Chemically Active Fluid-bed Process For Sulfur Removal During Gasification Of Heavy Fuel Oil, Third Phase


    EPA-600/2-76-248
    September 1976
Environmental Protection Tec'
II
swft'S

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                                        EPA-600/2-76-248

                                        September 1976



CHEMICALLY ACTIVE FLUID-BED  PROCESS

            FOR  SULPHUR  REMOVAL

DURING GASIFICATION OF HEAVY  FUEL  OIL

                    (Third Phase)
                          by
   J.W.T.  Craig, G. L. Johnes, Z.  Kowszun, D.  Lyon,
 L.S. Malkin, G. Moss, O.R. Priestnall,  and D.E. Tisdall
                 Esso Research Centre
                Abingdon, Oxfordshire
                       England
                Contract No. 68-02-1359
                 ROAPNo. 21ADD-BE
              Program Element No.  1AB013
         EPA Project Officer:  Samuel L. Rakes

      Industrial Environmental Research Laboratory
        Office of Energy, Minerals, and Industry
           Research Triangle Park, NC 27711
                     Prepared for

     U.S. ENVIRONMENTAL PROTECTION AGENCY
           Office of Research and Development
                 Washington, DC 20460
                        ™ "i  —

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- ii

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                        ACKNOWLEDGMENTS
The support of Esso Petroleum Company Limited is  acknowledged
for the provision of a 2930 kW  (10 million BTU/hr) Chemically
Active Fluid Bed Gasifier facility at the Esso Research Centre,
Abingdon, Oxfordshire, England, and for various additions  and
modifications to this facility which made possible the gener-
ation of continuous gasification data for this project.

The authors also thank Mr. J. Buzzacott, Mr. D. Storms,
Mr. A. Brimble and Mr. A. Jennings for their invaluable
assistance in operating equipment and recording the experi-
mental data on which this report is based, and the many
other Esso Petroleum Company personnel involved for their
help in designing, constructing and maintaining equipment,
in operation of the pilot plant, and in chemical  analysis
of test samples.

Finally the authors acknowledge the value of many discuss-
ions and exchange of ideas with the EPA Project Officer,
Mr. S.L. Rakes, and the Westinghouse Research Laboratory
team led by Dr. D.L. Keairns.

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                           CONTENTS
ACKNOWLEDGMENTS

LIST OF FIGURES                                         vi

LIST OF TABLES                                          viii

I    INTRODUCTION                                           1

II   SUMMARY                                                9

III  CONCLUSIONS                                          11

IV   RECOMMENDATIONS                                      17

V    DISCUSSION

     BATCH STUDIES      - Fuels and Limestones            19
                        - Burn-Back Burner                23
                        - Dead Burning and Sulphation     49
                            of Spent Lime

     CONTINUOUS STUDIES - Analysis of Continuous          71
                            Runs 8 and 9
                        - Retention of Trace Elements     101
                        - Materials of Construction       1O9
                        - Modifications of Equipment      115
                            and Operations

VI   APPENDICES                                           118

       A - Batch Tests on Limestones and Fuels            119
       B - Burn-back Burner Test Results                  128
       C - Spent Lime Weathering Results                  153
       D - Sulphation Test Results                        184
       E - Modifications to C.A.F.B. Pilot Plant for      2O4
           Runs 8 and 9
       F - C.A.F.B. Run 8 Operational Log, Inspection     210
           and Data
       G - C.A.F.B. Run 9 Operational Log/ Inspection     340
           and Data
       H - Programmes and Methods of Analysis of          532
           Continuous Run Data
       I - C.A.F.B. Pilot Plant Description and           546
           Operating Procedures

                            - iv -

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                     CONTENTS  (Continued)




                                                         Page




VII  GLOSSARY OF TERMS                                    592




VIII REFERENCES                                           593




IX   PATENTS                                              594
                              - V -

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                        LIST OF FIGURES

                                                        Page

1.   Overall Programme of Work                            2

2.   Reverse Airflow Decoking Burner                     24

3.   Line Diagram of Batch Unit                          25

4.   Coked-up Primary Air Pipe                           3O

5.   Coked-up Gasifier Gas Duct                          31

6.   Partially Decoked Primary Air Pipe                  32

7.   Decoked Gasifier Gas Duct                           33

8.   Decoked Primary Air Pipe                            34

9.   Decoked Primary Air Pipe (close-up)                 35

10.  Burn-out Gas Analyses During Run No.3               37

11.  Burn-out Gas Analyses During Run No.5               38

12.  Burn-out Gas Analyses During Run No.7               39

13.  Pressure Across Gasifier Gas Duct as a Measure      41
     of Duct Decoking/Coking

14.  Variation of Rate of Gasifier Gas Duct Coking       43
     with Gasifier Bed Air/Fuel Ratio

15.  Flame Stability - Primary Aeration Diagram for      45
     Experimental Burner

16.  Combustion Diagram for Burn-back Burner             47

17.  Possible Full Scale Version of Burn-back Burner     48

18.  Optimum Temperature for Sulphur Oxide               51
     Absorption by Lime (31% of Bed Reacted)

19.  Rate Controlling Factors for Gas-Solids             52
     Reactions

20.  Pore-size Distribution of the Calcined and          56
     Sulphated Stone

                            - vi -

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                  LIST OF FIGURES  (Continued)

                                                        Page

21.  Sulphation Profile for Run No.3                     58

22.  Potential Continuous Feed Sulphator                 60

23.  Weathering of Sintered Spent Lime                   64

24.  Weathered Sintered Spent Lime after 12 Months       65

25.  Effect of Weathering on Sample Temperature          66
     for Sintered and Non-sintered Spent Lime

26.  Effect of Weathering on Molar % Total Calcium       67
     for CaO and Ca(OH)2

27.  Effect of Weathering on Molar % Total Calcium       68
     for CaCO^, CaS and CaSO.

28.  % S.R.E. Versus Gasifier Bed Depth  (Runs 8 &9)      8O

29.  % S.R.E. Versus Gasifier Bed Temperature            81
     (Runs 8 & 9)

30.  % S.R.E. Versus % Air/Fuel Ratio  (Runs 8 & 9)       82

31.  % S.R.E. Versus Cyclone Temperature (Runs 8  & 9)    83

32.  % S.R.E. Versus Added Water  (Runs 8 & 9)            84

33.  % S.R.E. Versus Ca/S Mole Feed Rate                 85
     (Runs 8 & 9)

34.  % S.R.E.  (Residual Error) Versus % Bed Fines        89
     (60O-25Oy)

35.  % S.R.E.  (Residual Error) Versus Bed Sulphur        9O
     (Wt. %)

36.  % S.R.E.  (Residual Error) Versus Bed Sulphate       91
     (Wt. %)

37.  % S.R.E.  (Residual Error) Versus Bed Carbon         92
     (Wt. %)

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                        LIST OF TABLES

                                                        Page

1.   Mean Values of S.R.E. and Bed Depth                 12

2.   Compositions and Properties of Fuel Oils            19
     Used in the Batch Test Programme

3.   Chemical Compositions of Limestones Tested          20

4.   Summary of Batch Unit Loss Rates                    21

5.   Lined-out S.R.E.'s for Candidate Stones             22

6.   Temperature Increase during On-stream               27
     Gasifier Gas Duct Decoke

7.   Comparison of Gasifier Product Gas Compositions     36
     from Batch and Continuous Units

8.   Measure of the Rate of Gasifier Gas Duct            42
     Coking

9.   Range of Burner Parameters giving a Stable          46
     Flame

10.  Fluidised Bed Batch Tests                           54

11.  Sulphur in Stone Fractions                          55

12.  Continuous Spent Lime Feed Fluidised Bed            61
     Sulphation Tests

13.  Effect of Temperature on Spent Lime Acitivity       62

14.  Leachate Analyses                                   7O

15.  Summary Statistics for Runs 8 and 9                 73

16.  Linear Regression Equations to Predict % S.R.E.     76
     for Runs 8 and 9

17.  Prediction of Run 8 Data from Run 9 Regression      78
     Equation and Vice Versa

18.  Comparison of Polynomial Expression and Linear      86
     Expression for Regression Variables


                           - viii -

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                  LIST OF TABLES  (Continued)

                                                        Page
19.  Polynomial Regression Equations to Predict           82
     % S.R.E.

20.  Prediction of Averaged % S.R.E. from Runs 6 and      94
     7 Using Developed Equation for Runs 8 and 9

21.  Effect of Aragonite on % S.R.E.                      96

22.  Effect on Injecting Various Sulphur Compounds        98
     into the Gasifier Bed

23.  Effect of Position of Bottom Fuel Injector on      100
     % S.R.E.

24.  Operating Conditions for Period 10-1630 to         102
     13-0030 for Run 9

25.  Stone Inventory for Gasification Period 10-1630    103
     to 13-OO30 for Run 9

26.  Comparison of Analytical Results from Spark-       105
     Source Mass Spectrometry and Neutron Activation
     Analysis

27.  Mass Balances for Gasification Period 1O-163O      106
     to 13-OO30

28.  Comparison of Trace Element Enrichment Factors     108
     on Gasifier Bed Material and Boiler Cyclone
     Fines
                            - xi -

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                           INTRODUCTION
GENERAL

The Chemically Active Fluid Bed. process is a means of
avoiding sulphur oxide pollution while using heavy fuel oil
for production of power.  The process uses a fluidised bed
of lime particles to convert the oil into a hot, low sulphur
gas ready for combustion in an adjacent boiler.  Sulphur
from the fuel is absorbed by the lime which can be re-
generated for reuse.  During lime regeneration the sulphur
is liberated as a concentrated stream of S02 which may be
converted to acid or elemental sulphur.

Exploratory work on the CAFB began at the Esso Research
Centre, Abingdon (ERCA) in 1966.  In 1969 a six-phase
programme of work was prepared to take the CAFB process from
the laboratory stage through to a demonstration of the process
on a 50 to 100 megawatt (electrical) power generation boiler
located in the United States.  A summary of this six phase
programme is shown in Figure 1.  Phase I studies at Esso
Research Centre were funded under Contract CPA 70-46 in June
1970, and consisted of batch reactor fuel and limestone
screening studies,  a variable study with U.S. limestone BCR
1691, and initial operation of a pilot plant incorporating
continuous gasification and regeneration.  The results of
these studies were described in the final report (1) for
that contract, dated June 1972.

Work on the second phase of studies was carried out in the
period July 1, 1972 through May, 1974, and the final report
was issued in November 1974 (2).

This report covers work on phase three studies carried out
under contract 68-02-1359 between November 1973 and June
1975.

GASIFIER CHEMISTRY

When heavy fuel oil is injected into a bed of fluidised lime
under reducing conditions at about 9OO deg. C, it vaporises,
cracks, and forms a series of compounds ranging from H2 and
CH4 through heavy hydrocarbons to coke.  The sulphur con-
tained in the oil forms compounds such as E^S, COS and CS2
                             - 1 -

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with H2S predominating.  The sulphur  compounds  react with  CaO
to form CaS and gaseous oxides.

For example:

          CaO + H2S  	>  CaS + H20

The equilibrium for this reaction is  far to the  right.
With a fuel containing 4% sulphur the equilibrium permits  a
desulphurising efficiency greater than 90% up to 1100 deg.  C.
Other factors however limit gasification temperature to  the
range of about 850 to 90O deg. C where the equilibrium
sulphur removal would be about 99% (see Reference 1).

In the shallow fluidised bed of the gasifier there is a
rapid circulation of lime between top and bottom.  Indications
are that coke is laid down on the lime in the upper portion
of the fluid bed by oil cracking and  coking reactions and
that this coke burns off in the lower portion where oxygen
is supplied by the air distributor.

Gasification conditions of temperature and air-fuel ratio
must be chosen to maintain a balance between the rate of coke
and carbon deposition and the rate of carbon burnoff.
Broadly, this balance is met at gasification temperatures in
the range of 850 to 900 deg. C and air-fuel ratios around 20%
of stoichiometric.  Lower air fuel ratios are operable at
the upper end of the temperature range, and higher air-fuel
ratios are needed as temperature is reduced.

Much of the oxygen entering the gasifier is consumed in
oxidising coke to CO and C02 near the distributor.  Of course,
some enters other regions of the bed where it reacts with H2
and hydrocarbons to form water and more carbon oxides.  The
final product from the gasifier is a hot combustible gas
containing H2 , hydrocarbons, CO, CO2 , ^O, and N2 •  Most of
the energy released by partial combustion of the fuel is
retained by this gas as sensible heat.

Only a portion of the CaO in the lime is reacted on each pass
of solids through the gasifier.  Good sulphur absorption
reactivity has been obtained with up  to 20% of calcium
reacted in single cycle batch reactor tests, but in the
continuous unit, the average extent of calcium conversion
to sulphide is held to less than 10%.
                             -  3  -

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When a single batch of lime is cycled between gasification
and regeneration conditions it gradually loses activity for
sulphur absorption.  The activity of the bed can be maintained
if some of the lime is purged each cycle and replaced by
fresh material.  Reactivity of the bed is therefore a function
of the lime replacement rate.  The replacement lime is usually
added to the gasifier as limestone which calcines in situ.

Vanadium from the fuel oil deposits on the lime during
gasification.  Experimental evidence" is that practically  all
of the fuel vanadium can remain fixed with the lime.

REGENERATOR CHEMISTRY

Calcium sulphide is regenerated to Calcium oxide by air
oxidiation.

          CaS + 3/2 02 	> CaO + S02

                                       AH = -485.1 kJ/mol

A competing reaction also consumes oxygen and forms calcium
sulphate.

          CaS 4- 2O2    	> CaSO.

                                       AH = -921.3 kJ/mol

Both reactions are strongly exothermic.  A third reaction
between the solid species is also possible.

          CaS 4- 3CaSO. 	> 4CaO + 4SO2

                                       AH = 926.8 kJ/mol

This reaction is strongly endothermic.

The equilibrium constants  (Appendix A, Reference 1) for these
reactions determine the maximum partial pressure of SC-2 which
can exist in equilibrium with mixtures of CaS, CaO, and CaS04
at any given temperature.  These equilibria also determine  a
relationship between regenerator temperature and the maximum
theoretical selectivity of oxidation of CaS and CaO.

At low oxidation temperature, the equilibrium S02 partial
pressure is too low to permit all the oxygen supplied to  leave
in the form of SO2•  The excess oxygen then goes to form
CaS04.  Experimental oxidation selectivities are lower than
the theoretical maximum, probably because of contacting and
kinetic factors.
                             - 4 -

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Since each sulphided lime particle passes  through  a  range  of
temperatures and oxygen concentrations  during  its  transit
through the regenerator, it is exposed/ on  average,  to  less
favourable selectivity conditions than  those at  the  top of
the bed.

Calcium sulphide oxidation selectivities to CaO  of 70 to 80%
and regenerator S02 concentrations of 8 to  10% have  been
achieved in pilot plant operations at regenerator  temperatures
in the range of 1040 to 1070 deg. C.

During the conversion of CaS to CaO and CaSO^  there  is
evidence for existence of a transient liquid state (Reference
17).  If air is passed through a hot static bed  containing CaS,
seme of the particles will agglomerate  into lumps  during the
regeneration reaction.  Agglomeration does not occur if the
bed is vigorously fluidised.

BACKGROUND INFLUENCES ON EXPERIMENTAL STUDIES

Details of the results of previous studies  are described
fully in previous reports (1)  (2), but  in summary  this  work
had confirmed that good desulphurisation results could  be
obtained and that the process was stable and controllable.
Sufficient information was generated by these  studies to
enable EPA to request Westinghouse Research Laboratories
(WRL), under contract to EPA, to carry out  a preliminary
technical and cost review and to recommend on  future deve-
lopment.  A report by WRL (3) confirmed that the CAFB process
was attractive when compared with the main  alternatives  for
Clean Power Generation - Flue Gas Desulphurisation orcom-
bustion of Heavy Fuel Oil desulphurised at  a refinery.

Acting on behalf of EPA, WRL presented  the CAFB process  to
a number of utilities, with the objective of interesting one
of them in participating under EPA support in  conversion to
CAFB operation of a power generation boiler of about 5O MWe
capacity.  Early in 1973 New England Electric System (NEES)
of Westborough, Mass, agreed in principle to cooperate  in
such a demonstration to be based on a 5O MWe boiler  at
Providence, Rhode Island.  EPA, NEES and WRL jointly selected
Stone & Webster Engineering Corporation (SWEC)  as  the
Architect Engineer for the conversion.  Details of the  SWEC
design and costing have been reported by WRL (4), but events
were overtaken by the decision of the Federal Energy Authority
to schedule NEES boilers for operation on coal only.  In
view of this, NEES withdrew from the demonstration programme
in April 1975.
                            — 5 —

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Fortunately for the progressive continuation of the CAFB
development programme Foster Wheeler Energy Coporation  (FWEC)
had been pursuing an independent programme as a worldwide
licensee of patents held on the CAFB process by Exxon Research
and Engineering Company  (ER&EC) and drew this to the
attention of EPA in April 1975.  Agreement was readily
reached between EPA and FWEC to fund engineering studies,
and FWEC in turn signed an agreement with Central Power and
Light  (CP&L) of Corpus Christ!, Texas, to convert a 20 MWe
boiler in the CP&L plant at San Benito, Texas.  This pro-
gramme is now continuing, with plans to construct the
demonstration unit during 1976, with a June 1977 startup
to commissioning and the test programme.

As set out in Figure 1, Phase Three was planned as a period
for supporting design studies and evaluations of the CAFB
process.  In the event the total EPA programme on CAFB
moved rapidly during this period through evaluation to actual
design details for the demonstration plant.  Consequently
the programme carried out by ERCA changed emphasis several
times during Phase Three, the contract tasks were modified,
and in November 1974 the programme was extended by starting
Phase Four in parallel, under EPA Contract 68-O2-1479.
The latter contract is still in progress, and is due for
completion in December 1976.

WORK OBJECTIVES

The final list of tasks adopted for this contract is set
out below:-

Task 1    A batch reactor study of up to three limestones
          which could be supplied to the demonstration
          plant, plus one alternative fuel oil.

Task 2    The derivation of a model to describe the be-
          haviour and performance of the CAFB process,
          based on data obtained in previous contracts,.
          to serve as a guide for the engineering design
          team working on the design of the demonstration
          plant.

Task 3    A run totalling 270 hours of gasification on  the
          continuous CAFB pilot plant, under conditions
          indicated by previous studies, and using a  fuel
          oil and limestone combination indicated by
          earlier work as being suitable for the demonstrat-
          ion plant.


                            -  6 -

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Task 4    A second run of 270 hours under  conditions  required
          to provide specific data for  design,  or  to  solve
          problems encountered in Task  3,  or  to test  an
          alternative limestone.

Task 5    Provide on-going advice and consulation  to  other
          contractors engaged in progressing  the CAFB
          demonstration unit.

Task 6    Test materials of construction for  their suit-
          ability in CAFB by exposing coupons or fabricated
          parts in selected positions during  a  CAFB pilot
          plant run.

Task 7    Determine to what extent CAFB retains  on the bed
          certain elements present in fuel oil  and which
          are potentially harmful when  emitted  into the air
          in flue gases.

Task 8    Determine the feasibility of  burner design  mod-
          ification to allow on-stream  gas duct  decoking
          by reverse air flow, isolation of the  gasifier
          from the boiler furnace and firing  the boiler with
          an alternate clean fuel.

Task 9    Evaluate alternate low cost methods for  purge
          stone and regenerator off-gas disposal.

Task 8 was added to test the principle  of  an  invention made
by ERCA under the contract whereby decoking of  the gasifier
ducts and cyclones could be carried out without  shutting
down the gasifier or boiler.

Task 9 was added to provide information on the  probability
of success of the route proposed by WRL for simultaneously
converting spent lime and the SO2 effluent from  the regen-
erator to an innocuous solid.  This was the process step
included in the SWEC design specifications for  costing
purposes.  As a backup tests were also  carried  out under
Task 9 to evaluate means for inerting spent lime by dead-
burning, to support an alternative process route of convert-
ing the S02 effluent steam into elemental sulphur.  This is
in fact the route now being pursued by  FWEC using  their
proprietary Resox process.
                             - 7  -

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REPORTING AND DISCUSSION OF RESULTS

The discussion is set out in Section V by task and in
chronological order, so that reasons for modifications to
the programme can be readily discerned.  Wherever
necessary for additional clarity, reference is made to
significant events external to this contract which are
summarised above, and which influenced the direction or
emphasis of the experimental programme.
                              - 8 -

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                          II SUMMARY
Phase three of studies on the CAFB process for desulphurising
gasification of heavy fuel oil in a fluidised bed of hot lime
was carried out between November 1973 and June 1975.  Object-
ives of the work were changed during this period due to
changes in the location of the proposed 50 MWe demonstration
from New England to Texas/ and in the engineering philosophy
of some features of the design.  Specifically, there was a
change from an intention to use spent lime sulphation as the
route to disposal of both S02 from the regenerator and spent
lime from the reactors to a process involving reduction of
regenerator S02 to elemental sulphur combined with marketing
of spent lime, or alternatively dead burning of spent lime
for landfill or other disposal.

Tests of candidate limestones confirmed the superiority of
BCR 1359 in its resistance to dust production, but showed
that several limestones and one dolomite could absorb sul-
phur just as effectively as BCR 1359.

Sophisticated computer analysis of data generated in phase
two and phase three studies identified hitherto unrecognised
significant variables, and pointed to areas of potentially
profitable further study.  Runs 7, 8 and 9 can now be des-
cribed very effectively by a polynomial expression, but Run
6 gave results consistently better than the predictive
equation, and thus offers potential for identification of
another significant variable.

As a result of the computer analysis it is now clear that
some variables have a fairly large effect, water being by
far the most potent (and deleterious), while others,
especially stone replacement rate, previously thought to be
of major importance, are now seen to be relatively minor
contributors.

Operability of the CAFB process was improved by demonstration
of decoking of gas ducts and cyclones over a bed slumped from
the gasifying mode.  No harmful reaction of the hot bed, con-
taining calcium sulphide, and coated with carbonaceous deposits,
was observed - especially there was no agglomeration to hinder
refluidisation.  On stream decoking trials were unsuccessful,
and an improved fines return system from the cyclones continued
to give trouble.
                             - 9 -

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Retention of a wide range of elements by the lime bed was
demonstrated, and in particular retention of alkali metals,
which will be of significance to use of a pressurised
CAFB for gas turbines, which is -currently being evaluated
under EPA Contract 68-02-2115.

A prototype burn-back burner demonstrated the suitability
of this approach to on-line decoking of gasifiers equipped
with parallel cyclones, ducts and burners, the potential
for a wide range of turn down, and potential for dual-fuel
or standby operation during gasifier outage.

Tests of sulphation of spent lime on a fluidised bed failed
to meet the technical objectives set, and this route to SC>2 .
and lime disposal does not seem viable.  Weathering tests on
deadburned lime samples showed promise for this technique
as an acceptable means of treating spent lime before dumping.
                             -  10  -

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                        Ill CONCLUSIONS
TASK 1

1.   The three stones which were tested were all inferior
     to B.C.R. 1359 in respect of dust production and
     were in fact comparable with B.C.R. 1691 from this
     point of view.

2.   Both the Tymochtee dolomite and the Aragonite were
     marginally inferior to B.C.R. 1359 in desulphurising
     performance during cyclic tests.

3.   The vacuum bottoms fuel was desulphurised just as
     effectively as the normal Amuay residual fuel oil
     despite its higher sulphur content.
TASK 2

The application of a sophisticated computerised regression
analysis technique, involving the use of polynomial funct-
ions, has enabled the desulphurisation results for Runs 7,
8 and 9 to be harmonised, and individual results to be
predicted in terms of the following variables

          Bed Depth
          Bed Temperature
          Air/Fuel Ratio
          Cyclone Temperature
          Ca/S Mol Ratio
          Added Water

The results for Run 6 are significantly better than would
be predicted by the use of the regression equation, but
nevertheless this approach looks very promising and will be
further tested and refined in future runs.

Whilst this type of equation is purely empirical, for pract-
ical purposes it can serve almost as well as an equation
based on a detailed physico-chemical model of the process,
and its precision and scope may be improved as more data
become available.

However, caution must be exercised in interpretation of
future tests on this pilot plant, or on other CAFB gasifiers,
in that other variables may then become of importance, or
                            - 11 -

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in that operating requirements may be extended outside the
range studied so far.
TASKS 3 & 4

Two sets of  conclusions may be drawn from an analysis of
the operating experience gained during Runs 8 and 9.  One
set relates to the effects of process variables on Sulphur
Removal Efficiency, the other set relates to factors affect-
ing the general operability of the gasifier.

The Effects of Process Variables

1. Contrary to expectations the very much deeper gasifier
beds used in Runs 8 and 9 did not give S.R.E.s which were
appreciably better than those obtained during Runs 6 and 7.
The mean values of S.R.E. and bed depth for the four runs
are shown in Table 1.

                           Table 1

              .Mean values of S.R.E. and Bed Depth

                    Mean bed depth              Mean S.R.E
Run No.             	cms	              	%	

   6                      52                        77.5
   7                      57                        75.4
   8                      91                        77.1
   9                     103                        79.1

Although analysis of the test results for Runs 8 and 9 showed
that within these runs there was a bed depth effect, it is
evident that there were other factors which had an over-
riding effect between runs.

As mentioned previously this apparent anomaly could be
accounted for in the case of Run 7 by the effects of the
other five apparently relevant variables, the main factor
being the absence of water in Run 7 due to  the very limited
use which was made of flue-gas recycle during this run.
In Run 6 however a very considerable amount of flue-gas re-
cycle was used and the regression equation gave results
indicating that the observed S.R.E.s were about 14 per-
centage points better than they should have been.  This
suggests that there must have been a factor operating in
                             -  12  -

-------
Run  6, which  is not  taken  into  account  in  the  regression
equation and  which had  an  advantageous  effect  large  enough
to offset  the water  debit.   It  would  clearly be  advant-
ageous to  identify this factor  if  possible.

2. The mean bed sulphur contents during Runs 8 and 9  were
very similar  and  the standard deviations were  small  in
both cases, consequently no  sulphur term appeared in  the
regression equation.  The  effect of bed sulphur  content  on
residual error is shown in Fig. 35 and  is  not  as simple  as
was  indicated by  the results of Runs  6  and 7.

At bed sulphur contents of up to 6.5%   by  wt,  the range
covered in Runs 6 and 7, the plotted  points indicate  a down-
ward trend for S.R.E. as the bed sulphur content rises.  At
sulphur contents greater than 6.5% by weight however  there
appears instead to be an upwards trend  in  S.R.E. as the
sulphur content of the  bed material increases  and a much
greater scatter of results.  It is difficult to account  for
this anomalous trend but it  is worth  remarking that many of
those high sulphur contents were obtained  during periods of
operation when the carbon  content  of  the gasifier was high
enough to render  the regenerator inoperative,  the tail gas
containing C02 and CO but  virtually no  SC>2.  It seems
likely that there is a  combined effect  of  sulphur and carbon
on S.R.E. in  which the  presence of carbon  will up to  a
point improve sulphur retention in the  gasifier by prevent-
ing the oxidation of CaS near the distributor.  At excessive
carbon levels however the  S.R.E. would  appear  to be reduced
as shown in Fig.  37.  These  two conflicting effects might
account for the scatter of points  in Fig.  35 at bed sul-
phur levels in excess of 6.5% by wt.

3. Within the temperature  range 86O-930"C  the  effect  of
variations in gasifier  bed temperature  on  S.R.E. during
Runs 8 and 9 was small, as can be  seen  in  Fig. 29.  This
is in line with previous findings but there are indications
of an optimum temperature  in the range  of  880-90O°C.  As the
bed temperature is increased above 930°C there is a rapid
decline in S.R.E., though  even at  99O°C a  substantial pro-
portion of the sulphur  entering the bed is retained.

4. The range  of air/fuel ratios explored during Runs  8 and
9 was much wider than was  the case for  Runs 6  and 7 and, as
can be seen in Fig.  30  there are indications that leaner
operation resulted in improved desulphurisation efficiency.
Unfortunately it is  not entirely clear  whether this effect
was in fact directly related to stoichiometric ratio  or
whether it arose from the  corresponding variation in  sul-
phur throughput, since  most of the variation in stoichio-
metric ratio was obtained  by varying the fuel  rate.

                            - 13 -

-------
5. The relationship between S.R.E. and Ca/S molar feed rate
for Runs 8 and 9 is shown in Fig. 33.  The information
presented here confirms the findings from the results of
Runs 6 and 7 which indicated that stone replacement rate
has a relatively minor effect on S.R.E.  According to Fig.
33 there is on average only a 2 percentage points improve-
ment in S.R.E. for an increase in stone consumption from
0.5 mols to 1.3 mols.  This indicates the desirability of
investigating stone feed rates of less than 0.5 mols.  It
would indeed be desirable to operate the unit at the min-
imum stone feed rate which will allow the bed depth to
be maintained constant, because this will minimise the
production of fines due to calcination and might in time
result in virtually dust-free operation.

6. It has been found that an operating variable having an
appreciable effect on S.R.E. is the rate of bed circulat-
ion through the gasifier cyclones.  A rough indication of
this circulation rate during Runs 8 and 9 was given by
the mean temperatures of the cyclone fines drain vessels.
In Fig. 31 these temperatures have been used as the
appropriate variable and over the range observed the
apparent effect on % S.R.E. is about 7 percentage points.
There are several possible explanations for this effect,
the simplest of which is that the fines recycle rate in-
dicates the extent to which lime particles are present in
the free-board.

7. Although fines recycle rate is a function of bed par-
ticle size, there is no evidence of a relationship between
bed particle size and S.R.E., as can be seen in Fig. 34.
This suggests that the effect of bed material size is fully
accounted for in the cyclone temperature term.

8. As mentioned previously the presence of water had a
marked adverse effect on S.R.E. as is shown in Fig. 32.
During most of the tests the water debit was relatively
small but the indications are that if sufficient water is
present it can virtually deactivate the sulphur absorbing
capacity of the bed.
Operating Factors

1. During Run 9  attempts were made  to  reduce  the  rate  of
carbon deposition  in  the cyclones by introducing  air and
steam under the  lid of  the gasifier.   These attempts were
not successful.
                           - 14 -

-------
2. It has been established that the  carbon burn-out pro-
cedure may be carried out successfully over the  slumped
gasifier bed without prior sulphation.  This procedure
was employed several times and each  time the gasifier
was put back on stream without any problems.  There was
nothing to indicate the formation of  a surface crust due
to oxidation of the calcium sulphide  in the surface layer
of the bed and it seems that the small bleed of  nitrogen
which was passed through the slumped  bed was sufficient
to prevent the oxygen from diffusing  to this region.

3. During both Run 8 and Run 9 a considerable amount of
trouble was experienced with the cyclone fines re-inject-
ion system.  It must be concluded that the Sturtevant
solids pump is unsuitable for this purpose because the use
of high gas pressures for solids transfer causes high
cyclone losses when the isolating valves fail to seat pro-
perly .
TASK 7

It has previously been established that the gasifier bed
material retains the bulk of the heavy metals in the fuel.
The more detailed analytical work carried out on samples
collected during Run 9 established that virtually all of
the sodium and potassium in the fuel is also recovered.
Previous results based on analysis of the gasifier bed
material indicated that only about 3O% of the sodium was
retained, but the complete analysis showed that the rest
of the sodium was recovered with the fines drained from
the boiler cyclone.  It seems therefore that the volatile
alkalis are trapped outside the gasifier at low temperature
regions within the boiler.  This suggests that, if the gas
is suitably quenched, alkalis will not present a problem
when a fluidised bed gasifier is used to fire a gas tur-
bine .
TASK 8

Tests made with the model burn-back burner showed that this
type of burner configuration, in which air is admitted
through a central duct and gas is introduced into a conical
casing, gives a very stable flame and a good turn-down ratio,
The burn-back principle was also successfully demonstrated.
                            - 15 -

-------
TASK 9

1. It does not appear to be feasible to achieve more than
60% sulphation of spent lime in a fluidized bed reactor,
consequently dry sulphation is not a very attractive route
for the disposal of the regenerator S02 stream.

2. Dead burning of lime at temperatures of 135O°C or greater
reduces reactivity to water considerably, but the initial
reaction process is still hydration.  The hydrated lime is
converted to calcium carbonate with little loss of calcium
from the exposed sample, even with monthly mixing of the
reacted crust with the bulk sample.  Thus this technique
seems promising as a procedure for treating spent lime prior
to dumping on land.
                            - 16  -

-------
                       IV RECOMMENDATIONS
1. Since the presence of water, both in the fuel  and in  the
recycled flue gas appears to have an adverse effect on sul-
phur removal efficiency, it is recommended that the flue gas
recycle scrubber of the gasifier be eliminated.   There are
two ways in which this may be done
  1.  The wet scrubber may be replaced by a bag filter.
  2.  The unfiltered flue gas recycle stream may  be intro-
      duced into the gasifier bed via a large bore tuyere
      situated above the distributor, instead of  being ducted
      into the plenum and passing through the distributor.
The second alternative is preferable, but provision should
be made to test both alternatives.

2. It has been demonstrated that reasonably good  desulphur-
isation is obtainable at stone replacement rates  of less
than half the Ca/S molar ratio.  There is an incentive,  in
terms of dust control, to investigate the minimum stone
make-up rates which will maintain constant bed depths
under various operating conditions.  Very low stone replace-
ment rates will also ease the stone procurement problem  and
may allow the recovery of heavy metals from the spent stone.

3. The effects of both stone sulphur content and  stone car-
bon content on S.R.E. are still in need of clarification
and should be examined in more detail.

4. The cyclone fines drain and return system used in Runs 8
and 9 was unsatisfactory and should be replaced by a simpler
system preferably without moving parts.

5. Attempts to control carbon deposition in the cyclones by
air and steam injection have been unsuccessful, therefore
the use of small but heavy and abrasive particles should be
considered.  Silicon carbide particles were used  in the
sulphation work carried out in Task 9 in an attempt to grind
the softer lime particles in a fluidised bed, but no such
effect occured.  It should therefore be possible  to scour
the cyclones without creating a dust problem by using silicon
carbide particles which are small enough to reach the cyclones
but large enough to be retained by them.
                           - 17 -

-------
6. The design of the existing gasifier will not  allow major
modifications to be made either to the configuration of  the
cyclones or to the cyclone drainage system.  It  is  therefore
recommended that the gasifier be replaced prior  to  Run 10
by a new unit in which the cyclones are replaceable and  are
mounted so as to allow a simple fines drainage and  return
system to be used.

7. Consideration should be given to the problem  of  injecting
fuel uniformly into a large scale unit and the new  gasifier
should incorporate provision for testing suitable injector
designs.
                            - 18 -

-------
                          V DISCUSSION
BATCH STUDIES

Equipment and Method of Operation -

The initial objectives of Task 1 were to check on  a batch  re-
actor three limestones and one alternative heavy fuel  oil
which might be used in the proposed 50 M.W.e. demonstration
plant.

The batch reactors have been described previously  and  so have
the test procedures used for measuring dust  cyclic tests  (2 ).
The tests carried out under task 1 were of a comparative
nature, the reference materials being Amuay  residual fuel  oil
and B.C.R. 1359 stone.

Fuels and Limestones - The alternative fuel  which  was  selected
was an Amuay vacuum bottoms stream and details of  its  com-
position and inspection data are shown in Table 2  together
with those for the reference fuel.

                            TABLE 2

           COMPOSITIONS AND PROPERTIES OF FUEL OILS
               USED IN THE BATCH TEST PROGRAMME
      PROPERTY
AMUAY RESIDUAL
   FUEL OIL
Specific Gravity           0.957
Kinematic Viscosity
  Cs at 140°F              201
        210°F             41.1
        280°F
        35O°F
        4OO°F
Carbon % by wt            85.9
Hydrogen % by wt          11.3
Sulphur % by wt            2.3
Nitrogen % by wt           O.35
Conradson Carbon % by wt  11.6
Asphaltene % by wt         7.1
Vanadium ppm              366
Nickel ppm                 43
Sodium ppm                 36
Iron ppm                    3
   AMUAY VACUUM
PIPESTILL BOTTOMS

     1.015
                      3180
                       321
                       24O
                        71
                     84.7
                     10.0
                      3.2
                      0.59
                     17.4
                      6.9
                     580
                      66
                       6
                       3.5
                           - 19 -

-------
Due to an initial delay in the procurement of suitable lime-
stone samples Tymochtee dolomite, which was already held in
store, was substituted for one of the candidate stones.
The two candidate stones which were tested were aragonite
which consisted of small seashells and a crystalline mat-
erial designated Conklin stone.

Analyses of these materials are given in Table 3

                            TABLE 3

          CHEMICAL COMPOSITIONS OF LIMESTONES TESTED
STONE
COMPONENT
CaO
MgO
Si°2
Fe2°3
A12°3
co2
S (total)
Vanadium
Sodium
Nickel
BCR 1359
% by
% by
% by
% by
% by
% by
% by
ppm
ppm
ppm
wt
wt
wt
wt
wt
wt
wt



54.
0.
0.
0.
O.
44.
0.
50
<20
30
1
6
75
09
31
0
12



TYMOCHTEE
DOLOMITE
31.
20.
3.
O.
1.
43.
0.
<25
175
10
1
9
1
4
13
6
13

ARAGONITE
57.
0.
5
65
<0 .2
Trace
0.05
40.8
0.
<50
17

2520

-

CONKLIN
39.
12.
12.
0.
0.
36.
<0.
<50
<50
53
6
0
3
13
53
9
04



Experimental results - At a very early stage it was found that
the Conklin stone was too prone to decrepitation to be con-
sidered for use in the demonstration plant and since no other
stone samples were forthcoming only the Tymochtee dolomite
and the Aragonite were fully tested.  The resources which
were released in this way were devoted to the burn-back
burner tests which are described later in this section of
the report.

The detailed experimental data which were obtained during
the dust tests and the cyclic desulphurisation tests are
reported in Appendix A.  Summaries of the dust results and
the cyclic test results are given in Table 4.  The results
                            - 20 -

-------
of the first sequence of cyclic gasification  tests made
with Tymochtee dolomite are not reported in Appendix A be-
cause it was subsequently found that the distributor of  the
batch gasifier had developed a large crack during the  course
of the test.

Dust results - As can be seen in Table 4 the  dolomite  and
the aragonite were both markedly inferior to  B.C.R. 1359 in
dust production and under cyclic conditions both were  infer-
ior to B.C.R. 1691 which, from pilot plant experience  in
Run 4 (2 )  is considered unsuitable for use in  a full  scale
plant.  It follows that neither of these stones appears  to
be a promising candidate for use in a demonstration plant.

                           TABLE 4
              SUMMARY OF BATCH UNIT LOSS RATES

                      LOSS RATE  (g/min)

                                               GASIFICATION
CONDITIONS  KEROSINE   FUEL OIL   FUEL OIL     REGENERATION
            COMBUSTION COMBUSTION COMBUSTION   CYCLIC TESTS

Limestone

Tymochtee                 1Q>5       1Q>3            6>4
Dolomite

Aragonite      6.6         6.9        6.4            5.9

BCR 1359       2.1          -         3.6            1.9

BCR 1691      22.6        13.5        7.8            4.5

Cyclic desulphurisation test results - Both the  aragonite
and the dolomite were subjected  to cyclic gasification tests,
using Amuay residual fuel oil, in order to assess  their  eff-
ectiveness as sulphur absorbers.  Additional  tests were  also
run under similar conditions with B.C.R. 1359.   The  overall
results of these tests are summarised in Table 5.  It is
normal for the results of the first six or seven of  a series
of cyclic tests to show a falling trend in sulphur removal
efficiency towards a stable value.  This was  observed in the
case of the dolomite and the B.C.R. 1359 stone but the ara-
gonite showed a fairly uniform result right through  the  test
                           - 21 -

-------
series.  The values shown in Table 5 were obtained by  aver-
aging all but the first eight results in the case of BCR
1359 and Tymochtee dolomite whilst all of the aragonite
results were used.

                          TABLE 5

          LINED-OUT S.R.E.'s FOR CANDIDATE STONES
      STONE


Aragonite

Aragonite

Tymochtee Dolomite

Tymochtee Dolomite

B.C.R. 1359
    FUEL


Amuay Resid.

V.P.S.B.

Amuay Resid.

Amuay Resid.

Amuay Resid.
MAKE-UP-RATE
% STOIC Ca/S

    1.10

    0.91

    0.64

    0.86

    1.10
% SRE


 65

 65

 68

 64

 68
It is evident that the desulphurising performances of the
aragonite and dolomite are not appreciably  different
from that of BCR 1359.  It is also clear that the heavier
vacuum pipestill bottoms having a sulphur content 40%
higher than that of Amuay residual fuel oil is unlikely  to
cause any problems.  Although the Ca/S make-up rate was
lower for dolomite than for the other stones, the actual
stone addition rates were comparable.  It is however diff-
icult to account for the fact that the higher stone re-
placement rate gave the poorer performance.  It seems
likely that both of the candidate stones are marginally
less effective than BCR 1359 as sulphur absorbents but
are quite acceptable from this point of view.  In both
cases dust production will be the deciding factor in
judging suitability for continuous operation in the
demonstration plant.
                           - 22 -

-------
Burn-back Burner

Introduction -

The objectives of this work were  as  follows:

o    To determine the feasibility of burner design modifi-
cation to allow:

     (1) on-stream gasifier gas duct decoking by reverse
         air flow.
     (2) isolation of the gasifier from the boiler furnace.

o    To provide burner performance data suitable for  scaled
up tests on a CAFB continuous gasifier.

Equipment and Operating Procedure -

A sectional view of the experimental burner which was used
to demonstrate the feasibility of on-stream gasifier gas
duct decoking is shown in Figure 2.  It will be seen  that
the primary air is fed to the burner through a central heat
resistant pipe which is retractable.  The secondary air is
fed tangentially into a swirl chamber and emerges from
equispaced nozzles near the burner orifice plate.  In the
normal running position the primary air pipe is retracted
and the gas and primary air are able to mix and pass  through
the orifice into the combustion zone where the secondary
air is added.

A design feature of the burner is the movable primary air
pipe which would allow isolation of the gasifier from the
boiler furnace.  When the primary air pipe is advanced, it
seals off the concentric gasifier gas duct, which may then
be burned out by introducing air into it through the  small
inlet pipe shown in the drawing.  This "burn-out" config-
uration allows an alternative fuel to be introduced with the
primary air whilst the burn-out is in progress, though no
provision has been made for this in the present design.
During the course of these decokes, whilst maintaining gas-
ification, the gasifier product gas was flared from an
alternative outlet and the combustion products of the burn-
out flowed back into the gasifier and left via the second
burner.  A line diagram of the complete apparatus is  shown
in Figure 3.
                           - 23 -

-------
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                           - 24  -

-------
The existing 4A batch gasifier was used but it was necessary
to provide additional items of equipment in order to supply
primary, secondary, and burn-out air to the reverse airflow
decoking burner.  It will be seen that the main fluidisat-
ion air and primary burner air were metered by positive
displacement meters.  Flow-raters were used for the fuel
injection air, secondary burner air, burn-out air and
oxygen, and the bleeds to the manometers which were used
to measure the pressure drops across the burner duct, bed,
and distributor.

The batch gasifier was operated under cyclic gasification/
regeneration conditions to simulate continuous CAFB gas-
ification and to produce gasifier product gas similar in
composition to that produced on a continuous CAFB gasifier.
The operating procedures for batch unit cyclic tests have
previously been reported (2).  Consequently only those add-
itions to the procedures will be noted.

During start-up and regeneration operations the primary air
pipe was advanced to seal off the gasifier gas duct and
nitrogen was passed into the duct to blanket any laid-down
carbon in the duct from contact with air.

The experimental burner flue gas analyses for CC^, CO, and
02 were obtained by sampling at an appropriate point in the
flue stack and using the existing train of analytical in-
struments.  During the course of an on-stream burn-out the
combustion products of the burn-out were metered for CC>2 /
CO, and 02 by sampling from a small pipe in the gasifier
gas duct shown in Figure 2.  Provision was also made for
sampling the uncombusted gasifier product gas during the
course of a run.  These samples were collected in large
plastic bags and were analysed by gas chromatography within
half an hour of collection.

Burn-back Evidence -

The on-stream gasifier gas duct decokes for which detailed
duct surface temperatures and burn-out combustion gas
analyses were obtained are listed in Table 6.  The duct
temperatures were measured by means of two thermocouples A
and B located in the gasifier gas duct as shown in Figure 2.
                           - 26

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- 21 -

-------
The evidence that successful decokes were achieved is four-
fold:

  o   Gasifier duct surface temperature trends during a
      burn-out
  o   Burn-out combustion product gas analyses
  o   Visual evidence that deposited carbon present just
      before a burn-out was removed during it
  o   Pressure across gasifier gas duct as on-stream
      measure of duct decoking/coking.

The rise in duct surface temperatures due to the exothermic
reaction of carbon and oxygen was observed as expected.
The maximum temperatures observed after the noted time in-
terval from the start of the burn-out, when the reverse
flow burn-out gas was introduced, are listed in Table 6.
When air was used to burn-out, as in Runs 3 and 5, rather
small temperature rises were observed as a result of part-
ial burn-out only.  Comparison of the photographs in
Figures 4 and 6 shows that carbon was only removed from the
primary air pipe outer surface in the direct locality of
the incoming burn-back air.  This poor burn-out performance
with air was a consequence of the gas duct temperatures
being rather low - in the region of 450°C - to initiate
the combustion reaction.  This temperature is lower than
that anticipated in a large continuous CAFB unit gasifier
gas duct.  Duct temperatures in the region of 85O°C have
been observed on the CAFB pilot plant when gasifying
normally.  With air as the burn-out gas the coke/atmospheric
oxygen reaction initiates readily and raises duct temper-
atures rapidly.  The duct temperatures are normally held
down in the region of 12OO"C by mixing the flue gas with
incoming air to control the oxygen concentration in the
burn-out gas and thus to prevent damaging the duct by
excessively high duct temperatures.  In the batch unit
tests large heat losses occurred from the gasifier product
gas in spite of considerable effort in lagging the gasifier,
product gas ducts, and the burners.  The introduction of
the primary air at ambient temperature also had a cooling
effect on the gasifier gas and duct.  This cooling is
clearly demonstrated by the temperature difference of about
15O°C observed between thermocouples A and B.  Coking
occurred preferentially on the cooled primary air pipe
outer surface.  For a scaled-up burn-back burner it is re-
commended that careful attention be paid to the design so
that moving surfaces are out of contact with gasifier pro-
duct gas and that these surfaces are purged with air to
minimise coking.


                            -  28  -

-------
The addition of oxygen to the burn-back air allowed complete
burning of deposited carbon to occur in the batch tests.
This method was used to increase the rate of decoking
because of the low duct temperatures.  Oxygen enrichment
will certainly not be required when decoking hot product
gas ducts on a larger scale gasifier, as described above
when oxygen dilution was required for control purposes.
The maximum burn-back duct surface temperatures observed
in the batch tests were in the region of 600°C and occurred
rapidly after introduction of the air/oxygen mixture.
Primary air pipe outer surface temperatures were in the
region of 15OO°C.  Comparison of the photographs in Figures
4, 5, 7, 8, and 9 shows that the coke was completely burnt
off from the gas duct.

The gasifier product gas produced by the batch gasifier
was similar in composition to that produced on the CAFB
pilot plant.  The product gas was analysed during the
course of several runs by gas chromatography.  This analy-
sis gives an air -, water -, and liquid hydrocarbon - free
basis composition.  The results are presented and compared
with gasifier gas analyses for continuous gasification
pilot plant runs 5 and 8 in Table 7.

The burn-back combustion gas analysis variations during
three of the batch test decokes are shown in Figures 10,
11, and 12.  The peak CO2 concentration occurs at the
time of maximum 02 depletion and maximum gasifier duct sur-
face temperatures, as expected for the exothermic combust-
ion of deposited carbon.  Burn-out gas analyses and gas-
ifier duct temperatures for all the decokes are listed
together with the gasifier operating conditions in Appen-
dix B.

The pressure across the gasifier product gas duct was ob-
served to rise steadily during the course of the gasificat-
ion runs and drop after a decoke.  This method of estimating
the rate and degree of gas duct coking and the degree of
decoking, both whilst maintaining gasification, was eval-
uated since it clearly would be of value when operating a
multi-burner gasifier with on-stream decoking burners.

The initial pressures across the gasifier gas duct after a
decoke are in the region of O.17 ±0.1 kilopascals.
                           - 29 -

-------
COKED-UP PRIMARY AIR PIPE
                           FIG. 4.
         - 3O -

-------
COKED-UP GASIFIER GAS DUCT
                            FIG.5.
          - 31 -

-------
PARTIALLY DECOKED PRIMARY AIR PIPE
                                  FIG.6.
                - 32 -

-------
DECOKED GASIFIER GAS DUCT
                           FIG. 7.
         - 33 -

-------
DECOKED PRIMARY AIR PIPE
                            FIG. 8.
         - 34 -

-------
DECOKED PR I MARY AIR PIPE
       (CLOSE-UP)
                           FIG. 9.
          - 35 -

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                                                  -  39   -
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The variation of the pressure across the gas duct during
the course of the gasification runs is shown in Figure 13.
The slope of the plot of this pressure against the cumulat-
ive total air to the gasifier bed at constant bed temper-
ature, fuel rate, bed depth, and superficial gas velocity
is a measure of the rate of gasifier gas duct coking and
is shown in Table 8.  The rate and degree of gasifier gas
duct coking is dependent mainly on the volume of product
gas passing through the gas duct and the composition of
the gasifier gas.  These two factors themselves are depend-
ent on the gasifier operating conditions.  The volume of
gasifier gas is proportional to the volume of air supplied
to the gasifier bed at constant bed temperature, bed depth,
and fuel rate.

The dramatic rise in the rate of gasifier gas duct coking
at gasifier bed air/fuel substoichiometric ratios less
than about 24% is clearly shown in Figure 14.

Burn-back Burner Performance Data -

It is desirable that low Btu burners should be as compact
as possible so that boiler modifications required for re-
trofits may be minimised.  From this point of view the
burner configuration shown in Figure 2 looks promising and
the following characteristics have been observed:

  o   Very stable flame which did not lift-off at high com-
      bustion intensities nor light-back under low flow
      conditions.

  o   Gasifier product gas throat loading turndown range
      of at least 8:1, where throat loading is the rate of
      flow of gas/unit area between outer surface of primary
      air pipe and refractory lining.

  o   Ignition took place readily.

  o   Quiet operation on ignition, during burning, and on
      extinction.

  o   Complete combustion.  Neither carbon nor carbon mon-
      oxide escaped from the flame when  stoichiometric air
      or greater was supplied.
                             -  40  -
-------
PRESSURE ACROSS GASIFIER GAS DUCT AS A MEASURE
            OF DUCT DECOKING/COKING

1.25

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                   - 41 -
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The normal procedure to determine the limits of flame
stability involves variation of the air supply rate at
given rates of fuel gas supply  (5, 6).  In this way the
locus of lift-off/flash-back points is used to establish
the region of stable flame over the whole turndown range
of operation.  The burn-back burner was tested in this
manner but it proved difficult to supply sufficient air
to extinguish the flame.  The proven region of stable
flame, when the total aeration was at least stoichiometric,
is shown as a function of primary aeration and throat load-
ing in Figure 15.  The range of gasifier product gas,
primary air, and secondary air velocities over which the
flame has been observed to be stable are presented in Table
9, and further details are given in Appendix B.

The combustion diagram for the burn-back burner, based on
batch test runs 11 to 14, is shown in Figure 16.  The
experimental flue gas analyses for C02, CO, and 02 are
superimposed on the theoretical curves calculated from the
combustion model presented in Appendix B.  The very good
correlation of actual flue gas analyses and the predicted
ones confirms that complete combustion of gasifier gas
occurs with the burn-back burner.

Future Design -

A possible full scale version of a burn-back burner which
incorporates the experience gained from the above batch
tests is presented in Figure 17.  It will be noted that
the moving surfaces are out of contact with gasifier pro-
duct gas and that these surfaces are purged with air to
minimise coking.  It will not be necessary for a complete
seal off of the gasifier gas duct from the boiler during
a burn-back  (which would be practically difficult to
arrange) since a small air flow into the boiler will not
seriously affect the operation.
                            - 44 -
-------
FLAME STABILITY—PRIMARY AERATION
100


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BURNER THROAT LOADING, m/s
FIG. 15
             - 45 -
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                            - 47  -
-------
POSSIBLE FULL SCALE VERSION OF BURN-BACK BURNER
                                Gosifier
                                Gas Duct
        Burn-back
        Air 	»rH
        Input            v.
  Retractable
  Axial Support
                                               Axial Swirl
                                               Vanes
Oil
Injector
                                               Refractory
                                               Nose Ring
        NB    in shut position the nose ring plugs
              the Burner Orifice with I/is"- i/a"clearance
              between refractory surfaces
                                                     FIG. 17.
                            -  48 -
-------
Deadburning and Sulphation of Spent Lime

Introduction -

The deadburning and dry sulphation work described  in  this  re-
port was initiated when the CAFB demonstration plant  was
based on the choice of Providence, Rhode  Island  as  the  plant
site, and dry sulphation was the preferred  design  option  for
SC>2 and lime disposal.  However, the current plan  is  for
Foster Wheeler Energy Corporation to build  the demonstration
plant in San Benito, Texas using the Foster Wheeler Resox
process for SC>2 disposal.  In view of this  development  dead-
burning becomes the preferred design option for  lime  dis-
posal.  Consequently the dry sulphation results  obtained  in
this work were not analysed to the fullest  extent  possible.


Dry Sulphation

Background and Objectives -

In the dry sulphation process spent lime  at 80O-900°C in  the
presence of air is used to absorb the SC>2 released  from the
regenerator.  The reactions involved are  as follows:

            CaS + 202        •*"       CaS04    -(1)
            CaO + S02 +^02   =       CaSO4    -(2)
The two by-products are, therefore, treated by  a  single  pro
cess to form a single environmentally acceptable  material
for sale as gypsum or disposal as landfill.

The dry sulphation process has been studied extensively
(1-10 and 13) and theories for the mechanisms of  SO2
absorption have evolved  (10 - 13) .  There would appear to
be two ways in which the sulphation of CaO, reaction  (2) ,
can occur.  The CaO and S02 can react to form CaSO3 which
is subsequently oxidised to CaS04 or else the S02 can be
oxidised to 303 which subsequently reacts to form CaSO4
directly.  Evidence has been presented to support the pre-
dominance of the latter route at temperatures above 850 °C
(11) .
                             - 49  -
-------
An optimum sulphation temperature in the region of  87O°C has
been identified  (Figure 18)v  It is interesting to  consider
why the optimum temperature is so far below 110O°C, the
temperature at which the thermodynamic data would allow a
S02 absorption efficiency of about 90%.

Three factors may be expected to limit the reaction rate be-
tween particulate solids and a gas over a range of  temper-
atues.  These are the rate of the chemical reaction itself,
the rate of diffusion of the gaseous reagents through the
surface film and the rate at which the gaseous reagents
diffuse through the reacted solids.  The observed rate is
never higher than that resulting from any of the individual
steps acting alone, because of the series relationship be-
tween these resistances to reaction.  As can be seen in
Figure 19 , the chemical reaction rate is highly temperature
dependent and soon ceases to be a controlling factor as the
temperature rises.  Film resistance tends to diminish less
rapidly as temperature rises and soon takes over from chem-
ical reactivity as the controlling factor.  Reacted solids
diffusion resistance tends to rise with increasing  temper-
ature.  The combined effect of these three influences is
therefore to produce an optimum temperature for reaction,
but, since the thickness of the reacted solids layer will
increase as the reaction proceeds, it follows that  the
optimum temperature should fall as the solid reagent is
utilised.  The argument suggests that the optimum temper-
ature for the absorption of the gaseous reagent can be
lower than that suggested by thermodynamic considerations.

Prior to the work discussed below there appears to  have been
no sulphation test runs on a semi-pilot plant scale using a
fluidised bed of spent lime discarded from a continuous CAFB
unit.  The objective of the present work was to determine
the practical feasibility under various operating modes on
a semi-pilot plant scale of sulphating spent lime withdrawn
from the CAFB continuous unit.  The target performace factors
were:

     i)  9O% absorption of SO2 from regenerator off-gas
    ii)  90 mole% sulphation of spent lime
   iii) 100% oxidation of residual CaS on spent lime.
                             - 50 -
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                      - 52  -
-------
Fluidised Bed Batch Tests -

The fluidised bed batch sulphation of spent lime tests are
summarised in Table 10.

Purely practical considerations limit the range of choice
available so far as particle size is concerned.  The bed
particles must be small enough to be fluidised at the super-
ficial gas velocity chosen for normal operation, but large
enough to be retained by the cyclones of the reactor.  The
size distribution about the mean will depend upon the method
used to prepare the stone, but sieving must be minimised
since it is desirable to discard as little stone as possible.
Very fine lime, of less than 100 microns mean particle size
is in any case difficult to fluidise and tends to rat-hole.

The fluidisation behaviour in a one inch diameter unit of
fine particles of CAFB regenerator material was not satis-
factory and the bed agglomerated (9).  Consequently the
tests were carried out in fixed beds.  More recent larger
scale batch tests (14) illustrate the difficulty experienced
in attempting to maintain bed fluidisation and in achieving
90% sulphation.

It would appear to be sensible to take advantage of the
higher specific surface of finer material.  Borgwardt
(8) has demonstrated that calcium utilisation in sulphat-
ion increases markedly as particle size decreases; plugging
of the gas-transport pores in the solid becoming less of a
barrier to reaction as the diffusion thickness of the product
decreases.  Thus, following the successful cold fluidisation
of 75 microns spent lime, an attempt was made to operate
the CAFB batch reactor at the sulphation temperature of
850°C.  The fine lime particles become loosely bonded into
cakes very shortly after they were fed into the vessel, as
expected.

A bed of elutriator coarse spent lime material was fluidised
by an SO2  containing gas.  The results were rather disappoint-
ing since  only 66% of the SO2 was absorbed under the test
conditions when the stone was 17 mole % sulphated.  A sample
of the bed material was subsequently sieved into closely
size fractions which were then analysed for sulphur.  The
results which were obtained are shown in Table 11.
                            - 53 -
-------



















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- 54 -
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            Table 11  i  Sulphur in Stone Fractions

         SIZE INTERVAL                  SULPHUR CONTENT
            microns                          wt.  %

          2800 - 1460                       6.32
          1400 - 1180                       6.58
          118O - 850                         6.73
           850 - 600                         7.43
           6OO - 250                         8.13
           250 - 150                         12.74
           150 - 106                         17.34
              < 106                          7.96
The sulphur contents of the two finest fractions are of
particular interest.  A large proportion of the material  in
these fractions was too fine to have been retained by the
bed during fluidisation and was probably produced during
the subsequent sieving operation.  This being so, it is re-
asonable to infer from these results that the dust produced
from the surfaces of the larger sulphated particles is not
pure sulphate but contains a large proportion of lime.  The
implication here is that the depth of penetration of the
particles by 803 is very restricted and that sulphation
proceeds in the main via the internal surfaces of pores and
fissures.  This is supported by the way in which sulphur
content varies with particle size in Table 11.  The 200O
micron stone is about 12.6% reacted and according to the
shell model the 700 micron stone should therefore have been
about 35% reacted whereas in actual fact it was reacted to
the extent of 15.4%.  In a paper by Hartmann and Coughlin
(10) it is shown that sulphation proceeds via pores having
diameters exceeding 4000  A.  It is pointed out by these
authors that the molar volume of CaC03 is 36.9 cm^/mole
whilst that of CaS04 is 52.2 cmVmole.  It follows that the
pores will close up as the sulphation proceeds.  This point
is very clearly illustrated with the data plotted in
Figure 20, which shows the pore size distribution of a sample
of limestone both after calcining and after its subsequent
sulphation.

The possible explanation can be found using the concept of
"grain theory" introduced by Szekely and Evans (12) and
developed by Pigford and Sliger (13) .  The theory assumes
that the porous particles are composed of grains separated
by pores through which the reacting gases diffuse.
                            - 55 -
-------
PORE-SIZE DISTRIBUTION OF THE CALCINED
        AND SULFATED<2)STONE
                                      (I)
 0.5 -
         2.6
3.2
3.8
                4.4
PORE RADIUS, LOG R (A)
5.0
                              FIG. 20.
             -  56 -
-------
The reaction starts on the fresh surface of the  subparticles
at high rate.  The CaSO^j accumulates on the surface  of  the
grains and the diffusional resistance increases  rapidly as
the reaction proceeds.  The volume of each subparticle  grows
and the porosity of the particle decreases as described in
Figure 20.  After some elapsed time the resistance of the
CaS04 film is so large that 803 can no longer reach  the
active CaO in the grain.  Although the particle  can  still
show some porosity at this stage and 863 can slowly  pene-
trate its interior, the reaction effectively ceases  for
practical purposes.  Following this line of argument it is
concluded (10) that it is difficult to sulphate  lime in a
dry process to a greater extent than 6O% reacted without
in some way modifying the particle structure during  the
reaction.

Two approaches to this problem were explored in  the  batch
and continuous studies:

  1.  The injection of fine spent lime particles into a
fluidised bed of coarser particles of spent lime or  an  inert
material which was used to hinder the entrainment of the
fines.  This procedure enabled advantage to be taken of the
large surface area of the fine lime whilst ensuring  that the
quality of fluidisation was maintained and the mean  residence
time of the fine particles was increased.

  2.  The injection of coarse spent lime particles into a
fluidised bed of particles of an inert abrasive material,
such as silicon carbide, which is used to try to grind  the
injected lime.  The fracture of the polycrystalline  spent
lime would produce fresh CaO surfaces and allow  rapid sul-
phation to be maintained giving high CaO conversion.

In batch run 3 spent lime (10% of total bed weight)  of  356
microns mean particle diameter was added to a fluidised bed
of silicon carbide of mean particle diameter 47O micron
(Table 1O).   Kerosine was added to the bed to maintain  the
temperature; this together with the carbon of thestone
resulted in about 10% vol. of CO2 in the exit gas.   The sul-
phation profile for the run is shown in Figure 21.   The fine
bed material was 50 mole % sulphated after about 2 hours re-
action.  The cyclone material was sulphated to the same
extent as bed material of the same size range.   The  corres-
ponding S02 absorption was about 24%.  The maximum calcium
oxide to sulphate conversion of fine bed material of 58 mole
% in this batch run is the highest yet achieved  in a fluid-
ised bed on a relatively large scale.  A reaction time  of
                            - 57 -
-------
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                                  - 58  -
-------
about 10 hours was required to compensate for  the  considerable
drop off in reaction rate with increased sulphation.   It  took
a further 8 hours after 5O mole  % sulphation to  sulphate  the
spent lime a further 8 mole %.   It was not possible to sul-
phate the spent lime beyond the  maximum of 60 mole % predicted
by Hartmann and Coughlin  (1O).   There was no evidence  for
the occurrence of bed grinding from the observed bed and
cyclone sieve analyses.  The  overall spent lime  and sulphur
recovery was about 90%.

Fluidised Bed Continuous Feed Sulphation Tests - It is not
sufficient merely to demonstrate high levels of  sulphation
by means which would not be practical on a commercial  basis.
The operation of a large scale batch sulphator with reaction
times of the order of 10 hours or more was considered  to  be
not commercially viable.

Two possible continuous feed  sulphator designs were tested
out in Runs 4 to 10.  One of  these designs is  illustrated in
Figure 22; operation on this  continuous feed basis has a
number of advantages over batch-working:

  1)  less storage of discarded  CAFB material  is required.
  2)  consequent reduction in fuel costs otherwise required
      to reheat the material  to  the optimum operating  temp-
      erature .
  3)  sulphated product is automatically elutriated into
      the cyclones.
  4)  coarse inert material,  if  any, in the bed  is separated
      from the product rather than requiring sieving off  at
      the end of the batch run and subsequent  reheating.
  5)  elutriation of the product allows the maintenance of
      a constant bed depth.

Six continuous sulphation runs covering a wide range in
operating conditions (Table 12)  were carried out.  Both
spent lime and silicon carbide initial beds were tested.
The detailed operating conditions are given in Tables  D.3
to D.ll in Appendix D.

An alternative continuous operation was tested.  Sulphated
lime was withdrawn directly from the fluidised bed rather
than from the cyclone.   This  method has the advantage  that
lower superficial gas velocities may be used.  The detailed
operating conditions are given in Tables 12, D.9, and  D.ll.

All of the runs demonstrate that continuous-feed dry sulphat-
ion is unlikely to be commercially or technically feasible.
The maximum calcium oxide to  sulphate conversion achieved
was of the order of 4O mole %.
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                                            -   61   -
-------
Deadburning of Spent Lime
Background and Objectives -

It was considered that the spent lime could be rendered inert,
and therefore suitable for disposal, by sintering at high
temperature.  This process would be used in conjunction with
a process for reducing SC>2 to elemental sulphur.  Although
two processes and two products are involved in this route
one of the products, sulphur, is marketable and the other,
sintered lime, could be produced in relatively small amounts
by minimising the gasifier bed replacement rate.  Gasifier
bed stone replacement could be reduced to the minimum
necessary to maintain satisfactory sulphur removal efficiency
as it would be independent of the regenerator SC>2 output.

Deadburning of the lime in the temperature range 15OO to
1700PC has been reported  (16) to virtually eliminate its
chemical activity.  The material produced is practically
as inert and stable as its limestone antecedent.  Compared
with normally calcined lime, it has a much higher specific
gravity and greatly reduced porosity.  In addition, tests
at Westinghouse Research Laboratories have indicated that
chemical activity of spent lime from the CAFB process can
be virtually eliminated when it is exposed to 14OO°C for
1 hour (Table 13) .
                          TABLE 13

         Effect of Temperature on Spent Lime Activity

Sintering Temperature,        Temperature Rise of Hydration
   No treatment                            77.5
   1200                                    28.5
   1400                                     0.38
   1500                                     0.36
   1550                                     0.24

It was considered that deadburned lime of this nature would
age on exposure to the weather to form inert CaC03 over a
prolonged period of time.
                            - 62 -
-------
The rapid material temperature rise due to the evolution  of
heat from the "slaking" reaction between finely divided
calcium oxide and water to produce water soluble  calcium
hydroxide was not expected.

The objective of the present work was to examine  the  feas-
ibility of spent lime sintering as a means of treatment
which is environmentally acceptable before disposal as land-
fill.

The test programme was to produce a range of sintered spent
lime samples, varying the sintering temperature and durat-
ion.  These samples were exposed to weathering over a twelve
month period.  The temperature changes relative to ambient
conditions were monitored and compared with a non-sintered
spent lime sample under similar conditions.  The  chemical
compositions of the spent lime and the rain water which had
leached through the samples were determined at regular in-
tervals by analysis.
Discussion of Results

Six containers were left outside and rainwater was allowed
to leach through the sintered spent lime in the upper vessel
and into the lower one, as shown in Figures 23 and 24.

A maximum temperature rise of 5°C above ambient was steadily
built up after 2O hours of exposure to weather for the sin-
tered spent lime.  This behaviour was in marked contrast to
that of non-sintered spent lime which showed a 3O°C rise in
the first hour of weathering due to the rapid 'slaking1 of
the calcium oxide by atmospheric water vapour.  The temper-
ature profiles of all the sintered spent lime samples were
similar and independent of the sintering conditions.  The
temperature profiles of sintered and non-sintered spent lime
are shown in Figure 25.

Within two weeks weathering, all sintered spent lime samples
had formed a crust over the upper surface which was most in
contact with atmospheric C02, water vapour, and rainwater.
The material was normally thoroughly mixed every month to
ensure that the sample taken was homogeneous.  The effect
of weathering on the molar % of total calcium for CaO,
Ca(OH)2/ CaC03, CaS, and CaSC>4 is shown in Figures 26 and
27 based on the analyses and chemical compositions given
in Appendix C.
                            - 63 -
-------
Fig 23 Weathering of Sintered Spent Lime
                -  64 -
-------
Fig 24  Weathered Sintered Spent Lime after 12 Months
                     - 65  -
-------
EFFECT OF WEATHERING ON SAMPLE TEMPERATURE
  FOR SINTERED AND NON-SINTERED SPENT LIME
                  NON- SINTERED SAMPLE

                  ALL SINTERED SAMPLE
  20
40    60    80     100
HOURS OF WEATHERING
                 -  66 -
-------
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                                                    -   68  -
-------
The following conclusions may be drawn from Figures 26  and
27:

o  Variation of the sintering conditions within the range
   1 hr. at 1350°C to 3 hr. at 155O°C had no effect on  the
   chemical changes which occurred on weathering.

o  The chemical changes occurred steadily during weathering
   and were not dependent on the monthly rainfall.

o  All CaO was converted to Ca(OH)2 after 2 months weathering.

o  After 12 months weathering the sintered spent lime consists
   mainly of Ca(OH)2 and CaC03 in 1:1 molar ratios.  The
   CaC03 was formed from the Ca(OH)2«

o  Weathering occurred faster in the top layer crust of the
   sintered lime.  For December and January the samples were
   taken from this crust.

o  The experimental scatter of the data is a measure of the
   effectiveness of the monthly mixing operation.

The weathering rate was greater under the test conditions than
would occur naturally with landfill since the test material
was regularly mixed.  This repeated exposure of fresh reactive
material would not occur during landfill operations.

The analyses of the sintered spent lime leachates are given
in Appendix C.  The evaporation losses from the leachates in
the lower containers were analogous to those of a stagnant
pond.  The maximum concentrations of various metals are com-
pared with World Health Organisation Standards for Potable
Water in Table 14.
                            - 69 -
-------
               Table 14 :  Leachate Analyses
METAL
CONCENTRATION
MAX. , ppm
MONTH
SINTERING
TEMP. °C
TIME, hr.
Ca
2800
June
1450
3
Mg
3.1
June
1350
1
Si
13
NOV.
1350
1
Fe Al
0.2 
-------
CONTINUOUS PILOT PLANT STUDIES


Analysis of Continuous Runs  8 and 9

Outline of Method of Analysis -

A previous report in this series  (2) describes how  the
data from Continuous Runs 6  and 7 were analysed.  Essent-
ially the hourly readings were grouped into  ten hourly
sets of data in which conditions were sufficiently  constant
to allow meaningful average  values to be derived.   A major
drawback in such an approach is that not all the data can
be used.  Gross effects were identified by plotting % sulphur
removal efficiency  (% S.R.E.) against individual independent
variables such as bed depth  or bed sulphur concentration.
This approach is excellent if the experimental design is such
that only one significant variable is altered at any given
time.  Unfortunately this is not always possible and the
effect of one variable can often be obscured by variations
of another.

The method of analysis used  for Runs 8 and 9 differed from
that adopted for previous runs in that the hourly readings
were treated separately.  Stepwise multiple regression
analysis was used to identify the contribution of signific-
ant process variables and empirical equations were  developed
to predict the % S.R.E. for each separate hour of the runs.
The underlying objective in  this approach was to use all
the data generated throughout the runs or at least  to just-
ify any that needed to be discarded.

Initially, Runs 8 and 9 were treated separately and regress-
ion equations were developed to explain each set of data.
The two runs were then looked at as a whole to try  to syn-
thesise the two sets of observations to give one common
picture or at least to identify why they should differ.

A useful tool in developing  the regression equations and
identifying significant variables was the graph plotting
qomputer programme written to generate the run graphs shown
in Appendices F and G.  Each time a regression equation was
developed the residual error between the hourly predicted
values of % S.R.E. and the experimental values were plotted
as a function of time throughout the run.  Thus it  was
possible to zero in on large differences between the pre-
dicted and actual values of  % S.R.E. and with the aid of
the run log-book identify the factors responsible.
                            - 71 -
-------
The approach outlined above can only be successful if the
time lag between a change in process conditions and a sys-
tem response in terms of % S.R.E. is comparatively short, ie,
a matter of minutes rather than hours.  Thus the apparent
success of this approach indicates short line-out times for
the process.

Further details of the method of analysis including pro-
rammes and data editing are to be found in Appendix H of
this report.

Summary of Process Data for Runs 8 and 9 -

A useful aspect of regression analysis is that it provides
summary statistics which help to give an insight into what
happened during the two runs.  Table 15 lists the mean values
for the % S.R.E. together with several key process variables.
Also listed is the standard deviation of each of the vari-
ables which is a measure of how that variable was changed
throughout a run.  Obviously an important variable which
significantly affects the process can be overlooked if it
is kept constant throughout the run.  In assessing the
effect of a variable on the % S.R.E. it is important to
know:-
  (1)  Over what range the variable was changed.
  (2)  What proportion of the time the variable was
       significantly different from the mean value.
The standard deviation gives a measure of both these aspects.
Two thirds of the hourly data lie within one standard de-
viation of the mean value whereas 95% of the data lies
within two standard deviations of the mean value.

% Sulphur Removal Efficiency -  Table 15 shows that the over-
all performance in terms of % S.R.E. for both Runs 8 and 9
was similar.  The mean value for the % S.R.E. of Run 9 was
only slightly better than Run 8.  Comparison of the stand-
ard deviation of this variable shows that there was less
variation about the mean value in Run 9 compared with Run
8.  This is an important observation and will be returned
to later in the discussion.

Bed Depth -  One of the objectives of Run 9 was to explore
deeper beds than previously and this is reflected in a
larger mean bed depth of Run 9 compared with Run 8.  A
larger standard deviation indicates that this variable was
also changed more widely in Run 9 than in Run 8.
                            - 72 -
-------
TABLE 15
Summary Statistics for Runs

Variable
% Sulphur Removal
Efficiency
Bed Depth (cm)
Bed Temper at ure( °C)
Air/Fuel Ratio
Cyclone Drain
Temper at ure( °C)
Added Water (m3/hr)
% Bed Fines (60O-25O/O
Bed Carbon (wt%)
Bed Sulphur (wt%)
Bed Velocity(m/sec)
Ca/S \tole Ratio

Mean
Value
77.1
91.0
891
23.9
365
16.6
16.4
0.3
5.2
1.62
1.58
Run 8
Standard
Deviation
10.8
11.8
13.2
1.9
109
13.1
3.7
0.5
1.8
0.17
0.7
8 and 9
Run
Mean
Value
79.1
103.1
921
26.9
356
4.75
18.4
0.24
4.5
1.7O
1.23
9
Standard
Deviation
6.8
14. 0
24.5
3.4
134
8.6
5.9
0.5
1.1
0.23
0.9
 - 73 -
-------
Bed Temperature and Air Fuel Ratio -  On average Run 9 oper-
ated at higher bed temperatures compared with Run 8 and we
can see this was largely achieved by operating at a higher
air/fuel ratio.  Comparison of the standard deviations of
both these variables indicates Run 9 again operated over a
wider range.

Cyclone Drain Temperature -  This variable was used as a
measure of the amount of fines circulating from the gasifier
bed to the cyclones.  In practice, the average of the two
cyclone drain temperatures was used to represent this vari-
able.  One might expect it to be related to the bed depth
and indeed inspection of the correlation matrices presented
in Tables H-I and H-II in Appendix H shows that particularly
for Run 8 ,a strong correlation exists.  After the completion
of Run 8 but before Run 9/ modification of the gasifier unit
to expand the free board space above the bed was carried
out.  The intention was to reduce the amount of fines cir-
culation and indeed the higher cyclone drain temperature
for a lower bed depth in Run 8 compared with Run 9 reflects
this design modification.

Added Water -  Table 15 shows that the amount of water added
to the gasifier during Run 8 was almost four times that
during Run 9.  To a large extent this was fortuitous.
During Run 8 a consignment of fuel oil with an unexpectedly
high level of water contamination was delivered to the bulk
storage tanks.  This resulted in periods of operation dur-
ing Run 8 when an emulsion of fuel oil and water containing
at times up to 27% water was added to the gasifier.  Another
major source of water was that introduced during flue gas
recycle.  The flue gas is passed through a water scrubber
system before it is introduced into the gasifier and con-
sequently is saturated with water vapour.  A third source
of water was steam injection into the plenum air which was
carried out over an approximate eight hour period during
Run 8.

Bed Finejs -  Samples of  the bed material were taken per-
iodically throughout each of the runs and subjected to
sieve analysis.  Only  a  small proportion of the stone
feed below  250y was retained in the bed  and the smallest
significant faction was  that between  600-250y.  The per-
centage of  the total bed material which  lay within the
range was used as an indicator of bed fines.
                            - 74 -
-------
Bed Carbon and Bed Sulphur -  Comparison of these  two vari-
ables indicates that the mean values for both runs are re-
markably similar.

Ca/S Mole Feed Rate -  On average slightly less feed mater-
ial was used in Run 9 compared with Run 8.  Again  this
variable was studied over a wider range in Run 9 than in
Run 8.

Bed Velocity -  Except for some brief excursions,  the bed
velocity was kept reasonably constant at about one m/sec.
throughout both runs.

An interesting aspect of the summary statistics in Table 15
is that with the exception of added water and to a lesser
extent bed sulphur all the other key process variables were
changed over a wider range in Run 9 compared with Run 8 and
yet in terms of % S.R.E. the reverse is true.  This can only
be explained if added water  (or bed sulphur) has a large
effect on % S.R.E.  In fact it was evident at the time when
high water levels were discovered in the fuel during Run 8
that this variable had a pronounced detrimental effect on
performance.

Linear Regression Equations for Run 8 and 9 -

As a result of a detailed analysis of the data (see Appendix
H) and evaluation of a large number of variable combinations,
six variables were chosen which best represented the results
for Runs 8 and 9.  The linear regression equations developed
around these variables are presented in Table 16.  The only
variable which needed to be forced into the regression
equation was cyclone drain temperature for Run 8 and this
was due to the high correlation between this variable and
bed depth for that run.  More accurate equations were ob-
tained by using the square of the variable 'added water"
and hence the regression coefficient listed in Table 16 re-
ports the square of this variable.

Also included in Table 16 is the residual error of each re-
gression equation and the '% explained1 by the regression
equation.  The residual errors for both equations are
virtually identical.  The % explained is a measure of how
much of the variance in the % S.R.E. is predicted by the
regression equation.  A higher % explained for Run 8 is a
direct result of the greater variation of % S.R.E. in Run
8 and not due to a lower residual error.
                             - 75 -
-------
                          TABLE 16^

          Linear Regression Equations to predict
                 % S.R.E. for Runs 8 and 9
                               Run 8
Run 9
Variable
Bed Depth (cm)
Bed Temperature (°C)
Air/fuel Ratio
Cyclone Temperature ( °C)
*Added water (m3/hr)
Ca/S Mole Ratio
Constant
Residual Error
% Explained
Regression
Coefficient

0.15
-0.035
0.94
0.0065
-0.011
1.96
71.8
3.94
86.8
Regression
Coefficient

0.17
-O.073
0.38
0.017
-O.O11
1.18
112.3
4.06
64.5
* square of variable
                          - 76 -
-------
Comparison of the  regression  coefficients  for  the  two runs
shows some interesting  consistencies  and  anomalies.   All the
coefficients are directionally  the  same in both  runs  although
the magnitude of the  contribution is  different for some  of
the variables.  The coefficients which compare favourably
are for bed depth, added water, and to seme  extent Ca/S  mole
ratio.  Those for  bed temperature,  air/fuel  ratio  and cy-
clone drain temperature are less consistent  and  this  raises
the question why this should  be.  Previously mentioned
design changes  could  account  for the  different cyclone
drain temperature  effect but  it is  difficult to  see why  this
should also affect bed  temperature  and air/fuel  ratio.   To
further test whether  the runs are in  fact  different,  the
regression equation for Run 8 was used to  predict  the mean
value for Run 9 and vice versa.  Table 17  shows  the results
of this calculation.  A feature of  regression  analysis is
that it arranges the  equation constants to predict the mean
of the data precisely so that Run 8 equation predicts Run 8
mean precisely  and similarly  Run 9  equation  predicts  its
mean precisely.  However, the Run 8 equation badly over-
predicts the performance of Run 9 whereas  Run  9  equation
under predicts  Run 8  performance.

Analysis of Run 8  and 9 Data  to determine  the  Non-Linearity
of Regression Variables -

One explanation for the poor  predictions of  the  regression
equations shown in Table 17 is that the regression variables
are not linear.  To test this assumption the following pro-
cedure was adopted:-

(1)  Assume as  a first  approximation  all the regression
     variables  are linear except one  and correct the  % S.R.E.
     experimental  values using the  linear  regression  co-
     efficients for deviations away from the mean  values of
     these five variables.

(2)  Plot the corrected % S.R.E. values against  the remain-
     ing variable  and to improve the  accuracy  average the
     data into boxes, eg, for bed depth average  the results
     between 5O-60 cm,  6O-7O  cm etc.

(3)  Repeat for each  variable in turn.

(4)  To compare on a  common basis Runs 8 and 9 the mean  of
     the two population means in Table 15  was  used.

An example of the  computer programme written to  carry out
this task is 'DLRESIDA1  listed in Appendix H.

                            -  77 -
-------
                           TABLE 17

       Prediction of Run 8 Data from Run 9 Regression
                   Equation and Vice Versa
                    Run 8                     Run 9
Equation    Mean % Sulphur Removal    Mean % Sulphur Removal
  Used            Efficiency                Efficiency


            Actual       Predicted    Actual       Predicted
Run 8        77.1          77.1        79.1           83.4

Run 9        77.1          74.9        79.1           79.1
                           - 78 -
-------
Figures 28-33 show  the end product  of  such  an  analysis  for
both Runs 8  and 9.   The numbers bracketed against  the points
refer to the number  of hourly readings contributing  to  each
data point.  Obviously the larger this number  the  more
accurate the data point and  the greater  the weight that can
be attached  to its value.

A striking feature of this approach is how  consistent the
two runs now appear  and shows that  the inconsistencies  in
air/fuel ratio and bed temperature  were  entirely due to
the fact that these  variables were  non linear.

Development  of Polynomial Equations for  Runs 8 and 9 -

A standard programme "Polynomial-Fit"  also  available on the
Honeywell MKIII Foreground system was used  to  find a poly-
nomial expression for each of the relationships given in
Figures 28-33.  This routine programme calculates  coefficients
and comparative data for fitting polynomials of the follow-
ing form:-

     Y = A + Bx + Cx2 + D3 + — 14x7

where the coefficients may or may not be zero.

A valuable feature of this programme is  that it allows
weighting factors to be applied to  the data points and  the
hourly readings bracketed in Figures 28-33 were used in this
way.  Table 18 gives the most significant polynomial ex-
pressions for each of the six variables  and compares the
standard error of the polynomial expression with the cor-
responding linear expression.  In the case  of bed  depth
and cyclone temperature the best polynomial is in  fact  a
linear expression.  However,  for the other four variables
a considerable improvement in accuracy can be achieved
as might be expected by drawing a curve  through the data.

Using the polynomial expression for each variable, the
data for Runs 8 and 9 were re-analysed separately  to gen-
erate the regression constant and the residual error and
'% explained' for the new polynomial equation.  The relev-
ant information obtained is given in Table  19.  A  slight
improvement in residual error and '% explained' over the
linear equation is noted.   Comparison of the regression
constants shows that Run 8 equation now  over-predicts Run
9 by 2.4% whereas Run 9 underpredicts Run 8 by the same
amount.
                            - 79 -
-------





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                             -  87  -
-------
In establishing the non-linearity of one regression variable
it was necessary as a first approximation to assume linearity
of the other five and correct the % S.R.E. values accord-
ingly.  Obviously the process can be repeated this time
using non-linear corrections for the other five variables.
Such an approach would undoubtedly bring the two regression
equations further into line but the exercise is costly in
time and effort and enters the area of diminishing returns.
A simpler approach to produce an overall mathematical
equation for Runs 8 and 9 is to take the mean value of both
regression constants.

Analysis of Run 8 and 9 Data to Determine Significance of^
Variables not Included in Regression Equations -

Since the non-linear feature of the variables has been ex-
plored, only two factors can now be responsible for the
residual errors of the polynomial regression equations ie.

     o  random experimental error

     o  signficant variables not included in the regression
        equation.

Undoubtedly a large proportion of the residual error is in
fact random experimental error and this is evident from the
the graphs of residual error as a function of time.  Never-
theless, it is instructive to analyse additional variables
to see whether their incorporation in the regression equat-
ion would contribute to the accuracy of the prediction and
hence reduce the residual error.

Four variables, bed sulphur, bed sulphate, bed fines and
bed carbon were analysed in this way and the results are
presented in Figures 34-37.  Again the results were aver-
aged in boxes and the bracketed numbers refer to the number
of contributing hourly readings.

% Bed Fines  (60O-25Qyi) -  Analyses of the residual error
from the polynomial equations for Run 8 and 9 with respect
to bed fines  (6OO-250p) is presented in Figure 34.  Over the
range 10%-30% no systematic trend is evident which implies
that this variable does not influence the % S.R.E. over the
range studied.
                             -  88  -
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                                             -   92   -
-------
Bed Sulphur  (wt%) -  Throughout Runs  8 and 9 the bed sulphur
level varied over the range 2-12 wt% whereas previous results
for Runs 6 and 7 were restricted to a maximum level of 6 wt%.
Fig. 35 shows a definite trend towards a reduction of desul-
phuring performance with high bed sulphur levels for Run 9
but this is not borne out by the Run  8 results which indic-
ate the opposite.  Interpretation is obviously made diff-
icult by the limited number of data points at high bad
sulphur levels and further tests are needed to identify the
effect of this variable.

Bed Sulphate (wt%) -  Figure 36 shows that up to 0.8 wt%
sulphate levels the % S.R.E. remains unaffected.  The in-
dications from start up results after sulphation are that
performance is affected at high sulphation levels but
within the range 0-0.8 wt% no detectable effect is noted.

Bed Carbon (wt%)  -  Figure 37 shows the results obtained
with bed carbon as a variable.  Unlike the other variables,
a definite trend downwards particularly for Run 9 data is
evident from the graph.  This indicates that at high levels
of bed carbon,  sulphur removal performance is impairad.
However, at the present time a question-mark hangs over
the precision of the method used to analyse carbon lavels
on limestone and consequently this variable has not been
incorporated into the regression equation.

Applying the Regression Equation to Earlier Runs -

Previous runs have been analysed in a different mannar and
obviously these runs warrant re-analysis in the light of
the apparent success of the new approach.  As a preliminary
step, the equation has been used to predict the desulphur-
ising performance of Run 6 and 7.  Table 20 shows the results
of this analysis for the ten hourly average readings of %
S.R.E.  Unfortunately, the cyclone drain temperatures for
this earlier runs are not comparable with Runs 8 and 9 due
to equipment changes.  Furthermore, the bed depths recorded
in Runs 6 and 7 were approximately half that of the later
runs.  Since bed depth and fines circulation (cyclone
temperature)  are loosely correlated this would suggest a
lower contribution from this variable.  However, this was
compensated by a smaller free-board space above the bed.
As a first approximation therefore the mean value of cy-
clone drain temperature for Runs 8 and 9 was taken as
consistently applicable to the earlier runs.
                             93 -
-------
TABLE 20
Prediction of Averaged % S.R.E. from Runs
Run No
7
7
7
7
7
7
7
7
7
6
6
6
6
6
6
6
6
6
6
Using Developed
Time of First
Reading
4.O63O
5.0230
6.1830
7.1430
9.2130
11.0930
13.OO30
13.1530
14.1630
MEAN
2-0830
3-0430
6-2230
8-O43O
9-O03O
11-0630
12-2030
15-1330
16-1930
19-1730
MEAN
Equation for Runs 8 &
Actual
% S • R. • E •
77.5
80.0
67.5
67.5
70.0
78.0
81.0
8O.O
77
75.4
75.5
80.0
80.0
71.5
71.5
84.0
82.0
82.0
71.5
78.5
77.7
Predicted
%Q TJ TT
O . X\ • J2j .
71.1
71.5
69.4
71.0
71.2
74.0
77.4
72.3
72.2
72.2
63.7
66.7
67.7
61.5
62.4
70.4
63.1
60.0
65.3
58.4
63.9
                     Difference

                         6.4
                         8.5
                        -1.9
                        -3.5
                        -1.2
                         4.0
                         3.6
                         7.7
                         4.8
                         3.2

                        11.8
                        13.3
                        12.3
                        10.0
                         9.1
                        13.6
                        18.9
                        22.0
                         6.2
                        20.1
                        13.8
 -  94  -
-------
Good agreement between the predicted  and  actual  % S.R.E.
for Run 7 has obviously been obtained but  the observed
results for Run 6 are much better than predicted.  This is
an important observation since detailed analysis of  this
run may reveal the factor responsible for  this superior
performance.

Use of Aragonite -

Throughout Runs 8 and 9, BCR 1359 limestone was  exclusively
used except for two short periods in  Run  9 when  Aragonite
stone was used.  During the periods of operation on  Arago-
nite, analysis of the flue gas SC>2 was made difficult by
the tendency of the stone to quickly  reduce to powder form
and to coat the sample line filter resulting in  erroneous
S02 readings.  Because of this, the periods of Aragonite
use were eliminated during data editing (see Appendix H)
and hence the mathematical equation was developed entirely
from experimental data using BCR 1359.

To compare the effect of the two limestones on sulphur re-
moval efficiency the results were analysed in the follow-
ing way:-

(1)  The average % S.R.E. values for  the Aragonite periods
     were compared with average values for BCR 1359  for
     periods immediately before and after Aragonite  use.

(2)  The developed mathematical equation  for BCR 1359 stone
     was used to predict the average  values for Aragonite.

Table 21 shows the results of this analysis together with a
sulphur balance for the periods under review.  As ex-
pected, the predicted values for the  periods of BCR  ..359
use compare well with the actual values but the  actual
values for Aragonite use are superior to  those predicted
by the equation.

The important question is whether this apparent  improvement
is due to the quality of limestone or due  to inaccuracy in
the measurement of flue gas SC^.  In  this  respect the sul-
phur balances of Table 21 are revealing.   The %  Sulphur
Imbalance is a measure of the amount  of sulphur not
accounted for during that period of operation.   In the
case of the BCR 1359 periods, on average  about 12% of the
sulphur remained unaccounted for whereas  for the Aragonite
periods this increased to about 23%.  The  implication of
this is that in fact the performance  of the two  stones was
similar and the apparent superior performance of Aragonite
was due to the powdered stone coating the  sampling filter
and giving artificially low readings  for  flue gas S02.

                            - 95 -
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- 96 -
-------
Injection of Sulphur Compounds  and  Steam  into  Gasifier  Bed -

During Run 9 various sulphur  compounds were  injected  di-
rectly into the gasifier bed  whereas during  Run  8  steam was
introduced by injecting it  into the plenum air.

Sulphur Compounds -  Table 22 shows  the effect  of injecting
H2S, SC>2 and thiophene into the middle of the  bed  through
a central tapping.  The rate  of sulphur injection  from
these additives corresponded  to approximately  25%  of  the
total sulphur added via the fuel during the  period of in-
jection.

Throughout the period when  both S02 and H2S  were injected,
the level of flue gas SC>2 remained  unaltered indicating
that the injected material  was  completely absorbed by the
bed.  However, in the case  of thiophene the  percentage
increase in the flue gas SO2  level was exactly the same as
the percentage increase in  total sulphur  added to  the bed
indicating that the sulphur removal efficiency for this
additive is identical to the  efficiency of removal of
fuel sulphur.

Steam -  During the period  7.1630 to 8.0030  of Run 8  steam
was injected into the plenum  air to assess the effect on %
S.R.E.  At the same time flue gas recycle was  reduced to
compensate.  The observation  at the time of  the  experiment
was that flue gas S02 levels  increased and indeed  added
water whether by steam injection, water saturated  flue  gas
recycle or emulsion of water  in the fuel has been  shown to
detrimentally affect performance.  In fact,  the  results
during the period of steam  injection were treated  in  the
normal way for added water  and  contributed to  the  data  used
to develop the regression equation.

Experiment with Movable Fuel  Injector -

At the end of Run 8 a short experiment was carried out  using
the bottom fuel injector to try to determine the effect of
bed depth on % S.R.E. in isolation of the other  process
variables.  The bottom fuel injector was progressively  moved
up through the bed effectively  changing the  bed  depth avail-
able for desulphurizing the fuel.

Unfortunately, the experiment was not as simple  as  first
envisaged and this was indicated by the fact that  the temp-
erature of the bed increased progressively as  the  injector
                           -  97  ^
-------




















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moved up through the bed.  The results of this study are
presented in Table 23.  At the maximum travel of the injector
('effective' bed depth 45.5 cm) readings at two different
bed temperatures are recorded.  In order to obtain the lower
temperature reading, the air flow had to be reduced.  Pre-
dicted values of % S.R.E. were obtained from a regression
equation using bed depth and bed temperature as the only
independent variable.  These together with the regression
equation are also given in Table 23.

The main point to note is that the correlation coefficient
for bed depth obtained in this analysis compares closely
with that produced from the regression analysis of the
bulk data.  The adverse effect of bed temperature, however,
is markedly higher and this warrants further study.
                           - 99 -
-------
                          TABLE 23
Effect of Position of Bottom


Movement Effective
(cm)
0
5
47.
47.
5
Bed Depth
(cm)
93
88
5 45.5
5 45.5
88
on % S . R . E .

Bed
Temperature
(°C)
899
903
945
915
902
Fuel Injector

% S.R.E. %

S.R.E.+
(Actual) (Predicted)
78.9
74.6
53.5
62.8
74.8
77.6
75.3
53.4
62.7
75.6
+ % S.R.E. = 0.22 x Bed Depth  (cm) - 0.3 x Bed Temperature
             (°C) + 249.2
                           -  100'-
-------
Retention of Trace Elements

In addition to a high sulphur content, heavy fuel oil con-
tains several other elements which can also be captured by
the CAFB process.  Previously reported work  (2) indicated
100% retention of vanadium, 36% reteation of sodium and
75% retention of nickel on the gasifier bed material.
This work was carried out during Run 5 of the continuous
unit and applies to both BCR 1691 and Denbighshire stone.
No measureable difference in the ability of these stones
to capture trace elements was identified but the BCR 1691
was subject to severe attrition, and high dust losses from
the system (^40%) were observed.

Retention of trace elements by the CAFB process is important
for several reasons.  Firstly these elements may be pollut-
ants in their own right and any process which reduces their
emission is desirable.  Secondly, elements like vanadium
are a major cause of boiler corrosion and removal of this
material from the boiler fuel should alleviate this problem.
Finally, enrichment of the bed material may be sufficiently
high to enable the spent bed material to be used as an ex-
tractable ore eg. recovery of vanadium apparently becomes
commercially viable above 2 wt% on spent stone.  This would
provide an attractive solution to the problem of spent lime
disposal.

To investigate the retention of trace elements by BC:* 1359
the period of gasification 10-1630 to 13-0030 for Run 9 was
selected for more detailed analysis.  Throughout this per-
iod the unit operated comparatively trouble free witn a
more or less constant bed level, stone and fuel feed rates.
The important operating conditions for this analysis are
given in Table 24.
                            - 101 -
-------
                          Table 24

            Operating Conditions for Period LO-1630

                      to 13-0030 for Run 9

Gasification time:- 57 hours
Total feed oil supplied:- 8670 kilograms
Total stone feed  (calcined):- 421.5 kilograms
Total stone recovered (calcined):- 393.4 kilograms
Total bed material  (calcined):- 422 kilograms

Gasifier bed temperature:- 91O + 10°C
Gasifier bed depth      :- 117 + 2 on
Ca/S mole feed rates    :- 0.95 + 0.3

Maximum Enrichment Factor:- 20.6
This shows the total stone addition to the gasifier during
this period was equal to the complete bed weight and there-
fore the period under review (57 hours) represents tie res-
idence time in the bed of an average particle of bed
material.  The ratio of the total fuel supplied to the total
stone supplied (measured as calcined material) gives the
maximum enrichment factor assuming 100% retention.  This
implies that with a homogenous distribution of the trace
element on the bed stone, the maximum enrichment at a one
mole feed rate is approximately twenty times the level in
the fuel.  In the case of the vanadium for example at a
level of 300 ppm in the fuel the maximum concentration would
be 6OOO ppm.  In order to achieve bed concentrations of
^2% vanadium an enrichment factor of about sixty six is
required implying a feed rate of about 0.3 molar.
                            - 102 -
-------
                          Table 25

            Stone Inventory for Gasification Period

                 10-1630 to 13-OQ3Q for Run 9

Location                                  Equivalent Burnt
                                          Stone  (kilograms)

Elutriator Coarse                                159
Elutriator Fines                                  41
Boiler  (back and flue)                           116.6
Regenerator Cyclone                               19
Gasifier  (samples)                                 16.2
Regenerator (samples)                             31.0
Bed depth correction                              10,6
Total stone recovered                            393,4
Total stone feed                                 421,5
Table 25 shows the stone inventory for the gasification
period under review.  Approximately 7% of the stone was not
accounted for which compares favourably with the overall
stone balance for the run which shows a 12% deficit.
Assuming that no bed sampling or recovery of material from
the elutriator coarse was carried out, it is possible from
table 25 to assess the minimum stone feed rate needed to
maintain a constant bed depth.  Because stone losses to the
boiler were high due to inefficient cyclone operation, a
feed rate of 0.5 molar was required simply to maintain bed
level.  More efficient first stage cyclones should allow
lower feed rates to be possible and hence higher tracie ele-
ment enrichment factors.
Trace Element Analysis^

Analysis of the trace elements for this study was carried
out by the Analytical R & D Unit, A.E.R.E. Harwell,  England,
Samples of the various exit streams from the gasifier were
taken at midnight on day 12 of Run 9 and analysed by Spark
- Source Mass Spectrometry.  The detailed results are pre-
sented in Appendix G, table XVI.  Samples of the fuel
                            - 103 -
-------
oil and fresh limestone were also analysed by this technique
(Appendix G) and for comparison, by Neutron Activation
Analysis.

Mass Spectrometric survey analyses normally cover most ele-
ments in the Periodic Table from boron to uranium, with the
exception of carbon, nitrogen, oxygen, tantalum and those
elements which are subject to interferences.  The accuracy
of this technique is usually accepted as being "x3" each
way.  That is to say, the true concentration of an element
probably lies within the range from one-third of the ob-
served value to three times that value.  For this reason
results are normally presented in the form of a 'probable
range1 covering one order of magnitude.  Where interference
is known to occur, or is seriously suspected, the upper
limit of the calculated range is reported as a maximum con-
centration, followed by the letter 'I' to indicate inter-
ference.  Where interference is noted it is possible that
the element is not actually present in the matrix ani the
concentration may be zero.  Consequently, a survey analysis
of this type should be considered as a useful guide to the
approximate concentration of a large number of element; but
specific analyses are recommended for those elements of
particular importance.

The results of Neutron Activation Analyses of fuel oil and
fresh limestone are presented in Appendix G Table XV.
A comparison of the results for several trace elements by
the two analytical techniques is shown in Table 26.  The
agreement in the case of fuel oil vanadium concentrebion
is particularly good but for some of the other elements
the agreement on the whole is rather poor.
                            - 104 -
-------
                          Table 26

      Comparison of Analytical Results from Spark-Scurce

      Mass Spectrotoefry and Neutron Activation Analysis
                    Fuel Oil
                    Limestone
            Neutron     Spark-      Neutron     Spark-
Trace       Activation  Source Mass Activation  Source Mass
Element     Analysis    Spectro-    Analysis    Spectro-
            (ppm)       metry (ppm) (ppm)       metry  (ppm)
Vanadium    300,290

Cadmium/    7
Indium

Cobalt      0.2

Chromium    1.4

Molybdenum  <1O

Manganese   O.9

Nickel      <5

Antimony    <2

Tellurium   <1
100-1000    3.5, 5

<0.1        29
0.1-1.0
O. 02-0. 3
0.1-1.0
0.06-0.6
6-60
O. 01-0.1
<0.006
0.3
2
-
22
<50
<20
2
0.06-0.6

<6


<20

<20

<2

6-60

<6

<0.3

<0.6
                            -  105  -
-------
Trace Element Recovery

In view of the high degree of inaccuracy of the analytical
techniques, conclusions regarding the retention of trace
elements must of necessity be tentative.  The approach taken
here is to accept the levels generated by spark-source mass
spectrometry as the best estimate and see what conclusions
this leads us to.  Important observations can then be sub-
jected to further more detailed analysis.

Mass balances of the period 10-1630 to 13-003O for trace
elements of particular importance are shown in Table 27.

                          Table 27

   Mass Balances for Gasification Period 10-1630 to 13-O03O

Trace
Element
Beryllium
Cadmium
Antimony
Molyb-
denum
Nickel
Vanadium
Tellurium
Arsenic
Selenium
Chromium
Manganese
Cobalt
Boron
Lead
Sodium
Potassium
From
Fuel
(g)
<0.1
<0.5
<0.3
- 3
173
2601
<0.05
8.7
<0.5
<0.5
2
3
<0.01
9
52
9
From
Stone
Feed
(g)
<1.5
<0.2
<0.2
<1.4
<4.5
-------
The concentrations of Beryllium, Cadmium, Antimony,  Tellur-
ium, Selenium, Chromium  and Boron were  too  low  for meaning-
ful balances to be obtained,  and the  concentration cf Mercury
both in the stone and the fuel was below detectable  level.
It is necessary to establish  whether  at these potential
pollutant levels, there  would be any merit  in further more
detailed analytical study of  retention  of these elements
on the CAFB bed.  The major contaminants in fuel  oil appear
to be fully retained within the system.  Indeed the  results
in Table 27 indicate with the exception of  Arsenic and
Manganese that the majority of trace elements are retained
in the system.  This of  course neglects the 7%  dust  losses
which will obviously contain  trace elements and is subject
to the accuracy of the analytical data.

For the period of operation under study the maximum  enrich-
ment factor has been calculated as 2O.6.  Table 28 shows
the enrichment factors in the gasifier  bed  material  and
boiler cyclone fines for various trace  elements.

     The values for the  gasifier bed material are consider-
ably lower than expected assuming 1OO%  retention whereas
the enrichment of the boiler  cyclone fines  are  considerably
higher.  This implies that the assumption of homogenous
distribution on the lime is incorrect and that  the trace
elements are preferentially laid down on the finer particles
in the bed.  Alternatively, the elements volatilise  from
the bed and condense on  the fine particles  in the boiler
cyclone.  This is an important observation  which obviously
warrants further study since  the previously reported retent-
ion levels of Vanadium,  Nickel and Sodium were derived from
gasifier bed material concentrations assuming homogenous dis-
tribution on the lime.

The picture becomes somewhat  complex when the trace  element
level on the original stone is high compared with the level
formed in the fuel.  The enrichment factors quoted in Table
28  are calculated assuming the trace element concentration
derived from the original stone remains constant throughout
the process.  However, at least in the  case of potassium and
manganese this is obviously not the case and an apparently
negative enrichment factor is obtained  indicating migration
of these elements from the gasifier bed material to  the
boiler cyclone fines.

Further work is clearly  necessary to establish the mechanism
and significance of this migration.
                           - 107 -
-------
                           Table 28

        Comparison of Trace Element Enrichment Factors

       on Gasifier Bed Material and Boiler Cyclone Fines


TraceEnrichment Factor -Enrichment Factor -
Element	Gasifier bed material	Boiler Cyclone Fines

Vanadium              6                30

Nickel                9.4              100

Molybdenum            ^4               180

Cobalt                ^0               480

Lead                  ^0               195

Manganese             -70              140

Sodium                6 ,               36

Potassium             -505             1300

Arsenic               MD               ^8
                           - 108 -
-------
Materials of Construction

The following materials were used  for  the  internals  of  the
C.A.F.B. units and were exposed  to the process  conditions:

Refractories: Durax C1600  (G.R.  Stein)
              Durax 1500GM  (Gunmix No.l)  (G.R.  Stein;
              Durax C1850  (G.R.  Stein)
              Greencast 94  (A.P. Green)

Fireclays and sealing materials: - various

Ceramics:  Self-bonded SiC  (British Nuclear Fuels)
           Self-bonded Si3N4  (Advanced Materials
                                 Engineering)

Metals:  18/8      stainless steel (various suppliers)
         Type 310  stainless steel (various suppliers)
         Type 321  stainless steel (various suppliers)
         Firebird Blue  (Land Pyrometers)

In addition to the above, calcium  silicate slab and  Junberlite
75 (both from G.R. Stein)  which were used  as insulating
refractories, were exposed  to process  and  regeneration gases
and to vapour phase tar which permeated through cracks in
the hot face refractory.

According to the original proposal (Task 6) we were  to test
up to 10 materials of construction as  requested by EPA or
EPA Contractors.  We did not in  fact receive any  requests
to test particular materials;  the only tests carried out
were therefore such as were necessary  to ensure that the
materials used in the pilot plant  were  satisfactory  for that
purpose.  These were locally available  materials  which may
or may not be readily available  in U.S.A.

The description of composition (where  appropriate) arid
performance follows:

(i) Durax C1600
This was a general purpose hot face refractory  suitable for
reducing gas conditions, supplied  by:

     GR-Stein Refractories  Ltd.,
     Monolithics Division,
     Sheffield,  U.K.
                            - 1O9 -
-------
Typical compositions:
     A1203    49.8%
     Si02     40.9%
     Fe203     0.7%
     Ti02      0.1%
     CaO       4.7%
     Alkalis   0.5%
     Refractoriness = +1730°C
     Continuous service limit = 1550°C

This was the main refractory used for the monolithic con-
struction of the continuous unit and for lining the batch
units.  In the continuous unit the refractory endured over
3000 hours of on-stream gasification, plus about 2OOO hours
of high temperature operation under combusting or burn-out
conditions.

The hot face became rough and lightly eroded on the three
faces adjacent to outside walls of the unit but there was
considerable erosion on the face adjoining the regenerator
where patches were eroded to the depth of \-\" at a height
of 3-5 ft up from the distributor.  There was a severe crack
between the gasifier and regenerator (3/16" to 1/4" at the
widest point and 2 ft long) which was probably closed at the
operating temperature.  The inside of the regenerator was
severely eroded, especially in the lower 3 ft where chere
was severe pitting and the refractory was soft and friable.

(ii) Durax 1500 GM (Gunmix No.l)
This is a fine grain high alumina high grade refractory also
supplied by GR-Stein.

Composition:
     Si02     6.45%
     A1203   76.2%
     Fe2O3    5.16%
     Ti02     2.46%
     CaO      9.32%
     Alk.     0.07%
     Refractoriness  = +170O"C
     Continuous service limit  = 1450°C

This material was used to line the early batch units and
gave a satisfactory performance over several hundred cycles,
gradually  acquiring longitudinal cracks.
                            - 110 -
-------
 (iii) Durax C1850
This is a tabular alumina refractory  cement  also supplied
by GR-Stein with the following typical composition:
     Si02    O.O6%
     A1203  96.8%
     Fe203   O.O7%
     Ti02   trace
     CaO     2.70%
     MgO     O.O6%
     Alk.    0.11%
     Refractoriness  = +18OO°C
     Continuous service limit  = 180O°C

This material was used to line the cyclones  in the continuous
unit after C160O was found to be inadequate  for that purpose.
The top lift of the regenerator was also cast in this
material.  After exposure to process  conditions for 1000
hours the cyclones and top of the regenerator were both in
excellent condition.

(iv) Greencast 94
This material was similar to C1850 in composition and.
properties but from

     A. P. Green Refractories Ltd.,
     Dock Road ,
     Bromborough,
     Merseyside,  U.K.

It was used for batch unit distributors and was satisfactory.

    Self-bonded Silicon Carbide
This was an experimental material containing no binder,
developed by the United Kingdom Atomic Energy Authority
and supplied to us by British Nuclear Fuels Ltd.

We used this material for cyclone offtakes, liners for the
cyclone drains, liner for the fines return duct, an extension
spacer to deepen the regenerator and as the central pipe
in the batch burn-back test burner.  After considerable
exposure to process conditions no deterioration was r.oticed.

(vi)  Self-bonded Silicon Nitride
This material, on paper, showed great promise as a more
easily machineable and cheaper alternative to silicon
carbide.  Unfortunately it disintegrated completely an
the presence of calcium ions and therefore could not be
used in this process.
                            -  Ill  -
-------
(vii) 18/8 Stainless Steel
Was used for making the internal cyclones in the batch units.
The 16-gauge material burnt out every 10 to 20 batch runs,
despite the low top temperature (^6OO°C) in the batch units.
It was also used for making the regenerator distributor,
for which it was satisfactory.

(viii) Type 310 Stainless Steel
This was used for oil lances for which it was suitable most
of the time.  It was also used for the top burn-out connect-
ion and for the steam/N2 injection pipe.  It was satisfactory
for both applications.

(ix) Type 321 Stainless Steel
This was used for distributor air nozzles and for this
purpose it was satisfactory.

This metal was also used as a liner in the cyclone drain
line and also for the cyclone offtakes, both plain and
steam cooled.  The cyclone drain liners suffered from severe
sulphide attack;  the plain cyclone offtake burned out quite
rapidly;  the steam cooled cyclone offtake lasted out a test
run but was showing signs of severe corrosion at welds after
2OO hours.

(x) Firebird Blue
This metal is a 27% nitrided chrome iron supplied by:

     Land Pyrometers Ltd.,
     Dronfield,
     Sheffield,  U.K.

It was used successfully for oil injectors, pressure tappings
and thermocouple sheaths.  The thermocouple sheaths in the
regenerator  (particularly if the regenerator temperature was
high) were occasionally very brittle.  Satisfactory for use
inside the gasifier, e.g. thermocouple sheaths, etc.

(xi) Calcium silicate slab insulation
Was in very good condition with no sign of compression or
disintergration.

(xii) Amberlite 75
This was a vermiculite based insulating refractory and
performed well but shrank away from the hot face refractory
in places, especially in areas which were discoloured in-
dicating contacting with product gas.  The shrinkage
appeared to be largely that of the vermiculite matrix,
indicating that a perlite based insulation may be preferrable,


                           - 112 -
-------
 (xiii) Fireclays and sealing materials
A number of different fireclays were used  for patching/
filling in cracks and sealing joints:

Air setting fireproof cement;  (from GR-Stein) was used,
in conjunction with asbestos rope for filling in gaps
around the gasifier and regenerator lid.   It was very
s atis factory.
Fireclay;  (from GR-Stein) was also used for lid and dis-
tributor seals, in conjunction with asbestos rope.  It was
quicker setting than the air setting cement and was
satisfactory.
Sairset: (from A.P. Green) was the most versatile of the
various fireclays.  It has been used for lid and distributor
seals, for filling in refractory cracks and for sealing
leaks during the test run.  It was very satisfactory.
Asbestos rope;  soft with woven outside cover was usad for
sealing mating refractory surfaces and gave satisfactory
performance, particularly when backed up with fireclay.
Such joints would hold 2-3 psi pressure across a 1/8"  (3mm)
sealed gap while allowing some thermal movement.
Fibrefrax paper and blanket; this material, supplied by

     The Carborundum Co. Ltd.,
     Mill Lane,
     Rainford St. Helens,
     Lancashire,  U.K.
was also used as a refractory joint seal, backed up by a
fireclay.  The joints were satisfactory but allowed little
movement and tended to break down if the thermal movement
was excessive.  Excellent as high temperature insulation.

Summary

Refractories:   Durax C16OO and Durax 1500GM were bot.i satis-
factory for gasifier hot face use.  Durax C16OO was not
suitable for long term use as regenerator lining material.

Durax C1850 was excellent for cyclone, regenerator top and
gasifier hot face construction.  Greencast 94 was excellent
for refractory distributors.

Ceramics:  Self-bonded silicon carbide was excellent for
cyclone offtakes, cyclone drains, fines return line and
regenerator bottom hot face.  It showed no deterioration in
use whatsoever.

Self-bonded silicon nitride disintegrated under C.A.F.B.
conditions and must not be used for internal construction.


                            - 113 -
-------
Metals:  18/8 and 321 S.S. were suitable for distributor
air nozzles in regenerator and gasifier, respectively.  31O
S.S. has been used for oil injectors with satisfactory
results.  In general the stainless steels cannot be used
uncooled inside the gasifier or the regenerator.  Firebird
Blue was satisfactory for uncooled (e.g. thermocouple sheaths)
or cooled (e.g. oil injectors) applications inside both the
gasifier and the regenerator, provided it was not overheated.

Fireclays and seals;  The various fireclays and sealing
materials were all satisfactory, Sairset was the best all
round fire-clay and asbestos rope the best high temperature
gasketing material.
                             -  114  -
-------
Modifications to Equipment  and Operations

The various modifications to the equipment/  carried  out  in
order to achieve a particular set of operating  conditions
or to attempt an improvement of faulty equipment,  are
described in detail in Appendix E.  The results  achieved
by these modifications are  briefly discussed below.

Run 8 -

(i) Bed velocity and depth  - The gasifier bed area was
reduced for this run so that the gasifier could  be operated
at higher bed velocities without overloading the boilar.
The total height of the gasifier bed was also increased  so
that deeper beds could be used without overloading the
cyclones with solids.  The  cyclones themselves were  re-cast
from a finer-grained, high  alumina refractory and  also the
cyclone drains and fine return system was improved so that
it should have been able to cope with a larger  load  of fines.
During Run 8 the unit was operated at up to  6 ft/sec.
(1.83 m/sec.) bed velocity  and up to 56 inches  (1.42m) bed
depth but for short times only because, despite  the  modifi-
cations, the cyclone drain  and fines return  system coaid
not cope with the larger load of fines.  Equipment problems
associated with the fines return system were identified
and were remedied in time for Run 9.  In Run 8,  howevar,
continuous and prolonged operation with a deep bed at a
high bed velocity was not possible.

(ii)  Water and Steam - Provision was made to inject  an oil/
water emulsion into the bed through the bottom injector.
This equipment was not used because we received  (unknowingly)
a supply of wet oil and were therefore obliged to  injact a
water/oil emulsion anyway for several days producing rather
more data on an emulsion operation than originally intended.
A steam connection to the plenum enabled gasification with
an air/steam mixture, replacing flue gas with steam  as an
internal coolant.  A short  test of air/steam gasification
was successfully carried out giving a comparison of  steam
v water (in emulsion) v flue gas as coolants.

(iii)  On stream burn-out - A steam injection point in the
side of the gasifier above  the bed and air injection nozzles
in the lid was used for an  attempt on an on  stream burn-out
of carbon from the cyclones.

In theory, if the total injected oxygen should be  abcve
about 33% of stoichiometric combustion requirement then,
instead of depositing carbon, removal of carbon  by gasifi-
cation should take place.   Injection of such a high

                            - 115  -
-------
quantity of air under the lid would have caused an
unacceptably high back pressure but injection of a smaller
quantity of air as a stratified layer should have given some
carbon removal, with the steam injected through the side
acting as a temperature moderator.  In the event, at  an air
injection rate of 12.5 scfm  (35O 1/mln) of air and 0,9 Ib/min
(0.4 kg/ruin) of steam there was no reduction in back  pressure
indicating no significant removal of carbon and the test
was discontinued after several hours.

(iv) Bottom injector scan - The gasifier monolith was raised
10" to allow about 20" vertical movement of the bottom
injector.  A test was therefore carried out, just before the
end of Run 8, in which the bottom injector position was
varied keeping all other operating variables constant.  The
results were very interesting in that the change in sulphur
removal efficiency (S.R.E.) with depth of injector immersion
followed the same relation as the change in S.R.E. with bed
depth with oil injection at a constant level, indicating
that oil should be injected as low in the bed as is practic-
ally possible.

(v) General comments - Because of asymmetric positiors of
cyclone inlets, the quantity of stone going to the tvro
cyclones was different although it probably did not affect
the performance.  Fines were returned to the gasifier in
slugs which lowered temporarily the gasifier temperature
and caused sudden increases in the stack S02 content.

Run 9 -

(i) Cyclone drains and fines return - Modifications to the
cyclone drains and fines return system included improvements
to all identified problem areas and indeed the performance
of the system was greatly improved.  There were, however,
frequent blockages at the bottom of the cyclone drains caused
by the condensation of vapour phase tar, blockages ir» the
pressure sensing lines, and the system failed to cope with
the circulation of solids above a certain rate, indicating
that either the solids transfer pipework needed to be in-
creased in size or that the whole systen needed to be
modified since it restricted our capability of exploring
a wider range of operating conditions.  One successful
improvement was the puffer on the fines return systeir , which
was intended to spread out the slugs of fines into a  fairly
continuous return, and which worked very well.
                            - 116 -
-------
 (ii) On stream burn-out- Air was injected  under  the  lid  at
 rates of up to 53 scfm  (1500 1/min) and  at times  it  appeared
 to  arrest the increase  in the back pressure caused by  coke
 laydown.  However, at no time did it give  any indication
 of  removing carbon.  The air injection system itself v>orked
 perfectly.

 (iii) Slumped bed burn--out - Provision was made  to inject
 nitrogen into the gasifier plenum during a shut  down,"thus
 inerting the gasifier bed and burn-out of  the carbon above
 the bed without having  to sulphate.  This  procedure was
 tried using:
     Air/steam
     Air/nitrogen
     Air/flue gas
     Air - injected for a short duration followed by a
     cooling down period.

All were successful at  a nitrogen bleed rate through the bed
of only 1 scfh/ft^ of bed.  There was no sign of  any
 agglomeration, slagging or overheating of  the gasifier bed
 and in each case gasification commenced within seconds of
initiating oil injection.

 (iv) Injection of sulphur compounds - H2S,  S02 and thiophene
were injected for short periods into the gasifier bed,  H2S
 and S02 were totally absorbed while the thiophene was de-
composed and absorbed to the extent of about 80%.  Th; s
verified the assumption that only thiophenic sulphur compounds
 are stable enough to survive a passage through the gasifier.

 (v)  General comments - The gasifier, some  of its  ancilliaries
 and most of the analytical equipment were  showing definite
signs of old age during this test run, which exhibitied
themselves in an excessive number of shut  downs, many of
them triggered by maloperation or failure  of detectors or
alarm circuit components.  However, the succession of shut-
downs did prove the efficiency of most of  the safety systems
on the pilot plant, and also demonstrated  that plant shut-
down and restart on gasification could be  achieved simply
and in safety with a minimum of training for operating staff.
                             - 117 -
-------
SECTION VI
APPENDICES
  -  118  -
-------
                             APPENDIX A
                Batch Tests on Limestones and Fuels
                                                             PAGE
Table AI       Kerosine Combustion Tests.

Table All      Fuel Oil Combustion Tests.

Table AIII     Fuel Oil Gasification Tests.

Table AIV      Cyclic Tests - Amuay Fuel/Aragonite.

Table AV       Cyclic Tests - Vacuum Pipestill
                  Bottoms/Aragonite.

Table AVI      Cyclic Tests - Amuay Fuel/Tymochtee
                  Dolomite.

Table AVII     Cyclic Tests - Amuay Fuel/BCR 1559-
120

121

122

123

124


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                            APPENDIX  B


                   Burn-back Burner Test Results

                      Contents


Burn-out Gas Analyses and Gasifier Duct Temperatures
Table B-I
Table B-II
Table B-III
Table B-IV
Table B-V
Table B-VI
Run 3
Run 5
Run 6
Run 7
Run 8
Run 9
Batch Gasifier Operating Conditions
                                                                129
                                                                130
                                                                131
                                                                132
                                                                133
                                                                134
Table B-VII        Runs 1-5                                      135
Table B-VHI       Runs 6-9                                      136
Table B-IX         Runs 10-14                                    137
Burn-back Burner Combustion Tests                               138
Model  for Prediction of Flue  Gas Analyses                      140

Table  B-X          Operating  Conditions                        143
Gas Velocities, Primary Aeration and Flue Gas Analyses

Table B-XI         Mixing tube length 20 mm, Run 13              144
Table B-XII          "     "       "  30 mm, Run 13              145
Table B-XIII         "     "       "  37 mm, Run 13              146
Table B-XIV          "     "       "  37 mm, Run 11              147
Table B-XV           "     "       "  37 mm, Run 12              148
Table B-XVI          "     "       "  37 mm, Run 12              149
Table B-XVII         "     "       "  37 mm, Run 14              150
Table B-XVIII        "     "       "  37 mm, Run 14              151
Table B-XIX          "     "       "  37 mm, Run 10              152
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Burn-Back Burner Combustion Tests

      The combustion test data is presented in Tables B-X  to
The method of calculation of the various terms used is presented
below.

      The gasifier product gas flow was calculated from a nitrogen
balance.

      Gasifier gas flow rate « 79 x A + 100 x N  to purges
                                  % Np in gasifier gas

        where A = total air rate supplied to gasifier bed

      The proportion of gasifier product gas passing through the
burn-back burner was calculated from a total system air and fuel
balance.
      Total air for complete
      combustion at burner        *=    100 - S
                                                 x  A
      and flare, C                        S

       where S = Air/fuel substoichiometric ratio % in gasifier bed

      Proportion of gasifier
      gas passing through         =      B
      burn-back burner                   C

      The term B refers to the air required for stoichiometric complete
combustion in the burn-back burner, and was taken as the mean of the
values calculated from the burner flue gas analyses.

      B = Primary + secondary air  x  (1 - Og - 0.5 CO)
          supplied to burner             •••  <    „	
                                -  138 -
-------
      where CO, CU  =  vol.$ carbon monoxide, oxygen in flue
                        gas respectively.

The primary air velocity

      =  Flow rate at ambient temperature
             Area of primary air duct

The secondary air velocity was derived similarly.

The burner throat loading

         (Flow rate of gasifier product gas through
          burn-back burner corrected for temperature)
         (Area of annulus between end of outer surface
          of primary air duct and refractory lining)
  'Mixing' Tube Length,
Distance X in Figure B-l               Burner Throat Area
            mm
            ?7                               19-9

            30                               16.2

            20              '                 11.2
                                - 139 -
-------
Model for Prediction of'Plue Gas Analyses -
Input  ~    Gasifier gas        100 moles
            Air                  X  moles
Output -    Dry flue gas         Y  moles
            Water                Z moles
Gasifier Product Gas -

co2
CO
"2
CH4
C2H4
C2H6
N2

Plue gas -

co2
°2
N2
Balances -
C
% vol. c OH
7.3 7-3 14.6
7.8 7.8 7.8
8.0 16.0
7.3 7.3 29.2
2.6 5.2 10.4
0.05 0.1 0.3
66.9
2777 22.4 55.9

% Vol. c 0
C0_ C02 2C02
°2 2°2
N2
C02 2(C02+ 02)

27.7 = CO x Y
                        100
0             0.42X + 22.4 = Z + 2(C02 +  02)  x Y
                                      100
H               55-9 - 2Z
N2              66.9 + 0.79 X = (100 - (>C02  +  02))x Y
                                      100
                                - 140 -
-------
 (a)   For stoichiometric air:  Op vol.% in flue gas  «  0
      X  »  145.12,  C0p % vol.  «=  13.24 from balance equations
 (b)   For > stoichiometric air supply:
% Stoichiometric Air
Supplied
120
140
180
220
260
340
420
X Moles
Air Supplied
174.14
203.17
261.22
319.26
377.31
493.41
609.50
C02 % Vol.
In Flue Gas
11.36
10.15
8.37
7.12
6.20
4.92
4.08
02 % Vol.
In Flue Gas
2.50
4.47
7.37
9.40
10.91
12.99
14.36
co
  2,770
69.68 -f X
 42X - 6095
from balance equations
          2(69.68 + X)
Flue gas for < stoichiometric air supply -
co2
CO


Balances -
C   27-7
                  % Vol.
                   CO
                               CO
                             co
           = (C02 + CO) x Y
                100
                                             co
                                                        0
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                                         CO
                                      2C02 + CO
                                 - 141  -
-------
0
H
0.42X + 22.4  «  Z + (2C00 4- CO) x Y
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55-9  =  2Z

66.9 + 0.79X



 42X - 3325
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 6095 - 42X
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                                   100
                        =   (100 -  (C00 + CO)) x Y
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% Stoichiometric Air
Supplied
100
90
80
60
X Moles
Air Supplied
145.12
130.61
116.10
87.07
C02 % Vol.
In Flue Gas
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10.92
8.33
2.03
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In Flue Gas
0
3.08
6.54
14.92
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                                         -  149  -
-------
I
    o
    a
M
W
H
cd
c
ta •
Cd r-H
,°
v >
H
£_j
Q
Total
Aeration
Primary
Aeration
Secondary Air Velocity
Thro1 Shroud Holes
Telocity
: Duct
•H C
< H
£0
Cd rH
_E x:
OH

ow

ow
o

o
o
•H
o
-p
CO
% Stoich
Metres/Sec/Hole*
o
w
0
•p

ON o in co o o m m ON o
H in in c— CM r-OrHCMt--COOC- r<^ [^
O O O O
CO CO CO CO

                                                                                                  OJ

                                                                                                  0)
                                                                                                  bO
                                                                                                  Q)
                                                                                                  CO
                                                                                                  tn
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                                                                                                  OJ
                                                                                                  rH
                                     -  150  -
-------






















t-
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hH *«
p> K
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co
•H CM
W O
rH
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cd H
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> 0
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rH
h
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c x;
0 0
rH iH -H
Cd -P O
+> cd +>
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EH 0
c x:

M *H *H
cd -P O
E cd -P
•H f-i CO
!U CU
PM < tR
>»
+>
•H CO *
O 0
0 rH 0
H O rH
0 W O
•a \.
•H O 0
<^co
>j CO CO
r( 0
CO - r)
tj O -P
C k 0
o ff s
o t-i
0
CO
-P
•H -P
o o
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0 0
> -P CO
3\
!H O. CO
<; H f-t

t<~o s
Cd r<

On

• O O O O • O O
rH OJ



CTiVO C\J-=1-CO OJ K\CO
CVJCOOOCOCOOJOOO
rH H rH
H (Tv cjs in rH r<~N
[^ t^co co -=t- \&



OMX> ^- t>-vo rH mMD
rH in-=i- c\j H t-------
w
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w ^
ctf
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Si
r? 0
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d ^
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rH -H vH
tfl -P O
•P OJ -P
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EH <1)
<•«.
d ^
>j 0 0
fn -H -H
Cd -P O
E nJ -P
•H ti CO
fn 0)
P4 < ^
Secondary Air Velocity
Thro' Shroud Holes
Metres/Sec/Hole *
• >>
-p
•H -P
0 O
0 3
H P 0
0) 0)
>-P^O
f-i ft W
•H C 0
< H fn
-P
PH O S
03 fc
1^
OH
CVJOJ rHiHlTvO^OOMAaDO
HHrHHHHOHHOrH
K>^J- C\J-=j-^tl>-O^-OCOCh
OH ONCOOOOC^COOoOOJ
rH H rH H rH
oo oooovocMLnr<->ot-
vD-^oooo t>-mc--!>-vooo H
o
CTNH f-vo-^-oocM ir\t-KAco
+1+1+1+1+1+1+1+1+1+1+]
SDLnooocvirHoo-=i-rHir\o
Cho t~-vo^J-cX) CM IAOO r^ON
H
OJCVJOJOJCMrHi-ttH CM
+ 1+1 +1+1 +1+1 +1+10 0 +|
^t-^-^t^t-^ooo r KM ff> i<> fOj r
                                         rH
                                          O
                                         OJ
-  152  -
-------
                            APPENDIX C
                    Spent Lime Weathering Results
                                                         Page
Figure C-I   Apparatus                                    154

Effect of Weathering on Deadburned Spent Lime             155

Table C-I  Sample Treatment Temperatures                  155

Determination of the Chemical Composition of              155
                                Spent Lime

Sintered and Weathered Material Composition               160
            Tables C-II to C-XIII

Sintered and Weathered Material Analyses                  172
            Tables C-XIV to C-XIX

Analyses of Sintered Lime Leachates                       178
            Tables C-XX to C-XXV
                               - 153  -
-------
Apparatus

     Six rigid P.V.G. containers with six collection vessels were set
up as shown in Figure C.I.   The containers were left outside and
rainwater allowed to leach through the sintered spent lime in the upper
vessel and into the lower one.    A thermocouple was placed i_i each
upper container so as to penetrate the lime sample to one inch from the
bottom of the container.   The thermocouples were connected to a temp-
erature recorder fitted with a timer and the spent lime temperature was
monitored for the first month of weathering.   Subsequently, the temper-
ature was recorded for one hour each day at noon.
                                Fig C.I.
                 Apparatus for Weathering Sintered Lime
                                             Temperature
                                              Recorder
                               'Tf//     Lime
                                ^*"     Sample
                                    Thermocouple Tip
                          1  ~2E-f—Laachate collected
                               - 154  -
-------
Effect of Weathering on the Deadburned Spent Lime

     Material used in the process was spent lime discarded from the CAPS
pilot plant during Run 8.   The test programme consisted of two parts, namely
deadburning and weathering tests.
     Six samples weighing 2.2 kilograms each were deadburned in a graphite
crucible in an inert atmosphere to a specified temperature, as shown in Table
C.I.
            Table C.I. : Sample Treatment Temperatures

     Sample No.            Deadburning Temperature, °C    Time hours

         1                            1350                   1
         2                            1350                   3
         2                            1450                   I
         4                            1450                   3
         5                            1550                   1
         6                            1550                   3

     The deadburned samples were placed in the perforated containers and
allowed to weather for twelve months.   A sample of the material from each
container was analysed before weathering.   Thereafter a sample of the
material was taken at fortnightly intervals for the first month and the.n at
monthly intervals.   Be fore sampling the material was thoroughly mixed except
for the months of December and January when a sample was taken from the top
of the bed of weathering material.   The samples were dried at 110°C to
constant weight and analysed for:

           CaO, MgO, Si02, Fe^, AlgO^, Na20, S, V, (X>2

released, and loss in weight at 600°C under N_.

     A sample of the rainwater leached through the sintered lime and collected
in the lower container was taken at the same intervals and analysed for:
                 Ca, Mg, Si, Pe, Al, Na, and V

     The results of these analyses are given in Tables C,XX to C.XXV.

     The temperature of the spent lime in the upper container was recorded
continuously for the first month and thereafter for one hour each day at noon.
The results are shown in Figure 25 in the Discussion section,

Determination of the Chemical Composition of the Spent Lime

     The chemical composition of the weathered sintered spent lime is shown
in Tables C.I to C.XIII based on the analytical results given in
                               - 155  -
-------
Tables CJIV to C.XIX.  The calculations made involve several assumptions.
Examples of these calculations, errors and assumptions are presented
below.   Only the total sulphur $ weight was measured.   The calculation
of the calcium sulphide % weight and the calcium sulphate $ weight
Involved the assumption that after 10 to 12 months weathering the
sintered spent lime contained no calcium sulphide.   This assumption
allowed derivation of a $ wt. CaSCv/CaO equivalent ratio which was
assumed constant.

               Analysis                   Assumed Maximum Error

             CaO equivalent                   + 3$

             C02                              1 3$

             Total S                          +0.2$

             Metal oxides                     + 10$

             % CaSO^/CaO equivalent           1 10$


Examples

1.   3 hours sintering at 1350°C sampled December

     CaO equivalent  =  54.6 1 1.6$

     C02 released    =  29.7+0.9$

     Total S         =  3-14 1 0.2$

     $ CaSO|,/CaO equivalent  =  0.112 1 .011

     $ wt. CaSO^  =   (54.6 1 1.6) x (.112 + .011)  =  6.1 + 0.6

     $ wt.  S as SO^ =  (6.1 1  .6)  x  32   =   1.4 1  .1

     $ S in CaS      =  (3.14 + 0.2) - (1.4 1 .1)  =   1.7 1 0.2

     $ wt. CaS       =  (1.7 1 0.2) x 7.2   =   3-8 ^ 0.6
                                     32

     $ wt. CaCO^.     =  $ wt. COP released  x  100
               ^                               ~44

                     =  (29.71-9)  x  100   =    67.512.0
                               -  156  -
-------
     Nett CaO equivalent  =  % wt. CaSO^  x  ^6

                             + % wt. CaCO,  x  56_   +  # wt. CaS  x  56
                                         -^    100                    72
                          =  (54.6 1 1.6) - (4J.3 I 1.2)
                          =   11.3 1 2.1

       # wt. Metal Oxides  =  % wt. MgO + % wt.  Si02 + % wt. PegO,

                              + % wt.  V20,- + % wt. AlpO,  +  # wt. Na20

                           =  2.2 +  0.2

Balance so far:                        % wt.
                CaO                11.3  1  2.1
                CaCO,              67.5  +  2.0
                CaS04               6.1  +  0.6
                CaS                 3.8  ^  0.6
                Metal oxides        2.2  +  0.2
                   Balance          9.1  +  5.0

     11.3 % wt.  CaO  requires  11.3 x 18   =    3-6  +  .7 jftrt. H20
                                       5^
     to form Ca (OH)2 completely.
     Assume all CaO is combined with H20 as Ca (OH)2

     % wt. GaO  =   0     % wt. Ca (OH)2   =    14.8  +  2.8
     % Chemically uncombined H20  =  (9.1 ^ 3.0) - (3.6 + 0.7)
                                  =   5-5  +  3-1
                             -  157  -
-------
       Resulting Composition:             % wt.




                CaO                        0.0




                Ca (QH)2              14.8  +  2.8




                CaCO-^                 67.5  +  2.0




                CaS04                  6.1  +  0.6




                CaS                    3.8  +  0.6




                Metal Oxides           2.2  +  0.2




                Free H20               5-5  *  3-1
                    Total             99.9  +  4.8



    Ca(OH)2 % molar of total calcium  =  gm.moles  Ca(OH)2  x  100
                                           total gm.  moles Ca salts




    Total gm. moles Ca in 100 gm.  sample





         =  14.8 + 2.8   +   67.5  +~ 2.0   +   6.1 + .6   +   3.8 + .6
                 74              100             136             72



         =  0.97  1  0.02





    Ca (OH)2  %  molar   .   20.6  +  4.0 %








2.  1 hour sintering at 1350°C sampled mid-October



    Calculated as before:                  % wt.



                     CaO                   60.4



                     CaCO^                 11.9



                     CaSO^                  8.2




                     CaS                    3-3



                     Metal oxides           3-8
                         Balance           12.4
                              - 158 -
-------
    60.4 % wt. CaO requires 19-4$ wt. H20

    Assume all balance  remaining is H20 combined with CaO as Ca(OH)2-

    % wt.  CaO  = 60.4   -  12.4 x
      wt.  ' Qa(OH)2   =   12.4 x
       Composition:
                     CaO

                     Ca(OH)2

                     CaCO
                     CaS

                     Metal oxides

                     Free H20
                               Total
                  21.7


                  51.22


                % wt.

                21.7



                11.9

                 8.2

                 3.3

                 3.8

                 0.0
               100.1
     The observed ignition losses under Ng at 600°C for the weathered
sintered spent lime samples are shown in Tables C.VTII to C.XIIT.    The
predicted ignition losses are based on the assumption that the weight
loss was due to the loss of free water and the decomposition of the
calcium hydroxide according to the reaction:
             Ca(OH),
600 °C
 No
CaO
H20
     The chemicalanalyses for the sintered lime leachate water are
given in Tables 0.3X to C.XXV.
                              - 159 -
-------
                                TABLE G.IT
SINTERING TIME,  hr    1




SINTERING TEMP,  °C    1350
                SINTERED AND WEATHERED MATERIAL COMPOSITION
                       CALCIUM SALTS MOLAR % OF TOTAL CALCIUM
Month
Sept*
Oct |
Oct 1
Nov
Dec t
Jan t
Feb
Mar
Apr
May
June
July
August
Sept
CaO
91.2
29.7
0.0
1.5
0.0
0.0
-
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
53.0
82.6
81.7
24.7
25.1
-
53.1
79-7
76.6
51.5
60.5
45.0
39.1
CaOO,
0.1
9.1
9.7
10.0
65.0
66.6
-
42.3
15.6
19.3
43.4
35-6
51.1
57.2
Caso,
4.6
4.6
4.6
4.6
4.6
4.6
-
4.6
4.6
3.7
3.7
3.8
3-9
3.7
CaS
4.0
3.5
3-1
2.2
5-6
3.6
-
0.0
0.0
0.5
1.3
0.0
0.1
0.0
Not exposed to weather
                                 sampled from top of bed
                              - 160 -
-------
                                TABLE C.III
SINTERING TIME,  hr    3




SINTERING TEMP,  °C    1350
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                        CALCIUM SALTS MOLAR % OF TOTAL CALCIUM
Month
Sept*
Oct \
Oct 1
Nov
Dec "t"
Jan t
Feb
Mar
Apr
May
June
July
August
Sept
CaO
90.3
15.6
0.0
16.6
0.0
0.0
-
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
73.0
80.0
64.7
20.6
27.0
-
57.5
73.6
80.0
34.9
67.1
47.2
58.5
CaCO-
0.2
3.6
12.9
13.2
69.4
68.0
-
37.9
21.8
17-9
63.9
28.0
48.9
38.3
CaSO^
4.6
4.6
4.6
4.6
4.6
4.6
-
4.6
4.6
1.6
1.5
4.9
3-1
3.1
CaS
5.0
3.1
2.5
0.8
5.4
0.4
-
0.0
0.0
0.0
0.0
0.0
0.7
0.0
     Not  exposed to weather   t sampled from top of bed
                             -  161  -
-------
                                TABLE C.IV
SINTERING TIME,  hr     1




SINTERING TEMP,  °C     1450
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                        CALCIUM SALTS MOLAR % OP TOTAL CALCIUM
Month
Sept*
Oct \
Oct 1
Nov
Dec "*"
Jan "*"
Peb
Mar
Apr
May
June
July
August
Sept
CaO
91.6
24.1
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
64.0
77. 8
84.1
15.8
17.8
84.7
6l.l
70.4
68.8
35-3
69.6
44.1
59-5
CaCO-,
0.1
5.8
14.5
9-3
73-9
77.3
10.7
34.3
25.0
27.6
62.7
29.0
52.4
39-1
CaSOji
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
3-3
1.4
1.4
3.3
1.4
CaS
3-7
1.5
3.0
2.0
5-6
0.3
0.0
0.0
0.0
0.2
0.6
0.0
0.2
0.0
      Not exposed to weather   '  Sampled from top of bed
                              - 162 -
-------
                                 TABLE C.V
SINTERING TIME,  hr     3




SINTERING TEMP,  °C     1450
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                        CALCIUM SALTS  MOLAR % OF TOTAL CALCIUM
Month
Sept*
Oct |
Oct 1
Nov
Dec "*"
Jan "*"
Feb
Mar
Apr
May
June
July
August
Sept
CaO
93.3
31.4
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
60.4
87.4
83.6
17.3
26.3
82.0
47.0
81.6
74.0
45.2
57.9
61.7
27.9
CaCO,
0.1
2.1
5.3
9.8
72.9
67-9
13.3
48.4
13.8
22.1
52.9
i 38.8
35.0
68.8
CaSO,
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6 ;
4.6
3-3 :
1.4
3-3
3.3
3-3
CaS
2.0
1.4
2.7
1-9
5.2
1.2
0.0
0.0
0.0
0.5
0.5
0.0
0.0
0.0
   * Not  exposed to weather   t sampled from top of bed
                              - 163  -
-------
                               TABLE C»yi
SINTERING TINE,  hr     1




SINTERING TEMP,  °C     1550
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                        CALCIUM SALTS MOLAR % OF TOTAL CALCIUM
Month
Sept*
Oct i
Oct 1
Nov
Dec +
Jan +
Feb
Mar
Apr
May
June
July
August
Sept
CaO
93.7
25.0
4.5
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
-
Ca(OH)2
0.0
64.0
77.5
69.1
0.0
5.1
76.7
86.6
80.2
76.4
39-8
66.5
49.8
-
CaCO^
0.1
2.9
11.4
24.1
90.8
90.0
18.6
8.8
15-1
19.2
1 56.5
29.7
; 46.7
I
CaSO^
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.6
4.4
3.7
3.8
3-5
-
CaS
1.6
3.5
1.9
2.1
3.6
0.3
0.0
0.0
0.0
0.0
0.0
0.0
0.0
-
   * Not exposed to weather
Sampled from top of bed
                             - 164  -
-------
                                TABLE C.VTI
SINTERING TIME, hr     3




SINTERING TEMP, °C     1550
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                       CALCIUM SALTS MOLAR % OP TOTAL CALCIUM
Month
Sept*
Oct \
Oct 1
Nov
Dec +
Jan +
Peb
Mar
Apr
May
June
July
August
Sept
CaO
93.7
19.1
0.0
4.0
0.0
0.0
8.7
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
71.4
80.9
63.6
10.6
8-9
58.9
72.5
67.7
64.4
61.9
62.9
54.1
53-6
CaCO-,
0.1
1.9
11.6
26.3
82.7
86.2
27.3
22.8
27.7
32.1
34.5
33-7
42.3
42.0
CaSO^
4.6
4.6
4.6
4.6
4.8
4.6
4.6
4.6
4.6
3-5
3.6
3.4
3.6
4.3
CaS
1.6
3.0
2.8
1.5
1.9
0.3
0.5
0.0
0.0
0.0
0.0
0.0
0.0
0.0
   * Not  exposed to  weather
Sampled from top of bed
                             -  165  -
-------
                                 TABLE C VIII
SINTERING TIME,  hr     1




SINTERING TEMP,  °C     1350
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                                % WEIGHT BASIS
Month
Sept*
Oct %
Oct 1
Nov
Dec "*"
Jan 1"
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
88.7
21.7
0.0
1.0
0.0
0.0
16.3
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
51.2
73.1
74.0
18.0
18.5
57-1
42.7
66.4
64.7
39-3
47.4
35-4
31.6
CaC02
0.2
11.9
11.6
12.3
63.9
66.3
15.8
45-9
17.6
22.0
44.8
37-7
54.3
62.5
CaSO^
10.9
8.2
7-5
7-7
6.2
6.2
8.0
6.8
7-1
5.7
5.2
5.5
5.6
5-5
CaS
5.0
3-3
2.7
1.9
4.0
2.6
0.0
0.0
0.0
0.4
1.0
0.0
0.1
0.0
Metal
Oxides
4.1
3-8
3.3
3.2
1-9
2.2
2.8
3-9
2.4
3-3
3.2
3-0
3.1
2.8
Free
H20
0.0
0.0
1.9
0.3
6.0
4.2
0.0
0.7
6.5
3-7
6.5
6.3
1.4
0.0
Loss at 600 °C
under Nitrogen
Pre-
dicted
0.0
12.5
19.6
18.0
10.4
8.7
13.9
li.l
22.7
19.5
16.1
17.9
10.0
5.2
Obs-
erved
2.3
9.2
15.2
15.2
22.9
28.9
17.8
9.1
15-3
-
14.0
12.5
14.1
19.2
     Not exposed to weather   t Sampled from top of bed
                            -  166  -
-------
                                 TABLE C.IX
SINTERING TIME,  hr     1




SINTERING TEMP,  °C     1350
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                                % WEIGHT BASIS
Month
Sept*
Oct |
Oct 1
Nov
Dec "*"
Jan "*"
Peb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
83.4
11.3
0.0
11.7
0.0
0.0
23.2
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
69.6
62.2
60.1
14.8
19-5
19.2
45-1
59-7
59.2
25.8
55.2
38.3 i
46.2
CaCO,
0.3
4.7
13.6
16.6
67.5
66.4
47.3
40.2
23-9
17-9
63.9
31.1
53.6
40.9
CaS04
10.3
8.1
6.6
7-9
6.1
6.1
7.5
6.6
6.9
2.2
2.0
7.5
4.6
4.5
CaS
5.9
2.9
1.9
0.7
3.8
0.3
0.0
0.0
0.0
0.0
0.0
0.0
0.6
0.0
Metal
Oxides
4.1
3.9
3.2
3.2
2.2
2.2
2.8
2.7
3.2
2.9
3.2
1.3
1.8 !
Free
0.0
3.6
12.4
0.0
5.5
5.6
0.0
5.3
6.3
3.6
5.1
6.2
0.2
6.6
Loss at 600 °C
under Nitrogen
Pre-
dicted
-
16.9
27.6
14.6
9-1
4.7
4.7
16.3
20.8
18.0
11.4
19.6
9-5
17-9
Obs-
erved
-
10.3
29.4
20.4
20.4
28.4
14.7
13.4
27.1
-
11.4
16.7
7-7
21.1
   * Not  exposed  to weather   * Sampled from top of bed
                             -  167  -
-------
                               TABLE C. X
SINTERING TIME, hr      1




SINTERING TEMP, °C      1450
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                               '% WEIGHT BASIS
Month
Sept*
Oct -|
Oct 1
Nov
Dec i"
Jan +
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
86.6
17.6
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
61.8
63.1
73-0
11.5
12.6
72.3
48.3
56.3
55-5
28.2
55-3
35-8
46.0
CaCO,
0.2
7.6
15.9
10.9
72.7
74.1
12.3
36.6
27.0
30.1
67.7
31.1
57.5
40.9
CaSO^
10.6
8.2
6.9
7.4
6.2
6.0
7.2
6.7
6.8
4.9
2.0
2.0
4.9
2.0
CaS
4.5
1.4
2.4
1.7
4.0
0.2
0.0
0.0
0.0
0.2
0.5
0.0
0.2
0.0
Metal
Oxides
4.1
3.4
2.2
2.9
2.1
2.2
2.6
2.5
3.4
3.2
2.7 ;
3.6
2.5
3.0
Free
H20
0.0
0.0
9-4
4.1
5-6
5.0
5-5
5.8
6.6
6.2
0.0
7.9
0.0
0.0
Loss at 600 °C
under Nitrogen
Pre-
dicted
0.0
16.5
24.7
21.9
8.4
8.0
23.1
17.6
20.3
19.6
6.9
21.4
7.8
5.5
Obs-
erved
4.3
12.3
25.8
18.0
19.6
20.9
21.6
11.9
16.9
17.2
9.6
19.4
11.1
PP.0 i
   *  Not exposed to weather  "*" Sampled from top of bed
                              - 168  -
-------
                              TABLE C.XI
SINTERING TIME, hr    3




SINTERING TEMP, °C    1450
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                                % WEIGHT BASIS
Month
Sept*
Oct \
Oct 1
Nov
Dec +
Jan '
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
87.2
23.7
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
60.2
76.6
71.9
12.4
18.6
73.2
36.1
67.6
60.6
35.8
46.1
50.1
21.9
CaCO,
0.2
2.8
6.3
11.4
70.7
65.0
16.1
50.2
15.5
24.5
56.6
41.8
38.4
72.9
4
10.5
8.4
7.4
7.3
6.1
6.0
7.6
6.5
7.0
5.0
2.0
4.8
4.9
4.7
CaS
2.4
1.4
2.3
1.6
3-6
0.8
0.0
0.0
0.0
0.4
0.4
0.0
0.0
0.0
Metal
Oxides
4.2
3.4
3.0
3.4
2.2
2.0
2.5
2.5
3.4
3-2
3.0
2.7
2.7
2.6
Free
H20
0.0
0.0
4.3
4.4
5.0
7.6
0.6
4.6
6.5
6.2
2.2
4.6
3.9
0.0
Loss at 600 °C
under Nitrogen
Pre-
dicted
-
14.6
22.9
21.9
8.0
12.1
18.4
13-4
22.9
21.0
10.9
15.8
16.1
5.0
Obs-
erved
-
9.8
23.8
14.7
27.7
17.6
18.3
20.7
23.2
23.0
12.7
17.0
9.8
18.3
       Not exposed to weather  t Sampled from  top of  bed
                              -  169 -
-------
                                  TABLE C.XII
SINTERING TIME, hr    3




SINTERING TEMP, °C    1450
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                                % WEIGHT BASIS
Month
Sept*
Oct \
Oct 1
Nov
Dec +
Jan 1"
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
87.6
18.5
3.1
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
-
Ca(OH)2
0.0
62.5
70.2
56.8
0.0
3.6
66.8
77.0
67.9
64.6
30.3
52.7
40.0
-
CaCO,
0.2
3.8
13.9
26.8
87.5
85.0
21.9
10.6
17-3
21.9
58.2
31.8
50.7
-
4
10.5
8.3
7.7
7.0
6.0
5.9
7.4
7.5
7.2
6.9
5.2
5.5
5.1
-
CaS
1.9
3-3
1-7
1.7
2.5
0.2
0.0
0.0
0.0
0.0
0.0
0.0
0.0
-
Metal
Oxides
4.0
3.6
3-3
3.1
2.1
2.5
2.4
2.5
3.3
2.9
2.6
2.7
2.7
-
Free
H20
0.0
0.0
0.0
4.6
0.0
2.7
1.4
2.4
4.3
3-7
3-8
7.3
1.5
-
Loss at 600 °C
under Nitrogen
Pre-
dicted
-
15.2
17-1
18.4
0.0
3.6
17.6
21.1
20.8
19.4
11.1
20.1
11.2
-
Obs-
erved
-
11.7
22.4
15.8
21.1
29.4
18.3
7-2
27-4
-
11.3
19-9
8.3
-
       Not exposed to weather  """ Sampled from top of bed
                              -  170 -
-------
                                TABLE C.XIII
SINTERING TIME, hr     3




SINTERING TEMP, °C     1550
                 SINTERED AND WEATHERED MATERIAL COMPOSITION
                                % WEIGHT BASIS
Month
Sept*
Oct ^
Oct 1
Nov
Dec "*"
Jan '
Peb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
87.1
14.0
0.0
2.6
0.0
0.0
5.8
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Ca(OH)2
0.0
69.1
70.6
54.9
7.4
6.2
51.6
62.1
55.2
53.6
48.0
52.0
44.7
42.0
CaCO,
0.2
2.5
13.7
30.7
77.7
81.4
32.3
26.4
30.6
36.1
36.1
37.7
47-3
44.5
88304
10.4
8.2
7.4
7-3
6.1
5.9
7.4
7-3
6.9
5-3
5.1
5.1
5.4
6.2
CaS
1.9
2.8
2.4
1.3
3-1
0.2
0.4
0.0
0.0
0.0
0.0
0.0
0.0
0.0
Metal
Oxides
4.1
3.4
3.1
3.2
1.9
2.1
2.5
2.5
3.4
2.9 i
2.5
2.5
2.7
2.6
Free
0.0
0.0
2.8
0.0
3.8
4.1 j
0.0
1.9
4.0
2.1
8.3
2.8
0.0
4.8
Loss at 600 °C
under Nitrogen
Pre-
dicted
-
16.8
20.0
13.3
28.2
5-7
12.6
17.0
17.5
15.1
20.0
15.4
10.9
15.0
Obs-
erved
-
11.1
30.4
19.0
28.2
29.0
17.5
7.8
11.2
-
12.3
23.1
11.8
19-5
      Not  exposed to weather  t  sampled  from top of bed
                              - 171 -
-------
                               TABLE C.XIV
SINTERING TIME, hr      1




SINTERING TEMP, °C      1350
                 SINTERED AND WEATHERED MATERIAL ANALYSES
                                % WEIGHT BASIS
Month
Sept *
Oct ^
Oct 1
Nov
Dec +
Jan T
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO 1 C02
Equivalent
97.2
73.0
67.0
68.5
55-1
55.7
71.6
60.8
63.0
64.0
58.7
61.4
62.4
61.2
0.07
5.24
5.08
5.4
28.1
29.2
6.97
20.2
7-75
9.72
19.7
16.6
23.9
27.5
MgO
.9
.7
.8
.6
.5
.5
.6
.5
• 5
.5
.6
.6
.6
.6
Si02
1.1
1.4
1.0
1.3
.4
• 7
1.2
1.1
1.1
1.1
1.0
• 9
• 9
l.l
Fe'
.10
.08
.08
.13
.08
.08
.10
.09
.08
.08
.10
.10
.10
.09
A120,
.8
.6
.4
.4
• 3
.3
• 5
1.9
.6
.6
.4
.4
.4
.5
Na
.006
.007
.004
.002
.012
.004
.002
.002
.002
.002
.008
.002
.002
.003
Total
S
4.77
3.38
2.97
2.64
3.25
2.03
1.61
1.39
1.57
1.55
1.68
1.26
1.38
1.28
V
• 69
.56
.55
.42
.37
.29
.19
.17
.50
.48
.50
.45
.41
• 37
     Not exposed to weather  "*" Sampled from top of bed
                              -  172 -
-------
                                 TABLE C.XV
SINTERING TIME, hr     3




SINTERING TEMP, °C     1350
                 SINTERED AND WEATHERED MATERIAL ANALYSES
                                % WEIGHT BASIS
Month
I
Sept*
Oct \
Oct 1
Nov
Dec f
Jan +
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
Cquivale
92.4
72.2
58.9
70.2
54.6
54.6
67-3
59-4
61.4
65.0
57-3
61.2
61.5
61.1
C0?
nt
0.1
2.06
5-99
7-3
29.7
29.2
20.8
17-7
10.5
14.1
28.1
17.6
20.9
27.5
MgO
• 9
.7
.6
-7
.5
• 5
.6
• 55
• 55
• 5
.6
.6
.6
.6
Si02
1.2
1.1
1.2
1.2
.6
.7
1.2
1.0
1.1
1.1
1.1
• 9
.9
l.l
Fe
.10
.08
.08
.12
.08
.08
.09
.10
.08
.08
.11
.09
.09
.09
A12°3
.6
.5
• 5
.4
.4
.4
.5
.6
.6
.6
.5
.5
.5
.4
Na
.007
.005
.004
.003
.002
.006
.002
.006
.003
.002
.005
.002
.002
.003
Total
S
5.06
3.21
2.38
2.15
3.14
1.78
1.45
1-35
1.12
1.29
1.06
1.20
1.09
1.27
V
.73
• 57
.49
.41
-35
.30
.17
.23
.50
.47
• 50
Al
.40
• 35
   * Not exposed to weather  "*" Sampled from top of bed
                              -  173 -
-------
                                TABLE C.XVI
SINTERING TIME,  hr     1




SINTERING TEMP,  °C     1450
                 SINTERED AND WEATHERED MATERIAL ANALYSES
                                % WEIGHT BASIS
Month
]
Sept*
Oct -5-
Oct 1
Nov
Dec ^
Jan '
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO ' CO
Equivalent
94.6
73-1
61.4
65-7
55-1
53.6
64.6
59-8..
60.5
61.0
61.2
61.3
61.5
59-7
.07
3.35
7.02
4.80
32.0
32.6
5.4
16.1
11.9
13.4
29.8
13-7
23.6
18.0
MgO
• 9
.7
.6
.6
.5
.5
.6
.5
.5
.5
.7
.6
.6
.6
Si02
1.1
1.0
1.1
1.1
.6
.7
.89
.9
1.2
1.2
1.1
1.1
1.1
1.1
Fe
.09
. .09
.07
.12
.08
.08
.09
.10
.10
.10
.11
.10
.09
.10
1
.7
.6
.4
.4
.3
.4
.7
• 7
.7
.7
.5
.5
.5
.6
Na
.003
.003
.003
.001
.001
.005
.002
.001
.002
.002
.005
.002
.002
.002
Total
S
4.50
3.37
2.68
2.47
3.24
1.47
1.71
1.54
1.45
1.24
1.43
0.93
1.42
1.01
V
.72
.55
.50
.40
.35
.29
.19
.21
.50
.44
.50
.43
.38
.35
    Not exposed to weather  t Sampled from top of bed
                              - 174  -
-------
                               TABLE C.XVII
SINTERING TIME,  hr    3




SINTERING TEMP,  °C    1450
                 SINTERED AND WEATHERED MATERIAL ANALYSIS
                                % WEIGHT BASIS
Month
]
Sept*
Oct %
Oct 1
Nov
Dec t
Jan T
Peb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
Equivale
93.5
75.4
66.4
65.0
54.3
53-6
67.5
58.1
62.7
62.0
61.2
60.3
61.4
59.4
co2
nt
.1
1.25
2.78
5-0
31.1
28.6
7.08
22.1
6.8
10.8
24.9
18.4
16.9
32.1
MgO
-9
• 7
.6
.6
• 5
.5
.6
.5
• 5
.5
.6
.6
.6
.6
Si02
1.1
1.0
1.0
1.4
.6
.6
• 9
.9
1.3
1.3
0.9
l.l
l.l
l.l
Fe
.11
.09
.08
.22
.08
.09
.09
.10
.09
.08
.10
.09
.10
.10
A1203
.7
.6
.4
.5
.3
.3
.6
.7
.7
.7
.5
.5
.5
.5
Na
.003
.003
.002
.001
.008
.005
.001
.001
.001
.001
.003
.001
.002
.003
Total
S
4.81
3-35
2.78
2.40
3.05
1.78
1.83
1.50
1.58
1.35
1.36
1.13
1.22
1.20
V
.73
.58
• 52
.40
.40
.30
.18
.19
.50
.46
• 50
.41
• 39
.35
   * Not exposed to weather  '  Sampled from top of  bed
                              - 175  -
-------
                                TABLE C.XVIII
SINTERING TIME, hr      1




SINTERING TEMP, °C      1550
                 SINTERED AND WEATHERED MATERIAL ANALYSES
                                % WEIGHT BASIS
Month
Sept*
Oct |
Oct 1
Nov
Dec +
Jan t
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
Equiva]
93.5
73-9
68.6
62.2
53-2
52.9
65.8
67-3
64.0
64.0
57.6
60.0
60.8
-
CO
Lent
.1
1.68
6.13
11.80
38.50
37.40
6.95
4.65
7-60
9-65
25.6
14.0
22.3
-
MgO
• 9
.8
.7
.6
.5
.5
.6
• 5
• 5
.6
.6
.6
.6
-
Si02
1.1
1.2
1.2
1.1
.6
.7
.9
• 9
1.2
1.2
0.9
1.1
1.1
-
Pe
.09
.08
.07
.12
.07
.07
.09
.10
.09
.08
.11
.11
.09
-
A1203
.7
• 5
.4
.4
.3
.3
.7
.7
.7
.6
.5
• 5
.5
-
Na
.001
.003
.002
.001
.007
.005
.001
.001
.001
.001
.003
.002
.002
-
Total
S
3.30
3-40
2.60
2.40
2.50
1.50
1.50
1.50
1.70
1.62
1.23
1.29
1.21
-
V
.68
.58
.51
.47
.36
.29
.18
.19
• 50
.44
.50
.42
.40
-
   * Not exposed to weather  1" sampled from top of bed
                              -  176 -
-------
                                 TABLE C.XIX
SINTERING TIME,  hr     3




SINTERING TEMP,  °C     1550
                 SINTERED AND WEATHERED MATERIAL ANALYSES
                                % WEIGHT BASIS
Month
Sept*
Oct ^
Oct I
Nov
Dec f
Jan +
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
CaO
Equival
93.0
73-3
66.0
65.3
54.0
52.9
66.2
64.7
61.7
63.0
58.6
58.8
62.5
59-2
co2
ent
.07
1.10
6.07
13-5
34.2
35-8
.14.2
11.6
13-5
15-9
15-9
16.6
20.8
19.6
MgO
• 9
.7
.6
.6
• 5
.5
.6
.5
.5
.5
.6
.6
.6
.6
Si02
1.1
1.0
1.0
1.4
0.4
.7
• 9
.9
1.2
1.2
0.8
0.9
1.1
1.1
Fe
.10
.09
.07
.13
.07
.08
.09
.09
.10
.10
.13
.09
.09
.10
A12°3
.7
.5
.4
.4
• 3
.3
• 7
.6
.6
.6
.5
• 5
• 5
.5
Na
.001
.001
.001
.001
.007
.006
.001
.002
.001
.001
.004
.001
.002
.002
Total
S
3-30
3.20
2.80
2.30
2.80
1.50
1.90
1.70
1.60
1.25
1.19
0.93
1.27
1.47
V
.68
.63
• 59
.41
• 36
.29
.20
.18
.50
.46
.50
.39
.41
• 35
   Not exposed to weather  t Sampled from  top  of bed
                                 177 -
-------
                               TABLE C.XX
SINTERING TIME, hr     1




SINTERING TEMP, °C     1350
                 ANALYSES OF SINTERED LIME LEACHATES
                   PARTS PER MILLION WEIGHT BASIS
Month
Sept*
Oct ^
Oct 1
Nov
Dec
Jan
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain-
fall
mm.
-
59-7
59-7
123.2
79-6
29-5
88.9
115.2
35-9
44.3
5-3
31-3
33-1
85.8
PH
Ca
Mg
Si
Fe
Al
Na
V
. No leachate

8
10
10
10
10
,10
10
10
10
10
10
10

440
700
1160
1500
1550
1300
1800
2300
1000
-
-
1410
No leachate
1
<•!
.3
.2
.2
.2
.3
.2
3.1
-
-
.2
6
13
1
2
2
4
2
2
<2
-
-
<2
<.l
- 1
<.l
<-l
<-l
<.l
.2
.2
-
-
-
.2
<1
<1
<1
<1
<1
<1
<1
<1
-
-
-
-------
                                TABLE C.XXI
SINTERING TIME, hr     3
SINTERING TEMP, °C     1350
                    ANALYSES OF SINTERED LIME LEACHATES
                      PARTS PER MILLION WEIGHT BASIS
Month
Sept*
Oct -|
Oct 1
Nov
Dec
Jan
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain-
fall
mm
-
59-7
59-7
123.2
79-6
29-5
88.9
115.2
35-9
44.3
5-3
31-3
33.1
85.8
PH
Ca
Mg
Si
Fe
Al
Na
V
No leachate
-
8
10
10
10
10
10
10
10
10
10
10
10
235
440
640
2160
1300
1250
1000
1500
1900
2600
-
-
1150
6
1
<.l
• 3
.1
.2
.2
.1
<-l
.5
-
-
.1
11
5
11
1
2
2
7
4
l
<2
-
-
<2
<.l
<-l
<.l
<•!
<.l
-------
                                TABLE C_.XX11
SINTERING TIME, hr      1




SINTERING TEMP, °C      1450
                     ANALYSES OF SINTERED LIME LEACHATES
                       PARTS PER MILLION WEIGHT BASIS
Month
Sept*
Oct |
Oct 1
Nov
Dec
Jan
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain-
fall
mm.
-
59.7
59-7
123.2
79.6
29-5
88.9
115-2
35-9
44.3
5-3
31.3
33.1
85.8
PH
Ca
Mg
Si
Fe
Al
Na
V
No leachate
9
10
10
10
10
10
10
10
10
9
9
9
9
153
390
600
2040
1300
1300
1100
1400
1950
1700
-
-
875
12
1.5
.1
.2
<.l
.1
.4
<.l
<.l
.7
-
-
<.i
4
5
11
1
2
2
6
4
l
<2
-
-
<2
<•!
<•!
<.l
<.l
<.l
<.l
<.l
.2
<.l
-
-
-
<.i
<1
<1
<1
<1
<1
<1
<1
<1
<1
-
-
-
«
28
125
6
11
8
11
14
12
14
21
-
-
16
9
2
<1
<1
<1
<1
<1
<1
<1
4
-
-
-------
                                TABLE C.XXIII
SINTERING TIME, hr     3




SINTERING TEMP, °C     1450
                     ANALYSES OP SINTERED LIME LEACHATES
                       PARTS PER MILLION WEIGHT BASIS
Month
Sept*
Oct |-
Oct 1
Nov
Dec
Jan
Peb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain-
fall
mm.
-
59-7
59.7
123.2
79-6
29-5
88.9
115.2
35.9
44.3
5-3
31-3
33.1
85.8
PH
Ca
Mg
Si
Fe
Al
No leachate
8
10
10
10
10
10
10
10
10
10
10
10
10
.100
310
600
1980
1170
1100
900
1400
1900
2800
-
-
1391
3
1.5
.2
.1
<.l
<.l
.3
.1
.1
1.2
-
-
<.i
15
5
11
l
2
2
7
3
1
<2
-
-
<2
<.l
<-l
<.l
<.l
<.i
<.i
<.i
.2
<•!
-
-
-
.2
<1
<1
<1
<1
<1
<1
<1
<1
<1
-
-
-
-------
                               TABLE C.XXIV
SINTERING TIME, hr      1




SINTERING TEMP, °C      1550
                    ANALYSES OF SINTERED LIME LEACHATES
                      PARTS  PER MILLION WEIGHT BASIS
Month
Sept*
Oct \
Oct 1
Nov
Dec
Jan
Feb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain- '
fall
mm
-
59-7
59-7
123.2
79-6
29.5
88.9
115.2
35-9
44.3
5-3
31.3
33.1
85.8
PH
Ca
Mg
Si
Fe
Al
Na
V
No leachate
8
10
10
10
10
10
10
10
10
9
9
9
9
128
360
580
i860
1300
1100
750
1500
1900
1700
-
-
883
4
1.5
.2
.2
<1
<.l
.3
<.l
<.l
.5
-
-
.1
4
6
10
1
2
4
7
3
1.0
<2
-
-
<2
<.l
<.l
<.l
<.l
<.l
<.l
<.l
.2
<.l
-
-
-
<.i
<1
<1
<1
<1
<1
<1
<1
<1
<1
-
-
-
<1
24
111
8
12
8
12
11
13
11
24
-
-
15
14
2
<1
<1
<1
<1
<1
<1
<1
1
-
-
-------
                                TABLE C.XXV
SINTERING TIME, hr     3




SINTERING TEMP, °C     1550
                     ANALYSES OF SINTERED LIME LEACHATES
                       PARTS PER MILLION WEIGHT BASIS
Month
Sept*
Oct -5-
Oct 1
Nov
Dec
Jan
Peb
Mar
Apr
May
Jun
Jul
Aug
Sept
Rain-
fall
mm
-
59-7
59-7
123.2
79-6
29-5
88.9
115.2
35-9
44.3
5-3
31-3
33.1
85.8
PH



9.5
10
10
10
10
10
10
8
8
8
8
' Ca



840
2040
1320
1500
900
1750
1900
1700
-
-
1110
Mg
Si
Pe
Al
Na
V
No leachate
No leachate
No leachate
.2
.4
.1
<.l
.2
.1
.1
.7
-
-
.1
10
1
2
3
5
3
l
.<2
-
-
<2
<.l
<.l
<.l '
<.l
<.l
.2
^.1
-
-
-
.2
<1
<1
<1
<1
<1
1
<1
-
-
-
<1

7
12
8
11
10
1*
14
40
-
-
24

<1
<1
<1
<1
<1
<1
<1
1
-
-
<1
      Not  exposed  to weather
                              - 183  -
-------
                             APPENDIX D



                         Sulphation Test Results

                                                               Page

Details of Sulphation Tests.                                     185


Data for Sulphation Runs, Tables D.I to I>.XI                    189
Cumulative Solids and Sulphur Balances, Tables D-XII to "        200
                                                  D.XIV
                                - 184  -
-------
DETAILS OF SULPHATION TESTS
      The exit gas from the sulphator was sampled continuously, passed
through a filter and a water condenser, and monitored directly for
C02, Op, and SOp.   The plenum dry gas analysis for 02 and SOp was
similarly obtained.

      The SOp absorption efficiency was calculated as shown below:

      % SOp absorption = gm. moles SO,, absorbed
          *              - E -  x 100
                          gm. moles SOp input

                       = gm. S02 in - gm. S02 out  ^ 1QQ

                                gm. S02 in

                       = 100 - Vol.$ S02 in exit gas x £ x 0
                               Flow rate SO  input, gm./min.

      The SOp input rate was determined by noting the weight of the
SOp cylinder and contents at regular intervals.
           A  =  density of SO^, gm./l
      The flow rate of exit gases from the sulphator, $ 1/min., was
calculated from a nitrogen balance.

      0  =  79 x Total air into unit + 100 x Nitrogen purges
                      Vol.# nitrogen in exit gases

      The vol.$ nitrogen in the exit gases was calculated by difference
from the CO^, 0?, and SO^ analyses.

      The Ca :  S molar feed rate was calculated as shown below:

      Molar Ca in feed :  SO  input

            = _ gm.  mols. CaO fed    _
              gm. mols. SOp input to sulphator
                                -  185 -
-------
            =  gm./min. CaO fed       64
              gm./min. SOp input      56"

      The spent lime feed was calculated in terms of equivalent
burned stone, CaO, as follows:

      gm. CaO = gm. spent lime x (1 - 0.01 x C - 0.00501 X S
                                                 - 0.01996 x SO

      where  C   =  total carbon, % wt.

             S   =  total sulphur, % wt.

            SO^  =  total sulphur present as sulphate, % wt.

      The mean particle diameters were determined by use of the
formula :

               1QQ
      Mean particle diameter            £    D

      where  x   =   % wt. of particles of diameter D
                                                     X

      The mole % sulphation was defined as:

      Mole % sulphation =       moles CaSO^. in sample

                          total moles Ca combined in sample

                        =  moles S present as SO
                                                ~
                          moles total S + moles CaO
                            32        x 100
                             ,  CaO
                                             xlOO
                          S +" CaO "x" 0.5714
      where  S   =  total sulphur, % wt .

            SO^  =  total sulphur present as sulphate, % wt.

            CaO  =  calcium oxide, % wt.



                                - 186  -
-------
      For mole % sulphation of sieved fractions of bed or cyclone
material analyses were obtained for these fractions directly.

      Corrections were made for oxide impurities such as SiOp, Fe^O-,,
and Al 0, present in the sulphated spent lime.   Each sample was also
analysed for acid insolubles to determine the % by weight of silicon
carbide present, and a correction applied.   These corrections are best
illustrated by several examples.

 (i)   Sulphation run no. 3 bed material 250-150 microns at 6^0 min.
          S = 17-5$ wt., 30^. = 17.5# wt., C = <0.01$ wt.
          Acid insolubles = 2.3$ wt.

       % wt. CaO in sample = 100 - % wt. CaSO^ - % wt. CaS - % wt. C
                                   - % SiC - % wt. oxide impurities

       Oxide impurity in burned stone = 3.4$ wt.

       Equivalent burned stone = 100 - C - 0.501 x S - 1.996 x SO^
        as percent of sample   = 56$

       Therefore % wt. oxide impurity in sample = 3-4 x  56 = 1.9$
                                                        100

       % Silicon carbide = % Acid insolubles observed - % Acid
                                        insolubles in spent lime

       Acid insolubles in burned stone = 1.5$ wt.

       Therefore % SiC = 2.3 - 1.5 x _5_6_ = 1.5$ wt.
                                     100

       % CaS = 0    ;  % CaSO^ = SO^ x 136 = 74.5$
       Therefore % CaO = 100 - 74.5 - 1.9 - 1.5 •= 22.2

       % mole sulphation = 58.!$

(ii)    Sulphation run no.  3 bed material 600-250 microns at 15 miri.
          S = 1.0$ wt.,  S0i± -r-. 1.0$ wt.,  C <0.01$ wt.
          Acid insolubles  = 89.2$ wt.
                                - 187 -
-------
The bulk of this sample is silicon carbide so % acid
insolubles in the -**10$ spent lime is negligible.

% SiC = % acid insolubles = 89.2$

SCty. in spent lime = SO^ in sample x     100
                                    100 - % SiC

SO^ corrected for SiC present =9.6$

Therefore % CaSO^ in spent lime = 40.9$

% CaO in spent lime = 100 - % CaSO^ in spent lime =

% Mole sulphation = 22.2$
                         - 188  -
-------
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                           -  199  -
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CUMULATIVE SOLIDS AND SULPHUR BALANCES

      A comprehensive solids and sulphur balance check was made for
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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  -
-------
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 -
-------
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  -
-------
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
                   -  281  -
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                                                      -   295   -
-------
                          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
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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
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K
IN
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. 157
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. 406

1
1
1
1
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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
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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
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- 6.12
- 14.63
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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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                            -  337  -
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                            - 338 -
-------
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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 
-------
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
50.8
45.3
49.2
45.3
54. 1
48.7
23.5
RFGEN.
S OUT %
OF FED
69.7
77.4
76.2
63.9
0.
0.
0.
52.7
47.0
39.5

42.4
51.2
53.0
60. 1
65.5
64.2
61 . 1
55.7
60.5
50.3
48.7
45.0
23.6
                     - 439 -
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-------
                   APEESDIX  G.    -  TABLE VII
        ANALYSIS OF SOLIDS REMOVED DURING RUN 9
             TOTAL   SULPHUR   WT.%
DAY.HOUR  OAS'R  REGEN  RFGEN  ELUTR BOILER  BOILER   ELUTH
                       CYCLONE FINES  BACK   FLUE  COARSH
2. 1800
4.0630
5.0001
5.0600
5 . 1 400
6.0000
6.0600
6. 1200
6.2100
7.0600
7. 1200
7 . 1 800
8.0000
8.0600
8. 1?00
8. 1800
8.2200
9 . 1 200
9. 1800
10.0600
10. 1200
10. 1800
1 1 .0000
1 1 .0350
1 1 . 1200
1 1 . 1800
12.0(7)00
12.0600
12. 1200
12. 1800
13.0000
13.0600
13. 1200
14.0600
14.1100
14.1 200
14. 1800
15.0000
15.0700
15. 1200
4.82
5.59
5.33
4.65
4.30
4.48
3.96
3.16
5.01
5.27
5.57
5.23
4.61
4.32
4.07
4.59
4.46
4.61
4.38
4.36
4.36
4.17
3.84
3.85
4.58
4.38
4.38
4.36
4.32
3.65
3.78
3.71
5.04
4.99
6.25
6.52
5. 18
4.66
4.88
4.39
3.89
4.65
4.22
3.39
4.27
3.38
3.05
2.67
3.86
3.92
4.26
3.73
3.79
3.80
3.53
3.83
3.80
3.71
2.80
3.32
3. 16
2.81
2.80
2.51
3.74
3.50
3.81
3.65
2.49
2.53
2.67
2.71
3.82
3.01
—
6.64
3.99
3.94
3.00
3.02
-
-
-
-
—
-
-
—
-
—
-
-
-
—
-
—
-
-
-
4.37
-
-
3.98
-
-
-
3.90
-
4.04
3.96
3. 18
-
4.34
-
-
5.05
5.42
4.75
—
5.54
-
-
-
-
6. 10
5.35
—
-
-
-
—
-
—
-
—
—
-
-
-
3.73
-
—
3.08
-
-
-
4.27
-
4. 15
3.93
3.87
-
3.89
-
-
5. 13
5.39
5.18
—
4.84
—
-
3.77
-
3.78
3.07
-
—
-
—
-
-
3.60
-
—
-
-
-
-
4.12
—
-
3.92
—
-
-
4.28
-
4. 15
-
4.30
-
4.37
-
—
5.00
-
6.1 1
—
5.66
-
—
3.82
-
2.67
3.50
-
—
-
—
—
—
2.48
—
-
—
-
—
-
3.25
-
—
2. 15
-
-
—
3.17
-
3.38
-
4.21
—
3.90
—
-
4.39
-
3.82
-
3.01
5.7P
6.21
5. Ib
4.90
5.06
3.69
3.75
3.80
-
5.75
4.71
4.81
4. 14
3.92
3.68
4. U
4.40
4.35
4.03
4.08
4.04
3.79
3.56
-
4.59
4. 10
4. 14
3.90
4.07
-
3.43
4. 12
4.82
4.67
—
6.38
-
4.59
4.66
-
                           - 482 -
-------
                     APPENDIX  G.
TABLE  VII
          ANALYSIS OF SOLIDS REMOVFD DURING  HUN  9
               TOTAL   SULPHUR   WT.%
  PAY.IIOUH
  16.1500
  17.0000
  17.0800
  17.1245
  17.1545
  17.1700
  18.0000
  18.K600
  18.1200
  Ib.1800
  19.0000
  19.0600
  19.1200
  19.1800
 20.0000
 20.0600
 20.1600
 20.1800
 22.1800
 23.0015
 23.0600
 23.1200
 23.1800
 24.0000
 24.0600
 24.0900
 24.1200
 24.1800
 25.0000
 25.0600
 26.0000
 26.0600
 27.0600
 27.1230
 27.1830
 28.0000
 28.0600
 28.1230
28.1845
30.0600
V'AS' H

4.98
4.01
3. 13
4.66
5. 12
—
5. 16
5. 16
4.70
7.95
7.24
5.32
4.77
3.86
4.39
4.69
4.28
4.80
4.39
3.83
3.52
3.74
3.34

4.23
6.77
6.95
5.30
3.43
2.80
2.73
4.59
6.03
3.24
3.41
2.32
2.56
2.78
2.89
3. 13
3.48
KhGhN

4.68
3.66
4.46
3.24
3.93
-
3.53
3.60
6.22
7.00
6.01
4.49
3.69
4.52
3.27
3.87
3. 68
3.67
2.85
2.72
2.26
2.38
1 .59

3.99
5.80
1.94
4.67
2.09
1.43
1.02
3.21
2.25
2.24
2.29
2.05
2.27
2. 18
6.30
2.22
2.61
RFGFN
CYCLONF
5.77
5.97
5.57
—
_
5.24
5.39
-
5.79
-
5.41
6.68
7.22
6.39
5.65
4.70
—
3.31
—
-
7.81
_

9.78
—
—
9.26
7.00
5.99
6. 15
5.75
7.45
7.53
6.24
-
6.93
—
5.55
4.37
-
F.LUTR
FINFS
3.90
3.71
3.38
—
_
3.46
3.77
—
3.57
_
4.01
_
_
4.89
2.82
«»
5.98
_
5.31
—


3.78
_
_
4.74
_
5.55
_
5.46
—
_
3.79
_
4.85
••»
3.39
3.22
6.08
POILFR
RACK
4.03
4.29
3.75

_
4.49
8.37
—
„
» .
5.39
— ^
—
5.42
_
^
_
_
—
4.02


3.86
^
w.
4.97

5.22
^
4.02
«.
^
4.71

3.75
^m
4.09
-
BOILFR
FLUF
3.34
3.25
4.07


4.63
4 . 64

_
	
5.65

_
3.63


_

2.78



4. 1 1


4.51

3.86

5. 12


4.71

4.79

4.42
—
FLUTK
COARSF

4 . 20
3.85


4.37
4.^5
4.41
6.57
6. 79
6.53
6 . 79
V i • 1 ™
R ^u
ZD • O^
5. 3j
' • -~> ^
4.21



5 1 7
} • 1 f
3.51
3.40
3.39
3—j ,
/O
* ( "
4.68
6 9 1
*•> • f. \
7 00
i • It/ v '
7.02
3 66
*~J • V. > V 1
4.64
? t>C1
- ' » ^ \J
5. 1 4
6. 90
A A/1
*T » t J l*
4.15
4 ^6
" • — i )
5. 65
/I O O
a . .s
3.22
2 ^6
e * ' J
8.23
                          -  483  -
-------
                   APPENDIX  .0.    TABLE VH

        ANALYSIS OF SOLIDS REMOVED DURING RUN Q
             TOTAL   SULPHUR   WT.%
DAY.HOUR  GAS'H  RFOEN  RFOEN  FLUTR BOILER  BOILER   F.UJTH
                       CYCLONE FINFS   BACK   FLUE  COARSE

                                 -                    5.33
                                                      4.18
                                4.12   6.63   5.31    3.76
                                 -                    4.76
                                                      7.08
31.1800    4.65   3.42   5.35    -                    3.86
32.0000    5.00   4.24   4.47   4.72   2.84   2.37    5.00
32.0600    5.77   4.78   5.14           -      -      4.46
32.0900    5.77   4.78   5.14   4.72   2.84   2.37    4.^6
30. 1200
30. 1800
31 .0000
31 .0600
31.1 200
3.90
4.27
11.17
4. 18
4.28
2.66
2.53
3.38
3. 15
3.40
8.68
7.59
5.96
8.79
8.73
                          -  484  -
-------
                        APPENDIX  G.  TABLE  VIII


        ANALYSIS OF SOLIDS REMOVED DURING RUN 9
          SULPHATE   SULPHUR   WT.%
DAY.HOUH  rtAS'H  RFGFN  REOEN  ELUTH  BOILER POILFR  FU'TR
                       CYCLONF FINES   PACK   FLUE  COARSE
? . ] 800
4.0630
S.000 ]
5.0600
5. 1400
6.0000
0.0600
6. 1200
6.2100
/ . 0600
7. 1200
7. 1800
8.0000
b.0600
h. I200
h. 1800
8.2200
V. 1200
9. 1800
10.0600
It). 1200
10. lbM0
1 ] . 0000
1 1 .0350
M.I 200
1 1 . IH3H
12.0000
12.0600
12. 1200
12. 1800
1 3.0000
13.0600
1 J. 1200
1 4 . 0600
14. 1 100
14. 127;0
U. 1800
15.0000
15.0700
If). 1200
0.03
-
0.22
0.06
0.06
0.06
0. 10
0.01
0.01
0.02
0.07
0.05
0.05
0.06
0.0H
0.06
0.06
0.04
0.0S
0.07
0.06
0.04
0.05
0.01
0.03
-
0.02
0.03
0.03
0.08
0.0Q
0.07
0.04
0.06
0.02
0.04
0.07
0.09
0.18
0.09
0.52
0.86
0.81
0.88
0 . 70
1.11 i-)
1 .09
1 .03
- -
0.88 - .
0.35
0.52
0 . 69
0 . 64
0.72
0.15
0.45
0.61
0.67
0.59 1.21
0.77
0.43
0.58 1.50
0.53
0.37
- -
0.65 1.51
0.07
0 .78 ] . 64
0.52 1.61
0.41 1.18
0.53
0.21 0.44
0.18
— —
0.04 1.61
0.52 1.34
0.46 3.34
1.12
1.08 4.30
-
-
—
-
0.34
0.35
—
-
-
-
—
-
—
-
-
—
-
—
-
0.27
-
—
0.26
—
-
-
1.00
-
0.38
0.37
0.25
-
0. 14
-
-
0.24
0.46
1 .06
—
0.85
-
-
0.93
-
0.16
0.91
-
-
-
-
—
-
1.59
-
-
—
-
-
—
1.57
—
-
1.31
-
-
-
1 .44
—
1 .44
—
1 . 17
—
1 .31
—
-
3.80
-
2.03
—
2.34
—
—
1.49
-
1.91
2.84
—
-
-
-
—
-
i.oy
-
-
-
-
—
-
2.33
-
—
2.00
—
-
-
2.70
-
2.26
—
2.28
-
2.07
-
—
2.37
—
2.67
-
2.36
0.22
1 . 06
0.05
0.11
K . 1 6
0.15
0 . 1 4
(5.02
-
0.03
0.23
0.09
0 . 09
0.10
0. 13
0.11
-
,*. 12
0. 10
0.1?
0. 16
0 . 1 y
0.09
—
(5.20
2.49
0 . 1 2
0.07
0.11
—
0.14
0.09
0 . 08
0.23
-
;;. 15
—
0.29
0.24
—
                             - 485 -
-------
                     APPENDIX G.   TABLE  VIII

        ANALYSIS OF SOLIDS  REMOVED  DUKINn HUN 9
          SULPHATE    SULPHUR   WT.%
DAY.HOUR  GAS'R  RFOFN  REGEN   ELUTR  BOILER BOILFK  FLUTR
                       CYCLONE  FINES   BACK   FLUE  COARSE
16. 1500
17.0000
17.0800
1 /. 1245
17. 1545
1 /. 17510
18.0000
18.*) 600
ib. 1200
18. 1800
19.0000
19.0600
IV. 1200
19. 1800
20.0000
20.0600
20. 1600
20. 1800
22. 1800
23.0015
23.0600
23. 1200
23. 1800
24.0000
P4.0600
24..J900
24. 1200
24. 1800
25.0000
2^.0600
26.0000
26.0600
27.0600
27. 1230
27. 1830
28.0000
28.0600
28. 1230
2b. 1845
30.0600
0.10
0.11
0. 12
CO . 09
0. 10
-
0.08
0.07
0.09
0.20
0.07
0. 10
0.08
0.07
0.18
0.08
0.08
0.15
0.08
0.
0.03
0.08
0.06
0.05
0.05
0.
0.
0.02
0.
0.03
0.
0.02
0.
0 . 1 8
0.02
0.03
0.05
0.01
0.04
0.04
0.86
0.97
0.77
0.73
0.75
-
0.44
0.16
0.24
0.01
0.
0.59
0.68
0.62
0.25
0.44
0.78
0.89
1 . 13
1 .04
1 .33
1.73
0 . 77
0.
0.05
0.74
0.23
0.03
0.80
0.45
0.05
1 . 16
1 .26
0.61
0.54
0.59
0.63
0.51
0 . 38
0.76
3.51
4.50
4.20
—
—
3. 14
3.05
—
2.26
-
1 .20
2.53
4.80
4.21
2.70
1 .82
—
0.17
—
-
6.33
-
-
6.79
-
-
2.24
3.50
4. 13
4.70
2.26
4.77
2. 10
2.74
—
1 .95
-
2. 16
2. 16
-
0.41
0.31
0.30
-
—
0.24
0.34
—
0.28
-
0.36
—
—
—
0.22
0.
—
4. 17
—
0.
—
-
—
0.20
-
-
0.07
-
1.23
-
0 . 6(0
—
—
0.34
-
0.36
—
0.31
0.09
0.27
1.24
2.65
1 .49
—
—
1 . 50
2.86
—
—
—
0.87
—
—
—
1.87
-
_
—
-
-
1.37
-
-
1.72
-
-
3. 14
—
2.46
—
2.77
—
—
2.83
—
2.56
—
1 . 95
—
-
2.43
2.24
3.26
—
—
3.20
3.28
_
—
—
2.74
_
—
—
2.84
-
_
—
—
2.21
—
-
—
3.02
—
—
2.71
-
2.78
—
3 . 00
_
-
3.37
—
3.37
-
3.01
—
—
_
0.11
0. 1 1
—
_
0.11
0.07
0.11
0.07
0.05
0.10
0. 10
0.29
fl . 08
0.11
—
_
_
0.
0.07
0.06
0.07
0.04
0.04
0.
0.
0 . 02
0.
1.26
*j *
:.).06
0.04
3.
0.10
0.07
0.03
0.05
k;.(M
0.03
0.10
                              - 486  -
-------
                      APPENDIX   G.   TABLE   VIII

        ANALYSIS OF SOLIDS REMOVED DURING RUN  9
          SULPHATE   SULPHUR   WT.%
DAY.HOUR  GAS'R  RFGEN  REGEN  ELUTR  BOILER  BOILER   FLUTR
                       CYCLONE FINES   BACK  FLUE   COAhSF

3i'.1?»i«    0.0b   0.75   2.67    -       -      -     0.04
IV. IW0    0.04   0.78   2.46    -                    0.06
31.0000    0.05   0.47   3.43   0.12    3.4?    4.61    0.1H
31.0000    0.07   0.45   3.33    -       -      -     0.12
31.1?00    0.06   0.Q4   3.73    -       -      -     0.13
31.1ht10    0.06   1.0?   3.05    -                    0.0^
32.0000    0.02   0.25   2.84   0.49    1.64    2.23    0.13
32.0600    0.05   0.76   3.72            -      -     0.46
3?.0900    0.05   0.76   3.7?   0.49    1.64    2.23    0.46
                              - 487 -
-------
APPENDIX   G.
                            TABLE   IX.
        ANALYSIS OF  SOLIDS  RFMOVFD DURING RUN 9
              101AL   CARBON   WT%
DAY.HOUR  GAS'h  RFGFN   RP.GFN   FLUTR ROILFR HOILFR  F.LUlh
                       CYCLONF FINFS  RACK   FLUF  COARSF
2 . 1 800
4.^630
5.000 1
5.060?
5. M00
6.0000
6.0600
6. 1200
6.2100
7.0600
7. 1200
7 . ] 8C*0
8.0000
8.,'; 600
8. 120?)
ci. 1800
8.2200
9. 1200
V. 1800
10.J600
10.1200
10. 1800
1 1 .K^P1^
1 1 .03^^
11.1 2BM
11.1 HC"B
12.I/50MM
12.W6/K
1?. 12KB
1 ? . 1 tf 00
13.0DMW
!3./06r/0
13. 12««
J4.«)6M«
U.I 1 0«
U. I2«M
14. IHC^tO
I^.OI^COM
IS. 07P«
IS. 12iW
W. 29
tf .34
0.
«.
0.
0.
0.
0.
0.58
0.09
0.19
0.37
0.
0.
0.
0.71
0.42
<;.06
0.
0.12
0.06
0.37
0.42
0.14
0. 14
0.24
0.
0.86
0.06
0. 14
0.3h
0.26
0.57
1 .87
1 .81
1 .39
0.
0.16
0.22
0.13
0.
0.02
0.
0.
(ft
VS 9 —
0.
0.
0.
0.07
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0. 2.30
0.
0.
0. 0.56
0.
0.
0.
0. 0.30
M
t> * ~~
0.
2.63
0. 10.40
0.
0. 0.36
0.
— -
0.45 0.97
0. 1.63
0.05 0.82
0.
0. 1.07
-
—
—
-
1 .63
0.59
-
—
-
—
—
-
-
-
—
-
-
-
-
7.07
-
-
3.53
-
—
—
2.77
-
10. 9b
0.79
-
—
lb.59
-
-
3.05
9.00
3.07
—
3.75
6.15
1 . 20
0.14 0.25 0.02
a . 3n
0 . 0 . 0.31
0 . 0 . 0 .
0.03
0.24
_ _ _
1.75
2.33
0 . 90
0. 0.06 0.
f*
"~ V> •
0.
0.56
0.03
vl.34
0.
0.16 2 . 82 J . 1 0
0.15
0.18
0.M 2.92 0.26
- - -
0.19
0 . 30;
0.13 3.3J 0.06
0.74
0.25
- - -
0.41
0 . 6S
0.67 12.88 1.13
1.80
_ _ _
0.21 7.48 1.56
_ _ -
0.37 0.31 0.^2
0.25
0.74 5.^4
                          -  488 -
-------
           APPENDIX   0.     TABLE   IX.

        ANALYSIS OF SOLIDS  RHMOVFD DURING HUN 9
              TOTAL   CARBON    WT%
UAY.MOUR  OAS'k  RF.GEN   RFGEN   FLUTH ROILFH BOILER  FLUTR
                       CYCLONE FINES  PACK   FLUH  COARSF
16. 1500
I /.Wiro
1 7 . 0fa00
17. 1245
17. 1545
17.1 700
18.0000
18.0600
18.1 200
IH. 1800
19.0000
19.0600
19. 1200
19.1 800
20.0000
20.0600
20. 1600
20. 1800
22. 1H00
23.0015
23.0600
23. I2C'0
23. 1800
24.0000
24.0600
24.0900
24. 1200
24. 1800
25 . 0000
25..J600
26.0000
26.0600
27.J600
27. 1230
27. IH30
28.0000
28.0600
28. 1230
28. J845
30.0600
0.
0.
0.
0.13
0.22
-
0. 13
0.40
0.21
0.
0. 18
0.
0.
0.
0.05
0.62
0.09
0.
0.20
0.
0.
0.
0.22
4.27
1.47
0.32
0.22
0.
0.
0.13
0.
0.71
0.
0.
0.
0.
0.
0.
0.
0.
0.50
0.
0'.
0.
0.
-
0.
0.
0.
0.04
0.
0.
0.
0.
0.
J.93
0.
0.
0.
0.
0.
0.
0.
0.32
0.45
0.
0.
0.
0.
0.
0.48
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.42
0.85
0.81
—
-
0.74
0.77
-
1.73
-
2.82
3.97
3.29
0.42
0.48
0.
-
13.95
-
—
2. 18
-
—
2.07
—
-
2.24
1.72
1.09
0.10
0.96
2. 19
0.20
1.03
-
2. 14
-
4. 1 1
0.26
-
6.57
17.24
18.23
—
-
11 . 05
12.89
—
20.54
—
24.09
—
—
—
1 1.69
0.
-
0.69
—
9.29
-
—
—
22.49
-
—
3.77
—
0.03
—
3.37
-
—
14.75
—
5.69
—
14.36
13. 15
0.35
0.59
0.04
0.28
—
—
0. 13
0.
—
-
—
0.88
—
-
—
0.09
—
-
—
—
—
0.25
—
-
0.02
-
-
0. 18
—
0.19
—
0.
-
-
0.20
-
0.17
—
0.28
—
-
6. 13
10.57
4.26
—
-
0.59
3.82
—
-
—
14.29
-
—
—
4.67
—
-
—
—
5.65
-
_
—
1 1.81
—
-
5.69
—
2.37
—
5.83
-
—
7. 18
—
6.47
—
0.85
-
—
—
0 . 15
0. 19
—
-
0.27
2.32
0.42
0.53
6.95
0.68
0. 36
3.27
1 .94
0.46
—
—
—
1 .35
0.08
0.
0.49
I .06
7. 11
3.25
1 .42
1 .70
0.
0.
0.41
2.24
0.
1 .47
1 .22
4.79
5.7^
2.22
1 . 16
3 . 09
9. 19
                           - 489 -
-------
                      APPENDIX G  TABLE IX

        ANALYSIS   i>F ^OLIUS  KFMOVhD OUR I NO  WIN V
DAY.HOUh   GAS'K  hFOFN  RFOFN  FLUTH ROILFH  BOILFH  F.LIJTI*
                        CYCLONF FINFS  PACK    FLUF  COAHSF
30.
30.
?1.
?1 .
31 .
31.
32.
32.
32 .
1 200
1 8.00
0000
0600
1 200
1 800
0000
0600
0y00
0.
0 .
0.
0 . 16
0.
0.
0.
0.
0 .
0.
0.
0.
0.
0.
0.04
0.
0.
0.
0.
2.
3.
0.
0.
0.
0.
0.
0.
55
97
15
90
54
23

36
36
—
-
4. 14
-
-
—
6.84
—
6.84
-
-
0.
-
-
—
0.
-
0.


16



12

12
-
-
4.
-
—
—
0.
—
0.


21



64

64
0.
10.8V
1 .28
1 3 . 62
3.93
0.67
2.26
0.71
0.71
                            -  490 -
-------
                   APPENDIX  G.
                             TABLE  X
       SOL IDS REMOVED DURING RUN 9, KG.  (RAW DATA)

DAY.HOUR  GAS'R  REGEN  RFGFN  ELUTR BOILER BOILER  FLUTR
                       CYCLONF FINES  BACK   FLUE  COARSF
 0. ! /30
 2.06ft;
 2 . ! 800
 3.0800
 4 . 0630
 4. 1525
 4. 1600
 4. 1820
 4. 1955
 4.?0?5
 4.2315
 5.^420
 5.0600
 5.1100
 5. 1205
 5. 1220
 5.
 5. 1720
 5. 1845
 5.2045
 5.2359
 6.0045
 6.0145
 6.0245
 6.0300
 6.0420
 6.0515
 6.0615
 6.0715
 6.0730
 6.0815
 6.0915
 6. 1 100
 6. 1200
 6. 1430
 6. 1600
 6. 1900
 6.2030
 6.2035
 7.0230
0.9
0.9'
0.91
0.91
0.91
0.9'
0.91   0.91
0.9'
0.91
               9.30
 0.68   0.11   4.V9
 0.91    -     14.06
32.21    -     5.44
        4.76
 1.59    -
 1.36
 1.59   2.49  23.59
 1.59
 4.08    -
 0.91   2.49   14.06
                      17.92
 0.91    -
 2.27  12.25  22.68   4.31
                      7.71
                      6.12
13.61   Q.53   7.26   2.95
20.41    -
 9.98   4.54   6.80   2.95
 5.44    -
32.66   3.63   9.07   0.91
 5.22    -
 5.90
               6.80
 8.16    -
 8.85
 2.49    -
 8.85    -     8.16   0.91
10.66
               3. 18
 5.67    -
 4.76
 3.40    -    12.70   15.20
 5.44  39.46
 5.44  27.67  14.06
12.70   9.53
 2.72    -
       11.11   5.44  21.77
               1.81  20.87
  -                   12.93
                          - 491 -
-------
                    APPENDIX G  TABLE X
       SOI. IPS  REMOVED DUOTfG    HUN 9   KG. (RAW DATA)
DAY.MOUH  GAS'h   h'FOHN
7.J700
/.0730
7.0830
7.0930
7. 1000
7. 1  100
/ . 1 5 3d
7 . 1 630
/ . 1 900
7.2130
7.2230
8.0005
8 . 00 30
8. ,1130
8.0230
8.0315
H.0630
8.0730
0.0830
  1000
  I 130
  1230
  1330
  1 "-,00
  1600
  1700
  1800
   2000
   2100
   2200
 9. ,3800
 9 . 1 1 30
   1230
   1330
   M30
   1 630
   1730
            1.36
1.36
            1.36
1.36
           2.72    2.72
           2.72    2.72
           2.72    2.72
          2.27    2.72
RFOFN
CYCLONE
_
-
-
-
-
-
—
-
-
-
—
-
—
-
-
—
_
-
—
—
—
-
—
1.13
-
1.59
1.13
0.68
-
1. 13
-
—
-
-
-
4.54
-
—
FLUTH ROILFH
FINFS RACK
3 . 63
20.87
— -
3. 18
1 . 36
1 .81
9 . 30
6.12
4.54
— —
_ _
51.26 6.80
0.91
- -
— —
— —
w _
— —
— -
— —
10.21
0.91
0.91
1.81
0.91
2 . 95
— -
3.18 12.70
— —
1.13
- -
— . —
— —
35.38
— -
0.91
1.36
0.23
HOILFH
FLUF
_
12.2^
-
4.54
-
_
—
—
8. 16
-
—
9 . 98
—
-
—
—
^
—
-
_
19.05
-
4.S4
2.05
-
2.72
-
4.54
—
2.95
~
-
12.25
-
7.71
—
-
-
FLMTk
COAHSF
_
6.35
4.54
3. 18
1.81
25. 8^
3.18
—
V . 0 1
4.^4
4.54
6 . 80
5.44
4.54
4.R4
4.54
4.^4
4.^4
4.54
4 .K4
7.26
9.30
10.43
4.oy
6 . 80
6 . 80
6 . 80
6 . 80
6.80
6.80
6.80
6.80
6.80
-
6 . 80
3 . 4;^
2.72
4 ,O^
                         2.27
                           - 492  -
-------
                    APPENDIX G  TABLE X

       SOL1PS  kFMOVF-n.n.UHJNO RUN  9, KG.  (RAW DATA)

PAY. HOUR  GAS'R   RFOFN  RFOFN  FLUTR  BOILFR BOILFH  FLUlh
                        CYCLONF FINFS   RACK   FLl.'F  CO,a RSh
y. 1800
9. 1930
y.2030
10.0300
10. 06 IS
10.0755
10.0900
10.1 200
10. 1400
10.1515
10. 1700
10. 1800
10. 1845
10.2150
10.P245
0.2255
0.2350
. <; 11 0
.0200
. *J 3 1 0
.0350
.«)4]0
.0600
. 0800
.,5900
. 1 000
. 1 100
. 1 200
. 1P30
. 1 300
. M30
. 1 730
. 1 800
. 1 830
.1930
.2030
.2130
.2230
.2310
.P3sy
P. 27 2.7?
- - _
1.36
- - _
1 . 36
_ _ _
- - _
2.27 2.72 2.04
- - _
- _ _
— - _
2.27 2.72
- - _
- _ _
5.44
— _ _
2.27 2.72 1.36
- _ _
1.36
- - _
2.27 2.72 0.91
— - -
0.91
1.13
— _ _
0.68
- _ _
2.27 2.72
— _ _
- - _
1.13
— - _
P. 27 2.72
— _ _
1 . 36
- _ _
— — _
— _ _
1 . 36
0.45
y . 98
1.59
— —
1.59 16.78
1.13 9.53
_ _
4.54
2.95 11.34
1 .81
— _
2.49 6.58
— _
2.95
— —
- -
— -
3.18 11.34
- -
1 .36
1.13
0.45
— —
1 . 36 9 . 98
2.04
— —
1 .81
— -
1 .81
- -
3.63
2.27
— —
1 .59 6. 1?
— _
— _
2.04
— _
_ —
5.22 12.02
1.13 3.40
11.34 0.91
6.3S
1.81
8.16
5.W/1 5.44
4.54
8.16
9.53 4.54
4.K4
6. 3^
5.90 4.^4
0.80
3.63
4.54
_ _
3.63
8. 16 6.80
9.07
y.07
9.07
_ _
9 . 0 /
7.71
9 . 0 7
9.07
9 . 0 7
9.07
9.07
P. 7?
8. 16
— _
4. /6
5.44 .0.91
4.09
4.99
4 . 76
4.5/1
4 . S 4
6.35 4.54
1.5y 5.4^
                            -  493 -
-------
                  APPENDIX   G.    TABLE  X

       SOLIDS  RFMPVPn pnpjvr. HUN 9, KG. . dM'" J'ATA)

nAY.IIOtJh  GAS'R   KFGFN  KFOEN  FLUTR  HOILFR hOILFR  FLUTK
                        CYCLONF FINFS   HACK    FLUF  COARSF
12.01130
12.0245
12.0345
12.0450
12.0550
12.0600
12.0700
12.0805
12. 1000
12. 1200
12.1530
12.1 800
12.2200
13.0000
1 3.0200
13.0600
13.0/30
13. 1200
1 4 . 0030
14.0^00
14.0800
14. 1200
14.1 800
I5.0000
15.^800
15. 1030
15. 1200
16.0430
16.0830
16.11 00
16. 1500
16. 1945
17.0000
1 /.0600
17.0800
17.1110
17. 1245
17. 1545
17. 1640
:
—
2.27
-
—
-
—
-
1 .36
-
1.36
—
1 .36
-
-
—
1 .36
—
-
_
2.72
1 .36
9.53
-
9.53
2.27
-
-
—
2.27
—
2.27
—
2.27
-
2.27
2.27
-
•"•"
—
2.72
4.99
-
4.54
4.54
-
1.36
—
1.36
-
1.36
-
-
-
1.36
-
-
—
1.36
1.36
9.53
-
19.05
0 . 9 1
-
—
-
0.91
-
0.91
-
0.91
-
0 . 9 1
0.9]
-
0.45
—
0.68
-
0.23
-
—
0.68
0.23
1.13
0.45
—
1 . 13
-
-
-
1 .36
-
-
—
0.91
0.68
-
-
5.44
0.23
-
0.91
0.23
0.91
0.45
0.45
0.45
0.23
-
-
-
-
1 .36
—
1 .36
—
1 .36
-
—
2.49
0.91
2.72
0.91
2.27
1 .36
1 . 13
3. 18
—
2.72
-
—
3. 18
1 .81
1.81
2.27
1.59
0.68
0.45
2.27
0.91
0.68
1 .36
2.04
3.63
2.95
2.27
-
-
—
-
™ *
—
-
—
4.54
-
-
-
3. 18
—
4.54
2.72
1 .36
-
1 .81
-
3.63
338.83
-
0.91
0.45
0.91
-
-
0.45
0.23
2.95
4.54
1 .36
3. 18
6 . 80
2.04
5.67
2.95
8.16
—
-
10.89
m^
—
—
-
4.08
-
-
-
4.54
-
3.63
3. 18
1.36
2.72
-
4 . 99
4.08
-
14.97
—
6.80
6.35
4.08
4.99
1 .81
1 . P 1
16. 10
-
6. 35
5.22
4. 99
2.72
7.03
1.36
-
-
-
-
4.S4
4.S4
A .54
4.54
-
0 . w ]
-
—
1 .36
0 . 9 1
-
-
—
1 .36
-
-
-
0.91
25. "0
—
—
0.91
-
2.95
1 .81
9.5 j
-
-
-
-
-
-
7.71
-
0.9]
-
—
-
-
1  /.I 700
1 .36
                         - 494  -
5.90
-------
                  APPENDIX  G.   TABLE   X.

       SOLIDS  kFMovpn  nuuiiNn RIIN-Q, «n. (ww PATM
HAY.HOUk  OAS'K   hFOFN   HFGFN  FLUTR HOILFk HOILFU  F.LU'IH
                        CYCLONF FINFS  RACK   FLUF  COAHSF

17.lo?h     -      -       -       -     7.71
i i . /<.) ri
18.^000
18.0600
18.0030
18. 1 1 30
18. 1200
18. 1400
18.1 700
18. 1800
18.2000
18.2200
19.0000
19.0600
19. 1030
19. 1 J30
19. 1800
1 9 . 2000
19.?345
?0.0230
20.0600
20. 1 K;0
20. 1430
20. 1530
20. 1630
20 . 1 8i00
?0 . 1 900
20 . 2000
??. I/, 30
22. 1320
22. 1600
22. 1730
22 . 1 800
22.2000
22.2245
23.001b
23.0200
23.0300
23.042^
23.0600
— — —
2.27 0.91 1.81
2.27 0.91
- - _
- - _
2.27 1.36 2.72
— — _
- - _
- - _
- _ _
- - ..
2.72 1.36 1.81
2.72 1.36 0.9!
- _ _
- - -
— — —
1.81
2.72 1.36 1.81
— _ _
2.7? 1.36 1.36
1.36
— — _
1.13
- - -
— _ _
0.91
— — —
1.81
1.36
— — _
1.13
?.?7 0.91
- — _
0.45
2.27 0.91 0.11
— — —
- - -
— — _
2.27 0.91 0.23
—
8.62
8.30
5.67
2.72
_
4.54
2.72
_
3 . 40
1 .81
2.27
2.27
?.95
2.72
8.62
4.99
9.07
7.71
5.90
9.07
4.54
1.36
—
_
5.90
1 .36
50.80
9.53
3. 18

2.27
.3.86
4.99
2.95
_
5.44
—
5.90
—
5.67
5.90
2.49
_
_
2.27
_
_
_
«.
5.44
7.03

4.99

•»
7.26

3.63
_
8.62

3.40

__
386.01
0.91

_
^
0.23

_
0.23

-
_
0.68
_
8 . 39
3.63
?.?7

«.
__
^^
3. 18

^
3.18
4.54
3.86
	
4.08

3. 18

4.54
9 . 30

_
^m
14.51
?.49
0.?3
7.?6


_
1 1 .79

	
2.7?

—
__
?.?7
6 . 35
2.^9
0.91
14.06
2.72
1 .81
4.0«
2.27

3.63
5.44
0.U 1
0.0)
?.40
3 . 1 ^
6. 3S
2.04
23.59

1 .36
2. 7?
2.27
2.27


_
6.80
4 1 . 73



1.81

_
0.9J
4.^4
* • r
4.^4
4.^4
5.4/1
                       - 495 -
-------
                  APPENDIX  G.     TABLE  X.

       SOLIDS  RFMOVFO DURING RUN 9,  KG.  (RAW DATA)
DAY.HOUR  GAS'k
HhGFK  KFGHN'  ELUTR ROIU-R i-iUL-s   F:.L!1TK
      CYCLONFJ  FINFS  BACK   FLUF  OOAkSF
23.0700
23.0^20
23. 1200
23. 1600
23. 1800
23.2045
24.0000
24.0600
24.0800
24.0935
24. 1045
24. 1200
24. 1500
24. 1800
24.2000
25.0030
25.0230
25.0430
25.0730
25. 1210
25. 1500
25.2030
25.2300
26.0530
26. 1200
26.2000
27.0000
27.0800
27. 1230
27. 1830
28.0000
28.0600
28.0700
28.0800
28.0900
28. 1 100
28. 1230
28. 1345
28 . 1 400
28. 1600
—
—
0.91
-
0.91
-
0.91
0.91
-
0.91
-
0.91
-
0.91
-
—
-
-
-
-
41 .28
—
-
-
124.74
—
—
-
0.91
0.91
0.91
0.91
-
-
—
-
—
-
0.91
—
— _ :
— —
0.91
- -
0.91
— —
0.91 0.34
0.91 0.45
_ _
0.91
- -
0.0] 0.45
— -
0.91 0.68
- -
0.45
- -
- -
- -
- -
0.91
- -
_ _
- -
_ _
- -
- -
10.89
0.91 1.59
0.91 2.04
0.91 2.27
0.91 6.58
- -
0.68
— -
— —
- -
- —
0.91 1.13
- -
-
4.99
17.24
3.86
2.27
-
4.99
8. 16
2.27
-
3.63
3.63
5.44
5.44
5.44
4.08
9.07
2.95
4.31
-
9.07
3.63
2.27
3.63
-
11 .79
1 1 .79
7.71
4.76
6.80
6.35
6.80
-
1 .81
-
-
—
-
2.72
-
-
-
0.01
-
0.45
-
1 .81
1.13
-
—
-
1.13
-
1 .81
-
" 0 . 68
0.45
-
-
-
0.91
4.08
-
-
41 .28
-
0.91
0.45
1 .81
2.04
1 .59
1.36
-
-
-
-
-
-
2.72
-
4.^/1
- -
3.18 15.88
- -
11.3/1 0.0)
86. 18
2.05 0.o|
2 . 95 0.0]
- -
0.0]
- —
0.91
- -
1.81 1.81
_ _
2.72 4. 08
5.90
2 . 72
2.49
19.06
- -
^ i v,
~j . i ^ >
2.27
0.01
- -
4. C38 -
6.58 5.44
^.67 10.89
5 . 90 0.0)
2.27 35.38
1.50 0.0|
1.81 16.78
3. 18
4.R4
4.^4
4.54
4.54
4.54
2.04
- 10.21
                         -  496  -
-------
       SOLIDS REMOVED DURING RUN 9, KG. (RAW DATA)

DAY.HOUR  GAS'R  REGEN  RFGFN  ELUTR BOILER BOILER  ELMTR
                       CYCLONE FINES  RACK   FLUE  COARSE
28. 1845
28.2045
28.21 15
28.2300
28.2345
29.0400
2V. 1440
29. 1600
2V. 1800
3i/;.«l00
30.0445
30 . J600
30.0745
30. 1000
30. 1240
30. 1 300
30 . 1 400
31.0000
31 .0600
31.0800
31.0900
31.1 000
31.1 600
31.1 700
3 1 . 2«00
31 .2030
32.0000
32.0600
32.0930
0.91 0.91
- -
9.07 16.78
17.24
15.88
— —
_ _
— —
33.57
— —
- -
0.91 0.91
- —
- -
13.61
4.54
6.80
0.91 0.91
0.91 0.91
- -
2.72
4.54
36.29
- -
- —
- -
0.91 11.79
0.91 0.91
1 18.84
5.44
14.51
—
-
8. 16
-
1.13
-
—
0 . 68
1.36
—
2.49
6. 12
4.08
-
5.44
3.63
6.80
3. 18
-
0.91
-
—
5.22
-
0.91
0.45
-
7.71
—
—
—
5.44
—
—
—
—
3. 18
5.90
1 .59
0.45
0.68
1.36
1 .36
—
1 1 .34
1.81
—
—
1 .36
—
3. 18
-
b. 16
7.71
12.25
—
3.63
—
—
-
0.68
29.48
—
58.97
—
—
-
7.26
-
3.86
-
-
-
7.26
5.44
—
-
0.91
—
—
—
8.39
4.54
3.63
—
4.54
—
—
—
4.54
—
—
—
—
—
—
16.78
—
2.27
—
-
—
5.90
2.72
—
—
5.90
—
_
—
7.03
2.27
2.72
—
0.91
—
_
—
—
—
—
—
—
—
—
0.91
-
11.11
4.51
1.81
—
0.V1
0.91
—
—
—
_
—
—
—
1 .36
—
_
                         - 497 -
-------
 Appendix G.   -   Table   XI
 Run 9 - Gasifier Bed Particle  Distribution

SIEVE  SIZE IN MICRONS
SAMPLE
NUMBER
SXSE3ESSSCS

51556
51559
51562
51567
51573
51576
51583
51585
51588
51591
51594
51598
51606
51603
51610
51615
51617
51620
51623
51631
DAY- 3200 2800 1400 1180 850
TIME 2800 1400 1180 850 600

2. 1800
4.0630
5.0001
5.0600
5. 1400
5.2359
6.0600
6.1200
6.2100
7.0600
7.1200
7.1800
8.0600
T .2359
8* 1200
8* 1800
8.2200
9.1200
9.1800
10.0615

• 1
• 5
.9
• 2
• 4
• 2
• 3
• 5
.2
• 2
• 3
.2
.2
.2
.2
.2
.2
.2
.2
.2
600 250
250 1 50
150
100
100
WT. PERCENT.
7.6
7.6
8*4
7.6
6.5
8.4
9.3
12.2
11.1
9.4
9-5
10.3
9.8
0.0
4.2
1*0
2.6
0*8
1.7
2.3
11 .3
10.9
11.5
10.6
9.4
11*3
12.0
14.2
14.1
13.0
12.4
12.6
13*2
12.1
5.5
13*6
14.8
13^5
14.4
14.9
25.6
24.5
24.0
24.5
23.9
26.4
27.8
28*4
29*6
28.3
26.8
26.9
29.0
27. 1
32.4
29.9
30*5
29.9
30.4
30.7
27.0
26.4
25.2
26.7
28.0
27.9
27.2
23.9
27.3
28.6
27.2
25.6
28.7
26.2
29.1
28.7
27.3
28-8
28.3
28.1
27.8
29.7
29.4
29.9
31 *0
25.5
23.0
20.3
17.5
20*4
23.5
23.6
19.1
24.2
18.4
6.5
4.5
6.7
4.9
3.8
• 3
• 1
.5
• 6
.7
• 2
.4
• 5
• 1
• 1
.3
• 8
.1
• 2
.2
• 1
• 1
• 2
• 1
• 1
• 1 !
. i
.0
.0
• 1
.0
. 1
.0
. 1
• 0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
• 1
. 1
• 0
• 0
• 1
• 0
.0
.0
. 1
. 1
.0
• 0
• 0
• 1
.0
.0
.0
• 0
• 0
.0
          - 498  -
-------
Appendix G.    -   TABLE XI
Run 9  -  Gasifier Bed  Particle  Distribution
SIEVE SIZE 1
-=====as==xa==========csss===z===a==r
SAMPLE DAY- 3200 2800 1400
NUMBER TIME 2800 1400 1180
S=========se*S3SZ==ax=3======Z==3===5
N MICRONS
1180 850
850 600
:============
600 250
250 150
150
100
100
WT. PERCENT
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
633 10.1200
636 10.1800
646
648
651
659
662
664
671
676
683
692
693
696
701
704
708
716
725
1.0350
1 .1200
1 . 1800
1.2359
2.0600
2* 1200
2.1800
2.2359
3*0600
3*1200
4*0600
4.1100
4.1200
4.1800
4.2359
5.0700
5. 1200
-2
.2
• 2
• 1
.2
• 1
• 1
.2
• 1
.1
.2
.1
.1
.2
.2
.1
.2
.2
• 2
10.0
10.5
11.1
8.7
9. 1
10.8
9.4
8*4
8*6
10*3
10*4
9.8
10.6
10.7
9.9
10.8
1 1 .0
9.3
9.3
13*0
13*4
14.3
12.9
12.9
13.5
13.3
12*8
12.8
14.3
15.7
14*2
14.9
14.8
14.5
14.6
14.7
14. 1
14. 1
29.5
29.8
30.7
30. 1
29.9
31*2
30.9
30.5
30.7
31. 1
33.7
31. 1
33*0
32.8
32*3
32.3
33.9
31*8
32.4
30*6
30.3
29.7
31 .9
31 .5
30.6
31 .2
32.2
31 .8
29.8
27.6
30.1
29.7
28.8
30.0
29.5
29.0
30.8
31 .0
16.7
15.7
13.9
16. 1
16*2
13.7
15.0
15.8
16.0
14.2
12.2
14.5
1 1.7
12.6
13*0
12.5
11.1
13.7
13*0
. 1
.0
. 1
. 1
.2
. 1
. 1
. 1
. 1
.1
.2
.1
.0
. 1
. 1
.1
. 1
. 1
. 1
.0
• 0
.0
.0
.0
.0
.0
• 1
.0
.0
.0
.0
.0
• 0
.0
• 0
.0
.0
• 0
.0
.0
.0
.0
.0
. 1
.0
.0
.0
• 0
.0
.0
.0
.0
.0
.0
. 1
.0
.0
         - 499 -
-------
Appendix G.    -   Table XI
Run 9 - Gasifier Bed Particle Distribution
SIEVE  SIZE IN  MICRONS
SAMPLE
NUMBER
*WS3E**SSS3
51732
51731
51739
51746
51749
51831
51839
51841
51848
51852
51858
51863
51868
51878
51880
51885
51887
51893
51900
DAY- 3200 2800 1400 1
TIME 2800 1400 1180
; 55 35 35 31 »»™»**~™^*"»"**"»"»**»"»"«»«"*p*»tf«*ww««*"»"
16.
16.
17.
17.
17.
17.
18.
18.
18.
18.
19.
19.
19.
19.
20.
20.
20.
22.
23.
2359 .2 8
1500 .2 6
0800
1245
1545
2359 .5
0600
1200
1800 •?
2359
0600
1200
7
8
7
I 6
5
7
> 5
5
5
5
1800 .1 5
2359 .0 3
0600 .1 4
1600 -2 5
1800 .2
1800 .1 5
0015 .2 6
180
850
• ••• w •* *» «w
WT. PERCENT
•0 12.7 33.0
.9
.5
• 1
.9
• 3
• 4
• 4
.4
• 3
.9
.7
.2
.2
.6
.0
4.5
• 4
.0
12.2
12*4
13.4
13* 1
1 1.3
10.4
13.4
10.5
10.9
1 1*6
10.9
10.3
7.5
9.3
10.1
9.2
9.9
1 1 .0
33.0
32.8
33.4
33.2
32.8
32.2
35.5
31.2
31.5
32.9
31.8
30.0
26.3
28.2
30*3
29.
30.8
32.5
850
600
33.7
34.8
34.7
33.4
33.9
36.4
37.5
32.4
36.8
37.2
36.3
36.4
35.8
38.0
35.6
35.6
2 36.
35.4
34.9
600 250 150 1
250 150 100
12.4
12.8
12.4
11.3
1 1.6
13. 1
14.2
10.9
15.6
14.8
13.0
14.7
17.9
24.3
21.5
18.4
4 20. 1
1 7.6
15.1

.
.
.
.
.0
• 1
.2
.2
. 1
. 1
• 3
.6
.7
.5
• 2
.2
.6
.2
.0
• 0
• 0
• 0
.0
.0
• 0
.0
.0
.0
.0
.0
.0
.0
. 1
. 1
. 1
.0
• 1
00
• 0
. 1
• 0
• 1
. 1
• 0
. 1
. 1
• 1
.0
.0
. 1
. 1
. 1
. 1
• 1
1
.2
.0
        - 5OO  -
-------
Anpendix G.    -  Table XI
R'in 9  -  Gasifier  Bed Particle Distribution
SIEVE SIZE IN MICRONS
SAMPLE DAY- 3200 2800
NUMBER TIME 2800 1400

51905
51906
51909
51912
51920
51925
51927
51934
51938
51945
51951
51958
51962
51972
52002
52004
520! 1
52020
52023

23.0600
23. 1200
23*1800
23.2359
24.0600
24.0900
24. 1200
24.1800
24.2359
25*0600
26.0001
26*0600
27.0600
27.1200
27. 1830
27.2359
28.0600
28. 1400
28. 1845
1400 1180
1180 850
WT. PERCENT
.2
.2
.1
.2
.2
.2
.1
. 1
. 1
.2
.1
.2
.2
.2
.1
.2
.2
.2
. 1
7.4
7.9
7.7
6.0
6.4
7.3
7.7
5.8
7.2
6.3
6.7
6.9
5.9
8.9
7.2
6.3
7.1
7.6
5.3
12.3
13.4
12*6
1 1.5
12.0
13*4
13.5
11*1
12.6
12.1
12.4
12.8
10.8
13.4
12.3
11.5
12.0
12.4
9.9
33.7
36.6
33.7
32«5
32.9
32.6
33.0
30.7
32.0
31 .7
32.3
31 .7
29.3
31 .9
31.2
30.8
30*6
31 .0
28.5
======
850
600

33.5
27.6
33-7
35.7
34.8
33. 1
32.7
35.2
33.0
34.0
33.7
32.5
33.4
30.6
32.4
33.4
31 .8
31 .8
34.0
600 250
250 150

12.8
14.2
12.2
14.0
13-4
13. 1
12.9
17.0
15.0
15-6
14.8
15.7
19.8
14.8
16* 5
1 7.6
17.9
16.9
21.8

• 1
• 1
• 1
• 2
• 2
. 1
• 2
.1
• 1
.2
.0
.2
.6
.2
.2
.2
. 4
. 1
.4
150
100

.0
.0
.0
• 0
.0
. 1
.0
.0
.0
.0
.0
.PI
. 1
.0
.0
.0
.0
.0
.0
                                                  100
                                                     .0
                                                     .0
                                                     .0
                                                     .0
                                                     > 1
                                                     .0
                                                     .0
                                                     .0
                                                     .0
                                                     .0
                                                     .0
                                                     • PI
                                                     >0
                                                     .0
                                                     . 1
                                                     . 1
                                                     > I
                                                     .0
                                                     .0
         - 501 -
-------
Appendix  G.    -  Table  XI
Run 9 -   Gasifier Bed Particle Distribution


SIEVE  SIZE  IN MICRONS
SAMPLE
NUMBER

52027
52031
52035
52039
52046
52051
52056
52060
52067
DAY- 3200 2800
TIME 2800 1400
1400
1 180
1180
850
850
600
600
250
250
150
150
100
100
WT. PERCENT
30*0600
30 • 1200
30. 1800
30.2359
31*0600
31 - 1200
31 • 1800
31 .2359
32.0600
.2
.2
.2
• 1
.1
. 1
• 1
.2
.2
5.9
4.2
5.2
4.9
4.6
4.5
5.2
5.1
5.7
10.7
8.3
9.3
9.1
8.8
8.5
8.5
8.5
8*8
29.3
25.3
26. 1
26.8
26. 1
24.2
23-2
23.8
24.4
34.0
33.8
31.5
33.1
33.0
31 .8
30.1
30.8
30.9
19.7
26.5
25.4
25.5
27.0
29. 1
29.9
30.3
29.8
.2
1.3
1.8
.4
.4
1 .3
2.1
1 .0
.2
. 1
. 1
.2
.0
.0
• 1
• 3
• 2
• 0
.0
.2
.2
• 1
.0
.3
.6
.2
.0
          -  502  -
-------
           APPENDIX G   TABLE XII
RUN 9 -Regenerator Bed Particle Distribution

         SIEVE SIZE IN MICRONS
SAMPLE
NUMBER
========
DAY-
TIME
=========
3200
2800
= S Z 3 S Z
2800
1400
ax = = = =
1400
1180
=======
1180
850
=======
850
600
=======
600
250
= = = = =
250
150
======
150
100
=====—
100


WT. PERCENT.
51557
51560
51568
51563
51577
51574
51584
51586
51589
51592
51595
51599
51604
5161 1
51614
51618
51624
51632
51634
2.1800
4.0630
5.0600
5.0001
5.2359
5*1400
6.0600
6.1200
6.2100
7.0600
7.1200
7. 1800
8.0001
8.1200
8. 1800
8.2200
9.1800
10.0615
10. 1200
• 2
• 3
• 2
• 2
• 3
• 2
• 2
• 5
• 2
.1
• 2
• 2
• 3
• 3
.2
• 3
• 3
• 3
.2
6.4
6.6
7.2
7.2
8.4
8.3
10.8
10.4
10.0
7.9
9.6
10.4
1 1.6
12.6
12.0
11.5
12.5
6.0
11.1
11*0
11*1
10.2
10.4
11.3
1 1.2
12.9
12. 4
13.1
12.0
12.9
13.2
14.1
14.6
14.2
14.3
14.7
16.7
14.0
25.6
24.3
23.4
23.5
25.7
25.4
28.4
27.9
28.4
27.9
26.9
26.6
29.1
28.9
29.1
30.1
30.0
33.1
30.2
27.0
25.0
25.7
26*3
27.3
26.9
26.1
25.9
29.9
30*6
26.9
24.8
27.2
26.4
27.9
28.2
27.8
29.4
29.3
28.9
31*6
31.2
31.5
26.6
27.4
21.4
22.4
18.3
21.1
23.2
23.4
17.7
17.0
16.5
15.7
14.6
14.3
15*1
.7
1.0
1.9
.9
• 3
• 5
• 3
• 5
• 2
• 4
• 2
1.2
• 1
• 1
• 1
• 1
• 1
• 2
• 1
. 1
• 0
. 1
. 1
• 1
. 1
.0
.0
.0
. 1
.2
.0
.0
.0
.0
.0
• 0
.0
.0
. 1
.0
. 1
.0
.0
. 1
.0
.0
.0
.0
.0
.2
.0
.0
.0
.0
.0
.0
.0
                 -  503 -
-------
          APPENDIX G   TABLE XII
RUN 9 -REGENERATOR BED PARTIBLE DISTRIBUTION
          SIEVE  SIZE IN  MICRONS
SAMPLE
NUMBER
X888B3S&.
DAY- 3200 2800
TIME 2800 1400
Ettr9999SS49*VV»»99SS«S*e««
1400
1180
»«K»SSV9
1180
850
• se *» • a! as *
WT. PERCENT
51645
51647
51649
51633
51607
51621
51637
51652
51658
51665
61672
51677
51684
51684
51694
51697
51709
10.2359
11.0350
11.1200
12.0600
8.0600
9.1200
10.1800
11.1800
11.2359
12.1200
12.1800
12.2359
13.0600
13.1200
14.0600
14.1200
14.2359
• 2
• 1
• 2
• 2
• 2
• 2
.2
• 1
.1
.2
• 1
.0
.2
.2
.2
.1
.2
10*8
1 1.2
11.2
12.0
9.5
9.8
11.0
10.2
1 1 .6
12.1
10.5
9.4
13.2
10.1
9.6
9.3
I 1.7
14.3
14.8
14.2
15.4
12.1
13*1
14.1
13.6
14.8
14.9
14.3
14.0
16.9
13.9
14.8
13.8
15.9
30.0
30.9
30.9
31.7
28*3
29.0
29.8
30*2
31.3
31 .9
30.9
29.2
33*3
30*8
31 *4
32. 1
33»1
850
600
333338

29.4
29.5
29.9
28*6
28.8
29.5
29.7
31.1
29.4
28*6
29.9
29.2
27.2
30.7
29.9
31.4
28*6
600 250
250 1 50

15. 1
13.5
13.7
12.2
20.9
18.2
15.1
14.7
12.7
12.3
14.2
18.0
9. 1
14.3
14.0
13.3
10.5

.2
.0
.1
.0
.2
.2
.1
. 1
.0
.0
.1
.2
.1
.1
.2
.1
.0
150
100

.0
.0
.0
.0
.0
.0
.0
• 0
.0
.0
.0
• 0
.0
.0
.0
.0
.0
100

.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
. 1
                 - 504  -
-------
APPENDIX  G.   TABLE XII
RUN 9  -  Regenerator Bed Particle Distribution
SIEVE  SIZE IN  MICRONS
                                          150
                                          100
SAMPLE DAY- 3200 2800 1400 1180 850 600 250
NUMBER TIME 2800 1400 1180 850 600 250 150
=======r===================2z=*==sz=========================
WT. PERCENT
51717
51724
51730
51733
51740
51747
51748
51832
51840
51842
51849
51853
51859
51864
51869
51877
51881
51886
15.0700
15*1200
16. 1500
16.2359
17. 1800
17. 1245
17. 1545
17.2359
18.0600
18* 1200
18*1800
18.2359
19.0600
19.1200
19. 1800
19.2359
20*0600
20. 1800
.2
.1
.1
.2
.1
.0
.1
.1
. 1
. 1
. 1
.1
.1
.1
.1
. 1
.2
.3
8.5
9.3
6.5
7.8
7.2
8.5
8.3
7.5
5.1
4.6
6.6
5.7
5.3
5.1
4.8
3.3
4.2
5.3
13.0
13*8
12.6
12.8
12.3
13.6
12*1
12.4
10.1
9.7
12.4
10.8
10.7
10.2
9.7
7.6
8.6
10.6
30*6
31.8
26*3
32.9
33.0
33.1
33.4
32.8
31.6
30*8
34.4
31.5
31 .6
30.5
29.3
25.9
27.7
30. 1
32.0
30.9
38.3
33.5
34.4
32.9
34. 1
34.4
37.9
39.0
35.4
37.0
37. 1
37.2
37.2
37.9
37.2
35.4
15.4
13.9
16. 1
12.7
12.9
11.7
11.9
12.7
15.0
15.6
11*1
14.7
1 5.3
16.8
18.2
24.7
21.7
18.2
.2
.2
.2
.
*
.
.
.
.2
*
.
.
.0
• 1
f c
• ^
. 2
.V
                                            .0
                                            .0
                                            .0
                                            .0
                                            .0
                                            >0
                                            • 0
                                            .0
                                            >0
                                            .0
                                            .0
                                            >0
                                            .0
                                            .0
                                            .0
                                            .0
                                            .0
                                            .0
100
   .0
   .0
   .0
   .0
   • 0
   .0
   >0
   .0
   .0
   .0
   .0
   .0
   .0
   .0
   > 1
   .0
   .0
   .0
       -  505 -
-------
Appendix G.   Table XII
Run 9 - Regenerator Beri Particle Distribution
SIEVE SIZE I
SAMPLE
NUMBER

51888
51895
51899
51094
51907
51910
51913
51921
51925
51928
51935
51935
51946
51952
51959
51963
51971
52003
52005
DAY- 3200 2800 1400
TIME 2800 1400 1180

20. 1800
22. 1800
23.0015
23.0600
23* 1200
23.1800
23.2359
24.0600
24.0900
24. 1200
24.1800
24.2359
25.0600
26.0001
26.0600
27.0600
27. 1200
27.1830
27.2359

.4
.2
.2
• 3
• 1
.2
• 1
.2
• 2
• 2
• 3
.2
. 1
.2
• 1
3*0
• 2
• 1
.2
N MICRONS
1180
850
850
600
600 250
250 1 50
150
100
100
WT. PERCENT
6.0
7.2
5.4
8.2
7.5
5.8
5.0
7.5
6.9
7.5
7.8
7.8
7.1
8.2
6. 1
15.2
7.6
7.6
6.9
10.6
11 *6
10.4
13.0
12.6
10.8
9.9
13.3
13.4
13.0
13*2
13.6
12.7
14.3
12.8
18*2
12.3
12.6
11 .8
30.5
31.5
31.5
33.9
32.1
32.6
32.5
33.3
32.5
32.8
32.2
32.3
31 .7
34.2
34.9
33-3
30.7
30.9
30.1
34.8
33.3
35.7
32.9
33.4
36.5
37.4
33.0
33.2
33. 1
32.2
32.5
32.7
31 .5
34.2
21.2
31 .5
31.9
32.5
17.5
15.9
16.6
1 1.8
14.3
14. 1
15.0
12.7
13.7
13.3
14.2
13.4
15.6
11.6
1 1.8
9.1
17.3
16.6
17.9
.2
• 3
.2
.0
.0
.1
.1
.1
.2
.2
• 1
.2
. 1
. .0
.0
.0
.4
. 1
.6
• 0
.0
• 0
.0
.0
.0
.0
.0
.0
00
.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
. 1
           - 506  -
-------
APPENDIX  G.   TABLE XII
RUN 9 - REGENERATOR BED PARTICLE DISTRIBUTION

SIEVE SIZE  IN MICRONS
SAMPLE
NUMBER
DAY- 3200 2800
TIME 2800 1400
3CSaES55S:s = .zs== = sss
52012
52022
52028
52032
52036
52040
52047
52052
52057
52061
52069
28*0600
28.1845
30*0600
30.1200
30. 1800
30.2359
31.0600
31.1200
31*1800
31.2359
32.0600
s s m x *n s .
.2
.2
.2
2*0
• 1
• 1
*1
• 1
• 1
• 5
.6
1400 1180
1180 850
850
600
600
250
250
150
150
100
100
WT. PERCENT
6.7
6.8
5.7
12.2
3.4
4*4
4.6
3.7
4.2
7.6
6.4
11*1
11.4
9.9
12*2
6.6
8*6
8.9
7*1
8*4
12*1
9*8
29.0
29.4
27.6
26.5
23.2
25.2
26*1
32*8
22*7
6*6
24*5
31*8
31*7
33*3
26.5
35.3
32.7
32.7
26.8
29.3
36.7
29.4
20.0
19.4
22.2
18.4
29.9
28*0
26.3
26*6
30.6
33.9
28*1
1. 1
!• 1
.9
2.0
1*3
.9
1.3
2*2
3.5
2.4
1.1
.0
.0
• 1
• 0
.3
.0
. r
• 4
.8
.0
.0
. 1
.0
.0
.0
.0
.0
.0
.2
.3
.2
.2
        - 507 -
-------
           APPENDIX G   TABLE XIII
RUN 9 - Elutriator Coarse Particle Distribution

           SIEVE SIZE IN MICRONS
SAMPLE
NUMBER
=========
DAY-
TIME
SXBSSS = =
3200
2800
======
2800
1400
======
1400
1180
=======
1180
850
========
850
600
= ===5
600
250
:======
250
150
======
150
100
=====-
100


WT« PERCENT.
51555
51558
51556
51566
51572
51578
51582
51587
51593
51596
51600
51608
51616
61605
51612
51619
51622
51625
51629
2.1800
4.0630
5.0001
5.0600
5.1400
5.2359
6.0600
6.1200
7.0600
7.1200
7.1800
8.0600
8.1800
8.0001
8.1200
8.2200
9. 1200
9.1800
10.0615
.0
.0
.1
.0
• 1
.2
• 2
.1
• 0
.0
• 1
• 0
• 1
• 2
.0
.1
.2
• 1
• 1
.2
.9
1.7
1.7
2.1
3.8
4.0
4.3
2.6
1.7
3.4
3.3
6.5
6.1
5.2
5.2
6.6
5.9
5.9
• 3
1.8
3*0
2.8
3*4
5.4
5.7
5.6
4.0
3.2
5.2
5.7
8.9
7.5
7.6
7.8
8.9
8*0
8.7
• 8
5.0
7.8
7.0
9.6
14.2
14.5
14*3
9.6
8*2
13.1
16*4
22.4
21.0
19.8
20.6
20.7
19.3
21.6
1.4
7.6
11 .7
10.3
15.8
20.0
19.6
19.0
12.6
11.8
17.1
24.3
27.9
27.1
26.6
26.7
24.6
24.0
29.1
20.5
42.3
48.0
42.0
49.9
47.4
44.0
38.7
36.3
40.4
36*6
38.1
29.4
35.8
33.9
30.2
29.3
29.2
31.5
37.3
30.6
20.1
27.4
15.4
7.9
10. 1
13. 1
22.3
24.2
15.9
7.2
3*0
i.7
4.6
5.5
6.3
7.4
2.9
9.1
4.3
2.1
2.2
1.3
.6
• 8
1.5
5.4
5.0
3.7
1.8
• 8
. 1
1. 1
1.9
1.6
2.3
.2
30.5
7.5
5.6
6. 5
2.3
.5
1.0
3.3
7.3
5.6
5.0
3.0
.9
.3
1.2
1.9
1.8
3.7
• 2
                   - 508 -
-------
           APPENDIX G   TABLE XIII

RUN 9 - Elutriator Coarse Particle Distribution
          SIEVE SIZE  IN MICRONS
: = = = *mr = :i3J:xzasax = aBaaxaaa»a«a
 3200  2800   1400    1180    850
 2800  1400   1180     850    600
:=================asz»ssa==xs»E!
                                         ===========-
600
250
250
150
150
100
                                       :sscsaz = = = == = = = = = z-
                                                           100
WT. PERCENT
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
51
635
638
643
650
653
660
661
666
678
685
688
695
699
710
718
734
741
829
833
10.1200
10.1800
10.2359
11.1 200
11.1800
11.2359
12.0600
12.1200
1 5.8
7.2
5.0
5.7
5.6
5*6
6.1
4.7
12.2359 .2 6.3
13*0600
1 5.3
13.1200 .0 3*6
14.0600 .2 5*7
14.1200
14.2359
1 6*6
1 5*0
15.0700 .0 4*3
16*2359 .3 3.1
17.0800 .2 5.3
17.1700 .2 4.3
17.2359 .0 2.7
8*5
10.1
7.8
8.8
8.5
8.9
9.4
7.7
9.3
8.5
6*8
8.2
9.8
8*3
7.6
6.7
9.2
7.3
5.3
21*
24.
29.
22.
22.
24.
24.
21.
22.
23*
21*
20*
27.
23*
21.
24.
26.
22*
17.
9
3
2
2
7
2
3
6
8
0
3
1
3
0
6
1
1
0
3
28.9
29.3
28.9
30*4
30.6
32.0
29.3
31.2
28.7
30.9
33.0
24.2
31.6
31*1
30*6
36.0
33.5
32.4
25.4
30.4
25.0
25.0
27.9
27.1
27.0
27.7
29.8
26.9
27.5
30.4
31.6
22.7
26.9
29.4
24*6
21.2
26.4
25.9
3.6
2.9
3.2
3.3
4.2
1.8
2.4
3«5
4.8
3.8
3.1
9.9
1.7
3.7
4.5
1.9
2.2
2.6
7.3
• 3
.4
.5
.7
.8
• 1
• 4
.8
• 8
.5
1.3
.0
.2
1*1
1.0
1*2
.7
1 • 1
4.2
.5
.6
• 3
.9
.4
• 2
.3
.6
.2
.3
.5
.0
. 1
.7
1.0
2.2
1.7
3.7
1 1.8
                     - 509  -
-------
           APPENDIX G   TABLE XIII
RUN 9 - Elutriator Coarse Particle Distribution
           SIEVE SIZE  IN MICRONS
•BBBSSSS
SAMPLE
NUMBER
DAY- 3200 2800
TIME 2800 1400
1400
1180
• S 8SSZ
1 180
850
850
600
600
P50
250
150
I S —
150
100
100
WT. PERCENT
51838
51843
51850
51855
51861
51865
51870
51874
51895
51897
51901
51908
5191 1
51914
51922
51926
51930
51937
51940
51947
51953
51960
51964
51970
52001
52007
52013
52014
52025
52029
52033
52037
52042
52049
52053
52058
52063
52070
18*0600
18* 1200
18*1800
18*2359
19*0600
19.1200
19.1800
19*2359
22. 1800
23*0015
23.0600
23*1200
23.1800
23.2359
24.0600
24.0900
24.1200
24.1800
24.2359
25*0600
26*0001
26*0600
27.0600
27.1230
27.1830
27.2359
28*0600
28.1230
28. 1845
30.0600
30* 1200
30*1800
30*2359
31 .0600
31 • 1200
31 • 1800
31 .2359
32.0600
•
•
.
.
.
.
.0
.0
.1
.2
.2
.1
.1
.3
.2
• 1
.1
.1
.1
.2
.1
.2
•
•
.0
*
.
*
• 0
• 0
.0
• 0
• 0
• 0
• 0
.0
.0
• 0
4.6
2.3
3.0
1*8
2.6
• 8
1.1
1.5
2.2
4.2
5.0
4.7
4.1
5.2
4.0
3.9
3.3
4*4
4.3
4.1
3.3
2.4
1.6
2.2
1.7
1.7
1 .8
2.4
2.4
.2
.2
.1
.0
.0
.1
• 2
.1
.2
5.8
5.7
6.3
4.8
5.7
1.8
2.5
3.8
4.2
7.0
8*8
8*6
7.3
8.9
7.3
7.6
6.8
3.0
7.9
7.8
6.6
4.9
3*0
4.4
3.4
3.5
3>6
4*4
4.4
.4
«4
.1
.2
.2
.2
.5
• 3
.4
18*2
20*5
20*4
18*4
20.8
6.4
8.9
14*4
13.5
20.7
26.9
25.6
21.7
23.0
18.9
21*4
20.0
22.3
21.6
21.5
18.7
15. 2
9.3
13.5
11.1
10.8
11.4
13.9
13.2
1.5
1 .6
.4
• 3
• 5
• 6
1.9
.7
1.5
26*6
34.7
29.3
32.3
33«2
10*6
14*9
15*3
18.8
27.6
34*0
31.9
27.6
25*6
22*0
26.1
26*3
27.6
27.3
27.5
25.1
22*6
14.2
20.0
16.7
16.3
17.4
19.1
18.2
3.0
2.8
.7
1.0
.7
1.0
4.0
1 .9
3*2
31*4
30.5
22.5
32.5
30.0
24.2
30.2
48.2
27.7
28.7
23-8
22.9
24.8
20*4
21*4
24.7
26.2
25. 1
28*3
29.0
35.7
32.7
38.0
34.2
28.9
24.6
33. 1
25.7
24*6
17.4
16.5
19.9
20.1
14.2
12.8
31.8
16.4
19.0
5.5
3.2
5.3
4.8
3.5
27.1
27.8
10.4
15.0
6.5
1.2
3.7
4.7
5.2
10.0
7.6
9.5
6.2
6*6
6*6
5*2
1 1 *6
26.9
7.7
10*3
12.3
21*1
7*4
9.4
25.0
40.7
38.4
12. 1
23.7
30.3
27.2
26.5
33*8
2.3
1.1
3.6
1.2
1. 1
9.3
8.6
1.9
5.8
1.7
. 1
1.2
2.5
4.7
5.9
3.4
4*6
2.4
2.0
1.7
2.2
5.6
5.6
3.7
4.5
5.3
5.4
3.5
4* 1
10.5
7.7
5-5
7.6
7.5
11.6
10*8
13.0
16.0
5.5
1.9
9.4
4. 1
3.2
19.7
6.2
4*4
12.6
3.4
. 1
1.2
7.3
6.6
10.4
5.2
3.2
4.0
1*9
1*5
3*2
4*9
1 *3
14.2
23.4
25.5
6* 1
23*6
23*7
42*0
30* 1
34*8
58.6
53.3
43*5
23*5
41*2
25*9
                    - SLOT
-------
                           APPENDIX G   TABLE XIV
                    RUN 9 - Stone Peed Particle Distribution

                           SIEVE  SIZE IN MICRONS
SAMPLE     DAY-   3200   2800    1400    1180    850   600    250   150    100
NUMBER     TIME   2800   1400    1180     850    600   250    150   100

                                 WT. PERCENT.
51237
51237
51675
51715
52055
.0000
7.1200
12.1200
14.2359
31*1200
• 3
.2
• 4
.8
• 3
1*1
8.0
19.2
23.2
12.8
7.2
6.7
15.5
17.4
1 1 .6
15.8
13.9
32.5
47.5
26. 1
18. 1
16*4
18.1
9.5
18.4
36.8
35.1
10.7
1.3
20.3
14.0
14. 5
2.2
.2
6.8
3.9
2.5
.5
.0
1.7
2.7
2.8
.9
.2
1.9
                                  - 511  -
-------
                        APPENDIX  G       TABLE  XV
          TRACE ELEMENT  ANALYSIS   BY NEUTRON ACTIVATION - RUN 9

(a)  Fuel  Oil
Isotope
*A.
115
Cd (115 In)
60
Co
51
Cr
203
Hg
99 (99
Mo Tc)
56
Mn
65
Ni
122
Sb
124
Sb
75
Se
127m
Te
Photon Energy
(keV)
560
337
1173; 1332
320
279
141
847; 1811
367; H15; 1^82
564; 693
603; 723
136;265;280
361
Half- Life

26.3 Hrs
55.2 hrs
5.24 yrs
27.8 days
46.9 days
66.7 hrs
2.58 hrs
2.56 hrs
2.75 days
60.9 days
121 days
105 days
Content
(ppm)
/-
7 + 1.4
0.2+.04
1.4+.14
*
< 10
0.9± -18
< 5
< 1
< 1
*
< l
Limit.
(ppm)
10-100
0.1
0.01
0.3
*
•* 10
0.5
*x> 5
'V* 1
*V>1
#
•wl
                                   - 512  -
-------
                              APPENDIX  G.    TABLE XV
              TRACE ELEMENT ANALYSIS  BY NEUTRON ACTIVATION       RUN  9

(b)  Fresh Limestone.
Half-Life          Content
                    (ppm)

26.3 Hrs            /-

55-2 Hrs           29+ 6

5.25 yrs           0.3+.01

27.8 days          2 + .2

46.9 days            *

66.7 hrs             0

2.58 hrs           22+1

2.56 hrs           <50

2.75 days          
-------
                         APPENDIX   G.        TABLE XVI
              Spark-Source Mass Spectrometric Analysis
       Run  9.
OIL  Sample
ELEMENT

Lithium
Beryllium
Boron
Fluorine
Sodium
Magnesium
Aluminium
Silicon
Phosphorus
Sulphur
Chlorine
Potassium
Calcium
Scandium
Titanium
Vanadium
Chromium
Manganese
Iron
Cobalt
Nickel
Copper
Zinc
Gallium
Germanium
Arsenic
Selenium
Bromi ne
Rubidium
Strontium
Yttrium
Zirconium
Niobium
Molybdenum
Ruthenium
Rhodium
Palladium
PROBABLE   RANGE
Less than
Less than
Less than
0.001 PPM
2 PPM
1 PPM
1 PPM
1 PPM
0.5 PPM
6 PPM
0.06 PPM
0.3 PPM
2 PPM
Less than
0.1 PPM
100 PPM
0.02 PPM
0.06 PPM
3 PPM
0.1 PPM
6 PPM
0.1 PPM
0.3 PPM
0.02 PPM
Less than
0.3 PPM
Less than
Less than
Less than
Less than
0003 PPM
Less than
less than
0.1 PPM
Less than
Less than
Less than
0.06 PPM 1
0.01 PPM 1
0.001 PPM
0.01 PPM
20 PPM
10 PPM
10 PPM
10 PPM
3 PFM
60 PPM
0.6 PPM
3 PPM
20 PFM
0.02 PPM 1
1 PPM
1000 PPM
0.3 PFM
0.6 PPM
30 PPM
1 PPM
60 PPM
1 PPM
3 PPM
0.2 PFM
0.2 PPM 1
3 PPM
0.06 PFM 1
0.002 PPM 1
0.03 PPM 1
0.2 PPM 1
0.003 PPM
0.02 PPM 1
0.001 PPM
1 PPM
0.002 PPM 1
0.03 PPM i
0.002 PPM 1
                                   - 514 -
-------
                            APPENDIX  G..   TABLE  XVI

          SPARK SOURCE MASS SPECTROMETRIC  ANALYSIS
         RUN
Oil  Sample  (contd)

                 Element
                 Cadmium
                 Indium
                 Tin
                 Antimony
                 Tellurium
                 Iodine
                 Barium
                 Lanthanum
                 Cerium
                 Praseodymium
                 Neodymium
                 Terbium
                 Dy sprosium
                 Hafnium
                 Tantalum
                 Tungsten
                 Gold
                 Lead
Probable Range

Less than
Less than
0.2 PPM
0.01 PPM
Less than
Less than
0.06 PPM
.0002 PPM
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
0.002 PPM
  0.3 PPM
0.06   PPM
0.03   PPM
 2 PPM
0.1 PPM
0.006  PPM
0.001  PPM
0.6 PPM
0.002  PPM
0.006
0.001
0.002
0.002
 0.01
0.003
 0.02
0.003
 0.02
  3
PPM 1
PPM
PPM 1
PPM 1
PPM
PPM
PPM
PPM
PPM
PPM
                 Internal  standard  -    Silver
                 Assumed concentration * 0.2973E-02#
                 Dilution  factor       « 1.0000

                 1= Interference by complex ions   suspected or known

                 All elements  from at.  No.  3 - 92 (with  exception  of C.N. & 0)
                 looked for; cone. in  PPM and % WT/WT

                 Unquoted  elements were below the detection limit  (.Ol-.l PPM)
                                  - 515 -
-------
                             APPENDIX  G.     TABLE  XVI

          SPARK SOURCE  MASS SPECTROMETRIC  ANALYSIS      -     RUN  9


Fresh BCR 1339 Limestone (con*)


                 Element                         Probable   Range

                 Silver                          Less  than         0.6     PPM  1
                 Cadmium                         Less  than         0.3     PPM  1
                 Indium                          Less  than           6     PPM  1
                 Tin                             Less  than           1     PPM  1
                 Antimony                        Less  than         0.3     PPM  1
                 Tellurium                       Less  than         0.8     PPM  1
                 Iodine                          1 PPM               10     PPM
                 Caesium                         Less  than         0.06    PPM  1
                 Barium                          30  PPM             300     PPM
                 Lanthanum                       0.3 PPM             3     PPM
                 Cerium                          Less  than           3     PPM  1
                 Praseodymium                    Less  than         0.3     PPM  1
                 Neodymium                       Less  than           2     PPM  1
                 Samarium                        Less  than           1     PPM  1
                 Europium                        Less  than           1     PPM  1
                 Gadolinium                      Less  than           1     PPM  1
                 Terbium                         Less  than         0.2     PPM  1
                 Dysprosium                      Less  than           2     PPM  1
                 Tantalum                        Less  than           2     PPM  1
                 Gold                            Less  than         0.6     PPM  1
                 Lead                            Less  than           3     PPM  1
                 Thorium                         Less  than         0.6     PPM  1
                 Uranium                         Less  than         0.6     PPM  1
                 Internal standard  calcium
                 Assumed concentration =  0.7147E 02  %
                 Dilution factor       =  1.0000
                 I = Interference by complex ions  suspected or known -
                All elements from at. No.  3  - 92 (with exception of C,N  &  0)  looked
                for  -   Cone,  in PPM and % WT/V/T.

                Unquoted elements were below the detection limited (.Ol-.l  PPM)
                                   -  516  -
-------
                           APPENDIX G     TABLE  XVI
      Spark-Source Mass Spectrometi^c Analysis  -   Run
Fresh BCR 1359 Limestone:

                    Element

              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphorus
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Ruthenium
              Rhodium
              Palladium
Probable Range
Less than
Less than
Less than
10 PPM -
0.2$
200 PPM
600 PPM
1 PPM
Less than
10 PPM
100 PPM
Less than
0.6 PPM -
0.06 PPM
Less than
6 PPM
200 PPM
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
100 PPM
Less than
Less than
Less than
Less than
Less than
Less than
Less than
2
6
2
100
2$
2500
6000
10
20
100
1000
0.3
6
0.6
20
60
2000
20
6
2
30
0.6
i
6
3
0.3
2
1000
2
2
0.3
2
1
0.1
1
PPM 1
PPM 1
PPM 1
PPM

PPM
PPM
PPM
PPM 1
PPM
PPM
PPM 1
PPM
PPM
PPM 1
PPM
PFHM
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
                                   - 517  -
-------
                            APPENDIX G         TABLE XVI

         Spark- Source Mass Spectrometric Analysis  -   Run

Gaslfier Bed (Sampled 13.0000)
              Element

              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphorus•
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Palladium
Probable   Range
Less than
Less than
0.2 PPM
30 PPM
Q.2%
Q.2%
0.2%
3 PPM
O.lg
3 PPM
10 PPM
Less than
2 PPM
600 PPM
0.6 PPM
6 PPM
200 PPM
2 PPM
60 PPM
0.2 PPM
Less than
1 PPM
Less than
Less than
Less than
Less than
Less than
100 PPM
Less than
Less than
Less than
Less than
Less than
10
20
2
300
2 %
2 %
2 %
30
1 %
30
100
0.1
20
6000
6
60
2000
20
600
2
20
10
1
6
3
0.2
0.2
1000
1
6
0.3
20
1
PPM 1
PPM 1
PPM
PPM



PPM

PPM
PPM
PPM 1
PPM
PPM
PPM
PW
PPM
PPM
PPM
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
                                   -  518  -
-------
                            APPENDIX  G     TABLE  XVI
      Spark-Source Mass Spectrometric Analysis  -  Run  9

Gasifier  Bed (Sampled 13.0000) Contd.


              Element                         Probable  Range

              Silver                          Less than         0.2    PPM 1
              Indium                          Less than           1    PPM 1
              Tin                             Less than           1    PPM 1
              Antimony                        Less than         0.3    PPM 1
              Tellurium                       Less than           3    PPM 1
              Caesium                         Less than        0.06    PPM 1
              Barium                          100  PPM        1000     PPM
              Lathanum                        0.3  PPM            3    PPM
              Cerium                          Less than           3    PPM 1
              Praseodymium                    Less than         0.3    PPM 1
              Neodymium                       Less than           6    PPM 1
              Samarium                        Less than           1    PPM 1
              Europium                        Less than         0.3    PFM 1
              Gadolinium                      Less than           3    PPM 1
              Terbium                         Less than         0.2    PPM 1
              Dysprosium                      Less than           1    PFM 1
              Holmlum                         Less than         0.2    PPM 1
              Erbium                          Less than         0.6    PPM 1
              Ytterbium                       Less than         0.6    PPM 1
              Tantalum                        Less than         0.6    PPM 1
              Gold                            Less than         0,2    PFM 1
              Thorium                         Less than         0.2    PPM 1
              Uranium                         Less than         0.2    PPM 1
              Internal standard       Calcium
              Assumed concentration   *   0.6790E
              Dilution factor         =   1.0000
              1= Interference by complex ions  suspected or known.
              All elements from AT. No. 3-92 (with exception of  C,N & 0)
              looked for -   Cone   in PPM and % WT/WT  -    Unquoted elements  were
              below the detection  limit (.Ol-.l PPM)
                                  -  519  -
-------
                         APPENDIX G      TABLE  XVI
Spark - Source Mass Spectrometric Analysis    -   Run  9

Boiler Cyclone fines (Sampled 13.0000)
              Element

              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphorus
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Ruthenium
              Rhodium
              Palladium
Probable   Range.
Less than
Less than
6 PPM
100 PPM
600 PPM
600 PPM
0.2$
10 PPM
0.3 %
300 PPM
600 PPM
Less than
6 PPM
6 PPM
20 PPM
600 PPM
60 PPM
600 PPM
10 PPM
less than
Less than
Less than
6 PPM
Less than
Less than
Less than
100 PPM
Less than
Less than
Less than
20 PPM
Less than
Less than
Less than
2
0.6
60
1000
6000
6000
2 %
100
3
3000
6000
1
60
60
200
6000
600
6000
100
300
30
3
60
10
3
6
1000
2
6
1
200
0.3
10
1
PPM 1
PPM 1
PPM
PPM
PPM
PPM

PPM
%
PPM
PPM
PPM 1
PPM
PPM
PPM
PPM
PPM
PPM
PPM
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM _
PPM 1
PPM 1
PPM 1
                                   -  520 -
-------
                            APPENDIX  G      TABLE  XVI


Spark-Source Mass Spectrometric Analysis   -  Run 9


Boiler Cyclone fines (Sampled 13.0000) contd.


              Element                         Probable  Range.

              Silver                          Less than         2   PPM 1
              Cadmium                         Less than       0.3   PPM 1
              Indium                          10 PPM          100   PPM
              Tin                             Less than        30   PPM 1
              Antimony                        1 PPM            Iffl   PPM
              Tellurium                       Less than         1   PPM 1
              Iodine                          Less than         3   PPM 1
              Caesium                         Less than       0.6   PPM 1
              Barium                          30 PFM          300   PPM
              Lanthanum                       0.3 PPM.           3   PPM
              Cerium                          Less than         3   PPM 1
              Praseodymium                    Less than       0.3   PPM 1
              Neodymium                       Less than         2   PPM 1
              Samarium                        Less than         1   PPM 1
              Europium                        Less than       0.3   PPM I
              Gadolinium                      Less than         3   PPM 1
              Terbium                         Less than       0.2   PPM I
              Dysprosium                      Less than         2   PFM 1
              Holmium                         Less than       0.2   PPM 1
              Erbium                          Less than      0.6   PFM 1
              Ytterbium                       Less than      0.6   PPM I
              Tantalum                        Less than         6   PPM 1
              Tungsten                        Less than      0.6   PPM 1
              Rhenium                         Less than      0.3   PPM 1
              Gold                            Less than      0.6   PPM 1
              Lead                            60 PPM         600   PPM
              Thorium                         Less than       Q<*6   PPM 1
              Uranium                         Less than       0.6   PPM 1


              Internal standand   calcium
              Assumed concentration «  0.6790E  02$
              Dilution factor        *  1.0000

              1=  Interference by  complex ions   suspected or known 1
              All elements  from AT.  No. 3 - 92 (with exception of C;N&  0) looked  for
              cone In PFM and % WT/Vt

              Unquoted elements were below the detection limit (.Ol-.l  PFM)

                                  - 521  -
-------
                             APPENDIX G     TABLE   XVI
Spark-Source Mass Spectrometric  Analysis   -   Run  9


Regenerator  Cyclone fines (Sampled 13.0000)
              Element

              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphorus
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Ruthenium
              Rhodium
              Palladium
Probable   Range
Less than
Less than
0.3 PPM
30 PPM
0.2 %
600 PPM
300 PPM
6 PPM
0.3#
30 PPM
60 PPM
less than
1 PPM
0.10
3 PPM
30 PPM
300 PPM
10 PPM
300 PPM
6 PPM
Less than
Less than
Less than
20 PPM
Less than
Less than
Less thatn
200 PPM
Less than
Less than
Less than
3 PPM
Less than
Less than
Less than
2 PPM 1
0.3 PPM 1
3 PPM 1
300 PPM 1
2 %
6000 PPM
3000 PPM
60 PPM
3 %
300 PPM
600 PPM
1 PPM 1
10 PPM
1 %
30 PPM
300 PPM
3000 PPM
100 PPM
3000 PPM
60 PPM
100 PPM 1
20 PPM 1
2 PFM 1
200 PPM
2 PPM 1
3 PFM 1
6 PPM 1
2000 PPM
2 PPM 1
2 PPM 1
0.2 PPM 1
30 PPM
0.6 PPM 1
0.6 PPM 1
1 PPM 1
                                    -  522  -
-------
                            Appendix   G     TABLE XVI
   Spark-Source Mass Spectrometrlc  Analysis   -   Run 9

Regenerator Cyclone fines (Sampled 13.0000)  Contd.


              Element                         Probable	Range

              Silver                          Less than         0.3    PIM 1
              Cadmium                         Less than         0.3    PPM 1
              Indium                          2 PPM             25     PPM
              Tin                             Less than         10     PPM 1
              Antimony                        Less than          2     PPM 1
              Tellurium                       Less than          1     PPM 1
              Iodine                          Less than         1      PPM 1
              Caesium                         Less than        0.6     PPM 1
              Barium                          100 PPM         1000     PPM
              Lanthanum                       0.3  PPM          3      PPM
              Cerium                          Less than         3      PPM 1
              Praseodymium                    L ess than        1      PPM 1
              Neodymlum                       Less than         1      PPM 1
              Samarium                        Less than         2      PPM 1
              Europium                        Less than       0.2      PPM 1
              Gadolinium                      Less than         2      PFM 1
              Terbium                         Less than       0.3      PPM 1
              Dysprosium                      Less than         2      PPM 1
              Holmium                         Less than       0.1      PFM 1
              Tantalum                        Less than         3      PPM 1
              Rhenium                         Less than       0.2      PPM 1
              Lead                            30 PPM          300      PFM
              Thorium                         Less than       0.2      PPM 1
              Uranium                         Less than       0.6      PPM 1
              Internal standard   calcium
              Assumed concentration » 0.6790E 02^*
              Dilution Factor       « 1.0000

              1= Interference by complex ions  suspected or known
              all  elements from AT. NO. 3-92 (with exception of C,N & 0) looked for
              Cone, in PPM and % WT/VT

              Unquoted elements were below the detection limit (.Ol-.l PFM)
                                   - 523  -
-------
                          APPENDIX G       TABLE  XVI
Spark- Source Mass Spectrometric Analysis   - Run  9


Elutriator Coarse  (Sampled 13.0000)
              Element

              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphorus
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Ruthenium
              Rhodium
              Palladium
Probable  Range
Less than
Less than
0. 3 PPM
60 PPM
0.2%
300 PPM
0.1 %
6 PPM
0.6 %
30 PPM
20 PPM
Less than
1 PPM
0.2 %
Less than
3 PPM
300 PPM
3 PPM
100 PPM
0.6 PPM
Less than
Less than
Less than
1 PPM
Less than
Less than
Less than
D.2 PPM
Less than
Less than
Less than
Less than
Less than
Less than
Less than
2 PPM 1
1 PfM 1
3 PPM
600 PPM
2 %
3000 PPM
1 %
60 PPM
6 %
300 PPM
200 PPM
0.3 PPM i
10 PPM
2 %
10 PPM 1
30 PPM
3000 PPM
30 PPM
1000 PPM
6 PPM
30 PPM 1
20 PPM 1
2 PPM 1
10 PPM \
2 PPM 1
0.3 PPM 1
0.3 PPM 1
2 PFM
2 PPM 1
2 PPM 1
0.2 PPM 1
10 PPM 1
0.2 PPM 1
0.06 PPM 1
3 PPM 1
                                   - 524 -
-------
                         APPENDIX  G        TABLE   XVI
         Spark-Source Mass Spectroraetric Analysis  -  Run 9.

Elutrlator Coarse (Sampled 13.0000) Contd.


              Element                         Probable  Range

              Silver                          Less than         0.  3   PPM 1
              Cadmium                         Less than         0.  3   PPM 1
              Indium                          Less than            2   PPM 1
              Tin                             Less than            2   PPM 1
              Antimony                        Less than         0.  6   PPM 1
              Tellurium                       Less than            2   PPM 1
              Caesium                         Less than         0.02   PPM 1
              Barium                          20 PPM            200    PPM
              Lanthanum                       0.2 PPM              2   PPM
              Cerium                          Less than            3   PPM 1
              Praseodymium                    Less than           \l   PPM 1
              Neodymium                       Less than            1   PPM 1
              Samarium                        Less than         0.  6   PPM 1
              Europium                        Less than         0.  6   PPM 1
              Gadolinium                      Less than            2   PPM 1
              Terbium                         Less than         0.  3   PPM 1
              Dysprosium                      Less than            2   PPM 1
              Holmlum                         Less than         0.  1   PPM 1
              Erbium                          Less than         0.  3   PPM 1
              Ytterbium                       Less than         0.  3   PPM 1
              Tantalum                        Less than            1   PPM 1
              Tungsten                        Less than         0.  3   PPM 1
              Rhenium                         Less than         0.  2   PPM 1
              Gold                            Less than            1   PPM 1
              Lead                            Less than         0.  6   PPM 1
              Thorium                         Less than         0.  3   PPM 1
              Uranium                         Less than         0.  3   PPM 1


              Internal standard      Calcium
              Assumed concentration  =    0.6080E   02$
              Dilution factor         «    1.0000
              I =  Interference by complex ions  suspected  or hnown   -   All elements
              from AT.  No. 3 - 92 (-with  exception of C,N and 0)   looked  for

              Cone,  in PPM and % WT/V/T

              Unquoted elements were below the detection limit-'  (.Ol-.l PPM)
                                   - 525 -
-------
                        APPENDIX  G.        TABLE XVI
  Spark- Source Mass Spectrometric Analysis       Run   9

Elutriator Fines.(sampled 13.0000)
              Element
Probable   Range
              Beryllium
              Boron
              Fluorine
              Sodium
              Magnesium
              Aluminium
              Silicon
              Phosphoiua
              Sulphur
              Chlorine
              Potassium
              Scandium
              Titanium
              Vanadium
              Chromium
              Manganese
              Iron
              Cobalt
              Nickel
              Copper
              Zinc
              Gallium
              Germanium
              Arsenic
              Selenium
              Bromine
              Rubidium
              Strontium
              Yttrium
              Zirconium
              Niobium
              Molybdenum
              Rothen!urn
              Rhodium
              Palladium
Less than
Less than
0.1 PPM
100 PPM
300 PPM
200 PPM
300 PPM
6 PPM
0.2 %
10 PPM
60 PPM
Less than
1 PPM
0.2$
3 PPM
3 PPM
100 PPM
3 PPM
30 PPM
2 PPM
Less than
2 PPM
Less than
0.3 PPM
Less than
Less than
Less than
60 PPM
Less than
Less than
Less than
1 PPM
Less than
Less than
Less than
2
0.3
l
1000
3000
2000
3000
60
2 %
100
600
0.3
10
2 %
30
30
1000
30
300
20
50
20
2
3
2
0.3
0.3
600
2
2
0.2
10
0.2
0.06
1
PPM 1
PPM 1
PPM
PPM
PPM
PPM
PPM
PPM

PPM
PPM
PPM 1
PPM

PPM
PPM
PPM
PPM
PPM
PPM
PPM 1
PPM
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
                                   - 526 -
-------
                             APPENDIX  G

  SparklSource Mass Spectrometric Analysis
     v

Elu-briiatarr fines (Sampled 13.0000) contd.
    TABLE  XVI
   Run 9
              Element

              Silver
              Cadmium
              Indium
              Tin
              Antimony
              Tellurium
              Iodine
              Caesium
              Barium
              Lanthanum
              Cerium
              Praseodymium
              Neodymium
              Terbium
              Dysprosium
              Hafnium
              Tantalum
              Tungsten
              Rhenium
              Gold
              lead
              Thorium
              Uranium
Probable  Range
Less than
Less than
Less than
0.6 PPM
0.2 PPM
Less than
Less than
Less than
Less than
20 PPM
0.1 PPM
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
Less than
0.2 PPM
Less than
Less than
1
0.3
0.3
6
2
0.6
0.6
0.06
0.06
200
1
1
0.3
1
0.1
" 0.6
0.3
1
0.2
0.1
2
0.1
0.2
PPM 1
PPM 1
PPM 1
PPM
PPM
B0M 1
PPM 1
PPM 1
PPM 1
PPM
PPM
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM 1
PPM
PPM 1
PPM 1
              Internal standard    calcium
              Assumed concentration  *   0.6080E  02$
              Dilution factor        »   1.0000

              I = Interference by complex ions  suspected or known.   -  All elements from
              AT. No. 3 - 92 (with  exception of C,N & 0) looked for  -  Cone,  in PPM and
              % WT/WT  -   Unquoted elements were below the detection limit (.Ol-.l  PPM)
                                       - 527  -
-------
                        CAFB  RUN. 9.
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            DAY, HOUR
                                     10.00

                                     FIG.G
                                                1.00

                                                23.
                         -  528 -
-------
                         CAFB  RUN.9.(contd)
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                       DAY, HOUR
                                          FIG. G-23(cont.)
                       -  529 -
-------
                     CAFB RUN.9.(contd.)
                                          Ill-
22 00 23.00 24.00 25.00 26.00 27.00 28.00 2900 30.00 31.00 32.00
                      DAY, HOUR
                                           FIG.G-23(cont)
                 -  530 -
-------
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-------
                            APPENDIX H





     Programmes  and Methods  of Analys-es of Continuous Run Data
Stepwise Multiple Regression




Limitations of Multiple Regression                              533




Regression Analysis Correlation Matrices for Runs  8 &  9         53"4




Bed Depth and Cyclone Drain Temperature                         535




Bed Depth and Bed Fines                                         535




Bed Velocity and Added Water                                    536




Bed Velocity and Air/Fuel Ratio                                 536




Bed Sulphur and Bed Temperature/Bed Depth                       536




Bed Velocity and Bed Depth                                      536




Correlation Between % SRE and Several Process Variables         53?




Editing of Runs 8 & 9 Data                                      537




Tables H-I to H-III                                             539




Computer Programmes
                                - 532 -
-------
                             APPENDIX H

            METHOD OF ANALYSIS OF CONTINUOUS RUNS 8 AND 9
Stepwise Multiple Regression

      Stepwise multiple regression analysis of the data was carried
out using a standard programme 'Mul-Correlation1 available on the
Honeywell MK III Foreground system.   This programme produces linear
equations of the form:-
      y = bo + b1X1+ bgXg +  —  b^ + e

where y is the dependent variable

      X-,, --- ^ are the independent variables

      bo, --- b  are the regression coefficients to be determined

      e is a random error term which gives the difference between
        the predicted and actual for the dependent variable

      In this stepwise regression routine, the basic premise which
distinguishes it from conventional approaches to multiple regression
is that intermediate partial regression equations are developed to
indicate whether a variable is significant in any early stage of the
regression calculation so that it may be entered into the regression
at that stage.   The final regression equation should, therefore,
only contain significant variables.  The programme allows the user
to specify the level of significance such that the independent
variable is entered or removed from the regression equation during
the analysis.   However, it is possible to override this mechanism
and force a variable into the regression equation despite the fact
that it may not meet the specified significance level criteria.   This
is obviously useful when the variable is known to be significant from
other sources.

Limitations of Multiple Regression

      Although multiple regression analysis, including stepwise, is an
extremely powerful tool, it is subject to certain limitations which
the user should be aware of in order not to be led astray.

      Perhaps the most important point to remember is that it is not
possible to infer cause and effect relationships from regression
                                - 533  -
-------
analysis.   The fact that a dependent variable is highly correlated
with an independent variable in no way suggests that a change in the
independent variable causes a change in the dependent variable.
Although such relationships may exist they cannot be proved.   We can
say that the results do not refute the theory, but neither do they
prove it.

      A second important point is that regression relationships are
empirical equations that apply only to the range of data on which they
are based.   Extrapolation can lead to highly erroneous results.
Since regression equations are based on the experimental data, then
the equation is no more accurate than the data.   If the data is
subject to large experimental error, the regression equation will
predict inaccurately.

      An underlying assumption in regression analysis is that the
independent variables are truly independent, and that there are no
interactions between variables.   In practice great skill in
experimental design is needed to achieve this end, and sometimes in
complex processes, such as this one, it is only possible to a limited
extent.

      A final important point to remember is that regression analysis
assumes linear relationships between the dependent variables and the
independent variable.   In order to deal with variables which are
obviously non-linear, it is necessary to transform the variable into
some algebraic function of itself before carrying out the regression.
A measure of the non-linearity of the variable is the improvement in
the '$ explained1 of the resultant regression equation over the linear
version.

Regression Analysis Correlation Matrices for Runs 8 and 9

      Another feature of the regression programme 'Mul-Correlation' is
the print out of the correlation matrix.   This provides on a one to
one basis the degree of correlation between the dependent variable
and each of the independent variables in turn, and also how each
independent variable correlates with the others.   This is particularly
useful in identifying which of the variables are truly independent.
                                - 534  -
-------
     A negative correlation matrix number indicates  that  during  the  test when
one variable increased in general the other decreased.  A useful
measure of the intercorrelation of the various variables is obtained
by taking the square of tne correlation matrix  number and  multilplying by 100
to give the '$ explained' of one variable by another.  Thus a correlation
matrix number of one or minus one gives '100$ explained', and means that
for the purposes of the test the variables are indistinguishable.  A
value of zero means the variables are truly independent of each other.
A value of 0.5 means 25$ of the variance of one variable is reflected
by the other.

     Table H-I and H-II contain the correlation matrices for the variables
that have been considered in this analysis.  A considerable amount of
useful information is contained in both tables, but it is sufficient
at the moment to indicate a few key points.  The correlation matrix
numbers of the variables with respect to % SEE will be considered
later in more detail, but for the moment let us concentrate on the
dependent variables.  Particularly important in this respect are
variables with a high degree of inter-correlation, and for the
purposes of this analysis we shall define this as having a correlation
matrix number (either positive or negative) greater that or equal to
0.5-  The values falling into this category are highlighted in Tables
H-I and H-II.

Bed Depth and Cyclone Drain Temperature

     The cyclone drain temperature is a measure of the amount of
fines circulating from the bed to the cyclones, and hence it is not
unexpected that the deeper the bed the more fines should circulate.
What is interesting is that this correlation is more pronounced in
Run 8 than in Run 9-  After Run 8 the gasifier was modified to expand
the free board space above the bed, and reduce the possibility of
fines circulation.  The drop in the correlation of these two variables
in Run 9 reflects this design change.

Bed Depth and Bed Fines

     The correlation matrix for Run 9 shows a surprisingly high
correlation between bed fines in the range (600-250p), and bed depth,
whereas in Run 8 the correlation is low.  At the start of Run 9
unsieved limestone was fed to the gasifier to increase the bed depth,
However, after several unsuccessful attempts to increase the bed depth
                                - 535 -
-------
to high levels using unsieved limestone, coarser material was used.
Thus as a direct result of how the experiment was conducted during
Run 9* a fortuitous correlation was established between these two
variables which was not present in Run 8.

Bed Velocity and Added Water

      The correlation between bed velocity and added water is an
important one, and has caused considerable difficulty in the analysis
of the data.   The fuel used in Run 9 was free from water contamination,
and as a consequence the only way water was introduced was via flue gas
recycle.   Unfortunately in the majority of cases, when high bed velocities
were evaluated this was carried out by operating at high flue gas
recycle levels, and hence the correlation was established.   Fortunately
in Run 8, water was also introduced from two other sources, namely
water in the fuel and steam injection, and this has lowered the
correlation between these two variables.   Since water in Run 8 has
been shown to be detrimental to % SRE, it has been assumed that water
and not bed velocity is the detrimental factor in Run 9»

Bed Velocity and Air/Fuel Ratio

      A fair degree of correlation exists between bed velocity and
air/fuel ratio, both in Run 8 and Run 9-   This probably relates to
the fact that to operate lean and at a reasonable bed temperature some
cooling with flue gas recycle was necessary.

Bed Sulphur and Bed Temperature/Bed Depth

      Bed sulphur in Run 8  correlates somewhat with bed temperature
and bed depth.   Fortunately in Run 9 "this correlation does not exist
indicating it may be somewhat fortuitous.

Bed Velocity and Bed Depth

      In Run 8 there was a high negative correlation between bed
velocity and bed depth.   Fortunately this is not reflected in Run 9,
and the correlation appears to be fortuitous.

      The above discussion illustrates some of the problems of
regression analysis, and clearly shows the value of looking at both
runs together.
                                -  536  -
-------
 Correlation Between % SRE and Several Process Variables

       Table H-III compares the correlation matrix number with
 respect to % SRE for Runs 8 and 9-   Several interesting points are
 highlighted in this table:-

       (a)   The best single predictor of % SRE in Run 8 was'added
             water* due to the high levels introduced by water
             contamination of the fuel.   In Run 9> bed depth followed
             closely by cyclone drain temperature was the best single
             predictor.

       (b)   The matrix numbers for air/fuel ratio, Ca/S mole feed ratio
             and bed velocity are comparable in direction and magnitude
             in both runs.

       (c)   Those for bed carbon, bed sulphur and bed temperature
             conflict between the two runs,  whereas bed fines shows no
             correlation with % SRE.

       The importance of looking at the data as a whole is again borne
 out in Table H-III.  For example, analysis of Run 9 in isolation could
 well have resulted in regression equations  incorporating bed sulphur
 as a significant variable,  which detrimentally affected % SRE.    In
 fact there is some supporting evidence from earlier runs on this subject
 However,  the data from 'Run  8 conflicts with this observation (see Figure
       Although on a one to one basis with % SRE,  the data for bed
 temperature is conflicting,  in actual practise when the effect of
 other variables were included in the multiple regression equation this
 variable gave a consistent negative correlation coefficient for both
 runs.   (See Table H-II).

'Editing of Runs 8 and 9 Data

       An important aspect  of the analysis method was to try to use,  as
 far as possible,  all the data generated throughout the runs.    During
 the course of the analysis,  however, it became clear that some editing
 of the data was necessary.   In this respect the graphical displays  of
 residual errors from the regression equations were invaluable.
                                 - 537  -
-------
      In order to improve the accuracy of the data some modification
of the hourly readings recorded in Appendices F & G tables was necessary to
take account of the method of retrieval.   Flue gas SOp levels for
example were recorded continuously throughout the runs and the values
listed in Table 5, Appendices F & G,  refer to the average value for the
previous hour, whereas other process variables, such as bed depth
for example were recorded only at the end of the hourly period.   This
is entirely satisfactory if conditions remain constant throughout the
hourly period, but is less so if the conditions are changed during the
hour whether deliberately or not.   To account for this the mean of the
process readings at the beginning and the end of the hourly period was
taken as the value for that hour.   This was only done with key
variables which might be incorporated in the regression equation, and
the computer programme written to perform this task is listed at the
end of this Appendix.

      During the course of the analysis some of the data was rejected
but not before a satisfactory reason was generated for doing so.
Data was omitted for the following reasons:-

      •     Incomplete data particularly if for one reason or another
            the % sulphur removal efficiency reading was unavailable
            or a key process variable, e.g. bed depth was unrecorded.

      •     Initial first or second hours operation after a shutdown
            particularly after sulphation.     The readings of sulphur
            removal efficiency were generally low compared with the
            predicted value, presumably due to the fact that some
            regeneration of the sulphated lime to produce SC>2 was
            taking place.

      •     Two periods in Run 9 when Aragonite limestone was used
            instead of BCR 1359 resulted in predicted values lower
            than experimentally observed.   It was decided to
            eliminate this data from the initial analysis and treat
            these results separately.
                                -  538  -
-------
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                         TABLE H-JII
COMPARISON OF CORRELATION MATRIX ONUMBERS
WITH RESPECT TO % SRE FOR RUNS 8 AND 9

Variable

Bed depth (cm)
*Added Water (m-yhr)
Run 8
Correlation . Numbers
With % SRE

0.49
-0.87
Cyclone Temperatures (°C) 0.31
Bed Temperature (°C)
Air/Fuel Ratio
Ca/S Mole Ratio
Bed Carbon (wt.#)
Bed Velocity (m/sec)
Bed Sulphur (wt.#)
% Bed Fines (600-250^0
0.13
0.35
0.27
0.16
-0.21
0.38
-o. 003
Run 9
Correlation Numbers
With % SRE

0.61
-0.25
0.56
-0.19
0.34
0.27
-0.16
-0.19
-0.42
-0.01
* square of variable.
                           - 541  -
-------
              COMPUTER PROGRAMMES FOR DATA ANALYSIS
GRAFPLOT

100 DIMENSION  VARC750)
110 INTEGER  MHRS<750>
120 FILENAME FN
130 20 PRINT ," WHICH FILE"U NPUT* FN
140 J=l
150 READTIM,VAR<1)1 150  FORMAT(V>
153 FIRS=100.*AMOD31,32*33
163 32 LOCK=0JGOT031
166 33 LOCK=LOCK-12
16B 31 LOCK=12-LOCK
170 TIM1=24.*A1NT(TIM)+FIRS
175 MHRSC 1> = HBIG=VAR( 1>ISMAL = BIG
180 2 JsJ-M
190 30 READ(FN,150,END*1>  TIM,VAR
196 IF< VAR< J»30,21,21
200 21 TIM=24.*AINTCTIM)+100.*AMOD(TIM*1.)
210 MHRSCJ>=1.5+TIM-TIM1
220 IFCVAR(J»-BIG>4*4,3
230 3 BIG=VAR< J)IGO TO  2
240 4 IF(SMAL-VAR(J»2*2*5
250 5 SMAL = VAR*GO TO  2
260 1 J*J-1
265 K=MHRS-1
270 PRINT»J>"   VALUES IN",K.M   MRS"
280 PRINT,"VARIABLE RANGES FROM ",SMAL*"TO",BIG
290 PRINT,"AT  WHAT VALUES  DO YOU WANT AXIS  MARKINGS -FIRSTASTEP"
300 INPUT* FIRS, STEP
310 PCE=(BIG-SMAL>/110.
320 PRINT,"2"IPRINT  102JPRINT,"     "
                            - 542  -
-------
GRAFPLOT  (Cont'd.)
330 PRINT  101
340 101  FORMAT <1H1 *30X*/»1H )
350 LHTX=0
360   11  IF(FIRS-BIG>7*7*6
380 102  FORMATC1H*>
390 7 LHT = 0.5-KF!RS-SMAL)/PCE
400 LCH=LHT-LHTX
410 10  IF8*8>9
420 9 PRINT  103
430 103  FORMATC2H* )
440 LCH=LCH-UGO TO  10
450 8 PRINT  107
455 107  FORMAT(2H*>
460 LHTX=LHT+U FIRS=FIRS+STEPJGO TO  11
470 6 LINE=UNCOL = 0JPRINT 102
475 LCH=0
480 DO 95 K=1*J
490 15  IF-LINE>12*12*14
500 14 LINE=LINE+ULCH=LCm-llPRINT  1 041 I FCLCH-LOCK ) 1 5* 35* 1 5
510 104  FORMATC1H*»"
                      ")
514 35 PRINT 102JPRINT  1 1 0J NCOL = 0I LCH=LOCK-1 2»1 1 0  FORMATC3H + -
516 GOTO 15
520 12 LHT=0.5«-< VAR(K ) - SMAD/PCE
530 18  IF(LHT-NCOL)13*16,17
540 13 NCOL = NCOL-U PRINT  105JGO TO  18
550 17 NCOL = NCOL+U  PRINT103JGO TO  18
560 105  FORMATC1H**"")
570 16 NCOL=LHT+U PRINT  106
580 106  FORMATC2H*.)
590 95 CONTINUE
600 PRINT  101  * GO  TO 20
610 STOPIEND
                            - 543 -
-------
 DLEDIT

 S0C  F41S P'-^nHA'NE  MODIFIES THE  HOURLY  ^EADIMOS SELECTF.O  F.-?"M
 /VIC  FILES  JM9( 4AI >4 DATA  ^A^JK-RU^ 9 ) * THY09 ( CYCL 1ME  TE ^IPF^AT1 RE S )
 700  OLHEr)F9(3Er) FIMES>'ANJ[)  FILES IM >3EG^ES9
M0 FlLELlSP  " jrir',"^EGRES9"»MTCYC9","r)L8EnF9"
US r-?F.AiK 1 )A
nci 1 P'^  ^EAO( 1 >F.MD=1000>A
              =I \JTC A( 1 ) )
111  TMA =1 MT< 100. *( A< 1 )-TIM )•»•?). «0 I)
     JI -1 = 2
    IF( J) ?
190 190 IF(( JI ^1 - JIM) .F.Q.-1 )RO TO  240
-M0 200 <^ = 0. ; Y^=0. 5 2^ = 0. ;QB = 0. s f^B = 0.
                                   (26) +C
                    2> 5 AF'^ = A( 31 > + (QR/2> J
    S= )A*C 100. -AC 1A) )
                          10) ) )
                                   ^EDD»BEOV/»^FnTj AF-^,C(2)»0( ?)»H?0> AC
^12 212 Fl^^ATCH » F^ . 4, F4 . 1 * Fft. 2* F6 .0* F^ .2» F6 . O* F^ . 1 , Fft . 0* IF A . 1 )
220  J = MJM1 = JI>1J ;RA=A(10);TA=A(S
    Gl  TO 120
                                   "/B = ZA-A(S> ;QR=QA-A( 11 ) ; R^RA- AC 1 0 )
2S0 G)  TT 20S
    1000 STOP
                              - 544  -
-------
  DLRESIDA
 sue  ms PROGRAM-IE TESTS THE  MOM LINEARITY OF  VARIABLE
 WC  AIR/F'JEL  RATI D AMD  GROUPS  HE DATA  IMTD RO * SETC 11 , 600 )
1124,S'.MC 1 1 >,T)TC 1 1 >,TEAMC 1 1 ),TEDC 1 1 ,600)
IIS TALLf=0.
120 m  140  J=l,ll; 0)  ITS 4=1*600
110 ^FDOC I,K) =0. i SETC J,K>=0.
ITS 1 3S  ClsITI MUE
I/id 140  CONTINUE
MS L = l
1S0 ISM  ^F.AOC 1 , 1 51 *EVJO = 300>AM SI  FORMAT(\/)
!(«,(,) K=0. 1 476*A(4>-0.03S3*A< 6 ) -t-0 . 9 44* AC 7)
170 y=0
    I) )  ?*•/» 1 = 10,40*1
    T=I
    OIF=A(7)-T
    IF(OIF.GE.3. .OR.DIF.LT.0. ) GO  TO 260
    IAC=I MTC ( (T-l 0. )/l. >+l . )
    ^EDOC IAC,L>=R + 0.944*A( 7)
    SETC IAC,L)=1 .
    TEOC [AC,L)=A( 7)
    GO  TO  ^70
>M 260  COM T I \li IE
270 270  L=L+1 JGO  TO 1 S0
100 10H  =0. ;TEAM( I )=0.
Wl A\7RG< I )=0.
310 310  CDMTIMUE
320 DO  350 1 = 1,11
330 DO  340 M=1,KAT
333 S'.MC I >=S'HC I )>^EDD( I,M) JTOTC I ) =TOT( I > +SET< I , M >
334 AWG< I )=AVKG( I )+TED< I , M)
340 340  COMTIMIJE
3S0 3S0  C  )MTI MUE
360 SE=SO^TCTALLr/CKAT-l ) )
370 DO  390 1=1,11
37S IFCSIMC I ) .EQ.0. ) RO  TO  390
330 TEAMC I ) =SUV1C I )/TOT( I )
3^1 ^EDCI )=AVRGCI )/TOT( I )
390 390  C DMT I MUE
400 W*I TEC 2, 410) SE, TEAM, TOT, BED
4100 4
410 410  F )WMAT( H  ,10<4HSE=  , F6 .2/4X6HTEAM=  ,
41 5*1 1 F6.2/4X5-IT }T= , 1 1 F6 . 0/4X5HRED= »11F6.1)
420 STOP  JEMD

                          -  545 -
-------
                     APPENDIX I






CAFB PILOT PLANT DESCRIPTION AND OPERATING PROCEDURES
                      -  546 -
-------
                             CONTENTS
                                                                        Page No.
I.   CAFB PILOT PLANT
     Introduction                                                          549
     Flow Plan and Layout                                                  549
     Process  Control                                                       549
     Gaaifier-Regenerator Unit                                             550
     The Stone Handling System                                             55^
     Main Burner Description                                               554
     Analytical Sampling and Instrumentation                               554
     Boiler and Pressurization System                                      553
     Safety Alarm Systems                                                  558
     FIGURES
     Figure 1-1                                                            550
     Figure 1-2                                                            55l
     Figure I-J,                                                            552
     Figure 1-4                                                            55}
     Figure 1-5                                                            556
     Figure 1-6                                                            557
II.  OPERATING PROCEDURES
     Safety                                                                564
     Fuel and Np Supply Prerun Checks                                      565
     Boiler and  Systems  Prerun Checks                                      56j6
     Gasifier  Prerun Checks                                                 565
     Gasifier  Warm Up                                                       567
     Preheat Burner Light Up                                               "568
     Preheat Burner Flame Out                                               570
     Heavy  Fuel  Oil Pump Calibration                                        570
     Change  from Propane to Kerosene                                        570
     Starting  Stone Feed                                                   571
     Boiler  Clean Out                                                       572
                                   - 547  -
-------
                        CONTENTS (continued)
                                                              Page No.
Start Main Flame Pilot Light                                    574
   (a)  Main Flame Out
   (b)  Main Flame On
Change from Kerosene Combustion to Fuel Oil Combustion          575
Change over from Combustion to Gasification                     575
On Gasification                                                 577
Trouble-Shooting on Steady State Conditions                     577
Planned Shutdown on Gasification                                581
   (a)  With Sulphation                                         581
   (b)  Without Sulphation                                      583
Emergency Shutdown                                              53^
Carbon Burn Out                                                 584
Completion of Carbon Burn Out                                   586
Restart after Shutdown
   (a)  From Sulphated Bed after Carbon Burn Out                586
   (b)  From Sulphided Bed after Carbon Burn Out                587
   (c)  From Sulphided Bed without Carbon Burn Out              588
Sampling of Hot Bed Material                                    589
Rodding Out                                                     589
Injection of Toxic Gases                                        589
Preventive Maintenance and Sampling during Run                  590
                               - 548 -
-------
T.   CAFB PILOT PLANT


    INTRODUCTION

    A continuous CAFB gasifier pilot plant has been constructed at the Esso Research
    Centre to provide a demonstration of the CAEB process under continuous operating
    conditions and to provide a means for studying those operational variables which
    cannot be measured in batch reactors.   Features of the pilot plant are summarised
    here.


    FLOW PLAN AND LAYOUT

    Figure 1-1 is a process flow plan of the continuous pilot plant.   The heart of the
    system is the gasifier-regenerator unit cast of refractory concrete contained in
    an internally insulated steel shell.   The product gas of the gasifier fires a 10
    million Btu/hr pressurised water boiler.   The hot water is heat exchanged with a
    secondary water circuit which loses its heat through a forced convection cooling
    tower.   The rest of the system consists of the necessary blowers, pumps and
    instruments to operate the gasifier, regenerator,  burner and solids circulating
    system.

    Figure 1-2 shows the layout of the pilot plant equipment within its building.   The
    gasifier itself sits within a pit to permit alignment of the gasifier outlet duct
    with the burner inlet.   Fuel pumps, flow meters,  and start up burner controls are
    mounted on a mechanical equipment console in the control room.   Electrical
    instrumentation and manometers are mounted in a separate control cabinet in the
    control room.   Gasifier blowers are located in a separate blower house outside the
    main building, and the cooling tower is mounted on the roof.


    PROCESS CONTROL

    Figure 1-3 is a diagram of the pilot plant instrumentation system.   Automatic control
    boxes are used to regulate regenerator temperature and regenerator bed level, and
    gasifier bed level.   A packaged pressurisation system maintains constant boiler
    cooling water pressure and temperature.   All other systems are manually controlled
    by the process operator.   Dashed lines in Figure 1-3 show the indicators and
    control valves normally used by the operator.   Manometers indicate pressures and
    pressure differences in most applications.   In four instances pressure differences
    are also detected by pneumatic delta pressure cells and transmitted to recorders.
    Pressure switches also are employed in several locations to operate warning lights
    for abnormal conditions.
                                      -  549 -
-------
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                                   -  550 -
-------
                GENERAL  PLANT LAYOUT
         Regenerator
         Cyclone
  Gasif ier
Fuel lnjector(3 off)

Air Supply to  	
Regenerator
                                                Heat
                                                Exchanger
              Electrical
              Control
              Cabinet
                                         Circulating Oil Supply
                            Air Supply to  fr°m 30x9 Tank
                            Gasifier
Electrical
Control
Cabinet
 Swinging Jib
 Pillar Crane
                                 SECTION
                                 39'0"



















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Room
1 t IT
Mechanical
Control
Console


Office
>
J 1
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32
1

                      Gasifier
                             Pit
                                      Boiler
                       Blowers for
                       Gasifier
                                                           r   ,.
                                     PLAN
                                         To 54 "O" High
                                          Stack
                                                    FIG.I. 2.
                           -  551 -
-------
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                                            -   552  -
-------
GASIFIER-REGENERATOR UNIT*

The gasifier and regenerator reactors are  cavities in  a single refractory  concrete
block.    The block  contains other cavities which make  up the gasifier outlet
cyclones, the gas transfer ducts, and the  transfer lines through  which solids
circulate between gasifier and  regenerator.    Figure 1-4 is a drawing of this
gasifier-regenerator assembly.    The gasifier cavity is rectangular in cross
section, tapering from 17.5 x 37 inches at the distributor level  to 19-5 x 39
inches  at the 21 inch level.    The upper portion has parallel sides.    The
regenerator tapers  from 7" diameter at the bottom to 8" diameter  22"  above
distributor datum and remains parallel thereafter.
                                            Conntction between cyclones
            Outer metal cosmg-
            Insutoting refractory '
            Ca«table refracfory\
Cyclone for
 gasifier
Expansion bellows to
absorb vertical expansion
on got outlets
                                            Rtmovabl* lid
                                                            X
                                    Regenerator
                                    Cyclone fines
                                   \ fed Into bed
                                    transfer pipes
                           Gas pulse
                                             Bed
                                             dram
                                                      Air Supply
                                                            Air Supply
                      LAYOUT OF CONTINUOUS GASIFIER UNIT
                                                                     FIG 1-4
*  Basic Unit  - see Appendix E for Modifications
                                     - 553  -
-------
The gasifier air distributor consists of ~$2. nozzles each of which contains
horizontal holes arranged in an offset manner with a •5-" diameter final hole to
reduce the gas velocity.   The nozzles are stainless steel mounted on a
refractory covered carbon steel plenum.

The regenerator distributor consists of 5 stainless steel nozzles each with 4,
1/8" holes which are not equally spaced around the periphery having a closer
pitching around the outer side of each nozzle.


THE STONE HANDLING SYSTEM

Limestone is fed to the gasifier through a gravity feed line from a pressurised
weigh  hopper.   A vibrator is used to control the rate of stone addition.   A
ground level hopper is charged from bags of stone.   A pneumatic transfer line
moves the stone from the ground level hopper to an upper hopper from which stone
is periodically dropped into the weigh hopper.   The upper hopper acts as an air
lock to avoid depressurising the weigh hopper.


MAIN BURNER DESCRIPTION

The standard oil burner of the 10 million Btu/hr boiler was replaced with an
experimental burner designed to handle the hot gasifier product.

A general arrangement of the gasified fuel burner is shown in figure 1-5.   It
will be seen that the air required for complete combustion is introduced in 3
stages.   Roughly about 10$ of the air enters a crude injector (l) and is pre-
mixed with the gas.   Further premix may be introduced at point (2) and the
remainder of the air is fed tangentially into a swirl chamber and emerges from
an annular nozzle which is concentric with the gas nozzle.   The design of this
burner was purely empirical and was based on recommended pressure drops at the
nozzle.   The main gas duct is sized to give a flow velocity of about Soft/second,
the gas nozzle gives a pressure drop in the region of 3" w.g., and the air nozzle
gives a pressure drop of about 4-5" w.g.

A pilot light fired by propane gas is used for lighting purposes.


ANALYTICAL SAMPLING AND INSTRUMENTS

On stream analysers monitor the compositions of the key gas streams.   Table 1-1
lists these analysers and their applications whereas Figure 1-6 gives a flow
diagram of the equipment layout.
                                  - 554  -
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        - 556  -
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                                                -  557  -
-------
    BOILER AND PRESSURIZATION SYSTEM

    A handbook containing details  of the boiler  and pressurization unit will be kept
    in the crew room.   If problems occur with this  equipment which is  not  immediately
    apparent call for  help.


    SAFETY ALARM SYSTEMS

1.  Types of Action

    The installation is protected  by a number of alarm circuits,  in  some cases the
    consequence of an  alarm is automatic where immediate safety is concerned, but
    many others are warnings of some changing condition where  there  is time for
    corrective action.

    Action A.

    This action is an  automatic plant shut down  and produces the following actions:-
       o   Fire valves close on oil feed and return lines at entrance  to building.
       o   Oil circulation pump stops.
       o   Gasifier control panel  shuts down everything apart  from main air blower
           on the boiler, primary  and secondary  cooling circuits of  the boiler
           cooling system blowers  on Jrd stage regenerator boost and pressure control
           (regen off  gas).
       o   Interior and exterior bells ring at 3P»  which may be silenced by a mute
           button on the auxiliary panel  in the  air lock passageway.
       o   Red light shows on the  auxiliary panel and also on  the gasifier control
           panel warning light for the auxiliary panel.

    Action B.

       o   Alarm light shows on gasifier  control panel and rings a bell  on the  panel
           which may be muted for  that particular alarm by a switch  located above
           that alarm light.  Automatic gasifier shut down is  not possible with
           action B.

    Action C.

       o   Alarm light shows on gasifier  control panel which can be  linked to
           a gasifier shut down by selecting the switch on the panel to  "Automatic
           Shut Down Mode".  This  alarm will ring a bell unless muted.

    Action D.

       o   Alarm light shows on gasifier control panel - cannot ring a bell or
           cause an automatic gasifier shut down.

                                        -  558 -
-------
      Action E.

         o   Alarm light on auxiliary panel and light on control panel.
         o   No other action.

      Action F.

         o   Horn type warning sounded in J>F,  JA and the grinding room.

      Action G.

         o   Low pressure in the pressurisation unit causes a unique operation - namely -
             a bell on pressurisation unit,  light on gasifier control panel,  auxiliary
             panel warning light,  and automatic shut down of all equipment controlled
             from main panel but not air to burner,  cooling pumps or shut down of fire
             valves or oil circulation pump.

  2.  Alarm Sources

      The installation is best considered as four main systems.

         o   The boiler and its cooling system.
         o   The gasifier.
         o   The experimental burner on the boiler
         o   General  alarms.

?.i   The Boiler and  its Cooling System

             The water in the boiler is pressurised  to about 48  psi  and is pumped through
             a heat exchanger.  The secondary side of the heat exchanger is cooled by
             an evaporative cooler on the roof of the building.

      Primary Circuit Protection

         o   The pressurisation unit has a low pressure warning  set  at 40 psi.

                                            Action G

         o   High water temperature in the boiler water - set at 245°P.

                                            Action B

      Secondary Circuit Protection

         o   Lack of  cooling water flow is detected  by a differential pressure switch
             across feed and return lines to cooler.  This switch is alarmed if the
             pump is  switched on and the differential pressure is less than 3 psi
             approx.

                                          - 559 -
-------
                                      Action A

   o   High water temperature to cooler - a mechanical reset overtemperature
       alarm set in the vertical leg from the heat exchanger - operates  at
       200°F.  The reset button is 10 ft up the vertical leg.

                                      Action A


The Gasifier and Regenerator

The gasifier has a variety of temperature alarms and high or low pressure
alarms.

   o   High temperature in the gasifier bed - usually set to 950°C - set,
       shown and alarmed from Guardian controller.

                                      Action B


    o   High temperature in the regenerator bed - usually set to 1100°C  - set,
        shown and alarmed on Leeds and Northups recorder.

                                       Action B

    o   Gasifier distributor low pressure drop - set to 5" w.g. by pressure
        switch - letter E.  (Under control panel.)

                                       Action D

    o   Regenerator distributor high pressure drop - set to 10" w.g. by  pressure
        switch -  letter D. (Under control panel.)
                                       Action D

    o   Regenerator low bed level - set to 10" w.g. by pressure switch - letter F.
        (Under control panel.)

                                       Action D

    o   Regenerator high bed level - set to 30" w.g. by pressure switch - letter
        C.
                                       Action D

    o   Pressure rise in gasifier gas space - set to 2V by pressure switch G.

                                       Action B
                                     -  560  -
-------
Main Burner and pilot? Burner

Main Burner

The main burner flame can be scanned by 2 detectors,  one at each end of the boiler
and failure of both will cause alarm C.

Pilot Burner

The pilot burner will only light up if there is gas pressure to the pilot and air
pressure to the experimental burner plenum.

If the f ireye which scans the pilot does not see sufficient flame it will cause
the pilot to lock out and show as an alarm light.  Failure of gas pressure or
plenum pressure will have the same result.  It is not possible to check action
of f ireye without attempting start up.
                                      Action B


General Alarms
   o   Ng supply failure  -  Action B
   o   Fire detector - a fusible link above the boiler set to melt at 155°F will
       cause

                                      Action A

       This link needs to be replaced after operation and because it may not be
       convenient to isolate the power at that moment a bypass electrical switch
       has been fitted on the auxiliary panel as a temporary prodedure until the
       link can be replaced.  Replacement must be done as soon as possible.

   o   Sump level

       If the level in the sump rises to about 1/8" of floor level a light will
       shov; on the auxiliary control panel,  the main panel will not be alarmed
       and no bells will ring.

                                      Action E

   o   Emergency Stop Buttons

       There are four emergency stop buttons located:

       o  Close to the sliding window in cubicle
       o  Main door at 3A end of laboratory
       o  Main door at main stores end of laboratory
       o  Adjacent to ladder on side of the pit

                                      Action A


                                     - 561  -
-------
          These must be reset by turning knob and allowing knob to spring back.

      o   Emergency Stop Button On Main Control Panel

          Located  in centre of gasifier control panel and shuts down all items
          controlled from this panel but does not shut down fire valves, cooler pumps,
          air to burner, or oil circulating pump regenerator boost or pressure
          control  blowers.  Reset by turning ring and allowing button to return.

          The fire valves and oil circulating pump can be shut down by then depressing
          the emergency stop button by the sliding window.

                                  i.e.   Action A

      o   Call for Assistance

          There are four buttons located on each wall of the pit with a further button
          on the cubicle wall at the top of the pit steps.  These sound horns in
          3A, 3F and the grinding room.

      o   Fuel Shut Off Valves

          In the event of an emergency shut down where there is any possibility of
          fire the propane gas and kerosene must be isolated at their external valves.
          The propane valve is situated at the external corner of the building
          adjacent to the supply feeder from the propane line.  The kerosene valve
          is located by the barrel stand adjacent to the semi buried storage tank.


                        Summary of Pilot Plant Alarm System


                                              Indication


        Source of Alarm           Auxiliary Panel      Main Control Panel


1.  Failure  of water circulating     Red Light        Red light titled "Auxiliary
    pump or  lack of water  in         and bells        Panel"
    secondary cooling  circuit

2.  High water temperature on        Red light        Red light titled "Auxiliary
    cooler feed  line                 and bells        Panel"

5.  High water temperature in        None             Red light titled "Boiler
    the  boiler                                        high temperature"

4.  Low  pressure  in pressurisa-      None             Red light titled "Auxiliary
    tion unit.                                        panel"
                                    n.b. Red  light  shown on  pressurisation panel,
                                         and  its own bell rings

                                        -  562  -
-------
 5.  Gasifier high temperature
None
 6.  Regenerator high temperature     None
 7.  Gasifier low pressure across     None
     distributor

 8.  Regenerator high pressure        None
     across distributor

 9.  Regenerator low bed level        None
10.  Regenerator high bed level       None
11.  Pressure rise in gas space       None
Gasifier high temperature
warning light and bell

Regenerator high temperature
warning light and bell

Gasifier low pressure distributor
warning light

Regenerator blocked distributor
warning light

Regenerator low bed level warning
light

Regenerator high bed level
warning light

Downstream pressure rise warning
light and bell
12.  Experimental Burner & Pilot
     Failure of:   Main Flame          None

                  Pilot Flame         None
                 Main flame failure warning light
                 and bell
                 Pilot flame warning light & bell
n.  N0 supply failure

14.  Fire detector


15.  Sump level

16.  Emergency stop buttons
     in building

17.  Emergency stop button
None

Red light
and bells

Red light

Red light
and bells

None
Warning light and bell

Redllight titled "Auxiliary
Panel"

Nothing

Red light titled "Auxiliary
Panel"

None
                                         -  563 -
-------
II    OPERATING PROCEDURES
Safety
      There are many possible hazards in the CAPB operation, and it is
essential that every person works carefully and safely.   The plant must
be operated by a three man team unless it is a warming up operation when
two men operation is permissible provided the activities are limited to
recording and controlling the temperature.

      If it becomes necessary to enter the pit at any time there must be
two men available at the top of the pit to render assistance should the
man in the pit get into difficulties.   Two sets of breathing masks fed
from bottles of breathing air must be available, one for use by the man
in the pit, and one for the man standing by at the top of the pit.

      Whilst every precaution has been taken to reduce the dust in the
laboratory area by local dust extraction ducts it may be necessary to wear
respirators when in this area when certain actions are carried out.   Please
ensure that you change the filters regularly and wash out the respirator
after use.

      There are also three positive pressure respirators which are powered
by rechargeable batteries fixed to the belt which also houses the blower
and filter unit.   These are available for general use, but people must
thoroughly wash the mask (as instructions) after use, and ensure that the
battery is recharged.

      Spare primary and main filters are available.

      Ear protection is available either as ear cups or Bilsholm wool plugs
- individuals may find that the use of this protection reduces fatigue
after long periods of time in the noisy area.

      Eye protection must be worn at all times and in some cases full goggles
or face shields must be used if there is a danger of hot or dusty material
being thrown or dropping onto the face.

      Asbestos gloves are available and particularly must be worn when
draining hot lime samples from the unit or any other operation involving
hot material.   Light weight gloves are available for general use.

      A safety helmet has been purchased for each person, and it is important
that these are always worn when in the gasifier area.   If they are too bulky
for some operations there are some hard hats available for general use in
such circumstances.

                                 - 564 -
-------
      In time of trouble assistance may be called by use of the alarm buttons
which sound outside the laboratory in JA and the stone storage garage.

Fire

      There are three powder fire extinguishers - one in the control cubicle
and two in the gasifier area.   Be familiar with their location and method
of operation, but remember that their operation time is short and they will
only deal with small fires.   Also available are two portable CO  extinguishers
- one in the crew room and one in the gasifier area near the control room
door.

      There is a CO  hose reel on the wall immediately outside the main sliding
door - there are two spare full C0p cylinders on the wall adjacent.    The main
reel must be immediately recharged with the two new bottles after it has been
used.

      There is a fire hydrant close to Featherbed Lane near the main door.   The
hose will be laid out as a safety precaution with an adjustable spray nozzle/
single jet fitting located on the end.


Fuel and N  Supply Pre-run Checks

(a)    Heavy Fuel Oil

•     Check tank contents.

»     Check outflow temperature is about l40/150°F.

•     Start compressor/oil pump on boiler by switching on at panel.    Do not run
      for more than five seconds at first few runs in order to set thick oil
      moving.    Continue until temperature gauge on outflow heater reaches 200/
      210°F and then pump may be left on.

•     The boiler heater circuit is now on automatic operation and is ready for use.


 (b)   Kerosene

 •     Stored in 500 gallon tank - check that there is enough for anticipated
       usage.    First check that isolating valve is turned off on pump supply
       feed pipe.   Then open valve at barrel.   Check fire valve has not
       actuated.

 (c)   Nitrogen

 •     Stored in liquid N2 tank.   Check that there is sufficient for
       anticipated usage.    Air Products (Bracknell) must be alerted to make
       daily "topping up"  visits during the operational  period.

                                 - 565 -
-------
•     Check all valves are turned off at the bleed locations on gasifier before
      opening valve on manifold.
(&}   Propane
•     Check valve on tank and valve outside building J>F is open.
Boiler and Systems Pre-run Checks
•     Check water level in pressurisation unit header tank is at
      marker.
•     Make up water supply open to tank.
•     Pressurisation unit on:  check N2 pressure is approximately 48 p.s.i.
•     On start up bell will ring.   Cancel bell.   N^ off at cylinder.
•     Air bled from boiler cooling circuit.
•     Valves open from water reservoir to cooling tower located on first floor
      of water tower (valve is labelled).
•     Notify site services of soft water usage.
•     Start boiler circulating pump.
•     Start cooling tower circulating pump;  hold cut-out for 15 seconds.
•     Power on to cooling tower fan.
•     Check automatic mixing valve working (temperature setting l60°F).
•     Open cooling system purge.   Check for flow in drain pit by blower house.
•     Switch boiler panel on.
•     Check fuel oil circulation in ring main.
•     Check fuel oil circulation in boiler circuit.
•     Check line up of three way valve for flow through boiler circuit heater.
•     Check water pressure in boiler is approximately 48 p.s.i.
•     Check sample lines are correctly installed in flue.
•     Boiler door shut, held on four bolts.
•     Ensure flue damper fully open.
Gasifier Pre-run Checks
•     The gasifier is assumed cold and empty of bed.
•     Check belts O.K.
•     First stage blower.

                                - 566 -
-------
 •     Second stage blower.
 •     Regenerator blowers.
 •     Extract blower.
 •     Vacuum cleaner for stone feed.
 •     Lubrication
 •     Fuel circulating pump.
 •     Fuel metering pumps  (3).
 •     First stage blower.
 •     Second stage blower.
 •     Recycle blower.
 •     Regenerator blowers  (3)-
 •     Main burner blower.
 •     Extract blower.

 •     Tuyere blower.
 •     Cubicle blower.
 •     Cooling tower water circulating pump.
 •     Boiler water circulating pump.
 •     Oil circulating pump under boiler.
 •     Bitumen circulating pumps (2).
 •     Bitumen metering pumps (2).
 •     Analysers
 •     Sample lines.
 •     Calibration.
•     Pumps working.
•     Filters and traps.

 Gasifier Warm Up

 •     Check action of alarms.
 •     Alarm switch to "all alarms show".

                                - 567 -
-------
•     Bell switches to MUTE.
•     Auto shutdown switches to inactive.
•     Main panel power on.
•     Instrument air on - 20 p.s.i.
•     Instruments on and working - charts O.K.
•     Np supply to ring main - 40 p.s.i.
•     Np to pressure tap bleeds -2.5 CFH each.
•     All manometers full.
•     D/P cells zeroed.
•     Regenerator blower on - 5 CFM flow.
•     Check water level in Cbmpton supply seal - 9 FT.
•     Line up to Comptons.   Check operation.   Set to 3 p.s.i.
•     Switch off Comptons, line up N2 via by-pass which avoids meters.
•     Adjust Np to 3 p.s.i.
•     Pocket agitator Ng flow to 4 CFH.
•     Injector N~ flow to 0.3 CFM.
•     Start pulsers and check action.
•     Check solenoid action and line-up to main  (M).
•     Regenerator temp control on manual.
•     Regenerator control switch behind panel  to "off".
Pre-Heat Burner Light Up
•     Close valve in line from stone feed hopper to gasifier.
•     Open line to low range orifice for gasifier air.
 •    Ensure  high range  orifice inlet  blanked.
 •    Ensure:-  Propane  gas line to burner open (three valves, on propane tank,
                    outside and inside  Building 3F).
              -  Igniter  and flame eye  connected.
              -  Visual sight glass clean and tight.
              -  Purge  to flame eye connected (4 CFH).
                 Burner air valve open  and throttle shut.
 •    Mtar-t  tioth jiatiifier- aip Mowers, set to "MO (7PM.
 •    Ensure  flue gas  recycle valve closed.

                                 - 568 -
-------
•     Ensure burn out connection shut.
•     Close plenum air valve and open burner throttles.
•     Compare burner air flow indicator and gasifier air flow indicator .

•     Check zero setting of both air flow gauges.
•     Open plenum air valve and set throttle to marking 1.5.
•     Adjust burner air to 30 CFM.
•     Check regenerator air - 5 CFM.
•     Air to fuel lower side injectors - 5 CFM each.
•     Check centre fuel injector retracted and Np purge to  sleeve to 0.7 CFM,
      and small air flow to injector.
•     Upper side injectors retracted and 4 CFH air bleed injected.
•     Start boiler burner blower - 200 CFM.
•     Air flow to stone feed - 90 L/Min.
•     Np flow to each fines return systems - 4 CFM.
•     4 CFH N2 bleeds to fines returns lines.
•     Start regenerator pressure control blower, and set G/R  £P
      controller to zero.
•     Check that propane pressure reads 30 p.s.i.
•     Turn on electric power to start up burner control.
•     Open pilot propane cock in the control room.
•     Close cock slightly on air to pilot to reduce pressure.

•     Activate start up burner control and go to propane throttle by
      gasifier.
•     Ad j UK I propane flow to 40 CFH as soon as propane solenoid opt;n.<;.
•     ,".lnil. off pi Lul. »'M'k In the oontrol Poom when wtitln 
-------
«     Increase flow of regenerator air if necessary.

•     Monitor temperatures and adjust gas and air flows to follow
      temperature schedule of 15°C per hour.

•     Maintain air/fuel ratio in the burner of 1 CFM/1 CFH and about 100 CFM
      air flow through the plenum.

•     Sequence for increasing the propane firing rate is:
                              i
          Increase total air (motor valve).

          Increase propane rate.

          Adjust burner air.
          Open plenum air throttle as required.

Pre-Heat Burner Flame Out

•     Flame out:  in case of flame out allow one minute purge time, identify
                  cause of failure and correct eg dirty fire eye then follow
                  "pre-heat burner light up" from the line "open pilot propane
                  cock in the control room".   When re-lit increase propane
                  and air (including plenum air) to the value before flame
                  out and continue raising temperature.
•     Observe for hot spots on the shell - correct by stopping leaks with
      fibrefrax or asbestos and sairset and by water spray.
Heavy Fuel Oil Pump Calibration


•     Close fuel valves to injectors.

•     Open sampling valves.
•     Verify trace heating on and pipes hot.
•     Line oil through to the metering pumps and calibrate.

•     Check operation of 80 p.s.i. overflow valve.
•     Line up fuel to centre injector.
•     Turn off fuel oil, turn on kero and line through to kero barrel, disconnect
      oil line to centre injector in the pit and clear through any P.O. into
      a bucket with kero (avoid spillage and have dry powder cylinder available).
      Reconnect oil line to centre injector.

Change From Propane to Kerosene

•     When gasifier temperature reaches 700°C raise centre injector to 3"
      begin kero injection at very low rate with 5 CEW of air.

                                 - 570 -
-------
 •     Gradually replace gas flow with kero while increasing plenum air flow to
       250 CFM and lowering propane to 50 CFH.
•     Line up air supply to the fines return  control panel.
•     Adjust air to fines return pulser to 3  p.s.i.
•     Set bleed below f" Audco on each fines  return pipe to 4 CFH and
      open the Audco valve.
•     Set N2 to each fines return injector to 4 CFM.
•     Set timers on fines return control panels to 5 rain, cycle and switch
      on.
•     N2 rate to fines return injectors and timers on the fines return panel
      may need adjustment once the system settles.

Starting Stone Feed
•     Record weight of limestone supply and fill ground level feed hopper.
•     Close main valve and balance valve between stone hoppers.
•     Start motor on transfer vacuum line.
•     Open valve on vacuum line and valve on fill line and suck stone up to
      overhead hopper.
•     Close fill line and vacuum line valves.
•     Equalise pressure between stone feed hoppers by opening balance valve.
•     Open big valve between hoppers and drop lime into lower hopper.
•     Check that weigh cell is working - record weight change.
•     Close main and balance valves between hoppers.
•     Check Np pressure to injectors is 3 p.s.i.
•     Open Mp to meters.
•     Check bleeds to injectors and agitators (0,3 CFM,  4 CFH respectively).
•     Set bleed Ng flows to pressure tappings (2.5 CFH).
•     Pressurise outer casing of gasifier to 10" WG and note flow rate.
•     Check manometer fluid levels.
•     Increase regenerator air flow to 15 CFM.
•     Adjust pressure balance to stop G to R gas flow.
•     Check regenerator to gasifier injector bleed is at 0.3 CFM.
•     Check that temperature at G to R pocket is below 1,000°C.
•     Start rapper stack cyclone.

                               -  571  -
-------
•     Do following to start stone feed:
          Start 1 CFM N? to stone hopper vessel.
          Open valve between hopper and gasifier.
          Start vibrator feeding lime at 50 Ib./hr.
          Check that lime is being fluidised.
          Increase lime rate as conditions permit - keep bed temperature
          above 850°C.
•     Check that the cyclone drains and fines return system operates
      satisfactorily:
          Visually from tops of cyclones.
          Visually through tops of boxes.
          Observe valve opening and closing sequence.
          Check that valves are opening and closing fully.
•     As bed depth increases to near 5" you roay need to increase the propane
      pressure by screwing down the propane pressure reducer.   Count the
      number of turns and record in log book.
•     When bed depth reaches 5" with good kero combustion.
•     Close main valve in propane line to burner.
•     Turn off power to start up burner control.
•     Close air valve adjacent to burner, 2" ball valve.
•     Start 4 CFM air to burner purge.
•     Stop combustion air to start up burner.
•     Open plenum throttle and adjust plenum air to 170 CFM using motor valve.
•     Adjust kerosene rate to maintain 870°C - note rate in log.
•     Adjust regenerator pressure to 3-V below gasifier.
•     Adjust pulsers to obtain good solids circulation.
•     Continue addition of limestone to specified level.
•     Check-regenerator drain operation.
•     Check cyclone drain system as specified above.
•     Timing of the fines return cycle may need changing.
Boiler Clean Out
•     Line up equipment and manpower to clean out boiler:
          Rake.

                                -  372  -
-------
          Breathing apparatus.
          Door bolts.
          Spanners.
•     Stop stone feed vibrator.
•     Close valve between stone feed and gasifier.
•     Stop Np feed to stone hopper.
•     Raise gasifier temperature  to 950°C.
•     Perform following operations in  quick  sequence  to  interrupt
      combustion and hold temperature.
          Stop fuel pumps and close fuel line valves.
          Switch off gasifier blowers.
          Close hand valve in air line to plenum.
          Stop regenerator air blower.
          Turn bed transfer pulsers to 10/2.
          Reduce air to all fuel injectors protruding into bed to 1 CFM.
          Stop air to stone feed.
          Stop Np to fines return.
          Stop cyclone drain controllers.
          Stop regenerator P control blower.
•     Perform following operations rapidly to prevent
          too much temperature loss in gasifier bed.
          Clean solids from boiler tubes.
          Remake boiler door seal with f-"  rope + bostick and close door.
          Check that main flue damper is open.
          Check flue gas recycle valves are  closed.
•     When all is ready, and before bed temperature falls below JOO°C resume
      combustion by following steps in quick order:
          Start air to protruding fuel injectors - 5 CFM each.
          Start blowers and open air to plenum,  check fluidisation.
          Open fuel line valves  and start  pump at rate for steady 870°C
          (eea log).
          Start air to stone  feed.
          Start Np to fines return.
                                  -  573  -
-------
          Start air to regenerator and adjust to 15 CFM.
          Start regenerator P control blower.
          Start cyclone drain controllers.
          Increase pulser rates to 5/1-
•     Raise gasifier temperature to 870°C.
•     Resume stone addition:
          N^ to stone hopper.
          Open feed valve.
          Start vibrator.
Start Main Flame Pilot Light
(a)   Main Flame Out
•     Clean fire eye and start purge air in control room (60 1/min.).
•     Set main burner air to 600 CPM.
•     Line up all three propane valves to pilot burner.
•     Check propane pressure at J>0 p.s.i.
•     Open air valve to pilot burner (set at 12 CFM, pitot 0.1).
•     Turn on power to pilot burner control.
•     Start control sequence.
•     When propane opens check flow is 1.9 CFM.
•     When lit check stability by inspecting.
•     Increase burner air to 800 CFM.
•     Check pilot stability.
(b)   Main Flame On
•     Clean fire eye and check purge at 60 1/min.
•     Line up all three propane valves to pilot burner.
•     Check propane pressure at 3° p.s.i.
•     Open air valve to pilot burner (set at 12 CFM, pitot 0.1).
•     Check power on to pilot burner control.
•     Start control sequence, but hold in cut out button until propane
      pressure gauge needle flicks to maximum position and release button


                                -  574 -
-------
 •      Check  propane  flow  is  1.9 CFM.
 •      Reset  pilot burner  alarm and  cancel mute.
 Change From  Kerosene Combustion to  Fuel  Oil  Combustion
 •      Activate  alarm bells - except main flame.
 •      Check  cooling  system - levels, pressures, flows +  set bleed, make up
       valve  in  water tower open.
 •      Check  that hand valve  (Pit) in the flue gas recycle line is closed and
       F.G.R. orifice gives zero reading.
 •      Line up valves from boiler flue through F.G.R. blower and filter to
       blower house inlet.
 •      Start  flue gas recycle blower.
 •      With motor valve fully closed, open hand valve (Pit) in F.G.R. line.
 •      Open flue gas  recycle  motor valve  to give ^0 CFM.
 •      Set plenum air supply  to 170  CFM.
 •      Adjust kero feed rate  to give steady 870°C.
 •      Check  that trace heating to oil feed lines is on and hot.
 •      Close  kero valve and open fuel oil valve.   Leave  pump running and
       adjust back pressure to 40 p.s.i.
 •      Stop stone addition:
          Stop  vibrator.
          Close feed valve.
          Stop NO to  hopper.
 •      Start  air bleed to  flame fire eye  at boiler back end.
 •      Check  operation of boiler main flame fire eyes (2).
 •      Re-install and  check isolating valve open for rear door fire eye and
       tapping clear  of lime.
 •      Check  rear door main flame fire eye light shows on boiler control panel.
 •     Switch off Middle and R.H.  metering pumps and adjust L.H. pump to give
       steady 870°C for an hour.    Record all flows and temperatures and any
       relevant comments in the log book.
Change Over From Combustion to Gasification
•     Ensure that combustion  is  steady on L.H.  pump only, Middle and R.H.  off.
•     Set Middle pump to 56 Ib./hr.
•     Set R.H.  pump to 146 Ib./hr.
                                -   SIS  -
-------
•     Stop L.H. pump and start Middle pump.    Adjust back pressure to 40 p.s.i.
      if necessary.
•     Control bed temperature by intermittent operation of Middle pump -
      estimated 20$ on 80$ off.
•     Set L.H. pump to 146 Ib./hr.
To Gasify
•     Verify boiler pilot alarm and check presence of flame visually.
•     Verify all other alarms and operation of main flame fire eyes (which
      respond to torch light).
•     Set high temperature bed alarm to 1,000°C.
•     Main flame failure and auto shut-down inoperative.
•     Switch Middle pump off and allow bed temperature to fall to 850°C.
•     Switch Middle pump on to purge boiler with inerts (10 sec.).
•     When bed temperature rises to 870°C do the following simultaneously and
      rapidly:
          Switch on L.H. and R.H. pumps.
          Start stop watch.
      8 sec.  - reset main flame failure alarm.
          If M.F.F. alarm cancelled switch off M.F.F. alarm mute and activate
          auto shut down.
          Proceed to "on gasification".
          If M.F.F. alarm did not cancel do as follows:
      9 sec.  - reset M.F.F. alarm:
          If M.F.F. alarm cancelled, do as at 8 sec.
          If M.F.F. alarm not cancelled do as follows:
      10 sec. - reset M.F.F. alarm:
          If M.F.F. alarm cancelled do as at 8 sec.
          If M.F.F. alarm not cancelled do as follows:
      11 sec. - reset M.F.F. alarm:
          If M.F.F. alarm cancelled do as at 8 sec.
          If M.F.F. alarm not cancelled:
             Switch off L.H. and R.H.  pumps.
             Reset L.H.  pump to steady combustion rate (approximately 30 Ibs./hr.)

                                  - 576  -
-------
             Switch off Middle pump before gasifier temperature reaches 1,000°C
             but not less than 10 sees, after L.H. and R.H. pumps off.
             Switch on L.H. pump.
             Line out on combustion at 870°C.
      Attempt to find out what went wrong, rectify if necessary and repeat
      from "change over from combustion to gasification".
On Gasification
•     Switch off Middle pump.
•     Reset high temperature bed alarm to 950°C.
•     Adjust metering pumps' pressure to 40 p.s.i. (if necessary).
•     Check for leaks on gasifier and seal if necessary with fibrefrax and
      sairset.
•     Resume stone addition:
          Np to hopper.
          Open valve between hopper and gasifier.
          Start vibrator.
•     Adjust flue gas recycle and air rates to obtain specified temperature
      and gas velocity.
•     Adjust stone circulation rate to obtain desired regenerator temperature.
•     Put regenerator temperature control on automatic:
          At controller.
          Behind panel switch to "on".
•     Check cooling system operation;  set cooler control to 160°F.
•     Bring conditions to specified level.
Trouble-Shooting on Steady State Conditions
•     Do not change any control settings unless one or more of the listed
      deviations occur.
•     Ensure:-  preventive maintenance procedures are carried out.
      Watch  •   Op level in the flue gas.
             •   Gasifier Bed Temperature.
             •   Regenerator bed temperature.
             •   Gasifier top space pressure.

                                -  577 -
-------
             •   Fuel delivery pressures.

             •   Fines return system.

             •   Regenerator CO. and S0_.

             •   Compton pressures.
             •   Boiler flue gas exit temperature.

             •   Gasifier bed depth.

•     Enter in the log book, details of any incidents which occur, together
      with the time of occurrence and the remedial  actions which were taken.

•     Possible Incidents due to Malfunction

1.    Bed Temperature Starts to Rise Rapidly

(a)   Check 02 level in flue gas.   If this is rising then the fuel is not
      getting through to the gasifier.

(b)   If C>2 level is normal check the stone feed and see that this is
      functioning properly.   If not try adjusting the feed rate, and other
      remedial actions such as refilling the hopper.

(c)   If the Og is rising then check the fuel pump delivery pressures.   If
      these are high (80) then fuel may be by-passing the injectors and blowing
      out into the dump can.   In this case check the dump pipe outlet for
      oil flow and adjust the fuel pressure control valve to bring the
      pressures both to 40 p.s.i.g.

(d)   If opening the fuel valve will not lower the  pressure then either the
      fuel injector is blocked or else there may be emulsion in the fuel.
      Try switching the fuel to the alternate injectors.    If this does not
      ease the trouble then switch back to the previous fuel tank and call for
      help.   If the fuel shortage persists then eventually there will be a
      flame-out and the unit will shut down automatically.   Initiate
      emergency shut down procedure.

(e)   If the fuel pressure is low with rising bed temperature then the fuel
      tank may be empty.   Check this and swap tanks if necessary.

2.    Regenerator Temperature Rises Rapidly

      The regenerator temperature actuates an alarm at 1,100°C and a nitrogen
quench if valve is open.   If it suddenly rises the chances are that the bed
transfer system is inoperative.
                                 - 578 -
-------
 (a)   First  check  the  Compton  pressures,  these  should be  about  J p.s.i.g.
      If  they are  low  then  the Comptons will have  stopped;   switch to the
      alternative  nitrogen  supply.

 (b)   If  on  automatic  control,  check the  rate at which the  gasifier to
      regenerator  pulseris  working.    If  this is very rapid then it will
      be  inoperative.   Switch to manual  and adjust  to a  reasonable rate,
      i.e. greater than 5/1* which brings the temperature back  into line.

 (c)   If  the temperature  is excessive and must  be  reduced quickly,  use the
      regenerator  pressure  control valve  to swing  the pressure  differential
      between the  gasifier  and regenerator.   This will rapidly exchange bed
      material and will temporarily  bring the regenerator temperature  down.

 (d)   If  manual  control does not work, and the  gas supply is satisfactory
      then there may be a blockage in the gas injectors.    Go down  into the
      pit, check and rod out injectors, bleeds  and transfer lines,  if
      necessary.

3.    Fines  Return N^  Pressure  Rising


      This indicates a blocked  fines return pipe.   Switch  off  the
corresponding control  panel and rod  out the pipe.

4.    Cyclones Not Draining Properly

      This is indicated by  cyclone drain  temperature  dropping steadily, and
can be verified  by a visual check through sight glasses in  the  top  of  the
cyclone and  on the box.   Check valve  operation;   if  not  satisfactory  then
rectify faulty valve.   If  blocked,  rod out.    If  the  blockage  appears  to be
in the pulser then turn off the control panel,  and turn off ^  to injector
and shut  off the -f" Audco valve.   Rod through  the valve  from below the puffer.
As a last resort dismantle  the  puffer, clean out and  replace.

5-    Regenerator  CCU  Increases and  SOp Decreases


      This indicates that too much carbon  is accumulating on the bed material.
The remedy is to increase the air and  flue gas  supply  to the gasifier to
maintain temperature.   Do not change  the  fuel  rate because this is related to
the stone feed rate.

6.    Gas Space Pressure Increases

      Prepare for planned shut down and decoke when the gas space pressure
approaches 20" WG.
                                 - 519  -
-------
7.    Automatic Shut Do*n

      Initiate emergency shut down on gasification procedure.

8.    Boiler Flue Gas Temperature Rises

      If this temperature rises rapidly then the brickwork .arch, which seals
against the boiler door will have developed a leak.   Call for help when
the temperature exceeds 500"P.

9-    Back Up Pump on the Pressurisation System Runs Continuously

      Call for help.

10.   Main Flame Pilot Light Goes Out

      This will actuate the alarm bell.   Try to relight the pilot using
'start main flame pilot light (b)'  procedure, and if unsuccessful call for
help.


11.   Nitrogen Supply Failure

      An alarm bell will actuate in control room.   The transfer system/fines
return system/nitrogen bleeds will fail.   The Comptons will automatically
switch off.   The regenerator temperature initially will rise rapidly and you
may need to activate the N2 quench, but eventually the regenerator temperature
will fall when carbon has been removed and stone sulphated.

      Transfer nitrogen bleeds to cylinder supply.   Identify cause of fault
and rectify immediately if possible.   If it is not possible to remedy fault
within five minutes initiate planned shut down without sulphation.   Note the
N  plenum purge will need to be  coupled to Ng cylinder supply.
                                  - 580 -
-------
                  PLANNED SHUT DOWN ON GASIFICATION


•     Possible reasons:

      (a)   Prior to decoke.

      (b)   Gasifier maintenance, e.g. removal of lime from plenum.

      (c)   Boiler Back End Clean Out.

Two alternatives:

      (a)   with sulphation.

      (b)   without sulphation.

•     If the reason for the shut down necessitates an activity in which the
      bed is exposed to the open air, then it is necessary to sulphate the
      bed to avoid formation of CO gas in the pit.

(a)    With Sulphation

•     Reduce gasifier temperature to below 850°C by increasing flue  gas recycle
      rate.

»     Switch regenerator temperature control to manual - switch behind panel
      to 'off'.

•     Increase pulse rate to reduce regenerator temperature below 1,000°C.

•     CHECK auto valve on cooler is functioning and pressure in pressurisation
      unit is O.K.   (If auto valve not working be prepared for loss of
      pressure in pressurisation unit, e.g. arrange for back-up (hand) pump.)

•     Shut vent  from boiler sample cyclone with plug.

•     Disconnect sample lines to boiler SOg analyser, and clip off so that
      other analysers can monitor boiler flue without sucking air.

 •     Shut off  auxiliary air bleeds  to gasifier -

       (a)    Air bleed  to lid if present.

       (b)    Air to  preheat  burner purge.

       (c)    Switch  fuel  injectors from air to N ,  set at 2  CM  (open  N FIRST).

       (d)    Air to  stone feed.

 •     Close  stone feed valve.

                                 - 581 -
-------
•     Close N2 to stone feed hopper.

•     Switch off stone feed vibrator.

•     Close needle valve on air meter manometer to prevent blowing.

•     Open flue gas orifice by-pass valve.

•     Switch automatic shut down to 'inoperative1 and mute main flame and
      pilot flame alarms.

Supervisor

      Switch off fuel pumps.

      Close gasifier air motor valve.

      Open FGR motor valve to give 140 to 280 CFM.
Man A
      As soon as M.F.F. light on, close throttleson main and premix burner
      air lines.
Man B
      As soon as M.F.F. light on, close fuel valves in control room, go to
      blower house and block off open air inlet.

      Control bed temperature to 900-950°C by regulating flow of air to main
      burner (use first primary  air throttle).   Oxygen concentration in
      flue gas recycle of -^.10 vol.$ is required (measured on plenum air Q^
      meter).

      Sulphation is complete (^*.20 minutes duration) when oxygen levels
      increase and bed temperatures falls.

      When complete -

      (a)   Shut off gasifier blowers.

      (b)   Close plenum valve.

      (c)   Close FGR valve in pit.

      (d)   Reduce regenerator air flow to 3 CFM.

      (e)   Close first primary air throttle to main  burner.

                                 -  582  -
-------
          (f)   Switch off fines return system.
           (g)   Np  to fines  injectors to 1  CFM each.
           (h)   Open needle  valve on air meter manometer.
(b)   Without Sulphation
     •     Increase gasifier temperature to 930*C by shutting off flue gas recycle
           and/or reducing fuel supply to gasifier.
     •     Close FGR in pit.
     •     Shut vent from boiler sample line with plug.
     •     Disconnect sample lines to boiler SOg analyser, and clip off so that
           other analysers can monitor boiler flue without sucking air.
     •     Shut off auxiliary air bleeds to gasifier -
           (a)   Air bleed to lid if present.
           (b)   Air to preheat burner purge.
           (c)   Switch fuel injectors from air to Ng set at 2 CFM (OPEN Ng FIRST).
           (d)   Air to stone feed.
     •     Close stone feed valve.
     •     Close N_ to stone feed hopper.
     •     Switch off stone feed vibrator.
     •     Mute main flame failure alarm.
     •     Switch off fuel pumps.
     •     Check blowers and pumps are off.
     •     Close regenerator blower outlet valve.
     •     Close plenum throttle.
     •     Close plenum valve tight.
     •     Open plenum throttle.
     •     Turn on plenum N~ purge at 1 CFM.
     •     Switch off regenerator blower and fines return system.
     •     N   to fines returns  to  1 CFM  each.
     •     Close fuel valves.
     Emergency T'hiit. Down on Gasification
     •     When ft.l Arms ring and main i'iutne failure uhowu:
               Check blowers and pumps are off.

                                      - 583 -
-------
          Close regenerator blower outlet valve and burner purge.
          Close plenum throttle.
          Close plenum valve tight.
          Open plenum throttle.
          Check plenum N^ purge at 1 CFM.
          Close air to stone feed.
          Close stone feed valve.
          Close Np to stone feed hopper.
          Switch off vibrator.
          Change fuel injector purges to Np and set at 2 CFM.
          Close fuel valves.
          Close off any air supply, e.g. to lid.
          Switch off regenerator blower and fines return systems.
          N? to fines return to 1 CFM each.
          Close FGR valve in pit.
      The gasifier is now safe to leave slumped for at least one hour to
investigate cause  for shut down and rectify, or call for help.   If the shut
down is likely to last for more than 15 minutes purcce through fuel oil lines
with kerosene.

Probable Causes for Shut Down
•     Failure of 12V stabilised power supply to main board.
•     Interruption of mains supply/fire eyes dirty/not connected/eye ports
      blocked.
•     Pressurisation unit lost pressure - pump failure/leak/non-ret valves.
•     Failure of fuel supply - tank empty/filters blocked/fire valves dropped/
      water-oil emulsion.
Carbon Burn Out
•     The procedure for carbon burn out is the same whether the shut down was
      planned (with or without sulphation) or emergency.
•     Put plug on air inlet to gasifier blower.
•     Put cap on outlet from sample cyclone.
•     Close throttle on main and premix burner air lines.

                                   -  584  -
-------
•     Restart gaslfl«r blowers.
 •     Open  FOR in  pit.
 •     Close flue gas  recycle  by-pass  valve.
 •     Open  FGR motor  valve.
 •     Open  valves  in  gas line to gasifier lid and start  small  flow initially,
       building to  a flow of 100 CFM flue  gas,  holding thermocouple in  duct  to
       below 1,000°C.
 •     Check main air  blowers  running,  and adjust  flow by opening premix throttle
       to give 02  content of w? vol.$ through lid.    (Measure  in flue  gas 02
       meter.)
 •     Monitor thermocouples downstream of bed and adjust air flow to maintain
       temperature below 1,000°C.
 •     Increase gas flow through lid to 150 CFM towards end of burn-out while
       still maintaining downstream temperatures below 1,000°C.
 •     Purge fuel lines to injectors with kerosene by opening drains or
       disconnecting lines in pit.   Run kero into a keg and have a dry powder
       extinguisher at the ready.   Close fuel valves and reconnect fuel injectors.
 •     Burn out is complete when COg in boiler flue gas begins falling.
 •     During burn out monitor bed temperature (T2).
 •     If temperature falls below 700°C and bed is sulphated, change to
       kerosene combustion:-
           Close off air/FGR to lid, and air bleed via burner premix throttle.
           Close FGR motor valve.
           Set one-fuel pump to deliver 56 Ibs./hr.
           Check trace heating is on and hot.
           Remove plug from air inlet to gasifier blowers.
           Open plenum valve  and adjust to 170 CFM by opening air motor valve.
           Start fuel  pump and open fuel valves to injectors.
           Continue combustion till bed temperature rises to 850°C.
          Maintain watch on  downstream thermocouples while bed is being heated
           up.
           At 850°C -  shut off fuel pump and close fuel valve.
           Shut off plenum valve and close air motor valve.
           Open FGR motor valve.
           Continue decoke from "Carbon Burn Out Procedure".

                                  - 585 -
-------
•     li' temperature falls to 700°C, and bed is sulphided:-
          Close off air/FGR to lid, and air bleed via burner premix throttle.
          Close FOR motor valve.
          Remove plug from air inlet to gasifier blowers.
          Open plenum valve.
          Adjust air flow to 170 CFM using air motor valve.
          Continue until temperature rises to 850°C.
          Maintain a watch on downstream thermocouples.
          At 850°C close plenum valve.
          Open FOR motor valve.
          Continue decoke from "Carbon Bum Out Procedure".
•     If re-heat of sulphided bed fails to reach 850°C, and temperature starts
      to fall because bed carbon is depleted and sulphide oxidised to sulphate,
      resume under "Temperature fall during decoke with sulphated bed".
Completion of Carbon Burn Out
•     When C02 level in flue gas starts to fall, indicating completion of
      burn out:-
          Close air plus FOR to lid.
          Close FOR valve in pit.
          Close FOR motor valve.
          Remove  plug  from  air inlet  to gasifier blower.
          Remove  plug  from  sample  cyclone.
          Increase  N?  to  fines return to 4 CFM each.
 Restart After Shut  Down
 (a)   From Sulphated Bed after Carbon Burn Out
 •     After  "Completion of  Carbon  Burn Out"  procedure:-
 •     Reconnect SO^ analyser to sample system,  zero and  check  calibration.
 •     Resume kerosene combustion using as a check list  the  procedure under
      "Boiler Clean Out" after the boiler door has  been  closed.
 •     Go to  procedure  for "Change  from Kerosene Combustion to  Fuel Oil
      Combustion",  but omit final  step of holding 870°C  for one hour.
 •     Go to  procedures for  "Change Over from Combustion  to Gasification" and
      "On Gasification".
 •     Resume test programme.
                                  - 586  -
-------
 (b)   From Sulphlded Bed After Carbon Burn Out
 •     After "Completion of Carbon Burn Cut" procedure:-
 •     Reconnect S0p analyser to sample system, zero and check calibration.
 •     Check main burner pilot or re-establish, see "Start main flame pilot light",
 •     Activate alarm bells except main flame.
 •     Check cooling system levels/pressures/flows/bleed.
 •     Check FOR blower on.
 •     Check FGR valve in pit is closed, and close FOR motor valve.
 •     Check trace heating is on and hot.
 •     Verify operation of main flame detectors.
 •     Check boiler pilot alarm and verify visually.
 •     Verify all other alarms except main flame.
 •     Set high temperature alarm on gasifier to 1,000°C.
 •     Main flame alarm muted and auto shut down inoperative.
 •     Set fuel pumps to deliver 292 Ibs./hr. total.   Arrange flows such that
      equal volumes flow down each injector with all pumps on.
 •     Open plenum valve.
 •     Adjust air to 170 CFM.
 •     Quickly open FGR valve to 30 CFM.
 •     Start air to regenerator and adjust to 15 CFM.
 •     With sulphided bed allow gasifier temperature to rise to 850°C.
 •     At 850°C simultaneously switch on two pumps totalling 292 Ibs./hr. and
      start stop watch.
 •     At 8 sec. reset main flame failure alarm (MFFA).
 •     If MFFA cancels switch off mute and arm auto shut down.
 •     Proceed to "On Gasification".
 •     At 9 sec. reset MFFA and repeat as above.
•     At 10 sec. reset MFFA and repeat as above.
•     At 11 sec. reset MFFA and repeat as above.
•     If MFFA has not cancelled at 11 sec. switch off pumps immediately.
 •     At 21 sec. switch off main air blowers and proceed as for "Restart After
      Shut Down".
•     Investigate causes for failure to ignite, rectify and repeat.

                                 -  587  -
-------
 (c)   From Sulphided Bed Without Carbon Burn Out
 •     If emergency shut down has been effected find the cause of shut down
      and rectify.
 •     Check fuel oil fire valves are open, and oil circulating pump is operating.
 •     Check red light is out on auxiliary panel.
 •     Check main burner pilot or re-establish, see "Start Main Flame Pilot Light"
 •     Activate alarm bells except main flame.
 •     Check cooling system levels/pressures/flows/bleed.
 •     Check FGR blower on.
•     Set N_ to fines return 4 CFM each.
 •     Check FGR valve in pit is closed, and close FGR motor valve.
 •     Check trace heating is on and hot.
 •     Verify operation of main flame detectors.
 •     Check boiler pilot alarm and verify visually.
 •     Verify all other alarms except main flame.
 •     Set high temperature alarm on gasifier to 1,000°C.
 •     Main flame alarm muted and auto shut down inoperative.
 •     Set L.H. and R.H. fuel pumps to deliver 292 Ibs./frr. total.   Arrange
      flows such that equal volumes flow down each injector.
 •     Open plenum valve.
 •     Adjust air to 170 CFM.
 •     Quickly open FGR valve to JO CFM.
 •     Start air to regenerator and adjust to 15 CFM.
 •     Allow gasifier temperature to rise to 850°C.
 •     At 850°C simultaneously switch on two pumps totalling 292 Ibs./hr. and
      start stop watch.
 •     At 8 sec. reset main flame failure alarm  (MFFA).
 •     If MFFA cancels switch off mute and arm auto shut down.
 •     Proceed to "On Gasification".
 •     At 9 sec. reset MFFA and repeat as above.
 •     At 10 sec. reset MFFA and repeat as above.
                                  - 588 -
-------
•     At 11 sec. reset MFFA and repeat as above.
•     If MFFA has not cancelled at 11 sec. switch off two larger pumps
      immediately.
•     At 21 sec. switch off main air blowers and proceed as for "Restart After
      Shut Down".
•     Investigate causes for failure to ignite, rectify and repeat.

Sampling of Hot Bed Material

•     Wearing of  asbestos  gloves  is recommended for this operation.

•     Ensure that both bleeds are at 2.5  CFH.

•     Open sample pot exit valve  and drain leg valve, and drain bed material
      into 28 Ib. keg until red hot bed material appears - rod out drain leg
      if necessary.
•     Close exit  valve and fill sample pot with hot bed material (^ 4 Ibs.)
      observe through sight glass.

•     Leave Np purge and leave sample to  cool  (^-30 mins.).

Rodding Out

•     Wearing of  asbestos gloves  and a face-mask is necessary, and in some
      instances,  for example rodding from the top of the cyclones, full
      breathing apparatus should  be used.

•     Turn on N?  to rodding lance and set at high flow rate.   N.B. too high
      a Np flow may trip the safety switch on the Compton compressors.

•     Remove plug, insert and position Np lance in rodding port before opening
      valve.

•     After rodding withdraw lance beyond valve, but not fully out and close
      valve.
•     Care should be taken when rodding fuel injectors, fines return pipes or
      manometer tappings where a  significant positive gas pressure exists on
      the other side of the blockage.   A cloth wrapped  (like a scarf) round
      the neck inside the overalls will save neck burns.   In the case -of
      regenerator tappings remember the gas stream will contain 8-10 vol.#

Injection  of Toxic Gases

      This will  only be carried out by a  qualified person fully familiar
with  toxicity of  handled materials, and with safe handling and test
procedures.
                                   - 589  -
-------
      Injection shall take place only when another shift supervisor is
present and observing the following precautions.

      (a)   Both sliding doors to gasifier area open.

      (b)   Access of personnel not involved in test to gasifier area must
            be prevented by posting sentries.

      (c)   Full breathing apparatus should be worn by tester and back-up
            man.

      (d)   All equipment should be leak tested before use.

      (e)   On the spot analysis for toxic materials of atmosphere in main
            pilot plant area and control room  must be  carried out throughout
            test period with a Drager.

      (f)   Samples and any necessary readings outside the  control room will
            be taken by the nominated person only.


Preventive Maintenance  and Sampling During  Run

      The following action items  should be  carried  out  on a  regular  basis
throughout  the  run  as  indicated below.

•     Blow  out  pressure tapping lines and zero manometers  (every shift).

•     Zero  and  calibrate  analytical  instruments/change  filters  (day  shift only)
•     Rod out flue  gas  sample  line  - change filter  on flue sample  line  and
      regenerator sample  line,  and  empty  knock-out  vessel  (every shift).

•     Clean fire  eyes  on  boiler (every  shift)
          Check if  red  light  is on  at boiler  control  panel,  showing  rear
          door  fire eye is seeing a  flame.    If light is on,  remove  and
          clean front  fire eye first, then  clean  rear door fire  eye.    If
          light is  off,  clean  rear  door fire  eye  first, then front fire eye.

          Always  check  red light  is  on  at boiler  panel  after cleaning rear
          door  fire eye.
          Failure to follow this  sequence for cleaning  fire  eyes may result in
          an  automatic  shut down.

•     Oil dust  extractor  fan bearings located in  roof and grease- boiler water
      cooling pump,  and boiler water circulating  pump (2 grease  points  each)
       (every  shift).
                                  -  590  -
-------
Check blowers for belt wear (a) blower house   (2)      /,    ,
                            (b) regenerator (J)          datasheet 4)
                            (c) cooling fan on roof

Bleed air from boiler water system - 3 points.

Every six hours take gasifier and regenerator bed samples and gasifier
cyclone (L.H.).

At 12.00 and 24.00 take gasifier, regenerator, regenerator cyclone,
boiler back and boiler flue, gasifier cyclones (2) samples.
                             - 591 -
-------
                     VII GLOSSARY OF TERMS
Watt (W)

Watt electrical  (We)
Vacuum bottoms
Ca/S
Air/Fuel ratio
 • Ix • £i •
Bed sulphation
Combustion
Basic unit of energy rate.

Rate of production of electric power.
A power generation boiler fired at a
rate of 100 MW, in terms of fuel
energy input, will produce 30 MWe at
an overall thermal efficiency of 30%.

The petroleum residue recovered from
the reboiler of a vacuum pipestill.
Typically about 30% by volume of
the residue from the reboiler of an
atmospheric pipestill.

The mol ratio of the rate of calcium
in the fresh stone fed to the gasifier
vs. the rate of sulphur entering the
gasifier in the fuel.

The total oxygen entering the gas-
ifier bed as air and flue gas as a
percentage of the stoichiometric
oxygen needed to fully combust the
fuel.
Sulphur Removal Efficiency
_,, _ S02 Observed in flue gas
        S02 if none absorbed
                                                       )x  100%
Oxidation of a bed of lime containing
carbon and calcium sulphide, resulting
in a bed containing lime and calcium
sulphate only under controlled temp-
erature conditions such that no SO
is released by regeneration of the
bed.

Operation at high excess air levels
during combustion in the gasifier
such that the gasifier temperature
remains at the required level  (Air
supply about 400% of that needed to
fully combust the fuel).
                         Micron
        (10 6 metre)
                               -  592  -
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VIII REFERENCES

1.   Study of Chemically Active Fluid. Bed Gasifier for Reduction
     of Sulphur Oxide Emissions.
     Final Report Contract CPA 70-46.  June 1972.

2.   EPA-650/2-74-109.  November 1974.

3.   EPA-650/2-73-048-d.  December 1973.

4.   D.L. Keairns et.aJL., Fluidised Bed Combustion Process
     Evaluation.  Westinghouse Research Laboratories,
     Pittsburgh.  Report EPA-650/2-75-027-b.  1975.

5.   R.W. Cox. et.al. , J. Inst. Fuel, 498 (1967).

6.   M.L. Hoggarth, Inst. Gas Eng. Journal,  285  (1965).

7.   G.L. Johnes f^t.ad., CAFB process for removal of sulphur
     during gasification of heavy fuel oil.   Esso Research
     Centre, Abingdon.  Report EPA-650/2-74-109.  1974.

8.   R.H. Borgwardt, R.S. Harvey, Environ. Sci. Technol.
     350, 6_, (1972) .

9.   M. Hartmann, W. Coughlln, Ind. Eng. Chem. Process
     Des. Develop., 248, 13,  (1974).

10.  G. Moss, Institute of Fuel Symp. Ser. No.l:  Fluidised
     Combustion, London.  1975.

11.  J. Szekely, J.W. Evans, Chem. Eng.  Sci.,  1901, 26, (1971)

12.  R.L. Pigford, G. Sliger, Ind. Eng.  Chem., Process Des.
     Develop., 85, 12, (1973).

13.  D.L. Keairns et.a_l. , Westinghouse Research Laboratories,
     Pittsburg.   61st. and 62nd. Monthly reports to EPA on
     contract 68-02-0605.

14.  W.F. Bischoff, P. Steiner, Chem. Eng.,  74  (1975).

15.  R.S. Boynton, Chemistry and Technology  of Lime and
     Limestone,  1966  (Interscience Publishers).

16.  G.P. Curran, C.E. Fink, and E. Gorin.
     Phase II Bench-Scale Research on CSG Process, R&D
     Report No.  16.  Report to Office of Coal  Research,
     Contract No. 14-01-O001-415, Consolidation Coal Co.
     July 1st,  1969.

                            - 593 -
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                         IX INVENTIONS


1.   US 551786      J.W.T. Craig, E.P. O'Neill, D.L. Keairns

     A process for reacting spent lime from the CAFB with air
     to oxidise calcium sulphide to calcium sulphate followed
     by reaction of the remaining calcium oxide with C02 to
     form calcium carbonate.

2.   US 551788      J.W.T. Craig

     The inerting of spent lime from the CAFB by exposure to
     temperatures sufficiently high to sinter the stone sur-
     face and render it relatively inert to reaction with the
     elements.

3.   UK 16145/74    J.W.T. Craig
     US 562080

     A process for reacting S02 from the CAFB regenerator
     with fine particles of spent lime to form calcium
     sulphate.

4.   UK 47152/74    G. Moss

     Fuel injectors are protected from exposure to hot bed
     material in extensive fluid beds by contouring the
     heights of air distributor nozzles to allow zones of
     slumped bed through which the fuel injectors pass.

5.   UK 53536/74    G. Moss

     A slurry of water and waste lime from the CAFB regener-
     ator is used to scrub SO2 from the regenerator off gas,
     part of the slurry being recycled and part concentrated
     by settling, the settled material being dried by in-
     jection into a hot agglomerating fluid bed, and dumped
     when agglomerated to an adequate size.

6.   UK 55373/74    G. Moss

     Coke deposits formed in cyclones and ducts downstream
     of a CAFB gasifier are removed by elutriating  abrasive
     particles in the gas stream leaving the fluidised bed.
     The particles scour the ducts and cyclones and are
     retained by the cyclones for return to the gasifier
     bed.

                              - 594 -
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7.    UK 10277/75    J.W.T. Craig, G.L. Johnes, G. Moss

     Tar and coke deposits in ducts and cyclones upstream of
     a CAFB product gas burner are removed by a sliding air
     supply duct which closes off the gas supply to the
     combustion furnace (e.g. boiler).  Air is supplied to
     the gas supply chamber in the burner so that deposits
     are ignited starting at the burner and proceeding back-
     wards down ducts and cyclones to the gasifier.

8.    UK 10731/75    G. Moss

     Fuel oil is injected into the regenerator bed of a large
     CAFB gasifier adjacent to the transfer point from the
     regenerator to the gasifier.  This improves the desulph-
     urisation efficiency of the unit and reduces residual
     calcium sulphate to S02 or elemental sulphur.
                              - 595 -
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                                TECHNICAL REPORT DATA
                         (Please read Instructions on the reverse before completing)
 . REPORT NO.
 EPA-600/2-76-248
       2.
                                  3. RECIPIENT'S ACCESSION NO.
4. TITLE ANDSUBTITLECHEMICALLY ACTIVE FLUID-BED
 PROCESS FOR SULPHUR REMOVAL DURING GASI-
 FICATION OF HEAVY FUEL OIL—THIRD PHASE
                                  5. REPORT DATE
                                   September 1976
                                  6. PERFORMING ORGANIZATION CODE
7.AUTHOR(S) j. w.T.Craig, G.L.Johnes, Z.Kowszun,
 D. Lyon, L.S.Malkin, G. Moss, O.R. Priestnall, and
 D.E  Tisdall
                                  8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
                                                      10. PROGRAM ELEMENT NO.
Esso Research Centre
Abingdon, Oxfordshire
England
                                  1AB013; ROAP 21ADD-BE
                                  11. CONTRACT/GRANT NO.
                                  68-02-1359
12. SPONSORING AGENCY NAME AND ADDRESS
 EPA, Office of Research and Development
 Industrial Environmental Research Laboratory
 Research Triangle Park, NC  27711
                                  13. TYPE OF REPORT AND PERIOD COVERED
                                  Phase; 7/73-9/75	
                                  14. SPONSORING AGENCY CODE
                                   EPA-ORD
is. SUPPLEMENTARY NOTES JERL-RTP project officer for this report is S. L. Rakes, Mail
Drop 61. 919/549-8411 Ext 2825. Previous EPA report on this work is EPA-650/2-
74-109 (NTIS PB 240-632/AS).  	
16. ABSTRACT
              repor|. describes the third phase of studies on the CAFB process for
desulfurization/gasification of heavy fuel oil in a bed of hot lime. Major conclusions
relating to process performance and oper ability are: (1) water, either in the fuel or in
the fluidizing air, has a strongly adverse effect on desulfurizing efficiency; (2) good
desulfurizing efficiencies are obtainable at very low stone replacement rates;  (3)
process performance can be expressed as a statistically derived equation;  (4)  a burn-
back burner is feasible for coke removal; (5) SO2/stone disposal by sulfation is not
feasible, but dead-burning looks promising; and (6) most trace elements are retained
in the bed. Among tasks included in this phase were: (1) batch reactor evaluation of
three limestones and gasification/desulfurization  of a vacuum bottoms fuel; (2) two
pilot plant runs using deep beds and demonstrating improved  operational techniques;
(3) development of a statistical method for analyzing results of the two pilot plant test
runs and reconciling them with earlier results; (4) sulfation of bed material as a means
of disposing of SO2 and spent lime; (5) dead-burning as a means of treating spent bed
material prior to disposal; (6) retention of the bed material of a wide range of trace
elements contained in the fuel; and (7) demonstration of a burn-back burner to over-
come coke lay-down in cyclone inlets.
17.
                             KEY WORDS AND DOCUMENT ANALYSIS
                DESCRIPTORS
                                          b.lDENTIFIERS/OPEN ENDED TERMS c.  COSATI Field/Group
Air Pollution
Fluidized Bed
    Processors
Regeneration
    (Engineering)
Sulfur
Des ulfurization
Gasification
Fuel Oil
Calcium Oxides
Limestone
Air Pollution Control
Stationary Sources
CAFB Process
Chemically Active
  Fluidized Bed
Fluidized Lime Bed
Heavy Fuel Oil	
13B
13H
2 ID
        08G
                                               07B
                                               Q7A.07D
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