ROBERT A. TAFT WATER RESEARCH CENTER
                       REPORT NO. TWRC-10
          MATHEMATICAL MODEL
                    OF
     SEWAGE SLUDGE FLUIDIZED BED
    INCINERATOR  CAPACITIES  AND COSTS
     ADVANCED WASTE TREATMENT RESEARCH LABORATORY-X
    U.S. DEPARTMENT OF THE INTERIOR
FEDERAL WATER POLLUTION CONTROL ADMINISTRATION
              OHIO BAS/N REG/ON
               Cincinnati, Ohio

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                          ERRATA SHEET
Page 3
     Add "HF - Height of freeboard"

Page 9
     After equation (6) add
     "Where PVS is the weight of volatile solids in the sludge"

Page 9
     After equation (7) add
     "Where PH2(j) is the weight percent water in the sludge"

Page 10
     The equations at the top of the page should read
     QSL = QS(P^)VS)/PS                (13)
     and                 _
     AIRCP = 4.76 (XF+Y)(M)(C )(T)

Page 10
     After equation (15) add
     "Where QFU is the higher heat of combustion of fuel"

Page 10
     Equation  (21) should read
     "THCP = SUMQ/PS
     Where SUMQ has the units of BTU and THCP has the units of
     BTU/lbs sludge"

Page 11
     The first sentence should read
     "The fuel rate and thus heat  input to the incinerator are
     adjusted by means of the mole multiplier FM"

Page 11
     In the section entitled "Limitations of the Theoretical
     Determination of BAF and QF", paragraph 1, delete second
     sentence.  Third sentence should read:  "When complete
     combustion equations are applied to data derived from an
     elemental analysis, an exact  calculation of the air
     required  for combustion is attainable".

Page 11
     Second paragraph should read:  "The heating value of a sludge
     could be  calculated based on  elemental analysis.  A bomb
     calorimeter could be employed in the laboratory to obtain
     the actual heating value (QS).  Because of the unavailability
     of data no attempt was made  to calculate QS in the computer
     program".

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                              - 2 -
Page 11
     Paragraph 4, line 5, change the word "Three" to "Two".

Page 11
     Paragraph 4, line 9, change the word "fourth" to "third".

Page 12
     Paragraph 3, second sentence should read
     "The maximum heat rate (BTU/hr) that can be obtained from
     the exhaust products without causing undue condensation is
     when the exhaust products are cooled from 1400°F to 400°F
     in the preheater.  The heat transferred per hour is
     PC, . (aEMcaP)                  (Z7)
Page 13
     Equation (30) should read
     "SUMS = (QSL + QFP + QL)CAP      (3O)
     where SUMQ in equation (30) is the heat input to the reactor,
     BTU/hr and QL is the heat loss from the reactor which must be
     generated by the heat of combustion, BTU/# Sludge.

Page 13
     Paragraph 4, delete the last sentence.  Add in its  place the
     following sentence:  "All incinerators have the same sand
     depth within reasonable limits (approximately 5 to  6 feet
     static level)".

Page 16
     In paragraph following equation (38), second sentence, delete
     "somewhat" .

Page 24
     In the section entitled "Sand Loss Rate" add at the end of the
     first paragraph:  "The sand that was used during the course of
     this study was obtained from a local supplier with  the require-
     ments that the sand have a high resistance to abrasion and
     fluidize at reasonable air flow velocities through  the grid."

Page 45                                           ,
     In the section entitled "Reactor Sizing Limit ", add footnote
     to read:  "Dorr-Oliver has informed the authors that they have
     industrial calciner units in operation with diameters of 45
     feet" .

Page 61
     Delete section entitled "Method of Rating" .

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                           - 3 -
Page o 7
     Delete SUNKJ and its defination and substitute
     "SlMJ = Total heat content of exhaust products based on
             specific heats,  BTU for page 10, equation 21.
      SUM3 = Total heat input to reactor, BTU/hr for page 13.
             equations 30 and 31"

     Add to the defination of the term THCP:
     "where SUMQ is obtained from page 10, equation 21".

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MATHEMATICAL MODEL OF SEWAGE SLUDGE FLUIDIZED

     BED INCINERATOR CAPACITIES AND COSTS
                    by


          G. J. Ducar and P. Levin



                    for


The Advanced Waste Treatment Research Laboratory

      Robert A. Taft Water Research Center
           This report is submitted in
           fulfillment of Contract No.
           1U-12-U15 between the Federal
           Water Pollution Control Admin-
           istration and General American
           Transpoitation Corporation.
        U. S. Department of the Interior

 Federal Water Pollution Control Administration

              Cincinnati, Ohio


               September, 1969

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                           FOREWORD
     In its assigned function as the Nation's principal na-
tural resource agency, the United States Department of the
Interior bears a special obligation to ensure that our ex-
pendable resources are conserved } that renewable resources
are managed to produce optimum yields , and that all resources
contribute their full measure to the progress, prosperity,
and security of America — now and in the future.

     This series of reports has been established to present
the results of intramural and contract research studies car-
ried out under the guidance of the technical staff of the
FWPCA Robert A. Taft Water Research Center for the pqrp
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                    TABLE OF CONTENTS

                                                          PAGE


FOREWORD

ABSTRACT

INTRODUCTION                                                if

DESCRIPTION OF SYSTEMS ANALYZED                             3

     Terminology                                            2

     System Components and Operation                        3

METHOD OF APPROACH                                          6

     Information and Data Gathering                         6

          Literature Survey                                 6
          Manufacturers' Survey                             6
          Field Survey                                      °

RESULTS                                                     7

     Data Collected                                        7

     Equations Developed                                   7

          Theoretical vs. Pilot  Plant  Data                  7
          Limitations of the Theoretical
              Determination,of BAF  and  QF                   J-B
          Air Preheater Sizing                             13
           Sizing  the Reactor                               ^
           System  Power  Requirements                         2^
           Sand Loss Rate                                   2f*
           Carbon  and Hydrogen Content  of Fue^s.             24

      System Costs                                          2^

           Cost Structure                                   ?T
           System Cost Less  Air Preheater                   26
           Air Preheater Cost                               30
           Total Equipment Cost                             30
           Installation Fee                                  30
           Consulting Engineers'  Fee                        33
           Total System Cost                                33,
           Air Preheater1 Fuel Savings                       33
                     iii

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                          TABLE OF CONTENTS (CONTINUED)

                                                                    PAGE

          Annual Operating Cost                                      33
          Annual Maintenance Cost                                     3^
          Annual Operating and Maintenance Cost                       35
          Scrubber Costs                                             35
          Cost of Installations                                      37

COMPUTER PROGRAM                                                     39

     Listing of Program                                              39

     Flow Chart                                                      1*3

     How to Use the Computer Program                                  kk

          Options in the Selection of Input Data                     kk
          Reactor Sizing Limit                                       45
          Air Preheater Option                                       U5
          Data Input and Output                                      U5

CONCLUSIONS AND RECOMMENDATIONS                                      6l

     Performance of the System                                       6l

     Method of Rating                                                6l

     Factors Influencing Operating Costs                             62

     Accuracy of the Equations Developed                             62

     Lime Recalcination                                              62

TERMINOLOGY                                                          63

REFERENCES                                                           68

BIBLIOGRAPHY                                                         69

PATENTS FOUND ON FLUIDIZED BED INCINERATOR EQUIPMENT                 72
                            IV

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                                  ABSTRACT
     This report describes the development of a computer program to evalute
sewage sludge fluidized bed incineration systems.  Data for the program was
collected from manufacturers, a literature survey and field trips to operating
installations.  Most of the data was obtained from the field because of the
lack of available information from the other sources.

     More than fifty correlation relationships were attempted before the
necessary data could be reasonably represented.  Equations were developed for
the least square curves which fitted the data best.  These equations were
used as the basis for the computer program developed to size some of the
major components and to estimate capital, operating and maintenance costs
for the fluidized bed incineration system.

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                                   INTRODUCTION


     Domestic and industrial sewage wastes ar ; mixed with water and piped Lo
a sev/age treatment plant.  To reclaim and purify the water mixed with the
sewage, many processes can be used.  When attempts are made to separate the
suspended solids from the water (dewatering), only a portion of the separa-
tion can "be achieved.  The resulting effluents from the dewatering device
are a stream of turbid water and a stream composed of approximately IVJo
water and 30$ solids by weight (sludge).  This sludge must be disposed of in
some sanitary way (ultimate disposal).

     The cost of the ultimate disposal of solids generated at waste water
treatment plants can amount to 25 to 50$ of the construction and operating
costs of an entire waste treatment plant.  Incineration of this sludge reduces
the volume of wastes to be disposed of by approximately 9°& &nd produces ash
and flue gas.  Incineration is often the only method available to dispose of
sludge.

     A recently developed incineration technique uses a fluidized bed qf inert
material capable of completely oxidizing all the organic material in the sludge.
This technique is based on the principle, long used for processing in the
chemical industry, that when solids are suspended in an upward-moving stream
of gases, the mixture possesses the characteristics of a liquid.  The properties
of this fluidized bed in terms of mixing and heat transfer can be utilized to
effect both rapid mixing and almost instantaneous incineration of the organic
material in sludge.

     The purpose of this study was to develop a mathematical model of fluidiaed
bed incinerators for burning sewage sludge.  The model was to be composed of
equations which represented the incineration equipment and process.  Such a
model would help FWPCA determine approximate sizing of the principal reaction
vessels and associated equipment, the amount of fuel and power required, and
estimates of the capital, operating, and maintenance costs for fluidized bed
incineration systems to be funded.  The necessary equations were developed
from data obtained in the literature, and surveys conducted at equipment
manufacturers plants and in the field.

     It was not possible to obtain itemized cost breakdowns for each of the
system components.  Therefore, capital costs were developed on a systems
basis:

     1)   The system costs developed in this program include the components
of Figure 2.

     2)   The stream vector required for input to this program is to repre-
sent the sludge cake leaving the centrifuge.

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                       DESCRIPTION OF SYSTEMS ANALYZED
Terminology
     A schematic of the reactor or combustion chamber which is the heart of
the fluidized bed incineration system is shown in Figure 1 which illustrates
the parameters related directly to the reactor and the various regions of the
reactor.  The lower section of the reactor consists of an air plenum and a
grid for sand support.  Above the grid is the sand bed (tapered portion of
reactor).  When air is blown through the sand, it is fluidized (thus expanding
the sand).  The section above the expanded sand bed is termed the area free-
board.  The terminology shown in Figure 1 is specifically related to the
reactor vessel.  However, this program required a more comprehensive system
analysis.

System Components and Operation

     The system components included in this study are shown in Figure 2, which
illustrates the complete fluidized bed incineration system usually purchased as
a package.  This system was used as the basis for including equipment in the
study because cost data collected included all of the components, as a group,
as shown in Figure 2.  The waste feed and dewatering system usually consists
of centrifuges, belt conveyors and a screw feeder at the reactor.  Since it was
not possible to get costs for the individual components, it was necessary to
develop cost information for the total system.

     Sludge is dewatered in a centrifuge or vacuum filter.  Costs developed
for this program are based on systems using a centrifuge.  The sludge cake is
conveyed directly into the reactor by means of a special screw feeder.  Some-
times the screw feeder is connected to flexible reinforced ducting through
which the sludge is conveyed, to the reactor.  Air from the blower is passed
into a plenum and through a sand-bed supporting grid.  This grid also serves
to distribute the air so that fairly uniform fluidization  of the sand occurs
above the grid.  The sand bed is maintained at temperatures between 1220° and
l800°F.  (The exact maximum and minimum temperatures attainable are determined
by the temperature at which essentially complete combustion occurs.)  Bed
temperature is controlled by fuel regulations, water sprays, and excess air
flow.  The sludge is burned almost completely in the bed, but because of the
mixing characteristics of the fluidized bed, there is considerable burning
above the sand bed in some instances.  Therefore, in some instances, the
above-bed temperature in the freeboard area may be several hundred degrees
higher than the bed temperature.

     The freeboard serves to keep the sand from being carried out of the
reactor with the exhaust products and also serves as a secondary combustion
chamber.  The exhaust products leave the freeboard section and pass through
an air preheater (if one is used).  The gases are then cooled to approximately
l£0°F by a water spray before entering the scrubber where the fly ash and
small sand particles, carried out of the reactor with the flue gas, are
removed from the gas stream.

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                                                          TO STACK
          A)K  SUPPLY'—0
ORH - Overall Reactor Height
 VE - Volume Expanded
 VS - Volume Static
 EOT - Diameter Freeboard
 AF - Area Freeboard
DS - Diameter Static
HS - Height Static
AG - Area Grid
DG - Diameter Grid
HP - Height Plenum
HE - Height Expanded
               Figure 1   REACTOR TERMINOLOGY

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     The warmup burner,  shown at the side of the freeboard in Figure 2,  is used
to preheat the reactor to 1000°F before the bed burners are ignited.  Alterna-
tively, the preheat burner may be located in the plenum to preheat the incoming
combustion air.  The warmup burner is usually extinguished when the bed burners
are ignited.

     The air supply is controlled so that approximately ^ Op is present in
the exhaust gases.

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                                                                            S  PUANT

                                                                              ^S- CENTR1FU&E
                                                                            '••— CENTRATE
                                                           WASTE  PS.E.D  ^
                                                    f  DEVWATERIWG.  SYSTEM
                                                    V^
                                                       SCREW  FEEDER
                                         PLE.WUV*
BL.fl \AJCR.
                                        Figure 2

              SYSTEM   COKAPCIWEMTS   IMCLUOEO  ^^«J

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                              METHOD OF APPROACH


     As the initial step in this program,  it was necessary to secure complete
representative data on the fluidized bed incinerator.   The procedure used is
described below.

Information and Data Gathering


     Literature Survey

     A review of the literature revealed that the first fluidized bed inciner-
ator in the U.S.A. was installed in 1962 in Lynwood,  Washington.   Information
was also available on one or two other installations;  however,  it soon became
apparent that there was insufficient information available in the literature
to generate a model.  However, since about 30 new installations were either
recently placed on stream or were in the design stage, a survey of equipment
manufacturers was initiated.

     Manufacturers Survey

     A letter of inquiry together with an information sheet was directed to
manufacturers advising that we were engaged in an FWPCA program and requesting
cooperation in securing the necessary information.  Very little data were
obtained from manufacturers.

     Field Survey

     At this point, it became apparent that the necessary information could
only be obtained from field installations.  Since a number of installations had
been financed under the construction grants program of FWPCA, visits were made
to selected FWPCA regional offices to secure design and cost data from plans
submitted for a construction grant.  Visits were made to regionel offices in
Chicago, Kansas City, Boston, San Francisco, and Edison, N. J.

     Subsequently, visits were made to treatment plants selected on the basis
of capacity, location and period of operation:  Sheboygan, Wisconsin; Kansas
City, Kansas; Bars tow, California; Port Heuneme, California; East Cliff,
Sanitary District, Santa Cruz, California; Foster City, California; Fairfield
Suisan City, California; Liberty, New York; Hazelton,  Pa.; and Pleasantville,
N. J.

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                                   RESULTS


Data Collected.

     A summary of the data collected during the field survey is presented in
Tables I and II.

     The equipment sizing and cost data are very reliable since they were
obtained from visual inspection or files.  However, the data for operating
costs (fuel consumption, power consumption, operator costs,  etc.) were not
readily available, since accurate operating records were not generally main-
tained at the plants.

     Since the plants surveyed were purchased at different times, a standard
cost reference date of February, 1968 was chosen for this program.  All unit
prices were corrected to February, 1968 prices, using the Department of the
Interior cost index for sewage treatment plant costs as  presented in the
Engineering News-Record Magazine.

Equations Developed

     Equations were developed from this data and an FWPCA report (Reference 1).
The data were plotted using various correlations; least square curves were
plotted using least squares fit equations generated by computer.

     Obviously, not all of the correlations attempted were successful.  Many
were discarded and equations were developed for only the best correlations
found relating the variables of interest.

     Theoretical vs. Pilot Plant Data

     The fuel needed to raise sludpe r-ombustion products to a selected tem-
perature can be determined from either theoretical calculations or pilot
plant data.  Note that in the discussion below, # indicates pounds and refers
to  the weight of  solids plus water in the sludge cake (dry solids are referred
to  as PDS).

     The variables needed for fuel rate determinations are:

     1)   BAF  =  combustion air required @ h% excess 02, # air/# sludge

     2)   QF    =  required heat from fuel, Btu/# sludge

     3)   QLE   =  heat  loss from  pilot equipment which fuel must  supply
                  (zero for theoretical calculations), Btu/# sludge

     U)   QPE   =  heat  supply to  the combustion air by air preheater  in
                  pilot plant tests  (zero  for  theoretical calculations),
                  Btu/# sludge.

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 PAGE NOT
AVAILABLE
DIGITALLY

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     Pilot plant data are more accurate than theoretical data for the above variables
for reasons explained in the next section.

     The procedure for calculating BAF and QF follows.   Given the elemental
composition of the sludge volatile solids the complete'combustion equation
for stoichiometric conditions is: (Note:(c) represents elemental carbon whereas
C represents the moles of 0p required for stoichiometric combustion of the
sludge volatile salads)

               sludge volatile solids
     A1(C)  +  B1(H2)  +  C(02)  +  D(N2)
               Fuel
                 V
     f

     FM  [
               Sludge Air                    Fuel Air


                                      )  +  3-76F (N)
                   Combustion Products


    'A3(C02)  +  B3 (H20)  +   [D  +  3.76 (X + F) ]   (HI,)'           (D

where (X_+ F) = XF by the terminology chosen.   In this discussion X is the,
moles of 0p required for stoichiometric combustion of the sludge and F is '
the moles of 0p required for stoichiometric combustion of the  fuel.   Note
that the sulphur content of the sludge has been neglected since its heat of
combustion is usually negligible.

     From equation (l) the moles of C0p in the exhaust is given as

                  A3  =  Al  +  FM (A2)                                 (2)

and the moles of water in the exhaust due to the combustion of the H_
in the volatile solids arid fuel is

                  B3  =  Bl  +  FM (B2)                                 (3)

     The value of X + F now redefined as XF is determined from equation
(1) as

                  XF  =  A   4  B /2.0  -  C
                                      8

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     The pounds of volatile solids under consideration above  is  given  by

             P0VS  =  12.0^)  +  2.0(B )  +  32.0(C)  +  28.0(D)      (5)

and the volatile solids plus the inert solids gives  the pounds of dry
solids under consideration as

                  PESC  =  P0VS/(PVS^LOO.O)                            (6)

Therefore the pounds of sludge (dry solids plus vater) under  consideration
is

             PS  =  100.0 (PE6C/(100.0 - FH20) )                       (7)

and the pounds of water under consideration is

                  PFH20  =  PS - PD6C                                  (8)

     If the combustion products given "by equation (l) are added  to  the
water content of the sludge given by equation (8) the total moles of the
combustion products for the stoichiometric mixture for the volatile solids
under consideration is

             PVT  =  A   +  B   +  D  +  3-?6(XF) +  PPH20/18.0       (9)

vhere PPH20/18.0 is the moles of water in the sludge.   Note equation (9)
neglects the inert solids which remain in solid form and contribute little
to the total exhaust volume.

     The operation of a fluidized bed incinerator is adjusted so that  about
k% excess oxygen exists in the flue gas.  To accomplish this  concentration
of oxygen, the moles of excess oxygen (Y) which mast be added to the supply
air is derived as follows.  Four percent excess oxygen is defined as

                  0.0^  =  Y/(PVT  + 4.y6(Y))

where lt.?6(Y) is the total moles of air for Y moles  of oxygen.   Solving this
equation for Y yields

                  Y  =  O.Ol* (PVT)/.8096                               (10)

Then the total moles of the exhaust products at k percent excess oxygen is

                        =  PVT  +  ^^(Y)                            (11)
     The heat transported into the incinerator by the sludge is in two forms:
the heat contained in the mixture (using 0°F enthalpy base)  and the higher
heat of combustion.  The heat contained in the sludge entering the incinera-
tor is

                  SCP  =  PS (1.0 Btu/# °F) (60°F)                    (12)

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assuming the sludge specific heat as 1.0 and an inlet temperature of 60°F
the higher heating value of the sludge (OS) is given in Btu/# volatile
solids.  Therefore the higher heating value of the sludge Btu/# sludge
containing a given percent of volatile solids (PVS) is

                  PSL  =  OS (PJ0VS)/FS                                 (13)

     The heat content of the air entering the incinerator is

                  AIRCP  -  I*.?6 (XF  +  Y)  (M) (Cp) (T)

where M  =  molecular weight of air (28.9)

      C  =  specific heat of air (0.2k Btu/#°F)
       P
      T  =  temperature of air assumed as 60°F.

     Substituting the indicated values yields

                  AIRCP  =  1980.0 (XF  +  Y)                          (1*0

     Therefore the total heat supplied to the incinerator per pound of sludge
is given by

        THCPT  =  QSL  +  QFU (FM) (12.0 Ac  +  2.0 B0)  +  AIRCP  +  SCP/PS
                                          2          d                 (15)

     Next the total heat content needed to raise the exhaust products to
1^00°F will be derived.  The temperature of ltoO°F was selected because the
minimum operating temperature for fluidized bed incinerators is around
1300°F and a slight safety factor is desirable to assure sufficient odor and
bacteria control.  The heat content of the C0  , H^, BL, 0_ and inerts in the
lIj-00°F exhaust products from the volatile solids considered in equation (l)
and  resultant sludge are respectively listed below in the general form.

        CPC20  =  (moles)(molecular weight)(specific heat at lUoO°F)(lUoO°F)

        CPC20  =  A  (lA.O)(0.295)(ltoO.O)                             (16)

        CPH20  =  (B3  +  PPH20/l8.0Xl8.oX0.555)(l^OO.O)             (17)

        CP2N   =  (3-76(XF  +  Y))(28.0X0.279X1^0.0)                (18)

        CP20   =  Y (32.0X0.263X1^00.0)                              (19)

        CPIW   =  (PDSC  - POVS)(0.2U)(lUOO.O)                          (20)a-

      If the sum of equations  16,  17,  18,  19 and 20  (SUMQ) is divided by PS, the
heat content of the exhaust products  per  pound of  sludge (THCPT)  is determined.

                  THCPT  =  SUM3/PS                                    (21)

 a. Specific heat  is approximated by using data from Reference 46.
                                      10

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     The fuel rate and thus heat input to the incinerator adjusted by means
of the mole multiplier FM.  When the thermal balance is reached between the
heat input to the incinerator and the heat content of the exhaust products
the variables BAF and QF can be evaluated from the equations developed above.
Thus since

        BAF  =  (moles air required)(air molecular weight)/PS

        BAF  =  k.rf (XF  +  Y)(28.9)/PS                               (22)

and

        OF   =  (moles fuel)(fuel molecular weight)(fuel heating value)/PS

        QF   =  FM  [12.0 A2 + 2.0 Bg]  QFU/PS                         (23)

     Limitations of the Theoretical Determination of BAF and QF

     An elemental analysis of sewage sludge volatile solids does not identify
the various compounds containing these elements.  This analysis would be
extremely difficult to obtain.  Therefore, when complete combustion equations
are applied to data derived from an elemental analysis only an approximation
of the air required for combustion is attainable.  This is because the carbon
may exist as C, CO, CO^, CO  and the combustion equations for these composi-
tions would each yield different air requirements.  Thus it is anticipated
that the theoretical analysis set-up to determine BAF will yield a slightly
higher than actual value for most sludges.
     In addition the heating value of a sludge could be calculated based on
the elemental analysis.  However, the result would be in error for the same
reasons given above.  Therefore, since an elemental analysis must be obtained
in the laboratory it is a simple matter to also perform a bomb calorimeter
test  on the sludge to determine the actual higher heating value (QS).  Because
of the availability of the data no attempt was made to calculate QS in the
computer program developed.

     Air Freheater Sizing

     The economics of operation will  partially depend on the quantity of fuel
required to incinerate the sludge,  an air preheater can be used to reduce
the quantity of fuel required.  The equations developed below allow the
sizing of the air preheater so that a heat balance exists between the
exhaust products and incoming air.  Three restrictions placed on design are
that the exhaust product temperature is 11<-00°F entering the air preheater
and no less than ^00°F leaving the preheater, and the air temperature leaving
the preheater is held to 1000°F or less.  These restrictions are based on
the field data obtained and presented in Table I and II.  A fourth restric-
tion is that the total heat transfered in the air preheater cannot exceed
that required from fuel and/or preheat in the pilot test or calculated
theoretical fuel.
                                      11

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     The derivation proceeds as follows.   An air flow rate of BAF entering
the air preheater at 60°F has a heat content of

     QAIR  =  BAF (0.21* Btu/#°F)(60°F)  =  15-0 BAF                    (23-a)

     At l400°F the exhaust products Have a heat content of

     QE  =  QSL  +  QF  +  OPE  +  QAIR - OLE                         (2k)

based on the equations 1 through 23.

     An air preheater can transfer a quantity of heat into the supply air
as long as this heat input does not exceed that determined from pilot tests
or calculations as

                  QFP  =  QF  +  QPE                                   (25)

     For a unit vith no air preheater the fuel cost is

     CF  =  FC (QFP) (PCTY) (8750.0) (cAp)/io6                         (26)

where 8750.0 is the number of hours in one year.  If the exhaust products
are cooled from lUOO°F to 400°F in the preheater the heat transfered per
pound of sludge is
                  PC,  -  « (CAP) C,:,-)                    (27)
Thus PC  is seen to represent the allowable heat which can be removed from the
flue gas without causing undue condensation of the water in the flue gas.
Condensation prevention is assured by holding the flue gas temperature
around tOO°F.  The heat removed from the flue gas (PC ) is transfered to the
incoming combustion air.

     To heat the incoming air from 60°F to 1000°F the air preheater would
have to transfer

                  PC2  =  BAF (0.210 (1000.0 - 60.0)                   (28)

where 0.24 Btu/# °F is the specific heat of air assumed as constant over the
temperature range.  The allowable air preheater heat transfer per pound of
sludge is the lower of PC , PCg and QFP thus

                  APHS  =  PC  or PC2 or QFP                           (29)

whichever value is lowest.  Note that this is the maximum heat transfer rate
(and thus fuel saving rate) possible for the particular system.
                                     12

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     Sizing the Reactor

     The total heat release rate in the reactor is given by

                  SUMQ  =  (QSL  +  OFF) CAP  +  QL                    (30)

vhere QL Ls the heat loss rate from the reactor which must be generated by the
heat of combustion.  Figure 3 shows the best correlation found relating the
grid area to the total heat release in the reactor namely

                  AG  =  SUMQ/155>000.0                                (31)

This starting point was chosen because the heat release in an incinerator
is closely related to the volume of the combustion chamber.

     This correlation was obtained by omitting ("discounting") the data for
the early units.  Note that location 10 is shown as quoted insulation and
Hazelton insulation.  The point labeled "quoted insulation" was based on the
grid sizing obtained from the firebrick thicknesses stated by plant personnel.
The point labeled "Hazelton Insulation" was based on the refractory thick-
ness known to be installed at Hazelton, Pa.  Since the Hazelton unit was
roughly the same size as those at Kansas City it seems likely that the
refractory thickness would be very close for each of the units.

     If the bed is considered as  isothermal with combustion occurring near
the lower portion of the bed the ratio of AF/AG would be 1.0 as shown in
Figure 4 (assuming zero percent water content in the sludge).  As water
content of the sludge increases the expansion ratio AF/AG must be increased
if gas velocity is to be maintained within tolerable limits at the top of
the bed.  This is because the volume of combustion products per pound of
sludge increases when vaporization of the water and subsequent increases in
fuel and air requirements occur.  For practical purposes the ratio AF/AG
cannot be allowed to increase beyond reason because of construction costs.
Therefore an upper limit of AF/AG = 3 was arbitrarily chosen for 100$
water conditions.

     The combustion chamber for a fluidized bed is tapered so that the
upper cross-sectional area at the freeboard  is larger than the cross-
sectional area at the grid.  Such a taper prevents acceleration of combustion gases
and thus limits sand loss and over-fluidization at the top of the sand bed.
This taper was also found to be related to the water content of the sludge
as shown in Figure k.(3) Therefore the volume of the expanded bed (combustion
chamber) is related to the grid area, sludge water content and sand bed
depth.  If the grid area is fixed then the sand bed depth is fixed for a
given sludge.

     Thus for design purposes either the grid area or bed volume could be
selected first.  The end result would be the same regardless of which
parameter was selected.
                                     13

-------
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                                                                                                   X 1967,  1968
                             1967       1966       1965
                                                                                             O  Preheat
                                                                                                          .    .

                                                                                            | Quoted  Insulation
First units built  "discount" 1961 to 196^
                                                                                                              io
                                                                                                        :Hazelton
                                  First preheat unit  "discount"
                                                                                                               Insulation
                                                                                                            4~r4rH    • •
                                                                                                          i
                                                                                            155000 Btu/Hour/ft  grid

                       10
                                                       50

                                                     Grid Area,  Ft"
                                                                                                             100
                                                                                                                110
                                                         Figure 3   GRID SIZING

-------
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-------
     From Figure k the freeboard area is found to "be

     AF  =  AG/ 0.985 - 0.307 ((PH20/100.0)2 - 0-339  (FH20/100.0)^)    (32)

where AF/AG = (HF/DCJ)2

     Figure 5 shows the correlation developed for the expanded bed volume
which yields

                  VE  =  SUMQ/18,000.0                                 (33)

Since the bed volume is an inverted frustum of a cone having a volume VE
the height of the frustum is given from geometry as
        HE
= VE/  1.C&7 (AF/PI  +  (AF/PI)1'2 (AG/PI)1'2   +  AG/Pl)    (3*0
     The diameter of the grid (DG) and diameter of the freeboard (DF) are
determined simply as

                  DG  =  (k (AG/PI))1/2                                (35)
                  DF  =  (4 (AF/PI) J                                   (36)

     The standard practice appears to be to fluidize the  sand bed until it
reaches a volume of approximately 1.5 times the volume of the static bed.
From this the static bed volume is determined as

                  VS  =  VE/1.5                                        (37)

     Figure 6 shovs the correlation obtained for the height of the free-
board (HF)

                  HG  =  1.6 (HE)                                      (38)

     Figure 7 is the best correlation found for determining the plenum
volume.  It seems reasonable since the combustion air requirements are
somewhat related to the heat release in the reactor.   The  resultant
equation relating the plenum volume to the total reactor  heat input is

                  PV  =  SUVR (2.5)/(lO)5                              (39)

Thus the plenum height (HP) is

                  HP  =  PV/AG

     The overall reactor height is obtained by adding equations 3^> 3
and 40 as

                  ORH  =  HE  +  HG  +  HP
                                     16

-------
    300
ITS

 O
 ft
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 ta
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  03
  -p
  o
•+•  Expanded bed volume

O  Static bed volume
         o   50  100  150  200 250  300   350   Uoo 450  500  550 600  650 700   750   800 850  900 iooo  1050 iioo
                                                                     •3.
                                                       Red Volume, Ft
                                                  Figure 5   SAND BED SIZING

-------
                              :  2 x Expanded bed depth
 Assumed expanded volume
i =  1.5  static volume
1967, 1968:
                                                                    *
                                                              1.6 x Expanded bed  depth

                                                               1 x Expanded: bed  depth

                                                     SSTSi
                       8         10        12
                     Expanded Bed Depth,  Ft

                    Figure 6   FREEBOARD  SIZING
                                                                      18

-------
co
                                                                  >— Plenum volume = 2.5 x Btu/Hour  x 10~'
                    Total Btu/Hour (Volatile Solids,  Preheat,  Fuel)  x 10




                                                      Figure 7   PLENUM SIZING

-------
     Neglecting the plenum the  outside  surface area of the  reactor where heat
is lost to the atmosphere is

        A0  =  PI (HG(DF)  +  HE(DF  +   DG)/2.o)                        (te)
                                                                     o
     Assuming a heat transfer convection coefficient of k.O Btu/hr-ft -°F,
the convection heat loss from the  outside surface of the  reactor is

                  QLL  =  k.O (A0) (TW  - TA)                            (1*3)

If the wall temperature (TW)  and ambient air temperature  surrounding the
reactor (TA) are not given, values  of

                  TW  =  200.0°F

                  TA  =   60.0°F

are adequate.  Note that the  radiation  heat loss is negligible  at wall tem-
peratures in the range of 200°F.   A well insulated reactor  should not have
wall temperatures in excess of  200°F because of the safety  hazard of receiving
burns.

     Figure 8 shows the correlation developed for determining the number of
sludge feed points installed  in the bed section of the reactor.   As the size
of the incinerator is increased it becomes necessary to feed the sludge into
the bed at several locations  around the periphery of the  bed to obtain full
use of the fluidized bed incineration capacity. Thus the  number of feed
points required is given by

                  MFP  =  100.0 (PDS)/2000.0(PCDS)                      (MO

where NFP is rounded off to the nearest integer.

     System Power Requirements

     The installed horsepower for  the fluidized bed incinerator,  based on
field data is presented in Figure  9 as

        HPI  =  15.2 - 0.0102^  (PVSH)   +  0.0001607 (PVSH)2            (^5)

This includes the power requirements for all components from the centrifuges
through the ash system.

     The fluidizing blower horsepower is included in the  installed horsepower
above.  However, it may be of interest  and it is plotted  in Figure 10.  The
representative equation is

        FBHP  =  -5-68  +  0.908'HPI -  0.000565 (HPI)                   (k6)
                                      20

-------
£
I!
      0      2000      ^000     6000     8000      10000
                 Pounds of Sludge Per Hour
                                      Figure 8   NUMBER OF REACTOR FEED POINTS

-------
    i Actual Measurement
„...,:-- ;j..;.i. :;.,;> -,.;-.::
          •r":fi:
                                       HP  =  15-2 - 0.0102U# volatile solids/hour + 0.0001607 (#v.s.
                                      200        250       300

                                      Installed Horsepower


                               Figure 9   INSTALLED HORSEPOWER
koo

-------
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                                                                             X  Fluidizing Blower H.P.
                                                                                Total Blower H.P. = -5.68 -»•  O.TOU H.P.
                                                                                                              HOI
                                                                  _®,x  Data
                                                       A Fluidizing  Blower  H.P.  = -5.68 + 0.908 H.P.T - 0.000565  (H.P. )
            UO
            20
                                          150       200      250

                                            Installed Horsepower
                                                               300
350      koo
                                          Figure 10  BLOWER HORSEPOWER

-------
     The operating horsepower for  the  system was found to be

                  OHP  -  0.625  (HFI)                                   (47)

"based on the data obtained for locations  1 and 2 in Table,  I,  II.

     Sand Loss Rate

     Sand losses occur because of  non-uniform particle sizes cause by sieving
and attrition in the fluidized bed.  The  small particles are  carried out
more easily than the larger particles.  To fully fluidize the  bed a gas
velocity is required vhich will  fluidize  the large particles.   Since this is
too high a velocity to allow retention of the smaller particles the small
particles are gradually carried  out  the top of the bed.  This  sand  loss rate
can be reduced to reasonable levels  by providing a sufficient  freeboard height.

     A plot of field data gathered on  the sand loss rate from the bed caused
by carryover in the exhaust gas  is shown  in Figure 11.  The resultant equations
are

        SLR  =  (10350.0 (DF/HF  -  0.6)(PCTY) (8750.0)/30.0(8.0)) (ZIl) (48)

for

        (DF/HF  >  o.64) and

        SLR  =  (632.0 (DP) (PCTY)(8750.0)/30.0(8.0)(HF)) (ZIl)        (49)

for

        (DF/HF  <  o.64).

In the above equations where 8750.0  is the total hours in one  year, 30.0 is
the average number of days per month and  8.0 is the number  of  hours per day
the field units are operated.

     Carbon and Hydrogen Content of  Fuels

     Based on data obtained from major oil companies (Mobil,  American and
Sinclair) the ratio of the moles of  carbon to the moles of  hydrogen in
number two fuel oil ranges from  0.54 to 0.80.  For  the purpose of  this pro-
gram an average of the data collected  (determined as 0.6o)  was used for
the C/H ratio (i.e. 1.2 moles C  for  1  mole Hg).  For natural gas (CH^)
there is 1 mole of C for 2 moles of  Hp.

System Costs

     Cost Structure
     The costs developed for this program include  all  components required
                                      •24

-------

                                                  = 0.6 + 0.2/2070 (Sand  Loss,  #/month)
                                            (DF/HF > 0.6U)
DF/HF = O.U75/300 (Sand  Loss, #/month):
(#/month to
                                                                         Expanded
                                                                         Sand Depth
                DF  =  Incinerator inside diameter in freeboard
                HF  =  Expanded ( 50$) bed freeboard height
                   800     1000     1200      lUOO     1600     1800

                      Sand Loss Pounds Per Month (Carryover)
2000
                      Figure 11  SAND LOSS RATE

-------
for the fluidized "bed incineration system less the building and land re-
quirements.  The components included in the cost data are:

     l)  Comminuter

     2)  Sludge Pump

     3)  Dewatering Devices (centrifuge)

     *0  Waste Feed System

     5)  Reactor

     6)  Scrubber

     7)  Ash-Water Separation System

     8)  Air Preheater

The centrifuge is the only dewatering device included in the cost analysis.

     In addition to the basic system cost an installation fee of 10 percent
must be addeda   A Consulting Engineer's fee of 10 percent of the sum of
the System Cost plus installation fee must also be added.

     System Cost Less Air Preheater

     Figure 12 shows a plot of data -presented in Reference ^7.   An overlay
on this curve is shown representing the field data collected.   There appears
to be a significant discrepancy indicating that the manufacturers prices
quoted in Figure 12 are higher than the actual selling prices for this
equipment.

     Table III shows the data from which the field data curve was plotted.

     Since there was a significant difference in the cost data it was decided
to use both the manufacturers quoted prices and the field data prices in
the computer program for comparison purposes.

     It was found that the field cost was correlated more closely by relating
the cost to the capacity in pounds of volatile solids per hour.   This plot
is shown in Figure 13-
a.  Data from a conversation with Mr.  Stewart Peterson,  W.E.  Region Program
    Director,  F.W.P.C.A.,  Boston,  Mass.
                                      26

-------

w
TD
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fH
HI
ft
Td

EH
O
                                                                                   A -  A = 22$ TOTAL SOLIDS
                                                                                   LOG  COST = —
                                                                                                   LOG CAP.  -  1.64?
 ® - Units with air preheaters (not included in price)
 4t - Units without air preheaters.
(28) - Numbers indicate percent of total solids in sludge.
 11 - Other numbers indicate Installation location
      (Key to table I  ).
Points plotted using Engineering News-Record Dept. of Interior
Sewage Plant Cost Index for location  of installation and
include all equipment costs less air preheater.
All prices include centrifuges.
Prices do not include building stack,
installation or consultant engineering fee.
                                                                                   B -  B = Uof0 TOTAL SOLIDS
                                                                                                       1
                                                                                  LOG COST  =
  2.18 LOG CAP.  -
(Reference  1)
                                                                                                                    Jttti
                                                                                                                    T:
                                   400  900 t  1  • 9001000         2000     JOOO  4000 5COO 4  7 •  »  10000
                                      CAPACITY  (pounds  of  dry solids/hr)
   Figure' 12   FLUID BED COMBUSTION SYSTEM COSTS IN FEBRUARY 1968 DOLLARS - [dollars/( 100  pounds of dry solids/hr)]

-------
                                 TABLE III
                    DATA USED TO DETERMINE SYSTEM COSTS
Location
(Key to
Table I & II)
1
2
3
4
7
10
11
12
13
14
15
16
18
Systema
Costs
$
213,952
l4l, 500
220, 000
107, 446
150, ooo
673,810
191,000
171*-, 880
254,030
205,554
308, 600
222,100
172,600
Costb
Multiplier
1.01
1.16
1.10
1.14
1.00
1.05
1.05
1.08
1.01
1.01
1.01
1.01
1.04
Design
Capacity
#DS/HR
500
550
470
250
500
4910
282
490
875
500
1000
1210
450
$/100
#DS/HR
4.34
2.98
5-14
4.93
3-00
1.44
7.14
3-87
2.94
4.15
3-11
1.85
3-98
     Includes correction for air preheaters.
     air preneaters.
Costs are for systems witnout
b.   Based on Engineering News Record,  Dept.  of Interior Sewage Treatment
     Plant cost index from purchase date to February,  1968.
                                      28

-------
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            300
            200 - -
            100
                0   10    20    30  hO   50
                                            70    80   90  100  110  120  130   ikO  150 160  170   180 190

                                             Btu Per Hour Less Preheat  Capacity x 10


                                          Figure 13  SYSTEM COST LESS AIR PREHEATER  FEBRUARY 1968 DOLLARS

-------
     The equations resulting  from Figure 12 for the manufacturers  data are

     C0RD  =  1.0/(1.14(0.434294482) L0Ge (PDS) - ^'^  100.0  (PDB)    (50)

and

     C0RD  =  1.0/(2.18(0.434294482) L0G  (PDS) - 4.38)  1OO.O  (PDS)    (5l)

for 22$ and 40$ respectively,  total solids in the sludge.

     The equation resulting from the field data plotted in Figure 13  is

     C0R   =  100,000.0  + 212.0 (PVSH)                                (52)

It is recommended that Equation 53 ^e used for costing the system  less the
Air Preheater cost.

     Air Preheater Cost

     From the sizing requirement defined on page 12, an air preheater  can
be costed using Figure 14.  This figure shows a plot of air preheater  cost
versus size based on field data.  From the data available the cost was found
to be

                  APHC  =  2-9 (APHS)/60.0                              (53)

A linear relation was assumed because the heat transfer rate in an air
preheater is directly proportional to the heat transfer surface area.   This
surface area is related to the amount of steel required to construct the
preheater and thus to the cost.   The configuration of the air preheater used
in plants visited is shown in Figure 15-  Alternate annular spaces carry
hot exhaust gases and in the  other annular spaces the air moves in counter-
flow fashion.

     Total Equipment Cost

     The equipment cost is obtained by adding the reactor system costs (C0KD
or C0R) to the air preheater  cost (APHC)

                  BCD  =  C0RD  + APHC                                 (54)

                  EC   =  C0R  + APHC                                  (55)

     Installation Fee

     Based on the information described the installation fee is

                  CID  =  BCD/10.0                                      (56)

                  CI   =  EC/10.0                                      (57)

depending on the data used for costing.
                                        30

-------
CO
                                                                   February, 1968 Dollars =
                                                                   70/2k (Btu/Min.) = 2.9 (Btu/MLn.)
                                                                   Numbers indicate installation location
                                                                           (Key to Table I)
                                           Figure lh  AIR PREHEATER COST VS CAPACITY FEBRUARY  1968  DOLLARS

-------
Hot Flue Gas
  to Stack
                                  J
Preheated Air to
  Incinerator
                                                          Alternate annular
                                                          spaces carry counter-
                                                          current flowing air
                                                          and hot flue gas
     Figure 15  ANNULAR COUNTERFLOW CONCAR-TYPE AIR PREHEATER

-------
     Consulting Engineers' Fee

     Based on the information described on page 26,  the consulting engineers'
fee is

                  CEFD  =  (BCD  +  CID)/10.0                          (58)

                  CEF   =  (EC  +  Cl)/10.0                            (59)

depending on the data used for costing.

     Total System Cost

     The total system installed cost (TSCD or TSC) is the sum of the equip-
ment cost, consultants' fee and installation fee

                  TSCD  =  BCD  +  CEFD  +  CID                        (60)

                  TSC   =  EC  +  CEF  +  CI                           (61)

     Air Preheater Fuel Savings

     The cost of fuel used to operate an incinerator can be reduced by the
use of an air preheater.  The quantity of fuel saved is directly proportional
to the air preheater size thus

                  CFP  =  APHS (FC) (PCTY) (8750.0)/106                (62)

represents the annual cost of fuel saved by the preheater where 8750-0 is
the total hours in one year.

     In the above analysis of the air preheater the maximum preheater size
allowable for the system has been determined.  On this basis some systems
will allow the air preheater to be so large that it will cost more than the
reactor and other components combined.  The economics of capital cost vs.
operating cost cannot be dealt with directly here because the program is not
set up to evaluate this. This is so because FWPCA has planned to use this
program as a subroutine.  The main program is equipped to evaluate the economics
required above.  The exact routine to be used for evaluation of the economics
will depend on the shape of the fuel cost curve (considering variable fuel
cost vs. monthly usage and location).  A "Do loop" which increments fuel cost
along the fuel cost vs. usage curve and compares this cost to preheater cost
may be the best method of cost optimization.

     Annual Operating Cost

     The fuel required to operate the system must supply the heat required to
burn the sludge minus the heat supplied by the air preheater.  Thus the cost
                                      33

-------
of fuel to operate the system for one year is

     CF0  =  (QFP (CAP) - APHS + QLL(ZIl)) PCTY (8750.0) FC/106         (63)

where 8750.0 is the total hours in one year.

     Since the operating horsepower has been determined on page 25 the
yearly cost of electrical power is

     CP  =  0HP (EPC) (0.7^6) (PCTY) (8750.0)                           (6k)

where 0.7^6 is the conversion factor from horsepower to kilowatts.

     Reference 1 indicates that operating labor is required for I/1* of time
that the fluidized bed incinerator operates.  This agrees well with informa-
tion obtained in the field.  Therefore, the annual cost of operating labor
for the combustion system is

                       CL  =  0.25 (CLR) (PCTY) (ZIl)                   (65)

The reason for sometimes using more than one incinerator is described on page
^5.  Also note that Equation 65 is directly related to the system PVSH
because ZII is related to PVSH (see page ^5)-  Although a man is not re-
quired full time to operate the incineration system someone must be in the
general area in case of emergencies.  Therefore the reported labor costs
vary in different installations depending upon the work load which must be
handled by the plant operators.  In most cases the incinerator operators
can be used for other plant operations after an initial startup period.

     The annual operating cost is obtained by summing Equations 63, 6^ and
65

                       C0  =  CF0  +  CP  +  CL                         (66)

     Note that this cost does not include the cost of flocculent added at
the centrifuge inlet to aid coagulation.  The more commonly used flocculents
and dosages are listed in Table II of the field data summary.

     Annual Maintenance Cost

     The annual maintenance cost includes plant maintenance labor, service
and repair labor, component replacement cost and sand replacement cost.

     Plant maintenance labor cost is accrued because of repair work and jobs
such as lubrication and sand replenishing required during the year.  There
was no field data available on these costs, however, the maintenance costs
were stated to be quite low at all installations.   It is safe to assume a
maintenance cost of one man hour per day.  This yields

                       CIM  =  (CLMR (PCTY) (8750.0)78.0) (zii)         (67)

where 8.0 reduces the cost to one eighth of a man hour for every hour of
Operation.

-------
   Data were not available  for  the cost of labor to repair instrumentation
and other equipment requiring outside of plant service labor.  Therefore,
it was assumed that one man hour of service labor was required for each
150 hours of operation.  The service labor cost is given by

                  CLMA  =  (CLMS (PCTY) (8750.0)/150.0) (ZIl)          (68)

     The cost of equipment replacement was found to be very low.  Most failures
were in thermocouples and fuel nozzles.  There was not data on these cost.
Thus the expression which was assumed is

                  CEE  =  365.0                                        (69)

where CER  =  yearly cost of equipment replacement.  This is equivalent to
$1.00 per day of operation.

     The rate of sand loss per year was defined on page 2U .   Sand costs about
$20 per ton.  Therefore, the cost of sand loss per year is

                  CSL  =  SLR (20.0)/2000.0                            (?0)

     Then the annual maintenance cost is easily found as

                  CM  =  CLM  +  CLMA  +  CER (ZIl)  +  CSL            (?l)

     Annual Operating and Maintenance Cost

     The total annual labor and maintenance cost is

                  TCMO  =  CM  +  CO                                   (72)

Note that this cost does not include the chemical additives used to aid in
dewatering the sludge.

     Scrubber Costs

     Table IV shows representative scrubber costs for scrubbers made by the
Sly Manufacturing Company.  These scrubbers were installed on some of the
installations visited during this program.   Scrubber costs were included in
the computer program .lump sum costs, but are presented here to allow reference
at a future date should detailed cost data be available on other system
components.

     Scrubbers installed on installations visited allowed particulate emissions
in the flue gases of from 0.05 to 0.75 grains per standard cubic foot of
flue gas.   The tolerable emission level is determined by the local air pollu-
tion laws.
                                      35

-------
                                  TABLE IV
                            SLY SCRUBBER COSTS*
Inleta
Gas Volume
  CFM
500-1,000
  3,000
  5,000
  7,000
  9,000
 12,000
Inlet*
Gas Volume
  CFM
500-1,000
  3,000
  5,000
  7,000
  9,000
 12,000
Two Stage Impinjet
3 GPM Water/1000 CFM (inlet) *P = 4.
Outletb Outside
Gas Volume Diameter
CFM Inches
It76
2,856
4,760
6,664
8,568
11,424
24.5 GPM
20
30
40
^5
50
60
Three Stage
•5" H20
Material and
316 ss
(3/16")
$ 2636
4146
5897
6825
7969
10450
Impinjet
Water/1000 CFM (inlet) ^P
Outlet0 Outside
Gas Volume Diameter
CFM Inches
327-654
1,962
3,270
4,578
5,886
7,848
20
30
35
40
45
50
316 ss
(1/8")
$ 2162
3339
4708
5460
6349
8315
= 9" H20
Material and
316 ss
(3/16")
$ 3223
5157
6311
7396
8725
9538
316 ss
(1/8")
$ 2627
4144
5018
5799
6911
7554
Thickness
316 ELCSS
(3/16")
$ 2861
4479
6429
7410
8679
11318
Thickness
316 ELCSS
(3/16")
$ 3497
5558
6826
8003
9313
10400
316
ELCSS
(1/8")
$2436
3597
5086
5899
6882
897^
316
ELCSS
(1/8")
$ 2833
4445
5307
6386
7449
8198
*  Courtesy of Mr. Harding of Sly Manufacturing Company,  Cleveland,  Ohio.
   Costs do not include pump or surge tank.
a. Saturated @l60°F.
b. Saturated @156°F.
Q. Saturated @ 100°F.
                                      36

-------
     Cost of Installation^

     A plot of the cost for fluidized bed incineration equipment (less
a-ir preheater, for primary sludge is shown in Figure 16.  The assumptions
Tiade in plotting Figure l6 are that each person produces 0.2 pounds of
dry solids per day.  If ve assume primary treatment removal of suspended
solids is 60$ thus 0.12 pounds of dry solids per day per person must be
incinerated.  Each person creates 100 gal/day of sewage water.  Therefore
1 mgd is equivalent to sewage waste from 10,000 persons (1200 pounds of
dry solids/day) and 100 mgd is equivalent to wastes from 1,000,000 persons.

     Figure l6 shows the installed cost (less air preheater) of the
fluidized bed incineration system (based on the field data curve of
Figure 13) as a function of the primary treatment plant size in mgd.
The assumption of an 8 hour per day burning period has been made (i,e. 1200
pounds of dry solids/day -f 8 = 150 pounds of dry solids/hour).  A sludge
having 9000 Btu/#/s and 1% HO has been assumed.
                                      37

-------
CO
CO
        o
        Fn
        -P
        w
        O
        0
                            Cost of  Fluidized Bed  Incineration Systems
                            calculated assuming no Air Preheater is used.
               rtr rttr-tr-trrr- >:•!'.::.:. ^.:.t:.:: .!.::. rt- .'I I.;!..1;. .-;.'..  -            r-rr-rrrtm
               iSBg ::: Bpjtffin laa?J :::"- u :.'••• -             P [23 ::::-"' •:•.•::-iftrj
               r rli±±- — t!!!^!^^.-^---^!!^*!^:! ,,-1},-,, ;.f: -                        • : t: : ;(^-Utl-H
                   Largest  plant (10,000  PDS/HR) which cost data  was
                   available for (see Figure 12).
                                       m+
                                           Assumed 8 hr burning  duration/day
                                           Primary treatment sludge
                                           9000 Btu/lb volatile  solids
                                           PVS  =  75
                                           PH20  =  70
                                           Number 2 fuel  oil
                                           Less air preheater
                                       Extrapolated Curve
                       10
                                 20
30        Uo       50         60        70
      MLllions of Gallons Per Day
100
                                       Figure 16  PLANT SIZE IN MILLION GALLONS  PER DAY VS. COST

-------
                              COMPUTER PROGRAM






Listing of Program




     The complete program developed is listed in Fortran IV pn the following




pages.

-------
FLUIDIZED BED INCINERATION OF SEWAGE SLUDGE                      FBINC  1


4
DIMENSION A(3).B(3) fPCOl
FBINC
10.2./i' C3AIR.' .F10.2./.1 CAP' ' tF10.2 i/t ' PDS-1 tFlO.2 t / i ' PM20»' .F1FBINC
30.2,/,' OFU°< tF10.2)
FBINC
" •' II FORHATT IHO.'AF*1 iHU.Z./, • Dh" • >hlU.2i / t* A(i»' .h lU.Zi/ I ' Ub= ' .hlU.hUINV.
, 12./.< VE-'.FIO.Z./.' HE-'.F10.2./.' ORH»' iF10.2./ . ' OHF>- ' .F10.2./ .FBINC

f ,_,J— „








CO
40 n















{• «hK='.HU. «!•/«• HHIB- if-lU.il/. • hBMK"' .h JU.Z./i • Ml-"
12 FORMATdHO.'FCo' .F10.2./,1 CLR= ' .F10.2 ./ . ' CLMR*'.F10.
20<2i/f' CP°' >F15i2./i' CFO"1 •F15»2t/.1 APMC= ' iF10«2« / .
	 —72"f/ilfi CEF« ' tF10.2.^ > ' CEFP=* >F10«2» ft ' EC" ' IFI0.2 ./« •
13 FORMATIlHO.'TA»ltF10.2./«l TW= ' tF10.2«/i ' PAPH='.F10.2
• < r i u • <; i )- u i ii<.
2./.1 CLMS='FBINC
1 EPC"1 .FiO. FBINC
1='. F10. 2. /.FBINC
i/i1 SLRi'iFFBINC
10 FORMAT (1H0.1 ASSUMED PROGRAMMED SLUDGE ELEMENTAL COMPOSITION') FBINC
16 FORMAT (1H0.1 NATURAL CAS FUEL1)
18 FORMAT <1HO.' WATER QUENCH MAY BE REQD. IN REACTOR* 1
20 FORMAT (IHO.'CALC OFiBAF iQPE'O .OLE-0 ' )
FBINC
	 ••• mini.
FBINC
FBINC
— 71 FORHATtrHlV'TTAbt'iiUI mjNL
22 FORMAT (1HO. 'SYSTEM IS TOO SMALL TO BE COSTED BY DORR CURVES >,/•' FBINC
	 TAW-ESTTmTf-TVG'IVE'N' BTTTELD UATA lUOAT'lUNS*./ r'-'SMf
2 FOR CORD. CEFDiECO. CIO. TSCD. SHOULD BE DISREGARDED')
Z«, FORMAT! 13F6. 2)
26 FORMATC3I11
100 READI2.23 I OS.OFU .CAP.TA.TW.CLR
READI2.26 ILITEiLITiLll
WR1TEI3.21 ) M
110 READ12.23 I OF .OPE .OLE .BAF
GO TO 270
1-0
QPE-0.0
GO TO ( 130* 140ULIT
3(11* *Q3*7
D-. 001107
GO TO 150'
WRITEO.15 I

W™ •* * * * • -
i * i!"" . " -
DBTH ' KK 1 n 1 C'DKBTnVT
FBINC
FBINC
	 TUMI;
FBINC
" PblNL
FBINC
FBINC
F8INC
FBINC
FBINC
FBINC
FBINC
FBINC
u " 	 PC rwe
FBINC
FBINC
FBINC
FBINC
FBINC

•
•3
*•
5
1
a
9
1U -
11
13
1*
15
17
10
19
21
23
25
27
•fa 	 	 -•- _. . - - ... --
29
31
33 '
35
37
39
41
t!
45
47
49
»
11
59
57
59

i * •*
^
M


«


M
















.






r •
.

-------
0«0/28*
                                                                  FBINC 61
1
1
1
, 1
(
t


-.





\
11




1








r
n


160 A(2)«lt
WR!TEOtl6 )
170 A(2)"1.2
WRITcOil? )
PDSC-POVS/IPVS/IOO. >
PPH20-PS-PDSC
OSL-OS*POVS/PS
B(3I-B(1)+FM»B(2)
IF(XF) 200, 210,210
210 PVT"A(3)-»-8(3)+D-t-3.76»XF+PPM20/18.
V~ «0'iMPVT / • B096
PV4T«PVT+4.76*Y
CPH20=(B(3>+PPH20/18i)«14000.
CP20-Y»11800.
SUMO-CPC20+CPH20+CP2N+CP20+CPIN
AIRCP=IXF+Y)»19BO.
SUM-THCP-THCPT
IFCI-1) 230,230*220
230 IF(SUM) 240,260.250
60 TO 260
GO TO 190
BAF"137.5»UF+Y)/PS
QAIR«15.»BAF
QFP-QF+OPE
280 CF»FC»OFP«PCTY»I8750.)*CAP/10.«»6
PC(2)-BAF*(24*(1000.-60
300 PCI3I-PCI2)
?10 DO~OFP~PC(3)
IFIQFP-PCI3) 1 320,330,330
GO TO 340


•
mini ot ~~ 	
FBINC 63
FBINC 65
BIHC 4fi
FBINC 67
FBINC 60 J
FBINC 69
TIC TO
FBINC 71
FBINC 73
FBINC 75
FBINC 77
FBINC 79
FB INC BO
FBINC 81
FBINC 83
FBINC 83
FBINC as
pat Mr QfL
FBINC 87
FBINC 08
FBINC 89
FRINT 90
FBINC 91
FBINC 93
FBIMC Uh
FBINC 95
FBINC 97
FBINC 99
FBINC101
FBINC103
FBINC105
FBINC107
FBINC109
FBINClll
FBINC113
FBINC115
FBINCllt - - , - - t ,, r - T nnrr
FBINC117
v FBlNCllfl
FB1NC119
1
' "J s


"'

•a
v.







"U
u,
t
•a


H









.'


M

-------
»t
1—

4 	




























340 APHC-M2.9*APH5/6CN)
350 APHC-0.
IF(CFP) 370,370.390
GO TO 390
9 BO PC 1 3 I BU iO '
CFP«Oi
390 PCDS-UOO.-PH20)
PVSM-PDS*PVS/100.
if IPVSM— j5uo«l taumauitOu
400 ZII-2.
410 ZJ"PVSH/2li
1FIZI-1500.I 440.440.420
GO TO 410
taflr ZT'fvsrt
Z1I-1.
PDSJ»POS»ZI/PVSH
AG-SUMQ/155000.
VE-SUMO/18000.
DG»SQRT(4.0*AG/PI>
VS-VE/1.5
PV"SUMQ»2.5/10.t«5
AO"PI«(HF»OF+HE*(DF+DGI/2.0)
IF(QLL-OL) 470. 470.460
1 480 OL"GL*Z99ffU— • — ••• — • ' • •
GO TO 450
NFP»FLOATUFIX(100.0»POS!/<2000.»PCDS1+0.5000Q1> 1
480 NFP»1.0
IFIPCDS-31.) 500.500.510
GO TO 520
520 COR«100000.+212.«PVSH
FBKP1«-5.68*.90»HPI I-.000565«( (HPI I l»*2>
	 CHPTT,TSZS»HPTI
HPI-MP|I*ZII
OHP«OHPI»ZII
ECD-CORD+APHC
CJD-ECD/10. 	 	 __


FBINC121
FBINC123 - '
FBINC125
FBINC127
• FBINC12V
FBINC131
FBINC133
FB1NC135
FBINC137
FBINC139
FBINC141
FBINC149
FS1NC145
FBINC147
FBINC149
FBINCL51
FBINC153
FBINC155
FBINC157
FBINC159
FB1KC161
FBINC163
FBINC166
FBI NCI 67
FB'IMC169
-, ... i FU'iNL 1 T 0 ' |IT"
FBINC171
FB1NC173
F6UC175
FBINC177
FB1MC17^"^^— -~-_ x

- ^
t


•










,.






„
"li



1






-------
CEFD-1ECD+CID1/10.
                                                                  FBINCI81
•




























•fl >B

)f'»—
CL-0.25*CLR»PCTY»ZII
CFO-(OFP«CAP-APHS+OLL»ZIII*PCTY*8750.»FCi'10.«6
530 CFO-0.
IF( (DF/HFI-.64) S50t550i560
GO TO 570
570 CLM-CLMR«PCTY»1093.7»ZII
C5L-SLR/100.
TCMO-CM+CO
TSCO-ECO+CEFO-KIO
FBINC183
**
FBINC1B5 \
FBINC187
I
FBINC1B9
FB1NC191
FBINC193 , ,
FBINC196 !
FBINC197
FBINCI99 ' ,
— — — - CAPt'C'APv'ft 1 ————— — .-- — .. 	 .... •-•T-UITH.«VU , »
WRITE (3ilO I OS.QF»QPE1»QLEtQAIRiCAP.PDS.PH20.PVS.BAF.PVSHiPCOS.QFFBINC20l ,
WRITEOtll I AF»DF.AGtDG.VE.HE,ORHiOHP.NFP.HPI.FBHP»HF
580 WRITE(3>22 ' )
590 MR1TCO»18 1 f C iCtBrCfcMRir€teM&tCLMAtCSt;T€OT€f<»€PTCFO»APHCltifi^
ICEFDtEC.ECD.CFP.COR.COROtCI.CID.TSC.TSCD
WRITEI3>23)PV4T
CALL DATSW(4iMOREt
600 CALL EXI-T
	 CNP —————.——————— — — — — - — — — 	 	 	 	
-

t
.-' • -'

••""'--
. : .--ci -•-•»::... ,


. r 1 ' I ""
'.N-i-M
-t... -«.aj'.-.-
•

1
-
roinkcuc
FBINC203

FBINC205
FBINC2Q7
FBINC209
FBINC211 !
FB1NC213 ;

214 ;



"

•




".'
':
1 c ; .
-.- •. •
'
	 n ' «•"-«« — -

'









-------
Flow Chart
     The flow chart for the computer program developed  is  shown  in Figure 17-
                 Figure 1?  FK)W CHART OF COMPUTER PROGRAM

-------
How to Use The Computer Program

     Options  in  the Selection of  Input  Data

     The program is set up to follow different loops depending on the index
values read in.   The options available  are:

     l)  The  use of pilot plant data for fuel and air requirements or
         the  use of the calculation routine for these variables set up
         in the  program.

     2)  The  use of the programmed sludge chemical composition or an
         input sludge chemical composition for calculation of the
         variables in 1 above.

     3)  The  use of natural gas or Number 2 fuel oil in the calculation
         of 1 above.

     In the use  of option 2 above the operator should note that the programmed
sludge composition is a representative  value based on Reference 2.  The errors
involved in using this routine instead  of pilot data are that the assumption
must be made  that the sludge exists in  an unoxidized state.  Therefore,  the
oxidation reactions would be
However, the sludge consists of compounds in a partially oxidized state, for
example the combustion reactions

                  C0  +  4-
may occur instead of the complete combustion reactions shown above.  Thus
the difficulty and inaccuracy of determining the fuel and air requirements
needed to support sludge combustion is apparent.  Because of this limitation
it is advisable to use pilot plant data when accurate results are required.

     No assumptions can be made as to the accuracy of calculations when the
programmed sludge elemental composition is assumed.  The insertion of a true
elemental composition for the sludge of interest, with a corresponding sludge
heating value (OS) may yield a more accurate analysis.

-------
     Reactor Sizing Limit

     As with any mechanical equipment, there is a maximum tolerable size above
which a fluidized bed incinerator cannot be economically constructed.  The
physical size and operating stress combine to make this limit apparently a
unit with a design capacity of 1500 pounds of volatile solids per hour or
a reactor freeboard diameter of 16 to 17 fept (based on Kansas City units).
Therefore, when a system with a higher capacity than 1500# VS/HR and/or a
greater freeboard diameter than 16 feet is required, the system should be
split into two or more systems of equal size (i.e., PVS/2, FVS/3, etc.) if
it is to be handled by this program.  This is done in the computer program
and ZII is used to represent the number of incineration reactors having a
volatile solids capacity of 1500#/hr or less.  The computed capacity of each
reactor is ZI.  The system cost curves are defined to 10,000# dry solids/hr
(Figure 12).  Accuracy beyond this capacity is uncertain and the computer
program usage should be limited to capacities below the above.

     Air Preheater Option

     The decision to use an air preheater can only be made through an
economic analysis which FWPCA has set up in the executive program.  Since
this program will be used as a subroutine for this executive program, no
attempt was made to optimize the system.  The air preheater is sized based
on the required system heat requirement from fuel and the preheater.  The
maximum preheater capacity for each reactor vessel is given by

                    APHSI  =  APHS/ZII                                (73)

To optimize the air preheater size, a trade-off between fuel costs and air
preheater size must be accomplished in the executive program.

     Data Input and Output

     Figures 18, 19 and 20 show the input cards used to obtain the data for
Figure 16.  The output data from the computer program for each set of data
input are shown respectively in Figures 21 through 32.

     To obtain this data, two cards

                    APHC   =   0.0

                    APHS   =   0.0

were inserted after card FBIMC121 in the program listing shown in this report.
This was done simply to eliminate the air preheater,  since the cost optimiza-
tion needed from the executive program to aid in sizing the preheater, is
not included in this subroutine.

     The indices used for program control on Card 3 are described below:

     1)   LITE = 1 when pilot plant data are used for QF,  QPE, OLE,  BAF,
          LITE = 2 when QF,  BAF are unknown.
     2)   LIT  = 1 when sludge elemental composition is known from tests,
          LIT  = 2 when sludge elemental composition is unknown.
     3)   KEI  = 1 when using natural gas fuel,
          LII  = 2 when using #2 fuel oil.

-------
 CARD #1
 CARD #2
 CARD #3
QS, QFU, CAP, TA, TW, CLR
FC, PCTY, PVS, EPC, CLMR,  CLM3,  PB20
LITE, LIT, LII
9000
r-,-%
1 .3
C_ An
ecMrar
CTATCIAIT
CfOO
COWUT
STATEMENT
NUMBER
010 0 0 0
ri i « s
if't 1 1
Fill1 2 2
33333
44444
55555
66666
77777
88888
99999
.10000. 500. 60. SCO. 5000.
3| .24 70. .03 3. 8. 70.
— L : : ; i
s
£
S FORTRAN STATEMENT
<
IOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOCOOOOOOOOOOOOOOOOOQ
1 7 1 9 1011 UtJHlSlilT l8ISai1En2)BJ8z;n2SX31BU»35»373l33«tM!O»-, 45«47U45aiSiaaS4aaSI5l59S06l6JO«OS6S!OG9JOII7!
11 1111 til 1 It 1 11 111 11 1 11 11 1 1 1 11 1 11 11 1 1 111 1 1 1 111 1 111 11 1 111 11 M 1)1 Ml
!222222222 22 2 22 22222 22 222 2 2 222 222222222222 22222 222 22 22222222 2222222
1333333333333333333333333333333333333333333333333333333333333333333
1444444444444444444444444444444444444444444444444444444444444444444
1555555555555555555555555555555555555555555555555555555555555555555
.666666666 6.6 666666666666666666666666666666666666666666666666 6 G 66666
7 7 7 7 7 > 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7
888888888888888888888888888888888888888888888888888888888888888888
1999999999999999999999999999999999999999999999999999999999999999999
7 1 1 Hll I!131415I8H IIIS»!ina2«25a2iaaB!IB33»6»J7»lS<»4IC4J«45«47«Oa5l5JaM!BS85;aS96»SiaeiE46St56jaE9m7l7?
IDENTIFICATION
00000000
n74isii77itnn
11111111
22222222
33333333
44444444
55555555
66666666
77777777
88885888
99999999
11 74 75 76 17 71 79 n
       ISC 686157
Data  Cards  Case 1
9000
C IWI
COOCHT
1.3
Cm
"COMMENT
212
C_ «"
COMICMT
STATEMENT
NUMBER
OjOOOO
lf.111
L|2l22
33333
44444
55555
666G6
7|7 7 7 7
88888
9l9 9 9 9
1 1 12 ] « 9
.
s
3
i

«
s
i
0
1
2
3
4
5
6
7
8
9
c
10000. 5000. 60. 200. 5000.
.24 70. .03 3. 8. 70.
; 1 is ' ' B



FORTRAN STATEMENT

000000000000600000000000000000000000000000000002000000000000000000
T 1 1 18 till 13 14 15 U 17 11 19 70 21 U 23 N IS ZB 27 21 29 30 31 12 33 M 15 36 31 31 39 40 41 42 4] 4*i 45 46 47 49 49 SO 51 52 S3 54 55 SS 57 SI 59 GO 61 C2 S3 64 S3 U W 61 69 70 11 71
Ml 11 1 1111 1 1 1 11 II 1 i 1 1 1 1 111 1 1 til 1 1 11 1 11 1 1 11 1 111 1 1 11 1 11 11111 M 1 1 1 11 1
222222222222222222222222222222222222222222222222222222222222222222
333333333333333333333333333333333333333333333333333333333333333333
444444444444444444444444444444444444444444444444444444444444444444
555555555555555555555555S5555555555 55 555 55555555555555555555555555
B66666666666666EG6666G666666666666666666666666666666666666666666G6
7 7 7 7 7 > 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7 7
888888888888888888888888888888-888888888888888888888888888888888888
999999999999999999999999999999999999999999999999999999999999999999
7 1 1 Ull 12 11 14 IS 11 17 11 ISM II 21 13 « 2S 21 27 II 29 3D 31 » 33 MB* 37 » » M 41 4! 4] 44 4141 4f 41 4)951 B SIM 55 !> S7 a 59 GO 616261 14 DO (7 M U 70 71 72





IDENTIFICATION

00000000
73 74 n n n 7i n to
11111111
22222222
33333333
44444444
55555555
66666666
77777777
88888883
99999999
73 74 75 7t 77 II 19 10
ISC BBaiST
Data Cards Case 2
                           Figure  l8 DATA CARDS

-------
9000
Ck. rap
CHUT
1.3
c-.i.
212
Q_ ™>
-«Bft
STATEMENT
HUUBEB
00000
IjllH
A2,22
33333
44444
S55S5
66666
1
77777
88888
09999
i 1? i i i
10000.12500. 60. 200. 5000.
!
| .24 70. .03 3. 8. 70.

:
FORTRAN STATEMENT
lOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOSOOOOOOOOOOOOOOOQOO
11 11 11 1111 1 111 1 1 1 1 Mill 11 11111 11 111 1 11 111 1111 II 11 111111 1 t 111111 111
1222222222222222222222222222222222222222222222222222222222222222222
1333333333333333333333333333333333333333333333333333333333333333333
14444444444444444444444444444444444444444444444(4444444444444444444
1555555555555555555555555555555555555555555555555555555555555555555
>666G66E66GG6GG6666666E6G6666666666G 666 66666666 S6B6GG666666666G 6 B66
77777/77777777777777777777777777777T777777777777777777777777777777
888838888888888888888888888888888*88888888888888888888888888888888
999999999999999999999999999999999999999999999999999999999999999999
IDENTIFICATION
00010000
nnnnnnnn
11111111
22222222
33333333
44444444
55555555
66 6 6 66 6 B
77777777
98888888
99999999
u 14 TJ TC n n n n
       isc eaaisv
Data Cards  Case 3
9000
L/*"cw«ttPn
1.3
C»- "*
coHHcm
212
^ re.
^ MMCNI
STATEMENT
NUMBER
00000
IfllM
!i|2*22
33333
44444
955S5
66SB6
77777
88888
9|9 9 9 9
ill 1 « 9
i
3
s
2
i
i
0
i
2
3
4
S
6
7
8
9
c
10000.25000. 60. 200. 5000.
.34 70. .03 3. 8. 70.
n n

FORTRAN STATEMENT
000000000 000 00000000 UOO 00000000000000000 0000 000 COO 00 000000 00 0000 00
7 1 1 Nil l?UMIi16IIUUIDII2Zn!4ZSS779nBll329MEV3)3894414241ilG4i>Oia7l79«
1 1 Ml 11 1
22222222
33333333
44444444
5SSS5SS5
66666666
77777777
88B88B88
99999999
7J 74 71 75 77 n 78 •
Data Cards  Case
                            Figure 19  DATA CARDS

-------
9000
^ ran
^ COHHEMT
1.3
f* fOR
^/ COKM-NT
SIS
^ FOR
Lj COHCHl
STATEMENT
NUMBER
OjOOOO
1,111
 69 70 71 72
11111 1 1111 11 1 11 1 1H1 1 1 1 111 1 1 11 11 1 11 11 1 1 1 1 1 1 1 1 1 1 111 1 1 1 11 1 1 1 1111 1 11 1
!222222222222222222222222222222222222222222222222222222222222222222
1333333333333333333333333333333333333333333333333333333333333333333
1444444444444444444444444444444444444444444444444444444444444444444
1555555555555555555555555555555555555555555555555555555555555555555
!66666666666666 66666666666 6666666666666 666 666666666666666666666666 6
1777777777777777777777777777777777777777777777777777777777777777777
)88888888888888 888 88888888 Bfl 888 88888 888888 88 B88 8888 8888888 888 88 888 B
9999999999999999999999999999999999999999999999999999999999999999999
! 7 1 9 1111 1! 13 14 IS 1617 II 19 20 21 25 21 24 2! 26 27 213 » 11 32 33 14 15 3837 » 39 «41 42434(45 « 47 41 4) S3 51 52 53 54 55 5*5751 59 60 816261 6165 6667 U 69 70 71 72
IDENTIFICATION
00000000
13 71 19 71 17 71 19 B
11111111
22222222
33333333
44444444
55555555
66666666
77777777
88888888
99999999
73 74 75 78 77 ffl 79 «0
       ISC  BBBIB7
Data Cards Case 6
                             Figure  20  DATA CARDS

-------
      ..  -„- 	  ... -_..
      wr tofir tu*-c=utwLC"v
 WAICK UUtNtn MAT  DC  KtUtf*  114 KCAblUK
    QF«

    OLE"
          0*00
           OtOO
    WkIR«
    CAP»
           33.76
         500*00
„ PH20«
,. BAF-
KVSM»
1 PCDS»
70.00
2^25
1U5.UU
30.00
DF"

HE-
	 7V9V 	
3.16
2*94
"9"8v85 	 "" "
7.97
 ll__

\
 If—


^B...
 OHP
               9.93
 NPK
 HP1
 HF"
               l.OU
              15.89
             	-8V«T
             12.75
 .^SI---.I.?-I0?-S^*L._..T° Bf .C°JT5?-?Y^PP^-.^U.-VES	
 AN tSIIMATfe  15  GIVEN BY PItLD DATA EQUATIONS
 ANY DATA PRINTED FOR CORDtCEFD.ECD.CIDiTSCD. SHOULD  BE  DISREGARDED
     FC
           1.33
    CLMR
             3.00
1
•*
     CLMA
             BrOO
           111.99
 CO
                1086.39
    CP"
              466.94
 CFO"
. APHC-	  0.00

 CEF"  13448.60
~CBPD5—2557IV5T
 EC" 122260.01;

    ECD
    CFP
      Z320l4«3T
           0.00

-------
 —
         12226*00
    CIO"23201.43
    TSO 147934.62
    TW-    200.00
    SLR-   1379.19

       0.
V..
II	
         Figure 22  SAMPLE MTA
                                     50

-------
       TE
           uw      «       u/.         u

     OS*
     OF-      0.00
•)'— "QPE-- ........ 0.00
     OLE; _ o.oo
     wA!R»      33.76
^    CAP-   5000.00
""-— T»OS«— ~i50o-icro
     PH20«      70.00
ji —

 -            ._
     PV5H»    1050.00
1    PCDS"      30.00
 "-—- oTOir— TOT

}"--- -AF« .......
     OF" _ 9«67
     3S5»     63.21
     DQ"      8.97
 """VE^ ...... 5**Y3]f
     HE-      7.97
"'""""OffH-" ....... 24.60
     OHP"    113.51
     NFP»      3TS5
1    HP I"    181.61
 ..... FBMF; ...... i39VlV
 ,    HF-     12.75
^n

"1    FC-      1.33
 x   tLR"   sugo.gu
1    CLMR-       3.00
— "CLflSV ........ 1SV80'
     CLMA=     111.99
^-—-c^L«- ..... T«*;*9
     CO" _ 6606.37
     CM3   ifur.vs
 ,    CP"        5334.84
   -TCPO^ ------------ -yTT;
     APHC«       0.00
 "— -Epca --------- CTV07
     CEF»  35486.00
     ttru=   9^roH*Hd
1    EC" 322600.06
   ""ECBS'"4T9¥BO-;*T
     CFP»      0.00
-,"— "CORS-WZBOWCnS
 ,  ^ CORP-  479680.81
     tlB , 32ZOO.UU
 ,    CIO"  47966.07
                                   DATA
                                     51

-------
•x1 — -T SC&«"W41-3Y7$--
     I«»      OUtUU
\    ™"     200.00
 " "PAPH-"45"6V6b"
 ,    SUR»   14349.66
 if..
a—

n_
        0»
a.
>„	Figure. eh__BUmBJDKI!A_
                                       52

-------
           '3	

     I.AH. «r IBAP »WKtsUtULfcHU





 '    UATEfc mJENCn  HAV BE—(TEOO	TIT

   "05*	"90XTOVOO"
     OF-      0*00
^—-Qp-E-i-	-Q.-00	
     QLEa	0.00	
     OAIRo33.76
10    ^AP_"  12500.00
     ~PDS-""T75cf.o6	
     PH20-     70*00
""	-PVS-"	TO'iOQ—	'	—'
     BAF"	2.25	
     PV5H"2625*00
;L   PCDS-     30.00



     DF"      10.79	
     Au™ -     76.71
     06-      10.01

     HE"      7.97
,»	Toj^sr	ZVi'SO	
     PHP-     3<>B*23	
     Nf-HB      3.UU
^    HPI-     557.18
if	p^p..	TO2VW	
     HF"      12.75

     FC»      1*33
       ^_   _...... A..
     LLK"9UUU.UU
^    CLMR»       3.00

 n    CLI^A"  -- 223'9?.	

     CO-       1913,    EC- 656500.12 	_

     CFP-      0*00

     CORD- 965630*75	
 	Cl-  65650.01	
 '„    Cl?".. 96563.07	

                       Figure  25  SAMPLE DATA
 n..._______._..._._.......--_.-.......-..----•.«»-.--•.->.
                                      53

-------
 i.
             OU*UU
     TW«    200*00
 —TAPFfi—TI75VOD"
     SLR-  44615.71
 i
 li
 »—

 It- .
J
 B	
>n..

 !»..
                                       54

-------
 I.
    V.ALI UP tOAr »UHtBO»QLCBU
\

 4—•
 t.
           UUCnin n«T Dt KCUU*

        — "9000YOO-
    OF"      0*00
    OLE"       0*00
    Wni r»™     3 Jt f O
    CAP"   25000tOO
"— "PDfS» ..... 7900-fOO
    PH20°     70*00
 '— --PVS"- ....... TOiOO
    BAF»       2.25
    PCDS-     30.00
"""    — lOTJOTTSDO
 L—-AP»	
    OF"      10.79
    «UH  t    lot 11
    OG»  '    10.01
"—Vr-	6T7YB2T
    HE"       7.97
    OHP"     696.47
    NFPH       3.00
    HP!"    1114.36
          	eo4Yfio"
„.  FC
    tUK°    5UUU.UU
B   CLMR=       3.00
    "CLMS~«»	SVOO"
    CLMA=     447.97
II--
    CO"        38269.45
"—"CPUS
    CM"    59?0tl4
    CP»        32733.01
    APHC-       0*00
    Ep-fi ......... o-;0*3
    CEF" 133430.03

    EC=1213000.25
    CFP»       0.00
    CORO=1718258.25
R   r •_ i * *B"*"JiM >%•• *^ 1
    CIO-  171625.81
                                     55

-------
    TW«     200.00
   "PAPFfo"""2"25"6i"dO"
    SLRo   89231.42
         ""T890.-66"
       0.
it..
u	

»_
                                    56

-------
'

'	ASSWETJ- 1»roGKA!TOEI)"SLVDGE"EtE MENTAL" "COMPOS IT 1 ON"

    -NO-.-2-F-uet-ott:	-	
    wATER uwErain nAY BE REGti*IN kEACTOR"
'— "OS»— "9000VOO
    QF«       0.00

, _ OLE" _ 0.00
    OAIR*      33.76
    CAP-   37500.00
„
  •"
    PM20-      70.00
 —~
    BAF"       2.25

    PVSH*    I
    PCDS-      30.00
         	-91v5^-
    OF»      10.79
    DG»      10.01
   "VF* ...... B77Y87
    HE-       7.97
„

    OHP-    1044.71
II
„   HP1-    1671.54
    HF»      12*75

    FC"	1.33
    CCR"5WOU.OU
    CLMR-       3*00
  "'CLM5-'	-8VOO--
    CLMAa     671.96
ii.
n. ..
    CO"        57404.16
11 --- CM" --- 89?3.2T ------ ---
"— -XFO" ............ 65W.66

    CP-        49099.50
    XFO" ............ 65
    APHC-       0.00
    TprCa- ........ O.~03"
    CEF- 194645*03
    rET&«i"2-6-8r05Y36"
    EC«1769500*25
    CFP-      0.00
   "COR-I7i69500;Z5
    CORDo2437323.50
 - CT*~ 1T6950T03"
    CID- 243732.31
 .....
                   Figure .29.. .SAMPIJE. DATA
                                    57

-------
     FA"     OOcOO
).    TW»    200«00
   •pAPH.""3375VOO"
 .    SLR" 1338*7.12
y—-arc-
 	  o.
  -

)„..
                                 58

-------
 I.
 4	
 t.
                  IWT DC  KCUU*  IN KCnl I
 ' —
     OF-       0.00
     OLE"       0*00
     WM«-     33* /
3    CAP*  50000*00
  —     —       —
     PH20-     70.00
•j1— "pysar ------- HTiOO
     BAP-      2.25
 n.
     rvan*
^    PCDS-     30*00
        "-"~
     DF«     11*52
     ««•     ay* ro
     DG»     10*69
     Vr*	7T3VIT-
     HE-      7*97
     OHP-   1581*19
     NFF"      **00
X   HPI-   2529.90
 '•" "FHflFi— 'T7ZOT5V
     HF-     12.75

     FC-      1.33
            3UUU.UW
^   CLMR- _    3*00

 0 __CLMA-    783.95	

     CO-       84517*48
  ^   CH*
1   CP«       74312.75
—"CTO"	VXOVST
 M   APHC-      0*00
f—"Der	ff.'W
     CEP* 255860*03
 u.
 1   EC-2326000.50
 *-— •
     CFP»      0*00
 ) — 'C
     CORD-3197096*00
     CI» 232600*03
1    CIO- 313709*56
*—'-
                                    59

-------
>.   TW    200.00
 —warns—vsffov
 .   SLR- 192627.31
       »"
       0.
>«„..
                                 60

-------
                      CONCLUSIONS AND RECOMMENDATIONS
Performance of the System

     The personnel at all of the installations visited were very well pleased
with the performance of the fluidized bed incineration system.  Most operating
problems appeared to be caused by jamming feed systems.  Both the special re-
tractable screw feed (Patent,  Reference 3) and the screw pump- flexible line
feed system were subject to occasional jamming because of overdrying of the
sludge feed at the incinerator or because of silt carried into the feed system
with the sludge.  The only other frequently occurring problems appeared to be
the burnout of spray nozzles or thermocouples in the bed.

     The fluidized bed incinerator is uniquely qualified for applications
where liquified wastes having insufficient heating value or variable heating
value must be disposed of.  The height of the freeboard determines the sa,nd
loss rate.  This is a variable and should be stated with any price quotation.

Method of Rating

     All of the fluidized bed incinerator contracts reviewed at FWPCA offices
had a performance specification sheet which was supplied by the manufacturer
(Dorr-Oliver) of the incineration system.  These specification sheets were
seldom filled out to allow an adequate verification of any performance guarantee.

     Further, it was found that the method of verifying that the systems met
the contract specifications on capacity was totally inadequate. The method
uses an empirical relationship of 1 standard cubic foot of air equals 100 BTU
at stoichiometric conditions.  Therefore, the claim that the sludge burning
capacity of the incinerator can be measured by simply measuring  the air flow
is in error.  The discrepancy is apparent when one considers that H_ requires
1/2 mole of fip while C require 1 mole of 02 for complete combustion.  However,
HP produces aoout 6^-,OQQ Btu/# and C produces only 16,000 Btu/# when completely
burned.  The ratio  of Btu's produced to air requirements for Hp in standard
cubic feet is thus
                     2I
     64,000 Btu/#H  <
                  2  mole H2°          =   53,700 Btu/mole air
     k.^6 (1/2 mole 0  ) moles air

One mole of air has a volume at standard conditions of 378 ft .  Therefore,

     53,700 Btu/mole air (9>yfl pj^ m°*f ^J  =   ite Btu/SCF air

The ratio for C is

     12,000 Btu/#C (-
                                                       air
     k,j6 (imole jZL) moles air
                                      61

-------
Therefore,

     30,200 Btu/mole air (                ?    =    80 Btu/SCF air
Thus, it is seen that the air requirement per Btu of heating value of sludge
or any other fuel will vary significantly from a standard of 100 Btu/Std ft^
air.  It is therefore recommended that another method (such as sludge veighing)
be used for evaluation of the burning capacity of an incinerator during
acceptance testing.

Factors Influencing Operating Costs

     The effectiveness of the devatering system plays an important part in
determining the fuel requirements for a sludge incineration system.  A system
with a good devatering device, of sufficiently low power requirements, can greatly
reduce the fuel requirements.  At all plants visited, chemicals vere added to the
sludge prior to the dewatering device.  The cost of the chemicals required was not
clearly spelled out in any contract reviewed on this project.  Also, the contracts
failed to require any guarantee on fuel consumption or power consumption because
of the lack of data  supplied in the contracts.  The contract sheets requiring this
data were left blank in all cases.  The cost of operation in dollars per pound
of volatile solids should be clearly spelled out in any such contract.

Accuracy of the Equations Developed

     The equations developed on  this program were based on the most accurate
information attainable from the field.  There were significant variations in
system design from one plant to another.

     The costs for the units surveyed did not follow the costs submitted to FWPCA
(Reference l).  In most cases, the actual prices paid for the units surveyed were
significantly below the manufacturer's (Reference l).  As competition from other
manufacturers increases, the prices probably will be reduced belov the prices
now in effect.

     Since the above variations exist, it is recommended that the prices given
in the equations developed on this program be used as maximum prices rather than
use those suggested by the manufacturer (Reference l).

Lime Recalcination

     The fluidized bed recalcination process and equipment are very similar to
that used for fluidized bed incineration of sewage sludge.  It is recommended that
a mathematical model be developed for the lime recalcination process, since
phosphorous removal from sewage waste waters is fast becoming an important process.
                                       62

-------
                                TERMINOLOGY-
Al        =   Moles carbon in sludge considered based on sludge elemental
              composition

A2        =   Moles carbon in fuel for sludge considered

A3        =   Moles carbon in fuel and sludge considered
                                                2
AF        =   Freeboard cross-sectional area, ft
                                           2
AG        =   Grid cross-sectional area, ft

AIRCP     =   Heat content of combustion air @ 60°F for sludge and fuel
              considered (0°F base) Btu/#

A0        =   Outside surface area of incinerator freeboard and bed
              sections, ft

APHC-'     *   System air preheater cost for maximum allowable sizing,
              includes all reactors used, dollars as of Feb.^ 1968

APHS—'     =   Air preheater size (maximum) for complete system, BtfU/hr

Bl        -   Moles Hp in sludge considered

B2        -   Moles Hp in fuel for sludge considered

B3        =   Moles Hp in sludge and fuel considered

BAF       **   Air flow rate required for combustion of sludge and
              fuel at U.Qtf, excess 0L, # air/# sludge

C         =   Moles of 0p in sludge considered

CAP       =   Capacity of incinerator system, # sludge/hr

CAPI      =   Capacity of each incinerator reactor used in system,
              # sludge/hr

CEF       =   Consulting Engineer's fee based on study field data
              capital costs,  dollars as of Feb., 1968

CEFD      =   Consulting Engineer's fee based on Dorr curves for
              capital costs,  dollars as of Feb., 1968

CF        =   Fuel cost for QFP for 1 year, current dollars, no. preheat
a/ Mote:  # is an abbreviation used for pounds.
b/ APHCI and APHSI refer to a single incinerator system in a multiple
   incinerator installation.
                                       63

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CF0       =   Cost of fuel to operate, current dollars, not including
              startups, including heat loss from incinerator(s), $/yr
              (v/wo preheat)

CFP       =   Yearly cost of fuel replaced by air preheaters, current $/yr

CI        =   Installation cost based on study, $-Feb,, 1968

CID       =   Installation cost based on Dorr curves, $-Feb., 1968

CL        =   Cost of operating labor per yr, current dollars, $/yr

CLM       =   Total cost of maintenance labor, current dollars, including
              overhead, $/yr

CLMA      =   Total cost of maintenance service labor, $/yr, current
              dollars, incl overhead

CLMR      =   Maintenance labor ratea current dollars, $/hr

CLMS      =   Maintenance service labor ra+.n, current dollars, $/hr

CLR       =   Operating labor cost, current dollars, $/yr «  $/8?50 man  hrs

CM        =   Cost of maintenance, current dollars, $/yr

C0        =   Cost of  operation, current dollars, $/yr

C0R       =   Cost of  Reactor System less preheat based on field data,
              $-Feb.,  1968

C0RD      =   Cost of  Reactor System less preheat,  Dorr curves, $-Feb., 1968

CP        =   Cost of  electrical power, current dollars, $/yr

CPC20     =   Heat content of C^>  in exhaust @ 1^00°F for sludge and fuel
              considered, Btu
CPH20     =   Heat content of H^>  in  exhaust @ lUOOGF for  sludge and  fuel
              considered, Btu

CPIN      =   Heat content of inerts @  1^00°F

CP2N      =   Heat content of N  in exhaust @ 1UOO°F, for  sludge and  fuel
              considered, Btu

CP20      =   Heat content of 0  in exhaust @ 1^00°F, for  sludge and  fuel
              considered, Btu

CSL       =   Cost of sand loss, current  dollars,  $/yr

D        =   Moles  of Np in sludge considered
                                     6U

-------
DF        •=   Diameter of freeboard, ft

DC        =   Diameter of grid, ft

DQ        =   Difference between makeup heat required to burn sludge
              and maximum air preheater heat available, Btu/hr

EC        =   Equipment cost including preheat(s) based on field data,
              dollars as of Feb., 1968

ECD       =   Equipment cost including preheater(s) based on Dorr curves,
              dollars as of Feb., 1968

EPC       =   Cost of 1 KM hour of electrical power, current dollars, 4/KW hr

FBHP      =   Fluidizing blower HP for system

FBHPI     =   Fluidizing blower HP for each incinerator in system

FC        =   Cost of fuel, '68 $/l,000,000 Btu

FM        =   Mole multiplier for fuel

HE        =   Depth of expanded bed, ft

HF        =   Height of bed freeboard required, ft

HP        =   Height of plenum required,  ft

HPI       =   Installed HP for system

HPII      =   Installed HP for each incinerator in system

NFP       =   Number of feel points" per incinerator

0HP       =   Operating HP for system

0HPI      =   Operating HP for each incinerator in system

0RH       =   Overall reactor height, ft

PAPH      =   Pounds ash generated per hour of operation, #/hr

PCI       =   Preheater maximum heat transfer rate to air from exhause
              products l400°F inlet to 400°F exit, C  = const., Btu/hr

PC2       =   Preheater maximum heat transfer rate to raise air temperature
              to 1000°F, Btu/hr

PC3       =   Allowable maximum heat transfer in air preheater JLimited. by
              PCI or PC2, Btu/hr

-------
PCDB      =   Percent dry solids/100, # dry solids/# sludge

PCTY      =   Fraction of year, week or month to be operated, hrs operated/
              hrs yr (total hrs, not work hrs)

PDB       =   Pounds of dry solids per hour capacity of system, #ES/hr

PDBI      =   Pounds of dry solids per hour capacity of each incinerator
              in system, #DS/hr

PDBC      =   Pounds of dry solids under consideration from sludge elemental
              analysis considered, #

PH20      =   Percent HO in sludge

PPH20     =   Pounds HO under consideration from sludge elemental analysis
              considered, #

PS        =   Total pounds of sludge from sludge elemental analysis
              considered, #

PV        =   Plenum volume for each incinerator, ft

PVS       =   Percent volatile solids in sludge, ^weight

P0VS      =   Pounds volatile solids under consideration from sludge
              elemental analysis, #

PVSH      =   Pounds volatile solids/hr capacity of system

PVT       =   Theoretical product volume, moles combustion products from
              system
          =   Moles combustion products @ k% excess 02 from system

QAIR      =   Input heat from combustion air @ 6o°F, Btu/# sludge

QE        =   Heat content of combustion products and inerts leaving
              incinerator at l400°F, Btu/# sludge

QF        =   Heat required from fuel to burn sludge adiabatically with
              no preheat at lUOO°F and 4.0$ excess 0p, Btu/# sludge

QFP       =   Heat required from fuel and preheat to burn sludge at
              ltOO°F (QF + OPE), Btu/# sludge

QFU       =   Higher heat of combustion of fuel, Btu/# fuel

QL        =   Heat loss from combustion system by radiation and convection,
              which must be supplied by the heat of combustion, Btu/# sludge

CJLE       =   Heat loss from pilot test combustion equipment by radiation
              and convection, Btu/# sludge
                                    66

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QLL

OPE



OS

QSL

SCP


SLR

SUN


SUMQ


TA


TCN0

THCP


THCFT


TSC

TSCD

TW
Calculated heat loss from A0 (neglecting radiation), Btu/hr

Heat supplied to preheated air during pilot test Tor fuel
determination, Btu/# sludge, or heat content of air entering
bee (0°F base)

Total sludge heat input (higher heating value), Btu/# VS

Total sludge heat input (higher heating value), Btu/# sludge

Heat content of sludge   6dcF (sludge considpr°d in elemental
analysis), Btu

Sand loss rate from bed, #/hr

Difference between heat content of exhause products   1^00°F
and heat input from sludge, fuel and air considered, Btu/# sludge

Total heat content of exhause products based on specific heats
@ 1UOO°F, Btu/# sludge

Contract ambient air temperature surrounding incinerator
(if unspecified, use 60°F), °F

System annual maintenance and operating cost, current dollars

Total heat content of exhaust products @ l400°F = SUM^/PS,
Btu/# sludge

Total heat input to sludge from combustion and supply air
and sludge, Btu/# sludge

Total system cost based on field data, dollars as of Feb., 1968

Total system cost based on Dorr curves, dollars as of Feb., 1968

Contract wall temperature of incinerator (use 200°F if unspecified),
VE

VS

XF


Y

ZI


ZII
Volume of expanded sand bed required, ft

Static volume of sand bed required, ft

Moles N5 in theoretical fuel and sludge air for sludge elements
(composition considered)

Excess moles 02 required to reach U$ excess 0g

Design pounds of volatile solids each fluidized bed incinerator
in the system handles, #VS/hr

Number of incinerators, in the system, required to handle the
slude capacity at no more than 1500 # VS/hr per incinerator
                                     67

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                               REFERENCES
1.   Dl Gregorio,D:, "Information Development for Waste  Treatment Processes",
     .Contract lU-12-60, FWPCA, Progress Report No.  11, May,  1968.

2.   Albertson, 0. E., "Low Cost Combustion of Sewage Sludges", Water
     Pollution Control Federation, October 8, 1963.

3-   Albertson, 0. E., "Fluidized Bed Combustion System", Patent  Filed
     December 8, 1966, Released January 30, 1968, Wo. 3,366,080.
                                    68

-------
                               BIBLIOGRAPHY
 1.   Anderson, T. B. and Jackson, R. ,  "A Fluid Mechanical  Description of
      Fluidized Beds", I & EC Fundamentals. Vol. 6, No.  k,  November 1967,
      p. 527-

 2.   Stevens, J. I., "Fluidized Bed  Incinerator:  R   for Handling  Oily
      Sludges", Water and Wastes Engineering, September  1966,  p. 82.

 3-   Narsirahan, G. ,  "On a Generalized Expression for Prediction  of Minimum
      Fluidization Velocity", A.I.Ch.E. Journal, May  1965,  p.  550.

 k.   Wen, C. Y. and Yr, Y. H., "A Generalized Method for Predicting the
      Minimum Fluidization Velocity".

 5-   Leung, P. K. and Quon, D. , "A Computer Model for Moving  Beds - Chemical
      Reaction in Fluid Phase Only",  The Canadian  Journal of Chemical
      Engineering, February, 19^5 > p. ^5.

 6.   "Fluid Bed Incinerators Studied for Solid Waste Disposal", Environ-
      mental Science and Technology , Vol. 2, No.  1,  July 1968, p.  595-

 7-   Fair, Geyer and Okun,  Water and Wastewater  Engineering  (Volume 2),
      John Wiley and Sons, Chicago, 1968.

 8.   Proudfit, D. P., "Selection of  Disposal Methods for Water Treatment
      Plant Wastes", Journal AWWA, June 1968, p.
 9-   Fair, G. M. , Moore, E. W. , "Heat and Energy Relations  in  the  Digestion
      of Sewage Solids", Sewage Works Journal, March 1932, p. 242.

10.   Owen, M. B., "Sewage Solids Combustion", Water and Sewage Works,
      October 1959-

11.   Millward, R. S., Booth, B. B., "Incorporating Sludge Combustion  into
      Sewage Treatment Plant", Water and Sewage Works,  168,  p.  R-169.


12.   Landrock, A. H., "Fluidized Bed Costing with Plastics: Technology
      and Potential for Military Applications", Plastics Technical  Evaluation
      Center, Picatinny Arsenal, Dover, N. J., January  196k, D. D. C.

13.   Gilbert, L. 0., "Organic Coating Using the Fluidized Bed  Technique",
      Rock Island Arsenal, Rock Island, 111., September 20,  1962, D.D. C.

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                           BIBLIOGRAPHY  ( CONT.)
27.   Smith, A. R., "Incineration of Sludge-Some Governing  Principles",
      Sevage Works Journal, Vol. II, 1939, p.  35-

28.   "Three Ways to Dispose of Sewage Sludge", Engineering,  24  November 1967,
      p. 828.

29.   Dayan, Y. et. al., "Heat Transfer Efficiency  in a Fluidized  Bed",
      The Canadian Journal of Chemical Engineers, December  1966, p.  330.

30.   Buckham, J. A. and Levitz, N. M. , "Fluidized  Bed Technology",
      A.I.Ch.E., 1966.

31.   Legler, B. M. , "Feed Injection for Heated Fluidized Beds", Chemical
      Engineering Progress, Vol. 63, Wo. 2, February 1967*  P-  75-

32.   Halwagi, M. and Gomezplata, A., "An Investigation of  Solids  Distribution,
      Mixing, and Contacting Characteristics of Gar-Solid Fluidized  Beds",
      A.I.Ch.E. Journal, Vol. 13, No. 3, p. 503-

33.   Geldart, D., "Gas-Solid Reactions in Industrial Fluidized  Beds",
      Chemistry and Industry, 13 January 1968, p. hi.

3k.   "Free Fall, Fluid-Bed Setup Gasifies Coal", C and EN, September 25,  1967,
      P- 72-

35.   Holmes, J. T. et. al., "Fluidized Bed Disposal of Fluorine", I and  EC
      Process Design and Development, Vol. 6,  No. k, October  1967, p.
36.    "I and EC Reports and Comments", Industrial and Engineering  Chemistry,
      Vol. 59, No. 10, October 1967,- p. 11.

37.    "Photography Shows Fluidized- Bed Properties", C and EN, October  23,  1967,
      P- 67.

38.    Priestly, R. J., "How Good is the Fluosolids Reactor", Rock  Products,
      "July  1965,  p. 72.

39-    Anderson, T. B.  and Jackson, R., "Fluid Mechanical Description of
      Fluidized Beds", Industrial and Engineering Chemistry, Vol.  7, No.l,
      February 1968, p. 12.
                                     70

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                           BIBLIOGRAPHY  (COM1.)


UO.   Romero, J. B. and Smith. D. W.,  "Flash X-Ray Analysis  of Fluidized
      Beds:, A.I.Ch.E. Journal. Vol. 11, No. h,  July  1965, p.  595.

ill.   Wolf, D. and Resnick, W., "Experimental Study of  Residence Lime
      Distribution in a Multistage Fluidized Bed",  I  and  EC  Fundamentals,
      Vol. k, No. 1, February  1965,  p. 77.

k2.   Jonke, A. A. , et. al., "Candidate  for Second-Generation  Fuel-Reprocessing
      Plants". Nucleonics, Vol. 25,  No.  5, May 1967,  p. 58.

1*3.   Petrie, J. C. and Black, D. E.,  "Dry Collection and Disposition of
      Solids from Fluidized Bed Off-Gas", Atomic Energy Division,  PhillJps
      Petroleum Company, Contract AT(lO-l)-205,  July  1964.

kk.   Sawyer, C. N., Kah, P. A., "Temperature Requirements for Odor Destruction
      in Sludge Incineration", Journal W. P. C.  F., Vol.  32, No.  12,  December 1960.

k^.   Ridgeway, K., Segovia Ing Quim, E., "Fluidization and  Gas Suspension
      Techniques in Pharmaceutical Manufacturing",  Manufacturing Chemist
      and Aerosol News,  December 1966.

k6.   Marks, L  S., "Mechanical Engineers Handbook",  Fifth Edition,  McGraw-
      Hill, p. 733-

kj.   DiGregorio, "Information on Development for Waste Water  Treatment
      Processes", Contract 1^-12-60  FWPCA, Progress Report No.  11,  May 1968.

U8.   Albertson, 0. E., "Low Cost Combustion of  Sewage  Sludges",  Water
      Pollution Control Federation,  October 8, 1963.
                                     71

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            PATENTS FOUND ON FLUIDIZED BED INCINERATOR EQUIPMENT
1.   Albertson, 0. E., "Disposal of Waste Material by Combustion in an
     Inert Fluidized Bed", Filed March 31, 196U, Released May 16, 196?,
     No. 3,319.587-

2.   McKay, J. B., "Reactor Furnaces", Filed June 26, 1951, Released
     August 16, 1955, No. 2,715,565.

3.   Booth, P. B., "Gas Scrubber", Filed August 27, 1958, Released
     June ll*, I960, No. 2,9^0,51*0.

k.   Doyle, H.j "Gas Scrubber", Filed April 12, 19^9, Released December  16,
     1952, No. 2,621,75^.

5.   Albertson, 0. E., "Waste Burning System with Internal Screen
     Deliquifiers", Filed April 23, 1966, Released April 2, 1968,
     No. 3,375,79^.

6.   Albertson, 0. E., "Fluidized Bed Combustion System", Filed December 8,
     1966, Released January 30, 1968, No. 3,366,080.
                                        72

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