9a Chromate Removal Plant Part 1_20170726

IWC 11-41
Chromate Removal at the Hanford Site
Dean Neshem Jr.
CH2MHILL Plateau Remediation Company
Richland, Washington
Peter Meyers
ResinTech
West Berlin, New Jersey
Francis DeSilva
ResinTech
West Berlin, New Jersey
KEYWORDS: chromate, groundwater, Hanford, hexavalent chromium, ion exchange.

IWC 11-41
ABSTRACT
Remediation of groundwater containing hexavalent chromium has been in progress at
the Hanford site for more than 15 years. Although the early systems used type I (gel)
strong- base anion exchange resin and off site regeneration, the most recent systems
use a long -life single -use resin. Use of the long -life resin is projected to result in
significant operating cost savings. This paper explores the history of the chromate
remediation efforts at the site, a review of more than 15 years operating experience with
strong -base resin and the operating results with the long -life resin.

IWC 11-41
BRIEF HISTORY
The Hanford site, located in eastern
Washington state, was chosen in 1943
as part of the Manhattan project for
production of plutonium for nuclear
weapons (figure 1). The site was
chosen because it was close to the
established electrical infrastructure from
the Grand Coulee dam, was sparsely
populated, considered stable
geologically, and had a large amount of
water available from the Columbia
River.
Residents of the small communities of
White Bluffs and Hanford were given 30
days to move from their homes. The
initial reactor went from design to
completion in 13 months. The B reactor
was the worlds first plutonium
production facility. It had a graphite
core, 2004 process tubes and flowed
186,000 gallons per minute of cooling
water. (Hanford Story video,2011).
Cooling water taken from the Columbia
river made a single pass through the
reactor and was sent to concrete cribs
and basins to allow heat and short lived
radionuclides to decay prior to being
returned to the river. Sodium
dichromate was added to this water as a
corrosion inhibitor.
Naturally occurring (unenriched)
uranium 238 was transmuted into
plutonium 239, which was then
extracted and used in the Fat Man bomb
that was detonated over Nagasaki
Japan on August 9, 1945
The successful completion of the
Hanford works remains one of the
boldest and remarkable engineering
feats of all time. Although the use of
nuclear weapons remains very
controversial, there is little doubt that the
use of Fat Man greatly reduced
American casualties that would have
occurred had an invasion of the Japan
mainland been necessary.
Over the years, additional reactors were
built. A total of 8 single pass reactors
were constructed and operated at
Hanford between 1944 and 1971, all
using the same once through cooling
and sodium dichromate as a corrosion
inhibitor.
Much of the land surrounding the
Hanford site is very porous. Leakage of
concentrated sodium dichromate from
underground piping and other accidental
spillage resulted in substantial quantities
of chromate finding their way into the
soil and gradually moving downward
toward the Columbia River.

IWC 11-41
Washington
Seattle Spokane
Hanford Site
land
North Slope
100-H
AREA
100-K AREA �1O HR.3 GW.1 �100-F
AREA
')perable Unit
ff
100 HR-3 GW
aereble Unit
` 100 KR1 GW 100 FR-3 Gw'
Operable Unit
Operable Unit,
100 Areas
Figure 1. Location of Hanford site
CHROMIUM CONTAMINATION
Hexavalent chromium on the Hanford
site is primarily found near the reactor
sites. It is estimated that a 2.0 km2 (0.8
mil has contamination at concentrations
greater than 100 pg/L. (DOE CERCLA,
2011) Peak concentrations of 55,600
pg/L have been measured near the D
and DR reactors. A substantial
additional area has contamination below
100 fag/L. Plume maps are shown in
appendix A.
PILOT PLANT STUDIES
Following the shift from plutonium
production to site cleanup in the early
nineties, a pilot plant was constructed to
evaluate the use of ion exchange as a
means of remediating the chromium in
the groundwater on site. The initial
studies used a variety of ion exchange
resins available at the time and resulted
in a determination that ion exchange
could be used. A type I strong base
anion resin was chosen for the full scale
facilities to be constructed in the HR-3
and KR-4 operable units. Initially a 400
gpm plant was constructed (HR-3) to
treat the largest area of contamination
near the D and H reactors. A 200 gpm
plant was also built near the K reactors
with operation commencing in 1997.
Control of the contaminant plumes is
accomplished using a combination of
extraction wells and injection wells.
Contaminated groundwater is extracted
from near the Columbia river and
pumped to ion exchange facility for
treatment. Following treatment the
water is sent to a series of injection
wells upgradient of the plume. This
approximates a closed loop system
where the injection water drives the
contaminants toward the extraction
wells.
EXPANSIONS - As more information
about the size of the contamination was
gathered a series of expansions and
continued testing of additional
technologies have been implemented.
Pump and treat capacity in the K
reactors was expanded from 200 gpm in
1997 to 1100 gpm in 2009 with the
addition of two additional facilities.
Additional pump and treat capacity
around the D and DR reactors began in
2004 with a 50 gpm pilot scale facility
(DR-5) that is able to regenerate resin in
vessel.
Another innovative treatment technology
was also employed in this area. It is
known as the ISRM (In -Situ Redox

IWC 11-41
Manipulation) barrier. This barrier
consisted of a closely grouped network
of wells that had sodium dithionite
injected into them to create a reducing
environment, converting hexavalent
chromium to trivalent chromium and
greatly reducing the amount of
chromium reaching the Columbia river.
A portion of the barrier failed to stop the
flow of chromium prompting the
expansion of pump and treat capacity to
600 gpm beginning in late 2010.
The latest expansion of capacity is near
the H reactor. A new facility is replacing
the original IX system, increasing
capacity from 300 to 800 gpm.
Table 2. 100 Area
IX System Description
Influent Chromium
Number of
0esO Flaw
Conoantratlon
System
Tr -
(Umin[ppm])
1pa/l)
statue
KX
5
2.2i1 (EX)
60
AM,.
KR4
3
1.136 (300)
30
Ace -
KW
2
757(200)
150
AcM
UR-5
1
189(50)
1.13W-3,3W
Aclire°
DX
4
2.371 (600)
S00
Unger mnsin,atgnp
HR-3
3
1.136 (300)
50
AEGve
HX
8
3,028(8001
50
UnaarconsUuckv
a. Shatdawe
Spnnp 2011_
b. Complete
October 2010.
c Shvtdcwn
Spnnp W12.
E. Complete
W ber 2011.
HANFORD VESSEL DESIGN
Ion exchange vessels for chromium
treatment have employed the following
design philosophy, the only exception
being the DR-5 pilot scale plant. The
system is modular, utilizing groups of
four vessels or "trains" rated at 100
gpm. To expand capacity additional
trains are added rather than changing
the size of the vessels. Each vessel has
an 80 ft3 capacity for ion exchange
resin. Each of the four vessels in a train
are in active operation in a lead-lag1-
lag2-polish configuration.
Resin is removed when the lead vessel
is reaches capacity for chromium or the
polish vessel effluent is greater than 10
fag/L.
The four bed system has proven to be a
predictable and forgiving system.
Consistency in the vessel design
between facilities allows for operational
flexibility, since the operators can switch
between facilities without extensive
retraining.
Over the years several modifications or
changes were implemented to aid the
dependability of the system. Initially the
lead vessel was operated in a sacrificial
mode. This was due to concerns that
uranium and other radionuclides may
accumulate on the resin presenting a
transportation risk. During this time the
lead vessel would be left in service for

IWC 11-41
six months prior to removal, sampling
and disposal. The remaining vessels
would be rotated between lead, lag, and
polish positions based on chromium
breakthrough. Evaluation of sample
results showed this as an unnecessary
precaution and operation shifted to
rotating all four vessels allowing for
increased loading of the resin prior to
regeneration.
Containers appropriate for offsite
transport of the resin for regeneration
and a system to load/unload the resin
efficiently were also implemented to
minimize the need to handle the resin
and to speed the changing of resin from
the vessels.
Metering pumps to add sulfuric acid for
pH adjustment of the influent water were
also developed to maintain influent
water at pH 7 were implemented to
minimize mineral scaling that would
develop on the resin bed and
distributors that would cause additional
strain on the system pumps.
RESIN REGENERATION
The primary method used for treatment
of spent strong base anion resin at the
Hanford site has been off site
regeneration. This method is simple for
plant operation but leads to concerns
over shipping and treating resin off site.
Extensive sampling and analysis is
required to ensure that the resin meets
all shipping requirements. This requires
a large investment in resin due to the
long turnaround time as the resin is
sampled, shipped, regenerated, shipped
back and placed into service. Several
variations of onsite regeneration have
been tested over the years.
Regeneration at a facility onsite was
performed using sodium sulfate leaving
the resin in the sulfate form (as opposed
to the chloride form normally received
from offsite). This resin had
approximately 80% of the capacity as
the resin in the chloride form.
Additionally, the facility did not have the
capacity to regenerate all of the resin
needed to eliminate offsite regeneration.
A pilot scale facility (DR-5) was also
operated from 2004 to 2010 that used in
vessel regeneration. This process used
sodium chloride to strip the chromium
from the resin. Sodium dithionite was
used to convert the hexavalent chrome
(anionic) to trivalent chrome (cationic).
Hydrochloric acid was used in a second
step to condition the resin. Phosphoric
acid was used on the regenerant
wastewater solution to precipitate the
chrome, followed by sodium hydroxide
to increase the pH and aid precipitation
and settling. The precipitated chrome
was separated by a filter press.
BENCH SCALE TESTING
In 2008, plans to expand the pump and
treat capacity near the D and H reactors
were being finalized. With this
impending expansion, the decision to re-
evaluate the ion exchange resin and
regeneration process was made. A test
skid was procured that allowed for six
resins to be tested simultaneously using
a one inch diameter column with a bed

IWC 11-41
depth of up to 48 inches. The columns
had individual feed tanks and pumps
allowing for pH and flowrate to be varied
individually.
Figure 2. Resin test skid.
Beginning in March of 2009,
Seven
different resins were tested.
They
included several strong base
resins
(including the resin's currently
being
used onsite), a styrenic weak
base
resin, as well as granular and
bead
forms of an epoxy polyamine resin.
SeM[rnt< stymne St,— EPoq Epm:y pulyem—
diveryWevame drviaylbmarre palyemer
Shape h}sheriraf head %,h—I bead G.em.lm
SPh—.d heed
Acuvegml) Q-WM-Y'-- QPa---) P-M-tary
emmamum amine
P'rcgsac-Y
amine
'type (mvn nchange) TYPe t straps Type 1 sEmB W ase nk b
base I..
Wrak bax
ilPxr1-1 pB 6to 14 Il ro 11 16.5
16.5
.hbilty to be resenveted? Y. Yc. No
Nu
. The pressurt. amp is rNrnmipcd ai ike ic+n4M1+nuac in ae raw 1er4wa
b Ibe bahwa� Elax rrte is dCermieM. e�x rbe xnegenrme in rbe mw6ekm• ii
The initial testing showed results similar
to the operating facilities for the strong
base resins at pH around 7, confirming
the validity of the test skid as a method
of evaluating resin performance.
�- � Resin Evatl p2
Figure 7. Breakthrough Curves for the Second Resin Evaluation
Additional tests were performed with
the epoxy polyamine resins operated at
reduced pH (5) showed exceptional
affinity for chromate.
F•tgum 2. Breaftruugh Curves for the First Resin Evaluation
The initial test column of this resin
lasted through the entire duration of the
initial test series (almost nine months)
without nearing capacity. The
performance of this test column shifted
the focus of the testing to learn more
about this resin and evaluating if the
switch to this resin would be the right
choice for use at Hanford. Additional
columns with much smaller bed depths
were tested in an attempt to reach
capacity of the resin. None of the tests

IWC 11-41
were able to reach the total capacity of
the resin, an idea about when the
vessels would begin to allow chrome
leakage into the lag vessels was
determined.
EPDXY POLYAMINE RESIN
Making the switch to a weak base epoxy
polyamine resin would require some
significant changes to the way ion
exchange resin is handled on site. This
type of ion exchanger is granular rather
than spherical.
PHYSICAL PROPERTIES
Polymer Structure
Epoxy Polyarnme
Functional Group
R - N - (CH,)2+
Ionic Form as Shipped
Free Base
Physical Form
Tough, Uniform Granules
Screen Size Distribution
1.2 to 30 Mesh Nominal
+12 mesh (US Sid.)
C 25%
-50 in (US Sid-)
< 1%
PH Range
1 to 14
Uniformity Coefficient
Approximately 20
Stability
Insoluble In Acids, Bases
and Most Solvents
Water Retention
52% to 62%
Approximate Shipping Weight
38 lbs./cu. R.
Swelling (free base to salt form)
Less than 10%
Total Capacity (free base form)
>2.7 meq/mL
Salt Splitting Capacity
Approx. 10% Of Total
The facility would require systems to
deliver acid and caustic to adjust the pH
of the groundwater being treated.
These systems would also require bulk
deliveries of chemicals due to the
increased use rates needed to reach
lower pH's. Additionally the type of
coating inside the vessels was changed
to one more appropriate to use in acidic
conditions. Cathodic protection was
also added to the design of new vessels
to add an additional layer of protection
against corrosion.
The granular shape (instead of the
typical bead shape) of the best
performing resin generates increased
differential pressure across the resin
potentially increasing pumping costs
and requiring reevaluation of the sizing
of the feed pumps. Concerns about
loading and unloading of the resin,
resulted in a test to load resin into and
out of one of the existing vessels to
determine if the existing sluicing
mechanisms would work. The test was
successful, and not discernible
difference was noted by the operators
performing the work. New vessels also
have had four air ports added to the
bottoms of the vessels to aid the
removal of the resin.
Since the resin cannot be regenerated
for reuse, a disposal path is required.
To dispose of the resin onsite it must
meet certain requirements to be
accepted at the disposal facility onsite.
Samples of the resin from testing were
analyzed to determine if any additional
treatment would be required for
disposal. The results of these tests
showed that the resin would potentially
require stabilization (i.e. grouting) to
meet TCLP for total chrome. The initial
sample indicated stabilization would be
required. Later samples, that were
taken from resin samples with even
higher chrome loading met requirements
for disposal onsite.
Additionally these tests showed that
more than 90% of the chrome on the
resin was in the trivalent form rather
than hexavalent form. This helped to
confirm that the exceptional capacity of
the resin is due to more than simple ion
exchange. Testing showed the resin

IWC 11-41
had more than an order of magnitude
greater capacity than any of the other
resins tested. (Neshem, 2010)
We believe the mechanism is ion
exchange followed by reduction with the
resin matrix and precipitation inside the
resin matrix. This hybrid property
appears to be both flow and pH
sensitive in that the rate at which
chromate is reduced to trivalent chrome
is slower it higher pH.
pH Testing — An effective operating
range for the new range was determined
through a set of bench scale tests. Very
small volumes of resin were added to
beakers of highly contaminated
groundwater and stirred to ensure
mixing. Hexavalent chromium
concentrations were measured daily and
water was replenished until the resin
was unable to remove additional
chrome. The results shown in figure 3
indicated that the resin capacity
decreased substantially when the pH
was greater than 6. Additional testing
with larger resin volumes and samples
measured every minute to more closely
simulate normal operation showed a
decrease in the rate of chrome removal
at pH's above 6.5 as well
Table 5. Results of SIR-700 pH Evaluation
Chromium
Solution
(pH)
Absorption.
(mg)
Relative Capacity
5.0
57,0
1.00
5.5
44.3
0.78
6.0
43-6
077
6.5
24.3
0.43
7.0
17.5
0.31
8.0
11.2
0.20
Figure 3. pH optimization testing
INITIAL RESULTS WITH THE NEW
EPDXY POLY AMINE RESIN
Additional column testing was
performed with both sulfuric acid and
with hydrochloric acid to determine if
there was an advantage in operating
capacity to using one acid over the
other. Very little difference was noted.
a .eae �mw+ naa vo— '
Figure 4. Canparlson ofSIR-700 Performance Using Different Acid Types
A life cycle study was performed to
determine the present worth of various
options. The single use epoxy
polyamine resin was much less
expensive than off site regeneration of
strong base resin, very similar to the
present worth of on site regeneration but
without the complicated operation that
on site regeneration would require.

IWC 11-41
Table G. OX System Option Estimated Cost Comparlwit
EaHrnaw C.w
Baseline
RegenaralEonti
oftim
P.9- attan
0."a In-Veasel
Regeneretton` peeeneratm.-
SlnplaOse
Raaina
Capital coat
10.76
1.73
992 8.15
7.33
Mneal O&M wait
333
2.3S
221 1.58
1.84
Of—yde-1
39.60
28.15
2912 21.85
2325
a. In miltliona of tlallats.
5. Oowez 21K ream with o8slte reyenenallon.
e. P—te0 wait fer the Ok lacillty mel— 56 peeoent o'tntal reixteal regeneration faculty cods
d.0 Injectlon oftmaled.9anaratbn WBet—.,
With questions about the epoxy
polyamine resin answered, the decision
to use the resin in the newest pump and
treat facility was made. The resin was
loaded into the vessels and operation
began without pH adjustment due to
schedule constraints and positive short
term testing in the test skid. Operation
without pH adjustment occurred for
about 100 bed volumes over the course
of several weeks. More than a week
after the start of operation with pH
adjustment chrome leakage was
detected in the effluent of the lead
vessel.
1200000
1000000
800000
600000
400000
200000
0
12/2
Train A
tGW Total, gallons ♦ Lead Cr, ppb
12/4 12/6 12/8 12/10 12/12 12/14
70
60
s0
40
30
20
10
0
12/16
Lead vessel effluent values peaked
several days later before stabilizing near
10-20 pg/L (influent was about 325
pg/L). During this time the effluent
required little to no caustic to return the
pH back to neutral. Initial operation
stripped the pH buffering capacity of the
resin leaving few active sites available
for ion exchange. A week after the peak
in lead column effluents, a much smaller
peak in the lag-1 vessels as the resin
was re -acidified. Once the caustic use
increased to the expected levels the
chromate leakage stabilized and was
limited to the lead vessel only. After 2
months of operation the leakage from
the lead vessels dropped below
detectable levels (5 pg/L) and has
stayed below detection since. As of July
2011, the resin has processed about
40,000 BVs, removed more than 138 kg
(304 Ibs) and is not showing any signs
of reaching capacity.
After several months of operation,
differential pressure across the resin
beds began increasing to higher levels
than expected increasing with each
subsequent vessel in series. Inspection
of the resin beds showed a layer of resin
fines had built up on the top of each of
the lag-1, lag-2, and polish vessels.
Backwashing of the vessels, since they
had been exposed to little or no
chromate returned pressures to normal.
In the future the resin will be
backwashed more thoroughly when
loaded to help minimize this problem.
Additionally when the new facility near
the H reactor is started, a change to
three vessels in service at any one time
is being made to reduce pumping costs
since the resin is proving to be so much
more effective than the strong base
resins previously used.
COST EFFECTIVENESS
Along with resin testing, life cycle cost
estimates were prepared for the facility
built near the D reactors as shown in
Figure 4. This estimate used the strong

IWC 11-41
base resin with offsite regeneration as a
baseline and compared this with the
most effective strong base resin
regenerated both on and off site, and
the single use epoxy poly amine resin.
Resin life for the epoxy poly amine resin
was assumed to be 40,000 bed volumes
(very conservative) due schedule
constraints requiring the estimates to be
prepared in parallel to the resin testing.
These life cycle costs showed that the
epoxy polyamine resin to be the most
cost effective option saving almost $20
million over the 11 year lifespan of the
facility. This is roughly equal to the cost
of construction of the facility.
Figure 4. Estimated life cycle costs
With the successful implementation of
epoxy poly amine resin at the D area
facility, the next step is to evaluate the
conversion of the remaining facilities
near the K reactors to this resin. To do
this a test is being implemented at the
smallest facility to determine whether
the existing simple acid injection system
is capable of maintaining a desirable pH
for use with the new resin. Monitoring of
the vessel wall thickness will determine
the suitability of the liner for use in an
acidic environment. Operation with
smaller volumes of resin per vessel is
also being evaluated as an alternate
method to reduce pressure loss across
the resin bed. It is also beneficial to
increase the headspace for
backwashing since the vessels do not
have an upper distributor that would
prevent resin carry over in the event
backwashing was too vigorous (newly
constructed facilities have upper
distributors that match the lower
distributors to eliminate this concern.
Leachables from epoxy polyamine resin
The epoxy polyamine resins are
included in the CFR's that relate to the
use of ion exchange materials in food
grade applications. Preliminary
extraction and analysis indicate there
should be no problem certifying this type
of resin to ANSUNSF 61 at some future
date, should customer demand dictate
that this is necessary.
NMI :MAN0201WAI
Several significant challenges still need
to be solved at the Hanford site. A pilot
plant was also done for removal of
technetium from groundwater. The
results of this pilot plant were favorable,
however no extensive studies were
performed to optimize.
Perhaps the biggest remaining
challenge is that of removing radioactive
iodine 1129 Radio -iodine was released in

IWC 11-41
significant quantities over the years the
plutonium facility operated, much of it
airborne. As such there is significant
contamination in much of the
groundwater underlying the site.
Perhaps the biggest challenges still
await. The more that is learned about
the site, the more surprises there are.

IWC 11-41
References:
The Hanford Story video, (2011)
http://www.hanford.gov/c.cfm/video/tags.cfm/The_Hanford_Story
Neshem, D (2010). Resin Evaluation and Test Report to Support DX Treatment
System. SGW-41642, Rev. 1
Hanford Site CERCLA Five -Year Review, (2011), DOE-RL-2011-56

IWC 11-41
Appendix
_r 100-D -__ 1OO-H
100-N f
100-K 11O0-F
10
1 �
I r
200-West 1 i
13
I I
� 1
� 1
200-East
kw�r----------------
rconstituents `
6 d Chromium COWS = 100 uglLj A
Uranium (QWS � 30 ugfI-) �
Technetium-99 (D1NS = 900 pCilL)
Nitrate (OWS = 45 mgQ
Strontium-90 (DM = 8 pCilL)
lodina-129 (DWS= 1 pCK)
Tritium (UWS = 20,000 pCLfL)
® Carbon Tetrachloride (DWS = 5 ug1L)
Inner Area Boundary
Outer Area Boundary
Site Boundary
Basalt Above Water Table
0 Columbia River
0 3 5 9Km
I I I I
(J 1.5 3 4.5 Mi syPo9d
400 Area
5W
300 Area
rM

IWC 11-41
Hanford site groundwater contamination
plumes
In The Upper Unconfined l
• Mcnitoring Well Fall2009 Hexavalent Chromium
Plume p
g Extraction We] i Cr >= 20 ❑gIL and < 50 ug" ¢`I
® Injection Well Cr — 50 u & and < 200 uglL
+ Aquifer Tube Cr — 200 uglL and < 500 uglL
ISRM Barrier Wells Cr >= 500 uglL and < 1.000 ug1L
Transfer Line Cr >= 1400 uglL and < 2,000 uglL -� 1 • 96 523
Waste Sites M Cr>= 2,000 uglL and c 5,000 uglL %f Pump and Treat Buildings _ Cr >= 5,000 ug1L
Area Boundary
(] Columbia Mver R 100 200 300 M • DB 7D
DD-17 3 }
0 .53
350 700 1.050 Ft Q..i09aa'.; cs27B :7 a1
08-546 Jr OB-54A
D855
rd
•Des
/ AT-D-iEl
�, �j�/// • D8-73
,(L 36-o+ , D8-88
�C AT-0-2-rvn
• DB
.Q a3'.81-4n }
• D8-B
['ti pins..
��♦` D5 13
0537 /
AT-D-1.0 / / D5-A4 //r • D5-126
I
4 GS u'
•p5 t4
�D5-35 5DS-125
RCdOK-1$.Q t 04-83 D`-33
Redm-260 - D'I's
DS-15
Q4.39� D4-42 95-123 .0515
p0-69-2 i-
RedoK-3-4..1 + 2D4-00
__ pa-37 65 3d;
R¢GDD-41 0 * pq�8 0 D4 34 • DC - 3A D5-t 03
DD.-01.3 D4-32
DD-42-4+ �493 04-22 D4.11
,��� 0"'
DD-033+ 04-84 • 28 OS-179 D5.720
D4'13� \ 041 • D4.15 DS .� p5-104
DU-m4 D4-2a Da-31 Q5121
CN D4.eo
D4-92 Q1-99
53 Da.25 O5-9z2 DS-102
C 2]1 C62P0 D4-&5 • C5-1'
T'D4-19 D5.40 p5-98
Q4-20
/DD-49-3
680-6JI D-111
D32
D2-6 • Q2-11'//i /i////
/
i
/
/
/
/t � i/r/ /fi �"j//i✓//i
D area chromium plume

IWC 11-41
Yr Tta JpP.r J,K�emm.e
. fAwtom0 Vh9 HLMeq zaeHi4FexPnr Cl+Hmlya Rlwra j
aiP.r.�VrPa sa,waa,n Feemis ®Cr.,pwL wa.wwh jl
+ ATde'T✓b F I1—n ]al--iNWL.
" tlSRM Hnnlar Wain LJCr+. ,QaarH�ad-6W uyL
ii�Tmrn.Lrn �Gsa9liq^'•P+1:i.JpH VpL
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