
14. 5
15.4
15.4
14. 1
12.7
10.4
9. 5
10.9
10.4
5.9
3. 6
7.3
7.3
7.3
7.3
5.4
4. 5
4. 1
1 .8
0.5
7.3
6.8
8.2
- 381 -
-------
RUN 9:
APPENDIX G: TABLE I.
TEMPERATURES AND FFKD RATES PAGE
7 OF
DAY.HOUR TEMPERATURE* DEG.
GASIFIER REGEN. F
3.0130
3.0230
3.0330
3.0430
3.0530
3.0630
3.0730
3.0830
3.0930
3. 1030
3. 1 130
SH UT
4. 0 1 30
4.0230
4.0330
4.0430
4.0530
4.0630
4.0730
4.083"!
4.0930
4. 1030
4.11 30
4. 1230
4. 330
4. 430
4. 530
4. 630
4. 730
4. 1830
4. 1930
4.2030
4.2130
4.2230
4.2330
5.0030
5.01 30
9 18.
9 18.
920.
91 7.
917.
920.
925.
920.
925.
925.
920.
DOWN AT
925.
908.
900.
905.
910.
898.
895.
9 10.
915.
920.
930.
940.
945.
940.
930.
925.
920.
920.
900.
880.
878.
875.
875.
870.
863.
1055.
1045.
1042.
1060.
1065.
1 083.
1085.
1075.
1080.
1080.
1080.
13.1130 FOR
1055.
1043.
1050.
1065.
1065.
1075.
1080.
1095.
1095.
1070.
1 100.
1070.
1070.
1060.
1075.
1080.
1078.
1078.
1078.
1080.
1075.
1080.
1078.
1080.
1078.
C. FEED RATE KG/HR
CYCLE OIL
23. 147.4
23.
23.
23.
23.
23.
23.
20.
0.
0.
0.
47.0
47.0
49. 4
48.6
47.8
43.3
47. 4
51 .9
47.4
44. 5
STONE
5.0
10.4
1.8
6.8
5.9
5.4
4.5
5.0
4. 5
3.6
6.8
13 HOURS
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
52.
58.
58.
58.
58.
60.
60.
147. 4
150.3
137.5
51.5
51 .9
44. 5
46.6
35.0
38.7
44. 5
44. 5
43.7
141.6
141.6
143.7
146. 1
49.4
47.8
44. 5
44. 1
46.6
46.6
40.0
41 .2
47.4
17.2
15.0
24.0
12.7
10.4
1 6.8
18. 1
15.9
9. 1
5.4
5.9
6.4
7.7
5.0
5.0
5.9
8.6
9. 1
9. 1
10.0
8.2
8.6
8.2
9.5
9.5
- 382 -
-------
RUN 9:
DAY. HOUR
1 1.0230
1 5.0330
1 5.0430
5.0530
5.0630
5.0730
5. 08 30
5.0930
5. 1030
5. 130
5. 230
5. 330
5. 430
5. 530
5. 630
SHUT
16.0730
1 6.0R30
16.0930
16. 030
16. 130
16. 230
16. 330
16. 430
16. 530
16. 630
16. 730
1 6. 830
16. 930
16.2030
16.2130
16.2230
16.P330
1 7.0030
17.0130
1 7.0330
1 7.0430
APPENDIX G
TEMPERATURES AND FEr
TEMPERATURE* DEC.
GASIFIER
863.
875.
878.
880.
885.
895.
880.
888.
895.
900.
988.
9 16.
9 16.
91 7.
9 14.
DOWN AT 1
911.
90R.
915.
901 .
903.
901 .
901 .
903.
907.
916.
906.
90R.
899.
899.
893.
903.
912.
906.
TABLE
D RATES
c.
REGEN. RECYCLE
1078.
1078.
1078.
1078.
1078.
1078.
1078.
1077.
1078.
1078.
1075.
1078.
1078.
1079.
1081 •
5.1630 FOR
1058.
1060.
1072.
1048.
1058.
1058.
1058.
1057.
1058.
MISSED DATA
1056.
1060.
1061 .
1061 .
1060.
1061 .
1060.
MISSED DATA
MISSED DATA
1060.
1060.
60.
60.
60.
60.
60.
60.
60.
56.
56.
56.
55.
45.
40«
35.
30.
14 HOURS
50.
55.
53.
53.
63.
63.
63.
63.
63.
READING
65.
63.
63.
63.
61.
62.
62.
READING
READING
61 .
61 .
I .
PAG
FEED
OIL
1 42.0
143.3
1 45-3
145.3
142.0
144. 1
141.2
148.2
139.6
144. 1
1 42.4
142.8
1 42. 4
1 42.4
142.4
142.4
1 40.0
145.3
1 42.0
142.4
142.0
142.4
142. 4
142. 4
138.3
143.3
126.8
126.8
127.6
125- 1
125.6
122.7
1 64.7
8 OF 16
RATE KG/HR
STONF
9. 1
5.9
5.0
4.5
4.5
3.6
7.3
8. 6
9. 1
6. 4
5.9
7.3
5-9
6. 4
6.R
20.0
17.2
19. 1
21 .8
13-6
6. 4
6.8
5.4
5.9
3.2
27. 7
7.3
5.4
5.4
4. 1
4. 5
6.8
6.4
- 383 -
-------
RUN 9:
APPENDIX G.: TABLE I .
TEMPERATURES AND FFf-D RATES PAGE
9 OF 16
DAY. HOUR
1 7
17
17
17
17
17
17
17
17
1 7
1 7
17
17
17
17
17
17
1 7
17
18
18
18
18
18
I *>
18
18
18
18
18
18
1 F*
18
18
18
18
18
18
18
1R
.0530
.0630
.0730
.0830
.0930
• 1030
. 1 130
. 1230
. 1330
. 1430
. 1 53P
. 1 630
. 1 730
. 1830
. 1930
.2030
.2130
.2230
.2330
.0030
.0130
.0230
.0330
.0430
.0530
.0630
.0730
.0830
.0930
. 1030
. 1 130
. 1 230
. 1330
. 1 430
. 1 530
. 1630
. 1 730
.1830
.1930
.2030
TEMPERATURE*
GASIFIER
902.
899.
895.
901 .
894.
908.
905.
908.
910.
899.
9 13.
9 10.
886.
905.
9 1 4.
9 14.
951.
943.
941 .
941 .
940.
941 .
93?.
935.
940.
945.
950.
960.
955.
955.
950.
950.
945.
953.
960.
960.
960.
960.
925.
920.
DEG. C. FEED RATE KG/HR
REGEN. RECYCLE
1
1
1
1
1
1
1
058
058
055
055
056
056
059
1059
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
056
055
056
056
056
055
065
068
072
070
070
070
070
065
069
069
069
070
070
075
080
075
075
075
070
070
080
090
100
097
61 • 1
63. 1
62. 1
62. 1
62. 1
62. 1
62. 1
62. 1
53. 1
53. 1
61 • 1
61 . 1
61 . 1
60. 1
59. 1
OIL STONE
62.6 6.4
65.5 6.4
66.7 5.4
63.8 5.0
60.1 6.4
69.2 7.3
59 . 3 7.7
64.7 7.3
64.3 5.4
64.7 5.9
64.7 5.0
64.7 4.1
65.5 50.3
89.8 9.1
92.2 13.2
57. 193.1 7.3
42. 1
40. 1
40. 1
93. 1 9.5
95. 1 9.1
95. 1 9.1
40. 195.1 9.5
40. 1
40. 1
40. 1
40. 1
86.5 7.3
93.9 7.3
88. 5 10.4
93.5 9. 1
40. 194.3 8.?
40. 1
40.
. 40.
40.
40.
. 40.
. 40.
40.
. 40.
44*
. 40.
42.
40.
085. 40.
080
40.
94.3 7.7
88. 1 8.2
93.5 7.7
79.9 5.9
89.0 6.4
80.3 8.2
70. 4 8.2
78 . 7 6.4
78.7 5.0
58.5 5.9
58.5 5.4
59 . 3 6.4
57.7 8.2
55.2 9.5
31.7 10.0
- 384 -
-------
RUN 9:
DAY.HOUR
8.2130
8.2230
8
9
9
9
19
19
19
19
19
19
19
19
>330
0030
0130
0230
0330
0430
0530
0630
0730
0830
0930
1030
19.1130
19.1230
19.1330
19.1430
19.1 53^"
19.1630
19.1730
19 . 1830
19
19
19
19
19.
20
2fl
20<
20.
20.
20.
20.
20.
20.
20,
20.
1930
• 2030
2130
2230
2330
0030
0130
0230
0330
0430
0530
0630
0730
0830
0930
1030
APPENDIX G : TABLE
I .
TEMPERATURES AND FF.' D RATES PAG
TEMPERATURE* DEG. C«
GASIF1ER
920.
920.
930.
920.
930.
940.
920.
920.
920.
928.
924.
918.
903.
928.
920.
91 5.
920.
910.
918.
910.
915.
920.
918.
923.
935.
930.
928.
925.
925.
924.
928.
924.
930.
930.
935.
933.
935.
REGEN. RECYCLE
1070. 40.
1070. 40.
1070. 40.
1070. 40.
1070. 40.
1080. 40.
1070. 40.
1070. 40.
1070. 40.
1070. 40.
1070. 40.
1070. 55.
1066. 55.
1065. 45.
1065. 40.
1065. 38.
1065. 30.
MISSED DATA READING
1070. 30.
1065. 0.
1068. 0.
1070. 0.
1055. 0.
1058. 0.
1070. 0.
1070. 0.
STONE CHANGE
1070. 0.
1075. 0.
1065. 0.
1065. 0.
1065. 0.
1065. 0.
1065. 0.
1065. 0.
1065. 0.
1080. 0.
STONE CHANGE
1080. 0.
1 0 78 • 0 •
FEED
OIL
156.0
146. 1
146. 1
147.0
124.3
147.4
146.6
144. 1
148.6
146.6
145.7
146. 1
149.4
142.8
144.9
140.R
144.9
146. 1
1 47.8
148.2
144.5
144. 1
146.6
148.6
147.4
1 47. 4
147.0
147.8
147.0
147.4
147.0
147.4
147.4
147.4
146.6
146.6
150.7
10 OF 16
RATE KG/HR
STONE
9. 1
5.9
5.9
8.6
10.0
9. 1
7.3
5.0
3-6
4. 1
5.4
6.8
14. 1
17.7
18. 1
25-9
1 5.9
26-
19.
26.
15.
18.
26.
13-
16-
3
1
8
9
1
8
2
3
21 .8
21 .3
18.6
1 5.0
14. 1
10.9
5.9
10.9
10.4
10.9
9
8
1
6
- 385 -
-------
RUN 9:
APPENDIX G: TABLE I.
TEMPERATURES AND FE'.D RATES PAGE II OF 16
DAY. HOUR
20.
20.
20.
20.
20.
20.
20.
?0.
130
230
330
430
530
630
730
830
20. 1930
20.2030
TEMPERATURE*
GASIFIER
948.
952.
948.
925.
936.
940.
935.
930.
950.
958.
REGEN
1085.
10R5.
1080.
1080.
1080.
1078.
1078.
1075.
1075.
1082.
DEG. C.
FEED RATE
. RECYCLE OIL
0
0
38
0
0
0
0
0
0
0
*
•
•
*
*
•
45.7
45.7
45.7
48.6
46.6
46.6
146.6
1 46. 6
147.0
. 147.0
KG/HR
STONE
7.7
7.3
7.3
18. 1
17.7
14. 5
14. 1
18. 1
11.3
0.
SHUT DOWN AT 20.2030 FOR 35 HOURS
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1330
22. 1430
22. 1530
22. 1 630
22. 1730
22. 1830
22. 1930
22.2030
22.2130
22.2230
22.2330
23.0030
23.0130
23.0230
23.0330
23.0430
23.0530
23.0630
23.0730
23.0830
23.0930
919.
938.
921.
940.
922.
922.
925.
930.
924.
932.
932.
953.
949.
959.
964.
970.
974.
990.
993.
994.
997.
973.
972.
965.
970.
1039. 62.
MISSED DATA READI
1060. 53.
1060. 50.
1060. 42.
1062. 38.
1062. 34.
1069. 30.
1070. 30.
1075. 30.
1068.
1061 •
1050.
1061 •
1080.
1089.
1093.
1 1 12.
1 103.
1 106.
1 106.
1 108.
1 1 10.
1096.
1084.
1 105.
30.
30.
30.
30.
30.
33.
33.
32.
32.
37.
39.
39-
44.
44.
43.
0.
1 16. 5 51.3
NG
141.6 42.2
138.3 22.2
1 53. 1 27.7
142.0 38.6
142.8 29.5
154.0 20.4
136.7 20.0
131.3 20.0
1 49 . 8 21.8
133.8
133.8
1 12.8
1 15.3
113.6
111.6
109.9
108.7
106.6
107.0
107.0
107.0
107.0
8.6
5.9
4.5
7. 7
5.9
8. 6
7.2
3.6
5.9
6.8
3.6
9. 1
4. 1
107.0 26.3
110.3 29 . 5
- 386 -
-------
APPENDIX G.: TABLE I .
RUN 9: TEMPERATURES AND FR.KI) RATES PAGE IP OE 16
DAY. HOUR
23- 1030
P3. 1 130
?3. 1230
23. 1330
P3. 1 430
P3« 1 530
P3. 1630
?3- 1 730
P3. 183M
23. 1930
? 3. 20 30
P3.2130
P3.PP30
P3.2330
24.0030
P4.0130
P4.0230
24.0330
24.0430
P4.0530
P4.0630
P4.F5730
P4.0830
P4.0930
24. 1030
P 4. 1 1 30
P4. 1230
P4. 1330
P4-, 1 430
P4. 1 530
24. 1630
P4. 1 730
P4. 1830
P4. 1930
P4.2030
P4.21 30
P4.2P30
P4.2330
25.0030
P 5. 01 30
TEMPERATURE, DEG. C.
GA:>IFIER REGEN. RECYCLE
950.
940.
935.
940.
940.
920.
925.
930.
945.
950.
910.
928.
933.
931 .
947.
968.
970.
971 .
968.
963.
969.
969.
960.
955.
959.
955.
950.
945.
958.
945.
944.
942.
949.
945.
940.
940.
940.
943.
940.
940.
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
11
It
If
If
If
If
1 1
1 1
IP
IP
IP
1115.
125.
125.
140.
122.
130.
1 1 5.
120.
125.
30.
18.
22.
15.
15.
16.
27.
50.
149.
162.
162.
1 72.
182.
185.
045.
048.
050.
050.
175.
7)75.
975.
378.
570.
575.
580.
595.
08.
18.
180.
90.
85.
0.
0.
0.
0.
0.
0.
30.
30.
30.
30.
30.
30.
30.
30.
32-
32.
32.
32.
47.
49.
52.
52.
53.
50.
44.
40.
35.
33.
33.
33.
33.
30.
30.
34.
30.
30.
30.
30.
0.
0.
FEED RATE KG/HR
OIL STONE
1 19.8
130. 5
1 34.6
1 47.8
138.3
50. 7
50.3
49.4
49.4
49.4
49.4
44. 1
48.2
47.8
41 .6
38. 7
1 38 . 7
138.3
128.8
19.4
1 4.0
1 4.0
14. F?
13.6
20.2
23- 5
23.9
123. 5
123.5
123-5
123.5
123. 5
123. 5
1P3-5
123. 5
122.7
124. 7
123- 1
IP?. 3
1P3.9
23.6
19. 1
?0. 4
15.9
I -J • x
15.9
7.2
5.9
5.4
5.0
5.0
6.3
1 5.0
12.2
13.6
14. 1
10.0
7.3
8.6
6.8
6. 4
6. 4
5.0
6.4
16.3
25.4
P6.3
24. 5
PP.P
PI .8
21 .8
19.5
18.6
2.7
4. 1
7.2
5.4
4.5
18. 1
20. 4
16.3
387 -
-------
RUN 9:
APPENDIX G :: TABLE I .
TEMPERATURES AND FEED RATES PAGE 13 OF
25.0230
25.0330
25.0430
25.0530
25.0630
25.0730
25.0830
SHUT
25. 1 430
25. 1 530
SHUT
25.2230
25.2330
26.0030
26.0130
26.0230
26.0330
26.0430
26.0530
26.0630
26.0730
26.0830
SH UT
26.2230
26.2330
27.0030
27.0130
27.0230
27.0330
27.0430
27.0530
932.
933.
945.
950.
950.
960.
970.
DOWN AT
954.
960.
DOWN AT
960.
965.
965.
925.
940.
940.
943.
955.
945.
945.
942.
DOWN AT
870.
879.
885.
900.
900.
905.
908.
915.
1080.
1098.
1 105.
1110.
1 103.
1 100.
1095.
25.0830 FOR
11 10.
1 138.
25.1530 FOR
065.
108.
130.
135.
135«
143.
145.
1 10.
1095.
1085.
1087.
26.0830 FOR
970.
1000.
1030.
1025.
1035.
1030.
1035.
1040.
c.
CYCLE
0.
0.
0.
0.
60.
0.
0.
6 HOURS
0.
0.
7 HOURS
0.
0.
0.
0.
42.
42.
42.
0.
0.
0.
0.
14 HOURS
0.
0.
0.
0.
0.
0.
0.
0.
FEED I
OIL
123. 9
122.7
127.6
119.4
126. R
1 2. 1 . 0
121 .9
1 14.4
1 14.4
131.7
132. 1
125. 1
138.3
127.6
133.8
134.6
126.8
135. R
127.6
130.9
129.3
132. 1
132. 1
132. 1
132.6
131.3
130.9
128.8
2.
10.
4.5
10. 4
9. 5
12.7
1 1 .8
12.2
10.4
8.2
13.2
13.2
4. 1
51
50*
47
23
34
22
20
24
7
• 3
7
0
0
- 388 -
-------
RUN 9:
APPENDIX G :
TEMPERATURES AND FEED
14 OF 16
DAY. HOUR
27.0630
27.0730
27.0830
27.0930
27. 1030
?7. 1 130
27. 1230
27. 1330
27. 430
27. 530
27. 630
27. 730
27. R30
?7. 930
27.2030
27.2130
27.2230
27.2330
28.0030
28.0130
2R.0230
28.0330
28.0430
28.0530
28.0630
28.0730
28.0830
28.0930
28. 030
28. 130
28. 230
28. 330
28. 430
28. 530
28. 630
28. 730
28. 830
28. 1930
28.2030
28.2130
TEMPERATURE* DEG. C.
GASIFIER
928.
940.
953.
945.
941 .
955.
952.
956.
956.
950.
954.
950.
956.
950.
940.
940.
950.
950.
953.
945.
938.
940.
930.
935.
940.
938.
940.
936.
938.
929.
932.
946.
920.
920.
934.
928.
928.
945.
944.
950.
RE GEN.
1038.
1035.
1055.
1040.
1042.
1044.
1050.
1050.
1042.
1045.
1042.
1044.
1044.
1047.
1050.
1050.
1050.
1040.
1045.
1045.
1040.
1040.
1040.
1045.
1040.
1040.
1041 .
1039.
1042.
1040.
1038.
1040.
1042.
1045.
1056.
1055-
1054.
1050.
1055.
1050.
RECYCLE
0.
0.
32.
32.
32.
31.
31.
31 .
31 •
31 .
31 .
31 •
31 •
31 .
31 .
31 .
31.
31 .
31.
31 .
31 .
31 .
31.
31 .
31.
31 .
37.
36.
35.
34.
34.
35.
34.
34.
34.
33.
33.
33.
33.
33.
FEED RATE KG/HR
OIL
127.6
140.0
130.9
121.9
136.7
130. 5
130. 5
130.9
130. 5
130. 1
130. 5
130. 1
130. 5
130. 5
130. 1
137.9
130. 1
125.6
13L3
1 29 . 3
129.7
130. 1
1 33.4
127.6
135.8
127.6
123.9
132. 1
130. 1
130. 1
130. 1
134.6
134.6
148.2
1 47. 4
147.8
148.2
148.2
148.2
149.8
STONE
18.6
8.2
7.3
7.7
9. 1
10.4
12.2
7.3
6.8
19-5
11.3
9.5
7.3
6.8
11.3
14. 1
10.9
9. 1
0.4
2.7
7.7
4.5
5.9
8. 1
1 .8
3.2
7.7
5-0
2.7
3.2
2.7
3-6
1 .3
18. 1
12.2
11.3
7.3
0.
0.
0.
- 389 -
-------
RUN 9:
DAY.HOUK
2R.2P30
SH LIT
29.2330
3(71.0030
30.0130
30.0230
30.0330
30.0430
30.0530
30.0630
30.0730
30.0830
30.0930
30. 1030
30. 1 130
30. 1230
30. 1 330
30.1430
30. 1 530
30. 1 630
30. 1 730
30. IB 30
30. 1930
30.2030
30.2130
30.223(7)
30.2330
31 .0030
31 .0130
31 .0230
31 .0330
31 .043^
31 .0530
31 .0630
31 .0730
31 .0830
31 .0930
APPENDIX
TEMPERATURES AND (•
TEMPERATURE, DEG
GASIFIER
945.
DOWN AT 28
951.
955.
971.
REGEN.
1050.
.2230 FOR
990.
1020.
1045.
Gs TABLE
tiED RATES
. c.
RECYCLE
33.
24 HOURS
37.
37.
40.
I .
PAGf
FEED 1
OIL
145.7
161.8
162.2
161.4
MISSED DATA READING
MISSED DATA READING
945.
948.
918.
905.
908.
928.
935.
938.
942.
945.
948.
953.
958.
963.
975.
968.
975.
970.
1000.
955.
935.
905.
920.
930.
9 10.
925.
911.
920.
928.
920.
1045.
1055.
1040.
1030.
1025.
1015.
1035.
1035.
1035.
1035.
1035.
1035.
1038.
1038.
1045.
1045.
1045.
1050.
1060.
1055.
1055.
1060.
1055.
1055.
1055.
1060.
1065.
1065.
1065.
1062.
60.
60*
50.
47.
40.
40.
38.
35.
40.
35.
35.
35.
0.
0.
0.
0.
0.
0.
40.
42.
40.
40.
40.
38.
38.
38.
38.
38.
30.
30.
172.5
166.7
149.0
145.3
135.8
134.6
130.5
137.1
131.3
133.4
131.3
132.6
135.8
131.7
134.2
129.7
131.3
131.7
147.8
148.6
163.4
163.4
163.4
167.5
170.0
150.3
141 .6
141.6
139.6
142.0
15 OF 16
RATE
KG/HR
STONE
4.5
0.
19,
16.
8.6
18.6
23. 1
34.0
24.5
21.8
9. 1
9.1
11.3
1 1 .8
9.5
7.3
7.3
7.7
5.9
6-8
5.9
1.8
0.9
1.8
3.6
20.0
13.6
10.9
5.9
4.5
15.9
IB. 1
10.4
9.5
- 390 -
-------
APPENDIX G* TABLE
RUN 9: TEMPERATURES AND FEED RATES
PAGE 16 OF 16
DAY.HOUR TEMPERATURE* DEC. C.
GASIFIER REGEN. RECYCLE
FEED RATE KG/HR
OIL STONE
31 . 1030
31 . 1 130
31 . 1230
31 . 1330
31. 430
31. 530
31. 630
31. 730
31. 830
31. 9 30
31 .2030
31 .2130
31 .2230
31 .2330
32.0030
32.0130
32.0230
32.0330
32.0430
32.0530
32.0630
32.0730
32.0830
915.
940.
960.
953.
935.
973.
945.
980.
975.
965.
945.
945.
925.
910.
940.
935.
925.
925.
940.
935.
925.
940.
945.
1065.
1065.
1062.
1050.
1063.
1063.
1065.
1065.
1065.
1055.
STONE
1055.
1055.
1055.
1055.
1055.
1060.
1065.
1068.
1065.
1065.
1065.
1065.
1065.
30.
30.
30.
30.
30.
30.
42.
50.
50.
0.
CHANGE
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
129.7
1 34.2
136.3
140.0
132. 1
141.2
144.9
146. 1
152.7
149.8
135.4
147.4
147.8
148.6
149.4
144. 5
45.7
46.6
46. 1
46. 1
46. 1
36.3
29.7
12.2
3 2. 2
2. 3
0.
0.
1 • 4
63.0
43. 5
32.2
38. 1
48. 5
32.2
18.1
19.5
9.5
5.0
11.8
27. 7
5.0
20 • 4
10.0
10.0
5.4
- 391 -
-------
APPENDIX G .• TABLF II.
RUN 9» GA5 FLOW RATES PAGE
OF
DAY.HOUR
GAS
GASIFIEH
AIR FLUE GAS
RATES M3/HR RFGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
1 . 1 930
1 .2030
1 .2130
SHUT
2.0230
2.0330
2.0430
2.0530
2.0630
2.0730
2.4)830
2.0930
2 . 1 0 30
2 . 11 30
2. 1230
2.1330
?. M30
? . 1 530
2. 1630
2. 1730
?. 1830
P. 1930
P. 2 030
2.2130
2.2230
2.2330
SHUT
4.0430
4.0530
4.0630
A. 07 30
4.0830
4.0930
4. 1030
310.
301 .
301.
DOWN AT
357.
377.
347.
345.
340.
342.
342.
32 1 .
338.
338.
357.
355.
318.
353.
353.
379.
387.
387.
387.
404.
387.
387.
DOWN AT
308.
325.
325.
394.
377.
394.
36.
22.
19.
1 . 2 1 30
25.
34.
66.
62.
67.
66.
65.
47.
50.
50.
24.
20.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
2.2330
86.
86.
66.
54.
51 .
44.
3.0
3.0
3.0
FOR 4
2.9
2.7
2.9
2.9
3.3
3.2
3.2
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
2.9
2.9
3.0
3.0
3.0
FOR 28
4.6
4.6
4.6
4.6
4.6
4.6
26.5
24. 1
24. 1
HOURS
27.4
27.4
21. 1
29.9
23.0
24.2
25.4
24.0
24.5
24.4
24.7
27.2
31 .4
28.3
28.8
31.5
33.5
34.7
38.9
37.2
38.4
37.7
HOURS
28.9
27.8
30.9
29.9
30.0
28.4
2.5
2.5
3.8
3.6
3.6
3.6
3.3
2.3
3. 1
3. 1
2.3
2.1
2.0
2. 1
2.0
2.4
2.2
2.7
2.4
2.0
2.7
2.6
2.9
2.2
2.6
2.5
2.3
.6
,9
2.2
1 .5
2,
2,
1.32
1.19
1.21
1.37
38
08
44
09
16
1.23
1 . 18
.22
.21
.23
.34
.55
.38
.42
.52
.64
.69
.88
.82
.84
.82
1.33
1.33
1.54
1.50
1.47
1.37
MISSFP DATA READING
- 392 -
-------
APPENDIX G: TABLE II.
RUN 91 GAS FLOW RATES
PAGE 2 OF 16
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
4. 1230
4.1330
4. 1430
4. 1530
4. 1630
4.1730
4. 1830
4. 1930
4.?t}30
4.2130
4.2230
4.2330
"5.0030
5.0130
5.0230
5.0330
5.0430
5.0530
5.0630
5.0730
5.0830
5.0930
5. 1030
5 . 11 30
5. 1230
5. 1330
5. 1430
5. 1530
5. 1630
5 . 1 730
5 . 1 H30
5. 1930
5.2030
5 . ? 1 30
5.2230
5.2330
6.0030
6.0130
6.0230
6.0330
412.
395.
395.
394.
394.
395.
412.
394.
394.
412.
429.
429.
446.
446.
446.
446.
446.
446.
429.
429.
429.
429.
429.
429.
429.
446.
446.
429.
429.
430.
430.
430.
430.
429.
445.
446.
448.
448.
447.
446.
64.
126.
126.
126.
165.
165.
126.
126.
1 17.
107.
106.
106.
97.
97.
97.
87.
87.
87.
77.
77.
77.
77.
97.
97.
97.
97.
136.
136.
136.
136.
136.
136.
136.
1 17.
1 16.
1 16.
117.
117.
1 17.
1 17.
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.0
4.0
4.0
4.0
4.0
4.0
4.0
26.7
29.5
32.8
32.9
29.3
26.8
28.5
28.6
24.6
24.9
27.2
22.5
25.0
25.5
25.0
25.4
25.9
28.7
23.0
25.8
24. 1
24.2
23.9
24.3
27.5
28.7
29.9
29.2
28.9
27.6
27.7
27.6
26.4
24.5
27.7
29. 1
29.8
29.6
29.4
29.7
4.2
3.2
3.2
3.1
2.8
2. 1
2.2
2.5
2.0
2.2
2.2
2.2
2.4
3.3
3.3
3.3
2.4
2. 1
2. 1
2.2
2. 1
2. 1
2. 1
2.3
2.4
7.3
6. 1
6.9
6.2
3. 1
3.3
3.0
2.4
3.1
3. 1
3.2
3.2
3.2
3.3
3.2
1 .39
1.49
.65
.65
.47
.33
.42
.43
.23
.25
.35
. 15
.26
.34
.32
.35
.29
.41
. 15
.28
.20
.20
. 18
.21
.38
.64
.64
.64
.60
.39
.40
.38
.30
.25
.39
.46
.49
.49
.48
.49
- 393 -
-------
DAY.HOUR
RU
GAS
GASIFIER
AIR FLUF GAS
APPENDIX G: TABLE II.
UN 9: 0," j FLOW RATES PAGF 3 OF 16
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
6.0430
6./J530
6. 0630
6.0730
6.WH3W
6 . 0 930
6. 1030
6 . 11 30
6. 1230
6. 1330
6. 1430
6. 1530
6. 1630
6. 1730
6 . 1 830
6 . 1 930
6.2030
447.
447.
446.
447.
446.
464.
464.
446.
446.
446.
464.
412.
412.
412.
412.
377.
377.
107.
107.
107.
107.
107.
107.
107.
107.
107.
107.
107.
127.
1 17.
1 17.
1 17.
85.
1 18.
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
29.7
30.8
31.7
30.7
31.3
31.0
31.5
33.8
33.6
34.9
37.8
32.0
33.3
38.9
23.9
22.0
24.8
3.2
3.3
3.4
3.3
3.3
3.4
3.5
4.9
5.0
4.3
5.1
3.6
2.6
1.5
2.0
2.0 6
7.5
.49
1 .54
.58
.54
1.56
.55
1.58
.79
.71
.77
.91
.61
.62
.87
.04
5.99
1.42
SHUT DOWN AT 6.2030 FOR 4 HOURS
7.0130
7.0230
7.0330
.0430
.0530
.0630
.0730
.0830
.0930
. I 130
. 1230
7.1330
7,
7.
7,
7,
7,
1430
1530
1630
1730
1 830
7.1930
378.
464.
464.
481 .
463.
445.
428.
445.
445.
41 1.
428.
428.
428.
428.
428.
454.
428.
445.
445.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
25.5
34.4
35.0
37.7
36.2
35.8
36. 1
35.3
34.3
31. 1
31.2
32.2
31.6
31.7
30.8
29.2
25.7
24.5
22.4
3.3
3. 1
3.8
4.4
3.3
3.0
2.9
2.8
2.9
2.6
2.8
2.9
2.1
1.8
2.3
2.0
1 .9
2.2
2.2
1.32
1.72
1 .78
1 .91
1.79
1 .76
1.77
1.73
1 .68
1.52
1.53
1 .58
1.52
1.51
1.49
1.40
1.24
1.20
1.11
-'394 -
-------
DAY.HOUR
APPENDIX G t TABLF II.
RUN 9J GAS FLOW RATFS
GAS
GAS'IFIFR
AIR FLUE GAS
PAGE 4 OF 16
RATFS M3/HR REGEN.
PILOT RHGENFRATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
7.2030
7.21 30
7.2230
7.2330
8.0030
b . 0 1 30
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8. 0V 30
8. 1030
8.1130
8.1230
8. 1 330
8. 1430
8. 1530
8 . 1 630
8. 1730
8. 1830
8. 1930
8.2030
8.2130
SHUT
9.0630
9.0730
9.0830
9.0930
9. 1030
9 . 1 1 30
9. 1230
9. 1 330
9. 1430
9. 1530
447.
464.
464.
447.
447.
447.
447.
447.
447.
447.
447.
464.
464.
464.
464.
464.
464.
464.
464.
430.
430.
464.
447.
464.
, 464.
447.
DOWN AT
443.
426.
460.
460.
460.
460.
460.
460.
460.
460.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
8.2130
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.0
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
FOR 8
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
21.4
42.7
42. 1
39.7
40.3
37. 1
37. 1
37.0
37.5
36.4
36.9
46.7
40.0
41.3
39. 1
39.9
40.4
40.4
40.6
40.6
40.2
39.6
41.0
39.6
40.9
40.7
HOURS
42.4
43.8
34. 1
34. 1
38.3
37.2
33.6
35.2
36.3
36.3
2.4
3.4
3.3
3.4
3.6
3.1
3.2
3.2
3. 1
3.1
3.1
4.8
3.2
3.6
3.2
3.3
3.0
3.6
3.1
3.2
3.2
3.5
3. 1
2.9
3.4
3. 1
3.3
3.5
3.2
3.2
2.8
3.2
3.0
2.9
3.3
3.1
1 .08
2.08
2.05
1 .94
1.97
1.81
1.82
1.81
1 .83
1 .78
1 .80
2.31
1 .94
2.02
1 .90
1 .93
1.95
1.97
1 .96
1 .97
1.95
1 .94
1 .98
1.91
1 .98
1 .96
2.08
2.15
.69
.69
.86
.83
.66
.73
1 .80
1 .80
- 395 -
-------
APPENDIX Gi TABLE II.
RUN 9: GAS1 FLOW RATES PAGE 5 OF 16
DAY
. HOUR
GAS IF
GAS
IER
AIR FLUE GAS
9.
o.
9.
9.
9.
1 630
1730
1830
1930
2030
460.
460.
460.
461 .
461.
0.
0.
0.
0.
0.
RAT
PILOT
PROPANE
4.
4.
4.
4.
4.
6
6
6
6
6
E S M3/HR
REGENERATOR
AIR N
37.
36.
34.
34.
37.
0
8
0
6
4
ITROGEN
4
2
3
2
3
.0
.9
.2
.5
.4
REGEN.
VELOCITY
M/SEC
1.87
1 .82
1 .69
1.69
1 .86
9 . 1 630
0. 1730
9. 1830
9. 1930
9.2030
SHUT
10.0230
10.0330
10.0430
10.0530
10.0630
10.0730
10.0830
10.0930
10. 1030
10. 11 30
10. 1230
10. 1330
10. 1430
10. 1530
10. 1630
10. 1730
10. 1830
10. 1930
10.2030
10.2130
10.2230
10.2330
1 .0030
1 .0130
1 .0230
1 .0330
1 .0430
1 .0530
1 .0630
1 .0730
1 .0830
460.
460.
460.
461 .
461.
DOWN AT
440.
428.
446.
463.
445.
445.
445.
462.
462.
446.
445.
445.
445.
445.
445.
444.
444.
443.
427.
428.
428.
446.
446.
429.
446.
446.
633.
428.
428.
428.
446.
0.
0.
0.
0.
0.
9.2030
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.6
4.6
4.6
4.6
4.6
FOR 5
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
37.0
36.8
34.0
34.6
37.4
HOURS
40.4
37.7
37.5
37.1
36.3
36.9
34.7
27.1
23.1
39.0
36.6
39. 1
36.4
35.2
37.7
37.7
40.3
39.9
39.1
39.5
39.0
42. 1
43.0
42.4
35.4
34.4
34.5
34. 1
35.8
37.4
37.5
3.5
3.7
4.0
4. 1
3.7
6.2
6.7
7.2
6.7
6.8
6.8
7.0
7.9
5.6
7.2
6.7
7.3
6.9
6.9
6.9
7.0
7.3
6.8
6.0
4.7
5.6
5.7
6.4
7.6
7.6
6.8
.82
.89
.89
.87
.82
.98
.89
1 .59
.39
2
09
13
04
86
2. 1
1
2
2
1
2.04
03
18
14
1 1
12
61
2.29
2.31
2.26
1 .85
1.82
1 .83
1 .85
1.98
2.08
2.05
- 396 -
-------
APPENDIX G? TABLE II.
RUN 9s GAS FLOW RATES
PAGE 6 OF 16
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SFC
.(0930
. 1030
. 1 130
.1230
.1330
. 1 430
. 1530
. 1630
. 1730
. 1830
. 1930
.2030
.2130
.2230
1 .2330
2.0030
2.0130
2.0230
2.0330
2.0430
2.0530
12.0630
12.0730
12.0830
12.0 930
12. 1030
12. 1 130
12. 1?30
12. 1330
12. 1430
2. 1530
12. 1630
2. 1730
12. 1830
12. 1930
12.2030
1 2 . 2 1 30
12.2230
12.2330
3.0030
445.
445.
441.
442.
442.
443.
443.
407.
407.
407.
407.
441 .
441 .
458.
463.
394.
394.
394.
377.
377.
394.
394.
394.
412.
412.
412.
412.
412.
426.
407.
407.
407.
407.
407.
406.
406.
406.
406.
406.
406.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.6
4.6
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
3. 1
4.7
4.7
37.2
40.0
37.7
34.3
39.3
29.0
35.0
33.8
33.1
34.3
33. 1
34. 1
32.2
33.1
33.4
33.8
30.8
29.4
29.5
29.8
30.3
30.0
30.0
30.0
30. 1
30.0
29.8
34. 1
39.8
37.7
36.0
31.9
31.4
31 .7
31.3
31.4
31.3
31.7
31.4
31.9
6.8 2.03
6.2 2.11
5.8 .98
3.5 .71
3.8 .96
4.0 .49
3.4 .74
3.7 .70
3.5 .66
2.9 .68
4.2 .69
3.6 .71
3.3 .60
3.7 .67
3.4 .67
3.4 .72
4.2 .61
4.1 .53
4.1 .54
4.4 .58
4.3 .60
4.2 .57
3.7 .55
3.9 .56
3.8 .55
3.7 1.55
3.6 1.55
3.4 .73
3.1 .97
3.3 . .87
3.4 .78
3.1 .60
3.1 .57
3.0 .58
3.0 .56
2.9 .56
3.0 .56
3.0 .58
3.4 .58
2.8 1.58
- 397 -
-------
APPENDIX G« TABLE II.
RUN 9: GAS FLOW RATES
PAGE 7 OF 16
DAY.HOUR
AIR
13.0130
13.0230
13.033M
13.0430
13.0530
13.0630
13.0730
13.0830
13.0930
13. 1030
13.1 130
SHUT
1 4 . 0 1 30
14.0230
14.0330
14.0430
14.0530
14.0630
14.0730
14.0830
14.0930
14.1 030
M. 1 130
14. 1230
14. 1330
14. 1430
14. 1530
14. 1630
14. 1730
14. 1830
14. 1930
14.2030
14.2130
14.2230
14.2330
15.0030
15.0130
406.
406.
406.
406.
406.
406.
423.
414.
397.
396.
396.
DOWN AT
403.
403.
403.
403.
403.
386.
386.
403.
406.
406.
406.
441 .
441.
424.
424.
424.
424.
407.
390.
390.
390.
390.
390.
424.
390.
GAS
IER
UE GAS
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
3. 1 130
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
106.
73.
73.
73.
72.
82.
66.
RAT
PILOT
PROPANE
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.6
4.6
4.6
FOR 13
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
E S M.
REGI
AIR
31.7
31.0
31.2
30.6
30.7
29.9
30. 1
27.5
30. 1
34.6
38.6
HOURS
32.8
30.5
26.8
24.5
23.8
21.2
21 .8
19.7
20. 1
36.6
36.6
41.3
37.6
37.8
38.0
34.6
31.6
31.3
30.7
30.8
30.8
31.4
32.5
30.2
30.3
M3/HR
NERATOR
NITROGEN
3.0
3.
2,
,0
,9
2.9
2.9
3.3
4. 1
4.3
3.8
2.9
2.9
2.6
2.2
1.9
2.4
1.7
1.9
1.9
1 .8
1.3
2.6
2.6
2.7
2.7
2.5
3.4
3.0
2.9
2.8
2.8
.8
.8
2.8
2.7
.0
2,
2,
3
2.4
REGEN.
VELOCITY
M/SEC
,58
,54
,54
,53
,54
,54
,58
,46
,56
1.73
1.91
62
49
31
25
18
08
1 1
02
01
82
86
04
87
86
93
76
60
59
56
56
55
59
63
54
1 .51
- 398 -
-------
APPENDIX °< TABLE II.
RUN 9: GAS FLOW RATES
PAGE 8 OF 16
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR RFGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGFN M/SEC
15.0230
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
15.0930
15. 1030
15. 1 130
15. 1?30
15. 1330
15. M30
15. 1530
15. 1630
SHUT
16.0730
16.0830
16.0930
16. 1030
16. 1 130
16. 1230
16. 1330
16. 1430
16. 1530
16. 1630
16. 1730
16. 1830
16. 1930
16.2030
16.2130
16.2230
16.2330
17.0030
1 7 . 0 1 30
17.0330
17.0430
407.
424.
424.
424.
424.
424.
390.
408.
408.
425.
425.
442.
425.
442.
425.
DOWN AT
428.
428.
445.
445.
452.
451.
451.
446.
446.
395.
412.
395.
394.
377.
377.
378.
445.
444.
56.
81.
84.
84.
88.
16.
106.
73.
73.
67.
72.
0.
0.
0.
0.
5. 1630
51.
42.
43.
72.
155.
155.
155.
155.
155.
MISSED
17.
1 1.
10.
194.
184.
184.
184.
MISSED
MISSED
135.
136.
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
FOR 1
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
DATA
4.8
4.8
4.8
4.8
4.8
4.8
4.8
DATA
DATA
4.8
4.8
29.9
?9.5
33.4
26.5
29.6
29.4
28.4
33.2
29.6
32.2
30.8
30.7
31.2
31.1
35. 1
4 HOURS
34.2
27.3
28. 1
28.6
35.5
39.7
39.4
39.4
39.7
READING
30.6
35.4
39.5
38.9
41.3
39.7
39. 1
READING
READING
33.4
31.3
2.6
2.8
3.0
2.5
2.7
2.8
2.8
3.0
2.7
3.0
2.7
2.7
3.2
2.9
3.0
2.9
7.4
6.9
4.7
3.3
3.5
3.6
3.5
3.6
3.7
3.5
3.7
3.6
3.5
3.6
3.6
3.5
3.3
,51
,49
,68
,35
,50
,49
,44
,66
,49
,61
,53
,53
,57
1 .56
1.75
.70
.60
.62
.52
.77
.97
.97
.96
.98
1.
1 ,
2,
1 ,
2.
2.
57
80
00
97
07
01
1.97
1 .69
1 .58
- 399 -
-------
APPENDIX G-' TABLE II.
RUN 98 GAS FLOW RATES PAGE
9 OF 16
DAY.HOUR
GAS
OASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
17.0530
17.0630
1 7.0730
17.0830
17.0930
17. 1030
17.1 1 30
17. 1230
17. 1330
17. 1430
1 7. 1530
17. 1630
17. 1730
17. 1830
1 7 . 1 930
17.2030
17.2130
17.2230
17.2330
1 8 . 00 30
18.0130
18.0230
18.0330
18.0430
18.0530
18.0630
18.0730
18.0830
18.0930
18. 1030
18. 1 130
18.1230
18.1330
18. 1430
18.1530
18. 1630
18.1730
18. 1830
18.1 930
18.2030
443.
444.
443.
444.
461.
464.
464.
464.
464.
464.
464.
481 .
481.
446.
446.
463.
550.
515.
516.
516.
516.
515.
481.
481 .
481 .
498.
533.
515.
515.
532.
532.
498.
377.
446.
428.
41 1.
41 1.
359.
377.
394.
136.
136.
136.
126.
126.
1 16.
126.
126.
126.
106.
1 16.
126.
94.
58.
56.
61.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
53.
0.
0.
0.
0.
85.
67.
53.
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8 .
4.8
4.8
4.8
4.8
4.9
4.9
4.9
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
31.5
33.4
32.9
31.3
30.5
29.4
38.2
39.7
39.7
40.0
40.3
40. 1
39.7
38.4
38.8
42.9
41.0
33.3
29.7
31 .6
27.8
28.8
27.3
27.7
28.5
31 .7
31.5
31.8
30.5
30.6
30.2
28.8
32.4
31 .2
35.2
41.6
44.3
44.7
43.0
41. 1
3.3 .59
3.6 .69
3.1 .64
3.2 .57
3.3 .54
4.1 .52
3.3 .89
3.5 .97
3.7 .91
3.4 . 98
3.4 .99
3.5 .98
3.4 .96
3""7 f*\ 1
.7 .91
3.3 .92
3.3 2.10
3.5 2.04
2.9 1 .66
3.1 1.50
3t~ft \ r" c~\
.0 1
2.8 1
3.5 1
2.9 1
3.0 1
3. 1 1
3.2
3.2
3.3
3. 1
3.4
3.3
3. 1
3.7
3.5
3.9
4. 1
4.2
3.9
3.5
3.0
.DO
.40
.47
.38
.40
.44
.59
.58
.60
1 .55
1 .56
1 .53
1 .46
1 .64
1 .58
1 .80
2.13
2.27
2.27
2.15
2.03
- 4OO -
-------
APPFNDIX °- TABLE II.
RUN 9: GAS FLOW RATES
PAGE 10 OF 16
DAY.HOUR
G A S
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
18.? 130
18.2230
18.2330
19.0030
19.0130
19.0? 30
19.0330
19.0430
19.0530
19.0630
19.0730
19.0830
19.0930
19. 1030
19. 1 130
19. 1?30
19. 1 330
19. 1430
19. 1530
19. 1630
19. 1730
19. 1830
19. 1930
19.2030
19.2130
19.2230
19.2330
20.0030
20.0130
20.0230
20.0330
20.0430
20.0530
20.0630
20.0730
20.0830
20.0930
20. 1030
407.
407.
424.
389.
407.
407.
389.
389.
389.
389.
389.
389.
410.
427.
427.
427.
427.
427.
444.
444.
462.
444.
462.
444.
444.
462.
444.
4^4.
444.
444.
444.
444.
444.
444.
444.
444.
427.
55.
52.
64.
57.
16.
36.
78.
85.
81.
78.
83.
84.
77.
16.
16.
0.
0.
MISSEF
0.
0.
0.
0.
0.
0.
0.
0.
STONE
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
STONE
0.
0.
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
I DATA READ
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
CHANGE
4.8
4.8
4.8
4.8
4.8
4.8
4.4
4.8
4.8
4.8
CHANGE
4.8
4.8
45.8
27.3
34.9
33.9
26.7
34.0
34. 1
30.4
31. 1
31.3
28. 1
28.2
28.5
27.4
27.7
26.6
27.7
ING
37.4
37.7
37.5
36.7
36.3
36.7
35.6
32.9
32.9
32.6
32.5
32.4
32.2
32.3
32.0
31.8
35.7
35.0
35.0
37.7
3.5 ;
2.9
2.9
3.0
3.2
3.0
3.2
3. 1
3.2
3.2
3.2
3. 1
3.2
3.1
3.1
3.0
3. 1
3.0
3.2
3.1
3.2
3.3
3.2
3.3
3.1
3.2
3.3
3.4
3.4
3.4
3.3
3.2
3.2
3.4
3.2
3.2
3.2
?.26
1 .39
1 .74
1.69
1.37
1.71
1.71
1.53
.57
.58
.44
.43
.45
.39
.40
.35
.41
.85
.87
.85
.82
.79
.81
.78
.64
.64
.64
.63
.62
.62
.62
.60
.59
.78
.76
.76
.88
- 401 -
-------
APPENDIX 0*. TABLE II.
RUN 9: GAS FLOW RATFS
PAGF
DAY.HOUR
GAS
GASIFIFR
AIR FLUE GAS
RATES MS/MR
PILOT REGENERATOR
PROPANE AIR NITROGEN
20 .1130
20. 1230
20. 1 330
20. M30
20. 1530
20. 1630
20. 1730
20. 1830
20. 1930
20.2030
SHUT
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1 330
22. M30
22. 1530
22. 1630
22. 1730
22. 1830
22. 1930
22.2030
22.21 30
22.2230
22.2330
23.0030
23.0130
23.0230
23.0330
23.0430
23.0530
23.0630
23.0730
23.0830
23.0930
427.
427.
444.
427.
427.
427.
427.
427.
427.
427.
DOWN AT
51 1 .
510.
445.
464.
455.
446.
446.
446.
446.
410.
393.
392.
394.
392.
393.
410.
410.
410.
427.
426.
410.
375 .
393.
409.
427.
0.
0.
45.
0.
43.
0.
0.
0.
0.
0.
20.2030
53.
MISSED
44.
37.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
28.
29.
0.
0.
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
4.8
FOR
4.9
DATA
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
39.7
39.7
39.7
40.5
36. 1
41.2
31.2
35.0
36.8
35.0
35 HOURS
26.2
READING
35. 1
32. 1
32.5
35.6
31.8
34.0
31.6
31.8
30.0
32.9
28.4
25.3
27. 1
27. 1
28.8
29.4
28. 1
28.4
27.9
28.4
27.4
25.8
24.2
23.5
3,
3,
3,
3,
3,
4,
,7
,7
,7
,6
,4
,0
3.0
3.3
3.5
3.5
3.6
3.7
3.2
3.3
3.6
3.3
4. 1
4.4
4.0
5.2
5.7
5.5
4.8
5.6
4.0
4.2
6. 1
6.3
6.7
6.6
6.7
6.4
6.5
4.8
4.6
1 OF 16
REGEN.
VELOCITY
M/Sf-C
2.00
2.00
1 .99
2.01
1 .80
2.06
1 .55
1.74
1 .83
1 .76
1.35
1 .78
1 .63
1 .65
1 .HI
1 .62
1 .77
1 .67
1 .67
1 .63
1.79
1 .56
1 .39
1 .53
1 .47
1.57
1.72
1.65
1 .69
1 .66
1 .69
1 .63
1.54
1.37
1 .35
- 402 -
-------
APPENDIX G. TABLE II.
RUN 9» GAS FLOW RATES
PAGE 12 OF 16
DAY.HOUR
GAS
OASIFIEH
AIR FLUE GAS
RATES M3/HR
PILOT REGENERATOR
PROPANE AIR NITROGEN
23. 1030
?3. 1 130
23. 1230
23. 1330
23. 1430
23.1530
23. 1630
23. 1730
23. 1830
23. 1930
23.2030
2 3 . 2 1 30
23.2230
23.2330
24.0030
24.0130
24.0230
24.0330
24.0430
24.0530
24.0630
24.0730
24.0830
24.0930
24. 1030
24. 1 130
24. 1230
24. 1330
24. 1430
24. 1530
24. 1630
24. 1730
24. 1830
24.1930
24.2030
24.2130
24.2230
24.2330
25.0030
25.0130
428.
428.
375.
410.
410.
410.
410.
41 1.
41 1.
41 1.
341.
341.
375.
410.
427.
443.
445.
409.
410.
393.
376.
376.
376.
375.
393.
410.
410.
410.
410.
410.
393.
393.
393.
375.
375.
375.
410.
410.
410.
410.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
33.
34.
26.
27.
30.
29.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
25.3
25.7
24.9
27.5
25.5
?9,®
£4.6
34.4
34.8
36,1
34. 1
25.9
23.0
21.6
21.6
25.7
26.3
29. 1
25. 1
23.9
24. 1
24.3
22.7
19. 1
26.4
30. 1
30.0
29.4
28.8
28.6
28.8
28.7
28.7
28.5
28.7
27.9
28.8
28.5
28. 1
28.3
5. 1
4.7
3.1
3.3
3.2
3.4
3.3
2.8
3.5
3.4
3.4
2.4
2.5
2.4
2.5
2.7
2.7
2.4
2.9
3.0
2.8
2.7
2.7
3.6
5.3
5. 1
5.2
5.0
4.9
4.9
5.0
4.9
4.9
4.9
4.9
4.8
5.6
3.9
3.8
3.9
.47
.48
.36
.51
.39
.58
.83
.80
.86
.92
.81
.37
.23
. 15
. 16
.37
.43
.55
.39
.34
.34
.36
.28
.03
.44
.61
.61
.60
.56
.56
.57
.55
.56
.56
.58
.55
.65
.51
.50
.50
- 4O3 -
-------
APPENDIX G; TABLE II.
RUN 9: GAS FLOW RATES
PAOF 13 OF 16
DAY. HOUR
GAS
GASIFIER
AIR FLUE GAS
25.0230
25.0330
25.0430
25.0530
25.0630
25.0730
25.0830
SIIU1
25. 1430
25. 1530
SHUT
25.2230
25.2330
26.0030
26.0130
26.0230
26.0330
26.0430
26.0530
26.0630
26.0730
26.0830
SHUT
26.2230
26.2330
27.0030
27.0 130
27.0230
27.0330
27.0430
27.0530
410.
410.
410.
410.
393.
410.
410.
DOWN AT
375.
375.
DOWN AT
444.
444.
444.
410.
410.
410.
410.
427.
427.
427.
375.
DOWN AT
444.
444.
444.
444.
444.
462.
444.
479.
0.
0.
0.
0.
32.
0.
0.
25.0830
0.
0.
25. 1530
0.
0.
0.
0.
13.
13.
13.
0.
0.
0.
0.
26.0830
0.
0.
0.
0.
0.
0.
0.
0.
RAT
PILOT
E S M.
REGI
PROPANE AIR
4.9
4.9
4.9
4.9
4.9
4.9
4.9
FOR 6
4.9
4.9
FOR 7
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
FOR 14
4.9
4.9
4.9
4.9 *
4.9
4.9
4.9
4.9
28.0
27.6
28.5
26.5
27.8
26.4
26.8
HOURS
27.8
26.6
HOURS
32.6
32.8
31.5
32.3
27.9
26.5
27. 1
22.0
22.3
21. 1
21.5
HOURS
36.4
41 .4
42.3
42.3
45.0
44.3
41.9
42.0
M3/HR
NERATOH
NITROGEN
3.9
4.3
5.0
4.7
4.8
4.2
4. 1
4.6
5.0
4.9
4.8
5.5
5.6
5.2
5.3
5.5
5.3
5.8
5.5
5.5
4.6
4.6
4.6
4.6
4.7
4.6
3.b
3.0
REGEN.
VELOCITY
M/SEC
1 .49
1,51
1 .59
1 .48
1.54
1 .44
1 .45
1.53
1.51
1.73
1 .79
1 .80
1 .84
1.61
1.56
1 .60
1 .31
1.33
1 .25
1.27
1.77
2.04
2. 1 1
2. 10
2.2.4
2. 19
2.06
2.03
404 -
-------
APPENDIX G» TABLE II.
RUN 9: GAS FLOW RATES PAGE 14 OF 16
DAY.HOUR
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
27.0630
27.0730
27.0830
27.U930
27. 1030
27. 1 130
27. 1230
27. 1330
27. 1430
27. 1530
27. 1630
27. 1730
27. 1830
27. 1930
27.2030
27.2130
27.2230
27.2330
28.0030
28.0130
28.0230
28.0330
28.0430
28.0530
28.0630
28.0730
28.0830
28.0930
28. 1030
28. 1 130
28. 1230
28. 1330
28. 1430
28. 1530
28. 1630
28. 1730
28. 1830
28. 1930
28.2030
28.2130
462.
462.
427.
427.
393.
393.
392.
375.
376.
410.
410.
410.
410.
41 1.
393.
376.
376.
410.
41 1.
41 1.
393.
356.
388.
375.
375.
395.
376.
376.
376.
376.
377.
387.
387.
396.
396.
396.
379.
379.
396.
379.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
- 0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
5.0
41.6
45.6
46.0
43.2
45.6
42. 1
42.2
42.6
35.4
38.4
38.6
38.5
38.7
40.5
40.7
43.3
40.4
38.2
40.0
39.7
39.0
41.2
36. 1
37.5
39.9
37.2
35.7
38.4
37.5
37.3
36.7
38.6
39.5
47.2
48.7
49.0
51.0
46. I
41.8
40.3
3.1
3.3
3.5
4. 1
3.0
3.3
4.0
3.9
3.3
3.4
3.4
3.7
3.5
3.8
3.6
4.0
3.6
3.2
3.4
3.3
3.3
3.3
2.9
3.0
3.4
3.6
3.0
3.2
3.3
3.3
3.7
3.6
3.4
3.8
3.6
3. 1
3.9
3.3
2.8
3.2
2.02
2. 19
2.26
2. 13
2. 19
2.05
2.09
2. 1 1
1 .75
1 .88
1.89
1.90
1 .90
2.00
2.00
2. 13
.99
.85
.95
.93
.89
.99
.75
.82
.93
.82
.73
.86
.83
.81
.80
.87
1.90
2.27
2.34
2.34
2.47
2.21
2.00
1.95
- 405 -
-------
APPENDIX G; TABLE II.
RUN 9s GAS FLOW RATES
PAGE 15 OF 16
DAY.HOUR
28.2230
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HR
PILOT REGENERATOR
PROPANE AIR NITROGEN
345.
0.
5.0
40.0
SHUT DOWN AT 28.2230 FOR 24 HOURS
2.9
REGEN.
VELOCITY
M/SEC
1 .93
29.2330
30.0030
3W.0130
30.0230
30.0330
30.0430
30.0530
30.0630
30.0730
30.0830
30.0930
30. 1030
30 . 1 1 30
30. 1230
30. 1330
30. M30
30. 1530
30. 1630
30 . 1 730
30 . 1 830
30. 1930
30.2030
30.2130
30.2230
30.2330
31 .0030
31 .0130
31.0230
31 .0330
31 .0430
31 .0530
31 .0630
31.0730
31.0830
31 .0930
406.
440.
475.
406.
371.
373.
356.
344.
361.
344.
344.
344.
344.
344.
344.
344.
36 .
36 .
36 .
36 .
36 .
378.
413.
344.
345.
449.
443.
357.
357.
340.
340.
341 .
341.
87.
87.
88.
MISSED
MISSED
107.
147.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
27.
0.
0.
0.
0.
0.
36.
90.
0.
0.
0.
0.
4.9
4.9
4.9
DATA
DATA
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
30.5
30.3
30.5
READING
READING
31.6
31.2
35.2
31.7
34.6
31.5
24.2
27.7
26.7
27.7
28.9
26.9
28.6
28.0
28.7
27.6
28.2
28.4
34.6
36.4
35.2
34.2
34.5
38.5
40. 1
34.7
26.5
31.3
32.3
32.4
4.5
5.2
4. 1
2.6
4. 1
4.2
4. 1
4.4
3.8
3.6
2.4
2.5
2.8
2.6
2.6
2.8
2.7
3.0
2.8
1 .5
2.3
4. 1
3.7
3.3
2.5
2.6
3.8
3.9 ;
2.8
2.3
2.3
2.4
2.4
.53
.58
.57
.55
.61
.79
.62
.76
.59
.27
.37
.33
.39
.44
.34
.43
.40
.45
.39
.36
.40
.78
.83
.76
.69
.68
.92
?.01
.72
.32
1.55
1 .60
1 .60
- 406 -
-------
DAY.HOUR
APPENDIX G-' TABLF II.
RUN 9t GAb FLOW RATES
PAGE 16 OF 16
GAS
GASIFIER
AIR FLUE GAS
RATES M3/HH REGEN.
PILOT REGENERATOR VELOCITY
PROPANE AIR NITROGEN M/SEC
31 . 1030
3 1 . 1 1 30
31 . 1P30
31 . 1330
31 . 1430
31. 1530
31.1 630
31 . 1730
31 . 1830
31 . 1930
31 .2030
3 1 . 2 1 30
31 .P230
31 .2330
32.0030
32.0130
32.0230
32.0330
32.0430
32.0530
32.0630
32.0730
32.0830
341.
380.
361.
340.
340.
340.
381 .
382.
372.
490.
490.
490.
445.
41 1.
409.
402.
374.
406.
405.
404.
370.
369.
370.
0.
0.
0.
0.
0.
0.
72.
75.
75.
0.
STONE
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
CHANGE
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
4.9
30.5
31.9
31.8
33.0
31.0
31.3
28.9
29.4
30.7
31.0
28.5
30.6
31.2
31.3
31.5
30.9
30.7
29.8
29.5
28.8
28.9
28.6
29.8
2.2
2.2
2.3
2. 1
2. 1
2.4
2.5
2.6
2.7
2.3
2.0
2.4
2.6
3.0
3.0
3.0
2.8
3.0
2.9
2.6
2.6
2.5
2.5
.51
.57
.56
.60
.52
.52
1 .42
1 .45
1 .52
1.50
.37
.50
.54
.56
.57
.54
.53
.49
.46
.41
.42
.40
.46
- 407 -
-------
APPENDIX G* TABLE III.
RUN 9: PRFSSURES PAGE
1 OF 16
GASIFIER P. KILOPASCALS
DAY. HOUR
1 . 1930
1 .2030
1 .2130
GAS
SPACE
1 .9
1 .9
2.9
DISTRIB.
D.P.
2.4
2.4
2-2
BED
D.P.
5.5
5.5
5.5
GASI FIER
BED
SP. GP.
PI. 95
(7!. 95
0.95
RFGFN.
BED
D.P.
5.7
5.7
6.5
1 . 1930
1 .2030
1 .2130
SHUT
2.0230
2.0330
2.0430
2.0530
2.0630
2.0730
2.0830
2 . 09 30
2. 030
2. 130
2. 230
2. 330
2. 430
P. 530
2. 63P)
2. 730
2. 1830
2. 1930
2.2030
2.2130
2.2230
2.2330
SHUT
4.0430
4.0530
4.0630
4.0730
4.0830
4.0930
4. 1030
1 .9
1 .9
2.9
DOWN AT
2.6
2.6
2.7
2.7
2.9
2.7
2.7
2.9
3.2
3.4
3.4
3.5
3.4
4.4
4.4
4.5
4.4
4.2
4. 1
4.2
4.5
5.0
DOWN AT
2.4
2.2
1 .9
2.2
2.0
2.0
1.2130 FOR
2.4
2.4
2.6
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.4
2.4
2.4
2.4
2.4
2.4
2.5
2.2330 FOR
2.7
2.5
2.2
2.7
2.5
2.4
MISSED DATA READING
5.5
5.5
5.5
4 HOURS
5.2
5.5
5.6
6.0
6. 1
6.1
6.2
6.3
6.2
6. 5
6.5
6.6
6.6
6.7
6.8
7. 1
7.2
7.2
7.7
7.7
7.6
7.6
28 HOURS
7.8
8. 1
8.3
8.6
8.7
8.8
0.95
0.95
0.95
1 .00
1 .00
1 .00
1 .00
1 .00
0.95
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
6.2
6.2
6. 5
6.2
6.7
6.5
6.7
6.2
6.2
6. 5
6.2
6.2
6.2
6.2
6.2
7.5
7. 5
7.6
7.8
7.8
7.8
7.8
0.
0.
0.
0.
0.
0.
- 408 -
-------
DAY.HOUR
4.
A.
A'
4.
4.
4.
A>
1230
1330
1430
1530
1630
1730
1830
4. 1930
4.2030
4.2130
4.2230
.2330
. 0030
.0130
.0230
.0330
.0430
.0530
4
5.
5.
5.
5.
5,
5.
5.
5
S
5
5
5
5
5
5
5
5
5
5
5
5.
5
5.
6,
6.
6,
.0730
. 08 30
.0930
. 1030
. 1 130
. 1230
. 1330
. 1430
. 1 530
. 1630
. 1 730
. 1830
, 1930
.2030
.2130
.2230
.2330
.0030
0130
0230
APPENDIX G. TABLE III.
RUN 9: PRESSURES PAGE
GASIFIER P. KILOPASCALS
GAS DISTRIB. BED
SPACE D.P. D.P.
2 OF 16
6.0330
2.4
2.4
2.2
2.3
2.4
2.4
2.3
2.2
2.3
2.5
2.6
2.2
2.7
2.7
2.6
2.6
2.6
2.5
2.5
2.6
2.6
2.6
2.7
2.9
2.9
2.7
3.5
3.7
3.7
3.7
3.7
3.7
3.7
3.7
4.0
4.0
4.0
4.0
4.0
4.0
4.2
4.0
4.0
3.9
4.2
4.4
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
3.7
3.7
3.7
3.7
3.7
3.6
3.9
4.0
3.7
3.9
4.2
4. 1
4. 1
4.0
4.2
4.2
4. 1
4.5
4.2
4.5
4.5
4.5
4.5
4.5
8.6
8.7
8.7
8.7
8.5
8.5
8.7
9.0
9.1
9.2
9.2
9.8
9.0
8.7
9.0
9.0
9.3
9.3
9.5
9.7
9.7
10.0
10.0
10. 1
9.8
10. 1
9.5
9.2
9.5
9.7
9.2
9.7
9.8
9.7
9.8
9.7
9.7
9.7
9.7
9.7
GASIFIER
BED
SP . G R .
1 .00
1 .00
1 .05
1 .00
1 .00
0.95
1 .05
0.97
.00
.00
.00
.00
.00
3.90
.00
.00
.00
.00
.00
.00
.00
.98
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
REGEN
BED
D.P.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
PI.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
- 4O9 -
-------
APPENDIX Q. TABLE III .
RUN 9t PRESSURES PAGF
3 OF 16
DAY.HOUR
GASIFIER
GAS
SPACE
6.0430
6.0530
6.0630
6.0730
6.0830
6.0930
6. 1030
6. 1 130
6. 1230
6. 1330
6. 1 430
6. 1 530
6. 1 630
6. 1 730
6. 1830
6. 1930
6.2C/3P
SH UT
7.01 30
7.0230
7.0330
7.043T"
7.0530
7.0630
7.0730
7.0830
7.0930
7. 1030
7 , 1 1 30
7. 1230
7. 1330
7. 1 430
7. 1 530
7. 1630
7. 1 730
7. 1830
7. 1930
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4. 1
4. 1
4.2
3.7
4.0
3.9
3.9
3.4
3.4
DOWN AT
3.3
3.9
3.9
3.9
3.7
3.5
3.5
3.5
3.6
4.0
4.0
4.1
4.1
4.0
4.0
4. 4
4. 1
4. 1
4. 1
R P. KILOPASCALS GASIFIF.R
DI STRIB.
D.P.
4.5
4.5
4. 5
4. 5
4.2
4.2
5.0
5.6
5.6
5.6
5.6
5.4
5. 5
5.5
5.5
5.0
5.0
6.2030 FOR
4. 7
5.2
5.2
5.2
5.1
5. 1
5.0
5.0
5.0
5.0
5.0
5.0
2. 7
2.2
2.2
2.5
2.P
2.5
2.5
BED
D.P.
9.7
9.3
9.5
9.2
8.6
9. 1
9.0
8.8
8.8
8.6
8.3
8.5
7.7
B.I
8.1
7.8
7.6
4 HOURS
7.7
7.7
8. 1
8.1
8 .2
8.2
8.2
8.2
8.3
8.3
8.5
8.5
8.6
8.7
8.8
9.5
10. 1
10.7
10.9
BED
SP. GR.
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
0.95
0.95
0.95
1 .00
1 .00
1 .00
1 .00
1 • 1P-
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
RFGEN
BFD
D.P.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
171.
0.
0.
0.
P.
C-l.
0.
0.
0.
0.
R.
0.
0.
0.
0.
0.
0.
10.5
10.5
10.6
10.7
10.7
12.4
12.4
12. 1
1 1 .9
- 410 -
-------
APPENDIX G. TABLF III.
RUN 9: PRESSURES PAGE
4 OF 16
DAY. HOUR
7.2030
7.21 30
7.223(7
7.2330
R.0(?3fl
8.0130
R .0230
8.0330
R .0430
8.0530
8 .0630
8.0730
8.0830
8.0930
8. 030
8. 1 30
8 . 230
8. 330
8. 430
8 . 530
8. 630
8. 730
8. 830
8. 930
8.2030
8.2130
GASIFIER P. KILOPASCALS
GAS DI STRIP. BED
SPACE
4. 1
4.4
4.4
4.4
4.4
4.4
4.4
4. 4
4. 4
4.4
4. 4
4.5
4.5
4.5
4. 5
4.5
4.5
4.5
4.5
4.2
4.2
4. 5
4. 5
4.5
4.7
5.0
D.P.
2.5
2.5
2.5
2.6
2.6
2.6
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2. 7
2.5
2.5
2.7
2.5
2.7
2.7
2.6
D.P.
1 1 .2
10.7
10.7
10.7
10.7
10.7
10.7
0.9
0.8
0.8
0.8
0.8
0.9
1 .2
1 .2
1 .3
1 .3
.3
.6
.6
.8
.6
.7
.6
.6
.6
GASIFIER
BED
SP. GR.
.Pi PI
• 00
.00
• H0
.00
.00
• 0R
.00
.00
. 00
.00
.00
.00
.00
.00
.00
. 00
. 00
.00
.00
. 00
.00
. 00
.00
1 .00
1 .00
REGEN
RED
D.P.
1 Pj.P
11.9
12. /i
1 2. /I
13.7
13.7
13.7
13.7
13.7
13.7
1 3.7
13.7
13.7
13.7
13.7
13.7
13.7
13.7
13.7
13.7
13. 7
13.7
13.7
13. 7
13.7
1 3.7
SHUT DOWN AT 3.2130 FOR
8 HOURS
9 .0630
9.0730
9 .0830
9 .0930
9 .
9 .
9 .
9.
9 .
9 .
030
130
230
330
430
530
3.2
3.2
3.4
3. 5
3.5
3.5
3.5
3.5
3.5
3.7
2.6
2.7
2.7
3.0
2.7
3.0
3.0
3.0
3.0
3.0
10.8 0.90
10.9 0.90
10.9
10.7
10.7
10.9
10.8
10.8
10. 5
10.2
.00
.00
.00
.00
. 00
.00
.00
.00
13.7
13.7
12.4
12.4
12.4
12.4
12.4
12.4
12. 4
12.4
- 411 -
-------
APPENDIX G< TABLF. Ill .
RUN 9: PRESSURES PAGE
5 OF 16
9. 1 630
9. 1 730
9. 1830
9. 1930
9.2030
SHUT
10.0230
10.0330
10.0430
10.0530
10.0630
10.0730
10.0830
10.0930
10. 030
10. 130
10. 230
10. 330
10. 430
10. 530
10. 630
10. 730
10. 830
10. 930
10.2030
10.2130
10.2230
10.2330
1 .0030
1 . 0 1 30
1 .0230
1 .0330
1 .0430
1 .0530
1 .0630
1 .0730
1 .0830
3.7
3.7
3.7
3.7
3.7
DOWN AT
2.9
2.9
3.4
3.5
3.6
3.5
3.7
3.7
3.5
3.7
3.7
3.7
3.7
3.7
3.7
3.7
3.6
3.6
3.6
3.6
3.6
3.6
3.6
3.7
3.6
3.6
3.7
3.5
3.5
3.6
3.6
9.2030 FOR
2.6
2.7
2.7
2.9
2.9
2.9
3. 1
3.0
3.0
3.0
3.0
3.0
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.7
2.9
2.7
2.7
2.7
2.7
2.7
2.5
2.5
2.6
2.6
SCALS GASIFIER
BED BED
D.P. SP. GR.
10.5 1 .00
10.5 1.00
10.6 1 .0!?)
10.7 1 .00
10.9 1.00
5 HOURS
0.9
0.9
0.9
1 . 1
.3
.3
.3
.6
.4
• A
.4
. 4
.4
.4
1 .4
1 .7
1 .4
1 .4
1 .4
11.7
11.7
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
11.7 1 .00
11.7 1 .00
11.4 1 .00
11.2 1 .00
11.2 1 .00
10.9 1.00
1 1 .2 1 .00
11.3 1.00
11.7 1.00
11.6 1 .00
REGEN
BFD
n.p.
12.4
1?. 4
12.4
1?.4
12.4
13.7
13.7
13.7
13.7
13.7
13.7
13.7
12.9
12.4
12.4
12. &
12.4
12.4
12.4
12.4
12. 4
12. 4
12.4
12.4
12.4
11.2
9.5
10.0
10. 5
11.2
11.3
11.1
10.7
10.7
10« 5
10.6
- 412 -
-------
DAY.HOUR
1
1
1
1
I
1
1
J
1
1
1
1
1
1
1
IP.
IP,
IP.
IP.
IP.
IP.
JP.
IP..
1?
IP.
IP.
IP.
IP.
IP.
IP.
0930
• 1 130
• 1230
• 1 330
. 1 430
. 1530
. 1630
• 1 730
. 1330
-1930
.2030
•PI 30
.2230
.2330
.0030
.0130
.0230
.0330
.0430
.0530
.0630
.0730
.0830
.0930
.1030
1130
1230
1330
1430
IP. 1 530
IP. 1 630
.1730
. 1R30
. 1930
• P030
• PI 30
.PP30
12.2330
1 3.0030
1 P.
IP.
IP.
IP.
IP.
IP.
APPFNDIX G> TABLE: m
RUN 9: PRESSURES
GASIFIER P. KILOPASCALS
GAS DISTRIB. BED
SPACE D.P. D.P.
PAGE 6 OF 16
3.7
3.9
3.9
4.0
4.0
3.7
3.7
3.7
3.6
3.9
4.0
4.2
4.P
4.2
4.2
3.7
3-6
3.6
3.5
3.4
3.6
3.6
3.6
3.7
3.7
3.7
3.6
3.6
3.7
3.7
3.7
3.7
3.7
3.9
3.9
3.9
3.9
3.9
4.0
4. 1
P.9
2.7
2.9
3.0
3.0
3.0
3.0
2.7
2.7
2.7
2.9
3.0
3.0
3.0
3.0
2.6
2.4
2.4
2.4
2.4
2.5
2.6
2.7
2.5
2.6
2.6
2.6
P.6
2.7
2.7
2.6
P.7
2.7
P.7
2. 7
2.7
2.7
2.6
2.6
P.6
1 1
1 1
1
• 4
.3
.2
10.9
1 . 1
1.3
1 *4
1 .4
1 .6
1 .4
11.4
11.4
1 1 .4
11.4
11.4
1 1 .4
11.6
11.6
.7
7
7
7
1
7
6
7
6
7
6
7
8
R
1
1
.8
.R
.7
.7
.7
1 .7
1 .7
1 .8
1 .8
GASIFI ER
BED
SP. GR.
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .05
1 .05
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 . 0Pi
1 .00
1 .00
1 .00
1 .0PI
1 .00
1 .00
1 .00
1 .00
REGEN.
BED
D.P.
10.6
10.7
1 L3
11.7
1 1 .8
1 1 .8
1 1 «8
1 1 .8
1 1 .8
1 1 .8
1 1 .8
1 1 .8
1 1 .9
1 1 .9
1 1 .9
11.7
1 1 .9
1 1 .9
1 1 .9
11.7
1 1 .9
1 1 .9
1 1 .9
1 1 .9
IP. 4
IP. 4
12.4
1 1 .9
11.7
1 1 .7
1 1 .9
1 1 .9
1?. 4
IP. 4
IP. 4
IP. 4
IP. 4
IP. 4
12.7
IP. 4
- 413 -
-------
APPENDIX G> TABLE
RUN 9: PRESSURES
III
PAGE 7 OF 16
DAY. HOUR
3.01 3d
3.0230
3.0330
3.0430
3.0530
3.0630
3.0730
3.0830
3.0930
3. 1030
3. 1 130
GASIFIER P. KILOPASCALS GASIFIER
GAS DISTRIB. BED BED
SPACE
4. 1
4. 1
4.?
4.?
4.2
4.2
4.7
4.9
4.7
4.9
4.9
D.P.
2.6
2.6
2.5
2.5
2.5
2.5
2.6
2.6
2.7
2.6
2.6
D.P. SP. GR.
11.8 1 .00
1 1 .9 1 .00
1 1 .9
12.1
12.1
12. 1
1 1 .8
1 1 .8
1 1 .7
1 1 .8
.00
.00
.00
.00
.00
.00
.00
.00
11.7 1 .00
REGEN.
RED
D.P.
12.4
12.7
12.7
12.7
12.7
12.7
12.7
12.7
12.9
1 1.9
1 1 .9
SHUT DOWN AT 13.1130 FOR 13 HOURS
1 4.
/I.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
5.
5.
0130
0230
0330
0430
0530
0630
0730
0830
09 3P
1030
1 30
230
330
430
530
1630
1730
1830
1930
2030
2130
2230
2330
0030
0130
3.
3.
3.
3-
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
4.
4.
4.
3.
4.
4.
4.
4
4
2
2
2
2
2
5
2
5
6
2
2
2
2
4
9
9
0
1
4
9
1
2
4
4
3
3
3
3
3
3
3
4
4
4
3
3
3
2
2
2
3
3
3
3
3
3
3
3
•
•
*
•
•
•
•
»
*
•
•
•
•
•
•
*
•
*
•
»
•
»
»
»
*
0
9
7
7
7
7
7
7
0
0
0
2
1
1
7
9
9
0
5
2
2
1
1
1
4
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
0. 1
0.3
0.6
0.8
0.9
1 .1
1 .3
1 .7
1 .6
2.1
1 .8
1 .3
0.9
0.9
1 • 1
1 . 1
0.5
0.5
0.6
0.7
0.7
0.9
0.8
0.8
0.8
.00 1
.00 1
.00 1
.00 1
.00 1
.00 1
.00 1
.00 1
1.00 1
1 .00
1 .00
1 .00 1
1 .00 1
1 .00 1
1 .00 1
1 .00 1
.00 1
.00 1
.00 1
.00 1
.00
.00
.00
1 .00
1 .00
0
0
1
1
1
1
2
2
3
7
7
0
0
0
0
0
0
0
.6
.7
.2
.7
.8
.9
.2
. 4
.7
.0
.0
.0
.3
.9
.0
.7
.7
.7
.4
.
-------
APPENDIX G> TABLE
RUN 9: PRESSURES
III
PAGE 8 OF 16
JAY.
HOUR
5.0P30
5.0330
5.0430
5.0530
5.0630
5.0730
5.0830
5.0930
5. P30
5 »
5.
5.
5.
5.
5.
130
P30
330
430
530
630
GASIFI
GAS
SPACE
4. 4
4.5
4.4
3.7
4. 1
4.?.
4.5
4.9
4.7
5.5
5.8
5.7
5.6
5. 7
5.7
ER P. KILOPASCALS
DISTRIB. BED
D.P. D.P.
3.4 10.9
3.5 10.9
3.6 11.1
3.6 11.7
3.5 11.3
3.2 10.8
3.1 10.7
3.4 10.9
3.5 10.9
3.4 10.9
3.4 10.9
3«0 10.9
2.9 10.9
2.9 10.9
2.9 10.9
GASIFI ER REGEN
BED BED
SP. GR. D.P.
.00
.00
.00
.00
.00
.00
.00
1 .8
1 .7
1 • 1
1 .9
1.9
0.5
0.0
.00 9.7
.00 10.5
.00 10.5
.00 9.5
.00 10.2
•00 10.2
.00 10.5
•00 10.2
SHUT DOWN AT 15.1630 FOR 14 HOURS
16.0730
16.0330
6.0930'.
6. 1030
6.11 30
6.
6.
6.
6.
6.
6.
6.
6.
230
330
430
530
630
730
830
930
6. 2030
6. PI 30
6.PP30
6.P330
7.0030
7.0130
7.0330
7.0430
3
3
3
3
4
4
4
4
3
3
3
3
3
3
3
3
3
4
.6
.5
.6
. 7
. 1
.0
.0
.0
.7
. 7
. 1
.0
• 1
.0
.0
.0
.9
.2
4.9
5.0
5. 1
6.0
7.0
6.R
6.R
7.0
7.0
MISSED
7. 5
8.0
R.0
7.7
8.0
8.0
8.0
MISSED
MISSED
7.?.
7.P
1
1
1
1
1
DATA
1
1
9
9
9
0
0
0
0
9
0
9
0
0
10
1
1
1
DATA
DATA
0
0
0
9
9
• 3
.6
.7
.0
. 1
. 1
.0
.8
.0
READING
.6
.0
.0
.0
.0
.0
.0
READING
READING
. 7
.8
!
1
.00
• 00
.00
.00
• 00
.00
.00
.00
.00
. 00
.00
. 00
.00
.00
.00
• 00
. 00
.00
10
10
10
9
9
9
9
9
9
9
9
9
9
9
9
9
in
10
.0
.?
.5
. 5
.7
.7
.7
.7
.7
.5
.P
. 5
.P
• 3
• 3
• 3
.0
.5
- 415 -
-------
APPENDIX
TABLE III.
RUN 9: PRESSURES
PAGE 9 OF 16
GASIFIER P. KILOPASCALS
DAY. HOUR
1 7.0530
1 7.0630
1 7.0730
1 7.0R30
1 7.0930
1 7. 1030
17. 130
17. ?30
17. 330
17. 430
17. 530
17. 630
17. 730
17. 830
17. 9 30
1 7.2030
17. 21 30
1 7.?? 30
1 7.2330
1K.0M30
1 R .PI 1 30
18 .0230
18.0330
18 .0430
18 .0530
18.0630
18.0730
18 .0830
18.0930
18 . 1030
18.1130
8. 230
8. 330
8 . 430
8 . 530
8. 630
8. 730
8. 1830
8 . 1930
R.2030
GAS
SPACE
A.?.
4. 1
4. 1
4.2
4.?
4.?
4.?
4.2
4.?
4.2
4.2
4.4
4. 6
4.5
5. 1
5.5
4.9
4.7
4.7
5.0
5.0
4.9
4.9
5.0
5. 1
5. 1
5.?.
5.9.
5.2
5.?
5.?.
5.0
5.2
5.2
5.4
4.6
4.7
4.9
4.6
4.7
DI STRIB.
D.P.
7.2
7.2
7.2
7.2
7.5
7.2
7.2
7.0
7.2
7.2
7.2
7.7
7.6
8.0
7.8
7.5
7.2
6.5
6.5
6.3
6.2
6.3
6.2
6.2
6.2
6.2
6.5
6.5
6.2
6.2
6.3
5.8
7.1
5.5
4.9
4.9
4.7
6.2
5.7
5.7
BED
D.P.
9.7
10.0
9.R
9.7
9.7
9.7
9.7
9.8
9.8
8.3
9.3
9. 1
9 .6
9.5
9.2
9.0
9.7
9.7
9.7
9.7
9.7
9.7
9.8
9.8
9.8
10.0
10.0
10. 1
10. 1
10.0
10.2
10.2
10.2
10.2
10.0
10.7
10.8
10.5
10.6
10.6
GASIFIER
BED
SP. GR.
1 .00
1 .00
1 .00
1 .00
1 .PI0
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .30
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
REGFN
BED
D.P.
10.6
10.2
10. 5
10.3
10.5
9.P
9.3
9.5
9.3
9.0
8.7
8.7
10.0
9.2
9.0
9.0
9.0
1 .2
1 .2
1 •?
\ .2
1 .2
1.4
1 . 4
11.7
1 1 .2
11.4
1 1 .8
1 1 .8
11.4
11.4
10.7
10.9
7.5
9.5
7.0
7.2
6.7
6.R
7.2
- 416 -
-------
APPENDIX G« TABLE III.
RUN 9: PRESSURES PAGE I Pi OF
DAY.HOUR
1R.P130
1R.2P30
1R.2330
19.PK'3P
19.0130
19.0P3R
19.0330
19.0430
19. PI 530
19 .0630
19.0730
19.0R30
19.0930
19. 030
130
230
330
430
530
630
730
1830
19
19
19
19
19
19
19
19
19. 1930
19 .P030
19.2130
19.2230
19
?0
20
20
P0
P0
P0
P0
P0
?0
. P330
. 0030
.0130
• 0P30
.0330
.0430
.0530
.0630
.0730
• 0R30
20.0930
P0.1030
GASIFIER
GAS
SPACE
4.5
3.9
4.5
4.4
4.5
4.5
4.7
5.0
4.9
5.0
4.6
4.7
4.9
4.7
4.7
4.7
4.5
4.7
4.7
5.0
5.0
5.0
4.9
5. 1
5.4
5.4
5.4
5.P
5.P
5.
5.
5.
5.
5.
5.
5. 1
5.P
P. KI
DISTRI
D.P.
5.7
4.5
5.7
5.5
5.6
5.8
5.8
5.8
5.P
5.P
5. 1
5.0
5.0
4.5
4.6
4.5
4.4
MI SSED
5.2
5.0
4.7
4.7
4.7
4.7
4.9
4.9
STONE
4.9
4. 7
4.6
4.6
4.4
4.4
4.4
4* 4
4.4
4.4
STONE
4*4
4.5
LOPASCALS
B. BED
D.P.
10.5
10.3
10.2
10.0
9.7
9.5
9.5
9.P
9.3
9. 1
9. 1
9 .0
9. 1
9.3
9.4
9.5
9.5
DATA READI
10.0
10.2
10.3
10.2
10.3
10.6
10.5
10.2
CHANGE
10.3
10.5
10.6
10.7
10.7
10. 7
10.6
10.5
10.5
10.3
CHANGE
10.5
10.6
GASIFIER
BED
SP. GR.
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
NG
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
1 .00
1 .00
1 .00
1 .00
RFGEN
RED
D.P.
11.?
IP. 7
9. 5
10. P
9.5
9.5
9. 5
10.5
10. 5
10.6
10.6
10.5
10. 7
10.7
10.7
10.6
10.6
9.0
7.7
R.5
8.5
8.6
9.2
10.0
1 1 .P
1 .4
. 4
.7
.7
.7
.4
.4
.4
0.5
0.9
10.7
9.7
- 417 -
-------
APPENDIX V: TABLE III.
RUN 9: PRESSURES PAGE 11 OF
GASIFIER P. KILOPASCALS
DAY. HOUR
20.
20.
20.
20.
20.
20.
20.
20.
20.
130
230
330
430
530
630
730
830
930
20.2030
GAS
SPACE
5.5
5.6
5.7
5.7
5.8
5.8
5.9
5.9
5.9
6. 1
DISTRIB.
D.P.
4.5
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.7
4.5
BED
D.P.
10.2
9.8
9.7
9.8
9.7
9.7
9.7
9.7
9.7
9 .3
GASIFIER
RED
SP. GR.
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .05
REGEN
BED
D.P.
9.7
10.0
9.7
10.2
10.9
10.9
10.9
1 1 .2
10.7
10.5
SHUT DOWN AT 20.2030 FOR 35 HOURS
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1330
22. 1 430
22. 1 530
22. 1630
22. 1 730
P2. 1R30
22. 1930
22. 2030
22.2130
22.2230
22.2330
23.0030
23.01 30
23.0230
23.0330
23.0430
23.0530
23.0630
23.0730
23.0830
23.0930
3.6
3.6
3.4
3-2
3.4
3.4
3.4
3«4
3.4
3- 1
2.9
2.9
2.9
2.7
2.6
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
2.5
7.0
MISSED
7.5
6.0
5.7
5.4
5.2
5.2
5.0
5.0
4.5
4.7
4.7
4.7
4.5
5. I
5.0
5. 1
5.2
5.0
5. 1
5.2
5.6
5.6
5.5
5.7
9.3
DATA READING
8.6
8.8
9.0
9.5
9.7
10.0
10.2
10.2
10.5
10.7
10.7
10.7
10.9
10.9
11.1
11.1
10.9
10.8
10.9
10.9
10.6
10.6
10.7
10.2
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1.00
1 .00
1 .00
1 .00
7. 7
6.2
8.0
7.7
R.3
8.8
8.3
8.3
8.3
9. 1
8.7
9. 1
9.2
9.5
9.7
9.5
9.2
9.2
9.2
9.2
9.2
9.5
9. 5
10.5
10.0
- 418 -
-------
APPFNDIX G: TABLE III.
RUN 9! PRESSURES PAGE 1? Of \6
DAY. HOUR
23. 1030
23. 1 130
23. 230
23. 330
23. 430
23. 530
23. 630
23. 1730
23. 1830
23. 1930
23.2030
23.2130
23.2230
23.2330
24. 0030
24.01 30
24.0230
?/i.0330
p 4. 04 30
24*0530
24.0630
24.0730
P4. 08 30
24.0930
24. 1030
24. 1 130
24. I 230
24. 1 330
p 4. 1 430
24. 1 530
24. 1 630
24. 1 730
24. 1830
24. 1930
24.2030
24.2130
24.223'!
24.2330
25.0030
25.0130
GASIFI
GAS
SPACE
2.7
2.9
2.9
2.9
2.9
2.9
2.9
3.0
3. 1
3. 1
2.6
2.7
2.7
2.7
2.9
3.2
3.2
3.4
3.2
3.0
3.2
3.2
3-4
3.5
3.6
3.6
3.6
3.6
3.7
3.7
3.7
3.7
3.7
3.7
3. 7
3.7
3.7
3.9
3.7
3.7
ER P. KILOPASCALS GASIFI ER REGEN
DISTRIB. BED BED BFn
D.P.
5.4
5.8
5.8
6. 1
6.5
6. 1
6.3
6.5
7.0
7.7
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
D.P. SP. GR. D.P.
10
10
10
9
9
9
10
10
9
8
9
9
9
9 .
.0
.2
.2
.7
. 5
• 8
. 1
.0
.0
.7
. 3
. 5 I
.6 1
. 7 t
10.1 1
10. 1 1
10L ..
. 2 1
10.3 1
10.3 1
10.3 1
10.2 1
10. 1 1
10.
10.
0.
0.
0.
0.
0 . ,
0 1
1 l
3 1
7 1
8 1
9 1
9 i
1.1 1
• 1 1
.2
.2
.2
1 .2
1 .4
1.3 1
1.1 1 .
1.1 1 .
1.2 1.
1 .00 9.5
1 » 00 9*5
| . I / • r ,
. 00 6.2
• 00 5.7
. 00 5.5
m (TtfTi £. _ r*
. » .' V/ O • VI
• 20 7 . PI
• £1, v J 1 • v J
.30 7.5
.PS R . S
9 ri <~J O • VJ
.25 7.5
.00 8 . i"
. i?lf?l 7 . Pi
. / ' i ' i • fi
.00 8.0
.00 7.0
.00 6.7
. n rx (. c
• V ' •• O . J
.00 6*0
.00 8.0
.00 7 . c;
• Y 1 \ ' i • O
.00 9.3
.00 8.7
.00 8.7
.00 9.3
- nc\ a c:
. \ ! V J s * -J
.00 9.7
.00 9«8
.00 10.0
.00 10.0
.00 10.2
.00 10.5
.00 10.6
.00 10.6
.00 10.7
00 10.9
00 11.2
- 419 -
-------
APPENDIX G : TABLE
RUN 9: PRESSURES
III
PAGE 13 OF 16
DAY. HOUR
25.0230
25.0330
25.0430
25.0530
25.0630
25.0730
25.0830
SHUT
25. 1430
25. 1 530
SH LIT
25.2230
25.2330
26.0030
26.0130
26.0230
26.0330
26.0430
26.0530
26.0630
26.0730
26.0830
SHUT
26.P230
26.2330
27.0030
27.0130
27.0230
27.0330
27.0430
27.0530
GASIFI
GAS
SPACE
3.9
3.7
3.7
3.9
4.0
4.2
4.4
DOWN AT
4.7
5.2
DOWN AT
3.5
3.5
3.2
3.4
3.4
3.4
3.4
3.4
3.4
3.4
3.5
DOWN AT
2.7
2.7
3.7
3.6
3.6
3.6
3.6
3.9
ER P. KILOPASCALS GASIFIER
DISTRIB. BED BED
D.P.
0.
0.
0.
0.
0.
0.
0.
25.0830 FOR
0.
0.
85.1530 FOR
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
26.0830 FOR
3.1
3.1
3. 1
3.2
3. 1
3. 1
3.0
3.2
D.P. SP. GR.
1 1 .6
1 1 .7
1 1.9
1 1 .8
1 1 .8
1 1.8
11.7
6 HOURS
1 1 .8
1 1 .4
7 HOURS
10.7
10.7
10.6
10.6
10.7
10.8
10.8
10.8
10.8
10.9
10.9
14 HOURS
9.2
9.2
10.2
10.5
10.5
10.7
10.8
10.9
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
.00
.00
.00
.00
.00
.00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
1 .00
RE GEN.
BED
D.P.
1 .3
1 .6
1 .4
1 .7
1 .4
1 .4
1 .7
12.2
11.2
9.5
9.2
9.2
10.0
10.7
10.7
1 1 .2
1 1 .9
11.7
1 1 .7
11.4
9.0
9.0
7.5
7.2
7.5
7.7
8.2
8.7
- 420 -
-------
APPENDIX G: TABLE I II
RUN 9: PRESSURES
PAGE 14 OF 16
OASIFIER P. KILOPASCALS GASIFIFR
DAY. HOUR
? 7. 06 30
P 7. 07 30
27.0830
P7.0930
?7. 1030
?7. 11 30
P7. P30
P7. 330
27. 430
P7. 530
?7. 630
?7. 730
?7. 830
P7. 930
P7.P030
P7.P1 30
P7. PP30
P7.P330
P8 .O030
P8.01 30
PR. OP 30
P8.0330
P8.0430
PR. 05 30
P8 .0630
PR. 07 30
PR. 08 30
P8 .0930
P8. 1030
PR . 1 1 30
PR. P30
PR. 330
P8 . 430
PR. 530
PR. 630
PR. 730
PR. 830
PR. 930
PR .P030
PR .PI 30
GAS
SPACE
3.9
4.0
4.0
4.0
4 . 0
4.2
4.P
4.P
4.P
4.5
4. 5
4. 5
4.5
4. 5
4. 7
4.7
4.7
4.7
5.0
4.9
4.7
4.7
4.7
4. 7
4.9
5.0
5.0
5.0
4.9
5. 1
5.2
5.6
6.0
6.0
6.3
5.7
5.P
5. 5
5.6
5.5
DI STRIB.
D.P.
3. 1
3. 1
3. 1
3.4
3.4
3-6
3.6
3.6
3.5
3. 5
3.6
3-6
3.7
3.6
3.5
3.P
3.P
3.P
3.P
3.P
3.P
P. 9
?. 7
3.0
3. 1
3. 1
2.7
P. 7
P. 6
P. 7
2. 7
P. 5
p.o
P.0
2.0
2. 1
1 .9
P. 2
2.4
0.
BED RED
D.P. SP. GR.
11.1 1 .00
10.9
10.7
10.7
10.8
10.7
10.7
10.5
10.6
10.8
10. R
10.9
10.8
10.8
10.8
11.1
1 1 .2
1 1 .P
10.9
I .00
1 .00
I .00
I .00
1 .00
1 .00
.00
I .00
I .00
1 .00
.00
1 .00
.00
[ .00
[ .00
.00
.00
.00
10.9 1 .00
1 1 .P 1 .00
1 .P 1 .00
1 .4 1.00
1.4 1.00
.3 1 .00
.4 1 .00
.4 1 .00
.6 1 . 00
.7 1 .00
. 7 1 .00
1.7 1 .00
1.7 1 .00
P. 1 1 .00
IP. 1 1 .00
11.6 1 .00
11.7 1 .00
11.6 1 .00
11.1 1 .00
10.9 1 .00
10.2 1 .OP
REGEN.
BED
D.P.
R.7
R.P
7.5
7. 5
R. 1
R.5
R.7
R.7
9. 5
9.5
9. 5
9. 5
10.6
10.5
10. 5
10.5
1 0 . 5
10. R
1 .?
1 .P
1 .P
1 .4
1 .6
1 .7
1 .7
1 1 .R
1 1 .8
1 1 .9
1 1 .9
1P.P
1 1 .9
IP. 1
11.7
11.7
11.4
11.4
10.2
12. P
11.?
11.?
- 421 -
-------
APPENDIX Gs TABLE III.
RUN 9: PRESSURES PAGE 1 5 OF 16
GASIFIER P. KILOPASCALS GASIFIER
DAY. HOUR
PR . PP3F-
SHUT
P9.P330
30.0030
30.01 30
30 .0230
30.0330
30.0430
30.0530
30.0630
30.0730
30.0830
30.0930
30. 030
30 • 1 30
30. P30
30. 330
30. 430
30. 530
30. 630
30. 730
30 • R 30
30. 930
30.P.030
30. PI 30
30.2230
30.2330
31 .0030
31.0130
31 .0P30
31 .0330
31 .0430
31 .0530
31 .0630
31 .0730
31 .0830
31.09 30
GAS
SPACE
5.0
DOWN AT
3.2
3.5
3.7
4. 1
3.6
3.0
P. 7
2.6
2.5
P. 5
2.5
2.6
2.6
2.6
2.6
2.7
2.7
2.9
3. 1
3.0
3.7
3.7
3.7
3.7
3.7
4.2
4.6
4.0
3.6
3.7
3.6
3.7
3.7
DISTRI
D.P.
0.
28.2230
3.5
4. 1
4. 7
MI SSED
MISSED
5.2
5.0
2.5
2.2
2.0
2.0
2.0
2.
2.
2.
2.
2.
2.
2.
2. 1
19.9
2.0
2.5
3. 1
3.0
2.9
2.9
3.1
3.4
P. 4
2.4
2.5
2.5
2.4
2.4
B. BED BED
D.P. SP. GP.
10.2 1 .00
FOR 24 HOURS
7.1 1 .00
7.P 1 .00
7.5 1.00
DATA READING
DATA READING
7.2 1.00
7.5
7.6
8. 1
8.3
8.5
8.5
8.5
8.5
8.5
8.3
8. 1
8.0
7.8
7.5
7.1
7. 1
7.0
7.1
7. 1
7.0
7.3
7.3
7.5
7.7
7.6
7.7
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
. 00
.00
.00
8.0 1 .00
8.0 1 .00
8.0 1.00
RE GEN
RED
D.P.
1 1.?
8. 1
R. 5
8.5
9.0
8.7
8. 1
8. 1
8. 1
R.7
8.7
R.7
8.7
9.0
R.7
R. 5
R.P
R.P
8. 1
7.7
7.7
8.2
7. 5
8.0
8.0
8.P
9.0
9.P
6.7
7.7
8.2
R.0
8. 1
8. 1
- 422 -
-------
APPENDIX G. TABLE III.
RUN 9: PRESSURES PAGE 16 OF 16
DAY. HOUR
31 • 030
31. 130
31. 230
31. 330
31. 43(7'
31. 530
31. 63r-!
31. 730
31. 830
31. 930
31 .2030
31 .2130
31 .2230
31 .2330
32.0030
32.0130
32.0230
32.0330
32.0430
32.0530
32.0630
32.0730
32.0830
GASIFIE
GAS
SPACE
3.7
4. 1
4.2
3.9
3-9
5.6
5.5
5.7
5.5
5. 1
5.2
4.6
4.2
4. 1
4.4
4.6
5.0
5.6
5.8
6. 1
6.0
5.R
6.0
:R P. KI
DISTRI
D.P.
2.4
2.4
2.4
2.4
2.4
3.6
4. 4
4.7
4.6
3.7
STONE
3.5
3.5
3.0
2.9
2.9
2.9
2.7
2.7
2. 7
2.6
2.5
2.4
2.5
LOPASCALS
B. BED
D.P.
R. 1
7.8
7.8
7.8
8.7
8.6
8.2
7.8
8.0
7.8
CHANGE
8. 1
8.6
8.7
8.6
8.5
8.2
8.6
8.6
8.7
8.7
8.6
8.6
8.6
GASIFIER
BED
SP. GR.
. 00
.00
.00
.00
.00
.00
.00
.00
.00
.00
1 .00
1 .00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
.00
RE GEN.
BED
D.P.
8.2
8.5
8. 5
8.2
9 .P
10.9
10.9
10.7
10.2
9.5
10.0
10.0
9.3
9. 5
9.3
9.5
6.6
8. 1
8. 1
8.3
8.6
8.6
8.6
- 423 -
-------
APPENDIX Bl: TABLE IV.
RUN 9: DESULPIIURISATION PERFORMANCE PAGE
I OF 16
2,
2,
2,
2,
?,
2,
2,
2,
2,
2,
2,
2
2,
2,
2,
2,
2,
2,
2,
2,
2,
0230
43330
0430
0530
0630
0730
0830
0930
1030
1 130
1230
1330
1430
1530
1630
1730
1830
1930
2030
2130
2230
2.2330
4.0430
4.0530
4.0630
4.0730
4.0830
4.0930
4.1030
SULPHUR GAS
REMOVAL VEL.
% M/S
86.5 1.37
85.4 1.2b
87.6 1.25
SMUT DOWN AT 1.
55.4
59. 1
59.6
73.7
75.4
74.7
-
-
65.9
65.8
65.0
63.3
61 .0
56.5
64.9
67.7
69.2
71 .0
70.8
71.2
70.8
67.2
.51
.62
.62
.56
.54
.54
.54
.45
.53
.53
.45
.40
. 17
.28
.29
.37
.44
.42
.39
.50
.42
.42
SHUT DOWN AT 2.
.51
.56
36.6 .48
79.2 .72
80 . 3 - 65
81.7 .6b
(5- RED AIR/ CA.O/S
DEPTH FUEL RATIO 5
CENTIM % ST.
58.
58.
58.
2130
53.
55.
57.
60.
62.
65.
63.
64.
63.
66.
66.
67.
67.
68.
69.
72.
73.
73.
78.
78.
77.
77.
2330
80.
82.
85.
87.
88.
90.
18.5
16.9
16.9
FOR 4
22.8
21.6
25. 1
16.9
21.4
20.2
19.2
17.9
18.3
17.4
18. 1
18.1
15.8
17.4
17.4
18.7
19.8
19.3
19.5
21.0
19.2
19.4
FOR 28
18.7
19.8
19.7
24.0
22.8
23.8
REGEN.
6 CAS S OUT %
MOL. TO CAO
0. 17
0.16
0.32
HOURS
0.
1.29
2.29
1.46
1 .70
1 .83
0.25
0. 19
0.21
0.23
0.23
0.29
0.28
0.81
0.76
1 .65
1. 13
0.77
2.01
0.85
0.71
0.88
HOURS
0.27
0.91
1 .42
2.24
1 .18
2.16
25.5
45.6
—
16.8
20.2
34.1
35.1
33.0
30.8
36.7
62.6
67.2
62.1
63.8
62.3
61.0
70.4
59.4
55.9
55.1
56.4
51 .5
62.5
60.6
56.0
_
52.2
57.7
56.3
56.3
52.5
OF FED
21.0
29.9
0.
16.9
19. 1
28.5
29.2
27.0
24.4
30.6
57.3
60.7
52.6
53.2
53.8
57.7
53.1
50.2
50.5
57.7
58.3
60.5
62. 1
65.7
64.6
7.5
56.7
67.3
66.3
64.6
57.8
MISSED DATA READING
- 424 -
-------
IvlJN 9:
APPENDIX &;* TABLE IV.
DF5ULPHURISATION PEHFOHMANCE PAGE
2 OF 16
DAY. HOUR
4. 1230
4. 1330
4. 1/130
1. 1530
4 . 1 630
4 . 1 730
4 . 1 830
4 . 1 930
4 . ?030
4.? 130
4.2230
4.2330
5.0030
5.0130
5.0230
5.0330
5.0430
5.0530
5.0630
5.0730
^.0830
5.0930
5. 1030
5. 130
5. 230
5. 330
5. 430
5. 530
5. 630
5. 730
5 . 1 830
5. 1930
5.2030
5 . 2 1 30
5.2230
5.2330
6.0030
6.0130
6.0230
6.0330
SULPHUR
REMOVAL
%
74.5
71.9
73.4
75.8
71.2
68.8
69.7
73.9
73.4
75.3
76. 0
77.3
76.4
74.5
72.7
74.7
79.5
HI. 1
77.2
80 . 0
80.5
81 . 1
82. 1
82.2
82.4
81.9
77.8
79.4
80 . 6
81 .4
76.2
74.9
76.8
80.8
79. 1
80.7
83.2
82. 1
82.3
82.2
GAS
VEL.
M/S
1 .06
2.03
2.03
2.416
2.22
2 . 2r,
2.^9
2.01
1 . ^8
2.03
2.1 1
2.. 1 1
2. 14
2.14
2. 14
2.09
2.07
2.07
1 .93
1 .95
1 . 93
1 .93
2.01
2 . B 1
2.03
2. 1 1
2.29
2.22
2 . 2v)
2.17
2.20
2.20
2.17
2. 12
2. Ib
2. Ib
2.17
2. 18
2. Id
2. 18
G-RED
DEPTH
CENTIM
87.
88.
84.
88.
86.
90.
84.
94.
92.
93.
93.
100.
91.
98.
91 .
91.
95.
95.
96.
99.
09.
103.
101.
102.
100.
102.
96.
93.
96.
99.
93.
99.
100.
99.
100.
99.
99.
09.
99.
99.
AIR/
FUEL
% ST.
26.8
28.8
28.4
27.2
27.9
27.9
28.5
26.8
26.9
27.6
29.5
29.0
29.5
30. I
31.2
29.7
30.4
30.3
28.9
28.7
29.8
28.8
29. 1
29.2
30.2
30.3
31.3
30.0
30. 1
30.3
30.0
30. 1
29.8
28.8
31 .8
31.2
31.2
31.3
31.3
31.0
CAO/S
RATIO
MOL .
0.93
1.21
1.43
0.52
0.30
0.45
1 .87
2.66
2.78
1.92
0.76
2.50
1.17
2. 10
1.55
.52
2.15
0.98
2.44
1.75
.65
1 .98
1 .24
1 .99
1 .94
2. 10
2. 1 1
.31
.43
.73
.01
.65
2.61
3.60
3. 10
1.54
3.57
2.73
3.27
3.31
% CAS
TO CAO
_
-
—
51 .6
54.3
53.2
49.2
47.9
49. 1
53.4
51.6
52.6
53.9
57. 1
58.5
55.2
50.0
49.0
47.4
48.6
48.7
50.8
49.0
47.4
49.6
58. 1
53.5
54.2
53.7
49.4
49.7
49.2
45.7
51 .6
50.7
50.3
45.6
45.6
45.8
42.9
REOEN.
S OUT %
OF FFD
0.
0.
0.
76.2
72.6
65 . 0
62.7
61 .4
54.5
60.3
65.0
54.2
60.7
67.6
71.0
64.5
58.7
63.6
48.3
55.4
53. S
54.0
51.9
51.3
63.7
76 . 6
73. A
73.3
71.5
61 .5
61.8
61.0
52.9
55.5
65.6
66.6
61.4
60.7
60 . 9
56.7
- 425 -
-------
RUN 9»
APPENDIX AS TAPLF IV.
OESULP1IURISATION PERFORMANCE PAGE
3 OF 16
DAY.HOUR
6.0430
6.0530
6.0630
6.0730
6.08 30
6.0930
6. 10 30
1 130
1230
1330
6.1430
6. 1530
6. 16 30
6.1730
6.1830
6.1930
6.2030
6,
6,
6,
7,
7,
7,
7,
7,
7,
7.
7,
7.
7.
7,
7,
7,
7,
7,
I i
7,
7,
0130
02 30
0330
0430
0530
0630
0730
0830
0930
1030
1 1 30
1230
1330
1430
1530
1630
1730
I 8 30
7.1930
SULPHUR
REMOVAL
*
82.4
83.5
85.2
86.7
85.9
87.4
-
79.4
81 .8
84. 1
83.8
84.9
85.9
o3.8
84.0
80.6
78.5
SHUT DOWN
_
77.7
80.5
75.8
76. 1
79.4
79.5
78.8
79.6
78.5
78.9
77.3
76.5
77.6
76.4
78. 1
85.3
86.0
87.0
GAS
VEL.
M/S
2.09
2.1 1
2.09
2.12
2.1 1
2.20
2.20
2.1 1
2.09
2. 14
2.2t)
2.04
2.04
2.04
2.01
1 .75
1 . rt 7
AT 6.
1 .34
. 75
1 . Y6
.d3
.73
.67
.59
.65
.65
.53
.59
.59
.59
. 5b
.61
. <">2
.53
.01
1 .59
G-PED
DEPTH
AIR/ CAO/S RFGEN
FUFL RATIO % CAS S OUT
CENTIM % ST.
99.
95.
96.
93.
87.
92.
91.
90.
90.
87.
89.
90.
82.
82.
82.
80.
77.
2030
71.
78.
82.
82.
83.
83.
83.
83.
85.
85.
86.
86.
87.
88.
90.
96.
102.
109.
111.
30.9
30.9
30.4
31.5
30.9
32. 1
32. 1
30.2
30.6
29.2
31.8
28.6
28.9
27. 1
28.2
26.5
26.9
FOR 4
20.8
25.7
26.0
26.8
25.9
24.9
23.9
24.9
24.0
23.6
24.2
23.6
24.2
23.8
24.0
25. 1
25.3
26.7
27.2
MOL. TO CAO
3.4?
3.79
3.99
3.79
4.51
3.5?
3.83
3.1 1
5.13
3.65
4.24
2.55
1.87
2.62
1 .83
0.
0.
HOURS
0.
0.06
0.83
0.89
1.33
0.89
0.89
1 .24
1 .01
0.49
0.38
0.41
0.90
1 .20
5.23
3.96
3.92
3.47
2.36
41 .7
41.7
41.7
42.6
41 .6
50.2
44.2
39.5
39.7
43.3
42.2
36.4
48.0
-
-
-
—
78.7
67.7
50.9
58.2
55.2
57.2
55.2
56.6
63.4
63.0
64.7
60.9
58.7
60.4
57.3
62.9
64.0
66.7
75.4
OF FEf
54.6
56.6
57.3
59.6
57.4
71.7
63.4
58.3
59.0
64.5
71.2
49.8
62.2
0.
0.
0.
0.
55.6
85.2
66.3
84.5
74.4
73.5
69.7
68.2
69.6
65.2
63. 1
61 . 1
59.9
57.2
42.5
56.6
50.6
57.4
65.9
- 426 -
-------
RUN 9!
APPFNDIX G< TABLF IV.
DFSULPHURISATION PERFORMANCE PAGE
4 OF 16
PAY. HOUR
7.2030
7.2130
7.2230
7.2330
8.0030
8.0130
8.0230
8.0330
8.0430
8.0530
8.0630
8.0730
8.0830
8.0930
8. 1030
8. 1 130
8. 1230
8. 1330
8. 1430
8. 1530
8. 1630
8. 1730
8. 1830
8. 1930
8.2030
8.2130
SULPHUR HAS G-RED
REMOVAL VEL. DEPTH
% M/S CENTIM
-
-
92.5
88.4
88.4
88 • 8
88.9
88.3
88.6
88. 3
88.3
87.7
86.6
87.2
87.2
88.0
—
88.0
89. 1
88.8
86.0
87. 1
88. 1
88. 1
91.2
92.6
.62 114.
.72 109.
.73 109. .
.67
.67
.67
.67
.65
.07
.65
.65
.72
. /2
.72
. 12
.68
. 70
.70
.68
.58
.58
.72
.64
.70
.70
.64
109.
09.
109.
109.
1 1.
1 10.
1 10.
10.
10.
1 1.
14.
14.
15.
15.
15.
18.
18.
20.
18.
19.
18.
18.
18.
AIR/ CAO/S
FUEL RATIO
% ST. MOL.
27.7 5.31
27.6
28.3
28. 1
27.3
27.6
26.6
26.3
26.3
26.3
26.3
26.7
27.5
26.7
26.5
.45
1.45
1.53
.60
1 .36
.25
.47
1 .00
.07
.30
.27
.52
.01
.20
27.8 2.11
28.6 2.03
25.5 .68
26.8 .97
25.0 .35
25.1 .66
27.1 .29
25.6 .69
27.4 .71
26.9 .31
25.9 .55
% CAS
TO CAO
56. 1
56.6
57.5
55.8
55.7
56.3
56.6
57.5
57.8
58.0
57.9
56.9
52.9
54.7
53.7
54.8
53.2
52.7
54.4
62.3
46. 1
64. 1
58.9
60.5
59.9
58.5
REGFN.
S OUT %
OF FED
47.4
95.4
96.7
91.8
90 . 7
84.0
81 .4
80.3
81 .3
79.0
80 . 0
98.0
79. 1
81.3
76. /
82.4
84.8
74.2
80.5
83.4
41.7
81.4
62.7
76.7
78.4
77.4
SHUT DOWN AT 8.2130 FOR 8 HOURS
9.0630
9.0730
9.0830
9. 09 30
9. 1030
9. 1 1 30
9. 1230
9. 1330
9. M30
9. 1530
82.5
83.3
83. 1
84.2
86.0
65.8
-
85.8
85.9
86. 1
.64
.59
.75
.72
. /2
.72
.73
.73
. /3
.72
122.
124.
111.
109.
109.
111.
1 10.
1 10.
106.
104.
25.7
24.7
26.6
26.7
26.7
26.7
26.7
26.5
26.8
26.6
0.76
0.79
0.53
1 .02
1 .58
0.99
0.99
1.37
1 .62
2.20
49.8
51 .0
64.4
65.4
58.4
60 . 0
58.7
59.0
59.6
57.6
76. 1
81 .4
75. V
75.7
81 .5
80.7
72.8
75. 1
81.2
77.5
- 427 -
-------
APPENDIX G. TABLE IV.
HUN 9: DESULPHURISATION PERFORMANCE PAGE
5 OF 16
DAY.HOUR
V.1630
9.1730
9.1830
9.1930
9.2030
10.0230
10.0330
10.0430
10.05 30
10.0630
10.0730
10.0830
10.0930
10. 1030
1 130
1230
1330
1430
1 5 30
1 630
1730
1830
10.1930
lvi.2030
10. 2 1 30
10.2230
10.2330
.0030
.0130
.0230
.0330
.0430
.0530
.0630
.0730
.0830
10
10
10
10
10
10
1(7
10
SULPHUR GAS G-BED
REMOVAL VEL. DEPTH
* M/S CENTI
85.2 1.73 106.
86.4 1.73 106.
87.1 1.V2 ]07.
87.4 1.72 109.
87.5 1.72 HI.
SHUT DOWN AT 9.2030
_
84.9
82.3
84.4
86.4
87.0
87.2
87.5
87.7
88.2
86.2
86.3
86.3
86. 1
86.2
86.0
86.0
86. 1
85.5
85.6
b5.8
85.2
85.5
85.2
85.6
—
84.3
82.8
81 .0
.59 111.
.62 111.
.67 111.
.72 113.
.65 115.
.65 15.
.65 15.
./3 18.
.72 16.
.65 16.
.65 16.
.65 16.
.65 16.
.65 16.
.65 16.
.04 19.
.65 16.
.65 16.
.59 16.
.59 19.
.22 19.
.65 19.
.64 119.
.59 116.
.65 114.
.07 14.
3.36 111.
.59 114.
.61 115.
80.2 1.-59 19.
82.5 1.67 118.
_
AIR/
FUEL
M % ST.
26.6
27.3
27.6
27.6
25.0
FOR 5
25.7
25.0
26. 1
27.1
26.0
25.9
26.0
26.8
27.5
26. 1
26.2
25.8
26.3
25.6
26.3
26.4
25.2
26.2
25.0
24.3
25.2
26.2
26.2
25.3
26.1
26. 1
37. 1
25.3
25. 1
25.2
26.3
428 -
CAO/S
RATIO
MOL.
.70
. 14
.63
.77
.42
HOURS
0.46
0.50
0.63
1.30
2.02
0.86
1 .82
1 .25
1.32
1 .33
1 .30
1.12
1.31
1 .05
1.14
1.42
1.16
0.84
0.73
1 .36
1 .03
1 . 10
1.83
.24
1.06
1 .00
1.16
.04
0.77
2.04
1.07
% CAS
TO CAO
57.3
56.2
55.0
56.?
55.6
_
58.3
69.0
61 .7
59.0
61 .4
60.6
53.8
60.6
56.4
59.4
62.3
65.5
60. 1
60.7
61 .6
64.0
66.2
66.5
64.?
64.4
59.4
58.7
59.2
67 . 0
69.3
72. 1
90.9
41 .5
63.4
51 .6
REGEN.
S OUT J
OF FEP
80.4
79.6
73. 1
75.2
70.9
0.
71 .4
71 .2
74. 1
77.6
82.0
78.7
54. 1
54.3
83.5
82.5
87.5
86.4
74.0
81.4
81 . 1
83.7
86.0
83.9
79. 1
81 . 1
83.2
80.9
81.7
82.2
77.8
83.6
80.3
36.2
56.0
43.6
-------
APPENDIX G.: TABLE IV.
RUN 9: DESULPHURISATION PERFORMANCE PAOE
6 OF 16
DAY. HOUR
1 .0930
. 1030
. 1 1 30
. 1230
. 1330
.1430
.1530
.1630
. 1730
. 1830
1 . 1 930
1.2030
1 1 .?130
1 1 .2? 30
1 1.2330
12.0030
12.0130
12.0230
12.0330
12.0430
12.0530
12.0630
12.0730
12.0830
12.0930
12. 1030
12. 1 130
12. 1230
12. 330
12. 4 30
12. 530
12. 630
12. 730
12. 1830
12. 1930
12.2030
12.2130
12.2230
12.2330
13.0030
SULPHUR GAS 0-BED
REMOVAL VEL. DEPTH
% M/S CENTIM
84.5
85. 1
86.2
86. 1
86. 1
85.6
86.3
84.7
83.9
83.6
84.5
85.8
85.7
85.4
85.4
83.9
85.7
85.4
84.6
83.4
82.4
85.7
87.7
1
1
85.5
86.0
85.5
84.8
84.6
84. 1
84. 1
84. 1
83.7
83.4
83.9
82.4
81 . 1
80.2
80.0
.67 116.
.65 115.
.65 114.
.65 111.
.65 113.
.65 115.
.65 116.
.51 116.
.51 118.
.51 116.
.51 116.
.64 116.
.65 116.
.72 116.
.75 111.
.47 111.
.47 118.
.47 118.
.40 119.
.40 119.
.48 119.
.4b 119.
.48
.54
.54
.54
.56
.56
.61
.53
.53
.53
.53 1
.53 1
.53 1
.53 1
.53 1
.53 1
.53 1
.51 1
1 19.
1 18.
1 19.
1 18.
1 19.
18.
19.
20.
20.
20.
20.
19.
19.
19.
19.
19.
20.
20.
AIR/
FUEL
% ST.
26.0
26. 1
25.9
25.9
25.8
26.6
26.0
24.5
24.5
23.9
23.8
25.8
26.8
26.8
27.2
24.0
25.9
26.6
24.7
24.8
25.9
25.9
25.9
27.0
27.0
27.0
27.2
26.7
27.6
25.9
25.8
25.6
25.7
25.6
25.5
25.5
25.3
25.5
25.8
25.3
CAO/S
RATIO
MOL.
1 .56
1.20
1 .40
1 .33
0.99
.26
.20
.23
.51
.20
.29
.29
.31
.00
0.73
1.31
.79
.23
.26
.27
.15
.04
0.86
0.78
0.89
0.86
0.49
0.29
0.59
0.58
0.58
0.57
0.43
0.36
0.32
0. 14
0.04
0.57
0.54
0.64
% CAS
TO CAO
65.9
71 .6
77.2
70.4
66.9
69.0
62.0
67.3
64.9
57.3
59. 1
57.3
55.0
57.2
57.7
58 . 7
64. 8
64.5
73.9
50 . 8
53.9
79.6
71 .4
69.0
65.9
64.3
65.3
65.8
58.2
58.9
60.8
63. 1
63.6
61 .8
62.6
62.9
63.4
61.1
62.2
61 .9
REOEN.
5 OUT %
OF FED
64.9
90.8
99. 1
^ ^ • (
91 . 3
97.7
75. 7
77. 7
79. 1
1 s * I
72.7
i f • /
66.?
68. 4
73.0
69.0
\-J 7 * \.J
71.3
73.5
75.3
82. 6
\^ C~ • W
78. 7
78. 3
39.8
42.7
64. 9
85.3
87. 1
v. ' f • t
84. 0
83.?
81 .?
*--/ 1 • ^ _
94 . 3
94. 9
86. 9
83. 5
76. 4
75.7
75.5
I _ / • '
74. 6
74 . f)
78.2
75 1
* _ ' • 1
74.2
72.6
- 429 -
-------
RUN 9:
APPFNDIX G* TABLE IV.
DESULPIIURISATION PERFORMANCE PAGE
7 OF 16
DAY. HOUR
13.0130
13.0230
13.0330
13.0430
1 3.0530
1 3.0630
13.0730
13.0830
13.0930
13. 1030
13. 1 130
SULPHUR GAS
REMOVAL VEL.
% M/S
80 . 1 1 . 43
80.4 1.53
79.6
79. 1
78.4
75.8
75.5
77.5
77.3
77.2
77. 1
.53
.51
.51
.53
.59
.54
.48
.48
.48
G-RED
DEPTH
CENTIM
120.
121 .
121.
123.
123.
123.
120.
120.
1 19.
120.
1 19.
AIR/
FUEL
% ST.
25.6
25.7
25.7
25.2
25.4
25.5
27.4
26. 1
24.3
25.0
25.5
CAO/S REGEN.
RATIO % CAS S OUT %
MOL. TO CAO
0.39
0.83
0. 14
0.53
0.46
0.43
0.37
0.39
0.35
0.29
0.55
63.5
66.0
66.5
44.5
42.9
38 . 1
67.?
47.9
45.0
66.4
67.7
OF FED
67.7
65.0
65.2
34.2
3G . 0
33.6
73.5
44.6
29.8
75.9
96.2
SHUT DOWN AT 13.1130 FOR 13 HOURS
14.0130
14.0230
14.0330
14.0430
14.0530
14.0630
14.0730
14.0830
M.0930
14. 1030
1 4 . 11 30
14. 1230
14. 1330
14. 1430
14. 1530
14. 1630
14. 1730
14. 1830
14.1 930
14.2030
14.2130
14.2230
14.2330
15.0030
15.0130
71 .9
75.5
77.4
78.0
77.7
79.6
78.3
76.4
77.8
78.7
80.2
81.3
80.6
78.5
78.3
78.0
78.0
77.2
79.2
80.3
81 .0
—
79. 1
77.9
78.4
.53
.51
.50
.51
.51
./14
.'14
.51
.53
.53
.54
.70
.70
.64
.62
.61
.59
.53
.89
. /3
.72
.72
.72
.87
.67
102.
105.
107.
1 10.
111.
1 13.
15.
19.
18.
23.
20.
15.
111.
111.
1 13.
1 13.
106.
106.
107.
109.
109.
111.
1 10.
1 10.
1 10.
25.4
24.9
27.2
24.7
24.6
24.8
24.5
27.7
27.2
26. 1
26. 1
28.5
28.9
27.8
27.4
26.9
26.4
25.6
25.8
25.5
25.1
25. 1
26.2
28.4
24.9
1.36
1. 16
2.03
0.97
0.80
1.35
1 .44
1.37
0.76
0.44
0.47
0.51
0.63
0.41
0.40
0.47
0.67
0.71
0.73
0.81
0.65
0.68
0.68
0.78
0.75
58.8
62.3
65.3
70.6
61 .5
65.0
51 .8
62.8
43.3
5.0
8.0
38.6
75.9
60.6
61 .5
71.9
66.5
53.4
74.5
64.5
63.0
63. 1
63.5
65.1
64.6
78.2
69.9
67.6
61.6
41.9
40.3
29.6
42.9
23.4
4.4
1 1 .6
40.2
1 15.8
95.8
94.8
91 .8
83. 1
66.2
80.8
81.3
75.7
77.0
82.9
75.8
71 .5
- 430 -
-------
RUN 9:
APPENDIX G; TARLF IV.
DFSULPHUHISATION PERFORMANCE PAGE
8 OF 16
DAY. HOUR
15.02363
15.0330
15.0430
15.0530
15.0630
15.0730
15.0830
15.0930
15. 1030
15. 1 130
15. 1230
15. 1330
15. 1430
15. 1530
15. 1630
SULPHUR GAS G-BED
REMOVAL VEL. DEPTH
M/S CENT I M
78.?
78. 4
79.2
79.2
79.7
73.4
79.8
79.3
79.8
79. 1
79.3
78.4 |
77.1 1
78.7 1
77.9 1
1 . 7H
1 .87
1 . W
1 .9?
.93
.64
.U'f t
.79
.79
.83
.9fa
.64
.56
.64
.56
1.
1.
3.
9.
15.
0.
59.
.
1.
.
1.
.
.
1.
.
AIR/
FUEL
% ST.
26.9
27.9
27.5
27.5
28.2
27.5
26.2
26.0
27.6
27.9
28.3
28.8
27.7
28.8
27.7
CAO/S
RATIO
MOL.
0.74
0.48
0.40
0.36
0.37
0.29
0.60
0.68
0.76
0.51
0.48
0.59
0.48
0.52
0.56
% CAS
TO CAO
66.2
61 .4
59.8
62.6
61 .5
61.8
60.5
56.8
60.9
57.9
54.6
57.0
56.2
60. 1
53.6
REGElM.
S OUT %
OF FFD
74.2
71.8
79.5
67.3
74.6
73.5
66.3
74.6
69.8
77.2
69.6
73.9
73.9
78.3
72.4
SHUT DOWN AT 15.1630 FOR 14 HOURS
16.0730
16.0830
16.0930
16. 1030
16. 1 130
16. 1230
16. 1330
16. 1430
16. 1530
16. 1630
16. 1730
16. 1830
16. 1930
16.2030
16.2130
16.2230
16.2330
17.0030
17.01 30
17.0330
17.0430
75.
76.
77.
80.
80.
-
75.
74.
74.
69.
74.
76.
73.
72.
72.
74.
67.
64.
4
8
6
0
5
7
7
4
8
4
2
6
7
7
0
7
7
1
1
1
1
2
2
2
2
2
1
1
1
2
2
2
2
2
2
.HI
.'Ai
.86
.95
.37
.37
.37
. 36
.37
.56
.59
.53
.34
.23
.22
.25
.26
.25
95.
97.
99.
101 .
102.
102.
101.
100.
101.
MISSED
97.
101.
101.
10).
101.
101 .
101 .
MISSED
MISSED
99.
100.
28.
28.
28.
29.
30.
30.
30.
29.
30.
DATA
26.
26.
29.
29.
28.
29.
29.
DATA
DATA
35.
26.
5
8
9
9
7
3
2
9
0
READI
7
8
0
8
4
0
0
READI
READI
0
0
1.63
1.43
1.52
1 .78
1.11
0.52
0.56
0.44
0.48
NG
0.27
2.25
0.67
0.50
0.50
0.38
0.42
NG
NG
0.64
0.45
63
74
56
73
59
56
54
52
51
5
47
49
47
44
43
45
51
48
.5
. 1
.9
. 1
.5
.4
.8
.7
. 1
.8
.6
. 1
.0
.2
.3
.2
.7
.9
88. 1
86.5
67.7
85.9
88.5
95.6
91.2
87.8
85.5
7.3
69.5
90.3
8^.5
81 .9
77.9
79.8
79.8
53.6
- 431 -
-------
APPENDIX G» TABLE IV.
RUN 9: DESULPHURISATION PERFORMANCE PAGE 9 OF 16
DAY. HOUR
17.0530
17.0630
17.0730
17.0830
17.0930
17. K)30
17. 1 130
17. 1230
17. 1330
17. 1430
17. 1530
17.1 630
17. 1730
17. 1830
17. 1930
17.2030
17.2130
17.2230
17.2330
18.0030
18.0130
18.0230
18.0330
18.0430
18.0530
18.0630
18.0730
18.0830
18.0930
18. 1030
18.1 1 30
18. 1230
18. 1330
18. 1430
18. 1530
18. 1630
18. 1730
18. 1830
18. 1930
18.2030
SULPHUR GAS
REMOVAL VEL.
% M/S
63.6 2.23
68.7 2.25
69.4 2.23
67.8 2.20
68.7 2.25
70.3 2.25
70.3 2.2b
68.4 2.29
70.2 2.26
71.9 2.15
70.4 2.25
66.7 2.3/1
68.2 2.15
76.9
74.2
73.6
70 . 4 ;
70.3
71.8
72.0
71.2
71.3
71.9
-
70.8
71 .4
71.5 ;
72.0
73.8
. 90
.90
.97
. 1 1
.97
.97
.95
.95
.95
.81
.81
.83
.89
.03
.98
.yy
2.03
73.2 2.03
/1. 7 .90
69.8 .65
69.5 .70
70.1 .64
70.2 .59
70.5 .59
69.2 .75
71.6 . 6b
73.6 .66
G-BED
DEPTH
CENTIM
99.
101.
100.
99.
99.
99.
99.
100.
100.
85.
95.
92.
97.
96.
93.
91 .
99.
99.
09.
99.
99.
99.
100.
100.
100.
101 .
101 .
102.
102.
101.
104.
104.
104.
104.
101 .
109.
1 10.
106.
107.
107.
AIR/ CAO/S REGEN.
FUEL RATIO % CAS S OUT %
% ST. MOL. TO CAO OF FED
26.2 0.45 49.3 ^4.6
25.7 0.45 52.2 57.7
25.5 0.38 48.6 51.6
25.9 0.35 51.4 54.3
27.5 0.46 53.6 54.8
26.1 0.50 52.5 47.9
27.7 0.56 49.0 62.2
26.9 0.51 44.2 57.3
27.2 0.39 52.3 68.2
26.9 0.42 52.4 66.1
26.7 0.35 52.4 68.6
27.7 0.29 47.6 62.9
27.6
22.1
21 .9
22.6
26.4
24.5
24.6
24.6
25.7
24.7
23.7
23. 1
?3.0
23.8
26.3
24.7
26.6
26.2
27.4
27.1
20.0
23.2
25. 1
24. 1
24.0
22.0
23.3
28.5
3.54
0.56
0.80
0.44
0.57
0.54
0.54
0.57
0.45
0.44
0.64
0.55
0.49
0.46
0.50
0.46
0.38
0.39
0.53
0.56
0.41
0.32
0.43
0.40
0.46
0.60
0.71
0.88
43.8
59.2
61 .0
62.5
58.0
64.5
68.3
68.3
66.5
74.8
71 .8
71.0
74. 1
60.4
44.9
55.2
54.2
51.2
65.7
57.9
17.2
61 .5
45. 1
42.5
39 . 0
49.9
59. 1
65.9
56.9
60.8
60 . 6
72.5
73.0
66.6
61.0
64.3
59. 1
62.8
58.6
58.0
59.8
41 .6
26.4
36.7
36. 1
31 .2
51 .8
39.8
9.6
46.0
35.4
38.3
37.0
53. 1
74. 1
108.2
- 432 -
-------
APPENDIX G. TABLE IV.
RUN 9: DESULPI1URISATION PERFORMANCE PAGE 10 OF 16
DAY. HOUR
18.2130
18.2230
18.2330
19.0030
19.0130
19.0230
19.0330
19.0430
19.0530
19.0630
19.0730
19.0830
19.0930
19. 1030
19. 1 130
19. 1230
19. 1330
19. 1430
19. 1530
19. 1630
19. 1730
19. 1830
19.1 930
19.2030
19.2130
19.2230
10.2330
20.0030
20 . 0 1 30
20.0230
20.0330
20.0430
20.0530
20.0630
20.0730
20.0830
20.0930
20. 1030
SULPHUR GAS
REMOVAL VEL.
% M/S
76.0 1.75
76.5
72.8
71.5
71.6
71.3
69.9
6b.8
68.3
65.5
64.4
64.4
65.2
—
80.3
79.3
80.8
81.4
83.3
84.7
84.6 1
84.4
85.4
85.7
85.0
.75
.86
. 68
.61
. 70
.76
.79
.78
.78
.79
.81
.83
.67
.65
.59
.61
.58
.65
.64
. 12
.65
.72
.65
.67
83.0 1-73
88.5 1.65
89.1 1.6b
89.5 1 -65
88.4 1.65
88.4 1»67
88.1 1.65
87.7 1.67
87.4 1.67
87.2 1.67
86.7 1.67
86.3 1.61
0-PED
DEPTH
CENTI
106.
105.
104.
101 .
99.
96.
96.
93.
95.
92.
92.
91.
92.
95.
96.
96.
96.
M I SSFD
101.
104.
105.
104.
105.
107.
106.
104.
STONE
105.
106.
107.
109.
109.
109.
107.
106.
106.
105.
STONE
106.
107.
AIR/
FUEL
M % ST.
24.8
26.4
27.5
25. 1
30.6
26.0
25.4
25.9
25.0
25.4
25.5
25.4
26.2
27.9
27.5
28.2
27.4
CAO/S
RATIO % CAS
MOL. TO CAO
0.68
0.47
0.47
0.68
0.93
0.72
0.58
0.40
0.28
0.32
0.43
0.54
1 .09
1 .44
1.46
2. 13
1.27
76.5
71 .3
65.3
64.8
22.5
62.9
58.2
59.7
61 .3
60.3
56.0
57.3
53.9
58.9
56. 1
55. 1
57.5
REGEN.
S OUT %
OF FED
134.3
71.5
85.8
85.2
28.9
87.0
80.3
73.6
75.4
76.7
65. 3
65.4
58.8
66.0
61 .4
58.9
61 .8
DATA READING
27.2
27.9
27.9
29.7
28.7
29.3
27.8
28.0
CHANGE
29. 1
28. 1
27.9
28. 1
28.0
28. 1
28.0
28.0
28.0
28.2
CHANGE
28.2
26.3
2.09
1 .50
2. 10
1 .28
1 .46
2.12
1 .03
1.29
1.74
1 .71
1 .48
1 .20
1.12
0.87
0.47
0.87
0.83
0.87
0.72
0.66
55.0
49.9
46. 1
43.6
45.3
44.2
49.4
51.7
50.5
48.9
49.0
49.5
'51.8
55.4
54.2
58.5
53. 1
54.6
52.0
52.4
65.6
62.3
60.8
60.6
60 . 9
60. 1
65.3
65.5
64.4
62. 1
61 .8
62. 1
62 . 2
63.4
60.5
62.7
62. 1
65.7
63.5
61 .6
- 433 -
-------
APPENDIX 0; TABLE IV.
HUN 9* DESULPHURISATION PERFORMANCE PAGE 11 OF 16
DAY. HOUR
20.
20.
20.
20.
20.
20.
20.
20.
20.
20.
1 130
1230
1330
1430
1530
1630
1730
1830
1930
2030
SULPHUR GAS
REMOVAL VEL.
%
84.
79.
78.
-
80.
79.
R3.
85.
85.
81.
M/S
8
y
8
2
C^j
o
8
A
8
.62
.62
.90
.59
.81
.61
.59
.59
.62
.02
G-BED
DEPTH
CENTIM
104.
100.
99.
100.
99.
99.
99.
99.
99.
90.
AIR/
FUEL
% ST.
27.
27.
28.
26.
27.
27.
27.
27.
27.
27.
2
2
7
7
4
1
1
1
0
0
CAO/S
RATIO S
REGEN.
S CAS S OUT %
MOL. TO CAO
0.62
0.58
0.58
1.42
1.40
1. 15
1.12.
1 .44
0.90
0.
51
48
44
43
43
42
43
42
46
45
.4
.0
.9
.8
.7
.7
.6
.6
.6
.4
OF FF.D
72.4
69. 1
65.7
65. 1
59.1
67.4
51 .2
55.2
63. 1
60.2
SHUT DOWN AT 20.2030 FOR 35 HOURS
22.0830
22.0930
22. 1030
22. 1 130
22. 1230
22. 1330
22. M30
22. 1530
22. 1630
22. 1730
2.2. 1830
22. 1930
22.2030
22.2130
22.2230
22.2330
23.0030
23.01 30
23.0230
23.0330
23.0430
23.0530
23.0630
23.0730
23.0830
23.0930
67.0 ?
76.9 i
82. 1
82.0
81 .9
83.7
82.6
83.3
82.8
82.7
84.4
84.3
83.4
84.2
85. 1
84.9
84.5
83.0
81.0
80.3
78.8
77.3
77.8
79.0
78.9
> . 1 7
?. 15
.84
.78
.72
.68
.70
.70
.68
.58
.51
.53
.53
.54
.56
.64
.64
.65
.73
.73
.67
.62
.70
.62
.70
95.
MISSED
87.
90.
91.
96.
99.
101.
104.
104.
106.
109.
109.
109.
111.
1 1.
13.
13.
1 1.
10.
1 1.
1 1 .
07.
07.
09.
104.
41.3
DATA READ I
33.8
30.2
28. 1
29.7
29.0
26.9
30.3
31.5
25.4
27.3
?7.2
32.4
31.6
32. 1
34.2
34.7
35.0
37.2
37.0
35.6
33.0
34.5
35.5
36.0
5.1 1
NG
3.46
1.87
2. 10
3.16
2.40
.54
.70
.77
.69
.62
.38
.50
.78
.62
1 .94
1.82
1 .46
1.73
1 .82
1 .48
2.07
1 .53
2.86
3.1 1
26.4
34.0
9.4
42.8
43.7
47.8
51 .6
56.9
47.0
53.3
62.6
60.0
54.2
48.9
56.5
50.8
43.9
52.8
49.9
53. 1
46.2
43.5
50.2
65.8
55.4
31.6
48.8
1 1.2
54.9
65. 1
63. 1
66.4
76.2
65.2
63.3
92.8
78.6
76.7
70.5
86. 1
61 .7
60.5
82.5
79.7
84.4
72.9
66.6
75.2
97.3
64.9
- 434 -
-------
RUN 9:
APPFNDIX G. TARLF IV.
DFSULPHURISATION HERFORMANCE PAGE
12 OF 16
DAY. HOUR
23. 1030
23. 1 130
23. 1230
?3. 1330
23. 1430
23. 1530
23. 1630
23. 1730
23. 1830
23. 1930
23.2030
23.2130
23.2230
23.2330
24.0030
24.0130
24.0230
24.0330
24.0430
24.0530
24.0630
24.0730
24.0830
24.0930
24. 1030
24. 1 130
24. 1230
24. 1330
24. 1430
24. 1530
24. 1630
24. 1730
24. 1830
24 . 1 930
24.2030
24.2130
24.2230
24.2330
25.0030
25.01 30
SULPHUR GAS
REMOVAL VEL.
% M/S
78.3
79.6
78.9
79.4
75.0
75.6
77.6
78.0
74.0
72.8
73.4
67.3
64.9
61 .4
63.7
66.6
68.8
.67
.65
.^5
.59
.59
.56
.56
.58
.59
.59
.29
.31
.45
.58
.65
.75
.76
70.1 . 62
71.9 .76
1 . 70
71.2 1.61
73.9 ].61
70 . 2 1.61
70.8 1.59
74.0 .53
78.8 .59
80.6 .59
83. 1 .58
83.2 .59
83.5 .58
83.5 .51
83.4 .51
83.1 .51
82.9 .45
.44
.44
82.5 .58
82.5 .58
83. 1 1 .58
82.4 .^8
G-BED
DEPTH
CENTIM
101.
104.
104.
99.
96.
100.
102.
101 .
91.
88.
95.
80.
75.
79.
82.
102.
104.
105.
105.
105.
104.
102.
101.
102.
105.
109.
1 10.
111.
111.
1 13.
1 13.
1 14.
1 14.
1 14.
1 14.
1 16.
1 15.
1 13.
1 13.
1 14.
AIR/ CAO/S
FUEL RATIO % CAS
% ST. MOL. TO CAO
33.2 2.29 7.5
30.4
25.9
25.8
27.5
25.3
25.4
25.5
25.5
25.5
21.2
22.0
23.5 C
25.7
28.0
.70 40 . 8
.76 55.6
.25 38.7
.33 55.2
.33 49.0
.23 68.9
.20 59.3
. 16 51 .7
.16 43.7
.27 64.1
.21 29.7
5.96 11.0
.07
.15
29.7 0.84
29.8 0.61
27.5 0.72 4.5
29.9 0.61 6.0
30.9 0.62 12.2
30.9 0.65 48.1
30.8 0.51 73.5
30.9 0.65 82.7
30.9
.67 65.0
30.3 2.46 86.0
30.8 2.48 78.9
30.7 2.30 75.6
30.8 2.09 81.1
30.8 2.05 79.5
30.8 2.05 75.5
29.5
29.5
29.5
28.2
28.2
28.4
30.5
30.9
31 . 1
30.7
.84 72.2
.75 70.4
.20 69.7
.32 61.1
.62 50.9
.46 42.6
.35 44.1
.71 68.1
.94 64.7
.53 63.6
REGEN.
S OUT %
OF FFD
7.8
46.9
61.8
39.8
61 .7
55.4
87.0
70 . 7
64.5
58.2
72.0
23. 1
5.6
0.
0.
0.
0.
3.7
3.6
7.4
38.3
78.2
102.6
48.5
107.3
1 16.9
1 13.0
122.9
1 19.7
107.0
107.5
104. 1
103.9
8P.9
72.8
58.2
60.7
102.6
95.8
92.7
- 435 -
-------
RUN 9:
APPENDIX G: TARLF IV.
DESULPHURISATION PERFORMANCF PAGE 13 OF 16
DAY. HOUR
25.0230
25.0330
25.0430
25.0530
25.0630
25.0730
25.0830
SULPHUR GAS
REMOVAL VEL.
% M/S
b2.8
83.8
82.5
82.4
81.1
78.6
.56
.56
.58
,5b
.65
.59
79.9 1.61
G-BED
DEPTH
CENTIM
1 18.
1 19.
121.
120.
120.
120.
1 19.
AIR/
FUEL
% ST.
30.7
31.0
29.8
31.9
29.0
31 .5
31.2
CAO/S
RATIO 5
REGEN.
6 CAS S OUT %
MOL. TO CAO
1 .96
1.68
0.79
0.44
0.37
0.44
0.56
61 .2
31.3
78.7
56.8
76.2
52.4
6.7
OF FED
86.9
37.6
97.6
71.2
85.4
41 .7
7.7
SHUT DOWN AT 25.0830 FOR 6 HOURS
25.1430
25.1530
79.3
75.8
1 .44
1 .44
120.
1 16.
30.5
30.5
0.28
1.01
69.4
66.9
SHUT DOWN AT 25.1530 FOR 7 HOURS
SHUT DOWN AT 26.0830 FOR 14 HOURS
58.8
70.0
25.2230
25.2330
26.0030
26.0130
26.0230
26.0330
26.0430
26.0530
26.0630
26.0730
26.0830
70.6
73.0
73.4
75. 1
75.4
76.8
76.1
75.3
74.9
74.8
74.3
.73 "
.75
.75
.56
.64
.64
.64
.67
.65
.65
.45
109.
109.
107.
107.
109.
1 10.
1 10.
1 10.
1 10.
111.
111.
31.3
31.2
33.0
27.5
29.9
28.5
28.4
31.3
29.2
31. 1
26.6
0.40
0.92
0.88
1 .07
1 .07
1 .06
0.90
0.75
1.13
1.20
0.36
64.1
56. 1
50.9
28.3
31.4
33.2
16.7
76. 1
77.7
74. 1
73.7
71.7
60. 1
61.7
29.3
30.7
30.6
14.4
75.7
76.7
72.9
72.2
26.??30
26.2330
27.0030
27.01 30
27.0230
27.0330
27.0430
27.0530
75.1
79.3
84.5
84.7
84.2
86.9
87.7
88.4
.62
.64
.62
.65
.65
.72
.65
.79
93.
93.
104.
106.
106.
109.
1 10.
111.
31.9
31.2
31.2
31.2
31. 1
32.7
31.5
34.5
4.65
4.43
4. 15
2.03
3.02
2.01
1.77
2.17
36.3
35.7
-
55.6
56.0
53.9
61 .7
53.0
57.4
62.9
0.
99.6
1 14.7
106.8
105.8
99.8
- 436 -
-------
RUN 9:
APPFNDIX G- TABLE IV.
DESULPMURISATION PERFORMANCE PAGE 14 OF 16
DAY. HOUR
27.0630
27.0730
27.0830
27.0930
27. 1030
27.1 130
27. 1230
27. 1330
27. M30
27. 1530
27. 1630
27. 1730
27. 1830
27. 1930
27.2030
27.2130
27.2230
27.2330
28.0030
28.0130
28.0230
28.0330
28.0430
28.0530
28.0630
28.0730
28.0830
28.0930
28. 1030
28. 1 130
28. 1230
28. 1330
28. 1430
28. 1530
28. 1630
28. 1730
28. 1830
28. 1930
28.2030
28.2130
SULPHUR GAS
REMOVAL VEL.
% M/S
88.4
87.8
84.3
83.3
83.6
-
80.4
83. 1
80.2
82.0
85.5
85.6
85. 1
83.7
82.5
80.7
81.8
82.7
81.8
81.5
84.2
85.0
87.5
87.4
86.7
85. 1
85.2
85.7
86.0
86.3
86.3
85.9
84.5
84.0
-
88.7
89.5
89. 1
89. 1
89.8
.75
.76
.65
.64
.50
.51
.51
.45
.45
.58
.58
.58
.58
.58
.50
.44
./<
.58
.58
.56
.48
.36
.47
.42
.42
.50
.42
.42
.42
.40
.42
.47
.44
.47
.48
.48
.42
.44
.50
.44
G-PED
DEPTH
CENTIM
13.
1 1.
09.
09.
10.
09.
09.
06.
07.
10.
10.
1 1.
10.
10.
10.
13.
14.
14.
1 1 .
1 1.
14.
1 14.
1 16.
1 16.
1 15.
1 16.
16.
18.
19.
19.
19.
19.
23.
23.
18.
19.
18.
13.
1 1.
04.
AIR/
FUEL
% ST.
33.6
30.6
30.3
32.5
26.7
28.0
27.9
26.6
26.7
29.3
29.2
29.3
29.2
29.2
28. 1
25.3
26.9
30.4
29. 1
29.5
28.2
25.4
27. 1
27.3
25.6
28.7
28.2
26.4
26.9
26.9
26.9
26.7
26.7
24.8
25.0
24.9
23.8
23.8
24.8
23.5
CAO/S
RATIO ?
£ CAS
MOL. TO CAO
1 .69
0.68
0.64
0.74
0.77
0.93
1.09
0.64
0.61
1.74
1 .01
0.85
0.65
0.61
1.01
1.19
0.97
0.84
0.92
1.14
.59
.30
.38
.65
.01
.20
.66
.32
. 13
. 18
. 13
. 18
0.98
1 .42
0.97
0.89
0.57
0.
0.
0.
57.7
62.7
-
55.0
53.2
47.3
54.7
67.6
57.5
57.9
54.4
54.6
54.6
56.4
55.6
53. 1
51 .a
51.7
50.7
50.2
48.9
51.5
52.0
50.4
54.8
53.9
54.2
52.0
56.2
56.2
56.8
53.2
57.7
55.6
53. 1
45.7
49.9
54.4
56.9
60.3
RFGEN.
S OUT %
OF FED
104.8
106. 1
0.
108.5
104.6
91.6
107.7
141 .3
98.9
107.0
1 00 . 5
101 .5
101 . 1
106.9
106.9
103.8
99.0
96.6
96.5
94.2
89. 1
97.4
83.4
89.9
99.6
97.0
97.3
92.2
98.7
98.2
97.8
94.9
89.9
72.8
86.8
83.9
92.6
98.7
94.9
90.2
- 437 -
-------
APPENDIX G. TABLE IV.
RUN 9i DESULPHURISATION PERFORMANCE PAGE 1 5 OF 16
SULPHUR GAS G-BED
HAY.HOUR REMOVAL VEL. DEPTH
% M/S CENTIM
AIR/ CAO/S REGEN.
FUEL RATIO % CAS S OUT %
% ST. MOL. TO CAO OF FED
28.2230
87.4
1 .31
104.
22.0
0.36 46.0
SHUT DOWN AT 28.2230 FOR 24 HOURS
42.3
29.2330
30.0030
30.0130
30.0230
30.0330
30.0430
30.0530
30.0630
30.0730
30.0830
30.0930
30. 1030
30 . 1 1 30
30. 1230
30. 1330
30. 1430
30. 1530
30. 1630
30. 1730
30. 1830
30. 1930
30.2030
30.2130
30.2230
30.2330
31.0030
3 1 . 0 1 30
31 .0230
31 .0330
31 .0430
31 .0530
31 .0630
31 .0730
31.0830
31.0930
2. '.51
57.9 2.14
62.8 2.?b
54.5 2.04
54.2 2.11
66.3
76. 1
83.6
—
87.7
86.3
85.2
83.8
82.9
81.9
81. 1
80.3
77.4
75.8
74.3
71.5
58.7
63.3
63.6
68.9
77.0
74.6
74.0
72.6
75. 1
80.5
79.6
78.9
.42
.34
.29
.39
.33
.33
.34
.34
.34
.34
.36
.42
.44
.42
.44
.42
.64
.61
.31
.?fc
.68
.07
.50
.78
.26
.26
.29
.28
72.
73.
76.
MISSED
MISSED
73.
76.
77.
82.
85.
86.
86.
86.
86.
86.
85.
82.
81.
79.
76.
72.
72.
71.
72.
72.
71.
74.
74.
76.
78.
77.
78.
81.
81.
81.
23.8
25.7
28.0
DATA READ I
0.
1.40
1.21
NG
36.7
44.3
45.9
41.0
51.4
54. 1
DATA READING
22.5
21.7
23.3
22.8
23.5
24.9
24.5
23.3
24.3
23.9
24.3
24. 1
23.5
25.5
25.0
25.9
25.5
25.5
24.1
25.8
1-9.5
19.6
25.5
24.6
19.7
22.9
22.3
22.3
22.7
22.3
0.58
1 .30
1 .80
2.72
2. 10
1.88
0.81
0.77
1.00
1 .03
0.84
0.64
0.62
0.68
0.51
0.61
0.52
0. 16
0.07
0. 14
0.26
1 .42
0.97
0.76
0.40
0.35
1.30
1 .49
0.87
0.78
40.5
41 . 1
40.9
44.8
43.7
45. 1
53.9
51.6
53.0
56.3
55.2
53.5
53.5
53.4
54.9
53. 1
50.4
50.8
44.2
44.7
45.4
44.4
50.5
48.0
45.8
58.9
52.8
52. 1
54.2
55.2
45.7
47.0
57.4
56.4
65.5
62.3
57.7
62.6
65.4
71.8
73.2
65.5
68.3
68.8
74.0
71 . 1
67.7
68.0
63.9
64.0
57.8
51 .4
60.5
64.8
57.3
74.7
58.0
65.6
73.5
72.8
- 438 -
-------
RUN 9:
APPENDIX G. TABLF IV.
DFSULPHURISATION PEHFORMANCF PAGE
16 OF 16
DAY. HOUR
3! . 1030
31. 1 130
31 . 1?30
31 . 1330
31 . 1430
31 . 1-530
31.1 630
31. 1730
31 . 1830
31 . 1930
31 .2030
31 .2130
31 .2230
31 .2330
32.0030
32.0130
32.0230
32.0330
32.0430
32.0530
32.0630
32.0730
32.0830
SULPHUR
HFMOVAL
°/<
79.7
78.8
74.6
70.0
68.3
68.4
66.8
78.6
75. 1
81.9
84.0
84.3
84.2
84.5
84.2
84.0
85.8
84.6
84.7
84.8
85. 1
83.5
83.7
GAS
VFL.
M/S
1 .28
1.45
1 .40
1 .31
1.29
1 .31
1.75
l.cl
I .28
1 .by
1 ,d6
1 ,»7
1 .68
1 .UO
1 .56
1 .53
1 .40
1.51
1 .53
1 .51
1 .37
1 .39
1 .39
G-RED AIR/
DEPTH
FUEL
CENTIM % ST.
82.
80.
80.
80.
88.
87.
83.
80.
81.
80.
STONE
82.
87.
88.
B7,
86.
83.
87.
87.
88.
88.
87.
88.
87.
24.4
26.3
24.6
22.6
23.9
22.4
25. 1
25.0
22.3
30.4
CHANGE
33.6
30.9
28.0
25.7
25.4
25.8
23.8
25.7
25.8
25.7
23.5
25.2
26.5
CAO/S
RATIO
MOL.
1 . 10
1 .06
0.19
0.
0.
0.11
5.06
3.46
2.45
2.96
4.22
2.57
1 .45
1 .55
0.75
0.41
0.95
2.22
0.40
1.65
0.80
0.86
0.49
% CAS
TO CAO
51 .2
54.5
54.7
46.4
-
—
-
42.0
38. 1
32.7
34.5
41 .3
42.5
47.6
52.9
50.3
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