vvEPA
United States
Environmental Protection
Agency
EPA/540/SR-93/079
September 1993
SUPERFUND INNOVATIVE
TECHNOLOGY EVALUATION
Technology Demonstration
Summary
Resources Conservation
Company's Basic Extractive
Sludge Treatment (B.E.S.T.®);
Grand Calumet River,
Gary, Indiana
An evaluation of Resources Con-
servation Company's (RCC) Basic Ex-
tractive Sludge Treatment (B.E.S.T.®)*
pilot plant was conducted between July
1 and July 22, 1992, during a demon-
stration by the U.S. Environmental Pro-
tection Agency (EPA), under the
Superfund Innovative Technology Eval-
uation (SITE) Program. The demonstra-
tion evaluation was conducted in Gary,
IN; the material treated was contami-
nated river bottom sediments collected
from two locations within the Grand
Calumet River (GCR). The organic con-
taminants of concern were PCBs and
PAHs. Figure 1 shows the general lo-
cations of the demonstration test area,
test sediment collection points in the
GCR, and major regional features.
This demonstration was part of a co-
operative effort. In addition to the EPA
SITE Program, other agencies involved
included EPA's Great Lakes National
Program Office (GLNPO); the U.S. Army
Corps of Engineers (COE), Chicago Dis-
trict; and EPA Region V. The GLNPO
Assessment and Remediation of Con-
taminated Sediments Program through
the COE, in cooperation with EPA Re-
Mention of trade names and commercial products
does not constitute endorsement or recommenda-
tion for use.
gion V, arranged for the developer's
services and the location where the
demonstration was conducted.
GLNPO leads efforts to carry out the
provisions of Section 118 of the Clean
Water Act (CWA). Under Section
118(c)(3) of the CWA, GLNPO is re-
sponsible for undertaking a 5-yr study
and demonstration program of meth-
ods for the assessment and remedia-
tion of contaminated sediments. One
of the areas of concern for priority con-
sideration is the GCR. The COE (Chi-
cago District) has authorization (Rivers
and Harbors Act of 1910) to maintain
harbor channels by periodic dredging.
This includes the federal channel at
Indiana Harbor downstream of the GCR.
However, EPA has designated the bot-
tom sediments at various locations as
moderately polluted, heavily polluted
or toxic. As a result, materials to be
dredged from the Indiana Harbor and
Canal are not suitable for open-water
disposal in Lake Michigan. At the
present time, an environmentally ac-
ceptable disposal facility for dredged
materials from Indiana Harbor does not
exist. Consequently, dredging to main-
tain adequate navigation depths has
Printed on Recycled Paper
-------
not been conducted at this harbor since
1972.
The B.E.S.T.® Process is a patented
solvent extraction system that uses tri-
ethylamine at different temperatures to
separate organic contaminants from
sludges, soils, and sediments. The or-
ganics are concentrated in an oil phase,
thereby reducing the volume of wastes
that require further treatment. Multiple
extractions are conducted at predeter-
mined process conditions and are fol-
lowed by solvent recovery, oil polish-
ing, solids drying, and water stripping.
The use of triethylamine as the ex-
tracting agent distinguishes B.E.S.T.®
from other solvent extraction and soil
washing technologies. Triethylamine
has a property known as inverse misci-
bility. At temperatures below 60°F, tri-
ethylamine is miscible with water;
above 60°F, triethylamine is only
slightly miscible with water. Therefore,
at temperatures below 60°F, solids can
be dewatered and organic contaminants
can be extracted simultaneously. This
process is referred to as a cold extrac-
tion. Following cold extractions, the ex-
traction temperature is raised above
60°F, and any remaining organic con-
taminants are removed. These warm
and hot extractions are usually con-
ducted at temperatures ranging be-
tween 100°F and 170°F. The organic
contaminants initially present in the
sludge or soil are concentrated in the
oil fraction; additional treatment (e.g.,
incineration) is required to destroy or
immobilize these contaminants.
This Summary was developed by
EPA's Risk Reduction Engineering
Laboratory, Cincinnati, Ohio to an-
nounce key findings of a SITE Program
demonstration, which is fully docu-
mented in two separate reports (see
ordering information at back).
Introduction
The SITE Program was established in
1986 to promote the development and
use of innovative technologies to remedi-
ate Superfund sites. One component of
the SITE Program is the Demonstration
Program, through which EPA evaluates
field or pilot-scale technologies that can
be scaled up for commercial use. The
main objective of the demonstration is to
develop performance, engineering, and
cost information for these technologies.
This Technology Demonstration Sum-
mary highlights the results of an evalua-
tion of the effectiveness of the B.E.S.T.®
Process to remove PAHs, PCBs, and oil
and grease (O&G) from bottom sediments
collected from the GCR in Gary, IN.
Sediment B —
(Transect 6)
Figure 1. Regional location map.
Sample locations were chosen to obtain
two different sediment types, Sediment A
and Sediment B. Sediment A contained
high concentrations of metals and low con-
centrations of organic compounds, rela-
tive to Sediment B. Sediment B, collected
upstream from Sediment A, contained high
concentrations of organic contaminants
such as PAHs, PCBs and O&G.
Prior to the demonstration testing, both
sediment types were prescreened to sepa-
rate oversize materials and were thor-
oughly homogenized (mixed). Separate
bench-scale treatability tests were then
conducted on each of the sediment types.
These tests were performed by RCC
to determine initial operating conditions,
such as the number of extraction cycles,
to be used in the demonstration. A flow-
chart of the experimental design used to
guide the B.E.S.T.® evaluation is shown
as Figure 2.
The demonstration consisted of two
separate tests, one for each sediment type.
Each test consisted of two phases. Phase
I involved determination of the optimum
process variables from the results of three
runs, and Phase II consisted of two addi-
tional runs at the determined optimum con-
ditions. Samples of the untreated sedi-
ments, product solids, product water, and
product oil were collected during each of
the five runs (Phases I and II). These
samples were analyzed for total PAHs,
PCBs.and O&G. Product solids, product
water, and product oil were also anaylzed
for residual triethylamine solvent.
Results of the demonstration showed
that the process met (or exceeded) the
vendor's claims for organic contaminant
removal efficiency of £96% for treating
both of the test sediments. The analytic
results for Sediment A indicated that th.
process removed greater than 98% of the
O&G, greater than 99% of the PCBs, and
96% of the PAHs. The residual solvent in
River Sediment
Characterization Sampling
Collection of
River Test Material
Prescreening and
Homogenization
of Test Material
Bench-Scale
Treatability Tests
•e-
Demonstration
Tests
Figure 2. Experimental design flow diagram.
-------
the product solids and product water gen-
-rated from Sediment A was 45 mg/kg
.nd less than 2 mg/L, respectively. A final
oil product was not generated for Sedi-
ment A because of a lack of oil (less than
1%) in Sediment A feed. The analytical
results for Sediment B indicated that the
process removed greater than 98% of the
O&G and greater than 99% of the PCBs
and PAHs. The residual solvent in the
product solids, product water, and product
oil generated from Sediment B was 103
mg/kg, less than 1 mg/L, and 733 mg/kg,
respectively.
Process Description
The B.E.S.T.® pilot-scale system is de-
signed to separate organic contaminants
from soils, sludges, and sediments, thereby
reducing the volume of hazardous waste
that must be treated. Triethylamine is used
as the extracting agent because it exhibits
several beneficial characteristics. These
characteristics include:
• A high vapor pressure (therefore the
solvent can be easily recovered from
the extract of oil, water, and solvent
through simple steam stripping)
• Formation of a low-boiling azeotrope
with water (therefore the solvent can
be recovered from the extract to very
low residual levels, typically less than
100 ppm)
• A heat of vaporization one-seventh
that of water (therefore, solvent can
be recovered from the treated solids
by simple heat with a very low energy
input)
•Alkalinity (pH=10) (therefore some
heavy metals can be converted to
metal hydroxides, which can precipi-
tate and exit the process with the
treated solids).
The generalized B.E.S.T.® solvent ex-
traction process is shown in Figure 3.
Contaminated materials are initially
screened to less than 1/2-in diameter
(1/8-in for this demonstration). The
screened material is added to a refriger-
ated Premix Tank along with a predeter-
mined volume of 50% sodium hydroxide.
The Premix Tank is sealed, purged with
nitrogen, and then filled with chilled tri-
ethylamine solvent. The chilled mixture is
agitated and allowed to settle. The result-
ing solution from this cold extraction con-
sists of a mixture of solvated oil, water,
and solvent. The mixture is decanted from
the solids and centrifuged, and the sol-
vent and water are separated out of the
mixture by distillation.
The cold extractions are repeated as
additional feed is added to the Premix
Tank to accumulate enough solids to per-
form subsequent extraction cycles. Solids
with high moisture contents may require
more than one cold extraction. During this
demonstration, Sediment A (containing
41% moisture) required two cold extrac-
tions.
Once a sufficient volume of moisture-
free solids is accumulated, it is transferred
to the steam-jacketed Extractor/Dryer.
Warm triethylamine is then added to the
solids. This mixture is heated, agitated,
settled and decanted. The warm and hot
extractions separate the organics not re-
moved during the initial cold extractions.
Three products are derived from the total
process: product solids, product water, and
concentrated oil containing the organic
contaminants.
The pilot plant used for this demonstra-
tion is a self-contained mobile unit that
allows onsite testing to be performed at a
pilot scale. It consists of two portable skids
that are mounted on a low boy trailer (8 ft
x 45 ft) on which the unit is transported.
The process skid (20 ft x 8 ft) has two
levels and contains the majority of the
B.E.S.T.® process equipment including the
Premix Tank, the Extractor/Dryer, the Sol-
vent Evaporator, the Centrifuge, storage
tanks, pumps, and heat exchangers. The
second smaller utility skid (10 ft x 8 ft)
contains several utility systems to support
the operation of the process skid, includ-
ing a refrigeration unit used to cool the
solvent. Power requirements for the pilot
plant are 480 volts, three-phase power at
225 amps, which is accessed from a main
Primary Extraction/ I
Dewatering \
Soil-
Secondary Extraction/
Solids Drying
Solvent Recovery
Water Product
Figure 3. Generalized diagram of the RCC B.E.S. T.® solvent extraction process.
3
-------
power source (i.e., electrical drop) by an
electrical distribution panel supplied by
RCC. A support trailer accompanies the
pilot plant, transporting ancillary equipment
and providing a storage and working facil-
ity during testing.
Test Program
The primary objective of this SITE dem-
onstration was to evaluate the effective-
ness of the B.E.S.T.® solvent extraction
technology on two test sediments having
different contaminants or contrasting con-
centration levels of the same contaminants.
Therefore, the sediments treated were col-
lected at two different transect locations
along the east branch of the GCR (see
Figure 1). Sediments collected and homo-
genized from Transect 28 were designated
Sediment A, and sediments collected and
homogenized from Transect 6 were des-
ignated Sediment B. The transect loca-
tions were located approximately 2 miles
apart. The Sediment A (Transect 28) loca-
tion was located slightly downstream of
an oil-skimmed settling lagoon, which re-
ceives wastewater from primary bar plate
mills and basic oxygen process (BOP)
shops. Sediment B (Transect 6) was lo-
cated slightly downstream from the dis-
charge of a coke plant. Sediment A con-
sisted of high levels of metals and low
levels of organic contaminants relative to
Sediment B. Sediment B was composed
of high levels of organic contaminants and
lower levels of metals.
Prior to the demonstration, each of the
two sediment types was prescreened, thor-
oughly homogenized, and subjected to
bench-scale treatability testing. These
tests, which were conducted by RCC, pro-
vided initial operating conditions. Critical
measurements were identified with the aid
of sediment characterization analyses. The
critical parameters selected for the dem-
onstration tests were:
• PAHs and PCBs in all solid and liquid
process streams
• O&G in the feed material, treated sol-
ids, and water phase (O&G was iden-
tified as critical because oil is a pro-
cess residual)
• Triethylamine in the treated solids,
water phase, and oil phase
• Moisture in the feed material and
treated solids
• Toxicity Characteristic Leachate Pro-
cedure (TCLP) metals in the feed ma-
terial and treated solids
• Masses of feeds (including steam and
caustic)
• Masses of treated residuals (solids,
oil, water, and recovered solvent)
After the initial conditions and critical
measurements were determined, the ac-
tual demonstration testing was initiated. A
pilot-scale unit was utilized to conduct the
testing, and was batch-loaded on average
with approximately 170lbs of wet sedi-
ment/batch (test run). Two demonstration
tests were conducted, one for each sedi-
ment type. Each demonstration test con-
sisted of two phases. Phase I involved the
determination of optimum process vari-
ables for each test sediment. These vari-
ables included number of extraction cycles,
mixing times, and extraction temperature.
Three sets of conditions, determined by
RCC, were tested. Phase II consisted of
two additional runs at optimum conditions
determined in Phase I. This resulted in a
Table 1. Extraction Sequence Used for Sediment A
total of three runs at optimum conditions
for each sediment type. Tables 1 and r
present the actual sequence of extractio,
cycles conducted during the demonstra-
tion for Sediments A and B, respectively.
Samples were collected and analyzed
for each process stream specified in Table
3. PAHs, PCBs, and O&G were critical
analyses for all media except vent gas.
These contaminants were known to be in
both sediment types and were the primary
constituents targeted for removal using
the B.E.S.T.® Process. Triethylamine was
targeted for analysis in the product streams
and vent gas emissions because of its
Extraction Temperature (°F)
Phase I '
Extraction
Cycle
1
2
3
4
5
6
7
Run 1
cold (62)
warm (106)
warm (95)
warm (95)
warm (103)
hot (170)
--
Run 2
cold (50)
cold (40)
cold (38)
warm (98)
warm (125)
hot (160)
hot (160)
RunS
cold (53)
cold (45)
warm (1 00)
hot (155)
hot (166)
hot (166)
hot (166)
Phase II "
Run 4
cold (48)
cold (42)
warm (1 1 0)
hot (155)
hot (163)
hot (164)
hot (164)
RunS
cold (52)
cold (46)
warm (97)
hot (152)
hot (167)
hot (160)
hot (160)
Shaded columns indicate the three optimum runs.
Table 2. Extraction Sequence Used for Sediment B '
Extraction Temperature (°F)
Phase I b
Extraction
Cycle
1A1
1A2
1A3
1B1
1B2
1B3
2
3
4
5
6
7
Run 1
cold (49)
cold (47)
(NC)°
cold (41)
cold (53)
cold (52)
hot (145)
hot (152)
hot (161)
hot (148)
hot (157)
hot (143)
Run 2
cold (28)
cold (42)
cold (38)
cold (39)
cold (47)
cold (36)
hot (152)
hot (157)
hot (150)
hot (152)
hot (151)
RunS
cold (32)
cold (40)
cold (40)
cold (29)
cold (38)
cold (46)
hot (151)
hot (150)
hot (152)
hot (151)
hot (146)
hot (150)
Phase II "
Run 4
cold (28)
cold (48)
cold (39)
cold (51)
cold (53)
cold (46)
hot (147)
hot (156)
hot (170)
hot (155)
hot (158)
RunS
cold (51)
cold (41)
cold (39)
cold (3d)
cold (45)
cold (44)
hot (146)
hot (160)
hoi (153)
hot (154)
hot (152)
Because of the high moisturecontent of Sediment B,
both sediment and solvent were fed to the Premix
Tank. The portions of each were limited so that the
temperature rise of the solvenWwater phase was at
an acceptable limit.
b Shaded columns indicate the three optimum runs.
NC = Not conducted
-------
Tables. Summary of Analyses Conducted for the RCC B.E.S.T.® SITE Demonstration
Parameter
Untreated
Sediment
(Raw
Feed)
Treated
Sediment
(Product
Solids)
Water
Phase
(Product
Water)
Decant
Water
(from Raw
Feed)
Oil
Phase
(Product
Oil)
Intermediate
Solvent/Oil
Mixture
Solvent
Feed and
Recycled
Solvent
Vent
Gas
Critical
PAHS'
PCBs
Oil and Grease
Moisture
Triethylamine
TCLP Metals"
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Non-Critical
Total Suspended Solids
Proximate/Ultimate
Total Metals"
Total Recoverable Petroleum
Hydrocarbons
Volatile Solids
Total Cyanide
Reactive Cyanide
Reactive Sulfide
Particle Size
Total Phosphorus
pH
Total Disolved Solids
Total Organic Carbon/Total
Inorganic Carbon
Biochemical Oxygen Demand
Conductivity
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Special Studies
Biodegradation
A
Specific PAH compounds analyzed for are presented in table 4.
Moisture was critical for all samples except for the oil phase.
TCLP metals include As, Ba, Cd, Cr, Pb, Hg, Se, and Ag.
Total metals include Sb, As, Ba, Be, Cd, Cr, Cu, Mn, Hg, Ni, Se, Tl, Va, and Zn.
potential as a process residual. Moisture
content and TCLP were considered criti-
cal because of the original characteristics
of the sediments (high moisture and met-
als contents).
Six main process streams were sampled
and analyzed for each of the two tests.
These process streams included untreated
sediments (raw feed), product solids, prod-
uct water, product oil or oil/solvent mix,
recycled solvent, and vent emissions. De-
cant water collected from buckets holding
the feed material from one of the Sedi-
nent B batches was also sampled. Each
lot of product triethylamine was sampled
prior to use.
Results
The following data summary is derived
from this SITE demonstration:
• Contaminant reductions of 96% or
greater for total PAHs and greater
than 99% for total PCBs were
achieved from treatment of bottom
sediments collected from Transect 28
(Sediment A) of the GCR. Contami-
nant reductions of greater than 99%
for total PAHs and greater than 99%
for total PCBs were achieved from
treatment of bottom sediments col-
lected from Transect 6 (Sediment B)
of the GCR. Table 4 provides the
percent removals for individual PAH
compounds from test sediments, as
determined from averaging the three
optimum runs. Table 5 presents the
PCB removal efficiencies from test
sediments for each test run and as
total and optimum run averages.
• O&G removal efficiencies in excess
of 98% were achieved in the treated
solids generated from both sediment
types, as shown in Table 6.
• Mass balances calculated for all ma-
terials entering and exiting the pro-
cess indicated that very good mass
balance closures were achieved from
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Table 4. PAH Removal Efficiencies
Sediment
A
Treated %
PAH Analyte Feed8
Acenaphthene 68
Acenaphthylene <16
Anthracene 22
Benzo(a)anthracene 25
Benzo(a)pyrene 24
Benzo(b)fluoranthene 23
Benzo(k)fluoranthene 17
Benzo(ghi)perylene 15
Chrysene 25
Dibenz(a,h)anthracene <18
Fluoranthene 76
Fluorene 51
lndeno(1 ,2,3-cd)pyrene 15
2-Methylnaphthalene 25
Naphthalene <18
Phenanthrene 92
Pyrene 67
Total PAHs 548
Solids8
1.3
<0.8
1.3
0.52
0.34
0.36
0.22
0.20
0.52
<0.76
1.4
1.9
0.18
3.7
5.1
3.6
1.0
22
Removal"
98.1
—
94.1
97.9
98.6
98.4
98.7
98.6
97.9
—
98.2
96.3
98.8
85.2
—
96.1
98.5
96.0
Sediment B
Feed8
12800
210
2370
1050
810
857
533
457
937
140
4280
7290
547
6410
18700
10800
2810
70920
Treated
Solids8
42
6.6
16
4.7
4.6
4.1
3.6
2.3
4.7
<2.9
16
35
2.2
83
230
41
12
510
%
Removal"
99.7
96.9
99.3
99.6
99.4
99.5
99.3
99.5
99.5
>97.9
99.6
99.5
99.6
98.7
98.8
99.6
99.6
99.3
a Concentrations reported in mg/kg (dry weight basis) and are the average of the three optimum runs for each
sediment. (Sediment A = Runs 3, 4,and 5; Sediment B = Runs 2, 4, and 5.)
" Percent Removals = Feed Concentration -
Treated Solids Concentration
x inn
Feed Concentration
treatment of both test sediments. Clo-
sures of 99.3% and 99.6% were o^
tained for Sediments A and B, r«.
spectively.
• The products generated using the
B.E.S.T.® Process were consistent
with RCC's claims with regard to re-
sidual triethylamine concentrations.
Average triethylamine concentrations
of 103 mg/kg, less than 1 mg/L, and
733 mg/kg for solid, water, and oil
product, respectively, were generated
during the treatment of Sediment B
(Transect 6). Solid and water prod-
ucts generated from the treatment of
Sediment A achieved average residual
triethylamine concentrations of 45 mg/
kg and less than 2 mg/L, respec-
tively. Product oil was not generated
from treatment of Sediment A because
Sediment A originally contained very
little oil (less than 1%). A summary
of RCC's claims, and actual triethy-
lamine concentrations in the treated
solids, product water, and product oil
are presented in Table 7.
Costs
Operating and equipment capital cost
estimates were developed for the proposed
full-scale B.E.S.T.® system. The cost es-
timates were based on information pro-
vided by the vendor and on sevei
assumptions.These assumptions wet«,
based on the experiences of this demon-
stration and a previous full-scale test con-
ducted at a site in Georgia. Certain cost
factors which were not included in the
treatment cost estimate were assumed to
be the responsibility of the site owner/
operator. Costs associated with system
mobilization, site preparation, startup, and
TableS. PCB Removal Efficiencies
Parameter
Sediment A
Total PCBs - Feed (mg/kg - dry weight)
Total PCBs - Treated Solids (mg/kg - dry weight)
Percent Removal (%)
Sediment B
Total PCBs - Feed (mg/kg - dry weight)
Total PCBs - Treated Solids (mg/kg - dry weight)
Percent Removal (%)
R1
7.33
<0.07
>99
364
1.5
99.6
Test Runs
R2 R3 R48
6.41
0.20
96.9
316
2.1
99.3
8.01
0.05
99.4
495
1.2
99.8
11.8
0.04
99.7
462
1.8
99.6
R5b
16.4
0.04
99.8
497
1.4
99.7
Avgc Standard Deviation0
10.0/12.1
0.08/0.04
99.2/99.7
427/425
1.6/1.8
99.6/99.6
4.1/4.2
0.07/0.006
—
82/96
0.35/0.35
—
* Concentrations reported for Run 4 are the average of three field replicate measurements.
6 Concentrations reported for Run 5 are the average of samples analyzed in triplicate.
0 Two values are given; the first pertains to all five runs and the second pertains to the three optimum runs (Sediment A=Runs 3,4, and 5 and Sediment B=Runs 2, 4, and 5).
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Table 6. Oil and Grease Removal Efficiencies
Parameter
R1
Test Runs
R2 R3
R4" R5b
Avg° Standard Deviation0
Sediment A
Total Oil & Grease - Feed (mg/kg - dry weight) 9400 7800 7400 6600
Total Oil & Grease - Treated Solids (mg/kg - dry weight) 195 169 203 66
Percent Removal (%) 97.9 97.8 97.3 99.0
6700 7580/6900
65 140/111
99.0 98.2/98.4
1030/436
69/79
Sediment B 103,0007 41,600
Total Oil & Grease - Feed(mg/kg - dry weight) 66,400116,00067,300167,00099,100 127,000 35,300
Total Oil & Grease - Treated Solids (mg/kg - dry weight) 1800 1330 1490 1230 1810 1530/1460 266/310
Percent Removal (%) 97.3 98.9 97.8 99.3 98.2 98.5/98.9 —
• Concentrations reported for Run 4 are the average of three field replicate measurements.
b Concentrations reported for Run 5 are the average of samples analyzed in triplicate.
0 Two values are given; the first pertains to all five runs and the second pertains to the average of the three optimum runs. (Sediment A = Runs 3, 4, and 5 and Sediment B
= Runs 2, 4, and 5.)
TaWe 7. Triethylamine Concentrations - Treated Solids, Product Water, and Oil Phases
Parameter
Claim
R1
Test Runs"
R2 R3 R4b
R5
Avgc Standard Deviation'
Sediment A
Triethylamine in Treated Solids (mg/kg)
Triethylamine in Product Water (mg/L)
Triethylamine in Oil Phase (%)
Sediment B
Triethylamine in Treated Solids (mg/kg)
Triethylamine in Product Water (mg/L)
Triethylamine in Product Oil (mg/kg)
<150 61.7 93.1 27.8 28.0 79.6
<80 <1 <1 <1 <1 2.2
NA — — — — —
<150 106 88.7 55 130 89.3
<80 <1 1.0 <1 <1 <1
<1000 — — — — —
58/45
<2/<2
65.8d
94/103
<1/<1
733d
29.6/29.8
—
—
27.4/23.7
NA
—
* Concentrations reported for each of the five test runs for each sediment are the average of laboratory triplicate analysis conducted on the sample.
b Concentrations reported for Run 4 are the average of three field replicate measurements, each of which are the average of laboratory triplicate analysis.
0 Two values are given for treated solids and product water; the first pertains to all five runs and the second pertains to the three optimum runs (Sediment A = Runs 3, 4,
and 5; Sediment B = Runs 2, 4, and 5).
d The % values reported for the Sediment A oil/solvent mixture and the Sediment B product oil are the averages of five aliquot (field replicate) measurements.
demobilization were also excluded from
the treatment cost estimate. The reason-
ing used in making these estimates, or
omitting a particular cost category, is dis-
cussed in the Applications Analysis Re-
port.
The pilot-scale unit used in this demon-
stration operated at an average feed rate
of QOlbs of contaminated sediment/day.
The full-scale commercial unit is projected
to be capable of treating 186 tons/day
(TPD) of contaminated soil or sludge. The
cost estimates are based on the remedia-
tion of contaminated soil, sludge or sedi-
ment using the proposed full-scale unit.
The treatment cost is estimated to be
$112 Aon if the system is on-line 60% of
the time or $94/ton if the system is on-line
80% of the time. Cost information is pre-
sented in the Applications Analysis Re-
port for this demonstration.
Conclusions
The B.E.S.T.® solvent extraction pro-
cess is designed to treat sludges, soils,
and sediments contaminated with organic
compounds. The system is capable of
physically separating organic contami-
nants, such as PAHs, PCBs, and O&G
from contaminated media and con-
centrating the organics for contaminant
volume reduction. The prototype full-scale
system is only applicable to sludges, but
the proposed full-scale system will be ap-
plicable to soils and sediments as well.
The effectiveness of treatment can be
illustrated from this demonstration and from
previous case studies. This demonstra-
tion removed at a minimum 96% of the
PAHs, greater than 99% of the PCBs, and
greater than 98% of the O&G from the
contaminated sediments.
•fcll.S. GOVERNMENT PRINTING OFFICE: IM3 - 750-071/MNUM
-------
The EPA Project Manager, Mark Meckes, is with the Risk Reduction Engineer-
ing Laboratory, Cincinnati, OH 45268 (see below)
The complete report, entitled "Technology Evaluation Report: SITE Program
Demonstration; Resources Conservation Company Basic Extractive
Sludge Treatment (B.E.S.T.®); Grand Calumet River; Gary, Indiana",
consists of two volumes:
"Volume I" (Order No. PB93-227122; Cost: $27.00, subject to change)
"Volume II, Pi. 1" (Order No. PB93-227130; Cost: $61.00, subject to change)
"Volume II, Pt. 2" (Order No. PB93-227148; Cost: $119.00, subject to change)
"Volume II, Pt. 3" (Order No. PB93-227155; Cost: $36.50, subject to change)
"Whole Set" (Order No. PB93-227114; Cost: $207.00, subject to change)
will be available only from:
National Technical Information Service
5285 Port Royal Road
Springfield, VA 22161
Telephone: 703-487-4650
A related report, entitled "Resources Conservation Company, B.E.S.T.®
Solvent Extraction Technology - Applications Analysis Report
(EPA/540/AR-92/079) is available as long as supplies last from:
ORD Publications
26 W. Martin Luther King Drive
Cincinnati, OH 45268
Telephone: (513) 569-7562
The EPA Project Manager can be contacted at:
Risk Reduction Engineering Laboratory
U.S. Environmental Protection Agency
Cincinnati, OH 25268
(513) 569-7348
United States
Environmental Protection Agency
Center for Environmental Research Information
Cincinnati, OH 45268
Official Business
Penalty for Private Use
$300
BULK RATE
POSTAGE & FEES PAID
EPA
PERMIT No. G-35
EPA/540/SR-93/079
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