-------
In order to build up the solids content of the slurry fed  to the
filter, dry lime cake from refuse disposal piles was reconstitu-
ted and was used as a means of retarding the settling rate of the
sand fractions and as a filter aid.  The effect of solids on
filter yields is shown in Figure 4.  The solids added were of
such fine particle size that they aided filtration mainly by
keeping the coarser sand fractions in suspension and thus formed
a more permeable and firm cake.  Pilot runs later with the belt
filter gave good filter yields without the use of reconstituted
lime mud if the solids were concentrated to 15-20 percent in the
thickener.  See Table 9,
                                   I    «    I
                                 22.8% Solids
                                 89
                                 12 in. Hg Vac
                                          11  12
Figure  5«  Filter  yields vs pH of filter feed at constant
           percent solids, temperature and vacuum
                             29

-------
The addition of slaked lime to control pH nad a very great effect
on the filter yields.  In this series of experiments the alkaline
underflow from the clarifier was adjusted to a pH of 5*5 by the
addition of acetic acid and then adjusted to increasing pH values
by addition of calcium hydroxide.  The 3-5 ml/gal, of calcium
hydroxide slurry necessary for pH adjustment was insufficient to
affect the solids content of the slurry appreciably*  Increased
addition of lime as indicated by higher pH values increased the
filter yields very markedly as shown in Figure 5.

The effect of temperature on the filter yields at two pH values
are shown in Figure 6 for a solids content feed of 25.8 and 34*5
percent*  Increase in temperature resulted in an increased filter
yield and again the higher filter yield was at the higher pH
value.
                  40

                  36

                  32
O
D
34.5% Solids
25,9% Solids
                 a
                  24
                 £20
                 £
                 t-H
                  12


                   8

                   4

                   0
                                         10  11  12
Figure  6,  Filter  yields vs pH and  temperature at constant
           solids  concentration and 15 in. Hg vacuum
                             30

-------
Figure 7 shows  the  effect  of  temperature and polyelectrolyte on
the filter  yields at  two pH values  at  a solids content of 28
percent and 19,2 percent for  the feed  to the filter.  The higher
temperature and pH  values  again improved the filter yield.  The
pH adjustment was made with calcium hydroxide and  the increased
filter yield may have been due to the  coagulating  effects of
lime rather than pH as such.  The addition of 1 ppm Betas 142O
anionic polyelectrolyte further increased the filter yields.
                       - 23.0% Solids, 1O.5 pH

                     g- 18.2% Solids,  9.5 pH  -
                   3O  40  50  6O  70  80
                              TEMP °C
Figure 7.  Effect of temoerature and polyelectrolyte on filter
           yield at constant solids concentration, pH and
           15 in. Hn vacuum
                            31

-------
The best filter conditions  were obtained  on clarifier
underflow at pH of 1O.5 or above, treated with an anionic polymer,
thickened to a solids concentration above 2O percent and heated
to 90 °C and filtered at a vacuum of approximately 15 in. Hg.
The maintenance of a high pH with lime treatment appears to have
the greatest influence on f ilterability.  High solids concentra-
tion is necessary for satisfactory filter yields because of the
rapid blinding of the filter media from fine particles and
bacterial sliraes.  Satisfactory filter yields may be obtained
at low temperatures under ideal conditions, but high temperature
always improved filter yields.

Pilot Filter Units

Results of filtration trials with the three pilot units during
the 1970-71 test period were unsatisfactory until the final day
of operation for various reasons as discussed below.  No data were
obtained during the 1970-71 season.  Data from pilot filtration
during the 1971-72 season is presented in the section on pilot
filtration.

Tnitial lab tost leaf studies conducted in early campaign of 1970
indicated that satisfactory filter cakes could be obtained without
extensive clarifier underflow treatment other than further thick-
ening.  Delayed procurement and construction schedules delayed
pilot unit tests until mid December »  Low pH in the clarifier
with accompanying bacterial slime formation accounted for poor
filtration characteristics of the underflow during the 1970-71
tests o

Tnitial trials with the EIMCORELT filter were unsatisfactory,
with filtration rates ranging from O.1OO to O.422 gpm/sq ft of
filter drum area.  These poor results were attributed to low
solids, low temperature and low pH of the feed to the filter.

Trials with thp pre-coat drum filter resulted in rapid blinding
of the pre-coat surface with very slight cake pick-up.  A filtra-
tion rate of 4.5 gpm/sq ft at the end of the pre-coat cycle
dropped to .4 gpm/sq ft with thickened transport water solids.
The pre-coat filter appeared to have no advantages over the cloth
drum f ilter o
Tho RMD pressure leaf filter discharged filter cake from the leaf
by shock vibration on sional from a sensing device for sensing
predetermined cake thickness.  If the filter blinds before suffi-
cient cake thickness builds up, the thin cake does not discharge
                             32

-------
freely from the filter media.  The discharged cake falls to the
bottom of the pressure vessel, where it is repulped and pressure
discharged on signal from a density sensor.  The BMD pressure leaf
filter, equipped by the supplier with monofilament filter cloth,
was operated at 0.04 gpm/sq ft filter rate.  Rapid cloth blinding
and pressure build-up with resultant short cycles resulted with
low solids and low temperature feeds.  The addition of waste lime
mud to the thickener underflow at volume ratio of 1 part lime mud
to 4 parts underflow and elevated temperatures increased the cycle
lengths.  The nature and design of the test filter required the
recycling of the filter feed through the force pump system.  This
resulted in breaking up the floe formed in the coagulation and
thickening process with a resultant loss in filtration rates.
The BMD discharge varied from 40 - 5O percent solids.  Better
filtration rates may have been obtained had multifilament filter
media been available.

Of the three pilot filter units tested, the EIMCOBELT vacuum
filter was the most practical unit for evaluating the filtration
characteristics of the transport water solids, in that it pro-
vides for continuous cloth washing and visible cake, and rapid
clean up between varying test conditions.  Satisfactory filter
yields achieved on the last day of the 1970-71 campaign were the
basis for continuation of the studies during the 1971-72 campaign.

Pilot Filtration

A. series of 89 test runs covering 18 days of plant operations
during the 1972 campaign was made with an EIMCOBELT pilot model
filter with 3 ft diameter by 1 ft wide drum.  Test results were
tabulated under four different operating conditions:

     A:  Main clarifier underflow with pH adjustment followed by
     ""   additional thickening in the ENVIROCLEAR pilot thickener
         and temperature adjustment of the final underflow.  Data
         tabulated in Table 9.

     B:  Main clarifier underflow with pH adjustment followed by
     ""   additional thickening in the ENVIROCLEAR pilot thickener
         and additional solids added as reconstituted waste lime.
         Data tabulated in Table 10.

     C:  Main clarified underflow with pH adjustment followed by
     ~"   additional thickening in the ENVIPOCLEAR pilot thickener
         and additional solids added as lignite fly ash.   Data
         tabulated in Table 11.
                               33

-------
     D:  Main clarifier underflow and additional thickening with
         the addition of all of the lime cake from juice purifi-
         cation to the main clarifier.  Data tabulated in Table
         12.

The feed to the filter came directly from the underflow of the
115 ft main clarifier with the provision also that this underflow
could be thickened further in a pilot model BNVIROCLEAR thickener*
A heating tank was installed between the thickener and the filter;
chemical treatment or addition of filter aids could be done in
this heating tank, which was equipped with an agitator*

In the recycling of transport water organic matter builds up to
levels favorable for bacterial growth.  In order to keep bacteri-
al growth under control slaked lime was added to maintain a 10 -
11*5 pH.  When the pH did lower unavoidably below 3 because of
bacterial growth the slime formation adversely affected the fil-
tration rate*  Other variables such as percent solids, tempera-
ture and vacuum interacted at times so that it was difficult to
separate cause from effect*

Easily filtered material also dried quickly in the dewatering
segment of the filter and cracked to such an extent that high
vacuum could not be maintained*  The vacuum for best cake pickup
sometimes was at 8 - 1O in* Hg vacuum.  The vacuum pump was a wet
type pump and the supply of water to the building housing the
filter was through a single pipeline.  The supply could be either
hot or cold.  It was found that hot water was desirable for clean-
ing the filter belt after discharge of the cake but if this water
was  used through the vacuum pump the vacuum was several inches
less than when cold water was used.

The addition of slaked line at the rate of O.31 Ibs per 1O gal.
of underflow from the main clarifier to raise pH, and additional
thickening in the ENVIROCLEAR pilot thickener before filtration
resulted in satisfactory cake pickup and cake separation from the
belt when filtered on the EIMCOBELT filter.  During the few in-
stances of poor cake pickup it was noticed that temperatures were
down and also pH values had decreased.  This latter effect was
due to a lack of sufficient lime and, as in the filtration with
the leaf filter, lime was observed to be beneficial in filtering
with the belt filter.  Data for this series is shown in Table 9.
Betz 1420 anionic polyelectrolyte at 2 ppra was added to  the thickener for
all tests unless otherwise noted in the data tabulation*
                             34

-------
Table 9.  FILTER YIELDS WITHOUT ADDITION OF FILTER AIDS



Temp
Run
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
* No
PH
12
12
12
12
10*9
10.9
10.9
10.9
10.9
10.9
6.5
6.5
12.1
12.1
12.1
12.1
12.1
12.1
11.8
11.3
11.3
9.9
9.9
9.9
11.8
11.6
polymer
°C
82
60
62
78
90
80
70
57
65
60
33
85
45
85
70
95
93
85
66
95
70
75
95
95
77
90
Feed
Percent
Solids
13.3
13.3
13.3
13.3
16.2
16.2
16.2
16.2
16.2
16.2
8.1*
8.1*
8.1*
8.1*
8.1*
8.1*
8.1*
8.1*
11.2
15.1

18.5


17.6
20.9
Vac
in.
Hg
11
10
9

9
11
10
16
10
10
11
11
10
8
10
14
15
16
14
16
17
17
17
18
15
15

Dry Cake
Lbs/Sq Ft/Hr
4.4
4.5
3.6
3.1
6.5
8.5
6.4
5.8
4.4
4.6
Cloth Blinded
Thin Wet Cake
Thin wet Cake
5.7
6.0
5.4
5.1
5.0
3.6
7.3
3.5
2.8
3.7
5.3
7.1
11.4
Additions to
Thickener
Underflow
None
it
ti
ti
ti
»
t»
u
ii
ii
it
it
u
it
u
u
it
ti
it
it
ti
it
u
it
it
u
added to thickener
In operating condition B, (Table 1O) the underflow from the main
clarifier was run to the thickener and then treated with addi-
tional lime solids from dry waste lime cake reconstituted in the
thickener underflow to increase the solids content.  The pH was
controlled by the addition of calcium hydroxide.  The cake pitikup
                            35

-------
was variable but, except for the beginning of a day*s filtration,
was very good.  The additional solids increased cake pickup.
Table 10.  FILTER YIELDS WITH RECONSTITUTED WASTE LIME ADDITION



Run
31
32
33
34
35
36
37
38
38A
39
39A
40
41
42
43
44
45
46
47
48
49
50
51
52



J2«-
10.9
10.1
11.2
11.2
12.0
12.0
12.1
12.1
12.1
1005
10.5
12.2
12.3
12.1
12.3




11.6
12.0
12.3

12.3


Temp
°C
85
90
87
8O
75
78
95
95
95
95
9O
80
85
95
80
9O
90
90
95
9O
95
95
95
94

Feed
Percent
Solids
19.9
22.2
28.0
29.0
17.0
17.0
11.0
11.0
11.0
11.0
11. O
2O. 6
17.8
13.6
19.4




24.6
29.9
28.0

25.6

Vac
In.
Hg
17
17%
17
18
10
15
14%
14
9
15
16
14
11
12
12
16
17
17
16
17%
17
16%
16%
15


Dry Cake
Lbs/Sq Ft/Hr
4.1
3.9
6.3
5.1
11.6
6.4
3.5
7.4
6.7
2.3
4.1
11.2
10.8
9.2
1005
3.4
4.3
8.8
5.1
4.7
7.8
10.1
9.1
9.6
Waste Lime
Additions to
Thickener
Underflow
Lbs/4O Gal.

10
2O
30
30

2O
10
10
20
2O
20
20
20
10
10
10
20
20
10
20
20
10
10
The addition of fly ash under operating condition C, (Table 11)
after additional thickening of the main clarifier underflow and
adjustment of pH with lime was effective as a filter aid although
it does not appear to be significantly different than equal
amounts of reconstituted waste lime filter cake.
                              36

-------
Table 11.  FILTER YIELDS WITH PLY ASH ADDITION
Run   pH
53
54
55
56
57
58
59
6.0
61
62
63
64
65
66
67
12.4
12.0
12.4
12.4
12.5
12.3
11.9
1107
11.8
12.1
12.0
12.1
12.0
           Temp
95
95
95
95
95
95
95
95
95
95
95
95
90
80
80
             Feed    Vac
            Percent  in.    Dry Cake
            Solids   Hg   Lbs/Sq Ft/Hr
          6.0

         10.0
         12.6
         11.7
          9.1
14%       4.6
17%       4.3
16%       3.2
17%       5.2
11        6.1
10        7.5
12        8.4
24.8
24.0
24.4
22.5
21.6
22.4

16
16
10
11
16
17
16
17.6
29.0
26.0
26.2
18.0
19.6
21.0
(1J  2O0 Waste lime substituted for fly ash
(2)  1O# Waste lime substituted for fly ash
(3)   5# Waste lime + 5# fly ash
  Fly Ash
Additions to
 Thickener
 Underflow
_ Lbs/40 Gal.

     1O
     10
     10
      5
      2.5
     None
     None
     10
     10
     10
     10
     (1)
     (2)
     (3)
     10
Under operating condition D, (Table 12), the addition of all of
the lime filter cake resulting from juice purification to the
clarifier and the adjustment of the pH with calcium hydroxide
and additional thickening in the thickener resulted in a filter
feed which filtered at a higher rate than any other combination.
The solid cake was friable and non-sticky and the pickup was much
better than that when waste lime or fly ash were used as filter
aids.  Decreasing the temperature decreased cake pickup as shown
in run No. 70 and 7OA.  When both the temperature and pH were
lowered the cake pickup was very poor as shown in run No. 72.
                                37

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Table 12.
FILTER YIELDS WITH WASTE LIME FILTER CAKE FEED TO
MAIN CLARIFIES

Run
68

69
70
70A
71
72
73
74
75

12.1

12.0
12.1
12.1
11,3
7.0
11.4
11.5
11.6

Temp
PC
95

90
64
40
30
60
80
95
87
Feed
Vac
Percent In.
Solids Hg
23.6

19.8
11*6
11.6
8.0

26. O
21.4
15.8
14

11
8%
1O^
8

14
14
16%

Dry Cake
Lbs/Sq Ft/Hr
16.3

11.1
9.8
8.7
9.3
Thin Wet Cake
10.8
12.6
9.5

Additions
Lime Cake to Main
Clarifier
it
it
it
it
it
it
it
it
Cake yields of 4 Ibs/sq ft/hr, dry basis, produced cakes of 1/16
in. thickness which discharged freely from the filter media at
5O percent moisture or less.  Tt would appear from the data pre-
sented for the p^lot filter and comparing lab test leaf data with
filter yields on the belt filter that the lab test leaf filter
was much more effective in terms of pounds of dry solids per hour
square foot.  The data for the belt filter was calculated on the
basis of total drum area rather than area submerged and conse-
quently is about 2/3 less than it would be if calculated on the
basis of area forming cake.  The filter yields in the two types
of equipment were roughly equivalent when calculated on effective
filter area.

The conditions of the filter feed which produced the best filter
yields were pH above 11, solids concentration above 2O percent
a.nd temperature above 80 °C.

Additional analytical data on the thickener overflow and under-
flow are shown in Appendix C, Tables X - XII.

FILTER CAKE DISPOSAL STUDIES

Filter cake solids from pilot filtration studies had moisture
contents ranging from 40.O to 50.O percent as shown in Appendix
C, Table XIII.  The results of the filter cake decomposition
                              38

-------
 studies are shown in Table 13*   Odors  of the filter cake  as  pro-
 duced were characteristic of damp soil with a slight beet odor.
 No strong, foul,  or  objectionable odors were detected in  the
 cake as produced  at  any time. Mold growth was evident in the
 2 ft deep   windrows.
 Table 13.
DECOMPOSITION OF FILTER CAKE SOLIDS, ANALYSIS FOR pH,
TOTAL N, VOLATILE SOLIDS AND COD
Original Filter Cake
Sanitary Land Fill
Windrow at 2 ft Depth
Spreading at 6 in. Depth
Date
**
5-23-72
4-25-72
5-8-72
5-23-72
4-25-72
5-8-72
5-23-72
Total N Vol Solids COD
PH % » % * ppn
1O.4
9.2
9.0
9.4
9.1
9.2
9.6
9.4
O.39
O.25
O.42
O.36
0.37
O.43
0.41
O.41
15.8
11.3
14.8
13.3
13.3
14.7
14.0
12.7
146OOO
172OOO
*»
143000
129000
1460OO
141OOO
* Percent by Wt on Dry Substance
*» Average of two composites of 18 daily frozen composites of 82
   individual samples
Distribution of the filter cake solids were made in January under
frozen conditions.  Sampling for decomposition studies was done
first on April 25th, and- at two week intervals thereafter for 6
weeks.  The land fill site was still frozen at sample depth on
the May 8th sampling and the high water table at the site resulted
in unsatisfactory sampling.  The trench for the land fill had
partially filled with water and frozen before the filter cake
solids were dumped and covered.  The lower levels of total nitro-
gen and volatile solids found in the land fill sampled on May
23rd may be attributed to leaching from   the high water table
present at the site.
                                39

-------
No significant change was found in the total nitrogen levels in
the samples for windrow distribution at 2 ft depth or spreading
at 6 in. depth, indicating no significant release of volatile
nitrogen compounds,  A reduction of 16 percent of the volatile
solids in the filter solids in the 2 ft deep  windrow and 2O
percent reduction in the volatile solids spread 6 in. deep
indicate that decomposition was progressing, but at a rate slow
enough to permit oxidation of odorous compounds by the atmos-
phere.  Test data indicates that the sanitary land fill method
of disposal would not be necessary for the control of odors from
the filter cake solids.
                              40

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                           SECTION VI

            UTILIZATION OF PHASE I RESULTS (PHASE II)


FULL SCALE FILTRATION DESIGN

The schematic flow diagram for a full scale operation of a trans-
port water solids dewatering system by filtration is as shown in
Figure 1 for the primary clarification step and in Figure 2 for
the secondary thickening and filtration steps,  (For detailed
flow diagram see Appendix B).

To minimize the amount of water accumulated for treatment from
the transport recycle system it is necessary to minimize both the
quantity of water within the recycle system and the volume of
blowdown (clarifier underflow) from the system.  Since the system
is already installed there is little that can be done to reduce
the volume of water contained within the system.  The quantity
of blowdown should be regulated to maintain a uniform density of
solids in the underflow.  In order to accomplish this, the volume
of make-up to the recycle system must be equal to the volume of
underflow removed from the system.  This can be accomplished by
regulating the amount of in-plant water streams entering the
recycle system.

The design of the secondary thickening and filtration installa-
tion is based on the following factors:

     Length of Operating Season                  ISO Days

     Tons of Beets Sliced per Day                4OOO

     Average Mud Tare on Beets (Percent)          5

     Transport Water Flow Rate                   6OOO gpm

     Concentration of Solids in Clarifier
     Underflow (Percent)                         8

     Density of Clarifier Underflow              8.5 Ibs/gal.

     Flow Rate of Clarifier Underflow            410 gpm
                               41

-------
     Concentration of Solids in Secondary
     Thickener Underflow (Percent)               2O

     Density of Thickener Underflow              9.5 Ibs/gal.

     Flow Rate of Secondary Thickener Underflow  146 gpm

     Temperature of Secondary Thickener
     Underflow                                   25 °C

     Filter Capacity- (Lbs/Sq Ft/hr Dry Solids)  12

The clarifier underflow will be fed to a deaeration tank of a
15 ft dia by 4 ft 4 in. side wall ENVIROCLBAR thickener.  The
thickener will provide a 12,5 min retention time for the 41O gpm
feed from the clarifier.  Since pH control is provided in the
clarifier, no additional pH control should be required in the
thickener.  Milk of lime would be fed to the thickener deaeration
tank if necessary for pH adjustment.  Polymer addition to the
thickener feed will require two 125 gal. premix tanks with air
agitation, a O-2 gpm metering pump and a 10 gpm dilution pump.

Addition of filter aids to the thickener underflow may not be
required.  Provision for the addition of waste lime mud to the
thickener feed will be provided for by direct pipe line of waste
lime mud from factory production as required.  No additional
handling cost for waste lime mud as a filteration aid would be
incurred.

Thickener underflow will be pumped to the filters by a 175 gpm
diaphragm sludge pump.  Dpnsity control of the underflow will be
an integral part of the ENVTPOCLEAR thickener provided by the
supplier.  Thickener overflow will be returned to the clarifier
or to the transport mud pond as necessary for level control of
the clarifier.

Heat requirements to raise the thickener underflow from 25 ^C to
9O °C are 8-1O million British Thermal Units (RTUs) per hour.
Direct steam injection provided the most efficient heat transfer.
Direct, in line steam injection in the filter feed line will pro-
vide the least expensive heat exchange mechanism.  Steam will be
supplied from existing plant facilities,  in the event that
direct steam injection reduces the filter yields below acceptable
levels from excessive dilution or attrition of particle agglom-
erates formed during clarification and thickening, an indirect
heat exchanger would be provided.
                                42

-------
Filter requirements for 4OO,OOO Ibs of dry solids per day and a
filter cake rate of 12 Ibs per sq ft per hour are 1,388 sq ft of
filter area.  Three 12» x 12* rotary filters provide 1,362 sq ft
of filter area.  Filter cake discharge from the filter will be
conveyed by belt conveyor to a dump truck for truck haul to the
disposal area and dumped in windrows.  Filtrate from the filters
will be returned to the transport water system.

ECONOMIC EVALMATION OF FULL SCALE SYSTEM

Cost data for a complete separation, dewatering and disposal of
sugarbeet transport water solids by filtration is presented under
two categories, the primary clarification and closed loop recir-
culating system which is currently in use, and the secondary
thickening, filtration and disposal system as developed for this
project.

Cost data for the primary clarification system and transport
water recycling are:

Capital Costs:

                                                        Cost
                                                      Dollars
                  Item                                 (1971)

     1-  3- 6 ft x 12 ft Vibrating Screens with
         Trash Disposal System- Material and
         Installation                                  38,175

     2-  Housing for Screens                           24,150

     3-  1- 115 ft dia x 8 ft Sidewall Clarifier
         Material and Installation                    109,7OO

     4-  Lime Treatment System: 1- 10 ton/day
         Lime Slaker and Pump- Material and
         Installation                                  10,500

     5-  2- Clarified Water Recirculatino Pumps
         and Motors- Installed                         12,300

     6-  2- Clarifier Underflow Mud Pumps and
         Motors                                         4,3OO

     7-  Clarified Water Sump and Housing for
         Water and Underflow Pumps                     38,175

-------
     8-  Electrical Systems- Material and
         Installation                                  25,OOO

     9-  Piping                                        40,500

                  Total Capital Costs                 302,800


Operating Costs:

                                                       Cost
                                                      Dollars
                  Item                                 (1971)

     1-  Power: 155 HPH x .745 = 119.2 KWH
         119.2 KWH x 24 H x 1.83^/KWH x ISO days ~      7,853

     2-  Utilities (Heat and Lights at $15/day)          2,25O

     3-  Maintenance and Repair                         4,500

     4-  Operation (1 Man Day at $3/hr)
         $3.00 x 24 x 150 =                            10,800

     5-  Chemical
         Lime- 1Q T/day at $7.OO/ton x 150             1O,5OO

     6-  Administration and Supervision
         at 1O?B of Labor Cost                           1,O8O

     7-  Amortization of Capital Costs (15 Years)
         $302,800 at 7 percent Interest                33,245

                  Total Annual Operating Costs         7O,228

                  Total Annual Operating Costs
                  Per Ton of Beets

                              = 11.71 cents (jrf)/ton
                  4,OOO x

Tho above cost data do   not include taxes, land acquisition for
and construction of waste water ponds, waste water pumping sta-
tion, separation of condenser water and transport water loops,
and engineering costs.

Cost estimates for the secondary thickening filtration and dis-
posal system are:
                                44

-------
Capital Costs:
                  Item

     1-  Building- 60 ft x 24 ft

     2-  1- 15 ft dia x 4 ft 4 in. sidewall
         ENVIROCLEAR thickener
         Installation

     3-  2- 175 gpm Underflow Pumps with 5 HP
         Motors- Installed

     4-  Polymer Feed System

     5-
     6-
Heat Exchanger- Steam Injection at
1O Million BTU/hr

3- 12 ft x 12 ft Rotary Vacuum Filters
with Pumps and Receivers
Installation
     7-  Filter Cake Conveyor and Drive

     8-  Instrumentation
         Density Control
         Temperature and Flow

     9-  2- Clarified Water and Filtrate Pumps

    10-  Electrical System
         Material and Installation
                  Total Capital Costs
    11-  Piping
                                               Cost
                                             Dollars
                                              (1973)

                                              45,000
                                              41,088
                                              10,272
  2,350

    740


  l.OOO
179,000
 53,700

  2,5OO
                                               2,500
                                               3,000

                                               3,20O
                                               9,500

                                               3,5OO

                                             357,350
Operating Costs:
                  Item
     1~  Power:  198 HPH x .745 = 147.5 KWH
         145 KWH x 24 x 1.83^/KWH x ISO days
                                              Cost
                                            Dollars
                                              (1973)
                                               9,717

-------
     2-  Utilities (Heat and Light at $15/day)          2,25O

     3-  Maintenance and Repair                         5,OOO

     4-  Operation- 1 Man Day at $3.OO/hr              10, BOO

     5-  Administration and Supervision
         at 1O percent of Labor 'Costs                   1,O8O

     6-  Chemical
         Polymer at $15/day                             2,25O

     7-  Steam                                         19,2OO

     8-  Disposal of Filter Cake
         16.6 T/hr at 35^/ton (less than 1 mile)
         16.6 x 24 x .35 x 150                         2O,916

     9-  Amortization of Capital Costs (15 yrs)
         357,350 at 7 percent Interest                 39,235

                  Total Annual Operating Cost         110,448

                  Total Annual Operating Cost
                  Per Ton of Beets

                                       *«

Tha above analysis does not include taxes, land acquisition and
preparation of filter cake disposal area, annual maintenance of
disposal area, engineering costs, nor cost of an alternate direct
heat exchange system for heating thickener underflow.

Total annual operating costs for a complete separation, dewater-
ing and disposal of transport water solids by filtration are
ll,71*f + 18.41ff - 3O.12«? per ton of beets processed.  Assuming a
5 year average sugar content in beets of 14.8 percent in the Red
River Valley and a factory extraction of 75.4 percent, the annual
cost per hundred weight (cwt) of sugar would be:
              ^ft v  KA
             .140 X .754
                                46

-------
                           SECTION VII

                           REFERENCES
(1)  Fischer, J. H. and E.  H.  Hungerford.   "State-of-Art,
     Sugarbeet Processing Waste Treatment."  In:   Proceedings -
     Second National Symposium on Food Processing Wastes,  pp. 549-
     603.  Conducted March  23-26, 1971 in Denver, Colorado.   Co-
     sponsored by Pacific Northwest Water Laboratory,  U.S. Environ-
     mental Protection Agency, Corvallis,  Oregon  and National
     Canners Association, Berkeley, California.

(2)  Tsugita, R. A., W. J.  Oswald, R.  C.  Cooper,  and C.  G. Goleuke.
     "Treatment of Sugarbeet Flume Waste  Water by Lagooning:   A Pilot
     Study."  Journal of the American Society of  Sugar Beet Techno-
     logists, 15 (4):282-297.

(3)  Fischer, J. H. and W.  Newton II.   "Concentration  of Sugarbeet
     Wastes for Economic Treatment with Biological Systems."   Progress
     Report No. 1, Grant 12060 FAK.  Beet Sugar Development Foundation.
     Ft.  Collins, Colorado, September 1968.

(4)  American Society for Testing Materials.   "Standard  Methods of
     Particle Size Analysis of Soils,  ASTM D422-63."  In:  Part 11,
     1971 Annual Book ASTM  Standards,  1971.

(5)  Blankenback, W. W. and W. W. Willison.   "Chapter  21 - Environmental
     Problems.  Chemical Treatment."  In:   Beet Sugar  Technology.
     Second Edition (McGinnis, editor), pp.  649-650.   Robinson War-
     field Company, Ft. Collins,  Colorado,  1971.

(6)  Carruthers, A. and J.  F.  T.  Oldfield.   "Chapter 23  -  Microbiology
     and  Plant Sanitation.   Plant Sanitation Use  of Formalin."
     In:   Beet Sugar Technology,  Second Edition (McGinnis, editor),
     pp.  694-695.  Robinson Warfield Company,  Ft.  Collins, Colorado,
     1971.

(7)  Wintermeyer, A. M. and E. B. Kinter.   "Dispersing Agents for
     Particle Analysis of Soils."  In:  Laboratory Analysis of Soils;
     Grain Size and Liquid  Limit, pp.  1-14.   Bulletin  95,  Highway
     Research Board.  National Academy of  Science,  National Research
     Council, Publication No.  343, 1955.
                               47

-------
                        SECTION VIII

                        PUBLICATIONS
1.  Fordyce, I.  V.  and A.  M.  Cooley.   "Separation,  Dewatering,  and
    Disposal of  Sugarbeet  Transport Water Solids,"  Environmental
    Protection Technology  Series  EPA-R2-72-018.   Technical  Paper
    presented at the Third National Symposium on Food  Processing
    Wastes sponsored by the U.  S.  Environmental  Protection  Agency.
    March 28-30, 1972 in New  Orleans,  LA.

-------
                             SECTION IX

                              GLOSSARY
Slowdown  - A discharge from a system, designed to prevent a
buildup of some material, as in a boiler to control dissolved
solids*

Clarifier - A holding tank for the removal of turbidity or other
suspended solids from the suspending liquid.

Dewatering - Any process of water removal or concentration of a
sludge slurry, as by filtration, centrifugation, or drying.

Inter Campaign - The period of the year during which the factory
is not processing beets.

Polarization - Measurement of the optical rotation of a solution
by a polarimeter calibrated in International sugar degrees and
the measurement expressed as percent sucrose.

Polyelectrolyte - Long-chained, high molecular weight, synethe-
tic, water soluble, organic coagulants; also referred to as
polymers.

Transport Water - Water used to convey beets through a flume
from a receiving hopper to the factory for cleaning and process-
ing.

Waste Lime Mud - The washed calcium carbonate filter cakes,
including sludges from first and second carbonation.

Tare - Material which must be discarded.
                                49

-------
                    SECTION X

                    APPENDICES
Table II:
A.   Analytical Procedures

B.   Flow Diagram for Beet Transport  Water  System

C*   Data Tabulation

        Table I:     Main Clarifier Influent,  1971-72
                     Campaion Pilot Test  Period.  Composite
                     Sample Analyzed  for  pH, Settleable
                     Solids, Suspended Solids,  Filterable
                     Solids, COD,  BOD5

                     Main Clarifier Influent,  1971-72
                     Campaign Pilot Test  Period*  Composite
                     Sample Analyzed  for  Soluble CaO,
                     Total CaO, Total Sugar, Organic Acids,
                     Total P04-P

                     Main Clarifier Overflow,  1971-72
                     Campaign Pilot Test  Period*  Composite
                     Sample Analyzed  for  pH, Settleable
                     Solids, Suspended Solids, Filterable
                     Solids, COD,  BOD5

                     Main Clarifier Overflow, 1971-72
                     Campaign Pilot Test  Period.  Composite
                     Sample Analyzed  for  Apparent Sucrose,
                     Total Sugar,  Organic Acids, Total
                     PO4-P,  NH3-N, Organic- N

        Table V:      Main Clarifier Underflow, 1971-72
                     Campaign Pilot Test  Period.  Composite
                     Sample Analyzed  for  pH, Total CaO
                     and  i?«sidu«* on Evaporation
                                                     Page

                                                      52

                                                      54

                                                      56

                                                      57
58
Table III;
59
Table IV:
60
                                                      61
                       50

-------
Table VI:
Table VII:
Table VIII:
Table IX:
Table X:
Table XI:
Table XII:
Table XIlit
Filter Yields vs Percent Solids in       62
Filter Feed at Constant pH and Vacuum

Filter Yields vs pH of Filter Feed       62
at Constant Solids Cencentration,
Temperature and Vacuum

Filter Yields vs pH and Temperature      63
at Constant Solids Concentration and
Vacuum

Effect of Heat and Polyelectrolyte on    63
Filter Yields at Constant Solids
Concentration, pH and Vacuum

Combined Thickener Overflow and Filter   64
Filtrate.  Composite Samples Analyzed
for pH, Suspended Solids, Filterable
Solids, COD and BOD5

Combined Thickener Overflow and Filter   64
Filtrate.  Composite Samples  Analyzed
for Total Sugar, Organic Acids, Total
PO4-P, NH3-N, Organic- N

Thickener Underflow with Polymer         65
Addition Rate.  Grab Sample Analyzed
for pH, Total- CaO and Residue on
Evaporation

Filter Cake.  Composite Samples          66
Analyzed for pH, Moisture,  Organic
and Volatile Matter, and Total CaO
                       51

-------
                            APPENDIX A

                       ANALYTICAL PROCEDURES
ROD - Biochemical Oxygen Demand - "Standard Methods for the
Examination of Water and Waste Water" (hereafter referred to as
S.M.)  13th Ed., 1971> Pages 489-94  (All data are 5-day BOD (BODs)
unless otherwise noted)•

CaO - Soluble - An aliquat of filtered sample was titrated with
standard EDTA solution to the Hach Univer-I endpoint by the
procedure outlined in Hach Chemical Co. Catalogue No. 10, 1967,
Page 28-32.

CaO - Total - A ten gram sample is boiled with excess nitric
acid, cooled, made to volume and a filtered aliquat is titrated
with standard EDTA solution to the Univer I endpoint as for
soluble CaO.

COD - Chemical Oxygen Demand.  S.M. 13th Ed., 1971, Pages 495-99.

Organic Acids - Hach Volatile Acids Colorimetric Method.  Hach's
Water and Wastewater Analysis Procedures, Catalogue NO. 10, 1967,
Page 72.  Color compared photometrically with Bausch and Loxnb
Spectronic 20 at 51O millimicron wavelength against acetic acid
standards.

Pol - Direct polarization as read in a polarimeter calibrated
in international sugar degrees and expressed as percent sucrose.

Phosphate - Total PO4-P - S.M. 13th Ed., 1971,Page 530.  Stannous
chloride method.

Pesidue on Evaporation - S.M. 13th Ed., 1971, Page 535.

Filterable Solids - S.M. 13th Ed.,1971,Page 29O.  Glass fiber
filter disc.

Non Filterable Solids - S.M. 13th Ed.}Page 291.  Determination
made by difference between residue on evaporation and filterable
solids.
                                52

-------
Organic and Volatile Solids - S.M. 13th Ed., 1971,Page 536.

Percent Solids - Moisture loss determined by evaporation on
OHAUS direct reading moisture balance.

Settleable Solids - S.M. 13th Ed.; 1971, Page 539.

Suspended Solids - S.M. 13th Ed., 1971, Page 537.

NH-3-Nitrogen - Ammonia nitrogen.  S.M. 13th Ed., 1971, Page 222,
Section 132A and 132 B»  Ammonia determined colorimetrically by
Nesslerization.

Organic Nitrogen - S.K. 13th Bd., 1971, Page 468.  Kjeldahl-N
minus Amnonia-N,

Total Nitrogen - Methods of Analysis, AOAC, lOth Ed9> 1965,
Section 2.045, Page 16.

Total Sugar - Anthrone Method.  1 ml of filtered sample is mixed
with 5 ml of anthrone-sulfuric acid solution,  heated in a boiling
water bath for 1O minutes.  A color is developed which is pro-
portional to the amount of sugar present.  The absorbency of the
color is read on a colorimeter and compared with a graph of the
absorbency of standard sucrose solutions*
                                53

-------
                  APPENDIX B




FLOW DIAGRAM FOR BEET TRANSPORT WATER SYSTEM
                      54

-------
Ul
                                                                Dt$/NTEGR.&TFD
                                                                         Dw(Sr. No, B-2oe>K-Lty

-------
   APPENDIX C




DATA TABULATION
     56

-------
Table I.
MAIN CLARIFTER INFLUENT, 1971-72 CAMPAIGN PILOT TEST
PERIOD.  COMPOSITE SAMPLE ANALYZED FOR pH, SETTLEABLE
SOLIDS, SUSPENDED SOLIDS, FILTERABLE SOLIDS, COD,


Date
11-15
11-36
11-17
11-18
11-22
11-P3
11-24
11-25
11-29
11-30
12-1
12-?
12-6
12-7
12-8
12-9
12-13
12-14
12-15
12-16
12-20
12-21
12-22
12-23
12-27
12-28
12-29
12-30
1-3
1-4
1-5
1-6
1-10
1-11
1-X2
1-13


ES
6.5
6.5
7.6
7.3
5.7
5.3
6.1
6.3
6.4
6.8
6.5
8.0
11*9
12.0
11.4
11.6
11.8
11.8
11.4
ll.A
11.4
11.6
11.8
11.3
11.1
11.5
11.8
11.4
11. 7
11.2
11.6
11.1
11.4
9.5
11.8
11.2
Sett
Solids
ml/1
27
33
2
11
30
60
3ft
17
30
75
15
33
15
16
17
15
10
30
20
17

20
21
16
10
12
10
4
5
17
8
10
12
3
10
15
Susp
Solids
»g/l
640
121O
6flO
1420
1550
560
27O
320
630
520
650
590
440
500
850
1120
470
69O
170
670
510
510
490
700
129O
810
990
880
1370
1010
820
1130
1160
1360
1240
820
Filt
Solids
mg/1
9840
9130
9710
11410
11980
16O60
17450
17430
1232O
13660
11010
6500
8240
12650
662O
15360
12910
14630
17650
17670
13540
13550
12690
12950
1O96O
1O820
1043O
10130
1086O
1070O
11240
1072O
13290
11230
13330
12410

COD
mg/1





192OO




31360


39200
11760
19600


18360
19560

265OO
32640
8160
8160
16320
16OOO
16000

4OOOO
120OO
8800
7160
960O
14400
11850

BOD 5
mg/1





9600




96OO


105OO

1140O


9000
1220O
65OO
8300
69OO


5250
620O
91 SO

8100
9150
6310


69OO
8550
                  57

-------
Table TI.
MAIN CLAPIFIER INFUJONT, 1971-72 CAMPAIGN PILOT  TEST
PEP TOD.  COMPOSITE SAMPLE ANALYZED FOP, SOLUBLE CaO,
TOTAL CaO, TOTAL SUGAR, ORGANIC ACIDS, TOTAL  PO4-P


Date
11-15
11-16
11-17
11-18
11-22
11-23
11-24
11-25
11-29
11-3O
12-1
12-2
12-6
12-7
12-8
12-9
12-13
12-14
12-15
12-21
12-22
12-23
12-27
12-28
12-29
12-30
1-3
1-4
1-5
1-6
1-10
1-11
1-12
1-13

Sol CaO
mg/1
















800
690
700
900
75O
6OO
500
550
50O










Total CaO
mg/1
















1700
2000
1500
1800
1500
134O
1250
155O
1500

150O
1250
1100
100O
1500
5OO
1400
1000
Total
Sugar
(!)


2550
2200
7OOO
4800
5800
1O8OO
44OO
1330O
4600
aooo
312OO
3120O
1880O
237OO
18000
2200O
22OOO
19600
19600

180OO
180OO
16000

18000
18400
16400
154OO
16100
125OO
16700
17500
Organic
Acids
mg/1
1320O
64OO


2000
1400
16OO
2240
220O
50OO
3800
1200
4OO
40O
400
1OO
78O
1160
1620
128O
1360

10OO
720
840

1220
1160
1120
1060
1090
153O
1190
1120
Total
P04-P
mg/1


7.2
16.8
13.6
17. C
15. O
14.6

7.2
22.8
15.8
1.4
1.0
8.0
5.2

15.0
10.8
6.8
8.0
7.8
8.4
8.6
7.8
6.4
6.8
8.7
8.1
8.5
7.9
9.3
9.8
8.7
(1) Milligrams per liter as sucrose
                              58

-------
TABLE TIT.  MAIN CLARIFIER OVERFLOW, 1971-72 CAMPAIGN PILOT TEST
            PEPIOD.  COMPOSITE SAMPLE ANALYZED FOP pH, SETTLEABLE
            SOLIDS, SUSPENDED SOLIDS, FILTERABLE SOLIDS, COD, BOD5

Hate
11-15
11-1.6
11-17
11-18
1L-22
11-23
11-24
11-25
11-29
11-30
12-1
12-2
12-6
12-7
12-8
12-9
12-13
12-14
12-15
12-16
12-20
12-21
12-22
12-23
12-27
12-28
12-?.9
12-30
1-3
1-4
1-5
1-6
1-10
1-11
1-12
1-13

pH
6.5
6.5
7.5
7.2
5.4
5.4
5.6
5.9
5.9
6.4
6.4
6.4
11.9
12.0
11.7
11.4
11.5
11.7
11.3
11.3
11.3
11.6
11.9
11.4
11.1
11.5
11.8
11.6
11.2
11.1
11.3
10.6
11.4
9.2
nae
11.2
Sett
Solids
ml/1
2.0
1.0
0.2
0.5
Q»8
1.2
6.5
17.5
0.?.
0.5
0.7
0.4
0.4
0.7
1.0
0.5
0.1
0.5
0.2
0.5

0.6
0.6
0.4
0.1
0.1
0.2
0.4
0.1
0.1
0.5
2.O
O.6
0.5
0.4
0.4
Susp
Solids
mg/1
42O
540
230
540

600
480
300
170
24O
2OO
180
34O
240
370
56O
330
470
5OO
62O

40O
520
410
58O
46O
550
580
470
650
69O
830
670
620
580
44O
Filt
Solids
nig/1
10170
924O
994O
9290
11980
16940
17740
17030
13490
13600
13250
11520
12800
13970
1408O
15240
12840
15240
18880
14110

1392O
14240
11860
12360
11220
10820
1O480
11770
10790
1O820
10780
14400
14160
1324O
14560
COD
mg/1










31360


784O

7840

1248O
204OO
12490

2856O
3O6OO
204OO
1632O
8160
4OOO
4OOO

28000


932O
112OO
136OO
11060
BOD5
mg/1




1290O





850O


7500

8100


92OO
10900
725O
69OO
6650


5850
57OO
8250

60OO
8850
7500


660O
370O
                            59

-------
Table IV.
MAIN CLARIFIES OVERFLOW, 1971-72 CAMPAIGN PILOT TEST
PERIOD.  COMPOSITE SAMPLE ANALYZED FOR APPARENT
SUCROSE, TOTAL SUGAR, ORGANIC ACIDS, TOTAL PO4-P,
NH3-N, ORGANIC-N

Date
11-15
11-16
11-17
11-18
11-22
11-23
11-24
11-25
11-29
11-30
12-1
12-2
12-6
12-7
12-8
12-9
12-13
12-14
12-15
12-16
12-21
12-22
12-23
12-27
12-28
12-29
1-3
1-4
1-5
1-6
1-10
1-11
1-12
1-13
Apparent
Sucrose
(1)
.09
.04
006
.08
.44
olO
.24
.62
.18
.11
.OS
.30
.96
1.04
1.06
1.17
1«05
1.22
1.39
1035
1.03
1.00
.96
.82
.89
.81
.87
.85
.84
.84
1.01
1.09
.98
1012
Total
Sugar

2170
2170
22OO
58OO
48OO
5000
92OO
46OO
48OO
46OO
7800
3OOOO
348OO
188OO
22OOO
18000
22400
23OOO
19400
21400
21600

1880O
1880O
172OO
142OO
14400
16000
1580O
15900
1O5OO
14400
15800
Organic
Acids
tng/1
14000
5200


400
18OO
3800
172O
3600
12OO
62OO
3000
40O
4OO
4OO
20O
748
972
1348

1260
1200

740
62O
52O
1308
1240
1152
1100
1350
1800
950
1150
Total
PO4-P
mg/1


8.4
17.6
16.4
24.2
14.4


40. O
25.6
15.0
1.4
0.8
2.0
3.2
3.0
3.8
2.6
2.6
2.8
4.4
3.8
4.6
4.8
5.0
4.8
4.8
5.1
4.9
5.3
5.9
5.2

NH3-N
mg/1
3.7

3.7
3.7


4.6
1O.8

4.5
3.7
16.2


35.0
1506
16.2
21.2
23.7
27.5
20.0
31.2

22.5
26.7

27.5
21.2
23.0

22.4
24.0
22.3

Organic-N
mg/1
3.9

42.2
3.8


129.4
35.3

110.2
36.9
48.3


10.3
10.6
17.7
122.5
138.7
99.7
101.2
87.2

95. O
109.5

63.7
75.0
13.2

45.8
75.6
83.4
(1)  Direct Polarization as Percent Sucrose
(2)  Milligrams per liter as Sucrose
                             60

-------
Table V*  MAIN CLARIFIER UNDERFLOW, 1971-72 CAMPAIGN PILOT TEST
          PERIOD.  COMPOSITE SAMPLE ANALYZED FOR pH, TOTAL CaO
          AND RESIDUE ON EVAPORATION


Date
11-15
11-16
11-17
11-18
11-22
11-23
11-24
11-25
11-29
11-30
12-6
12-7
12-8
12-9
12-16
12-20
12-21
12-22
12-23
12-27
12-28
12-29
12-3O
1-3
1-4
1-5
1-6
1-10
1-11
1-12
1-13
1-14


£H
6.7
6.8
7.6
7.3
7.0
7.6
6.4
7.4
6.5
7.5
11.5
12.0
11.8
11.5
11.5
11.0
11.2
11.4
Ilo6
11.7
11.1
11.3
11.3
11.4
11.1
10.6
11.2
11.4
10.6
11.2
11.6
11.2
Total CaO
Percent
by Wt
1.3
1.7
1.5
1.3
1.4
0.5
0.4
O.6
0.5
3.0
0.9
O.8
0.5
0.4
0.2
0.5
0.5
0.4
0.5
0.6
1.2
0.3
0.7
1.1
0.8
0.4
0.3
0.5
0.2
0.4
0.4
0.5
Residue on
Evaporation
Percent by Wt
8.2
10.5
9.0
8.5

11.4
15.8
11.0
10.9
14.0
8.0
5.5
6.0
7.0
3.8
6.8
6.7
4.0
6.0
5.1
7.5
4.2
6.0
8.0
5.5
4.8
3.2
5.8
4.6
5.2
4.5
4.7
                            61

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Table VIo  FILTER YIELDS vs PERCENT SOLIDS IN FILTER FEED AT
           CONSTANT pH AND VACUUM (INCREASE IN SOLIDS CONTENT
           FROM DRY WASTE LIME SOLIDS)


£H
11.0
11.0
11.0
11.0
lloO
11 »0
11.0
11.0
Feed
Percent
Solids
15.0
17.3
19.5
21.5
23.5
23.5
23.5
23.5

Temp
°C
92
90
90
94
90
76
61
45

Vacuum
In. Hg
15
15
15.5
16
16
15.5
15.5
15

Dry Cake
Lbs/Sq Ft/Hr
2.1
6.7
10.4
13.8
18.4
18.8
16.3
<1

Table VII.
FILTER YIELDS
vs pH
SOLIDS CONCENTRATION


gH
5.5
6.5
8.7
9.4
10.0
10.8
11.2
11.7
Feed
Percent
Solids
22.8
22.8
22.8
22.8
22.8
22.8
22.8
22.8

Temp
«C
88
90
89
89
89
89
92
89
OF FILTER FEED AT CONSTANT
, TEMPERATURE

Vacuum
In. Hg
13
12
11.5
11.5
11.5
12.5
13
13
AND VACUUM

Dry Cake
Lbs/Sq Ft/Hr
3.8
4.1
8.7
10.7
14.6
17.8
21.2
23.4
                             62

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Table VIII
  FILTER YIELDS vs pH AND TEMPERATURE AT CONSTANT
  SOLIDS CONCENTRATION AND VACUUM


pH
6.6
6.6
10.9
7.2
7.2
11.0
11.0
Feed
Percent
Solids
34,5
34.5
34.5
25.8
25.8
25.8
25.8

Temp
°C
24
80
84
34
90
90
40

Vacuum
In. Hg
15
12
13
13
14.5
14
15

Dry Cake
Lbs/Sq Ft/Hr
9.8
18.2
30.9
3.2
5.2
23.8
13.7
Table IX.
EFFECT OF HEAT AND POLYELECTROLYTE ON FILTER YIELDS
AT CONSTANT SOLIDS CONCENTRATION, pH AND VACUUM


pH
10.5
10.5
10.5
9.5
9.5
9.5
Feed
Percent
Solids
28.0
28.0
28.0
19.2
19.2
19.2

Temp
°C
35
90
90
32
90
90
Polyelect-
rolyte
ppm (1)
0
0
1
O
o
1

Vacuum
In. Hg
16
15
16
14.5
14.5
12.5

Dry Cake
Lbs/Sq Ft/Hr
9.5
14.4
20.7
1.6
7.7
9.9
     (1) Betz 1420 (anionic)
                                63

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Table X.  COMBINED THICKENER OVERFLOW AND  FILTER FILTRATE.
          COMPOSITE  SAMPLES ANALYZED FOR pH,  SUSPENDED SOLIDS,
          FILTERABLE SOLIDS, COD AND BOD 5


Date
11-15
11-16
11-17
11-18
11-24
11-25
11-26
11-29
11-30
12-6
12-7
12-8


E«
11.0
11.9
10.0
9.8
11.4
11.3
12.3
11.4
11.9
1O.3
11.1
10.0
Susp
Solids
mg/1




230
22O
150
430
23O
380

230
Filterable
Solids
mg/1

1O09O
8720
1O720
13790
15140
1557O
14690
12500
1155O

7960

COD
rag/1




2352O
13200
3140


17840

1392O

BOD5
mg/1





745O
2400



7900
2750

Table XI.  COMBINED THICKENER OVERFLOW AND FILTER FILTRATE.
           COMPOSITE SAMPLE  ANALYZED FOR TOTAL SUGAR, ORGANIC
           ACIDS, TOTAL PO4-P, NH3^N, ORGANIC-N


Date
11-15
11-16
11-17
11-18
11-24
11-25
11-26
11-2Q
11-30
12-6
12-8
Total
Sugar
mg/1
4400
4400
2200
2170
52OO
7OOO
8800
5000
56OO
38800
13600
Organic
Acids
mg/1
12800
7200


1360
1440
1560
6OO
4200
4OO
20
Total
PO^-P
mg/1


1.8
3.8

3.4
2.O
11.0
12.4
3.4
5.2

NH3-N
mg/1

16.8
17.0
O.6
4.4
16.3
10.0
13.0
7.5

28.5

Total-N
mg/1

36.2
28.0
50.4
90.4
91.3
1OO.O
88.2
93.0

81.5
                                64

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Table XII.
THICKENER UNDERFLOW WITH POLYMER ADDITION RATE.
GRAB SAMPLE ANALYZED FOR pH, TOTAL CaO AND RESIDUE
ON EVAPORATION


Date
11-15
11-16
11-17
11-18
11-19
it
M
it
it
11-23
11-26
11-30
it
it
it
i»
12-1
it
12-5
12-6
t»
tt
12-7
12-8
it


pJH
12.3
12.0
10.9
12.1
11.8
11.3
9.9
11. S
11.6
10.9
12.3
12.1
12.0
12.1
12.1
11.3
11.4
11.5
11*6
11.4
11.2
11.1
11.3
11.6
11.5
Total CaO
Percent
by Wt
7.2
2.1
3.1
2.0





0.9
1.0
4.7
3.3
2.8
2.8
2.1
5.8
4.9
4.5
5.0
4.4
4.2
3.9
1.8
1.5
Residue on
Evaporation
Percent by wt
11.0
13.3
16.2
8.1
11.2
15.1
18.5
17.6
20.9
19.9
22.4
23.6
19.8
11.6
11.6
8.0
26.0
21.4
15.8
22.0
22.6
22.4
21.5
28.8
27.6
Polymer
Addition
mg/1 (1)
4
2
5
O
O
2
3
O
4
2
2
2
2
2
2
2
2
2
(*)
3
3
3
5
5
5
(1)  Betz #1420 anionic polymer
(*)  Betz #1260 cationic polymer  5 mg/1
                                65

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Table


Date
11-15
11-16
11-17
11-18
11-19
11-23
11-24
11-25
11-26
11-29
11-30
12-1
12-5
12-6
12-7
12-8
12-9
XIII. FILTER CAKE. COMPOSITE SAMPLES ANALYZED FOR pH,
MOISTURE, ORGANIC AND VOLATILE MATTER, AND TOTAL CaO


EH
12.1
11.9
10.6
11.3
10.4
11.3
11.4
11.7
12.4
11.4
12.1
11.1
10.5
10.5
10.5
1006
1O.4

Moisture
Percent (1^
46.6
48.3
42. 0
45.0
42.0
45. O
41.9
44.3
40.0
50.0
45.0
45.2
43.0
44.0
46.2
43.3
41.9
Organic and
Volatile
Percent (1)
6.4
6.7
6.5
6.8
5.8
6.3
5.7
7.0
7.6
4.8
5.4
5.1
4.9
6.7


7.2
Total
CaO
Percent (1)
9.3
8.8
9.3
8.8
8.0
7.6
7.8
6.9
5.8
7.5
9.2
8.3
9.8
8.9
8.0
5.0
7.6
(1)  Percent  by wt  on Original Cake
                               66

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                                   TECHNICAL REPORT DATA
                            (I'hvue read Instructions on the reverse before completing)
I. ntPORT NO.
    EPA-660/2-74-093
                                                           3. RECIPIENT'S ACCESSION NO.
4. TITLE AND SUBTITLE
    SEPARATION, DEWATERING  AND DISPOSAL OF
    SUGARBEET TREANSPORT WATER SOLIDS
             5. REPORT DATE
                December  1974
             6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)

    I.  V. Fordyce, A. M. Cooley
                                                           8. PERFORMING ORGANIZATION REPORT NO,
9. PERFORMING ORG \NIZATION NAME AND ADDRESS

    American Crystal Sugar Company
    P.O.  Box 419
    Denver, Colorado  80201
             10. PROGRAM ELEMENT NO.
                1BB037
             11. CONTRACT/GRANT NO.
                                                              12060 ESC
12. SPONSORING AGENCY NAME AND ADDRESS

   Pacific Northwest Environmental Research Laboratory
   National Environmental Research Center
   Corvallis, Oregon  97330
             13. TYPE OF REPORT AND PERIOD COVERED
                Final report	
             14. SPONSORING AGENCY CODE
IB. SUPPLEMENTARY NOTES
16. ABSTRACT
    The objectives of this study were to determine  the  settling characteristics  of
    solids from sugar beet washing and fluming operations  in a clarifier, the  filter-
    ing characteristics of the  underflow slurry from  a  clarifier and the disposal of
    the filter cake without subsequent development  of objectionable odors.  The  results
    of this study were to be  used to determine the  feasibility of installing full
    scale filters for filtration of and removal of  the  suspended solids from the trans-
    port water and complete recycling of water.

    Buildup of organic matter in the water and consequent  bacterial growth necessitated
    the maintenance of high pH  by addition of slacked lime.   It was necessary  a^so  at
    intervals to add paraformaldehyde to control bacterial growth.  Dosages are  given.

    Best conditions for filtration were obtained when,  the underflow from the  clarifier
    was heated, the pH was maintained over 10.5 and when the waste lime cake from beet
    juice purification was added to the feed to the clarifier.

    The filter cake which was accumulated was disposed  of  on farm land by three  differ-
    ent methods and did not develop objectionable odors in any of the methods used.
    fCoolev-Universitv of North Dakota)	;	
                               KEY WORDS AND DOCUMENT ANALYSIS
                  DESCRIPTORS
   Wastewater Treatment, Wastewater
   Quality Control, Water Reuse,  Industrial
   Waste Treatment, Treatment  Facilities,
   Pollution Abatement
b.IDENTIFIERS/OPEN ENDED TERMS  C. COSATI Field/Group
  Sugarbeet Waste Treat-
  ment,  pH Control, Coa-
  gulation, Filtration,
  Sludge Disposal
19. DISTRIBUTION STATEMENT

   Release Unlimited
19. SECURITY CLASS (This Report)
                                                                        21. NO. OF PAGES
20. SECURITY CLASS (Thispage)
22. PRICE
EPA Form 2220-1 (9-73)
                          U.S. GOVERNMENT PRINTING OFFICE: 1975-697-846/80 REGION 10

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