ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
EPA-330/2-75-004
Boiler Stack Emission Monitoring
Honokaa Sugar Company
Haina, Hawaii, Hawaii
NATIONAL ENFORCEMENT INVESTIGATIONS CENTER
DENVER,COLORADO
JULY 1 975
U32Z
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ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
BOILER STACK EMISSION MONITORING
HONOKAA SUGAR COMPANY
HAINA, HAWAII, HAWAII
NATIONAL ENFORCEMENT INVESTIGATIONS CENTER
DENVER, COLORADO
JULY 1975
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INTRODUCTION.
CONTENTS
1
SUMMARY AND CONCLUSIONS 2
POWER BOILER OPERATIONS AND EMISSION CONTROL EQUIPMENT 3
Power Boiler
Steam Distribution System 4
Air Pollution Control Equipment 5
DISCUSSION OF STUDY
Stack Monitoring 6
Visible Emission Evaluation ^
REFERENCES 12
APPENDICES
A Processing of Sugar Cane
B Steam Piping System and Boiler Operating Data
Honokaa Sugar Company
C Stack Monitoring Procedures
D Analytical Procedures for Stack Monitoring Samples
E Visible Emissions Evaluation, Honokaa Sugar Company Mill
May 25-26, 1975
ii
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TABLES
I SUMMARY OF STACK MONITORING RESULTS 8
HONOKAA SUGAR COMPANY, MAY 25-26, 1975
II SUMMARY OF BOILER OPERATING DATA 9
HONOKAA SUGAR COMPANY, MAY 25-26, 1975
FIGURE
HONOKAA BOILER STACK. .
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INTRODUCTION
The Honokaa Sugar Company mill is located about 64 km (40 miles) north-
west of Hilo, Hawaii. This mill presently has a rated capacity of
2725 kkg* (3000 tons)/day net cane** and generally operates 24 hours/day
7 days/week. During the period May 24-27 (3 p.m.-3 p.m. operating day),
the Honokaa mill processed an average of 2428 kkg (2675 tons) net
cane/day. The range was 2244-2580 kkg (2471-2841 tons) net cane/day.
Cane processing to raw sugar and molasses generally follows the flow
chart contained in Appendix A. As is typical at most sugar mills
in the Hawaiian Islands, the bagasse*** is used as the primary fuel
source for the boilers. The bagasse available for fuel is about 30
percent of the net cane processed. Company officials indicated that
about 95 percent of the available bagasse is burned with the remainder
being wasted.
At the request of Region IX EPA, the National Enforcement Investigations
Center (NEIC) conducted stack monitoring and visible emissions observa-
tions on May 25 and 26 to determine if applicable state air pollution
regulations were being met. The allowable particulate emission rate is
0.4 kg/100 kg (0.4 lb/100 Ib) of bagasse burned. For visible emissions
from existing sources, the regulations state:1
"No person shall cause or permit the emission of visible air
pollutants of a shade or density equal to or darker than that
designated as No. 2 on the Ringelmann Chart or 40 percent opacity,
except" that "A person may discharge into the atmosphere from
any single source of emission, for a period or periods aggregating
not more than 3 minutes in any 60 minutes, air pollutants of a
shade or density not darker than No. 3 on the Ringelmann Chart
or 60 percent opacity when building a new fire or when breakdown
of equipment occurs."
Information on process and boiler operations and air pollution control
practices was obtained from Mr. Cyril Rowsell, Factory Superintendent
and Mr. Jean-Paul Merle, Boiling House Superintendent. Mr. Harold
Tobin, Air Pollution Engineer of the Hawaii Department of Health,
observed the tests.
**Net cane is a calculated value and is essentially equal to the gross
cane brought into the plant minus the soil, leaves, rock, and other trash.
***Bagasse is the solid material remaining after the milling process has
removed the juice from the sugar cane. It serves as an excellent
fuel source with a heating value of 2580 gram-cal./gm (4650 BTU/lb).
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SUMMARY AND CONCLUSIONS
1. Stack monitoring was conducted at the Honokaa Sugar Company mill
May 25-26 to determine the particulate emissions from the bagasse-
fired boiler stack. Sampling was conducted as specified in Method
5 of the Standards of Performance for New Stationary Sources.
State of Hawaii regulations require that the particulate emissions
from this source not exceed 0.4 kg/100 kg (0.4 lb/100 Ib) of
bagasse burned. The average particulate load emitted by the
Honokaa Sugar Company was 0.53 kg/100 kg (0.53 lb/100 Ib)
of bagasse burned. This load is 33 percent higher than that
allowed.
2. Visible emission observations were conducted as specified in Method 9
of the Standards of Performance for New Stationary Sources. Forty
observations at 15 second intervals were made during each particular
sampling test. At the time of the observations the plant was
operating normally; thus the results were checked against that
portion of the regulations which specifies that the plume opacity
shall not be equal to or greater than 40 percent. The average
opacities for the three observation periods ranged from 49-52
percent. Individual opacities as high as 90 percent were observed.
The results clearly show violations of the state regulations.
3. A visible emission evaluation by NEIC on May 1 showed an average
plume opacity of 27 percent. Between May 1 and May 25, the company
installed a 6000 kw generator which was operating at 1700 kw.
When operating at full capacity, the power generated beyond factory
demand will go to the Hilo Electric Light Company. However, at
the time of stack testing, connection to the power company lines
had not been made.
The effects on boiler operation due to operating the 6000 kw
generator at a much reduced capacity is not clearly defined
but there has been a significant change in visible emissio
between May 1 and May 25. At present there are wide fluctuations
in the steam production rates. Operating the 6000 kw generator
at full capacity may provide for more uniform boiler operation
which in turn may help control the visible and particulate emissions.
4. The company has not complied with the Hawaii Department of Health
Compliance Order issued July 27, 1973 in that the fractionating
dust collector has not been installed. Present air pollution
control equipment consists of a multiple cyclone dust collector
unit [Western Precipitation Corporation multiclonc unit]. The
unit was, according to company officials, retrofitted to the
Honokaa boiler. No attempt was made to determine the collection
efficiency of the multiple cyclone unit during the survey.
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POWER BOILER OPERATIONS AND EMISSION CONTROL EQUIPMENT
The Honokaa mill requires both steam and electric power to operate
the various mechanical equipment trains and the evaporative processes
in the plant. Steam generated in the bagasse-fired steam boiler is
used to generate electric power, to drive a portion of the mechanical
equipment, and in the sugar evaporation and concentration processes.
The electrical power requirement for the mill is approximately 1700
kw. The majority of the electrical power is supplied by two steam
powered turbine generators, one rated at 6,000 kw and the other at 1,500
kw. A 1,000 kw hydrogenerator is also available. This hydro-generator
is powered by runoff water which is available at approximately 240 m
(800 ft) of static head. The hydrogenerator supplies approximately
400 kw.
By late summer 1975, the company anticipates completion of an electrical
tie-in between their power generation facilities and the Hilo Electric
Liqht Company power distribution lines. A contract has been confirmed
with the latter by which the mill will supply 800,000 kw per month to
the distribution system. When this tie-in is completed, the 6,000
kw steam turbine generator will probably be operated near capacity.
Currently this unit is operated at approximately 1,700 kw.
POWER BOILER
The steam boiler is a Combustion Engineering two-drum water tube and
water wall unit. The boiler was built in 1954 and was originally
designed to be operated on pulverized coal and/or natural gas.
In its original configuration the boiler had a capacity of 7^,000 kg
(160,000 lb)/hour of steam at a delivery pressure of 29 kg/cm (425 psi).
In 1964 the boiler was installed at the Honokaa Sugar Company and
modified to burn bagasse as a primary fuel, with Bunker C fuel™1
being used as supplemental fuel. In 1974 it was father modified by
the Babcock and Wilcox Company to increase its capacity to 73,000 kg
(160,000 lb)/hr of 45 kg/cnf (650 psi) steam.
Bagasse from the milling process train is conveyed by belt to four
feed chutes at the power boiler. The weight of bagasse is determined
by a g.-r-Ki ray sensor type weighing scale located on the conveyor belt.
The bagasse continually discharges into the tour chutes keeping these
filled at all times.
The excess bagasse continues on the conveyor and is currently discharged
to the trash cleaning system with the majority going to landfill along
with the cane trash. The company is in the process of installing a
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piping system to convey the bagasse pneumatically to the landfill area.
Excess bagasse can also be diverted to storage if necessary. Moreover,
during periods when bagasse production from the milling process is
not sufficient to supply the boiler fuel demand, bagasse can be with-
drawn from storage.
The bagasse is fed into the boiler furnace by four spreader stokers,
one located at the bottom of each chute. The stokers propel the bagasse
into the furnace by rotating flipper arms. Approximately 50 percent
of the bagasse burns in suspension in the furnace with the remainder
burning on the furnace grates. The amount of bagasse introduced into
the furnace depends on the flipper arm speed. In turn, the speed of
the arms is controlled by the boiler steam demand rate; i.e., as the
demand for steam increases, the bagasse introduced into the boiler
increases.
Ash residue is removed from the furnace by dumping grates. There
are four such dumping grates in this furnace. One grate is dumped
about every hour. When a grate is dumped, the underfire air is
shut off, the unit rotated and the ashes dumped pneumatically into
a collection hopper. The ashes are steam ejected from the hopper into
an open trench below and then sluiced along with the excess bagasse
to the wastewater outfall.
Three manually operated atomized oil burners are located on the front
wall of the furnace unit. During 1974, 1,475 bbls of Bunker C fuel
oil were burned. The majority of this fuel oil was used during season
startup and shutdown. Fuel oil is also used during the normal operating
periods when the steam demand exceeds that available by burning bagasse
only. This occurs when the bagasse is extremely dirty or when the
bagasse feed systems are affected by mechanical problems.
STEAM DISTRIBUTION SYSTEM
A schematic drawing of the boiler power plant steam piping system
and an operational narrative, are included in Appendix B. A brief
description follows.
The boiler produces superheated steam at 42 kg/cnr (610 psi) and
425°C (800°F). Under current (May 1975) operating modes, the pressure
and temperature of a portion of this superheated steam is dropped to 42
kg/cm2 (600 psi) and 400°C (750°F). This latter steam is used to
operate the 6,000 kw steam turbine unit. The 6,000 kw turbine has a
back pressure exhaust of 16.5 kg/cnr (235 psi) steam. This steam
exhaust temperature is further dropped to 225°C (455°F) and discharged
into the 16.5 kg/cnr (235 psi) header system. Steam from this system
powers the mill train, another steam turbine generator unit, and after
further pressure reduction is used for other purposes within the plant.
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The new 6,000 kw steam turbine generator is not currently operated
at full capacity, thus the supply of 16.5 kg/cm2 (235 psi) exhaust steam
does not meet the needs of the plant. Upon completion of the electrical
tie-in to the Hilo Electric Company, it is anticipated that this unit
will be operated at full capacity and the exhaust supply will be adequate
for plant needs. However, in the interim period a portion of the 42 kg/cm^
(610 psi) superheated steam from the boiler is run through a pressure
reducing station and desuperheated to provide 16.5 kg/cnr (235 psi),
225°C (435°F) steam. This steam is then introduced into the 16.5
kg/cm2 (235 psi) header system described above.
The 16.5 kg/cm2 (235 psi) steam is used at this pressure or further
reduced to satisfy various equipment requirements. The majority of
the equipment exhausts at 1 kg/cm2 (15 psi) steam which is collected
in an exhaust header main and used in the sugar evaporation and
concentration processes.
AIR POLLUTION CONTROL EQUIPMENT
Particulate emissions from the bagasse-fired boiler originate from
unburned bagasse, ash, and soot which are entrained in the combustion
gases. Combustion air is supplied to the furnace by a forced draft
fan (FD) which draws in ambient air and forces it through an air preheater
unit. From the air preheater unit the warm air is introduced into the
furnace, both below the ash grates and through overfire air ports. The
air supports the combustion of the bagasse both on the grates and in
suspension. The combustion gases are then drawn by an induced draft
(ID) fan up through the steam superheater and boiler tubes, and
exited through the upper rear portion of the boiler. These exhaust
gases then pass through the air preheater unit, a cyclone dust collector,
the ID fan and are exhausted to the atmosphere through a 2.1 m (6'10")
diameter, 12.2 m (40 ft) high steel stack.
The cyclone type dust collector is a Western Precipitation multiclone
unit, Type 9VGRAB-14, Model P-94348-B, size 200-10. The unit has 200
individual cyclone units and is rated at 171,000 kg/hr (376,000 Ib/hr)
of exhaust gas. This figure translates to approximately 4,700 actual
m3/min (166,000 acfm) of exhaust gases. According to company officials
the multiple cyclone unit which was retrofitted to the boiler was
installed in 1972.
Ashes collected in the multiclone unit fall into hoppers below and
are sluiced from here along with excess bagasse to the trash dewatering
system and thence into the effluent channel.
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DISCUSSION OF STUDY
STACK MONITORING
Stack monitoring, as previously mentioned, was conducted on May 25 and
26, 1975. The equipment used, the testing, calibration, and the sample
handling procedures followed are discussed in Appendix C.
The boiler stack at the Honokaa Mill is 2.08 m (6.83 ft) in diameter.
The sample ports are located approximately 8.25 m 27 ft) above the
exhaust gases inlet to the stack and 4.27 m (14 ft) below the stack
top [Figure 1]. The company had recently installed four ports located
at 90 degree intervals on the stack circumference. Because a 3.05 m
(10 ft) probe was used, sampling was accomplished through the north
and east ports. Sampling was accomplished in accordance with the Federal
Regulations (Method I)2 which dictate the number of sampling Points
necessary based on port location. In this case the ports are slightly
more than four diameters downstream from a disturbance (i.e., tne
point where exhaust gases enter) and two diameters upstream from the
exit; thus 36 points were required.
Each point was sampled three minutes in order that 1.7-2.1 m3 (60-75 ft )
of air could be sampled during a test. The heavy particulate load
required two filters per test. Three tests, one on May 25, and two on
May 26 were conducted. Isokineticity ranged from 97.7-102.4 percent*
[Table I].
Samples were recovered as specified for Method 52 [Appendix C]. The
samples were shipped to the NEIC laboratory in Denver for analyses
[Appendix D], The NEIC Chain of Custody procedures were followed.
During the stack monitoring NEIC personnel observed boiler operating
procedures in the control room. Pertinent operating readings were
obtained every ten minutes from the boiler instrumentation panels.
These data included the steam production rate, bagasse production
rate, superheater steam pressure and temperature, feed water pressure
and temperature, and feed water flow rate [Appendix B]. The average
steam production rates [Table II] during monitoring ranged from about
75-88 percent of the boiler capacity of 72,600 kg (160,000 lb}/hr.
The steam production rates during any one monitoring test differed by
as much as 14,980 kg (33,000 lb)/hr [Appendix B]. These varying steam
demand rates result from changes in processing operation, e.g., the
boiler house steam demand drop when a vacuum pan is pulled. Stack
monitoring was stopped on one occasion during test 3 when a breakdown
in the mill reduced the steam demand to 46,760 kg (103,000 Ibj/hr.
When repairs were completed and the steam production rate increased to
54,400 kg (120,000 lbs)/hr, sampling continued.
*Isokinetic sampling can be defined as sampling in a manner so that the
sampling velocity (Vn) is equal to the stack velocity (Vs) If
Vn < Vs i.e., percent less than 100, sampling is under isokinetic, if Vn > Vs
sampling is over isokinetic. For a valid test sampling must be in the
range 90 to 110 percent.
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SAMPLING PORTS
- 2 O8m -
(6 83ft)
I D FAN BY-PASS
E
n
E O
n -^
01 i-
co ^,
(used only during
boiler start-up)
SCALE
1 cm=O 72m
(1m=6ft)
NORMAL GAS FLOW
FROM I D FAN
Figure I. HonaKaa Boiler Stack
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TABLE I
SUMMARY OF STACK MONITORING RESULTS
HONOKAA SUGAR COMPANY
MAY 25-26, 1975
Test 1 Test 2 Test 3
Volume Metered
liters
(SCF)l/
Average Stack Temperature, °R
Molecular Weight
Percent Moisture
Stack Gas Velocity
M/Sec
Ft/Sec
Stack Gas Volume (Actual)
M3/Min
(Ft3/Min)
Percent Isold netic
Parti cul ate Collection-'
Front Half - gm
Back Half - gm
Total - gm
Bagasse Fired
Kq/hr
(Ib/hr)
Emission Rate
Front Half Collection
Kg/100 Kg Bagasse
(Lb/100 Ib Bagasse)
Total Collection
Kg/100 Kn Bngasse
(Lb/100 ID Bagasse)
1853
(65.45)
987
27.1
23.4
23.9
(78.5)
4,900
(173,000)
97.7
2.54
0.57
3.11
31,300
(69,000)
0.52
(0.52)
0.64
(0.64)
1931
(68.19)
989
27.3
20.9
24.0
(78.7)
4,888
(172,600)
98.7
2.41
0.48
2.89
27,900
(61,600)
0.55
(0.55)
0.66
(0.66)
1954
(69.01)
967
27.6
19.6
22.7
(74.4)
4,633
(163,600)
102.4
2.23
0.50
2.74
25,700
(56,600)
0.53
(0.53)
0.65
(0.65)
I/ SCF - Standard Cubic Feet
2/ Front half collection - Particulates contained on the filter, in the
cyclone, and in the sampling probe and nozzle.
Back half collection - The particulate material collected in the Impinger
case is in a gaseous form at 120°C (248°F) but condenses at lower
temperatures. This back half material is not at present considered as
part of the stack emissions for new stationary sources.
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TABLE II
SUMMARY OF BOILER OPERATING DATA
HONOKAA SUGAR COMPANY
MAY 25-26, 1975
NEIC Observations
Date and
No. Time
1 5/25/75
(1000 to 1300 hrs)
2 5/26/75
(0800 to 1100 hrs)
3 5/26/75
(1400 to 1700 hrs)
Steam
Production
kg (lb)/hr
64,400
(142,000)
61,700
(136,000)
54,000
(119,000)
Company Supplied Data
Bagasse Steam
Production Production
kkq (tons)/hr kq (lb)/hr
30.0
(33.1)
29.4
(32.4)
27.8
(30.6)
63,500
(140,000)
61,200
(135,000)
54,400
(120,000)
Bagasse
Fuel Used
kkq (tonsWhr
31.3
(34.5)
27.9
(30.8)
25.7
(28.3)
Bagasse
Moisture kg(lb) Steam
Content /kg(lb) bagass<
49.3 2.03
48.0 2.19
49.3 2.12
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During monitoring, personnel from the Honokaa Sugar Company were
obtaining samples of the bagasse produced and the raw cane processed.
From these samples the moisture content of the bagasse produced, and
the percentage of bagasse fiber in the raw cane were calculated. The
company routinely measures the amount of sugar produced over a given
time. Knowing this figure, the cane-to-sugar ratio, and the cane-to-
bagasse ration, the company then extrapolates the amount of bagasse
produced per hour of operation.
The NEIC requested and obtained certification of certain production
and boiler operating parameters for the test periods [Appendix B].
These certified data compare favorably with the numbers collected during
NEIC observations. The bagasse usage figures provided by the company
were used to calculate the particulate emission, i.e., kg/100 kg (lb/100 Ib)
of bagasse burned.
To ascertain the particulate emissions the amount of material collected
on the filter and in the cyclone along with any material contained in
the sampling probe and nozzle, i.e., the "front half" of the sampling
train were measured [Table I]. The results show that the average
particulate emission for three tests was 0.53 kg/100 kg (0.53 lb/100 Ib)
of bagasse burned. This violates the state regulations which specify
the particulate emissions shall not exceed 0.4 kg/100 kg (0.4 lb/100 Ib)
of bagasse burned.
The "back-half" collection represents the particulate material collected
in the impinger case and is that material existing in a gaseous state at
120°C (248°F) but condensing at lower temperatures. This material is
not presently considered in determining particulate emissions. It
is presented herein for information purposes only [Table I].
It should be noted that the company estimates that about five percent
of the total bagasse production is wasted in the current operating
modes, hence the amount of bagasse certified as being used as fuel is
generally lower than the numbers monitored by the gamma weight scale
in the cane mill. As mentioned previously the present air pollution
control equipment consists of a multiple cyclone unit which, according
to company officials, was retrofitted to the Honokaa boiler. The
collection efficiency of these units depends on numerous factors such
as dust particle size, particle density, inlet gas velocity, cyclone
body length, cyclone diameter, smoothness of cyclone walls, gas viscosity,
and gas outlet and inlet diameters. No attempt was made to determine
the collection efficiency of this particular unit during the survey.
The complete field data and analytical results are on file at NEIC and
are available upon request.
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VISIBLE EMISSION EVALUATION
Visible emission evaluations were conducted as specified in the Federal
Regulations (Method 9)2. Forty observations taken at 15 second intervals
were made for a ten minute period during each particulate sampling test.
At the observation times the plant was operating normally; thus the
results were checked against that portion of the regulations that
specifies the plume opacity shall not equal or exceed 40 percent opacity.
The average opacities during tests 1, 2, and 3 respectively were 52,
51, and 49 percent. Opacity reading ranged as follows: Test 1, 40-70
percent; Test 2, 40-90 percent; and Test 3, 35-90 percent [Appendix EJ.
The average opacities as well as most of the individual observations
violated the aforementioned state regulations.
A SIP inspection was conducted by NEIC personnel May 1, 1975. Visible
emission observations at that time showed an average plume opacity of
27 percent3. Between May 1 and May 24 the company placed a 6,000 kw
steam turbine generator on line. When operating at full capacity the
power beyond factory demand (approximately 1,700 kw) will go to the
Hilo Electric Light Company. However, at the time of stack testing,
the tie-in to the electric company transmission lines had not been
completed; thus the generator was operating at about 1,700 kw.
The effects on boiler operation because of the reduced generator operating
rate are not clearly defined but there has been a significant change in
the visible emissions from those observations made May 1 and those
made during stack testing. At present there are wide variations in
steam demand. Operating the boiler at a more constant steam production
rate may reduce the visible and particulate emissions.
This mill was issued a compliance order by the Hawaii Department of
Health on July 27, 1973 regarding its bagasse-fired boiler. The order
found the company in violation of the particulate and opacity regulations
and required the following approach to attain compliance:
1. By January 30, 1974, install an over-fire air system on the boiler.
2. By January 30, 1975, install a fractionating dust collector
(attendant to the existing multiclone unit).
3. By May 31, 1975, achieve compliance.
The company attained compliance with item 1 but has not installed the
dust collector and as the study results show has not achieved compliance
with the opacity and particulate emission regulations.
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REFERENCES
Public Health Regulations, Air Pollution Control, Department of
Health, State of Hawaii, Chapter 43, March 21, 1972.
Standards of Performance for New Stationary Sources, Environmental
Protection Agency, Federal Register, Vol. 36, No. 247, Part II,
Appendix Test Methods, December 23, 1971.
3SIP Report "Inspection of Honokaa Sugar Company," Environmental
Protection Agency, NEIC, June 30, 1975.
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APPENDIX A
PROCESSING OF SUGAR CANE-/
The processing of sugar cane to raw sugar and molasses generally
follows the steps discussed below [Figure Al].
Cane Cleaning
The replacement of hand cutting by mechanical harvesting has resulted
in an increase of mud and dirt content. This has necessitated cane
washing and it is the practice generally followed at mills on the Island
of Hawaii at the present time.* The cane is usually washed with warm
barometric condenser waters.
Milling
Following cleaning, the cane proceeds into the milling process of
which the purpose is to extract the juice from the cane stock. This
extraction is accomplished with revolving cane knives, shredders,
crushers, and roll mills. The knives cut the cane into chips in preparation
for grinding and to provide a more even feed rate to the mills. Shredders
further prepare the cane. These two operations increase mill capacity.
The crushers extract 40-70% of the juice. After the juice is extracted,
the remaining material (bagasse) representing about 30% by weight of the
cane entering the system, is usually used as feed for the boiler system
with the excess being hauled to landfill or, in some cases, discharged
in the wastewater.
Clarification
The juice from the milling operation contains impurities such as
fine particles of bagasses, gums, and waxes. Screening will remove the
courser particles which are returned to the mills. The majority of the
I/ Development Document for Interim Final Effluent Limitations Guidelines
and Proposed New Source Performance Standards for the Raw Cane Sugar
Processing Segment of the Sugar Processing Point Source Category,
Effluent Guidelines Division, Office of Water and Hazardous Material,
U.S. Environmental Protection Agency, Washington, D.C. 20460, pp 32-46.
*Hilo-Hamukua Coast of the Island of Hawaii Raw Cane Sugar Processing subcat-
eqories.
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remaining impurities are removed by clarification.
In the clarification process lime, heat and a small amount of phos-
phate are used to aid in removing the remaining impurities. During the
process a flocculent precipitate is formed and most of the suspended
solids remaining in the juice are occluded and settle out with the
precipitate. The precipitate is separated from the juice by settling
and decantation in continuous clarifiers.
Filtration
The clarification process separates the juice into two portions:
(1) the clarified juice and (2) the precipitated sludge or muds. The
first portion represents 80-90% of the juice which is usually taken directly
to the evaporator system. The second portion is generally thickened by
rotary vacuum filters. The filtered juice is cycled back through the
clarification system.
The filter cake produced (20-75 kg/kkg or 40-150 Ibs/ton of cane
ground) has a moisture content of 70-80 percent. It is general practice
to collect the cake in storage bins for subsequent removal to the cane fields.
In most cases, the filter cake is not discharged.
Evaporation
The clarified juice is about 85 percent water and 15 percent solids.
To obtain crystallization, enough water must be removed to produce a
60 percent solids syrup. This concentration process is usually accomplished
using multiple-effect evaporators in the interest of better fuel economy.
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Crystallization
The concentrated syrup from the evaporators is placed in single effect,
batch type evaporators called "vacuum pans". The pans are operated
using exhaust steam or vapor from the first stage evaporators discussed
above. Seed crystals are introduced into the vacuum pan at the beginning
of the operation. The pan must be maintained in a narrow range of sugar
concentration and temperature so that the seed crystals grow.
After sugar crystals form in the pan, the mixture of crystals and
syrup (massecuite) is agitated gently in a mixer. After mixing, the
crystals are separated from the syrup in a high speed centrifuge with
the raw sugar going to storage.
•
The vacuum pans generally operate in series with each pan
crystallizing a different grade of massaceuite. The last pan yields
a low sugar and final (blackstrap) molasses which is usually used for
animal feeds. The low grade sugar off the final pan is subsequently
melted into syrup and mixed with the syrup from the evaporators.
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Roller Food Water
C'.-r:Ms.:m
Discharge
Cane
j
Molasses
Washing
Condenser
Water From
Barometric
Leys
Lcvclcr Cane ,
— kr X >
•, u, — B- Car
^--zzZZZ^-
i
Cane Wa
to Disu
or Recy
\ / V J \
\ uiiu u:~"U '
V- JzL _ .iL.
— r'ZjS^-^/Ivl
Electricity T" H
Steam ' " ^
i
Turbogenerators pn,r<
steam Turbines °* \\^\^
Disc!-
1 1
Mechanical Mill Drive
•• Wash Imbibitior
J U __—- r-TTS.
\ /|X ~~3* "\I^LO Crusher il5£5?£yf Lei.
•:n~"Knives • ;/^O^'^'^>\-X>Xi>'"Vx
t^ %^%^^:^
Screening*: NEPJ Xl^'-CO NfO'S) NlO'-C
^
-------
Juice'From
Mining
(Sheet 1)
Weighing
Lime
Juice
Condenser
Cooling
Water
Heaters
Condensate
"11" To Condensate
Storage (Sheet 1)
CLARIFIEP.S
Water
Clarifier
Clarified Juice
bcum
Filter Cake
Discarded
Barometric
Leg
Condenser
Water to
Cane Wnsh,
Other Uses,
or Discharge
Multiple Effect Evaporation
Syrup to Vacuum
Pans (Sheet 3)
TYPICAL EVAPORATION SYSTEM
FIGURE A-l
Sheet 2 of 3
-------
SYRUP FROM
EVAPORATION
(Sheet 2)
Condenser Water to Cane Wash, Other Uses, or Discharge
-- ,--<•
_
A
VACUUM
PAN
L J
tfi)~~ Steam
Seed Sugar
^:../"
Mixer
^A" Molasses
VACUUM
PAN
Centrifuge
Condensate to
Conc'cnsate Tank
('Sheet T)
*"*""" Steam
«o— Seed Sugar
*
•N J MO'SASSES
~| lA-'IKS
Water •
s~~^
~~
1
X
X
c
VACUUM
PAN
31
«*—
I I
Steam
M1xer
(5~O~6 Crystalllzers
"R"
asses
Centrifuge
Commercial
Raw Sugar
Mixers
I Centrifuge
—js. Final Molasses
Seed Sugar
TYPICAL SUGAR COILING SYSTEM
FIGURE A-l
Sheet 3 of 3
-------
APPENDIX B
STEAM PIPING SYSTEM
AND
BOILER OPERATING DATA
HONOKAA SUGAR COMPANY
-------
HONOKAA SUGAR COMPANY
MARCH 18. 1975
A BRIEF DESCRIPTION OF THE STEAM PIPING & SYSTEM FOR THE 1975 CROP.
REFER TO THE ATTACHED SKETCH
BOILER; Steam will be generated at 6100 and 800+eF., at the superheater outlet. Pressure will be controlled by a
new Kagan controller in the back of the upright panel.
6000 Steam to the 6000 kW Generator will be desuperheated (1.) to 750°F and should enter the turbine at 6000 and 750*P.
The generator will not go on line until April.
600ff Stean reduced to 1359 for makeup. The 6000 steam is pressure reduced through two pressure control valves (A)
located beside the walkway to the top of the Control Room. It will then be desuperheated to 435'F by desuper-
heater (2) located at the boiler end of the old 2350 header.
This steam will supply the mills, fans, and turbine boiler feed pump as previously.
The entire boiler output will pass through this pressure reducing desuperheating system until such time as
the 6000 kW generator is put on line.
2350 Generator Exhaust Steam. This will, normally, when the 6000 kW generator is in operation, provide an adequate
supply of 2350 steam to satisfy the demand of all the 2350 steam driven turbines; Including operation of the
1500 kW generator, on part load.
The exhaust steam will be conditioned by desuperheater (3) to a temperature of 435'F.
If for some reason the supply of exhaust from the 6000 kW generator is inadequate, as the pressure drops,
the pressure control valves (4) will open and maintain a pressure slightly lower than 2350 and ensure
continuity of operation.
Boiling House Supply. The same control system (5) as used in previous years to control mill engine and boiling house
pressure at 1500, will be used to maintain a 1250 supply to the boiling house. The fuel oil heaters supply
is piped from the boiling house line.
New Mills. A 12" valve (9) has been provided to supply steam to the new mill building.
1500 kW Generator. The pressure control valve (6) will reduce 2350/1750 for this generator, as previously.
Deaerator Pressure. (Now 110 to 150) A new pressure control valve (7) will reduce 2350 steam to 110 and maintain
! this pressure in the cleaeralor when the 150 exhaust pressure drops below 110. This will provide hotter
j boiler feed water and improve the operation of the deaerator.
I Sootblowers. A 7000/2350 pressure control valve (8) will provide low pressure steam, from the drum to the soot blowers.
j Operation. Since the above control systems are automatic, there will normally be no need for the operator to do more
! than monitor steam temperatures and pressures, to satisfy himself that the systems are working correctly.
I However, if a control malfunctions hand operation can be used, where provided, to manually control critical
| temperatures or pressures.
i
Several changes have been m.-"!-; to the annunciator and temperature indicator systems to give warnings and
enable you to monitor the ci.'-ical points.
A temporary, amended log sheet will be used until a new log sheet can be'prepared.
-------
-------
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7^3 X^Xv /£n. 3v**~~£CL<> d
-------
ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER-DENVER
BUILDING 53. BOX 25227. DENVER FEDERAL CENTER
DENVER, COLORADO 80225
On the basis of my experience with the operation of this plant,
I submit that the following figures are the best determinations of the
pertinent operational parameters for this facility during the period
2;00 P.M. to 5;QO P.M. May 26 , 1975.
28.25
49.3
Negligible
120,000
Average bagasse usage
Average bagasse moisture content
Fuel oil usage (average)
Steam production (average)
Juice production (average)
Boiler efficiency
CERTIFIED/^///,
L I (/ ? I
x^tf' I*- ' <•'-' "3 < ^ ' Factory Superintendent
Signature Title
C. Rowsell
200,000
Not Known
Honokaa Sugar Co.
Haina
tons/hr
gal/hr
Ibs/hr
Ibs/hr
May 28, 1975
Date
Plant
As sanitary engineer for the Environmental Protection Agency, I agree
that the above figures are the best determinations of the pertinent opera-
tional parameters for this facility during the period 2. '00 P.M. to
5rOO P.M. May 26 _ , 1975.
7/22/75
Signature
Title
t
7,
Date
Signature
Chief, Field Operations Branch 7/22/75
Title Date
-------
ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER-DENVER
BUILDING 53. BOX 25227. DENVER FEDERAL CENTER
DENVER. COLORADO 80225
On the basis of my experience with the operation of this plant,
I submit that the following figures are the best determinations of the
pertinent operational parameters for this facility during the period
StOO A.M. to lliOO A.M. May 26 1975.
Average bagasse usage
Average bagasse moisture content
Fuel oil usage (average)
Steam production (average)
Juice production (average)
Boiler efficiency
30.81
tons/hr
48.0
Negligible gal/hr
135.000 Ibs/hr
240,000 Ibs/hr
Not Known
Signature
C. Rowsell
Honokaa Sugar Co.
Factory Superintendent May 28, 1975
Title Date
Ha ili
Plant
As sanitary engineer for the Environmental Protection Agency, I agree
that the above figures are the best determinations of the pertinent opera-
tional parameters for this facility during the period 8:00 A.M. to
11:00 A.M. , May 26 , 1975.
Signature
,j
-------
ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER-DENVER
BUILDING 53. BOX 25227. DENVER FEDERAL CENTER
DENVER. COLORADO 80225
On the basis of my experience with the operation of this plant,
I submit that the following figures are the best determinations of the
pertinent operational parameters for this facility during the period
10;00 A.M. to 1;00 P.M. . May 25 _ , 1975.
Average bagasse usage
Average bagasse moisture content
Fuel oil usage (average)
Steam production (average)
Juice production (average)
Boiler efficiency
34.45
49.3
Not Known
Signature
C. Rowsell
r -f
'fs)t*;* c U.
Factory Superintendent
Title
Hr-o'.aa S-irar Co.
tons/hr
Negligible gal/hr
140.000 Ibs/hr
270,000 Ibs/hr
May 28, 1975
Date
Plant
As sanitary engineer for the Environmental Protection Agency, I agree
that the above figures are the best determinations of the pertinent opera-
tional parameters for this facility during the period 10:00 A.M. to
1:00 P.M. May 25 , 1975.
Signature
^Y^yi-^f^^<-
Title
7/22/75
Date
Signature
Chief. Field Operations Branch 7/22/75
Title
-------
TM
APPENDIX C
STACK MONITORING PROCEDURES
Equipment
Particulate samples were collected using a Scientific Glass
sampling train equipped and operated as required by "Method 5 - Determi-
nation of Particulate Emission from Stationary Sources"!/. The method
requires that the stack gas be sampled between 90 and 110 percent
isokinetically; i.e., the kinetic energy of the stack gas must equal the
kinetic energy of the gas entering the sample nozzle within +^10 percent.
Since the kinetic energy of a gas is dependent only upon the mass and
velocity of the gas stream and the mass of the gas entering the nozzle is
equal to that in the stack at any given time, isokineticity can be satis-
fied by adjusting the gas entry velocity into the nozzle to that of the
stack velocity. The two velocities are related by an equation using
pressure drop across a S-type pitot tube (stack velocity) and a calibrated
orifice (nozzle velocity) located just prior to where the sampled gas exits
from the train. Rapid adjustments to the isokinetic sampling rate are made
possible by the EPA - Method 5 sampling train shown below and a (nomograph
which rapidly solves tlie pressure drop equation.
• •' 'n ,
IMplNGFR TJ-A'.H
/
HEATED AREA FILTER HOLDER
PROBE
REVERSE-T7PE
pitor TUBE
CHECK
.VALVE
,VACUU.U
LIME
THERSCMETERS'
DM TEST METER AlR-TIC,nr
PUMP
]_/ Standards of Performance for New Stationary Sources, Environmental
~~ Protection Agency, Federal Register, Vol. 36, No. 247, Part II,
Appendix-Test Methods, Method 5, December 23, 1971.
-------
-2-
The probe is moved to the location to be sampled and the velocity
pressure in the stack (pitot tube pressure differential, ^P) is read
on an inclined monometer. Using the nomograph, the operator solves
the equation and manually adjusts the sampling rate to obtain the desired
pressure drop across the calibrated discharge orifice.
The stack gases are pulled through the nozzle and probe to a cyclone
which collects large particulates and then through a glass fiber filter
which collects the remaining particulates. The train to this point is
heated to 120°C (248°F) to eliminate conder.batior,.
The gases then pass through four impinger tubes which are partially
immersed in ice water to maintain temperatures around 21°C (70°F).
The first two impinger tubes are prefilled with 100 ml of distilled water.
The third is empty and 200 gms of silica gel is added to the fourth. A
Greenburg-Snn'th impinger is used in the second tube; modified (3.8 cm
(1.5 inch) ID opening). Greenburg-Smith impingers are used in the first,
third and fourth tubes. The first three tubes collect water vapor and
other condensable material. The air is dried by the silica gel in the
fourth tube. As shown in the preceding figure, the heated box and impinger
case are at the stack.
The clean, dry gases then flow through the umbilical cord to the
leakless vacuum pump located at the control console. The pump operates
at a constant rate; valves adjust the amount of pump discharge air
recycled to the inlet of the pump and the amount drawn through the
nozzle to the pump. Since the pump is leakless, the air which is pulled
through the nozzle is equal to the amount which discharges from the
-------
-3-
pump under positive pressure to the 4.96 cmh (175 cfh) Rockwell dry
gas meter. Air discharges from the meter through the calibrated orifice
to atmosphere.
During the test, temperatures were measured at six points throughout
the train with chromel-alumel thermo-couples and displayed on a digital
temperature indicator (DTI) at the control console. The locations
monitored for temperature are the stack gas, the probe, the filter oven,
the impinger exit, the inlet to the gas meter and the exit from the gas
meter.
Molecular weight of the stack gas was determined using an Orsat
analyzer to analyze a composite sample taken with a hand pump during the
test period. The Orsat analyzer contains three reagents which selectively
absorb C02« QZ and C0* Tne molecular weight was then calculated by
assuming that the remaining gas was nitrogen.
Static pressure of the stack was determined by facing the openings
of the S-type pi tot tube parallel to the gas stream. The pressure differ-
ential (compared to atmosphere) was read on the inclined monometer at the
control console. Barometric pressure was read from a Lloyds barometer.
The percent moisture of the stack gas was estimated for the first test.
The calculated moisture content from each test was used for the following
test.
Calibration
The DTI was calibrated on site with a Mini Mite ™ pyrometer.
Nozzle diameter was measured with calipers to an accuracy of +. 0.025 mm
(+ 0.001 inch).
-------
-4-
Napp Inc. manufactured the S-type pi tot tube used for stack velocity
pressure measurement. A record of the Napp Inc. calibration of the pi tot
tube is on file at NEIC. The gas meter was calibrated by the Public Service
Company of Colorado. This calibration was checked by NEIC personnel against
an American ™ wet test and found to be accurate with +. 1%. Just prior to
use the meter calibration was again verified to be accurate by the Gasco Co.
in Honolulu, Hawaii. The discharge orifice was also calibrated by NEIC
against the wet test meter and was found to have a reference pressure drop
of 1.72 at a flow rate of 0.021 Std M3/min (0.75 scfm).
Test Procedure
The points for obtaining the particulate sample were located approx-
imately 11.6 m (38 ft.) above the ground on the bagasse boiler stack.
There were four ports located at 90° intervals around the circumference
of the 2.08 m (6.83 ft) diameter stack. These ports are located approxi-
mately 8.25 m (27 ft) above the exhaust gases inlet and 4.27 m (14 ft)
below the stack top. The NEIC team used a 3.05 m (10 ft) probe, thus
only the North and East ports were required. Thirty-six sample points
were required by Method 1 to obtain a representative sample because
of the port locations; i.e., 4 diameters downstream from a disturbance
2 diameters upstream.!/ The points were located at the centroids of
thirty six equal area portions of the total stack cross section. Eighteen
points were sampled on each diameter.
I/ Op. Cit. Method 1
-------
-5-
The static pressure was determined and a velocity traverse was
made. These data and estimates of percent moisture and molecular weight
were required to select a nozzle diameter. After the nozzle was selected,
the nomograph was set and a leak check of the sampling train was performed.
EPA Method 5 allows no more than 566 cc (0.02 cubic feet) leakage per
minute. After satisfying the leakage requirements, the probe was inserted
to the first sampling point and the test began.
The stack gas was sampled for three minutes at each point for a total
of 108 minutes sampling per test. This amount of time was adequate to
obtain the desired 1.7 - 2.1 m3 (60 - 75 ft3) of air. The 3 minute
sampling time per point was a deviation from that prescribed for Method 5
in the December 23, 1971 Federal Register which calls for a minimum of
5 minutes per sampling point. However, revisions to Method 5 are being
promulgated changing the minimum sampling time to two minutes. Current
practice is to sample a sufficient time (but not less than two minutes
at each point) to obtain the aforementioned air volume. Sampling for 5
minutes at a large number of points yields a larger than desirable air
volume.
Sample Recovery
At the end of the sampling period, the sample was recovered as
specified in Method 5l/. The probe was removed from the stack and
disconnected from the train. All open connections were capped immediately
to prevent gaining or losing particulate. The probe and nozzle were
rinsed with acetone and brushed. The rinse was collected in a clean glass
jar for later analysis.
Ibid
-------
-6-
The glass-ware portion of the train was taken to the plant chemistry
laboratory for clean-up. The filter was placed in a glass petri-dish
and sealed with aluminum foil. All glass-ware between the filter and the
probe was rinsed with acetone. All of the acetone rinse from this
portion of the train was placed in the same jar as the probe rinse.
Water from the impingers was measured and the silica gel weighed
to determine percent moisture in the stack gas. The water was placed in
a jar for subsequent ether-chloroform extraction. All back-half glass-ware
was rinsed with acetone which was collected in a third jar. A sample of
the distilled water and acetone used was also taken to determine what
weight was added to the samples from the clean-up liquids.
All samples were shipped to the NEIC laboratory for analysis.
Samples were handled under standard NEIC chain of custody procedures.
-------
APPENDIX D
ANALYTICAL PROCEDURES FOR
STACK MONITORING SAMPLES
Filters
(Jelmans glass filters were preweighed directly on the pan of a Mettler
analytical balance after 24 hours desiccation. They were then placed in
petri dishes prewashed and acetone rinsed. Finally, the petri dishes
were completely wrapped in foil to exclude dust.
Upon receiving the filters back in the lab they were placed in pre-
weighed 100 ml beakers. The aluminum foil used to seal the filters
was found to be free of parti culates collected during the sampling phase
and, therefore, discarded. One unused filter was used as a control.
Beakers were weighed until constant weight was achieved. As the material
on the filters rapidly picked up weight upon removal from the desiccator
only about three filters could be weighed at a time.
Chloroform - Ethyl Ether Extracts
The materials used here were a 25 ml graduate, 2000 ml separatory funnels,
pre-weighed 100 ml beakers, two square yards of chiffon nylon cloth, and
Burdick and Jackson brand solvents.
Each sample was serially extracted with three 25 ml portions of CCls then
three 25 portions of ethyl ether. The combined extract, in a 100 ml beaker,
was placed in a hood and the air intake covered with a nylon chiffon
cloth to prevent dust and parti culates from entering the sample. After
air drying, the sample was desiccated and weighed until constant weight
was achieved.
Hater Portions
The water portions v/ere measured before extraction in a large graduate
cylinder. After extraction they were taken down in 800 ml beakers and
transferred to 100 ml pre-weighed beakers and taken to dryness. The take
down was done on a concentric ring type water bath at approximately 95°C.
Measurements were recorded when constant weight was attained.
Acetone Rinses
These were first taken down in the quart sample containers inside of a
hood, the intake of which was covered with nylon cloth to restrict dust
from entering. When the samples were below 100 ml, they were transferred
to pre-weighed 100 ml beakers and taken down to dryness. The entire take
down procedure was accomplished at around 70°F and a blank was run along
with the samples. After no acetone smell could be detected, the samples
were placed in a desiccator and weighed 24 hours later. In some cases,
constant weight was not achieved until several days later.
vu~/( C . t£
Richard C. Ross
-------
Hawaii Air Sampling - Summary of Results***
Filters
Sample No.
4201-0526(02)
4201-0526 #2)
4202-0528 #1)
4201-0525 #1)
4201-0525 #1)
4201-0526 #3)
4201-0526(#3)
4202-0529(02)
4202-0529(#2)
Blank
CCU-Ethyl Ether Extract Residues
4202-0529 #2)
4202-0529 #1)
4202-0529 #3)
4202-0528 #1 )
4201-0526 #2) (Blank)
4202-0529(03) (Blank)
4201-0525(#1)
4201-0526(02)
4201-0526(03)
Water Residues - Post Extraction
4202-0529(02)
4202-0529(01)
4202-0529(03)
4202-0528(01)
4201-0526(02) (Blank)
4202-0529(03) (Blank)
4201-0525 #1)
4201-0526 02)
4201-0526 03)
Particulate Wt.
.3326
.3968
.4698
.3692
.3166
.2811
.3580
.3444
.4265
-.0002
Residue Weight (g)
.0081
.0194
.0043
.0006
-.0006
-.0007
.0670
.0575
.0553
Weight (g)
.1407
.0446
.1032
.0375
.0039
-.0003
.4907
.4056
.4019
Acetone Residues Weight After 24 hrs (g)
4201-0526(02)F.H.*
4201-0526(02)6. H.**
4202-0529(03) Blank
4201-0525(01) Blank
4201-0525(01 )F.H.
4201-0525(01 )B.H.
4202-0529 03)F.H.
4202-0529(03)6. H.
4202-0529(02)F.H.
4202-0529(02)8. H.
4202-0528(01 )F.H.
4202-0528(01 )6.H.
4201-0526(03)F.H.
4201-0526(03)6. H.
*F.H. Front Half Collection **Back
2.2073
.0320
.0026
. .0055
1.8652
.0242
.8474
.0129
.6884
.0285
.8641
..0383
2.5003
..0522
Half Collection
(fl)
***4201-Honokaa
Sugar Mill
4202-Kekaha
Sugar Mill
Original Water Volume
505 ml
620
560
265
275
435
705
865
775
Constant Weight (g)
1.6843
.0320
..0026
.0055
1.8528
.0242
.8434
.0129
.6866
.0285
.8614
.0383
1.5995
.0522
-------
APPENDIX E
VISIBLE EMISSIONS EVALUATION
HONOKAA SUGAR COMPANY MILL
MAY 25-26, 1975
-------
Dale I
Obsfc rver
ENVIRONMENT PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER- DENVER
BUILDING 53. BOX 25227. DENVtR FEDERAL CENTER
DENVER, COLORADO 80225
Location
//<&*=*
Address
— — r" Po. * AI'S*"-'// *-^f-
Stack - Distance From^/J"^ Height
Wind - Speed ^5~ Direction ,--^"7^,, —
Type of Installation S^Jft^f^ (~<^ SH* /?)!//
J-uel X&M-,><-<,*
Observation began/^^^Ended /.p 3 ^-
Remarks: / i
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31
32
33
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36
37
38
39
40
41
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43
44
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47
48
49
5C
51
52
53
54
55
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!
Jcr Mr. Cyril Rowsell ,
ractory SUpfirlntendeilL
"KB iir>.-.^im ^iina»» fninnanv
Haina, Hawaii, Hawaii
-------
ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER-DENVER
BUILDING 53. BOX 25227. DENVER FEDERAL CENTER
DENVER, COLORADO 80225
Date «*3 /$.&/'? ^'5,
Observer ' £?/ 4 /
Type of Installation fift/^^f f-X/5* t-t-fc *•*-
V) ( If / ' — •
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Observation began /<"/# Ended /0 ff)
Remarks: ,
$>vn ki^L &n
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-------
3
Date
Observer
ENVIRONMENTAL PROTECTION AGENCY
OFFICE OF ENFORCEMENT
NATIONAL FIELD INVESTIGATIONS CENTER-DENVER
53, BOX 25227, DENVER FEDERAL CENTER
DENVER. COLORADO 80225
Location
Name
Address
Observs tion Point / C<. J [ AA- * I
•> /,,.r
Stack - Distance From Height
Wind - Speed Direction
Type of Installation
Tucl "ftp^.ns.
Dbservalion began Itefc Ended /{*//;>
Remarks:
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21
22
23
24
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iTCr Mr. Cyril Rowsell ,
hactory Superintendent
nUflUKUU OUyuf L/UIII|/Liiijr
Haina. Hawaii. Hawaii
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