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-725-
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REVISIONS
REVISIONS
DATB I •. M. HO.
-------
A 20 hectare (50 acre) site has been assumed with 13
hectares (31 acres) cleared, fenced, and developed with
roads, parking area, surfacing, landscaping and railroad
tracks. One track is provided for incoming coal and empty
outgoing cars, one track for empty incoming product coal
cars and full product coal cars, and the third for unload-
ing raw materials and loading product sulfur and waste
sulfates, all as shown in Figure 26.
4.8.4.2 General Facilities - The major general facilities
are the administration building and the maintenance shop
and stockrooms and stores building. The location of these
is shown in Figure 26.
The administration building has been assumed to have 2200
square meters (24,000 square feet) of floor area for office
space for the administrative personnel.
The maintenance shop and stores building has been assumed
to have 5500 square meters (60,000 square feet) of floor
area for maintenance and stores personnel, shop equipment
and tools, and spare parts and maintenance materials.
-126-
-------
5.0 PROCESS ECONOMICS
A capital and operating cost study for the base case is
given in this chapter with examples of the effect on the
return on total capital (ROTC) shown for variations in
capital cost and in product coal price.
5.1 PROCEDURE AND BASES
The bases listed in Section 3.4 are repeated below and
further detail is given.
Location and site
Pennsylvania-West Virginia area
Major river valley
Major branch of a coal hauling railroad
Site relatively level and suited to construction
Overall plant description
Turnkey installation
Self-sufficient; purchased power and water
Receive raw Lower Kittanning coal in rail cars
Specify coal storage, reclaim, and grinding
facilities
Pass all coal through chemical desulfurization
process
Remove 95% of the pyritic sulfur
Supply 9070 metric tons per day of 95% pyrite-free
coal ready for transport
Supply 95% pyrite-free coal for steam generation
Provide for removal of by-products and wastes
-127-
-------
Economics
1975 costs and wages (1973 dollars)
Capital costs built up on an installed equipment
basis
The operating costs include depreciation
Profit calculated as return on total investment
Minimum daily production of 9070 metric tons
(10,000 short tons) of product coal, dry basis,
without binder plus fuel coal
Run of mine coal purchased at $9.70 per metric ton
($8.80 per short ton), dry basis, delivered to
plant site.
Conventional engineering units were used in the
computer program
A land purchase cost of $100,000 is included in
Site Development
5.1.1 Capital Cost Estimate and Related Costs
5.1.1.1 Capital Cost Estimate - The capital costs are
given in Table 13 for complete engineering, purchasing,
and installation of battery limits equipment and off-site
utilities and facilities for the plant whose conceptual
design is developed in Chapter 4.0. Details for the
sectors are presented in Sections 10.2, Equipment; 10.3,
Instrumentation; and 10.6, Capital Costs. The estimates
are based on major equipment costs from vendors' quotations
or Company purchase records. These data are built up on
a unit operations basis for the components of each sector
using judgment, plus conventional and proprietary factors.
-128-
-------
Table 13. CAPITAL COST ESTIMATE SUMMARY
SECTOR
000 Coal Handling & Preparation
100 Mixing
200 Reaction
400 Filtration
500 Extraction
600 Filtration/Decantation
700 Water Washing
800 Filtration/Decantation
900 Drying, Decantation, Compacting
1000 Product Coal Handling
1100 Iron Sulfates Removal
1400 Distillation
1500 Vent Scrubbing
1900 Building & Miscellaneous
SUB-TOTAL PROCESSING
2000 Utilities
3000 Site Development & General
SUB-TOTAL
Allowances (10%)
TOTAL
M$ (1975)
8,800.0
1,044.5
23,960.1
6,906.1
1,010.1
7,338.2
1,126.3
8,630.6
6,984,9
3,770.0
13,891.3
4,931.7
642.0
10,864.3
99,900.1
28,251.8
4,503.9
132,655.8
13,344.2
146,000.0
PROBABILITY - 80%
Maximum (+22%) $180,000.OM
Minimum (-18%) $120,000.OM
-129-
-------
5.1.1.2 Capital Related Costs - A large proportion of the
operating costs is related to capital. The detail is given
below for depreciation, maintenance, insurance and taxes.
Depreciation - The data of Table 13 are regrouped in Table
14 according to depreciation category. Depreciation is
calculated on a straight line basis, i.e., for 20 year
depreciation l/20th or 5% of the original capital is
taken as an annual cost.
Maintenance - Annual expenditures for maintenance materials
and labor, spare parts, replacement, and revisions are
variable and need careful control. For purposes of a
cost estimate an overall maintenance cost of 4.0% of the
capital was chosen.
Insurance and Taxes - The annual premiums for fire and loss
insurance are directly related to capital values, as are
local property taxes and some state taxes. A total of
2.0% for these is realistic.
General and Administrative - A number of cost and capital
items that are important but relatively small in some cases
are grouped in Table 14 as "G&A and working capital." An
example of the items included in working capital is given
below. Inventories were valued at cost less any deprecia-
tion component included in the cost. The dollar amounts
will vary slightly from one alternative calculation to
another. These are representative. In addition to the
capital items listed below there will be other costs
associated with functions that might be performed at
another location and added to the manufacturing cost just
prior to sale. These would include corporate administration,
-ISO-
-------
Table 14. CAPITAL-RELATED COSTS GROUPED ACCORDING TO
DEPRECIATION PERIOD
Section or Category
Coal handling
Site development and
general
Utilities and services
Oxygen plant
Chemical processing
SUBTOTAL
G&A and working capital
TOTAL, metric tons
TOTAL, short tons
a$ Cost = $MM Cap. (0.04
Depre-
ciation
Years
20
25
20
20
10
(13.6
wtd avg)
N.A.
Mntce+0
Product, dry basis a
Capital
$MM
13.8
5.0
22.1
9.0
96.1
146.0
9.0
155.0
155.0
$ Capital
Ann. ton
4.6
1.7
7.4
3.0
32.0
48.7
3.0
51.7
47.0
.02 Taxes &Ins+1.0/yrs
$ Cost"
ton
0.51
0.17
0.81
0.33
5.12
6.94
0.09b
7.03
6.39
Depr)/yr
ton 3.0MM metric tons/yr
G&A cost/ton = $270M f 3000M = $0.09. There is no cost
component to working capital or G&A capital.
-131-
-------
selling, research and other general expenses. An allocation
of about 1/2% of sales income less raw material cost, or
$270,000, has been used for the cost component of general
and administrative functions and $90,000 has been allocated
for capital associated with these functions. These data
have been expressed as rounded totals in Table 14.
Working Capital:
Materials and supplies $ 250 M
Raw material inventory 1600
In-process inventory 140
Product inventory 500
Cash and accounts receivable . 6470
SUBTOTAL working capital $8960 M
General and Administrative 90
TOTAL G&A and working capital $9050 M
The grouping in Table 14 shows the relative contribution of
the various components of the overall installation to the
capital as total capital in column two and as capital cost
per annual ton in column three for unit comparison with
other processes. Column four shows the relative contri-
bution to operating cost per ton of product. The Allowances
from Table 13 were spread proportionally among the groups.
5.1.2 Manpower
The process was examined in detail and the duties of the
operators were listed in order that a good estimate could be
made of the number of people needed to operate four process
trains on an around-the-clock basis. Table 28, Section
10.7.1, presents a listing of example duties for the process
-132-
-------
operators. A schedule of three eight-hour shifts per day
was chosen with a crew manning a shift for seven days, being
off for two days and then coming back on the next shift.
With this 7 and 2 arrangement four crews provide continuous
full time coverage. There is one 3 day time-off period for
each crew every month. Others on the 7 and 2 schedule would
be the plant guards, the quality control technicians, the
operators of the steam plant, and other utilities and a few
individuals from the service station, or motor pool, and
from the Maintenance Department.
On the basis of the plot plan, utility requirements, esti-
mated plant capital and the process manning the additional
manpower to adequately staff the entire complex was estimated
based on general Company experience and on the current
personnel list of a similarly sized independent operating
unit of the Company at a particular location. A job listing
for this complex is given in Table 27, Section 10.7.1.
Table ISA below shows a summary of manpower by department
and section or function. The data are further subdivided
into broad classifications of skills or wages to facilitate
analysis and development of alternative manning plans. The
total personnel for this complex will be well over 500
people. For purposes of economic evaluation the maintenance
personnel have been subtracted. Their costs are included
in the charges for maintenance, described in Section 5.1.1.2.
An alternative to including maintenance men in the total
personnel list would be to have the maintenance done by
outside contractors.
-133-
-------
Table ISA. MANPOWER SUMMARY
Number of Employees in Broad Skill/Wage Ranges
Labor Classification
Department, Section or Function
Administration
Plant Manager's Office
Accounting, Purchasing, Office Svcs.
Traffic, Communications, Secretarial
Ind. Relations, Plant Safety & Security
SUBTOTAL
Production
1 Supervision and Administration
w Coal Receiving and Shipping
•^ Shift Operators, 10/train-shift
1 Spare Operators, Janitors
SUBTOTAL
Services
Engineering and Process Development
Quality Control
Utilities and Oxygen
Service Station, Warehouse, Laborers
SUBTOTAL
Maintenance
Shops and Field Services
TOTAL Personnel
TOTAL, Excluding Maintenance
A
Management
1
2
I
_2
6
10
— —
—
—
10
4
3
2
2
11
5
32
27
B
Technical
1
4
2
il
20
23
—
—
—
23
11
2
11
_1
25
5
73
68
C
Labor
—
—
—
4
18
160
12
194
_-.
16
18
!§.
59
157
410
253
D
Secretarial Totals
1
3
2
1
1
1
1
14
11
3
9
5
33
38
18
160
12
228
16
22
32
218
98
170
529
359
extended listing in Table 16 and additional detail in Tables 27 and 28.
-------
It could be expected that a plant such as this might start
out with one process train plus appropriate utilities and
services. Personnel would be scaled accordingly. During
the start-up, additional services manpower could be ar-
ranged for with the prime contractor, and a smaller Admin-
istration Department could handle the plant needs. After
all units were on stream and personnel became more experi-
enced the spectrum of jobs could also change. An example
might be a reduced requirement for supervisory personnel
in the Utilities Department.
Several functions are shown in Table 27, as more or less
secondary to the main personnel assignments. Local condi-
tions for a particular plant would determine if these or
other jobs could be given peripheral importance. Examples
are:
Public relations and ecology planning,
Office manager, receptionists, person responsible
for answering the general plant telephone,
Fire protection, first aid and industrial hygiene
sections. Local municipal and private participa-
tion is assumed.
In addition, a large degree of flexibility should be built
into the jobs in the Services Department to provide efficient
response to changing requirements.
In the economics program in Section 10.7.2 the total person-
nel, excluding maintenance, for each labor classification
from Table ISA was used as input. In Table 15B, the wage range
for each group is listed and the annual costs of labor by
skill and department are estimated and totaled. These totals
are rounded and were increased by $24M above the labor shown
-135-
-------
Table 15B. MANPOWER COST SUMMARY
Labor Classification A
Management
Annual 1973 Wage plus 20% escalation and
25-33% fringes, $M/man-year 27-33
Annual Cost of labor to the plant, $M
Administration 190
Production 295
Services . 325 *
Maintenance 150
TOTAL 960
TOTAL, excluding maintenance 810
B
Technical
18-28
C D
Labor Secretarial
14-20
9-15
400
500
600
100
1600
1500
3450
990
2800
7240
4440
80
15
40
30
165
135
Totals
9965
6885
CO
05
Average cost to plant, $M/man-year
Administration 31.7
Production 29.5
Services 29.5
Maintenance 30.0
All Departments 30.0
All Depts., excluding maintenance 30.0
20.0
21.7
24.0
20.0
21.9
22.1
—
17.8
16.8
17.8
17.7
17.5
11.4
15.0
13.3
10.0
11.5
12.3
20.3
18.7
19.9
18.1
18.8
19.2
Extended labor classification listing:
A. Management, Top Supervision, Experienced Technical
B. Other Technical, Foremen
C. Operating Labor, Craftsmen, Other Plant Labor, Clerks, Janitors, Crew Leaders
D. Secretarial, Office Assistants, Labor Trainees, Part Time Labor
Additional detail is given in Tables 27 and 2S.
-------
in the program to allow for a wide variety of miscellaneous
services. The $24M was taken from the water and refuse
disposal estimate so that the total cost for sale is not
affected. Examples of some of the miscellaneous services
that would be performed by the listed personnel or others are;
— Miscellaneous receiving, warehousing/ and
package delivery,
Laundry and safety supplies service,
— Recovery of salvageable materials,
— Temporary employment programs (summer painting,
contract yard cleanup and repair service,
training programs).
-137-
-------
5.1.3 Unit Ratio Based Costs
The single largest cost item is the purchased coal used as
feed to the chemical leach process. Detail pertinent to the
coal balance is given in Table 16. The other raw materials,
utilities and waste streams can be related to the coal
throughput, and for convenience these have been expressed
as a fraction of the product coal, less moisture.
Most of these inputs are identified and listed in Figure 1,
Block Flowsheet, Section 4.1.2 and in Figure 29, Utilities,
Section 4.8.3. These have been tabulated in Tables 17A & 17B,
wherein are shown the units, the number of units used hourly
in one process train, the value of a unit and the number of
days of inventory for each item. Table 17A utilizes metric
units and 17B conventional engineering units. The basis for
the unit ratios is the product coal from the last column in
Figure 1, Block Flowsheet, less moisture and binder. The
unit ratios were rounded by about 2% in the direction of
increased cost for some of the items other than coal
received and ash loss.
The following were taken directly from Figure 1: coal
received, oxygen, sulfuric acid, naphtha, binder, sulfur
credit, fuel coal, and iron sulfates disposal. The ash loss
is taken as the initial pyrite content less the pyrite and
iron and sulfur-containing residual salts left from the
reacted pyrite without correcting for the oxygen component
of the sulfates. The nitrogen produced was taken as a
weight ratio of about 3:1 to the oxygen. Approximately one
tenth market value was assigned to nitrogen for by-product
credit.
A term was entered to allow for miscellaneous chemical agents
as defined in the table. This was set to be somewhat of the
order of cost magnitude of the smallest raw material, the
solvent.
-138-
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Table 16. DETAIL OF ANNUAL COAL RATES
The amount of coal used or produced on an annual basis is
given below. The letters mpf are used to signify a moisture
and pyrite free basis without binder.
metric tons short tons
per hr, M per yr, per hr, M per yr,
one train four trains one train four trains
Feed
Coal, mpf
Pyrite
102.94
7.39
SUBTOTAL 110.33
3260
234.1
3494
113.50
8.15
121.65
3596
258.2
3854
Fuel
Coal, mpf 8.435 267
Iron & sulfur
Compounds 0.036 1.1
SUBTOTAL 8.47 268
9.30
295
1.3
296
Product
Coal, mpf 94.510 2994
Iron & sulfur
Compounds 0.535 16.9
SUBTOTAL 95.04 3011
104.20
0.59
104.79
3301
18.7
3320
Ash loss, by
difference
Iron & sulfur
Compounds
6.82
216.1
7.52
238.2
Product
Coal,dry basis 95.04
Binder 1.42
Moisture 3.80
TOTAL
100.26
3011
45
120
3176
104.79
1.57
4.19
110.55
3320
50
133
3503
-139-
-------
Table 17A. DATA FOR UNIT RATIO BASED COST ITEMS, METRIC
O
Cost Item
Product coal, dry basis
Coal received, dry basis
Ash loss, net iron and sulfur compounds only
Oxygen, 99.5%
Nitrogen credit
Sulfuric acid, 98%
Naphtha
Chemical agents
Binder, lignin sulfonate
Sulfur credit
Power
Fuel coal, dry basis
Water
Cooling tower blow-down disposal
Water treating plant waste
Iron sulfates disposal
Steam plant ash disposal
Units
Hourly Unit
Units Ratio
per Train Used
1973
Value, Days of
$/Unit Inventory
MT
MT
MT
MT
MT
MT
MT
kg
kg
MT
KW
MT
M3
M3
M3
MT
MT
95.0
110.3
6.82
4.52
-13.6
1.53
0.11
Variable
1,550
-1.48
5,682
8.5
284.0
52.0
4.5
14.3
1.31
1.0
1.17
0.072
0.048
-0.14
0.016
0.0012
0.0010
16.0
-0.015
60.0
0.09
3.0
0.55
0.05
0.15
0.014
27.56
9.70
N.A.
N.A.
nil
39.68
49.60
55.11
0.11
13.23
0.012
N.A.
0.0026
0.0013
0.0026
2.75
1.65
3
14
—
1
nil
5
5
30
30
7
—
3
—
- —
Wetting, defoaming, flocculating agents and alkali
DProcess, utility, and potable water -20%; Cooling tower make-up water -80%
"Negative numbers indicate by-products credited to the raw material cost section
-------
Table 17B. DATA FOR UNIT RATIO BASED COST ITEMS, CONVENTIONAL
Cost Item
Product coal, dry basis
Coal received, dry basis
Ash loss, net iron and sulfur compounds only
Oxygen, 99.5%
Nitrogen credit
Sulfuric acid, 98%
Naphtha
Chemical agents
Binder, lignin sulfonate
Sulfur credit
Power
Fuel coal, dry basis
Water
Cooling tower blow-down disposal
Water treating plant waste
Iron sulfates disposal
Steam plant ash disposal
Units
tons
tons
tons
tons
tons
tons
tons
cwt
cwt
tons
KW
tons
M gal.
M gal.
M gal.
tons
tons
Hourly
Units
per Train
104.8
121.65
7.52
4.98
-15.0
1.69
0.12
Variable
34.2
-1.63
5,682
9.34
75.0
13.6
1.2
15.75
1.44
Unit
Ratio
Used
1.0
1.17
0.072
0.048
-0.14
0.016
0.0012
0.0010
0.34
-0.015
54.0
0.09
0.75
0.29
0.012
0.15
0.014
1973
Value,
$/Unit
25.00
8.80
N.A.
N.A.
0.70
36.00
45.00
50.00
5.00
12.00
0.012
N.A.
0.01
0.005
0.01
2.50
1.50
Days of
Inventory
3
14
—
1
nil
5
5
30
30
7
—
3
—
—
—
—
__
Wetting, defoaming, flocculating agents and alkali
Process, utility, and potable water -20%: Cooling Tower make-up water -80%
'Negative numbers indicate by-products credited to the raw materials cost section
-------
The only purchased utilities are electricity and water.
These were estimated as follows:
Electric power;
32,470 KW total connected load x 70% load factor
= 22,729 KW for the complex or 5,682 KW for one
train, excluding power for fire protection.
Water:
~ o
Process 35 M /hr 155 gpm
Steam plant 182 800
Potable 8 37
Cooling tower make-up 908 4000
1133 M3/ hr 4992 gpm, or
300 M gal per hr,
The amount of water treatment plant effluent and the cool-
ing tower blow-down disposal or waste side-stream are given
in Figure 29, Sector 2204. Disposal costs were taken arbi-
trarily as equal to one half the average water cost. Ash
from the fuel coal is also listed in Figure 29, Sector 2100.
The costs of disposal of ash and sulfates refuse listed in
tables 17A and 17B are nominal values used for landfill.
The sulfates refuse cost allows for a thin membrane lining
for the landfill area(15'16'.
The unit costs in Table 17 were chosen from published and
private sources for 1973 and 1974. The inventories were
generally taken as less than the design specification
capacities.
-142-
-------
5.2 OPERATING COST ESTIMATE
5.2.1 Basic Conceptual Design Costs
A proprietary universal economic evaluation program (UEEP)
was used to develop an estimate of typical operating costs
at capacity for the plant utilizing the values presented in
the preceding sections. An example of the detailed computer
printout is given in Section 10.7.2 in conventional engineer-
ing units. Tables ISA and 18B summarize the data.
Table ISA summarizes the cost items and gives the annual cost
per ton of product coal on a dry basis, and as sold includ-
ing binder and about 4% moisture. The coal forwarded to the
plant boiler house as fuel and the ash loss are treated as
costs because they constitute a consumption of the purchased
coal. An upward rounding of 0.9% in the unit ratio of
coal-received to coal-product required an increase of 11%
in the ash and coal losses in the cost estimate to balance
the coal accounting. The remainder of the coal appears in
the product. When this remainder is subtracted from the
total cost, a treating cost is obtained.
Table 18B shows the sales income and several profitability
measures using the cost data of Table ISA. The data for
return on total capital before taxes (ROTCBT), or return on
investment (ROI), are further plotted in Figure 30 to show
the impact of variations in direct fixed capital, selling
price, or production rate. The base case shows a 12.2% ROI
at a sales price of $28.00 per ton, dry basis, for the capital
level presented in Section 5.1.1, i.e. $146 million DFC.
From Figure 30 it can be determined that to obtain a 20% ROI
it would be necessary to increase the price by 14% to $32
per ton or reduce the DFC by 25%. A 20% decrease in produc-
tion rate for the base case DFC and price would result in an
ROI of 6%.
-143-
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Table ISA. OPERATING COST ESTIMATE SUMMARY
Annual production:
Dry basis
As sold, 1.5% binder
3/000 x 103 MT (3,300 x 103 short T)
and 4% moisture 3,170 x 103 MT (3,500 x 103 short T)
Working Capital: $9,050 x 10'
Total Capital: $155,050 x 10'
Cost Item
Raw Materials and By-products
Coal 3
Ash & coal loss 264 x 10^ T
To fuel 297 x 10^ T
To product 3,300 x 10 T
Sulfuric acid
Naphtha
Chemical agents
Binder
Sulfur credit
Nitrogen credit
Subtotal
Capital Related Costs
Depreciation
Maintenance
Insurance and taxes
Subtotal
Other Costs
Power
Water and waste disposal
Labor and miscellaneous
General and administrative
Subtotal
Total and unit cost
Treating cost
Total unit cost, metric
Treating cost, metric
$M/yr
2,323'
2,614
29,040
1,901
178
165
5,610
- 594
- 323
40,914
12,043
5,840
2,920
20,803
2,138
2,478
6,885
270
11,771
73,488
44,448
73,488
44,448
Dry basis
$/short T
0.704
0.792
8.800
0.576
0.054
0.050
1.700
-0.180
-0.098
12.398
3.649
1.770
0.885
6.304
0.648
0.751
2.086
0.082
3.567
22.269
13.469
$/MT
24.496
14.816
As sold
$/short T
0.664
0.747
8.297
0.543
0.051
0.047
1.603
-0.170
-0.092
11.690
3.441
1.669
0.834
5.944
0.611
0.708
1.967
0.077
3.363
20.997
12.700
$/MT
23.182
14.022
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Table 18B. PROFIT SUMMARY AT CAPACITY
Annual sales of product coal: _ ^
Dry basis 3,000 x 10 MT (3,300 x 10 short T)
As sold, 1.5% binder » _
and 4% moisture
3,170 x 10 MT (3,500 x 10 short T)
Cost Item
Net product sales
Cost for sale
Profit, before tax
Profit, after tax
Working capital
Total capital (TC)
Profit ratios, BT
ROTC, %
Return on Sales, %
Turnover, Sales/TC
Sensitivity, BT
ROTC @ 50% capacity, %
ROTC @ 120% DFC, %
ROTC § 80% DFC, %
Treating cost/heating value,
@ 25.8MM Btu/short T
or 7.2 MM kcal/MT
$M/yr
92,400
73,488
18,911
9,834
Dry basis
$/ short T
28.00
22.27
5.73
2.98
As sold
$/short T
26.40
21.00
5.40
2.81
$M
9,050
155,050
$/TPY
2.74
46.98
$/TPY
2.59
44.30
12.2
20.5
0.6
- 3.8
8.1
18.5
52C/MM Btu
$1.87 /MM kcal
-145-
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Figure 30. Effect of Variations in Price, Direct Fixed
Capital (DFC), and Production Rate on the Return on
Investment (ROI) of Base Case.
PRODUCTION
RATE
•20 -10 0 +10
Variation from Base Case, %
-146-
+20
-------
5.3 COMPARISON WITH OTHER RELATED PROCESSES
5.3.1 Criteria of Performance
There are a large number of processes being investigated
that will bring about better utilization of coal or reduce
the sulfur oxide pollution from coal combustion. Several
of the yardsticks used to compare these processes are given
below with comments and data from the chemical desulfuriza-
tion process.
Engineering feasibility — This conceptual process design has
been shown to be completely feasible and can be used as a
basis for development of detailed engineering plans and
ultimate construction.
Sulfur removal efficiency — This process does not remove
organic sulfur, and it may leave a residual of up to 0.1%
sulfur as free sulfur and sulfates. This places it between
coal conversion and mechanical cleaning in sulfur removal
ability. For a wide range of coals this would be ample
beneficiation(2'15).
Commercial practicability — Coal beneficiation has the ad-
vantage that it can be performed in large volume production
facilities, the product can be sold for use in existing
large and small facilities without need for costly remodel-
ing, the cleaned coal can be stored outside for use, and
its cost for consumption varies directly according to the
output of the using facility.
Thermal efficiency — The following approximate calculation
shows close to 90% thermal efficiency for the overall proc-
ess from run of mine coal to cleaned and crushed product
coal.
-147-
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Basis: One ton of coal feed, dry basis
M Btu
Energy out:
Coal out, 1 ^* x <12'900 x 2,000) Btu/T= 22,227
Energy in:
Coal in, 1.0 T x (12,300 x 2,000) Btu/T= 24,600
Process power, including C^ plant,
54 KWH 0.86 T product ,Q 5QO Btu_
T product x T feed x 10'500 KWH"
TOTAL Energy in: 25,088
Thermal efficiency,
Energy out _ 22,227 ,nn _ fifi ,
Energy in ~ 25,088 X iUO ~ 88'6%
The actual thermal efficiency will depend on the manner of
calculating the heating value and the amount of water dried off.
Capital investment tp_ power production ratio, $/KW. For those
areas of the country where coal with a fairly high ratio of
pyrite to organic sulfur content is available and coal com-
bustion facilities exist, the chemical desulfurization process
offers the following capital investment to power ratio:
Basis: One year
Total capital investment for the complex
excluding start-up costs and interest on
construction capital $155,050M
Potential power production
3,300M tons coal x ?n'!|nnMJ??/£L x a ^n^g 926M ™
Total capital investment _ $155,050M _
Annual power production 926M KW
-148-
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5.3.2 Closely Related Process Studies
It is very important that similar bases be developed when
interpreting different studies, and that major differences
be recognized when close comparisons are being made. The
following studies are related to the process design pre-
sented in this report but the bases and methods are enough
different that a meaningful quantitative comparison cannot
be made using the reported data.
University of Michigan — A study made by a faculty team of
the College of Engineering at the University of Michigan for
the Electric Power Research Institute (EPRI) presents a
detailed comparison of a large number of clean coal utili-
zation processes
The University of Michigan study presents a flowsheet, capital
estimate and operating cost calculation for the reported TRW,
Inc., process , and it includes economics using a different
capital estimating method and costs estimated on the basis
of the Federal Power Commission Supply Task Force Utility
Financing Method. For a 10,000 short ton/day plant the
U of M EPRI study reports total capital of $146 million
including working capital, interest during construction and
start-up costs. The annual cost for 330 production days
including return on rate base, Federal income tax, depreci-
ation and net operating costs amounts to $78.7 million the
first year, decreasing to $61.7 million the eighteenth year.
Dow Texas Division — A cost analysis of the TRW process was
developed by personnel of the Texas Division of The Dow
(18)
Chemical Company for a 2400 short ton/day plant having
approximately the same flowsheet as the U of M EPRI report,
i.e. only that part of the process from the initial conveyor
to the mixer to the final product storage but excluding
compaction of product fines and detailed waste sulfate pro-
cessing. This report showed a capital investment of $29.5
-149-
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million for the smaller plant and a conversion cost of about
$10/short ton for 355 operating days annually. The M. W.
Kellogg Company cost models were used.
Kennecott Copper Corporation — A closely related Oxygen
Leaching Process is under development at the Ledgemont Labor-
(19)
atory of Kennecott Copper Corporation . The reported
process uses more oxygen and does not make elemental sulfur.
A generalized block diagram of the process is given and pre-
liminary scoping economics show somewhat lower capital and
operating cost:
Inc., process.
(17)
operating costs than the U of M EPRI study ' for the TRW,
Research Triangle Institute — A survey of stack gas scrub-
bing alternatives by the Research Triangle Institute
for a wide range of coal fired steam and power generation
plants showed that, for more than 75% of existing industrial,
commercial and institutional boilers, de-pyritized coal at 40
to 60C/MM Btu additional cost would be competitive with stack
gas cleaning.
The Institute also estimated^ ' that 23.2% of the coal
currently being mined could be satisfactorily processed
by mechanical and chemical means to meet present source
performance standards. The data are summarized in Table 19.
These data are based upon the total domestic coal base.
Application of a coal desulfurization process which removes
only inorganic sulfur, such as the TRW process, would be
restricted by'local and/or regional coal characteristics
and sulfur removal requirements.
-150-
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Table 19. SUMMARY OF COAL SUITABILITY TO MEET STANDARDS*
Percent of Re-
coverable Reserves
Percent of 1971
Coal Production
Coal Source Performance Stds Source Performance Stds
Characteristics New Present New Present
Low sulfur coal,
no processing re-
required 1.6
2.2
9.4
9.8
Cannot be cleaned
to meet standards 91.9
82.8
78.6
67.0
Can be cleaned by
mechanical and
chemical means 6. 5
15.0
12
23.2
*Present standard, 688 g S02/ GJ (1.6 Ib S02/MM Btu)
New standard, 516 g S02/GJ (1.2 Ib S02/MM Btu)
For the product coal of the design in this report the
present standard would permit 1.03% S and the new standard,
0.77% S, calculated as follows:
i
JL •
SO,, 0.5 Ib S/lb S0
^*™ *• ™'™"
x
100
MM Btu 1 T Coal/25.8MM"Btu 2000 lb/T
= 1.03% S
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6.0 PROCESS ALTERNATIVES AND THEIR ECONOMICS
The Base Case capital estimate was built up from a compre-
hensive base of experience within The Dow Chemical Company
and by the vendors whose quotations were used. At the
levels of development and design represented the precision
is reliably estimated such that the capital cost figure
has an 80% probability of lying between $120MM and $180MM.
This was on the basis of 1973 dollars and economic conditions
projected two years using historical norms. It does not
include the effects of the increased inflation of 1974 and
beyond.
The alternatives in this chapter were not "engineered," and
this must be taken into consideration. However, the various
cases do show the relative effects of the various hypothet-
ical alternatives.
The development of the economics for alternatives in this
chapter utilizes the regions indicated in the Block Flow-
sheet, Figure 1, to more readily identify and emphasize the
effects. Four regional groupings were used with the essen-
tially non-chemical processing regions combined in one group.
These are shown below with the included regions or sectors
and showing the proportion of treating cost represented as
a result of the calculations.
Coal Handling 27%
I 000 Coal Receiving and Preparation
IV 900 Drying, Compacting, Decantation
V 1000 Product Storage and Shipping
-153-
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Leaching and Regeneration 35%
II .100 Mixing
200 Leaching and Regeneration
400 Filtration No. 1
Extraction and Washing 20%
III 500 Extraction
600 Filtration No. 2 and Decantation
700 Water Washing
800 Filtration No. 3 and Decantation
1400 Distillation
1500 Vent Scrubbing
Iron Sulfates Removal 18%
VI 1100 Filtration No. 4, Concentration/
Filtration No. 5, Evaporation and
Sulfates Drying
After an explanation in Section 6.1 as to how the base case
data were distributed, the alternatives are explored accord-
ing to the above four regional groups.
-154-
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6.1 BASE CASE, CASE 1
6.1.1 Case 1
The base case economics data are displayed in Table 20 in
regional groups. Care was used in proportioning the data
among the groups, and the salient features of this propor-
tioning are given below.
Process Capital — The sector totals were all taken from
Table 13. The fraction of each group to the total is given.
Other Capital — Proportioning of the other capital items
was according to overall usage of the process region. These
were developed generally as follows:
Buildings and Miscellaneous — mostly buildings and
construction related to chemical processing sectors.
Site and General — Coal Handling region largest in
area. Administration buildings, railroad facilities,
road and yard development were heavily assessed against
Coal Handling. Maintenance shops more evenly propor-
tioned.
Oxygen Plant — all to Leaching.
Utilities — predominantly steam plant plus water
supply treatment and cooling. Proportioned according
to utility usage.
Allowances — proportioned according to Process
Capital plus the above Other Capital.
-155-
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Working Capital — Inventories were proportioned according
to appropriate region. Cash, and Accounts Receivable were
essentially all assigned to Coal Handling.
Capital Related Operating Costs — Depreciation was re-
estimated from Table 14 modified by the capital proportion-
ing discussed above. Maintenance, Insurance and Taxes
followed the percentage assignments used previously, viz 4%
and 2%. Labor was proportioned from Tables 15, 16 and 27.
It is designated as capital related because, for large
incremental changes in constructed plant capacity, the labor
will be proportional to the fixed capital. General and
Administrative costs followed the labor pattern with a
slight increase in the main chemical processing regions.
Unit Ratio Based Operating Costs — These costs were assigned
according to consumption or usage. Fuel coal was propor-
tioned according to steam usage. Ash loss represents the
weight loss due to FeS- removed, and was all assigned to
Leaching. Water supply, disposal of treatment plant ef-
fluent and cooling tower "blow-down," steam plant ash
disposal and waste sulfates disposal, and miscellaneous
services costs were spread according to usage.
Coal to Product — The entire cost of that proportion of
the feed coal that ultimately ends up in the product was
assigned to Coal Handling so that the chemical processing
costs could be clearly identified. When the feed coal to
product is subtracted from the total operating cost, the
process cost contribution of each region is shown.
-156-
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Table 20. BASE CASE, CAPITAL AND OPERATING COSTS BY REGION
I
M
ui
i
Region A!
Sectors A!
Fixed Capital
Process Capital
Other Capital,
Bldgs. & Misc.
Site & General
Oxygen Plant
Utilities
Allowances
TOTAL
Working Capital:
Operating Costs:
Capital Related,
Depreciation
Maintenance
Ins. & Taxes
Labor, Misc. Svc.
Gen'l & Adm.
SUBTOTAL
Unit Ratio Based,
Coal—to fuel
—to product
—ash loss
H-,SO., Chem. Agents
Naphtha
Binder
Sulfur, N,
Power
Water, Waste Disp.
SUBTOTAL
TOTAL
Less coal to product
Treating Cost,
—annual, $M
—$/T product
*f « fraction of all regions where no parentheses are used.
(f) = fraction annual depreciation where figures are in parentheses.
.1 Regions Coal Handling
.1 Sectors 000,900,1000
$M
89,037
10,864
4,504
8,130
20,121
13,344
146,000
9,050
$M/yr
12,043
5,840
2,920
6,885
270
27,958
2,614
29,040
2,323
2,066
178
5,610
-917
2,138
2,478
45,530
73,488
-29,040
44,448
13.47
$M
19,555
1,630
2,252
2,730
2,535
28,702
8,640
$M/yr
1,722
1,148
574
1,655
54
5,153
340
29,040
5,610
427
300
35,717
40,870
-29,040
11,830
3.59
f*
0.22
0.15
0.50
0.13
0.19
0.20
f
(0.06)
0.24
0.20
0.20
0.13
1.0
1.0
0.20
0.12
0.78
0.56
—
0.27
Leaching
100-400
$M
31,911
5,432
1,126
8,130
1,160
4,804
52,563
210
$M/yr
4,494
2,102
1,051
2,520
108
10,275
2,323
2,066
-330
962
390
5,411
15,686
—
15,686
4.75
f*
0.36
0.50
0.25
1.00
0.06
0.36
0.36
f
(0.085)
0.37
0.40
0.41
1.0
1.0
0.36
0.45
0.15
0.12
0.21
—
0.35
Extraction
500-800
1400, 1500
$M
23,680
2,716
676
7,250
3,470
37,792
140
$M/yr
3,402
1,512
756
1,870
81
7,621
1,046
178
-587
385
300
1,322
8,943
—
8,943
2.71
f*
0.27
0.25
0.15
0.36
0.26
0.26
f
(0.09)
0.27
0.30
0.26
0.40
1.0
0.64
0.18
0.12
0.03
0.12
—
0.20
Waste Sulfates
1100
$M
13,891
1,086
450
8,981
2,535
26,943
60
$M/yr
2,425
1,078
539
840
27
4,909
1,228
364
1,488
3,080
7,989
—
7,989
2.42
f*
0.15
0.10
0.10
0.45
0.19
0.18
f
(0.09)
0.12
0.10
0.13
0.47
0.17
0.61
0.07
0.11
—
0.18
-------
6.1.2
Summary — The totals from Table 20 are summarized:
Coal
Handl-
ing
Capital, $MM
Process Capital
Other Capital
Working Capital
Total Capital,
including other
capital
Operating Costs, $MM/yr
Capital Related. 5.1
Unit Ratio Based, 6.7
excluding coal to
product
Total Treating Cost 11.8
Treating Cost per
ton of product
Leach-
ing
10.3
5.4
15.7
Extrac-
tion
Waste
Sulf-
ates
Total
19.6
9.1
8.6
37.3
31.9
20.7
0.2
52.8
23.7
14.1
0.1
37.9
13.9
13.0
0.1
27.0
89.1
56.9
9.0
155.0
$3.59 $4.75
7.6 4.9 27.9
1.3 3.1 16.5
8.9 8.0 44.4
$2.71 $2.42 $13.47
The relative size of the above numbers provides an index
as to where appreciable capital or operating cost reductions
might be made.
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6.1.3 Effect of Production Rate
Estimates for the capital and operating costs for plants
of different sizes may be made using the subtotals from
Table 20. The development and use of such an estimating
procedure is shown in Table 21. The assignment of scaling
exponents is shown with the capital cost data for the
Base Case. The Coal Handling and Waste Sulfates regions
were combined as were the Leaching and Extraction regions.
The capacity of the Coal Handling and Waste Sulfates regions
could be increased by utilizing larger equipment and so these
were assigned a scaling exponent of 0.7 for scaling up and
0.65 for scaling down. The Leaching and Extraction regions
are so dominated by the reactors that it is likely that they
would be scaled in 100-130 T/hr increments with some sharing
of equipment, so a scaling exponent of 0.85 was assigned.
The Other Capital is made up of components that could be
expanded efficiently, so 0.65 and 0.7 exponents were used.
For the alternative cases in the lower section of the table
production rates of one half and two times the Base Case
were chosen. Thus, the Coal Handling and Waste Sulfates
regions were estimated as follows:
Production Rate Process Capital
M T/yr Calculation $MM
3300 33.4
1650 33.4 x (0.5)0'65 = 33.4 x 0.636 = 21.2
6600 33.4 x (2.0)°'7° = 33.4 x 1.63 = 54.4
The Capital Costs were estimated for each group and totalled
down and across. Then the production costs were estimated.
-159-
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The Capital Related Costs (CRC) from Table 20 are shown for
the Base Case and compared to total capital (TC). Ratios of
CRC/TC of 0.18 and 0.20 were obtained and used. The Unit
Ratioed Costs (URC) are not much affected by production rate,
so were used as constant $/T values for all cases. These
costs were estimated and totalled.
A plot of the effect of production rate for plants operating
at design capacity is shown in Figure 31. The open points
represent production multiples of 1,2,1/2 and 1/4 times the
Base Case. The short steeper curves represent the effect of
production rate changes on the operating cost for the base
plant and a half-size plant without changes in respective
design rate capital, i.e., the Capital Related Costs remain
constant on an annual basis while the Unit Ratioed Costs
remain constant on a unit basis. The net result of these
calculations is to show that the costs are not greatly
affected by volume of production in the vicinity of the
Base Case, e.g., for a 100% increase in rate, costs decreased
only 9%; for a 50% decrease in rate, costs increased 13%.
For smaller plants, debottlenecking can appreciably reduce
costs.
-16O-
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Table 21. EFFECT OF PRODUCTION RATE ON TREATING COST
FOR VARIOUS SIZE PLANTS
Base Case
Production Rate (P) , M T/yr
Process Capital(PC), $MM
scaling exponent (e)
Other Capital(OC), $MM
scaling exponent(e)
Total Capital (TC), $MM
Capital Related Costs(CRC)
CRC,$MM/yr
CRC/TC
CRC,$/T
Unit Ratioed Costs (URC),$/T
Total Operating Cost(TOC), $/T
Alternatives
P,
PC,
OC,
TC,
CRC,
URC,
TOC,
P,
PC,
OC,
TC,
CRC,
URC,
TOC,
M T/yr
$MM
$MM
$MM
$MM/yr
$/T
S/T
$/T
M T/yr
$MM
$MM
$IIM
$MM/yr
$/T
$/T
$/T
Coal Handling
plus Waste
Sulfates
3300
33.4
0.7a
22. 2a
0.7a
55.6
10.1
0.18
3.05
2.96
'T 6.01
1650
21.2
14.1
35.3
6.4
3.85
2.96
6.81
6600
54.4
36.2
90.6
16.3
2.47
2.96
5.43
Leaching
plus
Extraction
3300
55.6
0.85a
34. 8a
0.7a
90.4
17.9
0.20
5.42
2.04
7.46
1650
30.7
22.1
52.8
10.5
6.40
2.04
8.44
6600
100.6
56.7
157.3
31.5
4.77
2.04
6.81
Total
of All
Regions
3300
89.0
57.0
146.0
28.0
0.19
8.47
5.00
13.47
1650
51.9
36.2
88.1
16.9
10.25
5.00
15.25
6600
155.0
92.9
247.9
47.8
7.24
5.00
12.24
For the scaling factors the following were used:
0.7
(2.0)
= 1.63,
(2.0)0'86 = 1.81
(0.5)0'65 = 0.636, (0.5)°*86 = 0.553
-161-
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I
H
Oi
to
I
25
20
15
-p
o>
o
c
•H
•P
0)
1O
8
Operation at
Design Capacity
Short Term Operation
Above or Below
Design Capacity
.O.8
152 3
Production Rate, million tons/year
Figure 31. Production Rate vs Treating Cost
-------
6.2 COMPREHENSIVE ALTERNATIVE CASES, CASES 2, 3 and 4
Cases are developed below showing how interrelated process
changes and accounting procedures could greatly reduce
the apparent cost of installing chemical desulfurization.
Example calculations for the first three cases are given in
Section 10.7.4.
Assumptions:
The following letters are used in the summaries of capital
and cost reductions to designate the manner in which the base
case capital and operating cost items were adjusted:
(a) eliminate, facilities or personnel in similar jobs
already exist
(b) greatly reduce, share personnel or facilities after
modification
(c) accept an allocation of a larger facility
(d) adapt and use a different processing step or system
6.2.1 Coal Handling
Case 2 CH
Assume that the chemical desulfurization process is installed
on the site of an existing complex that has coal handling
facilities. The new facilities must bear their share of
the new capital and operating costs. An example of such an
installation is given in the Appendix, Section 10.7.3.
Arbitrary, but realistic, assumptions have been chosen, and
a case is built up for a plant with over twice the coal
receiving capacity of the base conceptual design with coal
washing and 'some drying facilities, plus storage and pulver-
izing facilities at an on-site powerhouse that will consume
up to 20,000 tons of coal per day.
No new receiving and storage areas or labor will be needed.
Some conveying required to new site. Pulverizers modified
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(3)
to grind wet fines. Grind only through 14 mesh . Share
dryers but only dry down to about 13.4% moisture rather than
4%, thus reducing drying capacity by as much as 50%, e.g.,
with 22.8% moisture from the final coal filtration,
22.8 - 13.4 9.4
22.8 - 4.0 18.8
= 0.50
Eliminate compaction and use binder fluid described in
Section 4.4.2.4 to minimize dust loss in transfers. Share
product storage and build storage equivalent to 50% of base
case. Utilities and services supplied at 70% of the cost
used in the Base Case.
Capital Reduction, $M
Process Capital,
Receiving(a) and Preparation(b) 3,000
Drying(b) 2,600
Compaction, eliminate compactor (a) , -, 200
keep tank and pumps(d) '
Product Coal Handling(b) 1,700
Other Capital,
Site, Building, General(c) 2,800
Utilities(b), less steam, lower
unit capital 1,700
Allowances, 4% of reductions 500
Total Fixed Capital Reduction 13,500
Ratio to Base Case Coal Handling($28,702M) 0.47
Working Capital Reduction, $M
Cash and 'Accounts Receivable(a,d) 6,000
Coal Inventories(d) 600
Other Materials and Supplies(b) 100
Total Working Capital Reduction 6,700
-164-
-------
Operating Costs Reduction, $M/yr
Capital Related,
Labor and G&A(afh,c) 1,200
Other Capital Related 1,620
Unit Ratio Based,
Binder(d) 4,170
Other Unit Ratioed; Services and 320
fuel coal equivalent(c) '
Total, Operating Costs Reduction 7,310
Effect on Coal Handling Region -$2.22/T
(7310 T 3300)
Alternative Unit Cost
Base Case Coal Handling 3.59
Less Reductions -2.22
Case 2 CH, Coal Handling $ 1.37/T
Case 3 CH
If it is assumed that chemical desulfurization is being
added to the coal preparation complex of a large coal user,
e.g., a utility or coking plant, for the purpose of decreas-
ing the total sulfur content of the coal while improving the
yield (usable coal/coal received), then it is conceivable
that the entire operating cost of the Coal Handling region
could be absorbed into other accounting functions.
This is not too extreme an assumption. In such a large
complex essentially all of the coal handling facilities,
working capital, personnel, and services would already exist
or be able to be assembled with little more than normal
project maintenance, service costs and disruptions.
Case 3 CH, Coal Handling nil $/T
See also Cases 3 CP and 3 U which approach this concept
differently.
-165-
-------
Case 4 CH—Merchant Coal
In the above context chemical desulfurization could be
added to a large merchant coal preparation plant with
relatively minor cost increases for Coal Handling. In
this case coal fines stabilization could be employed as
described in Section 4.4.2.4. Further elaboration would
be needed but it is possible to adequately protect against
fine coal losses in storage, transferring and transit for
less than $0.50 per short ton
Case 4 CH, Coal Handling $0.60/T
-166-
-------
6.2.2 Chemical Processing
Case 2 CP
Continue developing the Chemical Processing steps to match
the Coal Handling of Case 2 with the same assumptions where
applicable; 14 mesh topsize coal, utilities and services at
30% lower cost. Analysis of the job functions of Table 27
shows that more than half of the Administrative and Ser-
vices personnel would not be required for this case, as
either these services would not be needed for selling and
shipping coal or they could be obtained from personnel
already employed by the utility. The net reduction in
labor is estimated as 25%.
Other alternatives under development or contemplated are
included in the discussion by region below.
Assumptions:
Leaching — Very fast reacting coals and complete foam-
ing control in the mixer greatly reduce the required number
of reactors and cut process capital in half (See 6.3 Case 5)
Extraction — Elemental sulfur remaining after the leach
step is cut in half by control of acidity and oxidation
(19)
conditions in the leach process . A solvent with a very
high sulfur solubility is used above 120°C in counter
current flow ' . Capital of Sector 1400 is cut in half.
Waste Sulfates — Part of the waste is reprocessed to
recover salable products. See Table 22 . The remai
is disposed of in an abandoned section of a nearby deep
mine . One half of the capital is removed by elimin
or by charging its cost to the reprocessing.
-167-
-------
Capital Reduction, $M
Process Capital,
Leaching(d) 15,000
Extraction(d) 2,500
Waste Sulfates(d) 6,500
Subtotal, Process 24,000
Other Capital,
Site, Buildings, General 3,400
Utilities
Waste Sulfates(b,d) 4,490
Remainder (b) 2,520
Allowances
Process and Other Capital 2,750
Reductions
Subtotal, Other 13,160
Total Fixed Capital Reductions 37,160
Ratio to Base Case Chemical
Processing ($117,298M) 0.32
Operating Costs Reduction, $M/yr
Capital Related,
Labor and G&A(b) 1,360
Other Capital Related 5,550
Unit Ratio Based(b),
Utilities, Waste Disposal, Coal 1,550
Equivalent to Fuel & Ash Loss, Less
Reduced Sulfur Credit
TOTAL, Operating Cost Reduction 8,460
Effect on Chemical Processing Regions -$2.56/T
(8460 r 3300)
Alternative Unit Cost
Base Case Chemical Processing $9.88/T
Less Reductions 2. 5.6
Case 2 CP, Chemical Processing $7.32/T
-168-
-------
There would be an Increase in product tonnage corresponding
to the fuel coal equivalent of the lower steam requirements.
Assume that this amounted to 30% of the fuel coal, 90M tons
per year, or an increase of 2.7%. From Figure 30 this
would represent about a 1% improvement in ROI. The profit
before tax is $18,911 M/yr at 12.3% ROI (Table 19), so for
an increase of 1% to 13.3% ROI, for 3300 M T/yr the
improvement could be :
18,911 (' ~ i-0) f 330° =
This improvement could also be expressed as a decrease
in cost.
Achievable Treating Cost, full production,
Case 2 CP, Chemical Processing ($7. 32-0.47) $6.85/T
Case 2 CH, Coal Handling 1.37
$8.22/T, or
33C/MM Btu
-169-
-------
Table 22. VALUE AND DISPOSITION OF BY-PRODUCTS PROM COAL LEACHING*
By-product
Ferric
Sulfate
Ferrous
Sulfate
Iron Oxide:
Pigment Grade
Iron Ore Grade
4
Sulfur,
Elemental
By-product productior
for plants treating
100 and ,420 T of
coal/hr.
100
T/hr
3.7
4.3
6.0
1.2
420
T/hr
15.5
18.1
25.2
5.0
1,000
Tons/yr
122
142
198
39
U.S. Market
1,000
T/yr $/T
100 37
112 24
140 300
45,000 10
12
10,500 to
32
Most likely disposition for
by-product from numerous
plants
Haul to an abandoned mine or
quarry for disposal at $2.50/T
or build a processing unit
to upgrade to iron oxide if
the process economics and
markets warrant it.
Small amount could go into
pigment market.
Entire output could be shipped
to steel mills within 100 mile
radius if the quality was
acceptable.
Sulfur should be marketable if
there are customers within a
100 mile radius. Could also
be collected at a central river-
front location and shipped by
barge .
I
M
^4
o
aAdapted from data by Liang '
bl T =• 1 short ton - 907.2 kg
1 metric ton = 1,000 kg
-------
Case 3 CP
Using the assumptions for Case 3 CH Coal Handling, i.e. decreas-
ing the total sulfur content while improving the coal yield,
the original large plant might be facing a situation where
an appreciable fraction of the coal from the existing mechan-
ical separation facilities could not be used. In this event
some value for the unusable coal at that point plus the cost of
disposal could be credited to the chemical processing facility.
Example calculations for such a hypothetical situation are
given in Case 3CP, Section 10.7.4 with a suggestion that a
credit of $2.00/T be used in lieu of a larger calculated,
but indeterminate, credit.
Case 3 CP, Chemical Processing ($6.85-2.00) $4.85/T
Case 3 U
The ideas presented in Cases 2 and 3 are approached from the
standpoint of overall coal costs to the utility plant in
Case 3 U. The details are given in Section 10.7.4 and the
cases may be summarized as follows:
Cases Compared 2 CH, 3 CH, 3 U CH,
2 CP 3 CP 3 U CP
Product Coal, MM TPY 3300 3300 4510
Fixed Capital, $M
Coal Handling 15.2 nil 25.3
Chemical Processing 80.1 80.1 80.1
Total Unit Costs, $/T
Coal 8.80 8.80 8.80
CH Operating & Coal Loss 1.37 nil 2.91
CP Operating 6.85 4.85 5.36
TOTAL Operating Cost 17.02 13.65 17.07
Treating Cost 8.22 4.85 8.27
Recall that Case 2 allows some charges to be picked up by the
existing plant and provides for some improvements in technology,
Case 3 uses the same technology but charges all of the coal
-171-
-------
handling to the plant plus another $2.00/T for processing the
middlings. From the example calculation of Case 3 U it is
apparant that the economics and accounting practices for the
rest of the plant play an important part in the determination
of the treating cost for upgraded coal.
Case 4 CP — Merchant Coal
A complete coal preparation plant could take advantage of
the same type of cost reductions described in 2 CP and 3 CP;
however, for this example a less optimistic view was chosen —
no appreciable reduction in Utilities Capital and Cost and
only 25% reduction in sulfur credit and all other capital
and cost items. See 10.7.4 Case 4 CP.
Case 4 CP Chemical Processing ($7.73-$2.00) $5.73/T
6.2.3 Combinations and Extensions
The total treating costs for various combinations of these
comprehensive cases would be as follows, in $/T:
Coal Chemical
Handling Processing Total
Base Case, Case 1 1
Cost 3.59 9.88 13.47
Utility Cases - costs added to existing plant for chemically
desulfurized coal:
All facilities bear their share of the cost and share
utilities, fast reacting coal, new developments in extrac-
tion and sulfates reprocessing.
Case 2 CH 2 CP
Cost 1.37 6.85 8.22
-172-
-------
As above, but chemical desulfurization plant is not charged
for coal handling as plant wishes to decrease sulfur, improve
yield, so allows credit for less fuel coal consumed and
for refuse saved.
Case 3 CH 3 CP
Cost 0 6.85 - 2.00 4.85
Utility Case - Costs spread across all coal used:
Above case stated on the basis of the entire coal handling
and cleaning operation for the utility plant.
Case 3 U CH 3 U CP
Cost 2.91 5.36 8.27
Merchant Case - costs added to existing plant for chemically
desulfurized coal:
Add to existing facilities, fast reacting coal as in 2 CP
but less optimistic cost reduction. Use 3 CP type credit.
Case 4 CH 4 CP
Cost 0.60 7.73 - 2.00 6.33
The Merchant Coal example is an illustration of how the
foregoing discussion and calculation summaries can be
readily used to build a case to a certain requirement.
The above combination cases and others are plotted in
Figure 32 and further described following the plot.
If a chemica.1 desulfurization plant were installed at a
utility plant distant from the coal fields the freight cost
of the material later disappearing as ash loss could raise
the cost of this item 50% or more. Proximity to a source
of waste sulfuric acid could provide a compensating cost
reduction.
-173-
-------
35
30
25
o
o 20
ffi-
15
10
5
0
Legend:
<5s
XX
YTT
Equivalent
Coal Price
fen
EH
53 bo
s^>
+*
§0)
OQ
0 9
«H
a rt a)
8* -H
rt rt
A h
•H
n A 73 -P rt
« +* C!
•H A
ft • £
a) A bo
to o B rt
A -HA
u bo to o
B 01 O
0) i-l a)
OH rt 0 rt
A T3 O A
A ft O
No.
i" -. •
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*E* ^K * .
'•'•
' X'
^
\>
1
^
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Coal Hndlg,CH 1 2
Chem Proc ,CP 1 2
FeS2 Level, FL 1 1
*/ «
|
%
. \
i
3j
^r\
4
4
1
.
15% Return oh
Coal Handling
>\ <
:apital
>.
s^> Coal Handling
Cost
%
,
e1
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rt bO 0) 0)
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01 °£S 55*^ 25*°
"1 M*
^
1
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4
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i^ <«< <— ' >b W U
n
1
^
xs
1
5
^TN
\
I
OO
OC
^~ T
&J
XV
3 33
133
717
- 25% Return
on Chemical
Processing
/ Capital
^ Chemical
Processing
, Cost
73
A bo
O h
0 A
•C
rt O
d bo
B
* -H
•P tfl
•rt tQ
* O
o
-P 5 •
o Cjupj
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S
. bo
O B O
S5 -H rt
rt in
a> 73 TJ<
£ A 0
•i T-
— ,_
T-?
IT S
y'.
* /
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& 8.8O
i
1
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3U
3U
1
25oo
00*
20 8
o>
rt
B
O
- 10
. 5
-- 0
Figure 32.
Case Numbers Graphed
Effect of Basic Coal Price, Coal Handling,
Chemical Processing and Return on Total Capital (ROTC) on
Product Costs
-174-
-------
Figure 32 (contd.) Summary of Calculations
Example No. (see
Bars on Graph
Product Coal, M TPY
Coal Receiving
and Handling (CH)
CH Case No.
Capital, $MM
Fixed
Working
TOTAL
ROTC(15%), $/T
Costs, $/T
Coal
Operating
ROTC
TOTAL CH
Chemical Process-
ing (CP) and FeS?
Level(FL)
CP Case No.
FL Case No.
Capital, $MM
Fixed
Working
TOTAL
ROTC(25%), $/T
Costs, $/T
Coal, CH
Operating
ROTC
TOTAL
1
1
28.
8.
37.
1.
8.
3.
1.
14.
1
1
117.
0.
117.
8.
14.
9.
8.
32.
7
6
3
70
80
59
70
09
3
4
7
91
09
88
91
88
2
2
15.
1.
^_^_^_
17.
0.
8.
1.
0.
10.
2
1
80.
0.
80.
6.
10.
6.
6.
23.
2
£
1
78
80
37
78
95
1
4
5
10
95
85
10
90
3
3300 -
4
nil
nil
nil
nil
8.80
0.60
nil
9.40
4
1
89.4
0.4
89.8
6.80
9.40
5.73
6.80
21.93
4
3
nil
nil
nil
nil
8.80
nil
nil
8.80
1
7
86.3
0.4
86.7
6.57
8.80
6.82
6.57
22.19
5
3
nil
nil
nil
nil
8.80
nil
nil
8.80
3
1
80.1
0.4
80.5
6.10
8.80
4.85
6.10
19.75
6
3
nil
nil
nil
nil
8.80
nil
nil
8.80
3
7
80.1
0.4
80.5
6.10
8.80
4.82
6.10
19.72
7
4510
3 U
25
1
27
0
8
2
0
12
3
80
0
80
4
12
5
4
22
.3
.9
.2
.90
.80
.91
.90
.61
U
1
.1
.4
.5
.46
.61
.36
.46
.43
-175-
-------
Using flocculants, moving the water wash ahead of extrac-
tion and feeding drained extraction filter cake to the
dryers could result in some savings in the filtration
and decantation sectors and reduce steam costs for driving
off naphtha instead of water. These savings would be
balanced against flocculant cost and increased naphtha usage
(less naphtha fuel value).
Figure 32 shows a bar graph of several combination cases.
An equivalent coal price of $8.80/T was used for all cases
except that where there is a $2.00/T credit for a Case 3 CP
situation, this is portrayed as decreasing the coal cost to
the process. A table summarizing the calculations is given
as the second page of Figure 32. Following are examples of
what is shown in $/T:
Base Cases
Case 3 & 7*
Coal Price 8.80 8.80
Coal Handling,
Cost 3.59 nil
15% ROTC 1.37 nil
Chemical Processing,
Cost 9.88 4.82
25% ROTC 8.91 6.10
32.88 19.72
A number of such cases can easily be approximated from the
various unit costs given in this report. Such approxima-
tions can indicate the value of obtaining further data.
Cases involving various iron pyrite levels are given in the
next section.
*Case 2 CP capital and Case 7 cost chosen (less $2.00
credit of Case 3 CP), could be $1.00/T less.
-176-
-------
6.3 LEVEL OF IRON PYRITE, CASES 5 TO 10
The costs in this section reflect a more detailed analysis
of process variables and equipment sizes than those pre-
sented in the previous sections of this chapter.
Based on the computer printout represented in Table 8,
Section 4.2.4, the data were plotted in Figure 33 as
the log of the weight fraction of residual FeS2 versus the
log of the number of reactor sections. For the system of
continuous reactors in parallel used in the base case the
data for the mixer and the ten well mixed sections in the
reactors were taken from stepwise output internal to
Program B, described in 10.4.1.
About 14% of the FeS2 is reacted in one-half to one hour in
the mixing tank at 102°C (215.6°F). Then in the first section
of the parallel reactors the reaction is brought to about 43%
of completion in another hour. The reactors have final condi-
tions of 5.6 kg/cm2 (80 psia) and 150°C (302°F).
Described below are several cases for differing FeS2 content
in the feed or differing degrees of removal. The same coal
rates were assumed so there would be no change in the Coal
Handling region. Also, for 6.7% FeS2 or less, the liquid
to coal ratio was assumed to be unchanged, so there would be
little or no change in the filtration, extraction and
washing equipment. The 20% foam disengaging volume in the
reactors was maintained for volumes less than the Base Case.
The adjustments that could be expected in capital invest-
ment are developed in Table 23. The factors by which the
major chemical equipment in affected sectors differs and
-177-
-------
•Mixer —
O.8 1 O ~ A 4
Number of Reactor Sections
Figure 33. Weight.Fraction of Original FeS2 Remaining in the Coal After
Mixer and After Each Section of the Parallel Reactors
1O
the
-------
the factors to be used for scaling the cost of these sectors
are given. Subtotals for each region are shown and the
total fixed capital is given.
The operating cost changes are developed in Table 24. The
changes shown in Table 23 are expressed in Table 24 as per-
cent change in FeS2 removal and fraction change in Chemical
Processing capital. The use of these is detailed in the
description at the left in the table. The capital related
cost changes predominate. The cost changes related to coal
consumed for fuel and for purchased power are tied to equip-
ment changes and so were adjusted according to capital changes
All other costs were calculated on the basis of FeS2 removal
changes.
The rationale for each of the various cases of different
starting FeS- levels or different degrees of removal is
given below. The operating cost reduction estimates follow
the pattern of Table 21. The effect is shown in Figure 34.
Case 5 6.7% FeS2, 90% removal
0.67% FeS2 residual
From Figure 33, 50% of Base Case reactor volume is re-
quired. The reactors were reduced to one-half Base Case
capacity. Distillation and waste sulfates equipment were
little affected by the 5% reduction in FeS2 removal. In
practice, the filter would probably be Base Case size and
more filtrate would be recycled so that a more concentrated
solution could be fed to the evaporator.
Capital Reduction $12 MM
-as percent of Chemical Processing, 10%
Operating Cost Reduction $0.91/T
•179-
-------
Case 6 6.7% FeS2, 14.5% removal
5.7% FeS2 residual
From. Figure 33, no reactors used other than the mixer.
An allowance of $2MM was made for the solution regeneration
facilities for a hypothetical case where all of the reaction
occurred in the mixer. The distillation and waste sulfates
sectors were reduced to 20% of the Base Case as were
utilities.
This case and Cases 8 and 10 are used to define the lower
limits of sulfur removal in Figure 34, the plot of the
cases in Table 23.
Capital Reduction $56 MM
-as percent of Chemical Processing, 48%
Operating Cost Reduction $5.38/T
Case 7 3.35% FeS2, 90% removal
0.34% FeS2 residual
Assumed one half the initial FeS2 content and the same
percent removal as in Case 5. Should require 50% of Base
Case reactor volume, but 40% was assumed because it should
be possible to recycle iron sulfate back through the mixer
to build up its concentration. Distillation and waste sul-
fates capital and cost would be about half of Case 1 because
of smaller absolute levels of FeS2 dissolved.
Capital Reduction $31 MM
-as percent of Chemical Processing, 26%
Operating Cost Reduction $3.06/T
Case 8 3.35% FeS2/ 14.5% removal
2.86% FeS2 residual
-180-
-------
This case bears the same relationship to Case 7 that Case
6 does to Case 5, i.e., a definition of the lower limits of
sulfur removal for Figure 34.
Capital Reduction $62 MM
-as percent of Chemical Processing, 53%
Operating Cost Reduction $ 5.90/T
Case 9 13.4% FeS2, 95% removal
0.67% FeS2 residual (to <0.4%)
Twice as much iron sulfate solution required to maintain
the same stoichiometry, doubled equipment size for all
Chemical Processing except washing, filtration and vent
scrubbing as well as for utilities in Chemical Processing.
Capital Increase $61 MM
-as percent of Chemical Processing, 52%
Operating Cost Increase $ 5.98/T
Case 10 13.4% FeS2, 14.5% removal
—by proportion, 11.5% FeS2 residual
—used, 6.7% FeS2 residual
Case chosen to augment Case 9. No data have been presented
for this particular case but it is believed that such a high
level would provide much exposed FeS2 to be dissolved in
the mixer. This could be as much as 50% in three times
the residence time in the mixer. Data for some coals show
over 80% FeS~ reacting in the first hour of the reacting
time<3'.
Capital Reduction $42 MM
-as percent of Chemical Processing, 36%
Operating Cost Reduction $2.81 to 4.14/T
-181-
-------
Table 23. SIZE AND CAPITAL COST FACTORS FOR VARIOUS IRON PYRITE LEVELS
Case No.
Initial FeS2, %
Percent Removal
Final FeS2, %
Region & Sector
Coal Handling, $MM
Leaching
100 Mixing
200 Reaction
400 Filtration #1
, SUBTOTAL, $MM
M
oo Extraction
to
I 500 Extraction
600 Filtration #2
700,800,1500 Wash,Filt.#3
1400 Distillation
SUBTOTAL, $MM
Waste Sulfates
1100 Waste Sulfates
SUBTOTAL, $MM
Other Capital
1900,3000 Bldgs.,Site,Gen11
2000 Utilities
Allowances
SUBTOTAL, $MM
TOTAL, $MM
*e = exponent used in cost factor
** (0.5,0.58) means that the size of the equipment is 0.5 x Case 1 and the capital cost is estimated
to be 0.58 x Case 1.
*e
0.55
0.9
0.9
0.55
0.85
0.5
0.7
0.5
1
6.7
95
0.34
$t-IM
19.6
1.0
24.0
6.9
31.9
1.0
7.3
10.4
4.9
23.6
13.9
13.9
15.4
28.3
13.3
57.0
146.0
5
6.
90
0.
**Size
19.
0.5,0
21.
0.95,
23.
0.95,
13.
0.95,
56.
134.
7
67
and
6
.58
7
0.97
4
0.96
3
0.97
2
2
6
14
5
Cost
19
0.1
9
0.2
20
0.2
4
0.2
35
90
6
.7
.5
.7
Factors
.6
,0.13
.9
,0.45
.7
,0.32
.5
,0.45
.7
.3
7
3.35
90
0.34
Other than
19.6
0.4,0.44 0
21.3
0.5,0.71 0
22.1
0.5,0.62 0
8.6
0.4,0.63 0
43.7
115.1
8
3.35
14.5
2.86
1.0,
19.6
.1,0.
9.8
.1,0.
20.2
.1,0.
2.8
.1,0.
32.1
84.4
13
95
0
9
.4
.67
also Capital
19
2.0
13 2.0
2.0
59
2.0
2.0
32 2.0
31
20 2.0
22
32 2.0
73
206
.6
,1.5
,1.87
,1.87
.3
,1.5
,1.8
,1.4
.8
,1.6
.2
',1.4
.7
.5
10
13.4
14.5
11.5
Subtotals
19.6
3.0,
0.15,
12.
0.4,0
21.4
0.4,0
7.2
0.4,0
42.5
103.5
1.8
0.18
9
.63
.52
.63
-------
Table 24. OPERATING COST CHANGES FOR VARIOUS IRON PYRITE LEVELS
00
CO
I
Case No.
Initial FeS2/ %
Percent Removal
Final FeSjt %
Percent Cnange in FeS2 Removal,
_,.,_,Initial FeS^-Final FeS? >. .
Initial-final=6.36''x'
Capital, $MM
Working Cap. & Coal Handling
Chemical Processing(CP)
Change as Fraction of CP Capital
Operating Cost (TOG), $/T
Coal Handling, (CH),
From Table 20
Chemical Processing (CP)
Capital Related (CRC),
Section 6.1.2; (27.9-5.1) f 3.3
0.194 x CP Capital Change f 3.3
Unit Ratioed (URC)
(Excluding coal to product)
Fuel & Power x Fr. Cap. change
All Other x % FeS2 change/100
TOTAL TOC(CP) or change
Total Operating Cost, $/T
Chemical Processing
Coal Handling
TOTAL
1
6.
95
0.
5
7 6.7
90
34 0.67
0 — - 5.2
Base
Case
37.
117.
3.
6.
1.
1.
9.
9.
3.
13.
7
3 -12
- 0.10
59
91
- 0.70
21 - 0.12
76 - 0.09
88 - 0.91
88 8.97
59 3.59
47 12.56
6
14
5
-86
-56
- 0
- 3
- 0
- 1
- 5
4
3
8
6
.7
.5
.7
.0
anges
.48
- No
_-. r"Vi
.29
.58
.51
.38
- New
.50
.59
.09
7
3.
90
0.
35
34
-52.7
from Base
-31
- 0.26
change for
anges from
- 1.82
- 0.
- 0.
- 3.
cost
6.
3.
10.
31
93
8
3.
14.
2.
-92.
Case
-62
- 0.
these
Base
- 3.
- 0.
"* -L *
35
5
86
13
95
0
9
.4
.67
3 +100.2
Shown below
53
Ce
Cas
64
64
62
06 - 5.90
levels shown
82 3.98
59
41
3.
7.
59
57
+ 61
+ 0.
ises -
+ 3.
+ 0.
+ 1.
+ 5.
below
15.
3.
19.
52
59
63
76
98.
86
59
45
13.
14.
11.
-70.
-42
- 0,
- 2.
- 0.
- 1.
- 4.
5.
3.
9.
10°
4
5(50.)
5(6.7)
K+5.4)
36
47
44
23(+0.10)
14(-2.81)
74( 7.07)
59 3.59
3 (10.66)
iSee description of Case 10. Final FeS- is expected to be below 11.5%.
-------
I
M
00
I
18
16
14
c.
o
ifi-
12
•*->
(0
c
•H
M
rt
S 6
6
0>
O
I i I 11
Case numbers are encircled.
Initial
Pyritic —
Sulfur
7.2% S
10 (13.4% FeS2r
?3:
3.6% S
(6.7% FeS2)
35% FeS2)
O.2 0.4 O.6 O.8 1 2 4 6 8 1O
Residual Pyritic Sulfur, "Jf in Feed Coal
Figure 34. Chemical Processing Costs for Various Levels of Initial
and Residual Pyritic Sulfur Content
-------
6.4 MISCELLANEOUS COST EFFECTS
Aggressive process development will undoubtedly decrease
the overall capital and operating costs for this process,
excluding the effects of inflation. As fuel prices con-
tinue to increase it should be possible to show increasing
improvements in the relative economics of desulfurization.
Capital Reductions — From Table 20 it can be seen that
annual Capital Related Costs amount to about 15% of Fixed
Capital. A savings of $1 million in capital will be re-
flected in $150,000 per year, or 45C/T, in operating costs.
Thus the potential annual benefit of eliminating the 20%
foam disengagement volume in the reactors and decreasing
the liquid to solids ratio slightly in Sector 200 would be
(see Section 10.6.2, sheets 4 & 5):
$21.4MM(1-(0.8)°'7) = $21.4MM(1.0-0.856) = $3.08MM
At 45C/T per $1MM reduction this would be $1.39/T.
The cost savings for capital reductions can thus be compared
with corresponding required operating cost increases. As
an example, assume the filter sizes in Sector 800 can be
reduced by 40% by the use of flocculants and that redesigns
of Sector 700 would allow inclusion of a settler with no
increase in capital cost.
Projected capital related cost savings on reductions in
purchase cost of filters and accessories (Section 10.6.2,
sheets 11 & 12):
($0.515MM x 4) (1-(0.6)°'7) x $0.45/(T)($1.OMM)
= 2.6MM x 0.30 x 0.45/1.OMM = $0.35/T, saving
-185-
-------
First approximation for flocculant cost (Section 4.4.2.2(a)
and Table 17b):
0.05 Ib of flocculant/T x $0.50/lb = $0.025/T
The cost of using an effective flocculant appears to be
very favorable with respect to the potential cost savings
related to capital. Data to allow a more vigorous evaluation
of attractive potential trade-offs should be obtained from
vendors' tests and pilot plant operations.
Raw Material Prices — The impact of price variation, and
of raw material usage changes, can be estimated using the
data in Table 17B and the desired price or unit ratio.
data in Table 17B and the desired price or unit ratio.
Prices are shown below for the major raw materials, all in
short tons. More recent prices are given in the right hand
column and explained in parentheses.
Tons raw
material 1973 1974
Cost Item Ton coal $/T $/T
Coal received 1.17 8.80 9.50
(Typical f.o.b., mine)
Nitrogen credit -0.14 0.70 1.00
(10% of package plant price)
Sulfuric acid f2Q, 0.016 36.00 47.70
(100%,tanks,works,E Coast^ )
Naphtha (2Q) 0.0012 45.00 100.00
(Petroleum,tanks,NJ,0.67sp gr( ')
Sodium lignin sulfonate, 0.017 100.00 95.00
(bags, c.l., works1 ')
Sulfur credit f2Q) -0.015 12.00 47.00
(f.o.b. vessels, Gulf ports )
-186-
-------
Example effects: cents/ton
Coal
1.17 x (9.50 - 8.80) 82
Nitrogen credit
-0.14 x (1.00 - 0.70) -4.2
Sulfuric acid
0.016 x (47.70 - 36.00) 18.7
Naphtha, doubled consumption
2 x 0.0012 x (100 - 55) 13.2
Sulfur credit
-0.015 (47-12) -52.5
As can be seen, the impact of moderate price changes in the
non-coal raw materials is minor and the increases could be
balanced by an increase in by-product sulfur price.
Oxygen could have been included as a purchased raw material,
but at the low return shown in Table 18B it is unlikely that
a "make vs buy" study would show purchasing to be favorable.
This would need to be reevaluated if a higher return case
were anticipated.
Another case that should be examined but which is beyond
the scope of this report is the utilization of high sulfur
coal refuse for the steam generation plants. In the base
case 79.2C/T, dry basis, represents product coal used for
fuel at raw material coal price, or $2.6MM per year. This
will increase as coal prices increase; thus a cost of $2.6MM
per year could be expended in a merchant coal plant for the
operating cost of a suitable means to utilize high sulfur
coal, e.g. stack gas scrubbing or high-sulfur fuel com-
bustor techniques. This would permit the large coal prep-
aration plant to take advantage of economies for a scrubber
system on a large steam generation plant running at a steady
rate and to pass these economics along to the smaller
coal user for whom scrubbing might be impractical.
-187-
-------
Cost Escalation — In addition to considering process
alternatives it may be desired to project costs several
years into the future in order to compare the Base Case
with other options. Two cost indexes that are frequently
used by process engineers are plotted in Figure 35. These
are the ENR Building Cost Index , based on construction
wage rates and material costs in 20 cities in the U.S., and
(34)
the CE Plant Cost Indexv , based on a variety of industry
data. The year end index is published the first week in
January for the ENR Index and in April for the CE Index.
These are different from the annual averages . Figure
36 is a plot of the average value of bituminous coal, F.O.B,
mines . The data are given below. The projections
reflect the thinking of cognizant departments of The Dow
Chemical Company.
CONSTRUCTION COST ESCALATION
Year
End
1969
1970
1971
1972
1973
1974
1975 (Est.;
ENR Bldg.
cost'33'
802
866
1005
1090
1158
1240
ENR
Factor
1.00
1.08
1.25
1.36
1.44
1.55
1.69
CE Plant
Cost(34)
121.3
129.0
134.0
139.1
148.2
177.8
CE
Factor
1.00
1.06
1.10
1.15
1.22
1.47
1.69
BITUMINOUS COAL PRICE INCREASES
(36)
Year
End
1968
1969
1970
1971
1972
1973
1974 (Est.
1975 (Est.
Ave . , U . S . ,
$/T
4.67
4.99
6.26
7.07
7.66
8.42
U.S.
Factor
0.94
1.00
1.25
1.42
1.54
1.69
1.85
2.03
OH,PA,WV,
Ave. , $/T
4.88
5.23
6. .6 5
7.77
8.35
9.83
OH,PA,WV
Factor
0.93
1.00
1.27
1.49
1.60
1.88
2.04
2.20
-188-
-------
H 2.2
H
O
§ 2.0
rH
I-9
o 1.8
o 1.7
c
1.6
1.5
H 1.4
rt
I 1'3
01
o
o
1.2
1.1
1.0
i < '
9.5%/yr Increase,
1975-1978
T~7
D = ENR Building Cost
Index, 1969-1974.
/
O = CE Plant Cost
Index, 1969-1974
'69 '70'71 '72'73 ' 74 ' 75 '76'77 '78'79 '80
Year
Figure 35. Cost Escalation Factors for Construction
O
O
ii
OJ
O5
o
0)
(0
s
{-,
S
0)
u
2.2
2'°
1.3
1.8
T n
1.7
1.6
l-5
1.4
1.3
1-2
1.1
1.0
7.5 Vyr Increase,
1975-1978
/
/r
/
.Bituminous Coal, s
Average Value per tor^D
~T. 0. B. mines
1969-1973
O «= Average U.S.
D = OH,PA,WV Ave.
ill
'69 '70'71 '72'73 '74 '75 '76 '77 '78'79 '80
^f&fl V»
Figure 36. Price Increase Factors for Bituminous Coal
-189-
-------
7.0 CONTINUOUS SIMULATION MODELING PROGRAM
7.1 INTRODUCTION
The purpose of this investigation was to examine the
chemistry of coal desulfurization in relation to the pro-
posed process with emphasis placed on the leach, regenera-
tion, and iron sulfates removal steps. There were two ways
to approach this problem: (1) Each process area would be
examined separately and conclusions would be drawn. These
individual conclusions would then be brought together and
modified if necessary to account for their interactive
effect on the entire process. (2) Each area of interest
would be investigated separately but in such a way that
the impact of any changes on the rest of the process would
be reflected. This latter approach was selected as the
better way to study the process.
The link used to tie the process areas together was a mass
balance simulation model. Further, in an effort to make
the simulation more realistic, it was developd as a tran-
sient state mass balance instead of a steady state mass
balance. The transient state model adds additional insight
in several ways: (1) It shows how accurate steady state
assumptions are and it shows the time required to reach
steady state from start-up. (2) The effect of condition
changes during operation can be examined and the time re-
quired to reach new steady state conditions determined.
(3) The transient state simulation will better illustrate
the effects of critical chemical parameters and stream
components on the entire process. (4) The model can be
modified to include and optimize capital and operating costs
under any constraints that are imposed on the process.
-191-
-------
The material balance model was developed using the Con-
tinuous Simulation Modeling Program (CSMP). CSMP is a high
level IBM programming language that minimizes the amount
of programming required by the user. For example, efficient
subroutines are available for the performance of numerical
integrations, determination of roots in implicit equations,
generation of impulses, random numbers, debugging, etc.
This program was written to output all stream components,
molar flow rates and the molar amounts. These molar quan-
tities were then used as a base for calculations related to
the coal desulfurization chemistry. A copy of the program
is listed in the Appendix, Section 10.8.1. Because of
storage limitations this program listing is not complete
for handling all variations that were simulated.
-192-
-------
7.2 BASIC PROCESS EXAMINATION
7.2.1 Simulation Model Assumptions
The building and use of a model to simulate the chemistry of
a process provides one immediate advantage in that it shows
areas where additional data are needed. This study was no
exception. In the building of the model, assumptions had
to be made as to where data were lacking. The use of the
model indicates how sensitive the process is to variations
in these assumptions. Generally, the areas where assump-
tions had to be made in the absence of data can be classified
into one of two types: (1) Those assumptions that had to
be made about the process in order to develop the material
balance. (2) Assumptions made about the chemistry so that
inferences could be extended to the process. Those that fit
the first category will be discussed in this section while
those relating to process chemistry will be discussed in
sections wherein they pertain.
Solution density and specific heats have to be assumed in
order to calculate volumetric flow rates, volumes, and
the rate of iron sulfates removal from the evaporator-
filter system. Also a better knowledge of the solution
density variation as a function of component concentration
should be obtained because it may have a significant effect
on the residence times and, therefore, on the product coal
quality.
7.2.2 CSMP Output
One of the features of CSMP is its ability to print any
calculated quantities in table and/or plot form with a
-193-
-------
minimal amount of user programming (no format required).
Figures 31 a, 37b, and 38 show some typical output for the
iron sulfate stream flow rates and amounts as a function
of process operating time. The quantities shown in these
figures are simulated results based upon the proposed coal
desulfurization plant design. The initial conditions and
flow rates are based upon the steady state quantities used
in the process design.
The cyclic shapes of the curves in Figures 37a, 37b, and
38 are caused by residence times in the different vessels.
The small irregularities are caused by vessels having
small residence times, while the large cyclic variations
are caused by the ten hour residence time for the reactors.
Note that these cyclic effects have begun to dampen as
the time of process operation increases, indicating that
the process is approaching steady state. Outputs for all
streams were examined to see if there were any excessive
buildups or depletions. No obvious problems of this nature
were observed.
7.2.3 Location of Iron Sulfates Removal Operation
The location selected for the removal of excess iron sul-
fates is quite important, as it will have a significant
effect on the efficiency of the oxygen usage and the
efficiency of the energy used in evaporation. Oxygen is
added to regenerate ferric ions so that the leach process
can proceed at a favorable rate. When ferric ions are
removed from the process, the oxygen use efficiency de-
creases because the removal of one mole of ferric ions from
the process means 0.25 mole of oxygen is wasted. Conse-
quently the optimal iron sulfate removal location would
-194-
-------
500
Ul
40O
CO
0>
0>
•p
ri
tf
O
30O
200
ti
3
O
I
SH
CS
rH
O
s
-::
Recycle to
Flow Rate
fflttittr
r Figure 37 a f_
EffiiTE
Mixer
Amount
Figure 37b
Flow Rate
---r-r-r--r- ,
: :Ll±h:.in:
Reactor
!-'r- Influent
150
1OO
3O 5O 70
Process Operation Time, Hours
Figure 37. Representative Output from CSMP
-------
Mixer -
Amount ~*-'-'.
Recycle
to Mixer
Flow Rate
Evaporator
30 5O 7O
Process Operation Time, Hours
Figure 38. Other Representative Output from CSMP
-------
be one where conditions were most favorable for ferrous
sulfate precipitation (to minimize evaporation costs) and
least favorable for ferric hydroxide and ferric sulfate
precipitation. There are two general areas in the process
where the excess iron sulfates can be removed: (1) somewhere
in the recycle stream from the reactors to the mixer (2) in
the mixer effluent. On the proposed flowsheet the chemical
compositions at these locations are best described as that
of stream #9 and #19 respectively. The process design calls
for removal of coal by filtration of stream #16 followed by
evaporation of the filtrate, stream #19, with subsequent cooling
and removal of iron sulfate crystals by filtration. There is
good reason for choosing this location. Figure 39 shows the
product Kw [Fe ][H ] as a function of process operation
time (See Appendix Section 10.8.2 for a discussion of iron
precipitates and the conditions of their formation as well as
the definition of Kw). This product gives a relative indica-
tion of the degree of stream, or vessel, liquid saturation as
a function of process operation time. Stream #9 has a much
higher solubility product than stream #19. Figure 40 is a
(21)
Posnjak and Merwin ternary diagram that has the 90 hour
region of process operation marked as an overlay. Note that
the conditions in stream #9 place it in a region where pre-
cipitate is formed, whereas stream #19 is in a region where no
ferric sulfate forms. It is clear from these figures that con-
3+
siderably more Fe would be removed if the evaporation-
filtration operation were located after the reactors. By
waiting until this ferric ion rich solution is recycled
through the mixer, several things are accomplished. Ferric
ions are depleted in the mixer during preliminary leaching.
The mixer effluent is now more rich in ferrous ion and
somewhat depleted in ferric ion, which means a minimal loss
of ferric ions with a maximum amount of ferrous ion re-
moved per unit of energy (Figure 41) for evaporation.
-197-
-------
CO
i
co
0)
CO
•p
O
73
O
O
to
0)
73
•H
X!
O
JH
73
o
•H
0)
10
•39
10~4° ^_J
10
-41
10
-42
Stream 19, _
Evaporator Feed
• !—>—«=_- -
24 36 48 60
Process Operation Time, Hours
Figure 39. Ferric Hydroxide Solubility Product
Variation with Process Operation Time
-198-
-------
Figure 40. Regions of Process
Operation Superimposed on Posnjak
and Merwin Ternary Diagram for
Fe203-S03-H20 System
Fe203
CO
co
Stream
Mixer
Stream
9, Reactor Effluent
21, Eva'porator Feed
(Filtrate from
Mixer Effluent)
3Fe2O3'4S03'9H20
HoO
-------
w
it Stream 19:ir;
30 50
Process Operation Time, Hours
Figure 41. Ferrous Sulfate Solubility Product
Variation with Process Operation Time
70
-2OO-
-------
This situation may even be further improved by placing a
surge tank between the mixer and the point where stream #16
is taken from stream #5. The capital cost of such a tank
would have to be balanced against the savings of increased
oxygen usage efficiency.
7.2.4 Leach Solution Loss in Clean Coal
Figures 39 and 40 that were alluded to in the previous
discussion bring a potential operating problem to surface.
The ternary diagram shows a ferric sulfate precipitate
to be forming in stream #9. Also, the chance of ferric
hydroxide forming in stream #9 is very high. The 25°C
— 37 — 38 (22)
K of ferric hydroxide ranges from 10 to 10 .
Bringing into account the high temperature and the high
-39
ionic strength of the process, the K is probably 10
-40 p
to 10 (see Section 10.8.2). This situation may be un-
favorable for several reasons: (1) The ferric precipitate
may be removed with the coal at the F-400, F-600, and F-800
filters. A water wash of the filter cake may solubilize
the iron sulfate precipitate, but it will probably mean
that it is converted to ferric hydroxide. Possibly this
hydroxide conversion may be prevented if the initial wash
is a cold water wash, but data are not available to predict
this accurately. (Section 10.8.2 discusses areas where solu-
bility data are still required.) (2) The pyrite leaching
rate may be affected. Ferric ions present as ferric hydrox-
ide will not leach pyrite as rapidly as ferric ions in
solution. Possible remedies to this problem are: (a) Run
the entire system in a more acidic environment from start-
up, (b) Provide pH controlled make-up acid to the reactor
effluent.
-201-
-------
7.2.5 Stoichiometric Variations
The leaching of pyrite by acidic iron sulfate solutions is
not a new area of study. This chemistry has been studied
extensively, as it is the principal cause of acid mine drain-
age in coal and copper mining areas. However, in mine
drainage studies the goal was to determine the rate mech-
anism in order to inhibit the leaching rather than to
(23)
enhance it. Garrels and Thompson v studied both the leach
and regeneration reaction chemistry and rates. Their find-
ings are not in complete agreement with those of TRW. The
TRW stoichiometry for the leach and regeneration steps are:
LEACH:
9.2Fe3++FeSn+4.8H00 ^ X 10. 2Fe2++9. 6H++0. 8S+1. 2S0.2~ (3)
~"
REGENERATION:
Fe2++H++l/402 ^ ^ Fe3++l/2H20 (4)
The reported findings of Garrels and Thompson are in
agreement on the regeneration step stoichiometry but not
in agreement with regard to the leaching step. Their
proposed stoichiometry is:
14Fe3++FeS2+8H20 ^ > 15Fe2++2S042~+16H+ (10)
The questions of interest are: If the Garrels and Thompson
stoichiometry is correct, what process alterations could be
considered, and what type of products would be obtained if
the proposed process remains as designed?
Obviously, the absence of any intermediate sulfur product
would mean reduced capital and operating costs in the design.
If it can be demonstrated that a sulfur reaction product does
-202-
-------
not form or that operating conditions exist such that sulfur
will not form, then the sulfur solvent extraction opera-
tion can be eliminated from the process. Some initial
calculations were done to see if the Garrels and Thompson
findings are feasible. Section 10.8.3 shows how E_-pH
relations can be derived to study the findings of Garrels
and Thompson using thermodynamics. Figure 42 is an E.-pH
plot that shows regions of stability for sulfur species.
In order to use this plot in conjunction with the CSMP
simulation of the process, the factors that determine the
stream or vessel E, must be determined. The H~O-02
system could be used to calculate the E, at the bottom
of the reactors because the high oxygen, partial pressure
would make that system the one that controls the En
Eh = 1.23 + 0.0148 log PQ - 0.059pH (11)
However, as the oxygen supply is depleted during the re-
generation of ferric ions, the ferric-ferrous system will
become the E, controlling system(30)
n •
[Fe3+]
E. = 0.771 + 0.059 log r_ 2+, (12)
n LFe J
Consequently, equation (12) was used to calculate the Eh
since it provides the lower E, limit.
The ferrous and ferric quantities are known from the molar
flow rates and molar amounts in the CSMP calculations, so
the solution E, for different vessels and streams in the
n.
desulfurization process can be calculated and printed as
part of the CSMP output. The overlay segments outlined on
Figure 42 show the operating regions for several parts of
the process. The E, of the mixer is the lowest of the
-203-
-------
1.0
Reactor
Effluent
Operating
— Region
I ! I I I I !
Mixer Operat-
ing Region
Elemental
3456
Hydrogen Ion Concentration, pH
Figure 42. Regions of Process Operation Superimposed
on an Eh-pH Diagram for the Sulfur-Water System
-204-
-------
process, since this is the part of the process where the
ferric ion quantity in solution has been depleted the most.
Even under these conditions the sulfate or bisulfate forms
of sulfur are most stable. This information does not com-
pletely rule out the possibility of sulfur formation. There
are other ways that two studies could arrive at different
results:
(1) While thermodynamic relationships show sulfur to
be unstable, the kinetics may be slow enough such
that sulfur is formed as an intermediate. There
definitely is a need for a more detailed rate
study to determine the steps in the mechanism.
(2) The studies of TRW showed sulfur as a product in
the batch tests. Garrels and Thompson also
observed sulfur when the ferric ion concentration
was depleted. In all cases pf continuous oper-
ating experiments TRW reported a calculated sulfur
amount based on the results of the batch tests.
Perhaps the reaction does not go far enough to
completion when the batch leach is near equilibrium
and the ferric ion concentration is essentially
depleted.
(3) It was suggested that coal may be acting as a
reducing agent at these elevated temperatures
with the coal being oxidized and sulfate reduced.
°
2C + S04 ^ S + 2C02 + 2e (13)
The change in free energy for this reaction is
-7.28 kilocalories. If this reaction occurs, it
may be possible to remove the sulfur by adding a
unit operation much like the cone precipitators
used in copper cementation. Here the coal could
-205-
-------
conceivably be sprayed with a solution having a
high E, . The sulfur would either be spalled
from the coal surface and oxidized or it would
be oxidized and then leached from the coal.
The other difference in stoichiometrics is in the amount of
ferric iron required to leach the pyrite. A CSMP simulation
was run using the proposed process and operating conditions
with Carrels' and Thompson's stoichiometry. It was antici-
pated that the results would not be favorable, as 3.5 moles
of 02 are required to leach one mole of pyrite while 2.3
moles are required by TRW stoichiometry. Figure 43 shows
the molar flow of pyrite from the reactors for both cases.
As expected, the proposed process only removed 65-75% of
the pyrite. To compensate for this loss due to stoichiom-
etry, the amount of oxygen would have to be increased by
50%. As long as the regeneration rate.is sufficiently
faster than the leach rate the reactor size would not have
to be increased. A CSMP simulation with 48 Ib moles of
oxygen per hour flowing to the reactors confirmed this
assumption.
-206-
-------
tPyrite Laden ±
-fCoal in
11 Reactors at r.r
tffiSE
3+PtJtT
-+-
~T~l"i~T~i~'~t"Ti'
.--.--i »_*_.! ., . ..,.,
-f-H—'-H--B-
T Carrels' and
4: Thompson's
4 Stoichiometry
i-r i-j~: -r-rl-T
t-MH •hn~<-i
Reactors
i Stoichiometry
30 50
Process Operation Time, Hours
Figure 43. Effect of Different Leach Stoichiometrics
on the Flow of Pyrite in Coal
-207-
-------
7.3 PROCESS AND OPERATING CONDITION VARIATIONS
7.3.1 Ferric Ion Regeneration in the Mixer
One alternative suggested as a potential process improve-
ment is regeneration of ferric ions in the mixer. Oxygen
would be added to the mixer with no change in pressure over
the mixer. A CSMP trial was made to see if an increase of
the ferric to total iron ratio would increase the amount of
pyrite leached in the mixers and subsequently reduce the
amount fed to the reactors so that fewer or smaller reactors
could be specified.
The simulation results indicate that this alternative is
not favorable for this level of pyrite in the coal. The
additional oxygen does increase the ferric to total iron
ratio, but it does not increase it sufficiently so that
the amount of pyrite remaining in the coal product is
reduced. Figures 44a and 44b show the molar flow of pyrite
from the mixer and reactors as the time from start-up
increases. These simulated results indicate that ferric
ion regeneration brings the mixer rapidly to steady state,
but the overall improvement in the clean coal product with
respect to pyritic sulfur is marginal. One reason that
this modification appears to be disappointing is because
the additional oxidation is depleting the system of acid.
Figures 45a and 45b show the molar flow rate of acid in
the stream that recycles to the mixer and the molar amount
of acid in the mixer, respectively. What is actually hap-
pening here is that the acidity in the system is now in the
form of ferric ion instead of free acid. Without any
further process modification, undesirable iron precipitates
will be formed, remain with the solids during filtration and
-208-
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140
i
to
§
QJ
•M
•H
' HT^ ^cgciicxa UJ.UI1 iiz 1V1XACI- I . i _i 1.1 I LI.J L Ll ! .| : I [.I [ -| :
^^g!_K^^ ntfl tt[
itic'Coal'ln :l-iL.V ' 3+ '' I '"' ' ::'l":l>_'j ' ^' ^jJ^'-trf-Tt''!-^ Fe + Regeneration i
[No Pyritic Coal in : F-!>F 3+ Regeneration ' in "liUxer ij-h^ - —- --??Sene-*"a-tio-n in Mixer'
r^Reactors at Start-up Fe Kegeneration in mixer , | j, Acid Make_up to Reactor
10
70
_up
Effluent 90
3O 50
Process Operation Time, Hours
Figure 44. Effect of Ferric Ion Regeneration in the Mixer on the
Rate of Pyrite Flow
-------
I
10
jure 45a.
; Acid • to; 'the ;-Mtb4eT
•f No Fe Regeneration in Mixer..]
Fe Regeneration in
-Figure 45b.
j-^rj-rH-Hi'H •
••^..--I.-L jn.frl'^- •*> i -i '!-.
j-r-;::::-.NO
i • j I Ll i • [• j_; Regeneration
"•"^"-II^L Regeneration
• •; ; ; • • in Mixer
3O 5O 70
Process Operation Time, Hours
Figure 45. Effect of Ferric Ion Regeneration in the Mixer on Acid
Requirements and Amount
-------
Figure 46. Reactor Effluent Operating
Region when Ferric Material Is Regenerated
in the Mixer and Superimposed on Posnjak
Merwin Ternary Diagram
Fe2O3
i
to
M
M
I
4S03-9H20
Fe
Stream 9
HoO
j03-2SO3-H20
xFe2O3-3SO3-6H20
Fe203-4S03-9H20
Fe203-4S03-3H20
-------
CO
I
Q)
•p
o
•o
o
•p
•H
rH
•H
o
CO
Q)
•H
X
o
SH
•o
a
o
•H
10
-36
10
Solubility Limit at
T-~ 25"C
No Fe~' Regeneration
in Mixer
18 30 42 54
Process Operation Time, Hours
66
Figure 47. Ferric Hydroxide Solubility Product Variation with
Process Operation Time when Ferric Material Is Regenerated in
the Mixer
-212-
-------
CO
I
B
0)
fa
CO
-p
o
o
w
73
•H
K
O
32
, ^
1O
-33
10
10
10
io
-37
3O 42
Process Operation Time,
Figure 47 (Continued) . Ferric Hydroxide Solubility Product
Variation with Process Operation Time when Ferric Material Is
Regenerated in the Mixer
-213-
-------
be lost in the leached coal. This fact is illustrated by
Figures 46 and 47, which show that a mixed ferric sulfate
and ferric hydroxide product will form in the reactor
effluent. In this process the relationship between ferric
hydroxide formation and the oxidation reaction is quite
sensitive because acid that prevents precipitation is being
removed as fast as ferric ions that promote precipitation
are being formed. The sensitivity of this relation is
reduced by the effect of leaching, but the point is clear
that excess use of oxygen means lower efficiency of oxygen/
mole FeS2 leached because of oxygen excess, system depletion
of acid, and lower efficiency of oxygen/mole leached due to
ferric ion losses. Also the excess ferric material that
will be present in the reactor effluent will mean possible
contamination of the product coal with ferric ion solids.
This last problem could be reduced by installing the pre-
viously mentioned acid make-up line to'the reactor effluent.
The simulated effect of this addition is shown in Figures 44a
and 44b. Without the improvements, 94-95% of the pyrite is
removed. With the suggested improvements where make-up acid
and 9-10 moles/hour of additional oxygen are required, the
amount of pyrite removed averages 95.6%.
This disappointingly small improvement in the product is
misleading because the percent pyrite removed is expressed
as a mole percentage (100 x moles of pyrite in process
effluent/moles of pyrite in process influent). If this
reduction in the amount of pyrite were expressed as a
percent reduction in residence time in a reactor, it would
be more meaningful, as residence time can be tied to equip-
ment size and capital cost. By taking a closer look at the
leach rate equation, an approximate expression can be
developed to make the point clear.
-214-
-------
dWr/dt = -KLWrY (9)
where KT = reaction rate constant
LI
W = pyrite/coal weight ratio
Y = ferric to total iron ratio
If Y is held constant (not true, but for the purpose of this
illustration this assumption can be made) and the expression
is integrated from f to f., then
where f = reactor influent weight ratio, pyrite/coal
f. = reactor effluent weight ratio, pyrite/coal
t = time in reactor
If t is the time to reduce the pyrite content from 100% to
5% of the influent amount and t1 is the time required to
reduce the pyrite content from 100% to 4.4%, then the
percent increase in residence time required is approximately
100((t'-t)/t).
This percent increase in residence time can be interpreted in
another way: If the residence time in the reactor is held
constant and the product is improved by increasing the pyrite
removal from 95.0 to 95.6%, then 100((t'/t)-l) is the per-
centage of residence time saved by regenerating ferric iron
in the mixer. Examples are given on the next page and in
Section 10.8.4.
These estimates are conservative since Y was held
constant. The value of Y will be higher when there
is regeneration in the mixer. On a weight ratio basis
the percentage of product improvement was 14-27% which
is in good agreement with this approximate analysis.
-215-
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Ferric Iron No Regen- Percent Improvement
Regeneration eration in Due to Regeneration
in the Mixer the Mixer in the Mixer
Case 1.
Percent
pyrite removal 95.6 95.0 0.6
Reaction time
improvement 14.73
Case 2.a
Percent
pyrdte removal 95.6 94.5 1.1
Reaction time
improvement 26.84
Cases 1 and 2 show the improvement in reaction time when
there is ferric ion regeneration in the Mixer with 95.6%
pyrite removal for the whole process compared to no regen-
eration in the Mixer and overall pyrite removal of 95.0%
for Case 1 and 94.5% for Case 2 (Calculations are given in
Section 10.8.4).
7.3.2 Leaching Rate Constant Variation
One of the process parameters that the quality of the
product coal is particularly sensitive to is the leaching
rate constant. This parameter is generally thought of as
constant at a particular temperature, but there are sev-
eral ways in which it will vary.
(24)
In other independent studies of pyrite leaching from coal,
it has been shown that the leaching rate varies for different
coals and that the rate is even different for stoichiometri-
cally similar but structurally different pyrites in the
same coal.
-216-
-------
Another source of variations in KT will occur because of
LI
feed coal mesh size variations. For instance, it may be
found that a larger feed size must be used because the
hydrophobicity of -100 mesh coal prevents it from forming
a slurry in the mixer.
In heterogeneous rate studies the specific rate constant
^ I
usually has a dimension (Area) . However, because of the
obvious difficulties that would arise in estimating the
surface area of pyrite, TRW expressed the leaching rate
constant for -100 mesh coal. Therefore, the actual rate
is constant.
K' = KT/A (15)
LI LI
Where A = surface area of pyrite in the coal.
In order to obtain a rough estimate of the sensitivity of
the process to a change of feed size from -100 mesh to -48
mesh a simulation was run. A particle size increase of
about two would mean an area reduction of about four. A
rate constant reduction of four is probably conservative
as there will be fewer fines and therefore more pyrite
occluded within the coal. Figure 48 shows the molar flow
rate of pyrite from the reactors under different operating
conditions. Curve #1 shows the results for the -48 mesh
coal and, for the purpose of comparison, curve #2 shows
the results for the -100 mesh coal. One can see that when.
processing -48 mesh coal additional process modifications
will have to be made in order to obtain a product with a
pyritic sulfur level similar to that obtained with -100
mesh coal.
-217-
-------
140 4
0
rH
O
6
CO
^
O
o
d
0
0)
«H
100
«H
O
JH
A
iH
O
; Pyritic Coal in Reactors;
: at Start-up LU .
III i , I i i i I i i IT i i :".".
::1- 48 Mesh Designed Process
" , Pr=120,T=170,
Regen. Acid
tra:7- 48 Mesh,P=120,T=170,Regen
i-4-U- •*•
„__ j , '
30 50
Process Operation Time, Hours
Figure 48. Pyrite Effluent Flow Rate Variation for
Different Process Operating Conditions
-218-
-------
Assuming that the rate limiting step in the reaction does
not change with increased temperatures and pressures and
that equipment modifications could be made/ several simu-
lations were made to see what type of conditions would be
needed to obtain an acceptable product. Actions that were
taken were intended to enhance the leaching rate. In the
first run ferric ions were regenerated in the mixer and
the pressure over the reactors was increased to 120 psia.
This result is shown as curve #4. This action does not
improve the results because the increased regeneration
depletes the system of acid. An acid make-up stream flowing
to the reactor effluent was included. This improved the
product coal but not sufficiently (curve #3). Curves #5
and #7 show the same effects as seen in #4 and #3 with the
average temperature in the reactors increased to 170°C.
This action increases the value of the leach and regenera-
tion rate constant, but the buoyancy pressure increases
rapidly with temperature, reducing the partial pressure of
oxygen. One final run (#6) was made where the temperature and
pressure were increased to 200°C and 250 psia. Under these
conditions, the product coal was acceptable. Yet, it must
be remembered that the process was designed for 80 psia and
128-160°C operation. Further, because of the limited range
of the temperature data, one does not know what step is rate
determining and extrapolation is no more than hypothetical.
Yet, even with these assumptions it is clear that sizable
changes in design conditions and equipment may be necessary
in order to compensate for any reductions in the leach rate
caused by larger feed size, different pyrite level, etc.
7.3.3 General Discussion
Discussion in the previous sections was centered around
-219-
-------
three general areas of chemistry and their effect on the
process. In Section 7.2.3 the impact of solution concen-
tration control on the operating efficiency and the quality
of the product coal was discussed. In Section 7.3.1 the
effect of increasing the amount of regeneration was touched
upon, and in Section 7.3.2 the leaching rate and regenera-
tion rate were covered. The knowledge obtained by looking
at these areas will now be used as input for making minor
changes, for selecting startup conditions, and for making
operating changes when process variations occur. This
discussion will by no means exhaust all the possible
changes or conceivable condition variations, but it will
show that the use of simulation can provide sufficient
insight into the process so that reasonable action can
be taken.
7.3.3.1 Variation of Pyrite Feed to the Process - The
assay of pyrite in coal has been assumed to be fixed at
135-136 Ib-moles per hour. It was of interest here to see
how the process would handle variations in the feed and
what changes might be made to accommodate these variations
in the best manner possible. The pyrite assay was made to
vary in two ways. In one simulation the amounts of pyrite
in the feed were drawn randomly from a normal distribution
having a mean value of 135.87 and a standard deviation of
25. This large standard deviation was selected in order to
see how the process would be affected by large perturbations,
Figures 49a and 49b show the influent and effluent pyrite
flow rates. While the variations shown in Figure 49a occur
every hour, in the actual simulation the variations
occurred every ten minutes. The difference is simply
-220-
-------
!.U.i_i.j IT-LTL1.I i'i .
200
Sffiffifi
Figure 49b.t
30 5O
Process Operation Time, Hours
Figure 49. Variation in Flow of Pyrite as the Pyrite Feed
to the Process Is Varied Randomly Using a Normal Distribution
-221-
-------
because step size for integration was made on a ten minute
basis and output printed only on an hourly basis. Figure
49b shows that even with the large fluctuations the process
removes at least 92 percent of the pyrite. Recall from
Figure 44a that ferric ion regeneration in the mixer
worked to dampen the pyrite flow fluctuation. If large
fluctuations are encountered, mixer ferric regeneration
might be considered as a way for maintaining steady pyrite
to the reactors.
Another approach to pyrite assay variation is to make
step variatons that persist for a period of time. This
method is very satisfactory for determining what accommoda-
tions are needed to meet with the change.
One such situation that is of interest is the determination
of the plant modifications that could be made when the
pyrite assay in the feed is lower. In the situation simu-
lated the assay was reduced by 50 percent. Figure 50 shows
the amount of improvement gained in the product for this
reduction in the pyrite feed. This figure further exem-
plifies what is stated in Equation (9), Section 7.3.1. The
amount of pyrite in the clean coal is quite insensitive to
the influent amount when residence time/ t, as well as KT
LJ
and Y are held constant. However, there is some improvement
in the product beyond specification. Some changes will be
considered that may reduce either operating or capital costs
at the expense of bringing the pyrite effluent level up. No
changes in process layout were considered, as they would pre-
clude any easy economic extrapolations from the existing
design.
-222-
-------
Two simulations were made where there were five and seven
reactors. The effluent reactor streams from these simu-
lations are also shown in Figure 50. Another simulation
was made where the mesh size was reduced to -48 mesh, and
this is also shown in Figure 50. As should be expected,
none of these simplifications produced an acceptable product
because feed concentration is not as important in the ki-
netic model as is the residence time or the leaching rate
constant. With further modifications such as increased
reactor height, higher reactor temperature, higher reactor
pressure, ferric ion regeneration, etc, these new configu-
rations may be feasible, but they will not be considered
here. The main point to be gained from this discussion is
that no significant cost savings will be realized (other
than reduced oxygen costs) by using a feed coal that has
considerably lower amounts of pyrite. Then it follows that
increases in the amount of pyrite present will mean only
minor adjustments in order to meet product quality specifi-
cations. Simulation results confirm this premise. In a
simulation the process was run for 20 hours at 135.87 moles
of pyrite/hour. At 20 hours the pyrite feed rate was in-
creased to 140 moles/ hour and then increased again to 145
moles/hour at 30 hours. The pyrite effluent flow rate is
shown in Figure 51. Clearly some adjustment will have to be
made to improve the product by a small amount. (This is
not as much as Figure 51 indicates because the initial Fe
amount was only 100 moles. If the initial condition amount
were higher, this pyrite level would be even lower. See
next Section). Past discussion would suggest regeneration
in the mixer as a logical adjustment choice.
-223-
-------
JS
CO
i
O
a
0
0
!-i
•H
i*
>,
ft
-------
7.3.3.2 Modification of Start-up Conditions - In all
simulations discussed the fractional amount of each, com-
ponent at startup was proportional to the amounts used in
the design of the plant. It is of importance to know which
components must be present at startup so that steady state
with an acceptable pyrite level is rapidly attained. It
is obvious that some components must be present in signif-
icant quantities. Acid must be present to keep ferric ions
in solution and to perpetuate the regeneration of ferric
ions. The total amount of iron in solution must be kept at
a reasonable level so that there is enough available to do
the leaching. Several variations were simulated to see
how long it took for the system to converge. In one set
of simulations the amount of ferric ion present in the
mixer at startup was varied. The curves are shown in Figure
52. Another simulation was done where the liquid to solids
ratio was increased considerably. These results are also
shown in Figure 52. From these simulations it is clear
that the amount of iron in the 3+ state present at startup
should be at the plant design level or higher. Otherwise
the product will not be acceptable until after the process
has been running for a considerable length of time. A
period of increased 02 to the reactors would improve the
initial product if the iron (III) were low. Note that a
high liquid to solids ratio means a very poor product coal
will be produced. Perhaps initial solids recirculation
would be the best way to bring the mixer up to volume.
-225-
-------
15
A 10
CO
0)
o
,0
r-l
CO
SH
O
-(->
O
rt
0
PS
O
^
«H
0>
Process Influent Initially
at 135.87
--
Process Influent Increased
to 140 •
—-process Influent Increased
to 145
No Pyritic Coal in Reactor
at Start-up
10 30 50
Process Operation Time, Hours
Figure 51. Effect of Step Changes in Pyrite Feed on the
Flow of Pyrite from the Reactors
t*
&
-p
a
rt
iH
O
20
15
10
i-mm::
i I —'-i— : I
Average Amount of
Coal N.ormally in
Mixer at Start-up
•_l Replaced with
Water
*_ Initial Amt.
-j ; : Fe in Mixer=
t ,^100 Ib. mo 1 e/hr.
Initial Amt.
Fe + in Mixer =
426 Ib. mole/hr.
10 30 50
Process Operation Time, Hours
Figure 52. Effect of Changes in Start-upConditions on the
Flow of Pyrite from the Reactors
-226-
-------
7.4 SUMMARY
This study satisfies two objectives: The coal desulfur-
ization chemistry as it relates to the process has been
studied and recommendations made concerning additional
data needs and process modifications. Also the simulation
model provides a means for studying the process sensitivity
to condition and equipment variations. Its use will provide
quick answers at a minimal expense to the user. Also, it
can be expanded in more detail once the needed data are
obtained. At that point it can be coordinated with an
economic evaluation program so that any questions can be
answered with reasonable accuracy from-both a physical-
chemical and economic point of view.
-227-
-------
7.5 CONCLUSIONS
A. The proposed process under the assumptions and condi-
tions of design shows no excessive buildup or depletion
of necessary components.
B. More laboratory data are needed in the following areas:
(1) Density and heat capacity data are needed to allow
better estimates for residence times, vessel volumes,
evaporation rates, and heat exchange calculations.
(2) The conditions of precipitate formation need to
be defined. The acidic-basic ferric sulfate system
is well defined in the temperature range of interest,
but the ferric hydroxide and ferrous sulfate systems
are not defined in the temperature and ionic strength
ranges of interest. Precipitation of ferric hydroxide
can mean contamination of clean coal and reduced effi-
ciency of oxygen usage. Iron sulfate removal energy
costs are directly related to ferrous sulfate solu-
bility, so the importance of this solubility data is
obvious.
(3) Experimentation should be done to determine
whether sulfur is a product of a continuous pyrite
leaching operation.
(4) The leaching reaction should be studied at higher
temperatures to determine whether increased temperature
causes any change in the rate controlling step.
(5) Experimentation should be done to determine the
correct stoichiometric coefficient for the ferric ion
-228-
-------
involvement in the leach reaction. There is some
indication that the oxygen requirement may be 50%
higher than the design indicates.
C. The iron sulfates removal operation is favorably located.
Ferrous sulfates can be removed at this point with a mini-
mum amount of water evaporation. Also, the potential for
ferric hydroxide or sulfate precipitation is lowest at this
location.
D. The oxygen usage efficiency would be increased by in-
stalling a surge tank for additional leaching between the
mixer effluent and the point where stream #16 is taken from
stream #5. The capital costs should be balanced against
lower oxygen cost.
E. A pH controlled acid make-up stream into the reactor
effluent is needed to keep ferric precipitates from forming,
adhering to the coal during filtration and leaving the
process with the clean coal.
F. Regeneration of ferric ions in the mixer does improve
the leach operation. The improvement studied used 9-10
moles/hour of additional oxygen. This regeneration in the
mixer rapidly depleted the system of acid, so an acid make-
up stream would be required. Regeneration in the mixer
would also mean low oxygen efficiency as more ferric mate-
rial would be removed in the iron sulfate removal stage.
Part of the efficiency could be regained if the surge or
holdup vessel mentioned in (D) above was used.
G. Reduction in the leach rate because of differences in
pyrite structure, mesh size of the coal, etc. will lead to
serious operating problems. Simulations for a hypothetical
-229-
-------
-48 mesh coal indicate that either much higher temperatures
and pressures or longer residence times will be required in
the reactors. Preliminary reduction of the amount of pyrite
in the coal will not solve the problem. A simulation of
-48 mesh coal with half the pyrite present does not meet
the specifications. The variable that could improve this
situation considerably is the level of pyritic sulfur in
the product. Small increases in this acceptable level
can mean decreased reaction time.
H. The process responds well to large random variations in
the feed. The pyrite removal remains within an acceptable
range with only small and infrequent time periods in which
oxygen is wasted.
I. Reductions in the pyrite feed assay which are constant
for considerable periods of time will reduce the efficiency
of the oxygen usage unless its flow rate is controlled by
some type of on-stream pyrite feed analyzer.
J. A large reduction in the amount of pyrite in the coal
fed to the system has only a small effect on the quality
of the product coal. Consequently, it does not follow
that a sizable reduction of the pyrite feed assay will
mean a considerable plant cost reduction. There will be
an operating cost savings through reduced oxygen costs,
however.
K. As the product coal quality is insensitive to reductions
in pyrite feed assay, it is also insensitive to increases
in assay. This means that this process can handle larger
amounts of pyrite by merely increasing the oxygen feed
-230-
-------
proportionately. If additional 02 is required, its addi-
tion in the mixer will provide a longer leach residence
time.
L. At startup, care must be taken to ensure that at least
minimum acid, Fe and liquid/solid levels are maintained.
Otherwise a large amount of the initial product will not
be acceptable.
-231-
-------
8.0 REFERENCES
1. U.S. Environmental Protection Agency, Office of
Research and Monitoring, Washington, DC, "Chemical
Desulfurization of Coal: Report of Bench-Scale
Developments," Volumes 1 and 2, by J. W. Hamersma et
al., Systems Group of TRW, Inc., Redondo Beach, CA,
Report No. EPA-R2-73-173a and b, February 1973,
Contract No. EHSD 71-7.
2. U.S. Environmental Protection Agency, Office of
Research and Development, Washington, DC, "Appli-
cability of the Meyers Process for Chemical Desulfur-
ization of Coal: Initial Survey of Fifteen Coals,"
by J. W. Hamersma et al., Systems Group of TRW, Inc.,
Redondo Beach, CA, Report No. EPA-650/2-74-025,
April 1974, Contract No. 68-02-0647.
3. U.S. Environmental Protection Agency, Research Tri-
angle Park, NC, "Bench-Scale Development of a Process
for the Chemical Extraction of Sulfur from Coal,"
Systems Group of TRW, Inc., Redondo Beach, CA,
Contract 68-02-1336. (Report in preparation)
4. U.S. Environmental Protection Agency, Research Tri-
angle Park, NC, "Pilot Plant Design of Meyers Process
for Chemical Removal of Pyritic Sulfur from Coal,"
Systems Group of TRW, Inc., Redondo Beach, CA,
Contract 68-02-1335. (Report in preparation)
-233-
-------
5. Staehlef R. W., and Latanision, R. M., "Stress Corro-
sion Cracking of Iron-Nickel-Chromium Alloys," pp. 214-
307 in Proceedings of Conference, Fundamental Aspects of
Stress Corrosion Cracking, The Ohio State University/
Dept. of Mechanical Engineering, Columbus, Sept. 11-15,
1967, published by National Association of Corrosion
Engineers, Houston, TX, 1969.
6. English, J. L., and Griess, J. C., Corrosion 20, 138t-
144t (1964).
7. Shell Development Company, Houston TX, Letter from
R. J. Grabowski to Lloyd Lorenzi, Environmental Pro-
tection Agency, Contract EHSD 71-45, Task 28, "Trace
Element Determination in Process Streams," 1-11-73.
8. National Research Council, Division of Chemistry
and Chemical Technology, Committee on Chemical
Utilization of Coal, "Chemistry of Coal Utilization,"
prepared by the Committee: H. H. Lowry, Chairman,
Wiley, New York, 1945, volumes 1 and 2; pp. 586-588
in volume 1.
9. Pollack, S. S., Fuel 5_0, 453-454 (1971).
10. Western Division of Dow Chemical U.S.A., Pittsburg,
CA, Letter from T. Lingafelter, to H. Farber,
Midland, MI, 8-8-73.
11. Visman, J., and Hamza, H. A., "Application of Floc-
culants in Hydroclone Separation," The Canadian Mining
and Metallurgical (CIM) Bulletin, Feb. 1973, pp. 78-85.
-234-
-------
12. Dowell Division of Dow Chemical U.S.A., Tulsa, OK,
Letter from C. F. Parks, to L. D. Boughton, Tulsa OK,
"Pelletizing Tests at Bethlehem Steel Company
Laboratory," 9-10-71.
13. Dowell Division of Dow Chemical U.S.A., Tulsa, OK,
"Pelletizing Coal," by K. H. Nimerick, Report No. DL
8086-4, 9-21-71
14. Dowell Division of Dow Chemical U.S.A., Tulsa, OK,
"Mineral Binder," by K. H. Nimerick, Report No. DL
50004 and 50005, 4-14-72.
15. U.S. Environmental Protection Agency, Research Tri-
angle Park, NC, "An Evaluation of Coal Beneficiation
by the Meyers Process," Final Report by George E.
Weant, Forest 0. Mixon and Faust L. Bellegia, Research
Triangle Institute, RTI No. 43U-893-30, July 1974,
Contract No. 68-02-1325-3.
16. Shell Development Company, Houston, TX, Letter from
S. A. Shain to Lloyd Lorenzi, Environmental Protection
Agency, "OAP Contract EHSD 71-45, Task No. 27,"
"Study of the Product Value and Pollution Aspects of
By-product Iron Compounds," by S. F. Liang, 11-7-72.
17. Electric Power Research Institute, Palo Alto, CA,
"Evaluation of Coal Conversion Processes to Provide
Clean Fuels," Final Report, by Donald L. Katz et al.,
Prepared Under Research Project EPRI 206-0-0 by
University of Michigan, College of Engineering, Ann
Arbor, Feb. 1974, Report No. EPRI 206-0-0, Parts I,
II, III.
-235-
-------
18. U.S. Environmental Protection Agency, Office of
Research and Development, Washington, DC, "Cost
Analysis of Meyers Coal Desulfurization Process," by
B. P. Shepherd, H. K. Michael, J. S. Wilson, The Dow
Chemical Company, Freeport, TX, May 1974, Contract
No. 68-02-1329.
19. Ledgemont Laboratory, Kennecott Copper Corporation,
Lexington, MA, "Chemical Desulfurization of Coal," by
J. C. Agarwal et al., paper presented at American
Mining Congress, Coal Convention, Pittsburgh, PA,
May 1974.
20. Chemical Marketing Reporter, 9-23-74.
21. Posnjak, E. and Merwin, H. E., J. Amer. Chem. Soc., 44,
Pt. 2, 1965-1994 (1922).
22. Langmuir, D., "Geochemistry of Iron in a Coastal-Plain
Ground Water of Camden, New Jersey Area," U.S. Geolog-
ical Survey, Professional Paper 650-C, 1969, pp.
C224-C235.
23. Garrels, R. M. and Thompson, M. E., Amer. J. Sci.,
258-A, 57-67 (1960).
24. Carrucio, F. T., "The Quantification of Reactive
Pyrite by Grain Size," Third Symposium on Coal Mine
Drainage Research, Mellon Institute, Pittsburgh, PA,
May 1970.
-236-
-------
25. "Handbook of Chemistry and Physics/" 53rd Edition,
1972-1973, Robert C. Weast, Editor in Chief, The
Chemical Rubber Co., Cleveland, OH. pp. B62-156,
C75-535, F251-276.
26. Popper, H., Ed., "Modern Cost-Engineering Techniques,"
McGraw-Hill, New York, 1970.
27. Miller, N. W., Dow Chemical U.S.A., Michigan Division,
Midland, MI, Chlor-Alkali Plant, Private Communication,
February 1974.
28. Nekervis, W. F., Dow Chemical U.S.A., Michigan Division,
Midland, MI, Contract Projects, to Lloyd Lorenzi, Jr.,
EPA, "Coal Preparation as an Adjunct to the Conceptual
Design," June 1974.
29. Seidell> A. and Linke, W. F., "Solubilities of Inor-
ganic and Metal-Organic Compounds," 4th ed.,(2 vols.),
American Chemical Company, Washington, DC, vol. 1,
1958; vol. 2, 1965.
30. Garrels, R. M. and Christ, C. L., "Solutions, Minerals
and Equilibria," text ed., Harper and Row, New York,
1965.
31. Arthur D. Little, Inc., Cambridge, MA, "Service to
Management Program," Report on "Powder Metallurgy,"
June 1969.
32. Hirschhorn, Joel S., "Introduction to Powder
Metallurgy," American Powder Metallurgy Institute,
New York, NY, 1969, p. 33.
-237-
-------
33. Engineering News-Record, McGraw-Hill, New York, NY,
January 2, 1975.
34. Chemical Engineering, McGraw-Hill, New York, NY,
April 28, 1975, P. 180.
35. Ricci, L. J., "CE Cost Indexes Accelerate 10-Year
Climb," Chemical Engineering, McGraw-Hill, New York, NY,
April 28, 1975, PP 117-118.
36. National Coal Association, Washington, DC, "Coal
Facts 1974-75," 1975., P. 68.
37. Ledford, W. E., Dow Chemical U.S.A.., Designed Products
Technical Service and Development, Private Communication,
Midland, MI, September 1973.
-238-
-------
9.0 GLOSSARY
The technical terms and abbreviations used in the text,
tables and figures (other than abbreviations for chemical
elements and terms previously defined for use in mathe-
matical derivations) are listed below with the correspond-
ing definitions. Conversions for metric and conventional
engineering units are also included.
Acre Acre (0.40 Hectares)
ASA American Standards Association
AT or A/T After Taxes
Ave or Avg Average
Baf Baffle
BHP Brake Horsepower (U.S.) (1.01387 Metric BHP)
BT or B/T Before Taxes
Btu, btu British Thermal Unit (252 calories),
(0.252 kcal), (1055 joules)
C Centigrade
ca Approximately
cal Calorie (gm) (0.003968 Btu)
CCW Counter-clockwise
Ch Channel
Cm, cm Centimeter (0.3937 in.)
22 2
Cm i cm Square Centimeter (0.1550 in. )
Cp Centipoise
Cs Centistoke
CS Carbon Steel
CSMP Continuous Simulation Modeling Program
Cu Cubic
Cu ft Cubic Feet (0.028317 M3)
-239-
-------
CW Clockwise
cwt Hundredweight (45.36 kg)
Deg Degree
DFC Direct Fixed Capital
DI Ductile Iron
E, Electrochemical Potential
F Fahrenheit
Fig. Figure
ft Feet (0.3048 M), also the symbol '
ft2 Square Feet (0.0929M2)
ft3 Cubic Feet (0.028317 M3)
Fltg Floating
gal U.S. Gallons (0.0037854 M3)
gpm U.S. Gallons per Minute (0.22712 M /hr)
g or gm Gram
9
GJ Gigajoules, 1 x 10 joules
H Heat of Reaction
Hd Head
hpf HP U.S. Horsepower (1.0139 metric hp)
hr, HR Hour
ID Inside Diameter
in. Inches, (2.54 cm), also the symbol "
2 2
in. Square Inches (6.45 cm )
IPS Iron Pipe Size
K Kelvin Temperature
kcal Kilocalories (3.968 Btu)
-240-
-------
kg
2
kg/cm
KW
KWH, kwh
Kilogram (2.205 Ib)
Kilograms per Square Centimeter (14.223 psi)
Kilowatt
Kilowatt Hours
Ib
Ib/hr
LMTD
1, L
Pound (0.4536 kg), also the symbol #
Pounds per Hour
Log Mean Temperature Difference
Liter (0.2642 U.S. gal)
M
MM
M
M3
M3/HR
MH
ink
min
ml
mm
mole, mol
mpf
MT
MTPH
MW
Thousand
Million
Meter (3.2808 ft)
Cubic Meters (35.315 ft3) (264.17 gal)
Cubic Meters per Hour (4.4029 gpm)
Manhole
Mark
Minute, also the symbol '
Milliliter
Millimeters (0.03937 in)
Mole, One formula weight of an
element or compound
Moisture and Pyrite Free, Without Binder
Metric Ton (1.1023 short tons) (1000 kg)
Metric Tons per Hour (1.1023 TPH)
Molecular Weight, also Megawatts (1000 KW)
N.A.
NO.
Not Applicable
Number, also the symbol #
OD
OAH
oz
Outside Diameter
Overall Height
Fluidounce (29.6 ml)
-241-
-------
pH Hydrogen Ion Concentration
PO Purchase Order
2
psi Pounds per Square Inch (0.070307 kg/cm )
psia Pounds per Square Inch Absolute
psig Pounds per Square Inch Gauge
Req'd Required
RL Rubber Lined
ROI Return on Investment
ROM Run of Mine
ROS Return on Sales
ROTC Return on Total Capital
rpm Revolutions per Minute
Sec Second, also the symbol "
Sq Ft Square Feet (0.0929 M2)
Stat Stationary
SS Stainless Steel
T, t Short Ton (0.90718 MT)
T Absolute Temperature |
Tan Tangent
TC Total Capital
Ti Titanium
TPH Short Tons per Hour (0.90718 MTPH)
TPY Short Tons per Year
V Volts
Vol Volume
Yr, yr Year
wt Weight
-242-
-------
°C Degrees Centigrade((°F-32)/I.8)
°F Degrees Fahrenheit ((°Cxl.8) + 32)
°K Degrees Kelvin (°C + 273.2)
% Percent
304 Type 304 Stainless Steel
316 Type 316 Stainless Steel
1 Feet (0.3048 M)
1 Minutes
Inches (2.54 cm)
" Seconds
A Delta, Change or Difference
AT Temperature Difference
# Number
# Pounds
-243-
-------
10.0 APPENDIX
10.1 DRAWINGS
10.1.1 List of Drawings
Page
Block Flowsheet
Process Flowsheets
Feed Coal Preparation
Mixing & Reaction
Filtration #1
Extraction, Filtration, Decantation
Water Washing, Filtration, Decantation
Drying & Decantation
Compacting
Product Coal Handling
Iron Sulfates Removal
Distillation
Vent Collection & Scrubbing
Utilities
Index Flowsheet
Legend Sheet
Plot Plan
Floor Plans—1st, 2nd, 3rd Floors
Floor Plans—4th, 5th, 6th Floors
JN-730623
34
Bl-001-730623
Bl-002-730623
Bl-003-730623
Bl-004-730623
Bl-005-730623
Bl-006-730623
Bl-007-730623
Bl-008-730623
Bl-009-730623
Bl-010-730623
Bl-011-730623
Bl-012-730623
Bl-013-730623
Bl-014-730623
B2-001-730623
B5-001-730623
B5-002-730623
93
96
99
100
103
106
107
108
111
114
117
125
91
92
122
123
124
-245-
-------
10.2 EQUIPMENT
10.2.1 List of Equipment
The equipment numbers refer to the respective equipment
positions in the process flowsheets of Section 4.5.
Sector 000 - Feed Coal Preparation
001 Car Dumper House
002 Rotary Car Dumper
003 Hopper
004 A-D Feeders
005 Collection Conveyor
006 Belt Conveyor
007 Belt Scale
008 Magnetic Separator
009 Transfer Tower
010 Distribution Conveyor
Oil A&B Rotary Plow Feeders
012 Reclaim Conveyor
013 Belt Conveyor
014 Belt Scale
015 Magnetic Separator
016 Gallery
021 Crusher-Pulverizer House
022 Surge Bin
023 A&B Crusher Feeders
024 A&B Crushers
025 A&B Pulverizers
031 Belt Conveyor
032 Distributing Conveyor
033 A-D Hoppers
034 A-D Feeders
-246-
-------
Sector 100 - Mixing
100 A-l Mixer Agitator
100 ME-1 Coal Elevator
100 V-l Mixer
100 V-2 Mixer Vent Absorber
Sector 200 - Reaction
200 E-l Reactor Product Cooler
200 P-1A&B Reactor Feed Pumps
200 R-1A-K Reactors
Sector 400 - Filtration #1
400 F-1A-D Rotary Drum Filters
400 ME-1 Conveyor
Sector 500 - Extraction
500 A-l Extractor Agitator
500 V-l Extractor
Sector 600 - Filtration #2 & Decantation
600 F-1A-D Rotary Drum Filters
600 ME-1 Conveyor
600 P-1A&B Filter Feed Pumps
600 P-2A&B- Aqueous Forwarding Pumps
600 V-l Decanter
-247-
-------
Sector 700 - Water Washing
700 A-l Water Wash Tank Agitator
700 V-l Water Wash Tank
Sector 800 - Filtration #3 & Decantation
800 F-1A-D Rotary Drum Filters
800 ME-1 Conveyor
800 P-1A&B Filter Feed Pumps
800 P-2A&B Aqueous Forwarding Pumps
800 V-l Decanter
Sector 900 - Drying, Compacting, Decantation
900 ME-1A&B Dryers & Solvent Recovery Systems
900 ME-2A&B Conveyors
900 ME-3 Conveyor
900 ME-4 Compactor
900 ME-5 Elevator
900 P-1A&B Binder Solution Pumps
900 P-2A&B Binder Unloading Pumps
900 T-l Binder Solution Tank
900 V-l Dryer Condensate Decanter
Sector 1000 - Product Coal Handling
1001 Belt Conveyor
1002 Transfer Conveyor
1005 Distributing Conveyor
1006 A-D Silos
1007 A-D(1-7) Feeders
-248-
-------
1008 Reclaim Conveyor
1009 Car Loading House
Sector 1100 - Iron Sulfates Removal
1100 A-l Reslurry Tank Agitator
1100 E-l Sulfate Evaporator Heater
1100 E-2 Sulfate Cooler
1100 E-5 Flash Steam Condenser
1100 F-1A&B Sulfate Filters
1100 F-2 Sulfate Filter
1100 ME-1 Wash Water Heater
1100 ME-2 Sulfate Waste Dryer
1100 P-1A&B Sulfate Forwarding Pumps
1100 P-2A&B Sulfate Evaporator Circulating Pumps
1100 P-3A&B Recovered Water Feed Pumps
1100 P-4A&B Sulfuric Acid Feed Pumps
1100 T-l Wash Water Surge Tank
1100 T-2 Sulfuric Acid Storage Tank
1100 V-l Sulfate Evaporator
1100 V-2 Reslurry Tank
Sector 1400 Distillation
1400 E-l Solvent Evaporator Reboiler
1400 E-2 Solvent Evaporator Feed/Overhead Exchanger
1400 E-3 Solvent Evaporator Condenser
1400 E-4 Solvent Cooler
1400 F-l Solvent Evaporator Feed Filter
1400 P-1A&B Solvent Evaporator Feed Pumps
1400 P-3A&B Recovered Solvent Feed Pumps
1400 P-4 Sulfur Loading Pump
-249-
-------
1400 P-5 Solvent Makeup Feed Pump
1400 T-l Solvent Evaporator Feed Tank
1400 T-2 Recovered Solvent Surge Tank
1400 T-3 Sulfur Surge Tank
1400 T-4 Makeup Solvent Storage Tank
1400 V-l Solvent/Sulfur Distillation Column
1400 V-2 Accumulator
Sector 1500 - Vent Scrubbing
1500 E-l Scrubber Cooler
1500 P-1A&B Scrubber Circulating Pumps
1500 P-2A&B Recovered Naphtha Pumps
1500 V-l Scrubber Tower
1500 V-2 Scrubber Surge-Decanter
Sector 2000 - Utilities
2100 Steam Generation Plant
2200 Water Supply
2201 Process Water System
2202 Potable Water System
2203 Fire Protection System
2204 Cooling Water System
2300 Oxygen-Nitrogen Plant
2400 Instrument Air System
-25O-
-------
10.2.2 Equipment Specifications
The following equipment specification sheets are arranged
according to sector and equipment number.
-251-
-------
FILE'JOB
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS c?/y.g-
8'M NO.
P. 0. NO.
s?
75
H.
r> f
C67
r
. _, ,
/rto-ror Pro De.//c.'A
, s>,
72O
TP fr
G -f
<--—
A"
C r\ e
€)/
Gallery
SPEC. BY
CHECKED;
APP'Di
DATE: '/,-. 7
3s5P> THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE
•HCCT or
25260 3-09
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO.
-252-
-------
r/c
FILE/JOB NO 7-?/^ 2
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
P. 0. NO.
1?
O?J
vert
7^ A/
Z(,&
621.
// "
r /
II •* ••
33
SPEC
IHECKEO:
kPP'O:
THE DOW CHEMICAL COMPANY
SERVICE
RE VISION DATE
|*HCBT OP
Itouir
cz/'
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO.
2&2BO 3-ft
-253-
-------
PLANT
TIC.
'f* to V.4-L
FILE/JOB NO. ~73Q£>2. 3
LOCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B'MNO.
P. 0. NO.
11
12
13
14
15
16
IT
18
TP H-
19
ti- a + THE DOW CHEMICAL COMPANY
SERVICE
REVISIONOATE
ItHllT of
OOO
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
252603-C8
-254-
-------
PLANT f.r>(J /- /cy/V/7'C J>
LOCATION
£, /-fjjr ytf*
fsyjAsa./ FILE/J
BLDG. NO. CHARG
MANUFACTURER Z/ *s ,/>//?/>? 8 *? <3S ~7 5 No,UNiTS 1 h? r Trf)>O B/MNO
i
2
3
4
5
6
7
8
9
10
11
12
13
TT
IS
16
17
18
19
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
*/>
I
n
z
n
OPERATING C
<
t-
<
TANK & INSTALLATION D
<
<
OL
UJ
>
0-
a
X
3
' P. 0. N
DB NO. Y3& & 2 a
E NO.
,
0.
Mounting: Portobl* • P*rmon*nt for Op*n Tank • Sid* Entering -Qop Entering. Bottom Entering
Mo!«riol» lo B* Mixed
{^SJJf / M
^f *%?'*' \
f~e?fS&A) $
//> &£) d-
iff* O
State 1
Lbper./j/" Viscosity .-ce
<$£>//£? •- *t & 7,k*?jr
• Liqcj/d
\
FrnufMi.hif* \S/(jrr^/
Solids Pr*>*nt Ar*: (Solubl.) Qniolubl
Porticl* Six* or Si*v* Aialysis:
S»ttling Roto of Solids:
/3Z2.-7'\
(o $ '.£ 1 °l \O-S.ef^5
4?&cf '
f+53 &3 j>"«
£ofi ?> & 3
Spec. Gray. e F
/•££> 7£>
/t/8 2. /^T
/. 2 2 i2.
«> AbroiivVv Crystalline • Sticky or Gummy - Lighter Fluffy
/£>£>
IS*
yfr^e?S/b ^r^yftSd' ^>c.\
rV S/Ot*J f0LO L/S 5
Foarning T*nd*ncy of Mixture: Low - Medium - High /^/ O
Class of Agitation: Blend • Dissolve -
Other: A-£{?f^/2
Disperse Gas-^gusi
end Solidly Heat Transfer- Emulsify
Degre* of Agitation: Mild -(MediurJ- Violent
Too Much Agitation Will /7^/^£. & <£ C, ff S.S / >^f* /Offf/i^T
Too Little Agitation Will S/£ J~ tt/& j~ 4f SJ ft / ^(vC-fj
Largest Batch or Greatest Liquid Depth:
Smallest Botch or Lowest Liqufd Depth:
Mixer Shot! Re Des gned to
In
Minutes
Mixci A.I! ^WTJI Not)Be operated While Filling or Drawing Off
Vessel Tyoe: Open Top -Closed Top^ Horiiontol t^Vertleal) QP\ Tonk> 0**T:
Site: Z4-'~&" te*
Bottom Tvoe:C>|st jFlanoad
Top Type: F ) vt . • .'-.•!
ID by 2_5'-G" tar Straight Sid* or
& Dished. 2:1 S*m
.'. u sH»-< - .-.] Semi
Elliptical- '.
Elliptical ^Con*")
in. Length
Vessel CD
Baffles: No. 4- ; Width 2.f
Stabilizing Ring Is - is Not Required;
?• In.; Length
Sixe
Shaft Seal: Mechanical Other
in.; Horixontal .(Vertical;) Other:
/4s r&f£s»f»cr)/fSL
; Typ* Lubrication WO.-Jff'
Soeciol Requirements:
Step Bearing U «
Length from Mounting Flange
In. OD: No. Blades ; Removable from Shaft: 01**} No
Additional Data:
SPEC BY£-/T/y <•§£> THE DOW CHEMICAL COMPANY
CHECKED: SERVICE ^^
APP'D:
OATEi "ZL/to/ftJL REVISION DATE
X£* ^^
A ^/,/74-
,/7*7*«>
*. / / -
B 7/X7/74 c $
IjSMtlT OP N
1 «OUI«>. NO.
/CO /^-/
AGITATOR OR MIXER
SPECIFICATIONS
PEC.
a
-255-
-------
PLANT
/c
FILE/JOB
LOCATION
BLOC. NO.
NO. UNITS / pe.r Tram
CHARGE NO.
MANUFACTURER
B'M NO.
-- /> r- £
33
34
35
SPEC BY
NECKED:
PP'O:
ATEl
THE DOW CHEMICAL COMPANY
SERVICE
REVISIONOATE A
ENDOW TO COMPLETE ALL INFORMATION MARKED
25260 3-66
I
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
-256-
-------
PLANT £'&&/- /sU/-f~ttr JF+frmVet/ FILE/JOB NO. •/Za/f.^ •*,
LOCATION BLDG. NO. CHARGE NO.
MANUFACTURER NO. UNITS / A ? f. TrA f/t B/M NO.
' P. 0. NO.
FIELD ERECTED ('YEsJ NO NO. UNITS / f)fr
1
2
3
4
S
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
MATERIALS
NOZZLE SCHEDULE
Operoting Pressure psig
Operating Temperature °F
Liquid Specific Gravity
Contents Lethal
Design Pressure esig
Design Temperature *F
Hydrostatic Tost P*ig
Shell Heads Corr. Allow. In.
Shell Heads Joint EH. X
Cede:
Radiograph: /*J O
O '
S,/ C
/ 2.
Yes rjle^
/G
3L£T&
&cs/ / e> ~f tt/t* Jer
Stamp Yes (fa)
Stress Relieve: /v/O
National Board No.
Type Supports: S£ / f 7*1
Insulation: /
Fi reproofing: S*O
Sandblast: /Jo Paint: /S/O
Manhole 2, Hinged CPovit.lT) Other
Platform Clips: fifo iLodder Clips: fj Q | Insul. Rings: yf»5
Dipe Supports: /V&
Wind Load: Pgf Q0£/£.
Wt. Empty Ik
Item Thickness Mat'l Clas
Shell in.
Heads In.
Lining Si/to '"•
In.
In.
NoiileNe&s
Flonpes
Coupling
M.H. Cover
Supports
Bolts/Studs
Nuts
Gasket*
Service
&J&J Fffft
A*r,- +ftt? r
/CO'V-1-
F,r»-C?O C
'
^' fff Mfo i. i me
" " /P»c<
•Stfff " F/9 t.f.
St f* I
Site Rating Face Typo
(2? S7 gfW &&>
3f" Zy* F-P-
tZ" J5c* f^F
gf it *
£•> t '•
2~ " «
£>tJ //*?/ //^^,5/C> fa. "/ £T
$par/c /es/&
See. &l-OO'Z-7$0£>2$ for
<2) 7c?>^z/fc/ loo -ME-' f
&8) To Mofcfo /bo- A- /
7g» ma 1cfi /&&-?* 2.
For Purifier Detail t, SM Sheet No.
<4$&> THE DOW CHEMICAL COMPANY / GO | f?""/ "*
W ' ^ /c- VERTICAL VESSEL
SPECIFICATIONS
RE VISION DATE A | J///7^ • | C SPEC
VI NOOK TO COMr>l_rTE ALL INFORMATION MARKED lllnftT O*" "(X
-257-
-------
PLANT Cea/- /J*/ri f-rc Scs/f-fr £*t
LOCATION
MANUFACTURER
•r>?£r'fr/ FILE/JOB NO. "7£,o& 2. i
BLDG. NO. CHARGE NO.
NO.
UNITS / f)sr Tra/ ^ B/MNO.
' P. 0. NO.
TYPE
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
"22"
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47_
48
49
50
!51
52
53
54
55
<
5
n
z
^
LU
0
ERNALS
z
«3
1-
ATERIAL SPECIFICATIONS
i
UJ
-J
13
o
tu
Ift
UJ
M
O
(FIELD ERECTED YES (uoj |NO. UNITS /
Op. Press. ^ pslg Op. Temp. £ / 2. ° F
Dei. Pre
ss. /O psig Des. Temp. 2/2- " F
Mo«. Allow. Press. (New & Cold) psig; Limited
Hydro. Test /O P«ig Code:
Corr. Allow, in.: Shell ; Heads
Joint Efficiency %: Shell ; Heads
v /" Self Supporting (77) No
Fi rep roo fui a: A'O
Manhole:
Platform
Hinged ^K>r»-»«£) Othen
Clips: f/O Ladder Clips
Liquid Sp. Gr. /,'/$
Contents Lethal Yes ''No)
By
Stomp Yes f^Ne^
Radiograph /\/o
Stress. Rel. A/D
Sandblast: //O
Paint: /V 'O
t/0
Pipe Supports: Insul. Rings: Y&5
Wind Load: Seismic:
Shipping
Wt. Ib Wt. Full
Tray No. Diam. Spacing Type
Thru
Thru
Thru
Thru
Material
Ib
Tray .Installation
Removable Yes No
Cartridge Support Ring
Tray Manway Yes No
Manway Size In.
Contact Device: Bubble Cops-Va ves-Perforations Weir Set. (Above Floor) In.
Describe: Adjustable to In.
. . (Adi. Slots Sealed at All Sotthgi)
Pocking:
^*
t,'-t,"£>t,t>-f-tl
Demi sten /V"^
Item
Shell. Top
Interned
Bottom
Heads- Top
Intermed
Bottom
Cone Section
Lining
Nozzle Necks
Flanges
Coupling
M.H. Cover
Skirt
Bolts/Studs
Nuts
Noz. Gaskets
Troy Gaskets
Service
Feed
Reflun
OH Vopor
Btms. Out
Retail Vop.
Refer! Llq.
Drain
Manholes
Handhotei
Th. Wells
>r. Gages
jage Gl.
SPEC BY £p
CHECKED:
Mk
A
B
C
D
E
F
G
H
J
K
L
M
Thickness Mat'l Class
In.
in.
In.
In.
In.
In.
in.
"b/Jtt in.
in.
No. Size Rtg Face Type
/ Z" >$o FF
-
1 1' " ''
-
-
-
-
i ie>" it* FF
-
-
-
-
Material
• Minimum Quality
S-fee /-
//
"
Stee. /
Mart A
N £-Dtir& n £.
S'fef 1 Alfff-t/pfn'f i~s/isd
l> l '/ /£•*<,«!•fs Q /-> neq^K
p-f~ /co- y- /
.y ^J5iv THE DOW CHEMICAL COMPANY ~/'&0 \ ^-"z."0'
SERV.CE yV?/ Vt=/^ l/^f.
APP'O:
DATE: 'tZfy/Jt.
f REVISIONDATE A
VENDOR TO COMPLETE ALL INFORMATION MARKED
J7~ ^r/^j^O^.f^^^ TOWER
SPECIFICATIONS
B C
SPEC.
HSMKCT OF NO.
-258-
-------
LANT
FILE/JOB NO. 73Q6Z
LOCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS I per
B/M NO.
P. 0. NO.
DUTY/UNIT
[NO. UNITS/Arr/'y'XlSHELLS/UNtT / |TEMA SIZE/TYPE
Vert. Slop.d
1 to horlx.
(TTS>ith Exp. Joint
U-Tub.
Kettle
Coll
Hetrpln
Be.
Flooting Hi-Pull Thru-damp Rlng-Pocked
Thermo syphon
Fintube
Other;
Add!Hanoi Pree. Doto en Sh««l No.
Inl.l
SHELL SIDE - Outlet
Inlet . TUBE SIDE - OulUt
Fluid
Totol Flow
Ib/hr
Liquid
Ib/hr
Density
Ib/eu ft
/•
Viscosity
Spec!fie Heat
Btu/lh.eF
O.
10
Thermal Conduct! vtty
Btu/h..»ef«.'>F/ft
Vgpor
Ib/hr
Mol Wt
Density
Ib/eu ft
13
Viscosity
CS-CP
Specific Heet
Bh,/lb.°F
IS
Thomtal Conductivity
Btu/hr-.o
16
Latwt Hoot
Btu/lb
17
Non>Cond«n >obl •
Ib/hr
M.W. <
M.W. <
V.loclty Mo../Min.
f»/ue
19
21
Norm. JMojc. Op«roting Tomp,
Operating Prtit. (InUt)
ptlg
Prvsfur* Drop
Allow.
Cole.
Allow
Film Co.H.
BTU/Hr. So. Ft.
Fouling Rosistanc*,
hr-»q (t-»F/Blu:
Ov»r*all Co*ffici»nK "U'o
Btu/hr-»q ft.
Cl«
S»rvie»
LMTD (
ln»toll«d Ar«o/Unit
5 SO
(t (Out»id«) Includino-Excluding Ar«o in tub* thoot*!
26
SHELL SIDE
TUBE SIDE
St..ll ID (Appreximo).)
In.
Potion Tomporoturo
No. Tub.i (Appmxlmoto)
Doftfgn Protsur*
pilg
ISO
Tub* 00
In. |Tub«Go9»
BWG
29
HydrottoUc Tot
J22.3
Tub.L«nath
Corro»ion Allew./Llnlng
In.
Tub« Pitch A O O
In.
31
Numb«r of Pottos
Joint
32
Insulation
Mol(«/Typ» Flntubot
33
Cros» Baffles: Type
Sagmcnt Cut
Spacing ApproM. Equal • S*a Sh««t No.
No. Fins
par tuba;
par In.
Numb.r
Fin Height
In. I Fin Thick.
Vessel Support»y5oddles^ Uufli Other;
In.
Provide
in. Horizontal Cut on Bottom for Condensate Drain
Long B of lies: Type
; Number
Weir Height
in.; Shell After Weir
37
Impingement Baffle Yesfffi j Condensote Lift Yes .
Removoble Bundle Yes -
Cothodic Protection Yes
TEMACIcss JLethol Ye,/No) [Cede
NoMenal Board Other
I Stamp (res)- No
Spot Radiograph; Shell Shell Cover
Cha
(Stress Relieve:
Shell
Shell Cover
Channel
Flooting Head
Weight Complete Empty/Full of Water
lb| Weight Bun die Only
41
Sandblost;
I Paint; A/Q
| Main loin
Shell ID
Tube Count
Installed Area*
Service
Inlet
Outlet
Drain
Vent
Mk
SHELL SIDE
Sin
/2
121'
Rtg
I5cf
Foce
See Neitlo Sketch on Sheet No.
Type
TUBE SIDE
SI 10
Face
Typo
Shell SleV.
Parallel Banks of
Shells In Scries
Tube SlaV.:
Parallel Banks of
Shells In Series
Stocked;
Wide
High
Ti ran turn
Stot Tube Sheet "
Fltg. Tube Sheet —
C»ss Bof./Tube
Lena Beffles
Impinge. Baffle
Weir/Lift
Tie Reds & Spacers 51 fe I
Shell
Shell Cover
Channel T<" Ll
Ch. Cover/Bonnet "
Shell Noi. Neck.
Shell Not. Flanees
Shell Fla
Chen. NOI. Necks 77Liaeel
Chen. Nai. Flanges
Chonnel Flanges
Fltg. Meod
Flta. Hd. Flange
Oemp Ring
Baits/Studs
Nut.
Vessel Supports
CASKETS & PACKING
Shall Cev
ShelUChon. Side
Channel
Channel Caver
Fltg. Hd.
CHECKED!
DATE.
THE DOW CHEMICAL COMPANY
SERV.CE
RE VISION DATE A
• MEET or
_, I BOUIf.
2-00 I £-/
HEAT
EXCHANGER
SPECIFICATIONS
SPEC
NO.
-259-
-------
PLANT (?C(ff~ fyflfj'C 5 ID XV» / FILE/J
LOCATION BLDG. NO. CHARC
MANUFACTURER NO. UNITS if)fff TfOi'1 B/MN0
' P.O. N
oBNo./'j;fc?€3 2. 'S
E NO.
_
D.
MODEL l>*&-tS NO. UNITS "]_ ASA PUMP r^YES n NO ASA DESIGNATION
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
Z
U —
it's
U
Z
o
t-
D
1-
z
u
(/I
<
a:
LLJ
<
^
UJ
a
-
r-
UJ
Liquid v<"*v**3£//£t'f-c4£o0/ S/Ltrr-y
Pumping Temperature (P.T. *p f ^^ 6F
Specific Gravity at P.T. /, *£,,
Viscosity at P.T. ^^ "2. *7* C.Ei^''
Vapor Pressure at P.T.
Corrosion or Erosion Factors: «^ t&O /M£2ff"l &£& V
Max. Capacity ot ^^-QoQ^COi.
Discharge Pressure / <^ *j[~
y Was / S 5O """
psia ft.
Suction Pressure «3 *^ pl'° ' *^.C5 '*•
Differential Pressure / / J^
Differential Head
NPSH Available
NPSH Required (Water)
psi
2-2.7 ft.
' ft.
ft.
Arrongement^fT0MT^Vert..|n Line Suction^Single^ Double
Cose: Design Pressure psig Number of Stages / ;Shut
Max. Allow. Working Press. psig Volumetric Efficiency at Rating
rpm
•Off Pressure ft.
X
Split; Horiz- Vert-Barrel Impeller Type XOl.^.tf/Tr1
Impeller Diameter; Supplied / ^T inches; Maximum f£ f inches
Vent and Drain Topped: Yes - No Bearings: Thrust
Suction £ **
Discharge ^ °*
Vents
Drains
Cooling HjO
Radio
Minimum f / inches
Type
Type
Oiler: Yes - No; Type
Coupling(Tej^. No; Mfr.
Coupling Guard('Y«y No
Baseplate :{fYe^- No; .Type
Water Cooling: Casing-Stuff. Box-Beorings-Pedestol-Glondffione) Total Water Required:
gpm
Smothering Glond: Yes - No Lubrication on Stuffing Box; Qi l-Grease-None $/& 7 € /*
Packing^Ves^- No; Type Sealing Oil Connection; (Je^- No
Mechanical Seal; Yes ^ojj Furnished by; ; Mfr.
Wa.if.f^
Type
Single - Double-|nside-Outside-Ba lonced-Unbalanced
Rotary Unit ; Sea Ring ; Face Material
; Shaft Packing
Insert ; Reversible: Yes - No ; Face Material
Insert Mounting; Clamped In - "0" Ring . Press Fit
Gland • ; Plain: Yes -No Throttle Bushing Carbon; Yes -No
; Other
Gland/Stuffing Box Machined & Topped for; Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass * Flushing Seal Faces with External Fluid
Auxiliary Stuffing BOX Req'd: Yes - No
Weight of Pump Ib; Weight of Base
Weight of Driver Ib; Shipping Weight
Cosing & Covers: ,«5/^**
Casing Wear Rings : £ / £
Impeller: 3 / &
Impeller Wear Rings : *$ / &
Stuffing Box Bushings: ^ f/L
Ib
Ib
Shaft: $f&C /
Shaft Sleeves: 3 / Cy
Lantern Rings:
Glands:
Gaskets:
Furnished by: ^g jj ^ * &f* ; Typ«(EJec. Moto^- Steam Turbine - Other
Electric Motor: Make Mounted by l/f fjtff&f*
Enclosure (/5? /"%.* ^ Temp Rise °c
Insulation Frame
Estimated BMP Req'd. /&& hP
Nominal Motor Size (Non-overloading) / 2- ^5*" ^P
Speed rpm
Volts ; Phase ; Cyc le
Speed Reducer; Integral - Separate
Mfr. Ratio
Model Class
See Driver Specification No.
Performance Curve:£Yej)- No; Curve No.
Certified: Yes ([N^
Hydrostatic Test; 'Yes)- No; Pressure psig
Shop Inspect on; Yes £No)
Steam Turbine; Moke
-------
•LANT
FILE/JOB NO.
LOCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS fc
Trf>i<~)
B/M NO.
P. 0. NO.
FIELD ERECTED £YEi> NO
I NO. UNITS
Trr>/sj I TOTAL VOLUME cO*OOO(£cicfi) CAL
Op.rotinfl Pf.»lur«
fat
VESSEL SKETCH
Operating T»mp»fetuf»
3 /O
Liquid Sp.cific Gravity
Cont.nli L.thol
Y.t
D«»lgn Pr«siuf»
D»iifln
Hydro»raHe
Sholl Hoodt Corr. Allow. in.
Sh.ll
Hoodt Joint Ell.
Cad*:
Rodtogroph:
Str««*
Nationol Board No.
IntuloMon:
Sandblast:
|p-""= Pr/me.
Monhel* 2. Hlng»d
°ip« Suppertt:
Otti»f!
Wind lead:
Wl. Empty
lltn
SSdl
H.od.
Lining
NOHUN.AI
Coupling
M.H. Ce»«r
Supporti
Bolti/Studi
Nut>
Ga«k*t>
ft)
Thickn.i.
> in.
0) In.
t/A>«.
In.
Ib Wt Full el Wol.r
Mat'l Clo.i
Svrvlc*
TC-
46
47
48
49
Mori, Kb.
g4"
Mol'l . Minimum Quollty
Act a
77 tort/urn
/Jonc.
2'-
e_
Rating
77s
Ty»«
Bo/fosn Mead.
NoilU to b< Plugged or Blinded
For Fuftri»t P»Hlli,
SPEC. BV
CHECKED:
APP'D:
DATEl
THE DOW CHEMICAL COMPANY
SERVICE —
RE VISION DATE A
i NOOR TO COMHLCTC ALL INFORMATION MARKCC
25*40 S-e«
VERTICAL VESSEL
SPECIFICATIONS
SPEC
NO.
-261-
-------
P0&CEL4/N
$T££L
M0ZZLE
° 73O&23
/va.
-262-
-------
8" ID
PoACSLAIN
IN
2 SQUAKE.
PORCELAIN
HOLE
fc
r
///
Sv
^
/
/
/
' /
//
r^- CurAao
BKICK
DSTA/L
P0BCELAIN &LOCK DETAIL
PLAN
JOB
Sf>erc.
73O&Z3
2OO-K-
3
-263-
-------
c-c
COUPLING
S/DES
///'
*
«• /y
. 80 T.O.E.
PCS -LENGTH
PLAM
CLOSE END
-4/ D&LL - APP&OX.
So 0 HOLES
DETA/L
73O&23
Svr. N2 4-
-264-
-------
PLANT ^00
LOCATION
MANUFACTURER
MODEL/TYPE fa
1
2
3
4
5
6
7_
J_
9
10
11
J2_
13
J4_
15
16
17
18
19
X
21
22.
23
24
25
26
27
28
29,
X
31
32
33
34
35
36
37
38_
39
40
41
42.
43
44
45
46
47_
48
49
50
51
52
53
54
55
UJ
DRMANC
U.
a:
UJ
RATIONAL
UJ
0.
O
O
vi
UJ
O
i/>
_J
CONSTRUCTION DETAI
| NOZZLE SCHEDULE
/- /•
fP^f
jrv^v
V/V
s~— s
fj'C ^C//f
~)/ J »•£ f"
> £n'mf/2.'+2.'2.'
DATA f/-i /~)t* )
Fluid f
Par
At/a, 7*5}
Flow-Process Basis
Flow. Filter Basis
Density
Viscosity
pH
Solids in
Str«om
Particle SiielAvg.
Normal
Normal
Mox. Opt
i
Ib/hr
Ib/hr
Ib/euft
eentipoise
vol.vwtT^
microns *
r. Press. elig
Max. Op«r. T*mp
Allowable Pressure Drop
°F
psl
Maximum
Cycle: P
F
CekeVo
ume:
ur frm
BLDG. NO.
NO. UNITS
att
r
FIL E/JOB NO. ~/£>T 6>3 3
CHARGE NO.
/ <9 B/M NO.
P. 0. NO.
'J NO. UNITS OPERATING 4- D?f TfO"* SPARES tfOf>&
FEED Y/O}
71 ~7ooo
A 2 3p.oo
/• 1 8 s^oo
AJP
,
-) BACKWASH
CAKE^ ty
Z.~f?OQO
/• 35S[>.Qr,
Type Discharge: Wet Coke- Dry Coke
; Precooting Time
k/onG.
; Filter Aid Application Time ft
; Slowdown Time
a
Cleaning/Backwash Time
Total Time Between Successive Filter Cycles tf? /T ff'S^&^^f^
Instrumentation: Manual- Semi AutomaticCAutomali^
Fi ter
Design Pressure
Design Temperature
Hydrostatic Test
Corr. Allow./Lin.- Shell H«
Joint Efficiency Shell Hi
psig
°F
psig
ads in.
ads ^
Insulation
Electrico
Shell Feeder Tonk Filtrate Tank (
c
l
Construction: Standard Open . Cwealherpfoofj
Other;
Piping. V
alves. Fittings Supplied with Filter to
"ode;
tamp Required; Yes- No
'adiogroph;
tress Relieve:
pecial Design: /P£O@f&f)£ ^fiJ&f&JS
fiaf*Jf)r'apy/es>e. G/a'f^t
National fe'oord r/o/
Explosion Proof
be n Accerdance with:
Filter Tonk: Horiiantol - Vertical: Size
Elements
Leaves:
Area/Element
Area/Leaf
in. IDx In. Ton to Ton; Type Heads
sq ft; No. Req'd
sa ft: No.
Element or Leaf Pore Site (Avg.)
MOM! mum
Cake Th
ckness
Req'd
microns
in. IDx In. OD« In. Length
Leof Height
in.; Leaf Spacing in.
•Minimum Particle Size Retained 'microns
in: Gross Filter Volume aol-cu ft: Heel Volume aal . eu ft
Precoat Req'd: Yes {NaV Material
Filteraid
Req'd: Yes /Na? Material
Feed Pump Furnished by £>UJ/) c* /"* i
Mot'
Other Accessories
(Wetted Ports)
/^£J
Pumfii /r'///-jfl
Filter Fabric: Material
Make
; Type Seal
^ffferd fbn
; Model
;
9/> Jn//j»isel}Cjvi
Paekoae Unit Yes • No: Shoo Assembled on Skids Yes - No: Floor Space Req'd
Weight Empty/Ful
Service
Inlet
Outlet
Vent
Drain
Relief Valve
Pressure Gage
Quick Open Caver
SeeNon
SPEC BY ^f/
e Sketch
of Wate
Mark
A
B
C
D
E
F
G
H
J
K
r / Ib; Shipping Weight
No. Siie R
tg. Face Type
on Sheet No.
Item T
Filter Heads
Filter Shell
.- Lining
_J
0? Elements
>" .
r- Leaves
\ M.H. Cover
Bolts/Studs
Nuts
Gaskets
ffo/ypr0/)]rl£n£ M«»H
; Max. Flow gpm at _p*io
$•• Pump Sp«c No. & p/te rt]^0&Gpflft
fr&/t }4fo fal&»* farf (evcj Ssuitsht
ft K ft; Height ft
Ib.
hicU.i Mat'l Clasi
n.
n.
n. j
n.
Mat'l-Mlnimum Quality
\/€cf>fvn e.
r
=vV <5g>> THE DOW CHEMICAL COMPANY 4fin\ ru'//°>>
CHECKED:
APP'D:
DATE! z/8/7*£
SERVICE _
REVISION DATE A 1
l»
VENDOR TO COMPLETE ALL INFORMATION MARKED
C
||(HKCT
SPE
SPEC
or NO.
FILTER
CIFICATIONS
n«
A
-265-
-------
FILE/JOB NO. 730 £ Z
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS /
ft I
B/M NO.
P. 0. NO.
11
12
13
IS
16
£3 r-
ir
18
re.
4 D
x?/a /•& jc /
C.Q
SPEC BY
HECKEO:
PP'O:
ATE:
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE
IEQUI^.
M£-
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
-266-
-------
<".a
Materials to B» Mixed
State
Lbper- /?/t>_
Viscosity • cp
Spue. Cfov.
ncy of Miatgr*: Low • Medium - High
Ms.
Cl
Dl»p»ri»
H«ot Tfon«f»r- EmulMfy
D«gr«» e( Aaltotlon:
Violent
Too Much Agilotion Will
Toe Llttl. AgiloHon Will
t Botch or Gr«ot«it Liquid
21
Smallelt Botch or Lew«») Llqotd Ocptht
Mlx«r Sholl B« Deiigned to
In
Mlnuta*
Bottom Type: Flot- Planned & Dished. 2:1 Semi Elliptical
Top Type: Flat.^FTonged & Dished 4 2:1
Vessel Con Be Altered: (Vesj No: Describe
S«ml Elllptleol - Can«
31
psig: Doslgn T*mp*rotur«
2.0 o
32
Dew Drawing Ne.
O *~l
Copl». Attottied!
i /Ne)
33
Slio of Opening for Impel lor Instollotien
; Sii.o(Nonl. for Mounting Agltotor
34
S«l«et»d MpunUng Flang« for Agitator; Sl»
Retina
Facing
Locotieft ef Mounting Fiona*:
Bain.
No.
WldhS
In.; Horizontal. Vortleel; Olriof! >fe
Stobillilng Ring Is • It Net R«qulf«J; Si»«
Shaft S.al: Mechanical i
Oth»n
; Typo LubH cotton 11/01 & f^
Spociol Re
uir
Step Bearing Is /Is Not
r fl b If. Head Room AvoilabU for Inttalllna Ml««f:
41
MeterioU ef Construction for Wetted Ports:
Mi«.f Meoel Ne.
Privet Supplied by
Gear Supplied fay
Motor Drlv
Mfa
rpm; Hersepewer
hp; Enclosure
NEMA From*
Volts
Phase
; Cycles
Turbine Drive: Mfgr.
Speed
rem; Horsepower
hp; Water Rete
l./hr
Inlet Steam; Pressure
piig at
Exhaust Steam; Pressure
psie- pslo et
Other;
G.or; Mfof.
; Rotie
; ACM A Rating
; Output Sp**d
Shod Ceupllna: De««rlbe
Mechenieol Seol: Describe
Stuffing Bex: Describe
Shaft: SUe
In. OP by
Length from Mounting Flonge
54
Impeller Type
; Site
In. OP; No. Bledes
; Removable from Sheft: Ye« - Ne
55
Additionot Doto:
SPECOY
CHECKED:
APP'O:
ATE.
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
ENDOH TO COMPLETE ALL INFORMATION MAflKCO
2*040 »-•!!
KOUIP>. NO.
AGITATOR OR MIXER
SPECIFICATIONS
SPEC.
NO.
-267-
-------
PLANT COC
LOCATION
?/- fyr*
J
MANUFACTURER
•7'C S/4/+ULr> if err
BLDG. NO.
NO. UNITS
0Va,/ FILE, JOB NO. 7?.er Tra/f) B/MNO.
' P. 0. NO.
FIELD ERECTED (^ES)
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
IS
19
20
21
|22
23
24
25
26
27
28
•n
X
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
MATERIALS
ZZLE SCHEDULE
z
NO |NO. UNITS / 1 TOTAL VOLUME 4-O,Ooc> GAL
Operating Pressure
Li qui d
Spvci fie Gravity
p.l,
"F
Contents Lethal
Desi gn
Design
Pr*tsur*
T*mp*ratur*
p»ig
"F
Hydrostatic Test
Shell
Shell
Code:
H.od» Corr. Allow.
H*od* Joint Eff.
psig
In.
X
&^>A1 £
Radiograph: //£>
^
/&>£}
J f3 7 t^/£/ff^f\
YM (N^
dJ-M.
2,OO
/O
Stamp Yes (ftf)
Stress Relieve: f^f O
National Board No.
Type Supports:
St/r-h
Insulation: f
Firoproonng: / c? ^>
Sandblast: fi/Q
Manhole •? Hinged fo
Plotfon
\ Paint: ' /S o
avlto<]^ Otfiar:
n Clips: NO |Lood*r Clip«:/V.O | tntul. Ring*: W&
°ipe Supports:
Wind Load:
Wt. Empty
Ite
Shell
Heads
Lining
n Thiekn*st
in*
in.
in.
in.
in.
Ib
Mat'l Clas
NonleNeoVs
Flanges
Coupling
M.H. Caver
Supports
Bolts/Studs
Nuts
Gaskets
Service
£c &&4- P&C*£a
5Cj& f-tf £ *?* fe/) ji£
•
•^
/JT^ " '' j f~)f)~
2-" /5&^" £* F^
Q'S it "
& „
£* '' *
Blinded
VESSEL SKETCH
/J-0" O O
SEt rf O' to 'fep of Cs^C
A- /
Far Further Details, See Sheet Ne.
r// - THE DOW CHEMICAL COMPANY ^Cf£> V'p'-/'"':
CHECKED:
APP'D:
DATE: "L/S/74
"""" e+TKAir,,*
REVISIONDATE A B
)«MAT10N MAHKEO
VERTICAL VESSEL
SPECIFICATIONS
C SPEC
|JIH«CT or NO.
25*40 3- en
-268-
-------
PLANT fSJSS/-
LOCATION
f^\/f
'
MANUFACTURER Dorr* o/t
/
/ ^~l C «J^£//
fC r*
•fi.fi' xr/»/
BLDG. NO.
NO. UNITS .4
^ ;'S> / FILE/JOB ^
CHARGE N
- f)rr Train B/M NO.
' P. 0. NO.
MODEL/TYPE/jb/r.'-V Dres/nf/2. '*2 2 '
i
i
3
4
_i_
6
7
8
9
10
11
M
13
14
IS
16
17
IB
19
IB
2L
11
23
14
2S_
26
27
a.
29
30_
31
32_
33_
35
36
37
33
39
40_
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
s
z
<
5
K
O
a.
ce
UJ
_i
z
*-
OPERA
DESIGN
CONSTRUCTION DETAILS
1 NOZZLE SCHEDULE
DATA ^6/V?£)
Fluid ( f^rt 1
Flow-Procan Bat
FlowFlltar Baili
Daniity
Viieoiity
PH
Solidi In Straam
•> 4-<-
i
Parti cla Sita(Avg.)
/*->/•/-?> i
Ib/hr
Ib/hr
Ib/cuft
cantipo ia
vol.%O7£f>f4,
^t/
/t>O /£o
FILTRATE/3*?. BACKWASI
2/34 o&o —
£•7 'SO?*.
'
f&o J(»o
*o- "73o £ ^ ^
3.
v^/?c.
H — CAKE £?}
2 73 GOO
Typa Diicharga: Wat Caka-Dry Caita
aparation Tlma /^ ' £ S) *£ ;
Filtar Aid Praparation Tlma
Filtaring Tima
Claoning/Bockwath Tlma
Totol Tim<
•
•
Prvcooting Tlma /
Filtar Aid Applicatian Tima
Slowdown Tima
lon-f
1
V
1'
i Batwaan Succaniva Filtar Cvclai
fnltrumantation: Monuo -S
•mi Automotic^Atitomo
^Filtar
Daiign Pranura ptig
Daiign Tamparahjra
Hydreltatie Tatt
Corr. Allow./Lln.-Shall Hi
Joint Effic-ancy-Shall Hi
Iniulotion
°F
piig
adi in.
odl ^
Elactrical Conitruction: Standard Opan
»ic}
Shall Faadar Tank
f-tf~> f) ~r~> f) IS D {/
s
Flltrata Tank Coda:
Stomp Raqu rad: Yai* No
Radiograph:
Strati Raliava:
Spacial Daiign:
National Board No.
Waatflarproof (*Explotion Proo?
Othar: . "^
Piping. Volvai. Fittingi Suppliad with Filtar to
ba in Accerdonca with:
Filtar Tank: Horiiontal - Vertical: Siia
Elamanti: Arao/Elamant
Laovai: Araa/Laof
in. IDx
iq ft; No. Raq'd ;
• a ft: No.
Elamant or Laaf Pora Siza (Avg.)
Maximum Coka Th
cknasi
In. Ton to Tan; Typa Haodi
in. IDx In. ODx in. Langth
Raq'd .-LaafHaiaht In.; L«of Spocino In.
micron i; Minimum Particla Sir. Ratainad
in: Groll Filtar Valuma aal-cu ft: Haal Vo uma
' mleronl
aal > cu ft
Pr.coot Raq'd: Yai • (NopMatariol
Filtaraid Raq'd: Yat ^No) Mot.riol
Faad Pump Furni triad by f)lL>/)f f :
Mor*
Othar Accatiotiai
(Wattad Parti)
VQS&
lrn.>a /r^ftfi i/t
Filtar
Moka
; Tyoa Saol
rfTtjj ffjnLfuf
Fabric: Mataria 3.O 4.
; Maih
Modal ; Max. Flow gom at otlg
; S.. Pump Spac No. Dtt/IV. Shftt' /VvlW
Packaaa Unit Y.a» - No: Shoo Vnamblad en Skids Yai . No' Fleer Soaea Raq'd ft x ft:
Wai^it Empty/Full
Sarvica
Inlat
Outlat
Vant
Drain
Rallaf Valva
Pranura Gaga
Quick Opan Covar
SaaNotilaSkatch
of Wot.
Mork
A
B
C
D
E
F.
G
H
J
K
' / Ib; Shipping Waight
No. Si i. R
g. Feca Typa
on Shaat No. ....
MATERIALS
Itam Thicknan Mot'lC
Filtar Haodi in.
Filtar Shall In.
Lining in.
In.
Elamanti
Laovat
M.H. Cov.r
Bohv'Studi
Null
Gaikatl
SPEC or £ Ftf THE DOW CHEMICAL COMPANY
CHECKED:
APP'Di
D*T£, Z/$/7Lf-
SERVICE
RE VISION DATE! A
l«
VENDOR TO COMPLETE ALL INFORMATION MARKED ______
I_
C SPEC
lltMIOT OF NO,
tvfl 5u..'i Jtkt}
Haight ft
Ib.
Ion Mat'l'Mlnimum Quality
^O<4-
3c4-
3
-------
PLANT
FIL E/JOB NO.
LOCATION
BLOC. NO.
CHARGE NO.
NO. UNITS /
MANUFACTURER
J~rs>> n
B'MNO.
P. 0. NO.
c
35
a n
•/IP
12
be.
Pf)
r /
34
35
HECK ED:
PP'D:
«3jP»- THE DOW CHEMICAL COMPANY
SERVICE
REVISIONDATE A
CNDOR TO COMPt-ETE ALL. INFORMATION MARKED-
2&260 3_6
• MCtT
.X I «QUI»> N
&OQ \/,/£•/
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC,
NO.
-270-
-------
PLANT /^^ /, p/n />
LOCATION '
MANUFACTURER
MODEL 4^y^-/o
1
2
3
4
~5~
6
7
8
9
10
TT
12
IT
14
15
16
17
18
19
20
21
22
23
24
"iT
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
SERVICE
ONDITIONS
U
-J
H
o
*
r-
CONSTRUC
t/>
_i
<
rr.
UJ
r-
<
X
or.
lu
£
t-
Ul
Liquid Pumped
Pumping Temperature (P.T
Specific Gravity at P.T.
Viscosity at P.T.
'ff / FILE/J
BLDG. NO. CHARG
NO. UNITS £ Off Tfft/fl B/MNO
' P.O. NO
JB NO. 7j3r3X 2 ?>
E NO.
.
NO. UNITS / ASA PUMP KJYES Cl NO ASA DESIGNATION
S/csrry
> /60 °F
/./A
CS'Cp
Vapor Pressure at P.T.
Corrosion or Erosion Factors: JStJlftf l&^&(,06 /
Ar range me nit Horixi Vert.-
Max. Capacity at P.T. / ^? ^T5^^ flr**»
Discharge Pressure
Differential Pressure
Differential Head
NPSH Available
NPSH Required (Wafer)
n Line Suction: Single - Double
Direction of Rotation Facing Pump Coupling: CW - CCW Speed: / 7* £&
Case: Design Pressure
psig Number of Stages ^hut-
Max. Allow. Working Press. psig Volumetric Efficiency at Rating
Mio QO ft.
psia <«#•<£ *'•
psi
34- "•
ft.
ft.
rpm
Off Pressure ft.
It
Split; Horiz-Vert-Barrel Impeller Type ^2&f fi
Impeller Diameter: Supplied ^ ' inches; Maximum l& ' inches;
Minimum j£> inches
Vent and Drain Tapped: Yes • No Bearings: Thrust Type
Monies Size
Suction ji *'
Discharge ^ "
Vents
Drains
Cooling H20
Water Cooling: Casing-Stu
Rating Facing Location
Radial
Type
Lubrication on Bearings; Oil - Grease
Oiler: Yes - No; Type
Coupling: Yes • No; Mfr.
Coupling Guard: Yes - No
Baseplate: Yes - No; Type
ff. Box-Beorings-Pedestal-Glond/ftone) Total Water Required:
gpm
Smothering Gland: Yes - No * Lubrication on Stuffing Box: Oil-Grease^ono fVfi tfP
Pocking: ^YeT) No; Type
Sealing Oil Cannection:^?*^ - No
H/6 f€f~
Type
Single - Doublo-lnside-Outside-Bolanced-Unbolonced
Rotary Unit
Insert
; Sea Ring ; Face Material
; Reversible: Yes - No ; Face Material
; Shaft Packing
Insert Mounting: Clamped In - "0" Ring - Press Fit
Gland
; Plain: Yes -No Throttle Bushing Carbon: Yes -No
• Other
Gland/Stuffing Box Machined & Tapped far: Dead - End Lub. - Circulating tub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes (TioJ
Weight of Pump
Weight of Driver
Cosing & Covers:
Ib; Weight of Base
Ib; Shipping Weight
3/£»
Cosing Wear Rings: 3 / &9
Impeller: ^/^
Impeller Wear Rings : &/&
Stuffing Box Bushings: /3/^>
Furnished by:
Electric Motor: Make
Enclosure
Insulation
Estimated BMP Req'd.
Ib
Ib
Shaft: £fcC /
Shaft Sleeves: .. £ / ' ^^
Lantern Rings:
Glands:
Gaskets:
; Type(Jlec. MotorJ- Steam Turbine • Other
Mounted by yfefydfi /**
SF Temp Rise °c
Frame
/"7 hp
Nominal Motor Size (Non-overloading) !L. S nP
Speed
rpm
Volts &•£•{} i Phase ^ ; Cycle THE DOW CHEMICAL. COMPANY
CHECKED: • SERVICE —
APP>D= /-firez /•£&& PcJAtF*
DATEtg/- / . REVISIONDATE A B
C 1
hp ; Speed rpm
; Max
; Max.
Ib/hr
mm - in. Hg - psia
p»l«
ating Facing Location
Page No.
I EQUIP. NO.
6OO \ P-/4*ti
CENTRIFUGAL PUMP
SPECIFICATIONS
PEC.
10.
1837004/73
-271-
-------
PLANT ff,na /• P
LOCATION '
MANUFACTURER
//
MODE L / V£ f ^ - IO
1
2
3
i
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
IT
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
Z
By
£5
mJ-
"8
INSTRUCTION DETAILS
U
"|
MATER
UJ
£
t-
UJ
/S"s TIC 5l) /tur Femora/ FILE JOBNO ??,(.
BLOC. NO. CHARGE NO.
NO. UNITS t_Qtp TrOlfl B'MNO.
' P.O. NO.
^bZ 3
NO. UNITS / ASA PUMP y O °F
Specific Gravity ol P.T. jt *j
Vapor Pressure at P.T.
S~~*\
Direction of Rotation Facing Pu
Case: Design Pressure
Max. Capacity at P.T. *7 ^} flPm
Discharge Pressure ^ C psio
Suction Pressure 2 ^> ' Plia
Differential Head ^y
NPSH Available
NPSH Required (Water)
e Suction: Single - Double
mp Coupling: CW - CCW Speed: / 7 5 O
psig Number of Stages ,-Shut-Off Pressure
Max. Allow. Working Press. pxig Volumetric Efficiency at Rating
Split; Horiz-Vert- Barrel
Impeller Diameter; Supplied
mpeller Type
^ ^Pt, inches; Maximum / O inches; Minimum {
ft.
ft.
f^ ft.
ft.
ft.
rpm
ft.
X
ff inches
Vent and Drain Tapped: Yes - No Bearings; Thrust Type
Nozzles Size R
Suction £ **
Discharge / Jr^"
Vents
Drains
Cooling H20
iting Facing Location
Radial Type
Lubrication on Bearings; Oil - Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes - No
Baseplate: Yes - No; Type
Water Cooling: Casing-Stuff. Box-Bearings-Pedestal-Gland^one) Total Water Required:
Smothering Gland: Yes - No
Pccking:{Tes}- No; Type
Mechanical Seal: Yes (No) Fu
Lubrication on Stuffing Box: Oil-Grease-None fr]/
Sealing Oil Connection: Yes - No
rnished by; ; Mfr. ' Type
gprr,
'&•/•£ f*
Single - Double-lnside-Outside-Bolanced-Unba lanced
Rotary Unit
Insert
; Sea Ring ; Face Material ; Shaft Pocking
; Reversible: Yes - No ; Face Material '
Insert Mounting: Clomped In - "0" Ring - Press Fit
Gland
; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for; Dead - End Lub. • Circulating tub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass * Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd; Yes • No
Weight of Pump
Weight of Driver
Ib; Weight of Base
Ib; Shipping Weight
Casing & Covers: ^3 /Si?
Casing Wear Rings:
Impeller:
Impeller Wear Rings:
Stuffing Box Bushings:
Furnished by :/^£> ftff /O /*
Electric Motor: Make
*
//
H
a
Ib
Ib
shaft: S fe.cz/
Shaft Sleeves: ^j Sf^*
Lantern Rings :
Glands:
Gaskets:
; Type^Elec. Motor^ Steam Turbine - Other ; Direct - Gear
Mounted by j/$ff> f)/j /) /**
Enclosure- TT^/""^ ^ Temp Rise °c
Insulation Frame
Estimated BMP Req'd.
3. 6* hP
Nominal Motor Size (Non-overloading) A* hp
Speed
Volts ^ <%.& ; Phase
Speed Reducer; Integral - Separ
rpm
£ : Cycle ^ Q
ale
Mfr. Ratio
Model Class
See Driver Specification Na.
Performance Curve: ^"»J- No; Cujve No.
Certified: Yes $3)
Hydrostatic Test:^es^- No; Pressure psig
Shop Inspection: Yes -{Nq/
SPEC. BY gpfj ^S^
CHECKED: SERVICE
APP'D: /3&SJ/
DATE: 2.f^/?tl. RE VISION D
Belt
Steam Turbine: Make Mounted by
Model:
Horsepower hp ; Speed
nlet Steam Temp., F: Normal
Water Rate:
rpm
; Max
; Max.
Ib/hr
Vacuum (If any) mm - in. Hg - psia
Back Pressure
Nozzles Size Rating Fac
Inlet
Exhaust
Serial Number
psig
ing Location
J Outline Drawing
5 Cross Section Drawing
Bulletin No. 'Page No.
THE DOW CHEMICAL. COMPANY ^f-y^
CENTRIF
SOOS> rogU)4£D/fi/6 J&A1P SPECIF
-------
=LANT C@/JL/ '- f*yr/'f"lC ^>u /f~u r AfesrJrtra,/ FILE/JOB NO. "T^syna. «i
LOCATION
MANUFACTURER
BLDG. NO. CHARGE NO. ~
NO. UNITS / per Tret/ 1 B/MNO.
' P. 0. NO.
FIELD ERECTED YES (NO)
1
•}
3
4
S
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29_
X
31
32
33
34
35
36
37
38_
39
40
41
42
43
44
45
46
47
48
49
X
51
52
53'
54
55
r-
Q
Z
0
I/I
UJ
o
MATERIALS
ZZLE SCHEDULE
o
z
Operating Pressure psig
Operating Temperature F
Liquid Specific Gravity
Contents Lethal
Design Pressure psig
Design Temperature *F
Hydrostatic Test psig
Shell Heeds Corr. Allow. in.
Shell Heads Joint Eff. %
Code: A^/^1 &
Radiograph: f/O
NO. UNITS / 1 TOTAL VOLUME / 'Q o oo CAL
cS>
Zoo
/.•a. ft&.6~~7
Yes (TNo3
2.C
•y, «TO
4.0
Stomp Yes ^fioD
Stress Relieve: MO
Nolional Board No.
Type Supports: ^. fj f» f±
Insulation: /"
Fireproofing: y £ ^
Sandblast: *A/O Paint: A/O
Manhole / Hinged (Dovlte?)
Other;
Platform Clips: A/O JLodder Clips: ft Q | Insul. Rings: /^ fc
°ipe Supports:
Wind Load:
Wt. Empty Ik
Item Thickness Mat'l Clas
Shell in.
Heads In.
Lining in.
In.
In.
NoiiloNeAs
Flanges
Coupling
M.H. Cover
Supports
Bolts/Studs
Nuts
Gaskets
Service
Jsi (BO)
ye/ >•{ (2.02.^
/5r& Ot/ffefh
/. *r
fig Cut (3z")
V
Mark No.
A /
B. /
C /
D /
E 2
F /
G
H
J
'K
L
M
N
P
0
ft
Seismic:
Wt F
s
ull of Water le
Mat'l . Minimum Ouollry
Steel
n
£&/ /dr> J& & £>4
&&/ /CJOTdL
s •/•&' BL-dL
r&r Tl C*a t
For Further De tells. See) Sheet No.
•
-------
PLANT £ptf/* /•V^V/7'c"' T
LOCATION
MANUFACTURER
(j/J-L/r f?&nn£'/O6>? ?>
HARGE NO.
/M NO.
. 0. NO.
Mounting: Portable. Permanent for Open Tank - Side Entering - (fop Entering} Bottom Entering
Type of Operation: Batch rf'Contir^u^ Operating Pressure /Lf,-f psia
Materiali to BeMived ~~"
/If.,-.- ' £ ff £, ^j_
£&iTi{,f £&rmJ'-> 5" Ittiti
Siz i i/e n i~ <* S O
/, 01. Z. £>e>
fl.faK 'l^Oo
(. 14- Z0£>
e) rtSbroiivel Crystalline* Sticky or Gummy - Lighter Fluffy
/C'& /Iff S/J f^~7^r-,£>^>f 3<£ )
^•/':>i S£ &CCJU0*~
Too Little Agitation Will ft & ~f~ //O'^-SA P /~ f /3 & /"/V '
Largest Botch or Greatest Liquid Depth:
Smallest Batch or Lowest LiquFd Depth:
Mixer Shall Be Designed to
Mixer Will - Wilkff4o~r)Be operated Whil,
Post Experience: /\/ O 1 ^.
Vessel Type: Open Top- (Closed Top
Size: 14 '- No; Describe
Dow Drawing No. t
psig; Design Temperature 'C-.f^O °F
HctlG, ; Copies Attached: Yes -f^C 1"
Motor Drive: Mfor ; Soeed rom; Hersepower / C2 O hp j Enc osure / £~ /— £*
NEMA Frame ; Volts «?- ; Phase 3 ; Cycles
& O
Turbine Drive: Mfgr. ; Speed rpm; Horsepower hp ; Water Rote Ib/hr
Inlet Steem: Pressure
Exhaust Steam: Pressure
Other:
Gear: Mfgr. ; Ratio
Shaft Coupling: Describe
psig at °r
psia. pslg at °F
; AGMA Rating , Output Speed rpm
Mechanical Seal: Describe
Stuffing Box: Describe
Shaft: Site In. OD by Length from Mounting Flonge
mpeller Type ; Size In. OD: No. Blades
Additional Doto:
SPECBY^T:^ <^> THE DOW CHEMICAL COMPANY
CHECKED: SERVICE
APP-D: tVATCZl
DATEi^/^/^*jC REVISIONDATE
Ms#TW>6irAr*e.
ABC
2S040 3-611
; Removable from Shaft: Yes • No
ICQUIF*. NO.
4-1
AGITATOR OR MIXER
SPECIFICATIONS
SPEC.
NO.
-274-
-------
PLANT/^)^/. /*/r/' Tt'C •%& Jftsr Jl?fmc>i'a/ FILE/JOB NO. 73o&f>>
LOCATION
MANUFACTURER
BLDG. NO. CHARGE NO.
NO. UNITS J Off Tfrtt*? B/MNO.
' P. 0. NO.
FIELD ERECTED f*t$)
1
2
3
4
5
6
]_
e
9
10
11
\2_
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
2B_
29
30
H
32
33
34
35
36
37
38
39
40
41
42_
43
44
45
46
47
48_
49
SO
51
52
53
54
55
<
r-
<
O
Z
0
Ul
o
MATERIALS
ZZLE SCHEDULE
2
NO NO. UNITS J (TOTAL VOLUME .^kp, C^'-'CD CAL
Op.roting Pr.ssur. P*ifl
Op.roting T.mp.rotur.
Liquid
Sp.ciftc Gravity
"F
Cont.ntt Lothol
D.sign
D.tign
Pr.sturo
Twnp.rotur*
p>ig
«F
Hydroirotic Tott p*ifl
Sholl
Sh.ll
Cod.:
H.odi Corr. Allow.
Hoodi Joint Ell.
In.
K
4 5/tf £
Rodiogroph:
//o
d7
/ , 2.00
(Slut r /)_/./ (R?
Strati Koliavo: //O
Notionol Boord No.
Typ. Supportc . 5^/*~">
IntuloHon: / »
Fir^>reoftn«: Y€^
Sondblost; f*Sc
Monhol. 2. Hlng.d (
Plot (on
"o,
Point: A^O
i^ToTj Othof;
m Clipt: /Vs
n.
n.
n.
n.
n.
Nozzl.Nodi t
Ib
Mot'l Chi
^
Flangot
Coupling
M.H. Cov.f
Support!
Boltt/Studi
Nut>
Ga>kot>
5,
rvie.
(?Q.MG In(&?
X3^7 1'-faffx*
Y4m~fZf*?\
/^ 7"
fliJ Wftftt )
Hi/ft (dd)
•Noitl
Marli
A
B
C
D
E
F
G
H
J
K
L
M
N
P
0
R
i to bo Plugg.d or B
SPEC.BY
3>O4~
3& 4-
*x?4. p&dea
$/*>&. £&.C£ct
Sf&t*/
Siza Rating Faea Typa
® TO/VKtfeJfr £>Of>
O * " ~JGO~
Z" 150* f^f-
2. »i li "
&" M "
£- •> i
indad
VESSEL SKETCH
/4-*?'/ £) i o rr) &J- e. r
/&* rfo "fo£ o i £os> c~
For Furlhor Octal) •. Jo« Shoot No.
•<^- THE DOW CHEMICAL COMPANY JO0 1 ^"/"°'
. . . . \/crDTi/*Ai v/cccci
?^//l J~J^ ' i& r\sJ&*5Jr 7^(3 A/^^ IwAL. VCOJCL.
SPECIFICATIONS
DATE: i/J/7<£ MEVISIONDATE A • 1 C SPEC
-275-
-------
PLANT /V,
LOCATION
MANUFACTURER
MODEL/TYPE /i
1
2
3
4
_5_
6_
7
8
9
10
11
12
13
14
J5_
16
17
18
19
20
21
22
23
24
25
U
27
28
29
30
31
32
33
34
35
36
37
38_
39
40
41_
42_
43
44_
45
46_
47
48_
49
50
51
52
53
4
55
B
Z
<
2
a:
o
u.
CL
LU
_J
2
t-
OPERA
o
1/1
UJ
Q
CONSTRUCTION DETAILS
:HEDULE
\st
UJ
_l
N
z
rf/~
fart
3/t7S\
/-^v
-- £v
'S*S +SC ±>
' t' Pf '"*
/ 2>r£//r)f/2.'t'2mt
DATA
fame. ")
Fluid
Flow-Process Bos
is
Flow-Filter Basis
Density
Viscosity
Ib/hr
Ib/hr
Ib/cu ft
eentipoise
PH
Solids in
Stream
Particle SixefAvg.)
Normal
Normal
vol.!S(wt^l
microns
Max. Oper, Press. p»ig
Max. Oper. Temp
. °F
Allowable Pressure Drop psl
Maximum
Coke Vo
ume:
BLDG. NO.
NO. UNITS
^fs-ns
4 />
/
P/) NO. UNITS OPERATING
FEED-'£:30
lisa,/ FILE/JOB NO. 7 Z-f £• '/ •*> \
CHARGE NO.
ft' Tff't tl B /M N 0.
P. 0. NO.
4. SPARES MDrte.
FILTRAT612 8ACKWASH/S.7) CAKE/fiiJ
5/c/rf'/
54.C. ooo
/« iSSfafj/l*
4-O
0 -JLOO
~5f /"ffffe.^} ' ^o1fr ' £&<%.f
25'5^coo $D Qoo 2-7^>/7^f
/, O -/ ir>»2/ /•05p'>As
Type Discharge: Wet Coke(&ry Coke,'
Cycle: Precoat Preparation Time rv & *O ^
Filter Aid
Preparation Time
Filtering Time
Cleaning/Backwash Time
Total Time Betwe
; Precooti
; Filter A
ng Time ,^^OX7*2-
d Application Time
; Slowdown Time 1r -
' IT
in Successive Filter Cycles C^£
?/7 // n
Instrumentation; Monua -Semi Automatic- Automatic
Design P
Design T
ressure
emp era Hire
Hydrostatic Test
Corr. Aliow./Lin.-
Jotnt Eff
Shell H
ciency-Shall H
Filter
psig
°F
psig
lads in.
tods S
Insulation
Electrica
Construction: Standard Open
Shell Feeder Tank
Filtrate Tank Code:
Stamp Required: Yes- No
Radiograph:
Weatherproof
Stress Relieve:
Special Design:
National Board No.
(*~Explosion ProoC
Other: ' "'~
Piping, Valves, Fitttnos Supplied with Fi ter to
be in Accordance with:
Filter Tank: Horizontal - Vertical; Size
Elements
L eaves:
Area/Element
Area/Leaf
Element or Leaf Pore Si ze
Maximum
sq ft;
sq ft; No.
(Avg.)
Cake Thickness
Precoat Req'd: Yes - tf3pi
Filteraid
Req'd: Yes -CNo]
Material
) Material
Feed Pump Furnished by /}j/Jt/) £r ;
Other Act
Mot1
e stories
(Watted
Ports)
fflb.K'/Jro'fr
in.
No. Req'd
Req'd
IDx
In. Ton to Tan; Type Heads
n. IDx in. ODx in. Length
: Leof Height in.; Leof Spacing in.
microns; Minimum Particle Si te Retained -microns
in: Gross Filter Vo
lume
Filter Fabric:
Make
; Typo Sea
dMjrtJ} PfC't
; Model
aal-eu ft: Heel Volume . aal • cu ft
Material 3 £><4- ; Mesh
; Max. Flow gpm at osia
; See Pump Spec No.
>i>/'f*Jbt)->ai>A/~£i#>/'(.>t;fitrt/l
_j
MATERI
Item
Thickness Mat'l Class Mot'l- Minimum Quality .
Filter Heads in. "Z>C4—
Filter Sh
L ining
ell in. ^CXL
in. ^O4-
in. .
Elements
Leaves
M.H. Covet
Bolls.'Sruds
Nuts
Gaskets
SPEC.BY^Vrr/V' -*3£». THE DOW CHEMICAL COMPANY gO0 \ ^'/X°A
CHECKED:
APP'D:
DATEt ~*-/&/7y
SERVICE
REVISIONDATE A
a
FILTER
SPECIFICATIONS
C SPEC.
2»«0 1-01
-276-
-------
itst •>
-------
PLANT s^ssa / - /Vy*
LOCATION
MANUFACTURER
/ ft c. StL/J'is/' ^p/TUPfa/ FIL
BLDG. NO. CHA
NO. UNITS 2. £&r'ff&'/? B/M
P.O
MODEL 4/6
1
2
3
4
5
6
7
8
9
10
TT
12
13
14
15
16
17
IB
19
20
21
22
23
24
25
26
27
28
25
30
31
32
33
34
35
36
37
38
39
40
41
42
-43
44
45.
46
47
48
49
50
51
52
53
54
55
UJZ
£5
u
1
o
Z
o
l~
o
CONSTR
./>
a
UJ
H-
-fc
UJ
tt
r-
LU
~/3 NO. UNITS ASA PUMP 5CYES C~
Liquid Pumped £ /L* Tr^
Pumping Temperature (P.T,) 21 OO °^
Specific Gravity at P.T.
Viscosity at P.T.
/. y^r
ct-cp
Vapor Pressure at P.T,
Corrosion or Erosion Factors: £fi& / ^/C^r^~^
E/JOB NO. 73&6Z 3
RGE NO.
NO.
NO.
NO ASA DESIGNATION
Max. Capacity ot P.T, /&O^& flPm
Discharge Pressure
Suction Pressure
Differential Pressure
Differential Head
NPSH Available
NPSH Required (Water)
p»'» 73 ft.
psia 4^/3 'f'
psi
Z5 "•
ft.
ft.
Arrangementrtoon^-Vert.-ln Lire Suction^SingTe^- Double
Direction of Rotation Facing Pump Coupling: CW - CCW Speed: //£/6s>
Impeller Wear Rings: £ / &>
Stuffing Box Bushings: 3 / &>
Furnished by: Y& f}O&f
Electric Motor: Moke
Vent & Drain
Ib
Ib
Shaft: Sfc<= /
Shaft Sleeves: 3 / &>
Lantern Rings:
Glands:
Gaskets:
: Typetlec. MotorJ. Steom Turbine - Other
Mounted by ^SjlCtOf
Enclosure / & £~£ ^F Temp Rise °c
Insulation Frame
Estimated 3HP Req'd.
Nominal Motor Size (Non-over
Speed / fJ5&
Volts d. A O ' Phase
2.O hp
oading) 25" hP
rpm
_3 ; Cycle ^^
Mfr. Ratio
Model Class'
See Driver Specification No.
Certified: Yes <
ED
Hydrostatic Test: O»O- No; Pressure psig
Shop Inspection: Yes -^lo^
SPEC. BY gFfJ ^^^
CHECKED: SERVICE
OATE: 2./£/7 4- REVISIOND/
Steam Turbine: Make '
(Direct/ Gear . Belt
Mounted by
Model:
Horsepower
Inlet Steam Press., psig: Normal
nlet Steam Temp., °F; Normal
Water Rate:
Vacuum (If any)
Bock Pressure
Noziles Size
Inlet
Exhaust
hp ; Speed rpm
; Max
; Max.
Ib/hr
mm - in. Hg - psia
psig
Rating Facing Location
Serial Number
J Outline Drawing
y Cross Section Drawing
Bulletin No.
THE DOW CHEMICAL. COMPANY
•LTee F££D *>»•*
TE A B
c
Page No.
600 \ P-TA4&
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
18370D4/73
-278-
-------
PLANT {faa./- /•fys'j /•/'£ r^fj/fes/* J(*0sn0Mdr/ FILE/
LOCATION '
MANUFACTURER
MODEL 3*4-G
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
To"
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
«o
7
SERVICE
CONDITIO
DETAIL
3
»-
a
H
t/>
r
u
MATERIALS
o:
UJ
>
or
O
r-
\U ,
BLDG. NO. CHAR
NO. UNITST, p#r Train B/MN
' P.O. 1-
JOB NO. 7306 2 *)
GE NO.
0.
40.
NO. UNITS ASA PUMP >C YES d NO ASA DESIGNATION
Liquid Pumped /i^f-, ^> /•*•/£. /£/?rrM± St//faff
2. e>a °F
Specific Grovity at P,T. /m f) ^
Viscosity at P.T.
cs-cp
Vapor Pressure at P.T.
Corrotion or Erosion Factors;
Arrongement^horiz^/ert..|n Lin*
Max. Capacity at P.T. *5"^PC^ *^m
Discharge Pressure
Suction Pressure
P«i« . ' ft.
psio «4O **'
Differential Pressure psi 7d
Differential Head
NPSH Available
3cO '*•
ft.
NPSH Required (Water It.
$uction;(bingl^ Double
Direction of Rotation Facing Pump Coupling: CW - CCW Speed: / *7 &Q
Case: Design Pressure
Max. Allow. Working press.
Split; Horiz-Vert-Barrel
Impeller Diameter: Supplied
Vent and Drain Tapped: Yes - No
Nozzles Size Rating
Suction £ i1'
Discharge Qtf
Vents
Drains
Cooling HaO
rpm
psig Number of Stages / ; Shu (-Off Pressure ft.
P«ig , Volumetric Efficiency at Rating
Impeller Type
X
^ inches; Maximum & ~t/i? inches; Minimum ^ inches
Bearings: Thrust ,
Facing Location
Radial
Type
Type
Lubrication on Bearings; Oil - Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes - No
Baseplate: Yes - No; Type
Water Cooling: Casing-Stuff. Box-Bearings-Pedestal-Gle:nd{None^ Total Water Required:
Smothering Gland: Yes - No
Pocking: Yes ^jj? Type
Mechanical Seal: /77>>- No; Furnished
gpm
Lubrication on Stuffing Box: Oil~Gr*ose-None M/& f~C f*
Sealing Oil Connection: rfes> No
by;/^a/i^^/* 'Mfr-
Type
Single - Double-lnside-Outside-Balanced-Unbolanced
Rotary Unit ; Seal Ring . ; Face Material
; Shaft Packing
Insert , Reversible: Yes - No ; Face Material
Insert Mounting; Clamped In - "0" Ring - Press Fit
Gland , Plain: Yes -No Throttle Bushing Carbon; Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for: Dead - End Lub. - Circulating Lub. - Quenching - Vent &VDroin
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing BOX R*q'd: Yes -No
Weight of Pump
Weight of Driver
Ib; Weight of Base
|b; Shipping Weight
Cosing & Covers: ' &/&&
Casing Wear Rings: H
Impeller:
*••*
Impeller Wear Rings: *f
Stuffing Box Bushings: _f._- __
Ib
Ib
Shaft: fc^JrV? ft f
Shaft Sleeves: J3 / <^J
Lantern Rings:
Glands:
Gaskets:
Furnished by; (/& f) jf/}/* ', TypeiEJec. MotoD- Steam Turbine - Other
Electric Motor; Make Mounted by V &flj$ Gf*
Enclosure 7*Cr r^Ci* ' ^
Temp Rise °£
Insulation Frame
Estimated BMP Req'd.
^C-/*O hp
Nominal Motor Size (Non-overloading) /*.f nP
Speed / ' *7 '£ £?
Volts 4-4& ' phas- 3
rpm
; Cycle ^ ^
Spe*d Reducer; Integral - Separate
Mfr. Ratio
Model ' Class
See Driver Specification No.
Certified: Yes ^No^
Hydrostatic Test; t^es}- No; Pressure
psig
Shop Inspection: Yes CN°7
Steam Turbine: Moke
lreet) Gear - Belt
Mounted by
Model:
Horsepower
fnlet Steam Press., psig: Normal
Inlet Steam Temp., F; Norma
Water Rote:
Vacuum (If any)
Bock Pressure
Nozzles Size
Inlet
Exhaust
hp ; Speed rpm
; Max
; Max.
Ib/hr
mm - in. Hg • psio
psiu
Rating Facing Location
Serial Number
!_,' Outline Drawing
5 Cross Section Drawing
Bulletin No.
SPEC. BY ^CT^xT// <3^t> THE DOW CHEMICAL. COMPANY
CHECKED: SERVICE
APP'Dt jt)^/ J^VO/
-» XHe#*XOM* PUHP
DATE! ^2/S'/7^~ REVISION DATE 1 A 1 B
C
»RKED tuc.T or
Page No.
I EQUIP. NQV-
Boa \ P'TJMt.
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
18370D 4/73
-279-
-------
LOCATION
C*oa/-
/
MANUFACTURER
FIELD ERECTED YES (\.
1
2
3
4
5
6
7
a
9
10
11
12
13
14
15
16
17
18
119
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
m
52
53
54
155
DESIGN DATA
MATERIALS
NOZZLE SCHEDULE
Operet
Liquid
ng Pre.sure
Spec! fi c Gravity
CV/*/ .//^ C>£J/*ftsr f?€mcya/ FILE/JOB NO. -yzft. £3 -^
' BLOC. NO. CHARGE NO.
NO. UNITS / Off 7~rc7/n B/MNO.
' . P. 0. NO.
iO> NO. UNITS l/sre?/'? 1 TOTAL VOLUME /O*OOO GAL
psig
"F
Contents Lethal
psig
eF
Hydrostatic Test
Shell
Shell
Cade:
Heads Corr. Allow.
psig
in.
Heads Joint Eff. %
AS:M E
Radiograph: /VQ
O
2.00
I,O 4 £>.6~7
Yes (^o^)
2-^T
2,^0
4-O
Stamp Yes CgcJ
Stress Relieve: .A/tO
National Board No.
Type Supports: ^ fj Q. g\
Insulation:
Firep roofing:
Sandblast: /V/D
Manhal
Plotter
» / Hinged f^
/**
x«s
I Point: S*/O
avitov Other
•n Clips: ffQ {Ladder Clips: Ji/Q Insul. Rings: \f&£
Dipe Supports:
Wind Load:
Wt. Empty
Item Thickness
Shell
Heads
Lining
in.
in.
in.
in.
in.
Ib
Mafl Clas
NotileNedts
Flange*
Coupling
M.H. Cover
Supports
Bolts/Stvdi
Nuts
Gaskets
Servi ee
Ttl/r'f £4- 2-
f;r~fffitJi~(?>y\
*
AT
Aa £k/J( 4£)
AffS?Jl£ )£.
•Nonle
Mark
A
B
C
D
E
F
G
H
J
K
L
M
N
P
0
R
to be Plugged or
SPEC. BY £ r/=//
CHECKED:
APP'O:
DATE: 2/6/74
Nt>.
/
(
1
I <
2
/
/ ,
Seismic:
Wt Full of Water Ib
s Mat'l . Minimum Quality
•SY*?* f
'1
£*£/'/ £o Xt? Ja4-
t
C<£t f£& ?£. b 4- jLi'nctf
'f ' ' F**£Jf'A.
M&fi -f
L£. 'li 'Cote. pSK^fJ
s~f *•*• /
Size Rating Face Type
£t H /'
& " " "
<•// // '/
£,>• * <>
&r &£''*' "
Blinded
•el
VESSEL SKETCH
f~ & D f-/&&c/$
y&r-fa c,& /
For Further Details, See Sheet No.
(3j>- THE DOW CHEMICAL COMPANY /?r>/~> 1 L?-'/ "°
D/=<"AtJT£rje> VERTICAL VESSEL
^ "' ' C "~ SPECIFICATIONS
REVISIONOATE ABC SPEC.
-280-
-------
PLANT
Su/i-ur
FILE/JOB NO.
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
7**
NO. UNITS
B-'M NO.
P. 0. NO.
12
13
14
We nlr
. SO
/13. SO
0.01-
3
O.OQ
0,01
IS. 10
D.
?. /
•rr~ots/'afe
Coo/
f3 tn/ncrS /oO
iPECDY
IHECKEO:
.PP'D:
>ATEi
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
•ENDOR TO COMPLETE ALL INFORMATION MARKED
2&2AO I -*»
IQUIP. MO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO.
-281-
-------
'LANT
FILE/JOB NO.
.OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
P. 0. NO.
cfit:
a* S /-<»xvg er- 35r*r-
c a /
c. g 2.15 f-f-
13
34
KECKED:
PP'O:
E: Z/S/74.
THE DOW CHEMICAL COMPANY
SERVICE
RE VISION DATE
ENDOR TO COMPLETE ALL INFORMATION MARKED
25260 3-6
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC,
NO.
-282-
-------
'I ANT
FILE/JOB
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/MNO.
P. 0. NO.
34
SPEC, or
ZHECKEOi
kPP'D:
THE DOW CHEMICAL COMPANY
SERVICE
RE VISION DATE A
•HKKT Of
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
25260 3-t
-283-
-------
fHE-JOB
.OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS /
7~rrjf
B/M NO.
P. 0. NO.
12
15
25"'
32
33
34
35
48
49
50
SPEC. BY
MECKEO:
PP'O:
THE DOW CHEMICAL COMPANY
SERVICE
Tc
REVISION DATE A
bNOON TO COMPLETE ALL INFORMATION MARKED
(QUIP. *O.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
-284-
-------
FILE/JOB
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS / p^f- 77/7//?
B/M NO.
P. 0. NO.
£>& r
47
48
SPEC BY
IHECKEDi
,PP'0:
)ATEi
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
.•ENDOX TO COMPLETE ALL INFORMATION MARKED
10200 »-••
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC,
NO.
-285-
-------
PLANT ^* eyy/- J-
LOCATION
MANUFACTURER
MODEL
1
2
3
4
b
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
~73~
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
5*
55
t/i
Z
ur
£o
u
-J
H
O
^
H
Z
o
u
"i
a
tu
r-
3
Hi
tt
tu
Liquid Pumped
-^//V?
/
he ^>e.
1 i !•%_
//y i.'f*
<^
Viscosity ot P.T.
°F
Cl-Cp
Corrosion or Erosion Factors :
Arrongement{_Horij^)-Vert.-(n Line
Direction of Rotation Focin
Max. Capacity at P.T. /^^ gpn>
Discharge Pressure psio ^ C^ **'
Suction Pressure psia 4^ *'•
Differential Pressure P*' '
Differential Head ^ ^ ft.
NPSH Available ft.
NPSH Required (Water) ft.
' Suction^Single^- Double
g Pump Coupling: CW . CCW Speed: 17 SO 'P™
Max. Allow. Working Press.
P«
19 Number of Stages / ;Shuf-0'f Pressure ft.
psig Volumetric Efficiency at Rating %
Split: Horiz-Vert-Borrel
Impeller Diameter; Supplied
Impeller Type
£ inches; Maximum (0 T~? inches; Minimum ^ ~ inches
Vent and Drain Tapped: Yes - No
Nozzles
Suction
Discharge
Vents
Drains
Cooling HzO
Water Cooling;
Size
/7i"
/"
Rating
Facing
Bearings: Thrust ^XP«
Location
Radio Typ*
Lubrication on Bearings; 0' - Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes * No
Baseplate: Yes - No; Type
Cosing-Stuff. Box>Bearings>Pedestal-Gland-Nonv Total Water Required: OP*
Smothering Gland: Yes - No
Packing: Yes •
Mechanical Seal
No; Type
: jfeT)- No
; Furnished
by; Vf>rtf
Lubrication on Stuffing Box: Oil-Grease-None
Sealing Oil Connection; Yes - No
icr* •• ™''- T/P«
Single • Double-|nside>Out«ide-Balonced-Unbolanced
Rotary LJn
insert
it
; Seo Ring
; Face Material . ; Shaft Packing
; Reversible: Yes • No ; Face Material
Insert Mounting: Clamped In • "0" Ring
Gland
- Press Fit
; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for; Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with D
scharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes - No
Weight of Pump
Weight of Driver
Casing & Covers:
Casing Wear Rings:
Impeller;
Ib; Weight of Base Ib
Ib; Shipping Weight Ib
DUCJ-} /£ Jtr/~<>
//
//
Impeller Wear Rings: *'
Stuffing Box Bushings: ty
Furnished by:'y
Shaft: ,5/«£ *tft /
Shaft Sleeves: flJ G /?C.
Lantern Rings :
Glands:
Gaskets:
/£?f)0t)r ; TypefMec. Motor} Steam Turbine - Other ; Direct - Gear . Belt
Electric Motor: Make
Enclosure "J
Insulation
-£H\/
Mounted by //Vj/XVV
SF
Frame
Temp Rise °c
Estimated BHP Req'd. ^ j
Nominal Motor Size (Non. overloading)
Speed
Volts 1-m {
Speed Reducer:
Mfr.
Model
J ; Phase «9j
; H3 <
1 hp
/ hp
rpm
5 &
Integral - Separate
Ratio
Class
Sec Driver Specification No.
..: (f.?.
Certified:
Shop Inspection
SPEC. BY fZZ C- ti
CHECKED:
APP'D:
DATE: 2/?/7^
VENDOR TO COMPLETE
Yes £NJ
psig
Yes THE DOW
SERVICE
t?///ey*t"
RE VISION DATE /
, /^ ^^^
k
ALL INFORMATION MARKED
Steam Turbine: Moke Mounted by
Model:
Horsepower hp ; Speed rpm
tnlet Steam Press., psig: Normal ; Max
nlet Steam Temp., F; Normal .' Max.
Water Rate: Ib 4u
Vacuum (If any) mm - in. Hq - psio
Back Pressure psig
Inlet
Exhaust
Serial Number
J Outline Drawing
2 Cross Section Drawing
Bulletin No. Page No.
CHEMICAL. COMPANY e7>^ 1 J§u"/^/<
/ <_ C - 1 ' / fT^Lj
L&TfCrt ptswp CENTRIFUGAL PUMP
SPECIFICATIONS
B
C SPEC.
JJSHCCT OF NO.
1B370D 4/73
-286-
-------
PLANT COAL- py^/Tic
LOCATION
MANUFACTURER
MODEL 3 / /^ - /Q
1
2
3
4
~r
6
7
8
9
10
'11
12
13
14
15
16
~
18
19
20
21
22
23
24
25
26
27
28
"29~
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44.
~4S
46
47
48
49
50
51
52
53
54
55
SERVICE
CONDITIONS
3
»-
O
«
t—
z
u
_J
MATER
DRIVER
*/>
r-
UJ
t-
Liquid Pumped *5£2^%> ^jffs} /~S)
Pumping Temperature (P.T. y^,
$Z3
GE NO.
0.
MO.
NO. UNITS ASA PUMP C^YES O NO ASA DESIGNATION
Ses/Sciate.
rn£>/£-T+~ °F
Specific Gravity at P.T. /, O
Viscosity at P.T.
cs-cp
Vapor Pressure at P.T.
Corrosion or Erosion Factors:
Arrangementt^Horiz^Vert.-ln Line
Max. Capacity ot P.T.
Discharge Pressure
Suction Pressure
Differential Pressure
Differential Head
NPSH Available
NPSH Required (Water)
Suction:(Sing e) Double
/GO «P">
P»i" Q O ft.
psia SL. ft.
psi
7S '*•
ft.
ft.
Direction of Rotation Facing Pump Coupling: CW - CCW Speed: / 75 & '*m
Cose: Design Pressure
Max. Allow. Working Press.
Split: Horiz-Vert-Borrel
psig Number of Stages ;Shut-Off Pressure ft.
psig Volumetric Efficiency ot Rating
Impeller Type
X
Impeller Diameter: Supplied ^f ' I** inches; Maximum / ^2 inches; Minimum ^f inches
Vent and Drain Topped: Yes - No
Suction ^
Discharge / /}*
Vents
Drains
Cooling H20
Bearings: Thrust
Radial
Type
Type
Lubrication on Bearings; Oil -C^reosfJ
Oiler: Yes /Ro) Type
Coupling t^V e^) - No; Mfr.
Coupling Guard:ffVs^- No
Baseplare:CYes)- No; Type
Water Cooling: Casing-Stuff. Box-Bearings-Pedestal-Glond^None) Total Water Required:
Smothering Gland: Yes (fto)
Packing: Yes - No; Type
gpm
Lubrication on Stuffing Box: Oil-Greose^lone^
Sealing Oil Connection: Yes - No
Mechanical Seal: (7e»3 No; Furnished by; ^p fjd& f ; Mfr.
Type
Single - Doublo-lnsido-Outside-Balanced-Unba lanced
Rotary Unit ; Seal Ring ; Face Material •
Insert ; R
Insert Mounting: Clamped In
sversible: Yes - No ; Face Material
• "0" Ring - Press Fit
; Shaft Packing
Gland ; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for: Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes
Weight of Pump
Weight of Driver
-No
Ib; Weight of Base
tb; Shipping Weight
Casing & Covers: • f}ur "rllf J^fG *~}
Cosing Wear Rings: ''
Impeller: "
Impeller Wear Rings: f
Stuffing Box Bushings: '/
ti
/•/
//
«/
Ib
Ib
shaft: 5Y«?«r/
Shaft Sleeves:
Lantern Rings:
Glands :
Gaskets:
Furnished ^y: f£f~)&&f° ; TypefElec. Motor) Steam Turbine • Other
Electric Motor: Make Mounted by^^/^^JJ f
Enclosure' SF
Temp Rise °c
Insulation Frame
Estimated BHP Req'd.
Nominal Motor Size (Non-overloading)
Speed / ?£
Volts 4-4 O • Phase 3
4- »-p
J» hp
^^ rpm
; Cycle &O
Speed Reducer: Integral - Separate
Mfr. . Ratio
Model Class
See Driver Specification No.
Performance Curve: v*0~ ^°' Cu^yo No.
Certified: Yes vNfi)
Hydrostatic Test; Yes - No; Pressure
psig
Shop Inspection: Yes -frT|
Steam Turbine: Moke
; Direct - Gear - Belt
Mounted by
Model:
Horsepower
Inlet Steam Press., psig: Normal
Inlet Steam Temp., °F: Nor mo
Water Rate:
Vacuum (If any)
Back Pressure
Nozrles Size
Inlet
Exhaust
Serial Number
ij Outline Drawing
hp ; Speed rpm
; Mo,
; Max.
Ib/hr
mm - in. Hg - psio
psig
Rating Facing Location
y Cross Section Drawing
Bulletin No.
SPECBY£Frtf- <3fj£t> THE DOW CHEMICAL COMPANY
CHECKED: SERVICE
£ZfA//)fjP
APP'D: *-" /V*^*. .">
°ATE: S/llo/74- REVISIONDATE 1 4
9 tSfi/LO*iDW6 P&Mf>
B
c |
VENDOR TO COMPLCTC ALL INFORMATION MARKED If.urvT Av
Page No.
Joo \ P2A& &
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
183700 4/73
-287-
-------
PLANT £.001- PJri //C, ^tJ/fesf f£ £ ^
LOCATION BLDG. NO. CHARGE NO.
MANUFACTURER NO. UNITS B/M NO.
P. 0. NO.
FIELD ERECTED YES Xy /?.' ^/ g J 'fi
Liquid Specific Gravity /. O
Contents Lethal Yes /No^J
Des. Press.- Positive Vacuum O in. HzOJ ^ ol
Design Temperoture °F ^i7~)2>^ & Sj*
Hydrostatic Test in. HjO £-£S/f fr'U'' '
Flanges "
Couoltno
M.H. Cover
Supports
Bolts/Studs
Nuts
Gaskets
Service Mark No. Size Rating Face Type
Manhdc* A / 18" .2.5* £F
1n/&-f' B J ^5 /&& £F
C..;f/r+ C / 2," "
^ ni- D / 4." " "
E
F
G
H
j
K
L
M
N
P
• Nozzle to be Plugged or Blinded.
VESSEL SKETCH
*t
For Further Detail
r
^
/
D ^
*, See Sheet No.
SPECBY ^r/C/y <35> THE DOW CHEMICAL COMPANY
THF
CKED: SERVIC«,./^^>=>
-------
PLANT COfi-/'
LOCATION
MANUFACTURER
/"V/V //C Sf/f-ftJl £f*i~i)fi S<* / FILE/ JOB NO. ?*,* £? •*>
BLOC. NO. CHARGE NO.
NO. UNITS / tJfr Tjrfi'si B/MNO.
P. 0. NO.
FIELD ERECTED YES
1
2
3
4
5
6
7
8
9
10
n
12
13
14
IS
16
17
18
19
20
21
22_
23
24
25
26
27
28
29
30_
32~
33
34
35
36_
37
38_
39
40
42~
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
MATERIALS
NOZZLE SCHEDULE
Oparoting Prassura
(N
Q) NO. UNITS 1 0*r Tf#l'r> I TOTAL VOLUME /OOO GAL
psig
°F
Liquid Spaciftc Gravity
Contants Lathol
Dasign Prassura
Dasign Tamparotura
psig
°F
Hydrostatic Tast
Shall Haods Corr. Alia
Shall Haads Joint Efl.
w.
prig
in.
X
Coda: A-SM &
Radiograph: f^O
O
2.0 O
t.o * o. <. -7
Yas fR?
z<£
'iSo
4-O
Stomp Yas fNo)
Strass Rallava: /J &
National Board No.
Typa Supports: •£•£*• £) £>
Insulation: / '
Firap mating:
Sandblast: NO
ManholaA/0 Hingad
/tf ^
Paint: //O
DavltaJ Orhar:
Platform Clips: ^\Q JLoddar Clips: JJ £ | Insul. Rings: \f f ^
Dipa Supports:
Wind Load:
Wt. Empty
Itam Thicknrss
Shall in.
Haads in.
Lining In.
In.
In.
No ill • Nadu
Ib
Mofl Cloi
Flangas
Coupling
M.H. Cevar
Supports
Bolts/Studs
Nuts
Goskats
Sarvica _
J^nlft"(4S)
/.£> . • '
l&sti '( ' Z&5}
£'1
Vet) \6tfH 5fh
Aa • Gtr+fSl}
v
Mark
A
B
C
D
E
F
G
H
J
K
L
M
N
P
0
R
M>.
/
/
/
/ t
Saismic:
Wt Full of Watar 1.
s Mofl . Minimum Ouollty
5lf*l'
V
&2J/£0fa. 6>4-
1?j /sif feb4- t-tfl fd
MCsj£^
Ce.i/c.o n* fa4- ftft^^L
^•/«r»r /
Slia Rating Faca Typa
4' 15(3 FF
£," // H
?u ft ' fi
?„ // '•
gil t, "
£•> tt /•
•Nozila to ba Pluggad or Blindad
SPEC, BY J~ C d
CHECKED:
APP'Oi
•4
VESSEL SKETCH
^ Y~ f"l' C^> /
For Furthar Datails. Saa Shaat Na.
Cjjl> THE DOW CHEMICAL COMPANY
-------
PLANT
T/C
FILE/JOB NO.
LOCATION
BLOG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO,
P. 0. NO.
10
13
14
15
650'
Tf>H>
16
ir
20
21
22
23
24
25
26
27
2B
7 .'-v
\J
29
A -
30
31
32
33
34
JOCS
^ X 3 5g
35
>-' r y'
36
7?
37
38
39
40
41
42
43
44
45
46
47
48
49
50
PEC.
HECKED:
PP'D:
ATE. I//5/74.
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE
W74-
ENOOR TO COMPLETE ALL INFORMATION MARKED
2B260 3-OB
CO.UIP. NO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC,
NO.
-290-
-------
PL ANT
- /y>-v -
FILE/JOB NO.
LOCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NCL.UNITS
B.'M NO.
P. 0. NO.
Mounting: Portable . Permonent hr Open Tonk • Side Enuring - Top Entering . Bottom Enterino
Type of Operotton: Botch - Continuous
Operating Pressure
pi 10
Operating Temperature °F
Materials te B. MU.d
Slot*
Lbp»f.
Viscosity . ep
Spec. Gray.
/
75 7s*/
Final Mixture
Solids Present Are; Soluble .(insoluble; ("AbroslveN Crystalline- Sticky er Gummy • Lighter Fluffy
12
PortleU Sli« er Si«v» Aiolyiii:
13
S«ttling Rot» et Solids:
FpominQ Tondoncy af Mlitturo: Low - Modium - High
/Vo
of Agttotlent Blond • Pissolv* - Dtip»r«« Gos-CSu»p»nd Solid»V H«ot Trentfef- EmulMfy
Toe Much Apilotion Will
19
Tee UlttU Ajltotien Will
Lorg»»t Batch er Gr«ot«it liquid D«pth:
SitiolU»t Botch or Lew««t LlquTd D«pttl:
Ml«er Shall BeDesigned te
Mixer Will -ftVill NoTlB. operated While Filling er Drawing Off
In
Mlnutoi
Post E»pori•no:
losod TopS Horiiontol XV.rticoU API Tank • Olti«f!-
Vossol Typo: Op»n Top
In. Straight SI da or
2:1 S*ml Elllntlcal . Can*
Flanged & DishedN 2:1 Semi Elliptical - Cone
Vessel Con Be Altered: -Yes j No; Describe
pslg; Design Temperature 2- 5&
Copies Attoehad; Yet
33
SI le of Opening for Impeller Installation
Site of Naiile for Mounting Agitator 12."
34
Selected Mpunting Flonge for Agitotar; Site /?" ; Raring 150* ; Facing
35
Location of Mounting Flonge: A £>
Baffles: No.
Width
In.; Lenflth
In.; Horliontol. Vertical; Other:
Stabllliing Ring Is - Is Not Required; Size
Short S»ol:CM»chonlcol> Packing • Other
; Type Lubd cation
Special Requirements;
Step Bearing Is |P«mil»ilbl»
Hood Room Aval I able for Installing Mixer
Moterlels'of Construction far Wetted Partt;
42
Mixer Model No.
Driver Supplied
Gear
43
Motor Drl ve; Mfof.
Speed
Enclo
NEMA From*
Volt,
; Pho.*>
___; Cyel»»
Turbine Drive: Mfgr.
; Speed
rpm; Horsepower
hp; Water Rote
Ib/hr
Inlet Steam; Pressure
pslg at
47
Enhoust Steam; Pressure
pslo. pslg at
48
Other;
Gear: Mfgr.
: Ratio
; AGMA Rating
: Output Speod
Shaft Coupling; Describe
51
Mechanical Seal: Describe
52
SluHino Ben: Describe
Shaft: Slie
In, OD by
Length from Mounting Range
Impeller: Type
; Site
In. OD; No. Blades
; Removable from Shoft; Yes • No
111 1 Additional Data:
SPEC.BV
XECKEDt
APPDi
ATEi
THE DOW CHEMICAL COMPANY
SERVICE
REVISIONOATE A
ENDOH TO COMPLETE ALL INFORMATION MARKED
AGITATOR OR MIXER
SPECIFICATIONS
SPEC.
NO.
-------
PLANT £
LOCATION
a a /- £>\/ri fi'C Z) e/ / -f- LS r £'em/)t'-
*-
K
Z
3
PERFORMANCE OF ONE
-i
_j
UJ
X
l/>
tt
UJ
a
•<
H
<•
0
O
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at
u
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UJ
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UJ
l/t
UJ
_J
N
N
O
7
Z
u
THori t.
2.1? J C'&f? O C- PTU'HR NO
Vert.
Sloped
° to horiz.
Rooting Hi-Pull Thru- Clomp Rlng-Pocked
Additional Proc. Data on
Sheet No.
UNITS/'?. ' '< SHELLS/UNIT
(fFTS^ith ExprjorrTt)
Tnermo syphon
Fluid
Total Flow
Liquid
Density
Viscosity
Specific Hoot
Th
Vopor
Mol
irmal
Wt
Conductivity
Density
Viscosity
Specific Heat
Thermal
Conductivity
Latent Hoot
Non- Condon sables
Velocity
Norm.
Mo«.
Max,
/Win.,
Operating Temp.
Operating Press. (Inlet)
Ib/hr
Ib/hr
Ib/cu ft
CS-CP
Btu/lb-°F
Btu/hr-sq
Ib/hr
Ib/cu ft
CS-CP
f*.°F/ft
Btu/lb.°F
Btu/hr-sq
Btu/lb
Ib/hr
ft/ sec
8F
pslg
f*.eF/r>
Pressure Drop psl
Film Coeff.
Inttulled Are*
BTU/Hr. Sq. Ft.
hrisq ft-»F/Btu:
t- "US
I/Unit
Design Temperature
Design Pressi
jre
Hydrostatic Test
Corrosion Allow./Linlng
°F
PS
ps
In
Number of Posses
Insulation
Btu/hr.sq ft. F;
4-&C''
"/
Inlet .
U-Tube
Fintube
/
SHELL SIDE -
TEMA SIZE/TYPE
Kettle Coil Hairpin Box
Other:
Outlet
fcrffi ^-t t' '? * >~> c?7)
/ y&} £ / /
/ 4-Ge (o/ 1
I4-O &( 1
1.0
M.W.
_&53
*
553
/•3.S
Allow. £
Cdc
. (e&
£~O
"7 &
2.
1"
; Segment Cut
Spacing Appro x. Equal - See
Horizontal
SHeel No.
%
Cut on Bottom for Condensote Drain
Impingement Boffl «£Y°ej^No j Condensate Lift
TEMA Class
;
Yes •("
[Lelhol Yes-tNcJ Code (
Spot Radiograph:
Weight Complete Ef
Shell
Shell Cover Channel
ip ty/ Full of Water
Sandblast: /Vo
Service
Inlet
Outlet
Dfoin
Vent
SHELL
Mk
^(o
?~l
Site
/£"
A1'
Rtg
150
ti
[point:
SIDE
Face Typ
ep
a
Number
OO
Inlet . TUBE SIDE - Outlet
^^IZrV"/"/' ^ t / / ^ (t't &? 7 y £ *•/
*/, 0"?7i yo<4
3of> 3L 3
M.W. .
/O
ZfO 1 _^_5£7. i?l
35
Allow 2S~ Cole. /S
LMTD (Corrected) ff3,^t °F
Shell ID (Approximate) in.
No.
Tubes (Approximate) ^ <^O^
Tube OD
/ in. [Tube Gage /Z. BWG
Tube Length 26' ( &JH J ft
Tube Pitch ^ DO A In.
Joint
Make/Type Fintubes
No.
Fins
per tube; per in.
Fin Height In. | Fin Thick. In.
Vessel Supports^Saddles^ Lugs Other;
Weir
Height in.; Shell After Weir In.
^ Removable Bundle Yes -(No'
ASME> National Board
(Stress Relieve: Shell
/
/^/ O Maintain
e Mk Size
1 r) /' "
£-O /u>
I2£ /£>"
TUBE
Rt,
I5&
ti
See Noille Sketch on Sheet No.
Shell Sid
Tube Sid
e:
P oral) el
Bonks of
.:: Parallel Banks of
Stacked:
SPEC. BY £pfZ //
CHE
CKED:
APP'D:
DATE, Z//4./74.
Wide
SIDE
Foe
f(l-
it
• Type
IA
O
1-
<
u
^
u
uj
IL
<
UJ
<
Shell sin Series *
Shells In Series
High
<^>THE DOW
Ib
Cathodic Protection Yes -Qip)
Other Txfv*//^ 1 StanlP C^«i> N«
Shsll Cover Channel Floating Head
Weight Bundle Only . Ib
Shell ID
Tubes 7
Tube Count Installed Area* X- *
IT t<£- Shell Cover
Ch. Cover/Bonnet " Shell. Chan. Side
Shell Not. Necks J /££ / Channel
Shd! Not. Flanges " Channel Cover
Shell Flanges
" Fltg. Hi
CHEMICAL COMPANY
SERVICE ,
o7£/ ' L f~&
PE VISION DAT!
/ C <~
: A
r ft
r~ fS t*-rj i t>
f. /if-'
B
7 '
C
•~ **.
OF
1 (QUIP. NO.
//CO \ £-f
HEAT
EXCHANGER
cpp(~|Fi/-ATinKK
SPEC,
Na
171502.SS
-292-
-------
'LANTC^a-.?
LOCATION
L - py
e/ r/c .
SVLFue. j?FMorAL
BLOC.
MANUFACTURER
NO.
NO. UNITS / aer -/rt>S ) P. 0. NO.
DUTY/UNIT /, 52^?^
1
3
3
4
5
4_
7_
8
9
10
11
12
13
14
IS
16
17
18
19
20
21_
22
23
24
25
26_
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42.
43
44
45
46
47
48
49
50
51
52
53
54
55
56
n(
K
PERFORMAMCE OF ONE UNIT
ESIGN DATA PER SHELL
0
_J
_J
111
NOZZLES PER St
a
*Horiz) Vert. Sloped
Flooting
OO BTU/HR !>
0 to hon
Z.
Ha1.- Pull Thru- Clomp Ring-Pocked
Additiono Proc. Data
on Sheet No.
JO. UNITS y
JSHELLS/UNIT /
^TS>vith Exp. Joint
Thermosyphon
Fluid
Total Flow
Liquid
Density
Viscosity
Ib/hr
Ib/hr
Ib/cu ft
CS-CP
Specific Heot Btu/lb-'F
Thermol Conductivity
Vapor
Mol
Wt Density
Vi scosity
Specific Heot
The
Lot
rmol Conductivity
Bit Heot
Non- Condensable*
Velocity
Norm.
Mox./Min.
Max. Operating Temp.
Operating Press. (Inlet)
Pressure
Drop
Film Coeff.
Foulina Resistance,
Over-all
Coefficient-
•US
Btu/h«.sq ft-°F/T>
b/hr
Ib/cu ft
cs-cp
Btu/lb.°F
Btu/hr-sq ft-°F/ft
Btu/lb
Ib/hr
ft/ sec
6F
psig
psi
BTU/Hr. So, Ft.
hr-sq ft-'F/Btu:
Btu/hr-
sq ft. °F;
Installed Area/Unit 4" ^f
Design Temperature
Design Pressure
Hydra static Test
Corrosio
°F
psig
psig
n Allow./Llnlng In.
Number of Passes
Insulation
lijlet .
U-Tube
Fintube
TEMA SIZE/TYPE
Kettle Coil
Other
SHELL SIDE - Outlet Inlet .
Hairpin Box
TUBE SIDE • Ourl.t
v Q) ft/ ft /• ^* /^" (7 1) f2.i}Ifcn5ts/-t"Tt?>ltit}
76>^ f ~f-G 4-
u
/'G^ffi.
// H
/.25/
M.W. =
8S
//
105 \ Z<••-) LMTD (Corrected) 15(0 °f
*q ft (Outside) ncluding.Excluding Area in tube sheets,
SHELL SIDE
/ S~Z)
/ S~£>
E.7-A
/
/Vi?
Cross Baffles: Type
Number
Provide
Long Ba
ffles: Type
TUBE
SIDE
2>CO
/ £~£>
2-"2 i~
r
/"
; Segment Cut
; Spacing Appro x. Equal ' See
Sheet
No.
%
in. Horizontal Cut on Bottom for Condensate Drain
> Number
Impingement Baffle Yes -ft
In.
Joint
Moke/Typ
No. Fins
> Flntubes
per tube;
per In.
Fin Height In. | Fin Thick. In.
Vessel Supports (Saddles/* Lugs Other;
Weir Height in.; Shell After Wei r • in.
ft Yes - No I Removable Bundle Yes - No I Cothodic Protection Yes - No
Q |Code
•II Shell Cover Channel
Weight Complete Empty/ Full of Water
Sandblast: I-"
Service
Inlet
Outlet
Drain
Vent
1 Point:
SHELL SIDE
Mk Si le R
7O 4" /j
IL$L *
tg Face Type
»0 fF
*
ASME
Nationol Board Other [Stomp Yes .^No)
(Stress Relieve: /Vo Shell Shell Cover Channel Floating Head
/
PfJ'f})£. [Maintain
Mk Si
27 2
HI Z
TUBE
ze Rtg
'" ISO
ti *l
SIDE
Face
fp
••
See Nozzle Sketch on Sheet No.
Shell Side:
Tube Side;:
Stacked:
SPEC BY /=: t
CHECKED:
Parallel Banks of
Parallel Bonks of
Wide
Shells In
Shells in
Type
Series
Series
High
tr/J. <3|5>THE
SE
APP'D:
DATE. Z//4
/7«/ u
VENDOR TO COMPLETE ALL
RVICE '
So
EVISIONDATE
INFORMATION
•^
A
DOW
Ib | Weight Bundle Only
Shell ID
Tubes 77
Stat Tube Sheet >
^ Fltg. Tube Sheet
5 Cross Baf./Tube
< Long Baffles 5
^ Impinge. Baffle
U Weir/Lift
Ib
Tube Count Installed Area* A- '
J&SllUtTl Chan.
Te/f Shell
< Ch. Cover/Bonnet '' Shell.
* Shell Noz. Necks
H Fit,.
Noz, Necks T-£
Nox. Flanges 74^£*t(£
el Flanges T<~ Ftf C C
Head
Hi Flange
Ring
'Studs
Supports $40^ /
•ASKETS& PACKING
Cover
Chan. Side
el
el Cover
Hd.
CHEMICAL COMPANY / loo \ J-0"'^"0
*T*
<2
B
MARKED
&£.£&
c
H.H..T
CI
SPEC.
OF NO.
HEAT
EXCHANGER
3ECIFICATIONS
171SOD 1/73
-293-
-------
PLANT S?S)0
LOCATION
/-
/-*
y/*/ )
I c
MANUFACTURER
' f"
f T ts r
BLDG. NO.
& m o ret
NO. UNITS / fiPf /Crti
/ FILE/JOB NO. ?£ £?£• 2 Q \
CHARGE NO.
1 n B/M NO.
' P. 0. NO.
DUTY/UNIT /£>7j
1
2
3
4
5
6
1
e
9
10
u
12
13
14
15
16
17
16
19
20
21
22
23
24
25
2o
27
28
29
X
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47_
48
49
59
51
52
53
54
55
56
UJ
0.
>-
H
r-
Z
->
UJ
PERFORMANCE OF ON
_j
_i
UJ
I
1/1
a:
UJ
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i-
<
0
z
o
to
111
a
-i
UJ
to
UJ
w>
uu
-1
N
1st
O
Z
Z
u
Hori i. ''Vert?
?.tc
f "/*
^Sloped
c:O
BTU/
° to horii
HR NO. UNITS /
SHELLS/UNIT / TEMA SIZE/TYPE
(^FTS^ith Exp. Joint
Floating Hd.-Pull Thru-Clamp Ring-Pocked YFiermo syphon
Additional Proc. Data on
Sheet No.
Fluid
Total Flow
Liquid
Ib/hr
Ib/hr
Density
Viscosity
Specific Heat
Thermo
Vapor
Mol
Conductivity
Ib/cu ft
CS-CP
Btu/lb." F
Btu/h«.sq f»-0F/ft
Ib/hr
Wt
Density
Viteoslty
Spec! fie Heat
Thermal
Conductivity
Latent Heat
N on- Conden tablet
Velocity Mo«./Minj
Norm.
Max.
Operating T
emp.
Operating Press. (Inlet)
Pressure Drop
Film Coeff.
Over-all
Coefficient. "US
Ib/cu ft
Btu/lb
Ib/hr
ft/ sec
°F
psig
psi
BTU/Hr. Sq. Ft.
hr-sq ft-°F/Btu:
Btu/hr-sq ft. °F;
Inilulled Area/Unit /£
Design Temperature
Design Pressure
Hydrostatic Test
Corrotion Allow./Lining
°F
ptig
psig
In.
Number of Pattes
Insulation
Cross Baffles
Type
Number e7 ,
P ro vi de
Long Bo
Ifles:
in.
Spac
y ^"£2
. SHELL SIDE
'nlet
U-Tube
Fintubo
SHELL SIDE
Kettle Coil Hairpin BOM
Other:
. Outlet
57*^(7 m
S&'7 5 £ fi-
le* j~rfe
/G'I f558
M.W. <
2i S
Allow.
1*\ $
2<">l "2 /"it-
/ A/^-)f
/ Cole. tJe*j
Clean
xq ft (Outside)
Service
Including-Excl
TUBE SIDE
J £O
/So
2 2-i"
/ ^p
2.S&
£•£>
75
/
; Segment Cut
*
ing Appro x. Equa - See Sheet No.
Horizontal Cut on Bottom for
Typ« ;
Impingement Baffle Yes^o/ !
TEMA Clots
Lethal
Spot Radiograph: A/^Shell
Condentote Drain
Number
o
S&G
Inlet . TUBE SIDE - Outlet
^Coi:-/i'nq M/&-fer(&rJ)
^?-,£':/&>>$e?^y~
// '1
M.W. •
*r 1 i?5 /OS \/Of
Allow £" Cole.
LMTD (Corrected) / / fj »F
ding Area in tube sheets
Shell ID (.Approximate) In,
No. Tubet (Approximate) / / 7 O
TubeOD /" In. | Tube Gage / 2, BWG
Tube Length /ft ft
Tube Pitch A DO A In.
Joint
IZclled
Moke/Type Fintubet
No. Fins per tube; per In.
Fin Height In. | Fin Thick. In.
Vessel
Supports Saddles- Lugs Other; /V£?/7£,
Weir Height in.; Shell After Weir In.
Condensate Lift Yes -fit \ Removable Bundle Yes -/KU
Yes -(N(
Shell Cover
) Cede (ASME
Channel
Weight Complete Empty/Full of Water
Sandblast: }/CS> 1 Paint: /**V"//77^
Service
nlet
Outlet
Drain
Vent
(£) &&
SHELL
Mk
'»e
b^
''/ i
Size
/(a1
itf
5 X
Rtg
ISO
tt
5 H
SIDE
Face
ftp
ft
5*rf
Type M
2
ff. es)
TUBE
k Size Rtg
0 — —
12. 3' /fr"
THE DOW
National Board
ell.ve:A/:3 Shell
J ICothodic Protection Yet -No/
Other: . | Stomp Yei.&>>
Shell Cover Channel Floating Head
Ib | Weight Bundle Only . Ib
V}
O
f-
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U
U
UJ
a
<
UJ
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Shell ID
Tubet
Tube Count Installed Area*- K- 91
3Cs*l Chan. Noz. Neck t $Ct-
Stot Tube Sheet 3 C 4. Chan. Nor, Flonoet 3f~* fft-C.
Fltg. Tube Sheet Chonnel Flanges ^dFl^Cf.
Cross Baf./Tube Sup. Fltfe Head
Lona Baffin
Impinge. Baffl
Weir/Lift
Fits. Hd. Flonae
> Clamp Ring
Bolts/Studs
Tie Rods & Spacers Nuts
Shell
Shell Cover
Channel
i>fff. 1 Vettel Supports
" GASKETS & PACKING
t>C -i- Shell Cover
Ch. Cover/Bonne! Z f •*• Shell-Chan. Side
Shell No z. Necks $ i r .' 1 Channel
Shell Noz. Flanges " Chonnel Cover
Shell Flanges
" Fltg. Hd.
CHEMICAL COMPANY
SERVICE
"•/.'
&y n
REVISION DATE *
*S 1 K
fj rrf {_
B
ft
VENDOR TO COMPLETE ALL INFORMATION MARKED
-YlSfiSv^t
C
jjiMrcT
OF
{equip. NO.
£-S.
HEAT
EXCHANGER
cpC(~|pipATinkK
jrci»int,A i luni
SPEC.
NO.
171002->l
-29?-
-------
LANT
/>/?/-
-?TF
/ / 'C
yp> motto/
FILE/JOB NO. "yBQAt
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER .Z/tT/~* OI /V'£ f
NO. UNITS
Tra' °
B/MNO.
P. 0. NO.
ODEL/TYPE >tfcy/£7/
'~) [NO. UNITS OPERATING 2,
SPARES
DATA
FEED
¥
FILTRATEf/^, BACKWASH
Fluid
Slurr
Flow-Process Basil
Ib/hr
7/3
Flow-Fill.r Bdiis
Ib/hr
Density
Ib/eu ft
/.•3-Sp^t
L/S
yjtceiit^
c*ntipois*
Solicit in Streom
3O
es
Parti cl* Size (Avo.)
microns
Normal
Max. Oper. Press. ftsig
Normal
Mox. Oper. Temp.
Allowable Pressure Drop
psl
Moximum Coke Volume:^
Type Discharge: Wet Cok*£bry Cak
Cycle: Precoat Preparation Tim*
; Precoating Time
Filter Aid Preporotion Time
Filter Aid *ppl,cotion Tim*
Filtering Tim*
Bio woo wn Tj me
Cleaning/Backwash Tim*
Totol Time Between Successive Fitter Cycles
Instrumentation: M onuol- Semi Automot,cJ Jfo*»/&ftV I/
Other Accessorial;
U^ff^^LoiJ^n LfVfl 5kjt h.kf^
Pockoae Unit Yes - No; Shop Assembled on Skids Yes - No; Floor Space Req'd
ft x ft; Height
Weight Empty/Full of Water
Ik; Shipping Weight
Ib.
49
Service
Inlet
Outlet
Vent
Drain
Relief Valve
SC-
SI
52
Pressure Gage
Quick Open Cover
Mark
No.
SI i*
Rtg.
Type
See Nozzle Sketch on Sheet No.
1 tern
Filter Headl
Filter Shell
Lining
Elements
i
Leaves
M.H. Cover
Bohl/Stud.
Nuts
Gaskets
Thickness
in.
Mot'l Class
fobrene.
Mot'l. Minimum Quality
PEC BY
HECKED:
PP'D:
ATE:
THE DOW CHEMICAL COMPANY
SERVICE
RE VISION DATE A
ENDOR TO COMPLETE ALL INFORMATION MAftKSvD
I loo [
FILTER
SPECIFICATIONS
SPEC
-295-
-------
PLANT<^9^/
LOCATION
MANUFACTURER
1^4
"/ 7V<
: ^tsJ+isr
ferntu
/<*
!
' BLDG. NO.
7>V/- - S">/j /• f r
NO. UNITS / /2X/-
FILE/JOB N
3. f ^ C2 M 7 ^s
CHARGE NO.
Trt? /O B/MNo.
' P. 0. NO.
MODEL/TYPE /f7/
1
2
3
4
5
6
7
8
9
10
11
12
13
14
IS
16
17
18
19
20
21
22
23
24
25
26_
27
_28_
29
30
31
32
33
34
35
36
37_
38_
19
40
41
42_
43
44_
45
46
47
48
49
50
51
52
53
54
55
111
U
z
"<
5
QL
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U.
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rRUCTION DETAILS
i& t •& ^9 ^"" "^
5/9
0
(^/Z2)CAKE
J5ts/ ' f& '£?>
/&. 15*4
f /
Type Discharge: Wet Cake-Dry Cake
Cycle: Preceat Preparation Time
Filter Aid
F
Preparation Time
iltering Time
Cleaning/Back was
T
h Time
Cycles
; Preeoating Time
; Filter Aid Application Time
; Slowdown Time
Instrumentation: Monua >Sem> AuromatiafAutomaJic J
Filter
Design Pressure
Design Temperature
psig
»F
Hydrostatic Test P*ig
Corr. Allow./Lin.- Shell H.
Joint Effi
Insulation
Electric a
eiency-SKetl H<
ads in.
ads %
Construction: Standard Open
Shell Feeder Tank Filtrate Tank Code:
i. No
Radiograph:
Weatherproof
Stress Relieve:
Specie Design:
National Board No.
Explosion Proof T/^ f~£.
Other:
Piping. Valves. Fi
.
Elements:
Leaves:
Maximum
ttings Supplied with Filter to
Area/Element
Area/Leaf
sq ft;
sg ft: No.
Cake Thiclcrtess
Precoat Rea'd: Yes -r^5o3 Material
Filteroid
be in Accordance with:
in. IDx
No. Req'd
Req'd
in. Ton to Tanj- Type Heads
n. IDx In.
ODx in. Length
: Leaf Height n.; Leaf Soacina in.
mi crons
•Minimum Particle Size Retained
In: Gross Filter Volume
Req'd: Yes ?%) Material
Feed Pump Furnished ^1&J£//} £f* ;
Mat1
(Wetted
Parts)
Make
Filter Fabric:
; Model
; Type Seal
oal»cu ft: Heel Volume
• microns
aal • cu ft
M aterl *\Pol^&tDI>/lfnt : Me sh
: Max. Flow oom at e«ia
: See Pump Spec tto.
Qther Access«riesJi7t/i//ri/» Pft ft/r7tbr ^tvt 1 tcr\ trc/L 1-lAL Of D Suit'tthf* Druni She?/ dcnhcl
Pockooe Unit Yes - No: Shop Assembled on Skids Yes - No;
Weight Empty/Ful
Service
Inlet
Outlet
Vent
Drain
Relief Va
ve
Quick Open Cover
See Nozz
SPEC BY 2E f~
of Wate
Mark
A
B
C
D
E
F
G
H
J
K
Floor Space Req'd ft x ft; Height ft
r / Ib; Shipping Weight
No. Size R
Fg. Face Type
e Sketch on Sheet No.
Item
Thickness Mat'l Cl
Filter Heads in.
Filter Sh
... Lining
_j
ell in.
in.
in.
£ Elements
m •
H Leaves
Z M.H. Covet
Bolts/Studs
Nuts
Gaskets
/V -<3^ THE DOW CHEMICAL COMPANY f/
CHECKED:
APP'D:
DATE,2//*/74
SERVICE
REVISIONOATE A
B
e
(
C SPEC
Ib.
ass Mot'l-Minimum Quality
N&of'ffnc.
'
1CQUI*. NO.
/="- 2.
FILTER
5PECIFICATIONS
28850»-OS
-296-
-------
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS / nor
B/M NO.
P. 0. NO.
0*-
2o_ps*'q Steam f .Off*
f€
/33 4/J
water
Jo/
-Z./H.00F
' oil'•
25
26
29
30
32
35
36
39
40
41
42
43
45
46
48
49
50
SPEC OY
rMECKED:
kPP'D:
>ATEt
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
/ENDOR TO COMPLETE ALL INFORMATION MARKED
I
CQUI*. NO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
-297-
-------
/- /"y/V/7'g
FILE/JOB NO.
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS / orr- Tfrf/ n
B/M NO.
P. 0. NO.
Z. 4-
212.4.
12
eet it/m
Tt=
33
34
49
50
SPEC. BY
MECKED:
PP'O:
«33>-THE DOW CHEMICAL COMPANY
SERVICE
REVISIONDATE A
ENDOR TQ COMPLETE AUL INTORMATION MARKED
2&260 3-68
•HCCT or
I IQUIP.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
NO.
-298-
-------
PLANT t^oA
LOCATION
MANUFACTURER
?/- P^f r/ r/c 5ts /f-t/r >
P^/D/5 m/ FILE
BLOC. NO. CHA
NO. UNITS 2,/Trot n B/M
P.O.
MODEL g X3 '
1
2
3
4
5
6
7
8
9
10
TT
12
13
TT
15
To"
17
18
19
20
~
22
23
24
25
26
27
IT
29
30
31
32
33
34
35
_36_
37
38
39
40
41
42
43
44
45
46
47
48
49
"so"
51
52
53
54
55
t/i
51
M
i/i O
U
ON DETAILS
CONSTRUCT!
MATERIALS
RIVER
t-
UJ
*/<
3
Liquid Pumped 5fc///<5
Specific Gfovi
ty ot
P.T.
NO
. UNITS
' fe. -£e<*f S/is rr- y
)
Viscosity at P.T.
&ft* °F
/••a
—
0.-7& £5>c"
Vapor Pressure at P.T.
Corrosion or Erosion Factors:
Arrange me ntQH or iz
Direction of F
Case: Design
)-V.rt..|n Line
ototion Facing Pump Coup
Pressure
Max. Allow
Split;
Horiz
Impeller Diameter;
. Working Press.
/JOB NO. 73^623
RGB NO.
*IO.
NO.
ASA PUMP 6JYES L7]NO ASA DESIGNATION
Max. Capacity at P.T.
D
ischarge Pressure / Q *~J
Suction Pressure ^ 7
Differential Pressure I ^L O
Differential Head
NPSH Available
NPSH Required (Water)
S
uctiortOingle^)- Double
ling: CW . CCW Speed: 3 5oO
2.-7O «P"
psia ft.
piio ft.
psi
2.10 "
ft.
ft.
rpm
psig Number of Stoges ;Shut-Off Pressure ft.
P«
-Vert- Barrel
Supplied g fa
ig Volumetric Efficiency at Rating
X
Impeller Type
inches; Moximum / ^^ inches; Minimum ^9 inches
Vent and Drain Topped; Yes - No
Nozz les
Suction
Discharge
Vent*
Drains
Cooling HzO
S
ze
3 "
ilL"
Rating
Facing
Bearings: Thrust
Location
Radial
Type
Type
Lubrication on Bearings; Oi • Grease
Oiler: Yes . No; Type
Coupling: Yes • No; Mfr.
Coupling Guard: Yes - No
B
Water Cooling: Casing-Stuff. Box-Bearings-Pedestal-Gland£Non^ Total Water Required:
Smothering Gl
Packing: Yes
Mechanical S«
Single
Rotary
Insert
and:
Yes -<5P
<52 Type
ah^VeJ- No
gom
Lubrication on Stuffing Box: Oil-GreaselcNone./
Sealing Oil Connection: Yes - No
, Furnished ^1 ,!/& r) C/ O f \
Mfr.
Type
Double-lnside*Outside-Ba lonced-Unba lanced
Unit
• S
eo Ring
;
; Reversible: Yes - No
Insert Mounting: Ciamped In - *'0" Ring
Gland
- press Fit
Face Material
Face Material
; Shaft Packing
t
; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for; Dead - End Lub. -
Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stu
ffing Box Req'd: Yes - No
Weight of Pump
Weight of Driver
Ib; Weight of Base
Ib; Shipping Weight
Cosing & Covers: & / £>
Casing Wear Rings: ^$ / C**
Impeller: * *? / ^
Impeller Wear
Rings: . 3 / (*
Stuffing Box Bushi
Furnished by
ngs :
3/t»
Ib
Ib
Shaft: 5-/
Lantern Rings :
Glands :
Goskots:
Mp/JCJfjF ' Type(Elec. Motor)- Steam Turb
Electric Motor: Make
Enclosure
Insulation
Estimated
Mounted by//Jf/7<^/»
rFFC. SF
BMP
Req'd.
Frame
Temp Rise °c
Nominal Motor Size (Non-overloading)
Speed
4f5 hp
£iO "P
rpm
Volts &.&Q • phos» J3 •' Cycle &&
Speed Reducer; Integral -
Mfr.
., Model
Separate
Ratio
Class
See Driver Specification No.
Performance Curve
•• (v«>
Certified;
No; Curve No.
Yes -(No)
Hydrostatic Test: (Yes^_No; Pre*sure
psig
Shop Inspection: Yes '- NoJ
SPEC. BY ^T"rr //
CHECKED:
APP'D,
DATE: Z//4/74L
ne - Other
Steam Turbine: Make
(•Direct? Gear - Belt
Mounted by
Model:
Horsepower
Inlet Steam Temp., °F: Normal
Water Rate:
Vacuum (If any)
Back Pressure
Nozzles Siie
1
ilet
Exhaust
/>
Serial Number
hp ; Speed rpm
; Max
; Max.
Ib/hr
mm • in. Hg - psia
psig
Outline Drawing
Cross Section Drawing
Bulletin No.
<&j$t> THE DOW CHEMICAL COMPANY
SERVICE
5ot.F47
REVISION DATE
-
C
VENDOR TO COMPLETE ALL INFORMATION MARKED
HIHEET OF
Page No.
1 EQUIP. NO.
P-/A6&
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
18370D4/73
-299-
-------
PLANT c&a/- Pyr/tiC <
LOCATION '
MANUFACTURER
MODEL /jf, X /4? ~ 22
1
7
3
4
5
6
7
8
9
10
TT
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
26
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
Z
lljO
So
-J
Q
Z
o
r-
D
Z
U
3
or
UJ
H-
3
UJ
£
UJ
jtf'TtJf j?emGfaf FILE
BLDG. NO. CHA
NO. UNITS 2/n/r 7V>f"l B/MI
P.O.
NO. UNITS ASA PUMP SffVES d
Liquid Pumped Xe?/v%3&/.3- Ffrric* Scf/-fa ft
Pumping Temperature (P.T.)
Specific Gravity at P.T.
Viscosity at P.T.
'S^O' °F
X.2.
^' V ^i^Cp
Vapor Pressure at P.T.
Arrangement Jmorizi Vert.- n Line
'JOB NO. 7^-5^6 J? 3
3GE NO.
>IO.
NO.
NO ASA DESIGNATION
Max. Capacity at P.T. • &t*y£2^^} flP01
Discharge Pressure ^L £)
Suction Pressure 3£
Differential Pressure 2. £j'
Differential Head
NPSH Available
NPSH Required (Water)
SuctionOingle)- Double
psia ft.
psia ft.
psi
£)C3 '».
ft.
ft.
Direction of Rotation Facing Pump Coupling: CW . CCW Speed: <9<9O rpm
Case: Design Pressure
Max. Allow. Working Press.
Split; Horiz-Vert-Barrel
/SQ Ps'^ Number of Stages / ;Shut-Off Pressure ft.
yi^^^J psig Volumetric Efficiency at Rating
mpeller Type
%
Impeller Diameter; Supplied /&j fyi. inches; Maximum ^"2. Vfe_ inches; Minimum /7 V*lrf tnche*
Vent and Drain Tapped: Yes - No
Nozzles Size Rating
Suction /4# /£O*
Discharge /4 * ''
Vents
Drains
Cooling HzO
Bearings: Thrust Type
Facing Location
£ ' f
"
Radio
Type
Lubrication on Bearings; Oil - Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes • No
Baseplate: Yes • No; Type
Water Cooling; Ccsing-Stuff . Box- Bearings- Pedestal- Glond^Nor^ Total Water Required:
Smothering Gland: Yes - No
Packing; Yes -^Si>C Type
Mechanical Seal: ^£p- No; Furnished
Single - Double-lnside-Outside-Ba
gpm
Lubrication on Stuffing Box: Oil-Grease-None ^^^yirf**/*
Sealing Oil Connection^Ves) - No
b* A&/7£/<9/* .Mfr.
lonced-Unba lanced
Rotary Unit ; Seal Ring ; Face Material
Type
; Shaft Packing
Insert ; Reversible: Yes - No ; Face Material
Insert Mounting; Clamped In - "0" Ring - Press Fit
Gland ; Plain; Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Topped for: Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with D
scharge Bypass ~ Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes - No
Weight of Pump
Weight of Driver
Casing & Covers: ~//
Casing Wear Rings:
Impeller;
Impeller Wear Rings;
Stuffing Box Bushings:
Ib; Weight of Base
Ib; Shipping Weight
tar)i u m
H
H
tt
H
Ib
Ib
Shaft:
Shaft Sleeves : / ^ r& /*) J '&//l>"7
Lantern Rings:
Glands:
Gaskets:
Furnished by: fof ft £&£)/* ; TypeQMec. Motor} Steam Turbine - Other
Electric Mofor: Moke Mounted by ^/?^{?/*
Enclosure 7"£" /*~"^
Temp Rise °C
Insulation Frame
Estimated BMP Req'd.
/ 3fi "P
Nominal Motor Size (Non-overloading) /,£?<£? ^P
Speed &&O . 'Pm
Volts ^4- O •' Phase ^
; Cyc le ^ O
Speed Reducer: Integral - Separate
Mfr. Ratio
Model Class
See Driver Specification No.
Certified: Yes irecjj> Gear - Belt
Mounted by
Model:
Horsepower
nlet Steam Press., psig: Normal
Inlet Steam Temp., °F: Normal
Water Rate:
Vacuum (If any)
Back Pressure
Nozzles Size
Inlet
Exhaust
hp ; Speed rpm
; Max
; Max.
Ib/nr
mm - in. Hg • psia
psig
Rating Facing Location
Serial Number
J Outline Drawing
J Cross Section Drawing
Bulletin No.
SPEC BVr/r// <5§>- THE DOW CHEMICAL- COMPANY
CHECKED: SERVICE
APP'Di ^5/J/f-i/)7t
DATE: iJjtf/jij. REVISIONDATE >
F &»/• CMC. f^f
\ B
c
VENDOR TO COMPLETE ALL INFORMATION MARKED H.^rrT n*
Page No.
//oo \ £-"£$&
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
18370D 4/73
-------
PLANT &0a./- Pynfic
LOCATION '
MANUFACTURER
MODEL 3't4-~/3
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
TZ"
TT
18
19
20
21
22
23
24
"2T
26
27
28
29
30
TT
32
33
34
35
36
37
38
39
40
41
42
43
44
7T
46
47
48
49
50
51
52
53
54
55
*rt
Z
^
26
_l
r-
UJ
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CONSTRUCTI
«
•<
Q£
UJ
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•«
1
DRIVER
r-
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Sc//fttr JFem^raJ F||-E
BLDG. NO. CHAR
NO. UNITS«i [)Pr TfOlIt B/Mlv
P.O.
/JOB NO. /&&£>£. 2
GE NO.
0.
NO.
NO. UNITS ASA PUMP 53YES LT1NO ASA DESIGNATION
Liquid Pumped /^/j*/» (7r&.C.£3 ^//•fa.feS }
Pumping Temperature (P.T.)
*Z./S. 6* ">
Specific Gravity ot P.T. /,&
Viscosity ot P.T.
Cl-Cp
Vopor Pressure at P.T.
Corrosion or Erosion Factors:
Arrongemens^Horizy Vert., n Line
Max. Capacity at P.T. ^j f?^^ flpti
Discharge Pressure
Suction Pressure
Differential Pressure
Differential Head
NPSH Available
NPSH Required (Water)
Suction^SinglcTV Double
Direction of Rotation Facing Pump Coupling: CW . CCW Speed: J **} 5 O
Case: Design Pressure
Max. Allow. Working Press.
Split: Horiz-Vert. Barrel
Impeller Diameter: Supplied r£
Vent and Drain Topped: Yes - No
Nozzles Size Rating
Suction ^£. "
Discharge £ "
Vents
Drains
Cooling HjO
piio 8 5" ft.
psta /O '*•
psi
7^ ft.
ft.
«.
rpm
p*ig Number of Stages / ;Shut*Qff Pressure ft.
P*'9 Volumetric Efficiency ot Rating
Impeller Type
s
^ inches; Maximum / ^ inches; Minimum <£f inches
Bearings: Thrust
Facing Location
Radial
Type
TXP«
Lubrication on Bearings; Oil - Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes * No
Baseplate: Yes - No; Type
Water Cooling: Costng-Stuff. Box*Bearing$-Pedestal-Gland(Nonjr Total Water Required:
Smothering Gland: Yes - No
Pocking: Yes - No; Type .
Opm
Lubrication on Stuffing Box; Oil-Grease-None
Sealing Oil Connection; Yes - No
Mechanical Seal: (Yes} No; Furnished by; l/<£f)CfOI~ ; Mfr.
Single - Double-lnside-Outside-So
lonced-Unba lanced
Rotary Unit ; Sea Ring ; Face Material
Type
; Shaft Pocking
Insert ; Reversible: Yes - No ; Face Material
Insert Mounting: Clamped In - "0" Ring - Press Fit
Gland ; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for: Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes - No
Weight of Pump
Weight of Driver
Casing & Covers: t
Cosing Wear Rings:
Ib; Weight of Base
Ib; Shipping Weight
3»/£
•3/<^
Impeller: 2>/ &
Impeller Weor Rings: ^ /£
Stuffing Box Bushings: _^/l£a
Furnished by: jflf^/yOr&f* ! "^X
Ib
Ib
Shaft: Stfff/
Shaft Sleeves: <*. //p
Lantern Rings:
Glands:
Gaskets:
p*^pfi*c. MotoT} Steam Turbine - Other
Electric Motpr: Make Mounted by y£fj£/&f*
Enclosure SF
Temp Rise °c
Insulation Frame
Estimated BHP Req'd.
25""P
Nominal Motor Size (Non-overloading) 3O "P
Speed
Volts /,/ LiQ; Phase *»)
rpm
; Cyc le ^ ^
Speed Reducer: Integral - Separate
Mfr. Ratio
Model • Class
See Driver Specification No.
Performance Curve: (Yes}- No; Curve No.
Certified: Yes /fTo)
psig
Shop Inspection: Yes -(No^y
Steam Turbine: Make
£"bir«y> Gear . Belt
Mounted by
Model:
Horsepower
inlet Steam Press., psig: Normal
Inlet Steam Temp., F; Norma
hp ; Speed rpm
; Max
; Max.
Water Rote: Ib^u
Vacuum (If any)
Back Pressure
Nozzles Size
nlet
Exhaust
Serial Number
fj Outline Drawing
9 Cross Section Drawing
Bulletin No.
SPEC.BY^-^-^ f)L/£
DATE: 2y/V/7V "EVISIONDATE
eeo Mmxfcee tuie
l-l =1
VKMOOK taCOWPI.kTSI.AUU INFORMATION MARKED [|.U*FT or
mm * in. Hg - psia
psig
Rating Facing Location
Page No.
//CO \ P'^fai
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
16370O 4/73
-------
PL4NTcC/%?/- /"V/> r7C Ses/fess" f<£.sjr)Ot/& / FILE J
LOCATION BLOC. NO. CHARG
MANUFACTURER NO. UNITS 2. P? T TrOtO B'MNO
P.O. NC
OB NO 7J&62.2
E NO.
).
MODEL /y/^-fi* NO. UNITS ASA PUMP StfYES Cl NO ASA DESIGNATION
1
2
3
a
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
Z
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Speed Reducer: Integral • Separate
Mfr. Ratio
Model Class
See Driver Specification No.
Certified: Yes -No
Shop Inspection; Yes • No
Steom Turbine: Make
; Direct - Gear . Belt
Mounted by
Mod*):
Horsepower
Water Rate:
Vacuum (tf any)
Back Pressure
Nozzles Site R
Inlet
Exhaust
hp ; Speed rpm
; Max
• Max
Ib/hr
mm - in. Hg * psio
psig
ating Facing Location
Serial Number
J Outline Drawing
2 Cross Section Drawing
Bulletin No.
QPFf* RY y ^rjs»fc_
jf? F M LFu£n- /9
Page No.
//oo | P-%/$fo
CENTRIFUGAL PUMP
SPECIFICATIONS
PEC.
0.
18370D4/73
--302--
-------
-------
FILE/JOB
LOCATION
BUDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS/
B/M NO.
P. 0. NO.
FIELD ERECTED
NO
INO. UNITS
NOMINAL VOLUME
Oper. Press.-Positivel Vacuum
in. HzOj
VESSEL SKETCH
Operating Temperature
Liquid Specific Gravity
Content*
P«». Pr«».*P_c«itive j Vacuum
in. H20|
Design T»mp_*fotuf»_
/SO
Hydrostatic T«st
in. H;0
She
Shell
H• odt Cofr. Allow. In,
Heodj Joint EH.
cod.:
Stomp
No
Rodiogroph:
Slmsi R«li«v«:
Insulation:
Fi rap roofing;^
Sandblast;
Point!
Manhole
Hinged
Orii«r:
Platform Clipi;
[Ladder Clips:-/^ | Iniul. Ringl;/>/O
Pip« Supports;
Wind load:
Wt. Ertipfy
Ib
Item
Shell
Cone Roof
Bottom
Lining
Neiil«Nedn
Flanges
Couolln
M.H. Cover
Supports
Bolts/Studs
Nuts
Gaskets
Thickness Mofl Cla
Seismic;
Wt Full
Servic
tfifC t
Mark No.
Size
*
Mol'l - Minimum Quality
SrteeJ
n
Raring
Fac*
NotxU to b* F*tugg*d or Blinded.
Typ.
5
For Farther Detolls, See Sheet No.
SPEC. BY
CHECKED:
»PP'D:
3ATE,
THE DOW CHEMICAL COMPANY
SERVICE
REVISIONOATE A
CNDOR TO COMPLETE. ALL INroRMATION MARKED
EQUIP. NO.
T--2.
VERTICAL TANK
SPECIFICATIONS
SPEC.
NO.
-------
PLANT. £
LOCATION
fO GAL
$5
&• "7 £2
Li-
lt* CNoJ
*£o
^oo
^
/s
Stamp tftlJ No
Strest Relievo: A1
'(.
3
Notionol Boord No.
Type Support.: SjC-J f* 'f*
In.ulotion: /
Firepro
otng:
t/a
Sandblast: Stll'f*t~ Point: ^jr//7>v f /-ft-
^ffitfr*
LT
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Mark
A
B
C
D
E
F
G
H
J
K
L
M
N
P
0
R
No.
/
/
/ ,
1
( ,
f
f
Seismic;
Wt Full of Water
I.
s Mat'l . Minimum Quality
77' 7^ f) / 'f-"t-/ £. /&&
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77 ' &fj)li.?jf ''{-(' f?J
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H
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Siie Rating Face
*^" /A"^* f f^
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/£' ' ' "
£11 H M
fA, " " "
2*
2"
Typ.
•Nonle to be Plugged or Blinded
SPEC. BV g'fZtf
CHECKED:
APP'Oi
VESSEL SKETCH
pff & Tbtp j-ffa&
For F.rtfier Details, See Sheet No.
•" THE DOW CHEMICAL COMPANY lt^n | £?T/"°'
SERVICE
^ / 4 / /"~ S\ *T~ ^ ^— IS JO- t
%^ t*' ' f~~ *3 f *~ •"• * *1 *"
DATE:£//^^«y MEVISIONOATE A
VINOOR TO COMPLCTE ALL INFORMATION MAA1KCO
0O£A TOG VERTICAL VESSEL
SPECIFICATIONS
• | c SPEC.
||>M(IT o» NO-
2SA40 3-0M
-305-
-------
PLANT f D /I f - /-'y'V1/ Tjf -5?/-////^/ >C Vxy X X^/ FILE/JOB NO. '/*••/.,£. y 1*>
LOCATION ' BLDG. NO. CHARGE NO.
MANUFACTURER • NO. UNITS / ffff Tfffl'f) B'MNO.
P. 0. NO.
FIELD ERECTED YES
S'f Cffiri
I/I* )1 4~ '
f/yst f-g f*
Cft,ff+/rt
LT
ft 1 -fr <* $•£-
tvj&iifrote.
Marie No.
A / /
B /
C /
o y
E / /
F /
G /
H /
J /
K/
L
M
N
P
0
R
Seismic:
Wt Full of Water Ib
s Mat'l . Minimum Ouallty
&i & te.
Z>ie*> I
Site Rating Face Type
'I" /££? FF
4" >• 1,
Z" •• ',
3" " 'f
f •/ •>
2." v '•
4" "
2.11 a a
ZH » n
to* 2- THE DOW CHEMICAL COMPANY //£/;• I p"'^"*'
jE?&^*~ts& /€y 7~/^vV/C VERTICAL VESSEL
SPECIFICATIONS
RE VISION DATE ABC SPEC
25HAO 3-Bt
-------
PLANT
/y/-v
FILE/JOB NO.
LOCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS / f)?r If ' '
B/MNO.
P. 0. NO.
DUTY/UNIT ?(o.
BTU/HR|NO. UNITS / [SHELLS/UNIT /
TEMA SIZE/TYPE
Herli. (Verfr Sloped
0 to horii.
CFTS-«lth Exp.Jeinj) U-Tube
phon~
Kettle
Coll
Hetrpln
Be.
.
Floating rTe^Pull Thru-Clemp Rlng-Pocked
Fin tub*
Other:
Additional Prec. Do to en Sheet Ne.
Inlet
SHELL SIDE • .Outlet Inlet
TUBE SIDE
Pullet
Fluid
(73)
a. 4
Tetol Flew
Ib/hr
Liquid
Ib/hr
Density
Ib/cu ft
Viscosity
CS-CP
Specific Hoot
Btu/lb-'F
Theme) Conductivity
Btu/h»sg ft.°F
Veper
Ib/hr
Mel Wt
Den llty
Ib/cu ft
Viscosity
CS-CP
Specific Heat
Btu/lb-° F
IS
Thermal Conductivity
Btu/hf.sqft.'>F/ft
16
L otent Heat
Btu/lb
17
Non-Condonsobles
Ib/hr
M.W. i
M.W. >
Velocity Mo«./Min,
ft/see
Norm. [Mex. OperoHng Temp,
I 36>o
ZS'Q]
Operating Press. (Inlet)
o»ig
71
Pressure Drop
pi!
Allow.
Cdc.
Allow
Cole.
Film Coeff.
BTU/Hr. So. Ft.
Foulinq Resistance^
hr-sq ft.«F/Btu;
24
Over-all Coefficient- "U'o
Btu/hr-sq ft. °F; Clean
Servl c. 75'&
Installed Area/Unit
LMTD (Corrected)
ft (Outside) Includirtg-Excludtng Area in tube sheets,
»F
SHELL SIDE
TUBE SIDE
She.ll ID(AppiCMlmate)
In.
Design Temperature
No. Tubes (Apprexlmat*)
Design Pressure
Tube OD
In. I Tube Gage
BWC
31
Hydrostatic Test
P«lB
Tube Length
Corrosion Allow./Lining
in.
Tube Pitch A QQ
In.
Number of Posset
Joint
34
Insulation
Make/Type Flntubes
Cross Baffles) Type
Segment Cut
No. Fins
per tube;
per In.
Number
Spacing Appiax. Equal - See Sheet No.
Fin Height
In. I Fin Thick.
In.
Provide
in. Horizontal Cut on Bottom for Condensate Droin
Vessel Supporti^Soddles3 Lugs Other;
Long Baffles: Type
; Number
Weir Height
in.; Shell After Weir
In.
Impingement Bafflepj^tNo \ Coodensote Lift Ye. -(fj^Removoble Bundle Yes ^SPrCethodie Protection Yei .
agj>tl
[Lett
TEMA Class
.thai Y.i-CHo) [Cede
-------
PLANT
LOCATION
f'fitf ,
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f
£>c
MANUFACTURER
//f /-
BLDG. NO.
/r
? n , f *•* •
NO. UNITS / fffr 7~fS>/r
' FILE/JOB NO. 7£ B/MNO.
' P. 0. NO.
DUTY/UNIT £
1
2
3
4
5
6
7
a
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
2JL
29
30
31
32
33
34
35
36
37
38_
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
56
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BTU/HR
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Vert. Sloped ° to horlz.
Floating Hd-Pull Thru- Clomp Ring-Pocked
Additional Proc. Data on Sheet
No.
. UNITS / ISHELLS/UNIT /
(FTS^i'h E«p. Joint
Thermo syphon
Fluid
Total Flow
Liquid
Ib/hr
Ib/hr
Density
Viscosity
Specific Heat
Thermo Conductivity
Vapor
Mol
Ib/cu ft
CS-CP
Btu/lb.°F
Btu/hr-sq
ft.°F/ft
Ib/hr
Wt
Density
Ib/cu ft
Viscosity
Spec! fie Heat
Th.
rmol Conductivity
Latent Heat
Nan- Con den sables
Velocity
Norm.
Max./Min,
Man. Operating Temp.
CS-CP
Btu/lb-eF
Btu/hr-.q fv'F/h
Btu/lb
Ib/hr
ft/ Si
*F
c
Operating Press. (Inlet) P*I0
Pressure Drop psl
Film CaeH.
Foulino Resistance.
Over-all
Coefficient- U'o
Instulled ArWUni
2
BTU/Hr. So, Ft.
hr-sq ft-OF/Btu:
Btu/hr-sq ft. °F;
. /2.£o
Design Temperature
Design Pressure
Hydm static Test
Corrosion Allow./Lining
Number of Posses
«F
pslg
pslg
In.
Insulation
nl.l.
U-Tube
Fintube
SHELL SIDE -
TEMA SIZE/TYPE
Kettle Coll Hairpin Boi
Other:
Outlet
f75)tJ3{>r>'fl<4 tSuifvr (7(r)
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247
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SHELL SIDE
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Number
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Impingement Boffle^Yes^o |
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Spot Radio graph: riioSh.il Shell Cover
Lift
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Sheet No.
Condensate Drain
Number
Shell ID (Approximate In.
No. Tubes (Approximate) 2> &1-?
Tube OD
J In. (Tube Gage || BWG
Tube Length & fS] ^2-fo ft
Tube Pitch ADO A In-
Joint
Make/Type Flntubes
No. Fins
per tube; per In.
Fin Height In. | Fin Thick. In.
Vessel Supports Saddles - Lugs Other;
Weir Height n.; Shell After Weir In.
Q| Removable Bundle Yes I^j0)|
[code CASM&)
Channel
Weight Complete Empty/Full of Water
Sandblast: /V0 I Paint: /(/O
Service
nlet
Outlet
Drain
Vent
See Nozi
Shell Sid
SHELL SIDE
Mk Size
75 12"
"Tff /&
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15(2 I*LF
ISO "
Type
Mk
b4-
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~
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Size
8"
S"
TUBE
R.?
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SERVICE
SOLI/ en
REVISION DATE
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Tube Count Installed Area* %• X
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'I Chan. Not. Flana*s?/'4 Ftit-f.
Channel Flanges **
Sup. '' Fltg. Head
Fits. Hi Flange
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Bolts/Studs
Tie Rods & Spacers // Nuts
Shell
Shell Cover
Chonnel
.< Vessel Supports
•- GASKETS ft PACKING
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Ch. Cover/Bonnet » Shell-Chan. Sid*
Shell No i. Necks
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Shell No*. Flanges ^Jl/w/^i Chonnel Cover
Shell Flanges
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CHEMICAL COMPANY
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EXCHANGER
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17180 2-B«
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-------
PLANT f
LOCATION
''rrtf- /-Y,
rjf/f ,5 //
/•*-(.//- x-
BLDG. NO.
MANUFACTURER
DUTY/UNIT y
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27_
28
29
30
31
32
21
34
35
36
37_
33
39
40
41
42
43
44_
45
46
47
48
49
50
51
52
53
54
55
56
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o
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BTU/HR
NO.
to horii.
Floating Hd.. Pull Thru- Clomp Ring-Packed
Additional Proc. Data on
NO. UNITS /
UNITS / SH
'•?,•..•/•;•*/
FIL
CH
per Trs>i n B/»
*
ELLS/UNIT /
fFT>with E«p. Jo nt U-Tube
Thermosyphon
Sheet No.
Fluid
Total Flow
Liquid
Density
Viscosity
Specific Hoot
Thermal
Vapor
Mol
Wt
Conductivity
Density
Viscosity
Specific Heat
Thermal
Conductivity
Latent Heat
NortrCondensobles
Velocity Max./Minj
Norm.
«*ox. Operating Temp.
Ib/hr
Ib/hr
Ib/eu (t
CS-CP
Btu/lb.«F
Blu/hr-sq
Ib/hr
f».0F/ft
Ib/eu ft
CS-CP
Btu/lb.°F
Btu/hr.sq
fl-'F/h
Btu/lb
Ib/hr
ft/so
°F
C
Operating Press. (Inlet) pslg
Pressure Drop psf
Film Coeff.
Over-all
Coefficient. "U'a
BTU/Hr. Sq. Ft.
hr-sq
ft-'F/Bru:
Btu/hr-sq
ft.°F;
In. tolled Area/Unit ^7 &
Design Temee
mature
Design Pressure
Hydrostatic Test
Corrosion Altow./Lining
"F
psig
pslg
In.
Number of Passes
Insulation
Cross Baffles
Irjlet . .
O4)
-^
Fintube
P.
TEN
Kettle
Other
SHELL SIDE • Ou.Het
yi/0 y e f» /^, '
'
/• O
/• ^
53
M.W. .
'%£
JO 5" I
Allow.
^. Cdc.
Clean
Servi ce 2-{~^ /**)
E/JOB NO. y~!Sf 3 ^
£~~D
f ~
A/O
; Segment Cut %
Equal - See
Sheet No.
Bottom for Condensate Drain
Type _ ;
Impingement Boffle" Y«^NoJ )
TEMA Class
Lethal
Spot Radiograph: ^Shell
Condensate Lift
Yes 4,
Number
Yes-'No 1-Removabl.
Shell ID (Approximate) In.
No. Tubes (Approximate) & 7
Tube 00
/
Tube Length
In. | Tube Gage // BWG
&M Z6\24- *»
Tube Pitch ADO ^ In-
Joint
Moke/Type Fintubes
No. Fins
Fin Height
per tube: per In.
In. f Fin Thick. In.
Vessel Supports Saddles • Lugs Other;
Weir Height
> Bundle Yes 4'rvl'Cathodic
ttJ ICode ("ASMS) National Board Other;
Shell Cover
Channel
Weight Complete Empty/ Full of Water
Sandblast; /(&S.
Service
Inlet
Outlet
Drain
Vent
SHELL
Mk
'p4-
'o5
—
-
SI i.
£>''
f?"
Rtg
150
»
'
I Polnh PtifnC.
SIDE
Face
H?
04
Type
Mk
7^>
5ft
-
-
TUBE
Si so
Iff*
e"
Rts
ISO
tl
See Nonle Sketch on Shoot No.
Shell Side:
Tube Si do::
Stocked:
SPEC.OY,C>CT#
CHECKED*
t t
DATEt 2yTHE DOW
Is | Weight Bundle Only . Ik
Shell ID
Tubes
Slot Tube Shoot
" Fltg. Tube Sheet
Tube
=>£
//
O Cross Baf./Tube Sup. _$/
< Long Baffles
^ Impinge. Baffle
D Weir/Lift
Count Installed Areo* X- T
'-t Chan. Noi. Necks "3 ^-4
. Chan. Not. Flonoes V4.^?<-fi
Channel Flanges * - h*f£
ff 1 Flto. Mood
Fife. Hi Flange
Clomp Ring
Bolts/Studs
" Tie Rods & Spacers i iff ) Nuts
* Shell
< Shell Cover
UJ Channel
Z> iff 1 Vessel Supports
tt
< Ch. Cover/Bonnet '•
a Shell Noi. Nocks
^frl
Shell No i. Flonges ,5 tr
Shell Flonges
GASKETS & PACKING
4- Shell Cover
ShelKChan. Side
/ Channel
l.y Channel Cover
~tce .' Fltg, HA
CHEMICAL COMPANY
SERVICE
s>i-l
/ cr
REVISION DATE
rfPLETE ALL IN
FORMATION
V
•1
c
r*t
f (~G*
0
MARKED
'IS CW ^> C~*
l«
HIHCIT
^
OF
I EQUIP. NO.
IV-6O 1 CL- "*j
HEAT
EXCHANGER
- SPECIFICATIONS
SPEC
Na
-309-
-------
'LANT
- Mn'-f/'c
FILE/JOS NO.
LOCATION
BLOG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS /
B/M NO.
P. 0. NO.
DUTY/UNIT /2J
Tetol Flow
Ib/hr
Liquid
Ib/hr
Density
Ib/cu ft
Viscosity
CS-CP
Specific Hoot
10
Thermal Conductivity
Btu/hr-lq ft.°F/ft
Vopor
Ib/hr
Mol Wt
Polity
Ib/eu ft
Viscosity
CS-CP
Sped fie Heat
Btu/lb-eF
Th»miol Conductivity
Btu/hr-sq ft.°F/ft
Latent Heat
Btu/lb
Non- Condon sables
Ib/hr
M.W. i
M.W. ,
V«lucity Mox./Minj
ft/sec
Norm. JMoH. OporoMng Tomp.
ID i
Operating Pr.il. (lnl«t)
ptig
Prostur* Drop
pii
Allow.
5
Cote.
Allow 2-
Colc.
Film Co.lf.
BTU/Hr. Sq. Ft.
23
Foulinq R«sistonc*j
hr-tq ft-'F/Btu:
24
Over-all Coefficient- "U'o
Btu/hr-5q ft. °F; Clean
Servi ce
LMTD (Corrected^ If) S "f
25
Inttulled Area/Unit
*q ft (Outside) Including-EKcluding Areo in tube theets.
28
SHELL SIDE
TUBE SIDE
Shell ID (Appro»imot»)
In.
De«ign Temporoturo
No. Tub«s (Appioxtmata)
247
Design Pressure
psig
Tube OD
in. TTube Gage l"1 BWC
HydipstoHc Test
piig
7 .C
TubeL»ngth
Corrosion Allew./Llnlng
in.
Tube Pitch ADO
In.
Number of Posses
Joint
32
Insulation
Moke/Type Flnlubes
Cross Baffles: Type
; Segment Cut
No. Fins
Number
Spacing Approx. Equal - See Sheet No.
per tube;
per In.
Fin Height
in. Fin Thick.
in.
P ro vi de
in. Horizontal Cut on Bottom for Condensate Drain
Vecsel Supports Saddles - Lugs Other;
Long Boffles: Type
Weir Height
Shell After Weir
i numoer nvir ncigni in.; onvil MTTBT r
j Cendensote Lift Yes • No |R»movoble Bundle Y«s • No I'Cothedic Protection Yes -
Yes /No) I Code { ASME* Notional Board Other. I Stami
O
Impingement Baffle Yes-No
No
TEMA Closs
Lethal
I Stomp
Yes.
Spot Roalegrotth/^uShell Shell CoveT Channel [stress Relieve; /v'l>6hell Shell Cover Channel
Floating Hood
Weight Complete Empty/Full of Woter
Ifa I Weight Bundle Only
Ib
41
Sandblast:
PoInt!
Shell ID
Tube Count
Installed Areo» %•
Service
nlet
Outlet
Drain
Vent
Mk
SHELL SIDE
Si i.
8'
Rtg
ISC.
Fact
Type
TUBE SIDE
Mk
Slle
Rtg
Face
Typo
See Noitle Sketch on Sheet No.
56
Shell Side:
Parallel Banks of
Shells In Series
Tube Side;:
Parallel Banks of
Shells In Series
Stacked;
Wide
High
Tubes'
\£jA
Slot Tube Sheet
Fltg. Tube Sheet
Cress Bof./Tube Sup.^ '
Lend Baffles
Impinge. Baffle
Welr/Llft
Tie Rods & Spacers
Shell
Shell Cover
Channel
Ch. Cover/Bonnet 3 C~'
Shell Not. Necks
Shell Noi. Flonges
Shell Flanges
Chan. No *. Neck i
Chon. Noi. Flanges.!
Channel Flonges
Fltg. Head
Fltn. Hd. Flange
Clomp Ring
Belts/Studs
Nuts
Vessel Supports
GASKETS & PACKING
Shell Cover
Shell.Chan. Side
Channel
Channel Cover
Fltg. Hd.
SPEC BY
CHECKEDi
APP'O:
ATE.
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
ENDOfl TO COMPLETE ALL INFORMATION MARKED
171(0 2-e«
COUI*>. NO.
g-v
HEAT
EXCHANGER
SPECIFICATIONS
SPEC.
NO.
-310-
-------
PLANT ftp/} / -
LOCATION
MANUFACTURER
/V/r^y £-J£
MODEL/TYPE
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
21
22
23
24
25
26
27_
28
29
30
31
32
33
34_
35
36_
37_
38
39
40_
41_
42
43
44
45_
46
47_
48
49
50_
51
52.
53
54
55
IU
3RMANC
li-
tt
UJ
.J
<
Z
0
<
Q£
UJ
0.
o
DESIGN
CONSTRUCTION DETAILS
NOZZLE SCHEDULE
DATA (
Fluid
Flow-Proce*» Bo* s
Flow. Filter Boiii
Deniity
Viscosity
pH
Solid* in Stream
Ib/hr
Ib/hr
Ib/cu ft
centipoise
vol.K4wt.X)
microns
Normal Max. Oper. Pre**. p*ig
Normal Max. Oper. Temp. °F
Allowable Pre«*ure Drop p*l
Maximum Cake Volume
3 f /•J'fSS' /^
BLDG. NO.
NO. UNITS / ,
£> tJ >/-,-'/*/ FILE/JC
CHARGE
{?'*/" 'h'S?/1* B/MNO
P. 0. NC
NO. UNITS OPERATING / f)rt flt"> SPARES
'73>EED
/ 3 &L &O(a.
O.6> 7 Spf.
' /
27
b£ b£
j &>o /£o
JO
73) FILTRATE BACK*
JfAfihrhA* fi/ftfth 1
/ %ft &Ot& '•/*/}*
)B NO. '?3>£'£% *>
: NO.
).
/Vr^Jei.
ASH CAKE
/; et. £03 f
'.'ft? tf£<7
'
: Type Discharge: Wet Cake-Dry Cake
Cycle: Precoat Preparation Time •— ;
Filter Aid Preparation Time •"• ;
Filtering Time £of) "ft S)lS G t* iJ ;
Precooting Time
Filter Aid Application Time
Slowdown Time
Cleaning/Backwash Time
Total Time Between Successive Filter Cycles
aj £«_
Filter
Design Pressure psig / 22.
Design Temperature
Hydrostatic Test
Corr. Allow./Lin.-Sh.l
Joint Efficiency-Shell
Insulation
°F Zc.
psig ZC.
\ Heads in. o
0
Filtrate Tank Code:
Stomp Required: YescNoJ
Radiograph:
Stress Relieve:
Spec! a Design:
Notional Board
Weatherproof Explo*ion
No.
Proof '
Other:
Piping, Valves. Fitting* Supplied with Filter to
be n Accordance with:
A/O i~ /P«"*7 'cf
Filter Tank: Horiuntal • Vertical: Size rf C 1 C. in. IDx
Element*: Area/Element sq ft; No. Req'd ;
Leave*: Area/L_eaf
«a ft: No.
Element or Leaf Pore Size (Ava.)
Maximum Coke Thlckn
Precoot Req'd: Yes -
Filter aid Req'd: Yes
ess
rfoj Material
<5rf Material
by Ou,>nff
Maf I (Wetted Parts)
tn. Ton to Tan; Type Heads
in. IDx
in. ODx In. Length
?eq'd : Leaf Height n.; Leaf Spacing in.
microns; Minimum Particle Size Retained
• micron*
n: Gross Filter Volume ool-cii ft: Heel Volume aal - cu ft
Filter
Make
; Type Seal
Fabric: Material 3 O 4-
Model ; Max.
; Mesh 4-OO
Flow oom at D>ia
; See Pump Spec No.
Other Accessories:
Packaae Unities)- No: Shop Assembled on Skids^esV No: Fleer Space Req'd ft x
Weight Empty/Full of Water
Service M
Inlet
Outlet
Vent
Drain
Relief Valve
Pressure Gage
Quick Open Cover
See Nozz e Sketch on
SPEC OY f^pft
CHECKED: SEf
, , ^»
APP'Di ~^
DATE: ^,/*7/'7^J Re
VENDOR Tfe COMPLETE ALL 1
ark No. Size R
A
B
C \
D AC A
E Ifr,* l
F £ A<*
G ' 0
H
J
K
Sheet No.
/ Ib; Shipping Weight
g. Face Type
.
1"
n '
"
MATERIALS
Item Thickness Ma
Filter Heads in.
Filter Shell in.
Lining in.
in.
Elements
Leaves
M.H. Cover
Bol It/Studs
Nuts
Gaiket*
<3f£> THE DOW CHEMICAL COMPANY
!VICE
VISION DATE A
NFOHMATION MAMKCD
T,4f>fe&0 <SK
• r
C SF
IjtHKCT OF N
ft: Height ft
Ib.
t'l Class Mot'l-Mlnimum Quality
3o-
-------
PLANT f*/i0 /* f^^/rifti ^U/'t'l/f ff&?m/Ofa/ FILE/JOBNO. 73G£Ji^)
LOCATION
MANUFACTURER
BLDG. NO. CHARGE NO.
NO. UNITS 'Losr 7r#f'*? B/MNO.
' P.O. NO.
MODEL 4 y £> -/3
1
~2~
3
4
~r
6
7
8
9
To"
11
12
13
14
TT
16
17
IB
19
20
21
22
23
24
25
26
27
"2T
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
IT
46
47
48
49
"so"
51
52
53
54
55
Z
Vp
LU 2
t-
UJ
D
R
r-
r-
Z
U
ERIALS
t-
•*
LU
ce
r-
LU
NO. UNITS ASA PUMP QYES QNO ASA DESIGNATION
Liquid Pumped M&h/}-f-/)tf f7s*&{Lf5 •>££>// f& ?*J
Pumping Temporoture (P.T
/& O °F
Specific Grovity ot P.T. f & *f
Vopor Pressure at P.T.
Corrosion or Erosion Factors:
Arrangement; ^lorix)*Vert..
Mo». Capacity at P.T. irecj>l Gear . Belt
Mounted by fr%* f)£/£>P
SF Temp Rise °c
Frame
£3 hp
Nominal Motor Size (Non-overloading) C^ £} hp
Speed / */£& rpm
Volts £ && '• Pnos" ^ /' Cycle ^5/*^>
Speed Reducer; integral - Separate
Mfr.
Model
Ratio
Closi
See Driver Specification No.
Performance Curve: p*«s> No; Curve No.
Hydrostatic Test; ft'esj* No; Pressure psig
Shop Inspection; Yes \ttoj
SPEC. BY^-^_^,' ^
CHECKED: SERVIC
APP'D: O-j
Steam Turbine: Make Mounted by
Model:
Horsepower hp ; Speed rpm
nl«t Steam Press., psig: Normal ; Max
Inlet Steam Temp., °F: Norma ; Mox.
Wot»r Rote: Ib /tlr
Vacuum (If any) mm - in. Hg - psio
Back Pressure psig
nlet
Exhaust
Seria 1 Number
J Outline Drawing
^ Cross Section Drawing
Bulletin No. Page No.
y> THE DOW CHEMICAL COMPANY Jtfar* I &-/4+/$
*•> r-~ n ^ CENTRIFUGAL PUMP
1-tSEfitr £l/4P F&&£> WMP SPECIFICATIONS
PATEi 2Jj/j£f. REVISION DATE A 1 . j B
<"
VENDOR TO COMPLETE ALL INFORMATION MARKED K.U»T "' NO
1JB3TOO 4/73
-312-
-------
PLANT Cl/jA/- r^/fij r/C.
LOCATION
MANUFACTURER
MODEL _3tf^?-/3
1
2
4
5
6
7
8
9
10
11
12
13
14
15
17
IB
19
20
21
22
23
24
25
26
7T
28
"iT
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
"so"
51
52
53
54
55
s°
t/» O
u
ON DETAILS
CONSTRUCTI
1
Ul
t-
UJ
u
H
UJ
1-
' ^>(S / 'f'iS f -X^-'/.?'^' 'f / FILE
BLDG. NO. CHA
NO. UNITS IjrjSr 7/VrVO B/M
r P.O.
/JOB NO. s"^ '£ £ ^ 3
RGE NO.
*10.
NO.
NO. UNITS ASA PUMP X^ES Q NO ASA DESIGNATION
Liquid Pumped fi/A&S)~&f)O
Pumping Temperature (P.T. '
/t^ O °F
Specific Gravity at P.T. 0t (9**^
Viscosity at P.T.
cs-cp
Vapor Pressure at P.T.
Corrosion or Erosion Factors:
ArrongementfHorizjVert.- n Line
Direction of Rotation Facing Pump Coup
Case: Design Pressure
Max. Allow. Working Press.
Split: Horiz-Vert-Barrel
Impeller Diameter: Supplied ^7
Vent and Drain Tapped: Yes - No
Nozzles Size Rating
Suction e^. "
Discharge £ O
Vents
Drains
Cooling HzO
Max. Capacity at P.T.
Discharge Pressur* ±) Q
Suction Pressure / Cf
Differential Pressure / ^f
Differential Head
NPSH Available
NPSH Required (Water)
Suction^ingleJ Double
ing: CW - CCW Speed: /7£^O
^2.^? "*"
psia f».
psio ft.
psi
AS" ««•
ft.
ft.
rpm
psig Number of Stages / ;Shut-Off Pressure ft.
PSig Volumetric Efficiency at Rating
Impeller Type
X
/ inches; Maximum f£ inches; Minimum £f inches
Bearings: Thrust
Facing Location
Radial
Type
Type
Lubrication on Bearings; Oil • Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard; Yes - No
Baseplate: Ye* - No; Type
Water Cooling: Casing-Stuff. Box-Beorings-Pedestal-Gland^None) Total Water Required:
Smothering Gland: Yes ^lo)
Packing: Yes -VNoJ Type
gpm
Lubrication on Stuffing Box: Oil-£reaso^ono
Sealing Oil Connection: Yes - No
Mechanical Seal: Yes ^NqJ Furnished by; l/<£f) tj D f* •' M(r- T*P»
Single - Double-Inside-Outside-Balanced-Unbalanced
Rotary Unit ; Sea Ring ; Face Material
; Shaft Pocking
Insert ; Reversible: Yes - No ; Face Material
Insert Mounting: Clamped In
- "0" Ring - Press Fit
Gland ; Plain: Yes -No Throttle Bushing Carbon: Yes -No ; Other
Gland/Stuffing Box Machined & Tapped for; Dead - End Lub. - Circulating Lub. - Quenching -
Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes
Weight of Pump
Weight of Driver
-No
Ib; Weight of Base
Ib; Shipping Weight
Casing & Covers: 3 / &>
Cosing Wear Rings: (9
Impeller:
Impeller Wear Rings:
Stuffing Box Bushings:
a
u
*
Ib
Ib
Shaft: 3*U>
Shaft Sleeves:
Lantern Rings:
Glands :
Gaskets:
Furnished by: yj& /~) ^f '^3 /* ; TypefETecI Motor)- Steam Turbine - Other
Electric Motor: Moke Mounted by Jtff/J&ffi f
Enclosure- f&fSC SF
Temp Rise °c
Insulation Frame
Estimated BHP Req'd.
Nominal Motor Size (Non-overloading]
/O "P
/S hp
Speed /7^& 'Pm
Volts 4-4-Q ; Phase j!>,
Model Class
; Cycle g,O
See Driver Specification No.
Performance Curve: ^Yes)- No; Curve No.
Certified: Yes ([No)
Hydrostatic Test; ;Ye>- - No; Pressure
psig
Shop Inspection: Yes SNo)
Steam Turbine: Moke
<6irecr) Gear - Belt
Mounted by
Model:
Horsepower
Inlet Steam Press., psig: Normal
Inlet Steam Temp., F; Nor ma
Water Rate:
Vacuum (If any)
Back Pressure
Inlet
Exhaust
Serial Number
(J Outline Drawing
y Cross Section Drawing
Bulletin No.
SPEC. BY f= p )j <3^" THE DOW CHEMICAL COMPANY
CHECKED: SERVICE
DATE: 2^7/py REVISIONDATE | t
eeo Sbuw reeo *>*i>
B
c
VENDOR TO COMPLETE ALL INFORMATION MARKED [f«i_ir.TT ntr
hp ; Speed rpm
; Max
; Max.
Ib/hr
mm • in. Hg - psia
psig
Page No.
}t4oo | *P-P$fc&
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
18370O 4/73
-313-
-------
PLANT Cna./- /V/V//C 5ts/-fes/' /^,e>/s ,^i-'sr/ FILE/J
LOCATION BLDG. NO. CHARG
MANUFACTURER NO. UNITS / /^>/» 7/&//) B/MNO
P.O. N
OB NO. 733 G>&3
E NO.
3.
MODEL /XV?-<£5 NO. UNITS / ASA PUMP l^YES O NO ASA DESIGNATION
1
2
3
4
^>
6
7
8
9
10
TT
12
13
14
15
16
17
IB
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
i/l
Z
UJQ
£3
U
ON DETAILS
u
h-
2
U
o
<
or
UJ
r-
U)
a
H
UJ
Liquid Pumped St£ I^Uf*
Pumping Temperature (P.T.) J2-4S <6 °^
Specific Grovity at P.T. SL^^
Viscosity at P.T. ^^ &&t'Se. *"*B"
Vapor Pressure at P.T, *2OO /97 f??
3'foa f>* J(?£££ Jgd - /ZL$p^ No; Type Sealing Oil Connection; Yes .^Ng/
Mechanical Seal: Yes {No} Furnished by; ; Mfr.
Type
Single * Double-lnside-Outside-Balanced-Unbalanced
Rotary Unit ; Sea Ring ; Face Material
; Shaft Packing
Insert ; Reversible: Yes - No ; Face Material
Insert Mounting; Clomped In - "Q" Ring - Press Fit
Gland ; Plain; Yes -No Throttle Bushing Carbon; Yes -No
; Other
Glond/Stuffing Box Machined & Topped for; Dead - End Lub. - Circulating Lub. - Quenching - Vent & Drain %^/£[£j^£ f'&^f
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing BOX Req'd: Yes - No
Weight of Pump Ib; Weight of Base
Weight of Driver Ib; Shipping Weight
Cosing & Covers -Sf^/tfg fc e* / ' £)£/ffT'//£. ' /V?/7
Cosing Wear Rings: /*• f/
Impeller: ft /'
Impeller Wear Rings: // /'
Stuffing Box Bushings: // //
Ib
Ib
Shaft: t_5"/i^£ /
Shaft Sleeves:
Lantern Rings :
Glands:
Gaskets :
Furnished by: ; Typ«£Elec. Motor/- Steam Turbine • Other
Electric Motor: Make Mounted by ts$2>S}£/fl /*
Enclosure J~£ f "g SF Temp Rise °c
Insulation Frame
. Estimated BHP Req'd. £ hp
Nominal Motor Size (Non-overloading) 7/H^ ^P
Speed I75O 'pm
Volts 4*£& ; Phase ^ ; Cycle & C)
Speed Reducer; Integral - Separate
Mfr. Ratio
Model Class
See Driver Specification No.
Performance Curve: ^e>/- No; Curve No.
Certijjed: Yes ^Na)
Hydrostatic Test;(Ve&}- No; Pressure psig
Shop Inspection: Yes O^2/
Steam Turbine; Moke
/Tfir.cl^ Gear . Belt
Mounted by
Model:
Horsepower
Inlet Steam Press., psig: Normal
nlet Steam Temp., °F; Nor mo
Water Rate:
Vacuum (If ony)
Back Pressure
Nozzles Size R
Inlet
Exhaust
Serial Number
J Outline Drawing
hp ; Speed rpm
; Max
; Ma«.
Ib/hr
mm - in. Hg - psia
psig
ating Facing Location
y Cross Section Drawing
Bulletin No.
SPEC. BY £p/J THE DOW CHEMICAL. COMPANY
CHECKED: SERVICE
APP'D: ^ULFCJK LOAD/*
DATEl £ -7- 7V/ REVISION DATE A B
'* &»,*>
c
VENDOR TO COMPLETE »LL INFORMATION MARKED Ij.urrT n» H
Page No.
J6O& \ X13N0'
CENTRIFUGAL PUMP
SPECIFICATIONS
PEC.
0.
18370D4/73
-------
PLANT coaf- w/*t f/e. 3tt /1-vr Remava / FU-E/J
LOCATION r BLDG. NO. CHARG
MANUFACTURER NO. UNITS/ &£/* 7/-^?/V? B/MNO
P.O. NO
38 NO. ;?3/96 Z ^3
E NO.
.
MODEL /ie/'/ NO. UNITS ASA PUMP &YES (UNO ASA DESIGNATION
1
~
3
4
~
6
7
e
9
10
11
12
TF
14
TT
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
~47~
48
49
50
51
52
53
54
55
«,
By
£5
1/1 u
ON DETAIL
r-
CONSTR
2
oe
UJ
i
Ul
o
lu
Liquid Pumped /\fQ A>A />7 &+
Pumping Temperature (P.T.) J&7) &/&/'} r °^
Specific Gravity at P.T. » ^^ £»*7
Viscosity at P.T. cs-cp
Vapor Pressure at P.T.
--— *_
Max. Capacity at P.T.
/O w
Discharge Pressure P*'o 4*& '*•
Suction Pressure
Differential Pressure
Differential Head
NPSH Available
NPSH Required (Water)
p»io /O '*•
pli
SO "•
ft.
ft.
Arrangement{Horuj}-Vert.-|n Line Suction^Single)- Double
Cose; Design Pressure psig Number of Stages / ;Shut.
Max. Allow. Working Press. psig Volumetric Efficiency at Rating
rpm
Off Praisur* ft.
X •
Split; Horiz-Vert-Borrel Impeller Type
Impeller Diameter; Supplied £ JF inches; Maximum Go^*f inches;
Vent and Drain Tapped: Yes • No Bearings: Thrusl
Nozzles Size Rating Facing Location
Suction / %2i **
Discharge / //
Vent.
Drains
Cooling H20
Radial
Minimum ^ /1^ inches
Typ.
Typ.
Lubrication on Bearings; Oil * Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard; Yes - No
Baseplate: Yes - No; Type
Water Cooling: Casing-Stuff. Box-Bearings-Pedestol-GlonojKRone} Total Water Required;
Bpm
Smothering Gland: Yes O^ Lubrication on Stuffing Box: Oi l-Greose^one
Mechanical Seal: ^i»l/- No; Furnished by; M^rt fJf3 /* ' ^'r-
Typ.
Single - Double-|nside-0ut»tde-flo fonced-Unbolanced
Rotary Unit ; Seal Ring ; Face Material •
; Shaft Packing
Insert ; Reversible; Yes - No ; Face Material
Insert Mounting: Clamped In - "0" Ring - Press Fit
Gland ; Plain; Yes -No Throttle Bushing Carbon: Yes -No
Oth»r
Gland/Stuffing Box Machined & Tapped for; Dead End L'ub. - Circulating Lub. - Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing Box Req'd: Yes -^4o)
Weight of Pump • Ib; Weight of Base
We.ight of Driver Ib, Shipping Weight
Cosing & Covers: J^L/tL ~f-/ * /£* .7^*^5/7
Casing Wear Rings: H ft
Impeller: " '/
Impeller Wear Rings: " "
Stuffing Box Bushings; // . __I"
Ib
Ib
Shaft: v_7y*c^ff f
Shaft Sleeves;
Lantern Rings ;
Glands;
Gaskets;
Furnished by; l/ff*/Jc/& (* ', Type(Elec. Motojt/- Steam Turbine - Other I
Electric Motor; Make Mounted fytf??f)£/&f*
Enclosure T^A/ ^ SF Temp Rise OG
Insulation Frame
Estimated BHP Req'd. £>„ 3 hp
Nominal Motor Size (Non-overloading) J hp
Speed f*7£) £J rpm
Volts 4-4-O ! Pha*« ^ ; Cycle &Q
Speed Reducer: Integral - Separate
Mfr. Ratio
Model Class
See Driver Specif icattjjn^No.
Performance Curvet/Yes/- No; Curve No.
CertTTTed : Yes ^ Ncp
Hydrostatic Test; ^'•>rt-J^0< Pressure psig
Shop Inspection: Yes <(Ng/
Steam Turbine; Make
j Direct^ G*or . B.H
Mounted by
Model:
Horsepower
(nl«t Steam Press., psig: Normal
Inlet Steom T»mp., F; Norma
Water Rate;
Vacuum (|f any)
Back Pressure
Nozzles Size R
nlet
Exhaust
Serial Number
J Outline Drawing
5 Cross Section Drawing*
Bulletin No.
SPEC. BY £j~fj . THE DOW CHEMICAL. COMPANY
CHECKED: SERVICE
APP'D: *3OL(/£'MT A'frfKec
DATE'2~7-7*£ REVISIONDATE A B
•f fk>»lf>
c s
VENDOR TO COMPLETE ALL INFORMATION MARKED ||.._.rr» nm H
hp ; Sp««d rpm
; Max
; Ma«.
Ib/hr
mm • in. Hg - psio
piig
Pog« No.
/4OO | /£-uJrNO
CENTRIFUGAL PUMP
SPECIFICATIONS
PEC.
0.
1S370D 4/73
-315-
-------
PLANT f?pa/~ /•y/*/7t/!
1~
2
3
4
B
6
1
8
9
10
11
12
\3
14
IS
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
MATERIALS
UJ
CHEDUL
UJ
_l
N
N
Z
Op.f. Press.- Positive Vacuum /O>"- HzO) 2- a>
Operating Temp.ratur. °F /£> G
Liquid Sp.cifit Gravity st In. HaO FU 1 1 O / ftfStffff*
Sh.ll Heads Corr. Allow, in.
Sh.ll H.adi Jrint E«. 51
Cod.: A f~* ^~ Stamp Yas ^NoJ
Radiograph: /VO Str.iss R.li.y.: A/ O
Typ. Supports: £^ f f~l £) f^OtJ fld&'f t Gt*)
Insulation: f
Fir«prooftng: \f G S
Sandblast: Afo • Paint: A/O
Manhol. / Hing.d (/Covi(.d') Orh.r:
Platform Clips: V'fSS |Lodd»r Clips: y^ Insu . Rinss:^^^
Pip. Supports: " '
Wind Load: Sdsmlc:
Wt. Empty Ib Wt Full
Itwn Thiclin.ss Mat'l Class Mat'l - Minimum Quality
Shell n. •Sf'SS ' /
Con. Roof n. ''
Bottom n. "
Lining n. d& 1 1 QtOlf* £>4~
n.
n.
Noni»N.cks 'i /.inect
Fiong« " Facfe/
Counllna A/i? l~l C.
M.H. Cover £&ilCot£ KICZQ
Supports
Bo Its/ Studs
Nuts
Gaskets
Service Mark No. Size Rating Face Type
"Xnleifss A / 3" I5c? EF
" /^3) B / 4" "
11 (So) c / &" " *
» P / ?" " "
Veni f2of) E I 2." "
^5 F / THE DOW CHEMICAL COMPANY
CHECKED: SE™'CE ffm ,_ c f
APP'D:
DATE: 2/7/74^ REVISION DATE A B
•£VO 779«K
C
~v
)
~'-Ji*
1 7 /
,* —\ n
*
I ^ ^> _ 1 EQUIP. MO.
J4OO T-t
VERTICAL TANK
SPECIFICATIONS
SPEC.
-316-
-------
>LANT (Lf>O/~ /•'Vf/Tt'f J5u /Jar f*0m0i'tT/ FILE/JOB NO. 73o& £ sf
LOCATION ' BLDG. NO. CHARGE NO.
MANUFACTURER NO. UNITS / ftf r "Tr^i'r1 B/M NO.
P. 0. NO.
FIELD ERECTED CvEs) NO NO. UNITS NOMINAL VOLUME fOO, GOOtftl
\
1
3
4
5
6
7
t
9
10
n
12
n
14
15
16
17
18
19
20
21
22
23
74
25_
26
27
28
29
X
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
MATERIALS
E SCHEDULE
N
Op«t. Press.-Posltive Vacuum JO In. HaOJ (£. o>
Operating Temperature °F / &O
Liquid Specific Gravity ^2 *£ T
Contents Lethal . Yes ^Ro^
Dos. Pross.->Pesitlvo | Vacuum /^In. Haul ^ Ol
Dosi^n T«fnporatur» °F ^rt/3
Hydro. totic T.it in. HaO f\fi / f Offt/Q'f-e.P
Shall H.od. Cerr. Allow. In. 1
Shdl H.odi Jdnt Eff. * 1
Co Other:
Platform Clips: V<£.S |LadderClips:y^5 | Insul. Rings: yft£
Pipe Supports:
Wind Load: Seismic:
Wt. Empty Ib Wt Full
Item Thickne s Mar1! Clan Mot'l - Minimum Oudlly
Shell n. ib f « -2 /
Cone Roof n. •
M i'*
Bottom n.
Lining n. Ll£./ ' /{.C f~£. &&
n.
in.
Noiile Necks (2 THE DOW CHEMICAL COMPANY
CHECKED: SERVICE ^
APP'D:
DATEi 2/7/7// REVISION DATE A 1 0
VENDOR TO COMPLETE At-L INFORMATION MARKED
'.m,T St,*«e
c
HIHCKT OF
. > 1 COUIr>. NO.
/4oo \r-z.
VERTICAL TANK
SPECIFICATIONS
SPEC
NO.
-3 IT-
-------
PLANT f£>(2/~ /c^//~'/ ~f~i d ~5c/ /J ts r* /&?m 0 S& / FILE/JOB NO. 730£>Z.?>
LOCATION ' BLDG. NO. CHARGE NO.
MANUFACTURER NO. UNITS / fj ? r 7V/> / '? B/M NO.
P. 0. NO.
FIELD ERECTED G&
Liquid Specific Gravity 2.O
Contents Lethal Yes CNo5
Des. Press.-Positive | Vacuum /S in. HjO 3 o»
Design Temperature °F *3O£^
Hydrostatic Test in. HzO Ft/// f3-f MfoT^f*
Shell Heads Corr. Allow. in.
Shell Heads Joint Eff. %
Code: A P X Stamp Yes <5fr^
Radiograph: A/fc> Stress Relieve: A/O
Type Supports: /€:»? SJ F&£J/~)Q[<3 + /' O O
Insulation: /
Fi reproofing: /Vt?
Sandblast: At> Point: AfO
Manhole/ Hinged /6ovit.d> Other:
Platform Clips: ^ffS Ladder Clipsi/fJ Insul. Rings: )/«?£
Pipe Supports:
Wind Load: Seismic:
Wt. Empty Ib Wt Full
Item Thickni s Mat'l Class Mat' . Minimum Quality
sheii n. 3fee/
Cone Roof n.
Bottom . n. "
Lining ' n. A/O 1 <&
n. '
n.
Nozzle Necks v_5V££'eJ/
FI onges
Couolina
M.H. Cover «
Supports
Bolts/Studs
Nuts
Gaskets
Service Mark No. Size Rating Faco Type
^L*-}!p~r . A / z.'1 \£>o PF
J ^ B ^ h M *
TS c 1 7»
Off-tlsl D / 4" H "
Yen* E ( 2." • "
-5r ^ ft tii • F j \ i" ;,:<-r>'/; /We H / 2^" y-s* ef
j
K
L
M
N
P
* Nozz e to be p'luogad or Blinded.
NOMINAL VOLUME 2.4-OQO <**&
VESSEL SKETCH
V
B
^ i_ f^&>*
tf r /^ a ^"<^J
/^ h
^3 oo °/-' ^v/ T^ /O THE DOW CHEMICAL COMPANY
CHECKED: SERVICE , , - . ~ ^-
APP'D:
DATEi 2-/7/7^ REVISION DATE A B
~&e
c
VENDOR TO COMPLETE ALL INFORMATION MARKED HflVf T ftm
"\
1
£
•>%>
^•11
^ i
x'H D
•Jey/s)-/
-------
•LANT £e>o /• &./ ft •/*'/• ^L/ff~i/r f&snava/ FILE/JOB NO. 73/C62. -5
LOCATION ' BLDG. NO. CHARGE NO.
MANUFACTURER NO. UNITS / /) p r Tf f> t' n B/M NO.
P. 0. NO.
FIELD ERECTED YES Cud) NO. UNITS •' NOMINAL VOLUME ^TOOOGff/
\
3_
3
4
S
t
7
t
9
10
11
12
13
14
IS
16
17
18
19
20
21
22
23
24
25
26
77
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
4«_
47
48
49
50
51
52
53
54
55
DESIGN DATA
i/>
_i
S
I-
2
lu
U
0
LU
I
u
LU
_J
N
M
Oper. Press.-Pesitive Vacuum /O '"• H2OJ ^** 01
Oparating T*mp*roturv ^F ^4 fT} L) / f/J^v
Liquid Specific Gravity £3, 67
Contend Lethal . Yet I'flD
Oe>. Pre>s.-Poilrlve | Vacuum /£ >n. H:OJ ^ 01
De>ian T«nperature °F /£> O
Hydro. totic Te«t In. H*0 /%*// V^O
Type Supports; £?//7£) /~f3tJf7CfO "f~SO f?
Insulation: yV^O
Fi reproofing: ^^ ^
Sandblast; y 'f £ ' 1 Point: f*rt'Syt€~
Manhole / Hinged rCavTted Other:
Plotfemi Clips;yg'S {Ladder Clips:1^ ^| Insul. Rlngs:/\/^
Pipe Supports:
Wind Load: Seismic:
Wt. Empty Ib Wt Full
Item Thickness Mat'l Class Mot'l . Minimum Quality
Shell In. £>•£-££/
Bottom n. "
Lining • n. A/ ' C'f) £*
n.
n.
Nonle Necks ^-f"£ S /
Flanges '•
Couollna "
M.H. Cover M
Supports
Bolts/Studs
Nuts
Gaskets
Service Mark No. Siie Raring Face Type
TV) 1 fl 'i" A / 3 '* 1 G& £"f~
AS B / 4-" " *
i~T c/2" " •
.vvnt D / 2" •»
C.V + IS+ E / 2" 'i •"
Manhole. F / w zs* «
G
H
J
K •
L
M
N
P
* Neule to be Plugged or Blinded. .
VESSEL SKETCH
V
IT' • '1
S-
J^
£ r
•>
:\
J
\
D
^^ A
'
HP
-fC .
For Further Details, See Sheet No.
SPEC BY £f# <3J$t> THE DOW CHEMICAL COMPANY
CHECKED: SERV'
-------
PLANT /
LOCATION
MANUFACTURER
"a a/- /?•//'/?/£ J>v/-fejr
X^
isrjas&S FILE/JOB NO. 73063. *
f BLDG. NO. CHARGE NO.
NO.UNITS /AfrTr/ti'n B/MNO.
'. P. 0. NO.
TYPE 'Pis-h' II a +-i C- i IFIELD ERECTED
1
2
3
X
5
6
7
8
9
10
n
12
13
u
IS
16
17
18
19
20
21_
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
DESIGN DATA
ERNALS
t-
z
•ri
i/)
•<
or
t-
ATERIAL SPECIFICATIONS
2
3
3
n
UJ
«/1
UJ
Nl
O
"
Op. Press. 'J ^ psig Op. Temp. Q ^ C2 °F
Des. Press. ^O P»'fl Des. Temp. ^ &~t^ °F
Max. Allow. Press. (New & Cold) psig; Limited
Hydro. Test "7 S" psig I Code: A
By
Stomp ^T es> No
Radiograph
Stress. Rel.
Sondblust: A/C?
Paint: /V O
Platform Clips: yV O Ladder Clips: /J &
Pipe Supports: ' Insul. Rings: \Xf" *?
Wind Load: Seismic:
Shipping Wt. Ib Wt. Full
Tray No
/ Thru '•
Thru
Thru
Thru
. Diom. Spacing) Type Matanal
Ib
Tray .Installation
5 <3» 18" Ea/k -4-
Zo 4- P^fc &A
Me n f
~^>£>4- £&&*•£- '
Sfee./ 7- >t
Z" » "
TOWER SKETCH
, lt .
T -O Di&sn&Tgf*
$ <^5> THE DOW CHEMICAL COMPANY T^OO \ "/- /"*'
SERVICE /
ivi"-.- i' t >' • / , ~ - • — f~
APP'O: ^ ' '
DATE: 2/7/7L/ REVISIONDATE A
VENDOR TO COMPLET
C ALL INFORMATION M A R 1C F n
-V.
B
** £/±T dr L. TOWER
SPECIFICATIONS
c
SPEC
|H«r c, na
-320-
-------
PL'ANT
LOCATION
COAL <• f*\
MANUFACTURER
'j&tr/t: JT^/./^/P je/rMici'/)-^
BLDG.NO.
NO. UNITS / fx>r Tra r'rj
"
FILE/JOB NO. ?3£ £J "Z
CHARGE NO.
B/MNO.
P. 0. NO.
FIELD ERECTED YES f HO) |NO. UNITS - [TOTAL VOLUME /4OO GAl.
1
2
3
4
5'
6
7
S
9
10
11
12
13
14
IS
16
17
18
19
a
21
22.
23
24
25
26
27
28
29
30
31
32
33_
34
35
36_
37
38
39_
40
42~
43
44
45
46
47
48
49
50
51
52
S3
54
55
VESSEL SKETCH
DESIGN DATA
MATERIALS
(*
\_
Operating Pressure "* ,
Operating Temperature
Liqui
d Specific Gravity
Contents Lethal
Design Pressure
Desip
w Temperature
Max. All. Prels. (New&GW)
Limited By
Hydrostatic Test
Shell
Shell
Code:
Heads Corr. Allow.
Heads Joint EH.
(4-5 A 7 fc
Radiograph: ' A/0
. /O'-O1' To. To Ten.
A B &
T r T
\ '/
'...,v
pslg US
0 F /tt O
0.&7
Yes No
Stress Relieve: /V O
Notionol Board No.
Item . Thickness
Shell
Heads
n.
n.
Lining n.
n.
n.
Not. Necks
Flonaes
Coupling
M.H. Cover
Supports
Bolts/Studs
Nuts
Gaskets
SPEC or^e/C/)/ «
CHECKED:
SERVI
APP'D:
DATEt t/7f
VEnriOH TO C
/7«y REVIS
Mali Class Mat'l-Minimum Quality
' *>04
II '
*>o4.
304. F^&eA.
/Yf/JC.
3s 4- Feyf.-faC
.Sievl
^yl D
Q \
V| •^^••••pws-*
For Furth«r Details S*. Sh*«tN«.
Typ» Supports: *5&.£*£y/&5
Insulation: /"
Fimproofing' */€$
Sandblast: yVfe Paint; N O
Man hoi • / • Hlngad .^DaviuO Other:
Platfenn Clips* A/o
Pip* Supports:
Ladder Clips: A/O
Intul. Rings: V(> S
f
Wt. Empty Ib
S«mc* Mark
7y? /" /C'O /f'F
£t, // *
2." '/ *
2_ •• " "
£>• t, >i
Zo" i-5& "
• Nonle to be Plugged or Blinded
33S&> THE DOW CHEMICAL COMPANY
CE
>*} ,****• , < * ,7 ' * ' >d '7~s?i /^
/*^ CC ^ /• / ~ *.- <7 / U> *~-
IONDATE A B
C
/4oo | T-Y°
HORIZONTAL
DRUM
SPECIFICATIONS
SPEC,
NO.
17740 2-OS
-------
PLANT Ca£.
LOCATION •
*f~ fy
T/fr
4 .
r^
/f
t/r
fCfttf
B LOG. NO.
MANUFACTURER
NO. UNITS j
76*
' £
*}
•>er Tr
FILE/JOB NO. '/ 3&$y£. "3
CHARGE NO.
•7/ /? B/M NO.
' P. 0. NO.
DUTY/UNIT 3OO> OOO
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30_
3J_
32
33
34
35
36_
37
38
39
40
41
42_
43
44
45
46_
47
48
49
50
51_
52
53
54
55
56
UJ
a
>-
K
K
2
UJ
2
O
u.
O
111
u
2
PERFORM/
_l
_i
UJ
X
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a
u
O.
•«•
DESIGN DAT
_>
_i
UJ
NOZZLES PER st
2
I
Horiz. (
tfe^rl) Sloped °
BTU/HR
(NO
to horiz.
Flooting Hd.-Pull Thro- Clomp Ring-Packed
.UNITS ISHELLS/UNIT
^FTSjvlth Exp. Joint
Thermosyphon
Additiona Pmc. Data on Sheet No.
Fluid
Total Flow
Liquid
Ib/hr
Ib/hr
Density
Viscosity
Specific Heat
Thermo) Conductivity
Vopor
Mol
Wt
Density
Ib/cu ft
CS-CP
Btu/lb.eF
Btu/h»sq
Ib/hr
ft.°F/ft
Ib/cu ft
Viscosity
Spec! fie Heat
Thermal Conductivity
Latent Heat
Non-Condensables
Velocity Mox./Min.
Norm.
Max. Ooerating Temp.
Operating Press. (In et)
Pressure Drop
Film Coeff.
Foulina Resistance,
Over-all
Coefficient-
"U'o1
CS-CP
Btu/lb.°F
Btu/hr.sq
ft-°F/ft
Btu/lb
Ib/hr
ft/sec
«F
psig
psi
BTU/Hr. Sq. Ft.
hr-sq
ft-'F/Btu:
Btu/hr.sq
ft.°F;
Installed Area/Unit / *y £2
Design Temperature
Design Pressure
»F
p>ig
Hydrostatic Test . psig
Corrosion Allow./Linlng
in.
Number of Passes
Insulation
Inlet
U-Tube
Fintube
TEMA SIZE/TYPE
Kettle Coil Hairpin Box
Other:
SHELL SIDE - Outlet
WG
/ tiLi.O^'i
&c>ee>o
M.W. *
g£
Allow.
/PZ> \
Cole.
Clean
*q ft (Outs
SHELL SIDE
}J5
2. 2.5
—
/
de)
Service
ncluding>E»
TUBE SIDE
/£&
/_fTO
2.2.5
—
/
—
Cross Baffles; Type
Nu
mber
• Provide
Long Bo
files: Type
in. Hori zontol C
Impingement Baffle Yes/fto) j
TEMA Class t
. ethol
ut on
Condensate
Yes -
No
Spot Radiograph: Shell Shell Cover
—
; Segment Cut %
Sheet No.
Bottom for Condcnsote Drain
Lift
Co
;
Yes -i
de
Number
2,00
Inlet . TUBE SIDE - Outlet
/(O^/D //« OH •+
^OjOOO
'QOt'^ifO $Q&£)O
f. O& Si}*}1,
M.W. <
75" \ / ' /£~r\
Allow Cole.
LMTD (Corrected) / O °F
eluding Area in tube sheets,
Shell ID (Approximate) In.
No.
Tubes (Approximate) *y Q
TubeOD /'' in. ] Tube Gage // BWG
Tube Length /2 ' ft
Tube Pitch A OO A In.
Joint £&//4?C/
Make/Type Fintubes
No.
rins per tube; per In.
Fin Height in. | Fin Thick. !n.
Vessel Supports Saddles > Lugs Other;
Wei
^o)j Removable Bundle Yes^
ASME
Channel
National Board
Stress Relieve: Shell
Weight Complete Empty/Full of Water /
Sandblast:
Se.-viee
Inlet .
Outlet
Drain
Vent
Paint:
SHELL SIDE
Mk Si ze R
/tjf 2," /•
SLZlL
Site Noizle Sketch on
Shell Side:
Tube Side::
Stocked:
SPEC. BY/fV^W
CHECKED:
s
APP'D:
DATE: 7^/3 /
7 4- R
tg Face
%2 4?F
II 'I
Sheet No.
Type
Mk
s
^
Size
£4
s'n
Parallel Banks of
Parallel Bonks of
Wide
^j-23
ERVICE
,5C
TUBE
Rig
I$O
SI
Maintain
SIDE
Face Type
J?F
II
Shells n Series
Shells in Series
High
Z>THE DOW
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0
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u
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Tubes
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B
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9
Wt
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HIMCCT OF
I5oo \ £-u'-/°
HEAT
EXCHANGER
^PFriFirATIDiSK
SPEC
Na
171SOD 1/73
-------
PLANT S*s>tf/. /-y/'/'V 7*7 'fL ^DiS/ftS/* /?&sns< S "F
Specific Grovity ot P.T. • /t &43
Viscosity ot P.T.
Vapor Pressure at P.T.
Corrosion or Erosion Factors:
Arrongement^Horiz^Vert.-ln Line
Max. Capacity at P.T. ^ ^a BP1*1
Discharge Pressure
Suction Pressure
Differential Head
p»'o 7f* '*•
psia /^O '*'
psi
<&O ''•
NPSH Available •'.•
NPSH Required (Water) 'I.
Suction(Singl^, Double
Direction of Rotation Facing Pump Coupling: CW - CCW Speed: /* ~7 £&
Cose: Design Pressure
Max. Allow. Working Press.
Split: Horiz-Vert-Barrel
Impeller Diameter: Supplied 7*5
Vent and Drain Tapped: Yes - No
Nozzles Size Rating
Suction . / TT ^
Discharge *X **
Vents
Drains
Cooling HzO '
rpm
psig Number of Stages / ;Shut-Off Pressure ft.
P /~P
Casing Wear Rings:
Impeller:
Impeller Wear Rings:
Stuffing Box Bushings:
»»
H
n
H
Ib
Ib
Shaft: 3'f
Nominal Motor Size (Non-overlwding) ^ hp
Speed / 7j£
Volts <£«*£j ; P"«" 3
& rpm
; "3 O
Speed Reducer: Integral - Separate
Mfr. Ratio
Model . Class
See Driver Specification No.
Perforrnance Curve iCYeV- No; Curve No.
Certified: Yes O^q)
Hydrostatic Test: Yes -^No; Pressure
psig
Shop Inspection: Yes fNoJ
Steam Turbine: Moke
; Direct • Gear - Belt
Mounted by
Model:
Horee power
Inlet Steam Press., psig: Normal
Inlet Steam Temp., F; Normal
Water Rote:
Vacuum (If any)
Back Pressure
Nozzles Size
Inlet
Exhaust
Serial Number
lj Outline Drawing
^ Cross Section Drawing
Bulletin No.
SPEC. B^^// af * e'*<**-*j™*
A B
C
VENDOR TO COMPLETE ALL INFORMA TION MARKED |[.urw n*
hp ; Speed rpm
; Max
; Max.
Ib/Sr
mm • in. HQ - psia
psig
Rating Facing Location -
Page No.
f&>o 1 E^-/*.5!
CENTRIFUGAL PUMP
SPECIFICATIONS
SPEC.
NO.
10370D 4/73
-323-
-------
PLANT^^^/. /-V^-/ /7 'C 3^
LOCATION
MANUFACTURER
MODEL /y/l£ "^
1
~2~
3
t
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
z
UJQ
£5
U
J
INSTRUCTION DETA
U
"1
Of
tu
1-
•*
DRIVER
t-
UJ
s/fc?/* /C&rt)0^# / FILE JOB N° 7*3£
BLDG. NO. CHARGE NO.
NO. UNITS^ Gfr Tf&SW B'MNO.
P.O. NO.
?62 a
NO. UNITS ASA PUMP gffYES O NO ASA DESIGNATION
Liquid Pumped /\/ fL&/) >>V>/t_-
Pumping Temperature (P.T.) '
//& °F
Specific Gravity at P.T. ^^ £» *^/
Viscosity ot P.T.
cs-cp
Vapor Pressure of P.T.
Corrosion or Erosion Factors:
Arrengement£Horiz}-Vert..|n Line
Direction of Rotation Facing Pump Coupt
Case : Design Pressure
Max, Allow, Working Press.
Split; Horii.Vert.Barrel
Impeller Diameter: Supplied 7>l
Vent and Drain Tapped: Yes - No
Nozzles Size Rating
Suction f^L**
Discharge /&
Vents
Drains
Cooling HzO
Max. Capacity at P.T. /*O OP"
Discharge Pressure .psia *
7& "•
Suction Pressure psia /.^3 ^*
Differential Pressure psi
Differential Head &)& 't.
NPSM Available
NPSH Required (Water)
Suction£5*ingie^ Double
ng: CW . CCW Speed: / 7 5" O
psig Number of Stages / ; Shut- Off Pressure
P*'0 Volumetric Efficiency ot Rating
mpeller Type
inches; Maximum j^j inches; Minimum ^3
(t.
(t.
rpm
ft.
S
t
•% inches
Bearings: Thrust *• Type
Facing Location
Radial Type
Lubrication on Bearings; 01 • Grease
Oiler: Yes - No; Type
Coupling: Yes - No; Mfr.
Coupling Guard: Yes • No
Baseplate: Yes * No; Type
Water Cooling: Cosing. Stuff. Box-Beorings-PedestaUGland-None Total Water Required:
Smothering Gland: Yes - No
Packing; Yes {_Ng} Type
Lubrication on Stuffing Box: 0'1-Grease-None
Seeling Oil Connection; Yes • No
gpn
Mechanical Seat; (?er) No; Furnished by; faf)r/t? f~ • Mfr- TVP«
Single - Double-|n$ide*Outside-fialanced-Unba lanced
Rotary Unit ; Seal Ring ; Face Material ' ; Shaft Packing
Insert ; Re
Insert Mounting: Clomped fn
• "0" Ring - Press Fit
Gland ; Plain; Yes -No Throttle Bushing Carbon; Yes -No ; Other
Gland/Stuffing Box Machined & Topped for; Dead - End Lub. - Circulating Lub. • Quenching - Vent & Drain
Flushing Seal Faces with Discharge Bypass - Flushing Seal Faces with External Fluid
Auxiliary Stuffing 8Ox Req'd: Yes
.Weight of Pump
Weight of Driver
-No
Ib; Weight of Base
Ib; Shipping Weight
Casing & Covers: &£**£. T~2 /& 7V"^'0
Cosing Wear Ring*: X/
Impeller: */
Impeller Wear Rings: */
Stuffing Box Bushings: i
Ib
Ib
Shaft; *5/ THE
CHECKED: SERVICE
._ Af^SS^LSt^g^f
A r r U ',
°ATE:2j/<7/7tiyi' REVISION DATE A
Belt
Steam Turbine: Make Mounted by
Model:
Horsepower hp ; Speed
nlet Steam Press., psig: Normal
nlet Steam Temp., F: Normal
Water Rote:
rpm
; Mo«
; Max.
Ib.-hr
Vacuum (If any) mm - in. Hq - psia
Bock Pressure
nlet
Exhaust
Serial Number
J Outline Drawing
5 Cross Section Drawing
psig
Bulletin No. Page No.
DOW CHEMICAL. COMPANY 1 5 &r^
*€/ A/&JbAt/* ftsmh CENTRIF
SPECIF
B
L
IECUIP. NO.
P-TL6*B
UGAL PUMP
'ICATIONS
183700 4/73
-324-
-------
PLANT eZexyJ. /<
Yes
FUE/JOB NO. ~73C) £>2.2>
CHARGE NO.
B/M NO.
P. 0. NO.
NO. UNITS
?
fNV
Men. Allow.. Press. (New & Cold) psig; Limited By
Hydra. Test <^O psig I Code:
Corr. Allow. In.: Shell ; Hoods
Joint Efficiency %: Shell ; Hoods
Insulation: /i/<3 |Self Supporting Yes (NV
Firaoreofrng: SJO
Stomp
Rodiogroph
Ye
, A
J
A/0
Stress. Rel. S^/O
Sandblast: X(?3
5 dot:
P
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ne.
Manhole: Hinged G>avited) Other:
Platform Clips: fJO . Ladder Clips: AXO
Pipe Supports: // ' O Insul. Rings: A/O
Wind Load: Seismic:
ShiDDing Wt. Ib Wt. Full
Troy No. Diem. Spodng Type
Thru
Thru
Thru
Thru
Material Tray
Removobl
Certrl dge
b
Installation
e Yes No
Support Ring
Tray Manwoy
Yes Ne
Monwoy Size
Contact Device: Bubble Copi-Va ves-Perforations Weir Set. (Above Fleer]
Describe: Adjuitokl
e to
(Ad|. Slots Sealed at
In.
In.
In.
All Sctthp)
Pocking: /" •&/&
//
//
A'io ^^\
St&G> /
•l
it
II
No. Si xe Rtg Face Type Service Mk
2. 4" /5? £F P,. Relief N
l_i" " " .evelCwt P
/ 3" " " Samples Q
/ A" " " /Scju R
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/ 18' zs* RF v
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No.
•
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1
Size
f»"
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tfo
SPEC BY £/=•& <§g£>-THE DOW CHEMICAL
CHECKED: SERVICE
APP'D:
?e>eK. y
OATEi "2^^/74- "EVISIONDATE A
VENDOR TO COMPLETE ALL INFORMATION MAR
KED
B
Face
/fr
Type
TOWER SKETCH
%
S
M
*
*
0
J
0
V
1
% '
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V
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COMPANY 7s£& \ 5?-*/"°
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TOWER
SPECIFICATIONS
c
SPEC.
[JSMICT OF NO.
-------
PLANT
yfAfr/o^ZT
FILE/JOB NO.
LOCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS / per'
B/M NO.
P. 0. NO.
IFIELD ERECTED YES
[NO. UNITS /
Tro / '1 [TOTAL VOLUME
cw-
J8-0" Ton. T, Ton.
For Further D.tolls S«* Sti««t Ne.
27
Operating Pressure
Type Supports:
28
Operating Temperature
Insulation:
29
Liquid Specific Gravity
Pi rep roofing!
X
Contents Lethal
Sandblost:
|Point!
31
Design Pressure
pslg
2.S"
Manhole
Hinged
Davited
Other
32
Design Temperature
Platform Clips:
Ladder Clips:
33
Mo«. All. Press. (New&Cold) p»i3
Pipe Supports:
nsul. Rings:
34
Limited By
35
Hydrostatic Test
psig
4-Q
Wt. Empty
Ib Wt. Full of Water
Ik
36
37
Heads Corr. Allow, in.
Shell Heads Joint Eff.
Code:
Stomp R«q V
Yes
RadioaroDh:
Stress Relieve; fJO
National Board No.
She
leads
.ining
Noi. Necks
Flanaes
louplinq
M.H. Cover
Supports
Bolti/Studi
Nuts
Gaskets
Thickness
in.
in.
in.
Mail Class
Mat'l.Min mum Quality
S«rvi c«
7~
Marie
No.
Si i.
Rating
Type
Notf • to b« Plugged or Blinded
PEC. BY
CHECKED:'
APP'O:
DATE: 2./ "7/7 ft
«d8>- THE DOW CHEMICAL COMPANY
SERVICE
REVISIONDATE
»M€IT or
COUIP. NO.
HORIZONTAL
DRUM
SPECIFICATIONS
SPLC.
17740 2-«t
-326-
-------
L ANT
/c
00 AT ION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS &/J E:
B/MNO.
P. 0. NO.
-to
, GOO
10
12
13
14
IS
18
iff- Sr,
C/
PP'O:
ATE, 2/7/7 -••
-327-
-------
FILE/JOB N0.,73£? 6 Z 3
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
12
13
£>
33
34
35
42
45
47
48
50
PEC. or
NECKED*
PP'D:
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
END01 TO COMPLETE ALL INFORMATION MARKED
2B200 )-fl
IMKCT or
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO,
-328-
-------
'(.ANT
FILE/JOB
&Z 3
OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
P. 0. NO.
12
rg~/P 5 rs
IHECKCOl
JATEi
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE
(MEET or
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO,
-329-
-------
FILE/JOB NO. '
LOCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
P. 0. NO.
ii
-A'
SPEC, or
IHECKEOr
PP'Oi
ATE, 7
THE DOW CHEMICAL COMPANY
SERVICE
5 >^S 7
RE VISION DATE A
ENOOM TO COMPLCTC ALL INFORMATION MAMKCO
UCO 9-61
«OOI». NO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO.
-330-
-------
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/MNO.
P. 0. NO.
13
14
TV
/- £? A-tt/JSort -per//AS?
i' f if m
a
ffff r
.& /w
35
41
43
45
46
HECKEOi
,PP'D:
)ATEl
THE DOW CHEMICAL COMPANY
SERVICE
REVISION DATE A
.ENDOn TO COMPLETE ALL INFORMATION MANKCD
28200 >-4l
• QUIP. NO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC.
-331-
-------
;L ANT
7~/C -^> L
FILE/JOB NO.7*?6 f> ei.
.OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/M NO.
P. 0. NO.
13
14
YS
Tt
¥h
si
25
SPEC. BY
HECK ED:
PP'D:
ATE,
3@f>THE DOW CHEMICAL COMPANY
SERVICE
REVtSIONDATE
•HKIT or
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
NO.
1B2AO I -0
-332-
-------
PLANT f
T/c,
FILE/JOB NO. ~/3£)(a 2. 3
OCATION
BLOC. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/MNO.
P. 0. NO.
3
SO
M-EC.OY
:HECKEDi
.PP'D:
THE DOW CHEMICAL COMPANY
SERVICE
OE VISION DATE
Jfc
IIOUI*
Z.3CJ
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC,
NO,
-333-
-------
FILE/JOB NO.
£ 2.
.OCATION
BLDG. NO.
CHARGE NO.
MANUFACTURER
NO. UNITS
B/MNO.
P. 0. NO.
V 0&A 77
•ft-
33
37
30
PEG DV
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PP'Oi
THE DOW CHEMICAL COMPANY
SERVICE
JT/VS
,' —>/'-•
REVISION DATE A
TION MAPtKCC
•MBIT or
fOUI». HO.
MISCELLANEOUS
EQUIPMENT
SPECIFICATIONS
SPEC
260 >-•!
-334-
-------
10.3 INSTRUMENTATION
10.3.1 List of Instruments
The instrument numbers refer to the instrumentation on the
process flowsheets in Section 4.5.
Sector 100 - Mixing
FR 100
FT 100
FE 100
WRC 101
WT 101
LRC 102
LT 102
I/I 102
LSH 102
LAH 102
TRC 103
TT 103
TE&TW 103
TV 103
DR 104
DX,DE, DIT-104
FQ 105
FI 106
PI 107
TE,TW
Flow Recorder
Flow to Current Converter
Magnetic Flow Meter
Weight Recording Controller
Weight Transmitter
Level Recorder & Controller
Level Transmitter
Current-Current Repeater
High Level Alarm Relay
Alarm Annunciator Point
Temperature Recorder & Controller
Resistance-Current Converter
Resistance Element & Well
Control Valve
Density Recorder
Density Transmitter
Gas Meter
Flow Indicator
Pressure Gage
Thermocouple & Well
Sector 200 - Reaction
FRC 200A-K
Flow Recorder & Controller
-335-
-------
FT 200A-K
FE 200A-K
FV 200A-K
FRQ 201
FT 201
FE,FX-201
FRC 202A-K
FT 202A-K
FE,FX 202A-K
FV 202A-K
FRC 203A-K
FT 203A-K
FE,FX 203A-K
FV 203A-K
FR 204A-K
FT 204A-K
FE,FX 204A-K
PRC 205A-K
PT 205A-K
PV-205A-K
LRC 206A-K
LT 206A-K
PT 206A-K
LSH 206A-K
LAH 206A-K
FV 206A-K
TRC 207
TT 207
TE,TW 207
TV 207
PI 208
PI 209
TE,TW
Flow-Current Converter
Magnetic Flow Meter
Control Valve
Flow Recorder & Integrator
Flow Transmitter
Orifice Flanges & Plate
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Pressure Recorder & Controller
Pressure Transmitter
Control Valve
Level Recorder & Controller
Level Transmitter
Pressure Transmitter
High Level Alarm Relay
Alarm Annunciator Point
Control Valve
Temperature Recorder & Controller
Resistance-Current Converter
Resistance Element & Well
Control Valve
Pressure Gage
Pressure Gage
Thermocouples & Wells
-336-
-------
Sector 400 - Filtration #1
FRC 401A-D Flow Recorder & Controller
FT 401A-D Flow to Current Converter
FE 401A-D Magnetic Flow Meter
FV 401A-D Control Valve
FR 402 Flow Recorder
FT 402 Flow to Current Converter
FE 402 Magnetic Flow Meter
PRC 403 Pressure Recorder & Controller
PT 403 Pressure Transmitter
LSH/L 404A-D High/Low Level Switch
LAH/L 404A-D Alarm Annunciator Point
Sector 500 - Extraction
FR 500 Flow Recorder
FT 500 Flow Transmitter
FE,FX 500 Orifice Flanges & Plate
LRC 501 Level Recorder & Controller
LT 501 Level Transmitter
LSH/L 501 High & Low Level Alarm Switches
LAH/L 501 Alarm Annunciator Points
TE,TW Thermocouple, Well & Recorder Point
FRC 502 Flow Recorder & Controller
FT 502 Flow Transmitter
FE,FX 502 Orifice Flanges & Plate
FV 502 Control Valve
FRC 503 Flow Recorder & Controller
FT 503 Flow Transmitter
FE,FX 503 Orifice Flanges & Plate
FV 503 Control Valve
-337-
-------
Sector 600 - Filtration & Decantation
FRC 600A-D
FT 600A-D
FE 600A-D
FV 600A-D
AIS 601A-D
AE 601A-D
AAH 601A-D
FR 602
FT 602
FE,FX 602
FI 603A-D
LRC 604
LT 604
LV 604
FR 605
FT 605
FE,FX 605
LSH 606
LAH 606
LSH/L 607A-D
LAH/L 607A-D
PI 608
PI 609
TE,TW
Flow Recorder & Controller
Flow to Current Converter
Magnetic Flow Meter
Control Valve
Oxygen Indicator
Oxygen Sensor
Alarm Annunciator Point
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Flow Indicator
Level Recorder & Controller
Level Transmitter
Control Valve
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
High Level Switch
Alarm Annunciator Point
High/Low Level Switch
Alarm Annunciator Point
Pressure Gage
Pressure Gage
Thermocouple, Well, Recorder Point
Sector 700 - Water Wash
FR 700
FT 700
FE,FX 700
LRC 701
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Level Recorder & Controller
-------
LT 701
LSH/L 701
LAH/L 701
TE,TW
Level Transmitter
High/Low Level Switches
Alarm Annunciator Points
Thermocouple, Well, Recorder Point
Sector 800 - Filtration & Decantation
FRC 800A-D
FT 800A-D
FE 800A-D
FV 800A-D
AIS 801A-D
AE 801A-D
AAH 801A-D
FR 802
FT 802
FE,FX 802
FI 803A-D
LRC 804
LT 804
LV 804
FR 805
FT 805
FE,FX 805
LSH 806
LAH 806
LSH/L 807A-D
LAH/L 807A-D
FR 808
FT 808
FE,FX 808
FFRC 809
FT 809A
Flow Recorder & Controller
Flow Transmitter
Magnetic Flow Meter
Control Valve
Oxygen Indicator
Oxygen Sensor
Alarm Annunciator Point
Flow Recorder
Flow Transmitter
Orifice Flanges $ Plate
Flow Indicator
Level Recorder & Controller
Level Transmitter
Control Valve
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
High Level Switch
Alarm Annunciator Point
High/Low Level Switch
Alarm Annunciator Point
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Flow Recorder & Ratio Controller
Flow Transmitter
-339-
-------
FT 809B Flow Transmitter
FE,FX 809A Orifice Flanges & Plate
FE,FX 809B Orifice Flanges & Plate
FV 809 Control Valve
FR 810 Flow Recorder
FT 810 Flow Transmitter
FE,FX 810 Orifice Flanges & Plate
PI 811 Pressure Gage
PI 812 Pressure Gage
FRC 813A-D Flow Recorder & Controller
FT 813A-D Flow Transmitter
FE,FX 813A-D Orifice Flanges & Plate
FV 813A-D Control Valve
TE,TW Thermocouple, Well, & Recorder Point
Sector 900 - Drying, Decantation
FRC 900A&B Flow Recorder & Controller
FT 900A&B Flow Transmitter
FE,FX 900A&B Orifice Flanges & Plate
FSH/L 900A&B High/Low Flow Switches
FAH/L 900A&B Alarm Annunciator Point
FV 900 A&B Control Valve
PRC 901A&B Pressure Recorder & Controller
PT 901A&B Pressure Transmitter
PSL 901A&B Low Pressure Switch
PAL 901A&B Alarm Annunciator Point
PV 901A&B Control Valve
AIS 902A&B Oxygen Indicator
AE 902A&B Oxygen Sensor
AAH 902A&B Alarm Annunciator Point
TRC 903A&B Temperature Recorder & Controller
-340-
-------
TE,TW 903A&B
TV 903A&B
FR 904
FT 904
FE,FX 904
FR 905
FT 905
FE,FX 905
LSH 906
LAH 906
PI 907
TE,TW
Temperature Element & Well
Control Valve
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
High Level Switch
Alarm Annunciator Point
Pressure Gage
Thermocouples, Wells, Recorder Points
Sector 1100 - Iron Sulfate Removal
FRC 1100A&B
FT 1100A&B
FE 1100A&B
FV 1100A&B
LSH/L 1101A&B
LAH/L 1101A&B
LRC 1102
LT 1102
LV 1102
TRC 1103
TT 1103
TE,TW 1103
TV 1103
FRC 1104
FT 1104
FE,FX 1104
FV 1104
Flow Recorder & Controller
Flow to Current Converter
Magnetic Flow Meter
Control Valve
High/Low Level Switch
Alarm Annunciator Point
Level Recorder & Controller
Level Transmitter
Control Valve
Temperature Recorder & Controller
Resistance to Current Converter
Resistance Element, Well
Control Valve
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
-341-
-------
PRC 1105
PT 1105
PV 1105
LRC 1106
LT 1106
PT 1106
LSH 1106
LAH 1106
TRC 1107
TT 1107
TE,TW 1107
TV 1107
FRC 1108
FT 1108
FE 1108
FV 1108
LC 1109
LV 1109
LSH/L 1110
LAH/L 1110
FR 1111
FT 1111
FE,FX 1111
FRC 1112
FT 1112
FE,FX 1112
FV 1112
LSH/L 1113
LAH/L 1113
LRC 1114
LT 1114
LV 1114
Pressure Recorder & Controller
Pressure Transmitter
Control Valve
Level Recorder & Controller
Level Transmitter
Pressure Transmitter
High Level Alarm
Alarm Annunciator Point
Temperature Recorder & Controller
Temperature Transmitter
Resistance Element, Well
Control Valve
Flow Recorder & Controller
Flow Transmitter
Magnetic Flow Meter
Control Valve
Level Controller
Control Valve
High/Low Level Switches
Alarm Annunciator Points
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
High/Low Level Switch
Alarm Annunciator Points
Level Recorder & Controller
Level Transmitter
Control Valve
-342-
-------
FRC 1115
FT 1115
FE 1115
FV 1115
AR 1116
AIT 1116
AE 1116
AAH/L 1116
LR 1117
LT 1117
FRC 1118
FT 1118
FE,FX 1118
FV 1118
LSH/L 1119
LAH/L 1119
PI 1120
PI 1121
PI 1122
PI 1123
TE,TW
Flow Recorder & Controller
Flow to Current Converter
Magnetic Flow Meter
Control Valve
Hydrogen Ion Recorder
Hydrogen Ion Indicating Transmitter
Hydrogen Ion Sensor
Alarm Annunciator Points
Level Recorder
Level Transmitter
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
High/Low Level Switch
Alarm Annunciator Points
Pressure Gage
Pressure Gage
Pressure Gage
Pressure Gage
Thermocouples, Well, Recorder Points
Sector 1400 - Distillation
LR 1400
LT 1400
LRC 1401
LT 1401
TCV 1402
TE,TW 1402
FRC 1403
Level Recorder
Level Transmitter
Level Recorder & Controller
Level Transmitter
Self-Operated Temperature Control Valve
Temperature Bulb, Well, & Capillary
Flow Recorder & Controller
-343-
-------
FT 1403
FE,FX 1403
FV 1403
PRC 1404
PT 1404
PV 1404
TRC 1405
TT 1405
TE,TW 1405
TV 1405
LRC 1406
LT 1406
LV 1406
FR 1407
FT 1407
FE,FX 1407
FRC 1408
FT 1408
FE,FX 1408
FV 1408
TRC 1409
TT 1409
TE,TW 1409
TV 1409
LR 1410
LT 1410
LR 1411
LT 1411
LRC 1412
LT 1412
LV 1412
FRC 1413
Flow Transmitter
Orifice Flanges & Plate
Control Valve
Pressure Recorder & Controller
Pressure Transmitter
Control Valve
Temperature Recorder & Controller
Resistance to Current Converter
Resistance Element & Well
Control Valve
Level Recorder & Controller
Level Transmitter
Control Valve
Flow Recorder
Flow Transmitter
Orifice Flanges & Plate
Flow Recorder & Controller
Flow Transmitter
Orifice Flanges & Plate
Control Valve
Temperature Recorder & Controller
Temperature Transmitter
Resistance Element, Well
Control Valve
Level Recorder
Level Transmitter
Level Recorder
Level Transmitter
Level Recorder & Controller
Level Transmitter
Control Valve
Flow Recorder & Controller
-344-
-------
FT 1413
FE,FX 1413
FV 1413
TRC 1414
TT 1414
TE,TW 1414
TV 1414
LSH/L 1415
LAH/L 1415
LSH/L 1416
LAH/L 1416
LSH 1417
LAH 1417
LSH/L 1418
LAH/L 1418
TSL 1419
TE,TW 1419
TAL 1419
PI 1420
PI 1421
PI 1422
PI 1423
PI 1424
Flow Transmitter
Orifice Flanges & Plate
Control Valve
Temperature Recorder & Controller
Resistance to Current Converter
Resistance Element, Well
Control Valve
High/Low Level Switch
Alarm Annunciator Points
High/Low Level Switch
Alarm Annunciator Points
High-Level Switch
Alarm Annunciator Point
High/Low Level Switches
Alarm Annunciator Points
Low Temperature Switch
Temperature Bulb, Well, Capillary
Alarm Annunciator Point
Pressure Gage
Pressure Gage
Pressure Gage
Pressure Gage
Pressure Gage
Sector 1500 - Vent Collection & Scrubbing
LRC 1500
LT 1500
LV 1500
AR 1501
AIT 1501
Level Recorder & Controller
Level Transmitter
Control Valve
Hydrogen Ion Concentration Recorder
Hydrogen Ion Indicating Transmitter
-345-
-------
AE 1501
AAL 1501
LRC 1502
LT 1502
LV 1502
AR 1503
AIT 1503
AE 1503
AAL 1503
LSH/L 1504
LAH/L 1504
PI 1505
PI 1506
TE,TW
Hydrogen Ion Sensor
Alarm Annunciator Point
Level Recorder & Controller
Level Transmitter
Control Valve
Conductivity Recorder
Conductivity Indicating Transmitter
Conductivity Sensor
Alarm Annunciator Point
High/Low Level Switch
Alarm Annunciator Points
Pressure Gage
Pressure Gage
Thermocouple, Well, Recorder Point
Miscellaneous
TR
TI
TE,TW
Temperature Recorders, 24 point (3)
Temperature Indicator, 50 point (1)
Thermocouples & Wells (50)
Panelboard (23-2 foot Sections)
Annunciator; Lights, Pushbuttons
-346-
-------
10.3.2 Instrument Descriptions and Costs
The sheets that follow provide further description and costs
for the instruments listed in 10.3.1.
-347-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
/OF 36
PROJECT ~~ [—3 ,--> /—-, -r- JOB NUMBER
COAL - rv/z/T/c OULPUH k-EMo r^ £r &
f L.& Vj ^ — ^- *- CsK—LsC *C.
u/ SHELF Af/0 CABLES
F'LO*/ -To - Cu£e.EMJ~
CohJVE£LT££-- W/ /Oder
OF CABLE.
(o " AMQA/£77C J~Lo\*j-
V/E-i^HT KECO&.D[N($
CoN T&OL L£.J8.
LEVEL £?£c OP.DEZ
AMD CoNTBOLL.LfL
w /siit-LF-' AMO CA&LES
Fl USH D/APH&A<5M
7'yPE LEVEL 7xPX/V5-
M/TTEE..
REPEATED.
/J/6H ALAPts CZLAY
^~^
T^/^fPEfiATUGE: KCCOf.DEf.
AND C,OfJT/3.OLLE.I5
w/sm.i.r /./•//> CABLES
SECTOR NUMBER L NAME
(QUANT.
QUANT.
'
/
I
/.
/
1
'
'
K [MATERIAL
CONSTRUCTION
MATERIAL
TEFLOH \nl
T/WTALUM
STEEL
•
TANTALUM
— -
1- CONDITION + COMPLEXITY]
DESCRIPTION
£~(JlifiJlSHE.[> AS PA&T
op COAL ST~o/2.A$E AMD
As ABOVE
- - •- • •'-
= M$(19 )
^
W
*) /n d t\"
»o C/ O J
I/7S
730
• 35
70
7/7-5
FORM 396SO PRINTED IN U.
-348-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
2 OF 36
PROJECT r— ) f- -, .— JOB NUMBER
COAL- rye/r/c ooLrue. REMOVAL — Jfjsr-^uf-ic^rs 73O&2.3
PHASE CASE BY . DATE EF NUMBER
/ 745^2 £. \V.C££WAZ t>57
SECTION NUMBER I NAME
100- MIXING
FACTORS
ITEM
TT
/03
T£
n/
102
TV
103
oe
io4-
DX
D£
DT.T
104-
ro
/OS
FZ
/Oh
PI
/or
T£
TyJ
BASE X ESC. X CAPACITY
NAME OF FACILITY
^£S/5T/\MC£ - To -
CuZREMT- CoNYE.e.T£g
£?ES ISTAMCE THEGMO -
VET££ ELEMENT v/ /
WELL AtiD HEAD.
£>"-/5ot.e GLOBE TYPE
COMTP.OL I/ALI/E vv/
x/p Poj5/rtofJE&
DENSITY &£co£.oee.
"/SHELF AMD CABLES
&ADIA 770V TYPE D£NSm
T£Atisyirn~Ee w/ soue.ce
DETECTOR # £L£creo*/ts
2 " ///
= MJ(19 )
535"
2.^7
7677
466
3,500
600
300
^5
• 250
J4600
Z058
/&>££$
rom MSO PRINTED IN U.S.A. Hi-el
-349-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
PROJECT x—
COAL-
PHASE __
FY&JT/C SuLrue &EMOVAL. -Hvsn
CASE BY
/AS K 2. Xr l^v L*EPM/{ JS
SECTION NUMBER 1 NAME —
20 O- KZACT/ON
FACTORS
ITEM
FGC
2.00A
1
FT
2.0OA
, 1
FE
2ooA
\
FV
Zoo A
i
20OX.
F&Q
2o /
FT
20 /
FE
FX
2o/
20 f A
j
20ft/
f
/•'/ f
I
/-'I/
?O ?. A
1
BASE
SHEET
3 OF 56
JOB NUMBER
IUMENTS 73062.3
DATE EF NUMBER
65"7
X ESC. X CAPACITY , XQUANT. [MATERIAL + CONDITION + COMPLEXITY] _ = M$(19 )
NAME OF FACILITY
/-Low £?£.CO£.DEJ$ AND
CONTROLLER. W/ SHELF
AME> CABLES.
CoN\/E£V6£ K// 100 FT
OF CABLE.
v5 WA$M£T/C FLOW-
Bu7rEE.FLY COMT&QL VALVE
FLOW f2i-COJ?PE& AND
AND CABLES.
TYPE fLO^s 77P.AMS -
MITTEfi W/ rfAfiJIFOLD
3 " OfUFlCE FLAfllGES
AND PLATE.
CQMreoLLE.R. W/ SHELF
AHO CABLES
TYPE FLQ*/ • TGA^S-
MI7T£-.fL *// MANIFOLD.
^.''O^I^ICE FL^N^E-S
AND PLATE
/"-/5Oi-B. GLOBE TYPE
(ZoMTEOL VAL v£ ^/
QUANT.
10
10
10
10
'
/
10
10
10
10
CONSTRUCTION
MATERIAL
TEFLON */
TANTALUM
ALL
ALL
3/6
STEEL
w/ 3/6
PLATE
ALL
3/6
STEEL
H//3/6
PLATS.
SJ-C.EL
W/ 3/6
DESCRIPTION
.C, **<{*.&
0*> 5£E.Vi<2£ CLEAHIrtQ
Qz SERVICE CLEAHIN
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
4-»36
PROJECT --. . . — . , r-j — JOB NUMBER
COAL - P/etT/c SULFUK. &EMOSAL - JHSTKUMEHTS 730 6 2.3
PHASE CASE BY , . DATE EF NUMBER
I TASK a g:K/.C£e.MA* £57
SECTION NUMBER I NAME
2OO- ffEACT/Ori
FACTORS
ITEM
FKC
203A
1
2o3£
"FT
2o3A
1
2o3£
FE
FX.
203A
203X
"JF/
Z03A
Z03Z
re
20+ A
1
204-K
'FT
ZO4A
1
204Z
Fa
fX
204A
1
204-K.
P£C
2 OS A
\
Z05Z
PT
zosA
205K
PV
20SA
1
205K.
L£C
206/1
/
206K
BASE X ESC. X CAPACITY !
NAME OF FACILITY
FLort £E£oe.DE& AND
COMrf20LL££ rt/ StfELF
AfJ£> CABLES.
DlFFEZEnr/Al. tfeESSUtiE
TYPE FLOvS T£A A/5 -
MITTES. W/ MA M/FOLD
Z" O&IFICE FLAM &ECOG.DE& w/
SHELF AMD CABLES
DlFFE/£ENr/AL PEESSuKE
TYPE FLOv PL A TE
PRESSURE SECONDER
AND COMT~e.01.LEe W/
SHELF AND CABLES
DJAPHSA^/^ TYPE
peESsuee -TEANSH/TTEB.
/"-/5OLB GLO&E TYPE
COMT/ZOL VALVE w/
X/P POS/TtONEK.
L.EI/EL £?ECO£.DEe. AHQ
COMT&OLLEZ ^/Sf^ELF
AMD CABLES.
SECTOR NUMBER I NAME
(QUANT. )
QUANT.
10
10
10
10
10
10
10
10
10
10
10
[MATERIAL
CONSTRUCTION
MATERIAL
ALL
3/6
STEEL
\»>/ 3/6
PLATE
STEEL
w/ 3/6
Tg/M
ALL
3/6
STEEL
*// 5/6
PLATE
ALL
3/6
SrEEt-
w/ 3/6
rz/M
CONDITION + COMPLEXITY]
DESCRIPTION
Oz SERVICE CLEANir^
Oz SE£V/CE CLEArtl^q
CtfgEQD = 3S
Oz SERVICE CLEA*m$
»
£v £EQD ' O.3
= M$(19 )
//, 750
8, 9 oo
780
5870
4660
*
7,250
700
1 /, 750
$350
5,970
II, 750
rOW MSO PRINTED IN U.S.*. R14I
-351-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
5- OF 36
PROJECT x^~ r-i S~ ~ D . T J0» "UMBER
COAL - ryz/r/c SULFUR. REMOVAL- IHSTZUMEMTS 73o 62. 3
PHASE __ CASE BY „ DATE EF NUMBER
I TASK 2. g.\V. CEevtAX 65*7
'SECTION NUMBER * NAME
2OO~ fCEACT/OM
FACTORS
ITEM
LT
20&A
1
2v
2.07
TV
Z07
PI
2.09
PI
2o H.D. MAFEfL
BUTTERFLY £C»JTG.OL VALVE.
W/ -% POStT/OtJES..
7EMPEZATU£e FECORDEZ.
AMD CO^TROLLES. iV/
SHELF AMD CABLES.
&ESISTAMCE. - TO-
CuglZENT COMEZTER..
EESISTAMCE T/-/EZMO-
METE& ELEMEM-r W/
WELL AND MEAD.
6"-/25Lff H.D. WAFEB.
BUTTERFLY Cotsreoi. I/ALI/E
w/, Jfo />OS/77OM££
4z*Pl5ESSU£E GAUGEvJ/
CAPILLARY TO DEMOTE
SEAL.
4z"PeESSV&E $AU$£.
SECTOR NUMBER 4 NAME
C QUANT.
QUANT.
10
10
10
10
10
1
/
/
/
/
1
\ [MATERIAL
CONSTRUCTION
MATERIAL
TANTALUM
TANTALUM
ALL
TITANIUM
TYPE
3/6
W£U-
leoN AND
STEEL
*s/3/6 TKJM
TAUTALUfSI
OlAPHeA6tf
IN TEFLON
SEAL
STEEL
ELEMENT
CONDITION + COMPLEXITY]
DESCRIPTION
_ : .._
CV&EQD = 2$
Q''L$ \rJeLLt2."-/5'OLO Ft.(j.
Cy Z.EQD - 3oo
1
O^SERVICE CLfLAMlNej
= M$(19 )
7JOO
7,070
850
70
/$670
firs'
535
/34-
' 9/7
170
35
FORM JMO PRINTED IN U.S.*. (U-69
-352-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
PROJECT ^ r— , • ' f~> I—I -T JOB "UMBER
COAL - rY£/r/c ouLrue REMOVAL - ZMSTZ.U
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
7 OF 36
"*"** COAL - PyEiT/c SULFUZ REMOVAL - INSTRUMENTS ** 738 623
PHASE CASE BY DATE EF NUMBER
T TASK a. jg.W.CEgMA* . 657
SECTION NUMBER * NAME __
4OO- r/LTZAT-tON A/0,/-
KACTORS
ITEM
F£C
40/A
\
4-OlD
FT
4otA
\
40ID
FE
40/A
I
4oi D
FV
4-olA
\
4oiD
FK
40?.
fr
402.
FE
402.
pec
405
PT
4-o3
L$%
404A
1
4o4£>
LAK
404A
\
404D
BASE X ESC. X CAPACITY
NAME OF FACILITY
FLOW &ECO&DE& AND
CONTROLLED. *// SHELF
AND CABLES.
FLO*/- ro -CUSEEMT
COMVEZTEIS. M// /OOfT
OF CABLE.
3 " MA 4 NE r/c FLOVS-
METEf>
3"-/SOL£ BALL TYPE
CoureoL ]/AL\/£. »//
fa reA/JSDUCEK.
FLOW ££co£.D£-£.
W/ SHELF AMD CA5LZS
FLOW- TO - cuee.£.Nr
CCtNVEZTEK vv/ /OO^-r
OF CABLE .
6>"M4G*/£r/c ft.o»/-
METEZ,
P&ESSUBE gecoeoER j
COfjreoLLE/3 *// SHELF
AND CABLES.
FLUSH DtApHeA^M
TYPE- P& ESSUKE.
TR.AHSMITTE-&.
H/GH /LOW PAN LEVEL
ALA&M SW/TCHC-5
At-AZM ANNUNCIATOR
POINTS
SECTOR NUMBER 1 NAME
(QUANT.
QUANT.
4
4
4
4
1
/
/
1
/
8
8
[MATERIAL -
CONSTRUCTION
MATERIAL
TEFLON */
TANTALUM
ELECTZODtt
ALL
3/6
Tzn.0* */
TAfJTAL Utt
ELECTRODES
TANTALUM
CONDITION + COMPLEXITY]
DESCRIPTION
CV£EQ'D = 75
Fu£NfSHED AS PAST oF
4OO-F-I SEHIES f/LTEe.
CONTROLS.
= H$(19 )
4,700
3396
4500
3648
466
849
2085
1175
840
560
22,2./<7
FORM 396SO PRINTED IN U.S.A. RI4I
To
-354-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
8 OF 36
PROJECT - — . . — 5 s-\ i — } f- JOB NUMBER
COAL - FYZ/TIC SULFUR REMOVAL - JMST&UMEUTS 73062.3
PHASE CASE BY — ^_, DATE EF NUMBER
I TASK 2 &W.CE£vfAK . 657
SECTION NUMBER & NAME
50 0 - E* TZACT/OH
FACTORS
ITEM
F£
5oo
FT
soo
F£
F/
5~OO
Lec
501
LT
50 /
LS%
Sot
*-*%
501
TE
rw
FZC
SOZ-
FT
SOZ
ft
502.
BASE X ESC. X CAPACITY
NAME OF FACILITY
/2eW /&£CoeD£e. \^
SHELF AMD CABL.C5
DlFFE£E*/r/AL PRESSURE.
7~YPE no*/ TeAMSMnTER-
\V/ MAM /FOLD.
S"O£>FICE FLAKES
AND. PLATE
LEVEL RECORDER. AMD
corJrje.OLLE& w/ SHELF
AND CABLES
FLUSH D/APHZAG^
TYPE LEVEL 7~£A'JS-
M/TTEe.
Hl$H AND L0\d LE.VEL .
ALARM SWITCHES
ALARM ANNMCtAroz
PO/MT5
THER. MOCOU PL E EL EMEMT
W/ THERMO WELL, HEAD
A'MD RECORDER PO/NT.
FLOW fc'ecoe.DE-Z. AMD
COMTE.OI.LEK. -vs/ SHELF
AMD CABLES
DlPFE&EMT/AL PRESSURE
TYPE FLOtV TRANSMITTER
H// MAfif/FOLO.
6" O&IF/CE FLAM5ES
AND PLATE
SECTOR NUMBER t NAME
(QUANT. )
OUANT.
/
/
/
/
/
2
^
/
/
/
/
I [MATERIAL
CONSTRUCTION
MATERIAL
ALL
3/6
5T££L
v// 3/6
PLATE
3/6 AHO
TAHTALUtf
3/6
WELL
ALL
3/6
STEEL.
*/ 3/6
PLATE
CONDITION + COMPLEXITY]
DESCRIPTION
= MJ(19 )
466
725-
174
1175
855
/70
140
/30
'1/75
115
/37
FORM 396U PRINTCO IN U.S.A. Rl-<9
-355-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
9 OF 36
™'™CoAL - Py£/T/c SULFU&. REMOVAL. ~ J/^sreu^iE^rs ™73O623
PHASE C*SC_ . BT / x— v DATE Ef NUMBER
_/"• TASK 2 &.W.CE&MAX £,57
SECTION NUMBER 1 NAME
Soo- EXTRACT/ON
FACTORS
ITEM
F\/
50Z
pec
503
FT
503
/=-£•
FX
503
FV
503
BASE X ESC. X CAPACITY
NAME OF FACILITY
4"-/5OLB GLOBE TYPE
CovrpoL VALVE "/
I/p TeArtSDUCEg
FLOW £?E.COK.D£.I5. AMD
CON TROLLE.Z W/ SHELF
AND CABLE. S
D/FFEZENriAL. PKESSUK£
TYPE FLOri T&AHSM/TrEK.
W/ MAMJFOLD
6" ORIFICE. FLAMG£S
AMD PLATE.
4*-/5Ot.B (jLoBE TYPE
CONTROL YALVE. "/
I/p TG.ANSDUCE/5.
F*&o£AT£ /
SECTOR NUMBER & NAME
(QUANT.
QUANT.
/
/
/
/
/
1/$<.
( [MATERIAL
CONSTRUCTION
MATERIAL
STEEL
*/ 3/6
-T£lM
ALL
3/6
STEE.L
iv/ 5/6
PLATE
^TEEL
*// 3/i53
7,4 3 /
11,584*
.^_. —
FORM 396SO POINTED IN U.S.A. R
•356-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
/O OF 36
PROJECT .^* /~) ^ *— 5 ~f JOB NUMBER
C.OAL — /~Y£/T/C ^)ULFU& REMOVAL — jMSr&UMCNTS 730&23
PHASE CASE BY . __, DATE EF NUMBER
I TASK 2 &.lA/C££rtA£ 657
SECTION NUMBER I NAME , •
6tf£- £~/LTE£ £ DECANT
FACTOR?
ITEM
^/ec
600
600/9
rr
600
FE
6 00 A
600D
FV
6ooA
\
&OOD
AIS
60/A
\
60 ID
AE
6o/A
\
60/D
AAH
60/A
I
60Z.
FT
602
._
603A
\
603 D
BASE X ESC. X CAPACITY 1
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
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COAL - rygiTic OULFUZ. REMOVAL - J^ST/^U^E^TS 73O623
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
/2 OF 36
PROJECT -^ f— ) >— » /—i __- J08 NUMBER
COAL - rye/7'ic SULFUR. REMOVAL - ^STB-UMENTS 730 6 23
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= MJ(19 )
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MIDLAND. MICHIGAN
SHEET
/3 OF 36
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-36O-
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
/4of36
PROJECT — -. ,—5 {-** /-) -7- JOB NUMBER
COAL - r-*YJ5iT/c OULFUZ REMOVAL - JMST&UME*JTS 73 O 6 23
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FORM J9CSO PRINTED III U.S.A. *!•«
-361-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
(MEET
/Sof36
PROJECT ^ ,-j -—l , — . —. JOB NUMBER
GOAL ~ Pye.mc SULFUR. REMOVAL - 2*jsreuMENTs 73O&Z3
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-362-
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
PROJECT ^— f—\ ' £~* »— JOB NUMBER
COAL - /-r/e/Tvc -SULFUE. REMOVAL — ZwsTeuMEK/Ts 73O623
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ALL
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-363-
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
PROJECT _,
COAL -
PHASt '
SECTION NUMBER I NAME
FACTORS
ITEM
pr
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-364-
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MIDLAND, MICHIGAN
SHEET
18 of 36
PROJECT --v /— -> f^ .—. __ JOB NUMBER
C.OAL- ryg.iTic Ee AND
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-365-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
PROJECT — , >-? -~, f-, -7- JOB NUMBER
COAL - ryGtr/c SULFUR REMOVAL - INSTRUMENTS 73062.3
PHASE _- CASE Br .- ^_^ DATE ff NUMBER
1 TASK 2 £:. w. CEZMAK 6S7
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-366-
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
£00f 36
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-367-
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PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEfT
2/0,36
PROJECT -^ f— j ^-> — . — . JOB NUMBER
COAL - Pyzmc OULFUZ REMOVAL — INSTRUMENTS 73O62.3
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MIDLAND, MICHIGAN
ftHCCT
"°JECT COA L - F^etT/c SULFUR REMOVAL. - Z^MSTRUMENTS '°*73o623
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7
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
PROJECT ^->
COAL -
P«ASE
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FACTOR!
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-------
PRELIMINARY CAPITAL - DETAIL SHEET THE °°» CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
24 OF 36
PROJECT ^^ .— * <~-N .— j -— . JOB NUMBER
UOAL - ryje/r/c ouLFY DATE EF NUMBER
I TASK a &.tf/.C£WIK 657
SECTION NUMBER 1 NAVE
//OO-JJSON SuLFATE REMOVAL
FACTORS
ITEM
LC
//o PLATE
FLOW ^Ecojeoejs AMD
co^reoLLEe w/ SHELF
AND CABLES.
DJFFE.KENTIAL PKESSUKE
TYPE FLOW TeAMSMlTrER.
M// MA M/FOL D.
/ "OeiF/cE ELANQES
AND PLATE
/-/SOLB GLOBE TYPE
CoMreoL. VALVE w/
*/p TSAMSDVCEie..
SECTOR NUMBER «• NAME
(QUANT. 1
QUANT.
/
/
a
£
/
/
. /
/
/
/
[MATERIAL H
CONSTRUCTION
MATERIAL
ALL
3/6
304 FLAHQES
w/ 3/6
PLATE
ALL
3/6
3O4 f-LAMGK
W/ 3/6
PLATE
ALL.
316
CONDITION + COMPLEXITY]
DESCRIPTION
r~U£NISHED AS PAST OP
//OO - F~~£ f/L TEG
CONTROLS.
FU&NISHE-D AS PAST Of
//oo-F-a nLTze
CONTROLS.
FliKNlSHED AS PART OF
/ //on — /^" ? f^l / TTP
CONTZOL.S
Cve£QD -1.6
= MJ(19 )
140
466
7£5
£37
1175
725
166
662
FORM 9WM PRINTED IN U.S.A. M14I
-371-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
^5'or36
PROJECT s~\ /—) /-> /— 1 T Jot "UM»ER
COAL - r^re/T/c ZDULFUZ . &£MOYAL - JLNsreuMEMTs 73 'O 623
PHASE _. CASE BV _. DATE EF NUMBER
/ Z4s^£ e.W.Ce&MAK • 667
SECTION NUMBER 1 NAME
IIOO-lEON SULFATE REMOVAL
FACTOR!
ITEM
LSH/L
fl/3
LAH/L
///3
tec
1114-
LT
JH4-
LV
11/4
&ec
///5~
FT
II IS
FEL
///s
rv
///s
Ae
///6
AIT
///&
BASE X ESC. X CAPACITY
NAME OF FACILITY
HlGH/UOH/ LEVEL
sw/rc/Y.
ALA eM AMNUUC/A TOR
PO/MT^S
LEVEL &ECOJSDEK. AND
COMTEOLLEe W/ SHELF
AMD CABLES.
D/FFEEE.HTJAL P&ESSUI2E.
TYPE L£\/EL 7eA^SMlTTE.K.
W/ MAM /FOLD.
l"-j5OLB GLOBE TYPE
CotsreoL VAL VE. w/
Z/p POSir/OAf££.
FLOW ^ECOXCEB. AMD
COfiJTEOLLEZ W/ SHELF •
AND CABLES.
FLOW- ~r~o - CUZK.ENT
CON VE^TEJS w/ /o OFT
OF CABLE
3 " MA$M£-r/c FLow-
METEE.
3"-/5OLB &ALL TYPE
CONT/SOL VALVE . w/
Z/p TeAHSDUCEZ.
HYDEOQEN - JON COM -
CENTRA~no*j FECO&DER.
^/Sh/ELF AND CABLES
HYDROGEN -/ON IN o/ CAT-
INQ 7TSANSM /TTEZ W/
/-//$/ f /t.otV ALA f&l SiV/TcH
SECTOR NUMBER * NAME
X QUANT.
OUANT.
/
2
/
/
/
/
/
/
/
/
/
( [MATERIAL
CONSTRUCTION
MATERIAL
STEEL AND
POBC.ELAIN
^/ 3/6
Tg/*f
ALL
3/6
STEEL
w/ 3/6
Te/M
TEFLOH »//
TANTALUM
ELECTRODES
ALL
3/6
•f CONDITION + COMPLEXITY]
DESCRIPTION
DISPLACEMENT TYPE
CV£EQD = 5T5"
C^EQD^/IO
= M$(19 )
£50
140
1175
7^5
597
117.5
847
iizs
9/2
466
700
ram MSO PRINTED m U.S.A. RHI
-372-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
26 OF 36
PROJECT, v /—. x-\ . /— 3 _ JOB NUMBER
COAL - J^ygmc OULFCJR REMOVAL - INSTRUMENTS 73O&Z3
PHASE CASE »Y DATE tf NUMBER
I TASK 2 JE.W.CZKVAK.- . 65"7
SECTION NUMBER 1 NAME
IIOO-T&ON SULFATE. REMOVAL
FACTORS
ITEM
AE
///6
M%
/II6
L£
///7
LT
///7
FRC
IIIQ
FT
Hid
FE
FX
nid
rv
1118
L5%
/i/q
LA%
///
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DO» CHEMICAL COMPANY
MIDLAND, MICHIGAN
PROJECT —
COAL -
PHASE
WEET
27 OF 36
PY&/T/C SULKUZ. &EMOVAL - INSTRUMENTS "* 7*30 62$
CASE »r ^^ DATE EF NUMBER
TASK £ K?.WC££MA£ 657
SECTION NUMBER * NAME
HOO-lEOM SuLFATE REMOVAL
FACTOR!
ITEM
PI
/tao
//^^
TE
71V
BASE
SECTOR NUMBER » NAME
X ESC. X CAPACITY XQUANT. X [MATERIAL + CONDITION + COMPLEXITY] § = MJ(19 )
NAME OF FACILITY
CAP/LLi
SEAL.
~SSU£E (yAifqE w/
t\zy TV DEMOTE
THERMOCOUPLE ELEM-
ENT w/ T/-/E&MOWELL t
HEAD AND JP.ECO&DEZ
POINT.
THERMOCOUPLE ELEMENT
K// TtfE/eMO WEL L /-/EA D
AND &ECOEDE/2 ' PO/N7~.
PXoe4T*M,'
QUANT.
2
'
'
CONSTRUCTION
MATERIAL
//V TEFLON
SEAL
T/TAN/UM
WELL
3/6
WELL
DESCRIPTION
'or^("eKnM'^
340
250
/30
7rJ
sttt?.
FORM 3M» PRINTED III U.S.*. RUt
-374-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
280f36
'K°*"CoAL - P/smc SULFUE. REMOVAL - IvsreuMEMrs ™j3o623
PHASE CASE BY _. ^_ DATE IF NUMBER
I TASK 2 e.W.CczMAK . 657
SECTION NUMBER & NAME
/4OO - D/ST/LL Ar/ow
FACTORS
ITEM
Le
I4oo
LT
I4OO
LRC
1401
LT
1401
7ZV
/40Z
TE
TVS
/40Z
Fee
1403
rr
1403
FE
FX „
/403
rv
1403
P£C
/404
BASE X ESC. X CAPACITY i
NAME OF FACILITY
L£VEL £?ECOeDEG. w/
SHELF AMD CABLES
D/FfEEEUTfAL PJSESSU&E
TYPE LEVEL TSANS^ITTEE
W/MA*/FOLD.
LEVEL teecogDEe. AMD
CONTROLLER. \^/ SHELF
AMD CABLES.
PlFFE&EMT/AL P£ESS(JG£
7~yp£ LEVEL rZAMSM/TTZg
to/ MA M/FOL D.
t "
~£ SELF -OPERATED.
TEMPERA TTJgE CQMrgOt-
VALVE
TEMPEEATUS.E BULB,
WELL AMD CAP/LLA&Y
FLOM y^ECOffDEjS AtJD
COfijrgOLLEE v// SHELF
AMD CABLES.
D/FFESENT/AL PffESSUSE
TYPE FLOW TZAMSM/TrEK
VS/ AfA^ /FOLD
6 '"O&/FICE -/^AN^ES
AND PLATE
4."-/5OLB C^t-oBE TYPE.
Covreot- VALVE */
X/p T&AMSDUc£.£
P/ZESSUK.E £?£Coet)EG.
AMD CONTkOLLEB. IA//
SHELF AND CABL.ES
SECTOR NUMBER fc NAME
(QUANT. !
QUANT.
/
/
/
/
/
/
/
/
/
/
/
[MATERIAL
CONSTRUCTION
MATERIAL
ALL
3/6
ALL
3/6
3/6
»// 3/6.
re/w
ALL
304-
ALL
3/6
STEEL
iv/ 3/6
PLATE
STEEL
*>/ 3/6
T&M
CONDITION + COMPLEXITY]
DESCRIPTION
CV2£QD=4.5
TMTE^ZAL PAST OF
TCV-/402. ABOV£
CyEEQD - I3O
= M$(19 )
466
Q55
1175
725
550
1175
725
757
//22
/1 75
FORM 996iO PWHTEO IN U.IA. "l-6»
-375-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
n°'™CoAL - Pfg/T/c. SuLFu/e &MOVAL - INSTRUMENTS " 73*0 623
PHASE CASE BT __ -^ DAT* If NUMBER
_F TASK 2 £>.IA/C££MAK 657
SECTION NUMBER I NAME
/4oo ~ J2/577LLA T?OA/
FACTORS
ITEM
/4o4
PV
/404
T2C
1405
TT
I4&5
TE
TvS
1405
TV
/40S
LEG
14-06
LT
1406
f&
re
/407
/407
BASE X ESC. X CAPACITY
NAME OF FACILITY
DlA PH1ZA GM TYPE
/-/SOLS (jLOBE TYPE.
CONTROL VALVE •*>/
TEMPEZATUZ.E &LCOBDEK.
AND COMTJS.OLLE&. \«//
SHELF AMD CABLES
£?£S/STAfi/CE -TO -
CUR.K.ENT CONVERTER
£?£SlsrArtC£ THERMO-
METER ELEMENT n//
WELL AMD HEAD.
6"-/25LB H.D. ]A/AFEK.
BUTTE&FLY Cbt/TjeOL \/AL\tE
W/ fyp POS/T/OMEE..
LEVEL &ECOE.£>£.£ AMD
COMTZOLLEe W/ SHELF
AND CABLES
D/FFEZENT/AL PRESSURE
TYPE LEVEL TeArtSMfTrER
W/ MAM/FOLD.
3"-/SOLB GLOBE TYPE
CONTTSOL VALVE \*//
-%, POS/T/OME&:
/^.OW &ECO&DEZ W/
St-fELF AND CABLES
DIFFERENTIAL PRESSURE
TYPE PLOW 772AMSA4/7TE&
W//JA A/ /FOLD.
SECTOR NUMBER I NAME
(QUANT.
QUANT.
'
'
'
'
'
'
'
>
/
/
'
( [MATERIAL
CONSTRUCTION
MATERIAL
ALL
3/6
STEEL
w/ 5/6
316
WELL
. STEEL
w/ 3/6
ALL
3/6
STEEL
V/3/6
ALL
3/6
\ CONDITION + COMPLEXITY]
DESCRIPTION
i *p
C- r/ KEQ D «
Cy J5£QD - 6OO
Cv gEQD - 75"
= MJ(19 )
535
597
1175
535
134
7/7
1175
72,5
/0/.7
466
7Z5
FWM 1»H PKINTEO IN UAA. Rl-O
-376-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE cow CHEMICAL COMPANY
MIDLAND, MICHIGAN
ftHEIT
300F^6
r*°'l"CoAL - Pyemc SULFUZ gtMOWL - TMSTJSUMENTS "730623
PHASE CASE §T . s~^ OATE EF NUMBER
I /%Sf ^ g.W.CE&MAK. 657
SECTION NUMBER I NAME
/40O- D/sr/L LATION
F ACTOSS
ITEM
FE
FX
1407
rec
{408
n~
1408
FE
FX
/408
FV
I4OQ
rec
1409
TT
/40
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
31 or 36
PROJECT /—>,•—./—> -I- JOB NUMBER
COAL - Py'eiT/c SULFUR REMOVAL - JTMST/ZUMELNTS 730 62.3
PHASE CASE •» __ . . _. DATE EF NUMBER
/ TASX 2 g.W.CzeMA* ^57
SECTION NUMBER I NAME
/4oo- D/ST/LLAr/oM
FACTOR!
ITEM
L.K
I4U
LT
1411
LRC
14 1£
LT
/4/2-
LV
14-12.
Fee
/4/3
FT
14-13
FE
FX
/4/3
FV
J4/3
TEC
/4I4
TT
/4-/4-
BASE X ESC. X CAPACITY
NAME OF FACILITY
sLZVEL &ECOEDER. W/
SHELF AMD CABLES
DIFFERENTIAL PSESSUEE
TYPE LEVEL T-KAHSMlTr&i
W/MA /V/ FOL D .
LE.VEL f2.Ecoe.DER. AND
CONT&OL.L.E& W/ SHELF
AND CABLES.
PLUSH DIAPHRAGM
TYPE LEVEL TGANS-
MtTTEe..
I"- /so LB JACKETED
£jLOBE TYPE. CoMre.oi-
VALVE w/faposmortEE.
/=Lo\A/ RECORDER AMD
aoMT-eoLLEtz. kv/ s/y£i/
AND CABLES.
D/FFEfZENTlAL PeESSUHL
TYPE FLOV/ 7~E.ANSMnTEK.
IV/ 'MA* '' 'FOLD
8" O&F/CE fi-AVGES
AND PLATE
6"-/25LB H.D. WAFEK
BuTTE&FLY CotJTeoi. I/ALVE
w/ Z/p TRANSDUCES.
TEMPERATU&Z &KO&DEK.
AMD CONTROLLED W/
SHELF AND CABLES
&ESISrANCE -TQ-
aU/2/e.CNT CON\SEGTOe
SECTOR NUMBER « NAME
< QUANT.
QUANT.
/
/
/
/
/
/
/
/
/
/
/
x [MATERIAL
CONSTRUCTION
MATERIAL
ALL
3/6
ALL
3/6
STEEL
"/ 3/6
TZIM
ALL
3/6
STEEL
™j 3/6
PLATE:
ttOH AMD
STEEL
v/ 316
TR/M
1- CONDITION + COMPLEXITY]
DESCRIPTION
TUT-E&FACE CONTROL
CV£EQD = /2
Cv &EQD = 42$
= M$(19 )
466
85^
/1 75
72.0
877
1175
7^5
/74
847
1175
S35-
FOH 39CSO PRINTED IN U.J.A. RUI
-378-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
IMttT
3c OF 36
non™CoAL — F'ygjr/c SL/LFUZ REMOVAL — J'NSTK.UME^ITS '^7^0623
PHASE CASE BY ^^ DATE Ef NUMBER
I TASK 2. £.W. L£et
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE °ow CHEMICAL COMPANY
MIDLAND. MICHIGAN
PROJECT ^->
COAL -
PNASE
SHEET
33 OF 56
/^y/s/T/c SULFUK REMOVAL- XMSTBUMZ-MTS i°*73o623
CASE BY __ • DATE EF NUMBER
Z45AT 2 £:.W.CE:ewA£ . 6S7
SECTION NUMBER 4 NAME
/4-oo - D/-3T/LL A noti
FACTOR!
ITEM
PT.
TE
rw
TSL
/4-/9
TAL
1413
BASE
SECTOR NUMBER » NAME
X ESC. X CAPACITY XQUANT. X [MATERIAL + CONDITION + COMPLEXITY] = MJ(19 )
NAME OF FACILITY
^2' 'PffESSUZE (jAUrA-L(P££ r/e/^/A')
170
780
100
_
70
3-5,32?
4,308
nmt 1M90 PRINTED IN UAA. RKI
-380-
-------
PRELIMINARY CAPITAL - DETAIL SHEET ™E DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
34 OF 36
PROJECT ^~ /— 1 ,— ' /— 1 -r- JOB NUMBED
COAL - Pye/r/c SULFUZ REMOVAL - INSTRUMENTS 73O&2.3
PHASE CASE BY OATt EF NUMBER
.7 /^s*- 2 &V/.CE.KMAK 657
SECTION NUMBER ft NAME ±
J5OO- VENT COLLECT qSceue.
FACTORS
ITEM
Z£>C
/5~^0
Z.T-
/5~o0
A/
/5£>0
/4£
/50/
AIT
/SO/
AE
/50I
AAL
1501
L£C
/soa
L7~
/502.
LV
/soa
AP
/S03
BASE X ESC. X CAPACITY !
NAME OF FACILITY
LEVEL &ECOGDEIZ AND
COMTgOLLEe. w/ SHELF
AMD CABLES
D/FFEZENT/AL PGCSSUGE
TYPE LEVEL T&AHSM/TrEZ
w/ MAM /FOLD
/"-/5OLB GLOBE TYPE
CONTROL VALVE iv/
*/p Pos/T-/oMEe.
HYDKOGEM-/OM Co/s-
CEUT&AT/OM &ECO&DEK
W/ SHELF AND CABLES
HYOZO&EU-/OM IHDICAT-
/NG, T~£AAlSM/rrE:g. \*//
LOW ALAP-M SWITCH.
HYDeoQELfiJ '- /V /JD T 5/>£e/Fl£D )
FLO^-THKU TYPE
Cy JSEQD = ?
(FL£W A'OT 5P£C/P)SD] _
= MJ(19 )
1175
72.5
597
466
700
400
70
1175
7Z5
517
466
ram neso PRINTED IN U.S.A. «H>
-381-
-------
PRELIMINARY CAPITAL - DETAIL SHUT THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SHEET
3£or 36
"*°""COAL - PYZ/T/C SuL.ru e REMOVAL - TMST&MENTS "* 730 62.3
PHASE ._ CASE BY _ , _ DATE If NUMBER
£ TASK 2. &.W.CE&MAK 657
1ECTION NUMBER I NAME J _ .
/5~OO -VENT COLLECT $ SCEUB
FACTORS
ITEM
AIT
/503
A£
/503
AAL
/S03
LS%
1504-
M%.
1504-
PI
/50S
ISO 6
TE
nv
BASE X ESC. X CAPACITY
NAME OF FACILITY
CoNDucTrv/ry IMD/CAT-
INQ TeAMSwnrzK. »//
LOW A LA KM sw/rcti.
CoNDUcriv/rY SENSOZ.
w/ ELECmODES AND
SAMPLE CHAMBE/S
ALAZ.M AMMUMc/AToe.
POtMT
H/$H/LO»S LEV£L
SW/T-CH
ALASM AA/MWC/AT~O&
Poturs
42'PzE.ssuG.E GAUGES
THERMOCOUPLE ELEMENT
W/ TV£eMOW£LL, HEAD
AMD gECoeoee po/tsr
f*& o&^ Tt? M,
SECTOR NUMBER 1 NAME
(QUANT.
QUANT.
/
/
/
/
a
^
a.
^ <:
X [MATERIAL
CONSTRUCTION
MATERIAL
.
'P/C A*">
CAZBON
*.
STE^L AND
PO£C£LAIN
iv/ 3/6
T&M
STEEL
ELEMEW
3/6
WELLS
*• CONDITION + COMPLEXITY]
DESCRIPTION
/2 OH/ - THeu TYPE
DISPLACEMENT T~YPE
Tor&i-(PeZ- n?A/»)
= M$(19 )
soo
175
70
250
140
SO
2.60
8,541
1) 204.
<7>74£
FOIW 3X50 PRINTED IN UAA. RIO
-382-
-------
PRELIMINARY CAPITAL - DETAIL SHEET THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SHEET
36 OF 36
P"°JEC1 COAL - P/e/r/c SULFUR REMOVAL - J^^/sreuMENrs ""730623
PHASE CASE BY DATE EF NUMBER
I TASK 2 X?. MCeevAK £57
SECTION NUMBER A NAME
M/SCELLANEOUS JfosTJSUMEWS
FACTORS
ITEM
7~X?
r£
nv
FOR
'ABOVE.
77
T£
rw/
/"o,e
/£ W/DE ST&IP
CHAP.T FQ£ 7U£gMOCOUf>tf$
THERMOCOUPLE ELEMENT
n"/ THEKMOMELL AND
>JUMCr/OM HEAD
TfiMPEKATUEE. INDICATOR
SO POINT t DIGITAL READ-
OUT' w/ OPTIONAL LOQC^E.R.
THERMOCOUPLE ELEMENT
tv/ TMEEMOWELL AND
POINTS
ELEMENTS AND COSTS
LISTED UNDER INDIVIDUAL
SECTORS,
J^NCL U0ES A NNUMC I A TOG
P/LOT L/GH7S, PUSt/B'JTrONS
AND ALL /NSTffu^f^^/TS
/^STALLED AMD M£££>
= MJ(19 )
3500
6SOO
5~0,6OO
6>O,(>OO
&Q&OQ
-o-
FORM 99650 PRINTED IN U.S.A. RKI
-383-
-------
Table 25. SUMMARY OF INSTRUMENTATION COSTS BY SECTORS
SECTOR
ALARM
TEMP.
POINTS POINTS
MISCEL-
PANEL PANEL LANEOUS INSTRUMENT INSTRUMENT
SPACES SECTIONS INSTRUMENTS COST COSTS
(2FT. WIDE) COST (EX MISC) (INCL MISC)
CO
I
100
200
400
500
600
700
800
900
1100
1400
1500
TOTAL
1 1 15
10 43 176
8 0 17
2 1 11"
13 1 23
21 5*
13 3 28__
9 9 16
13 2 45
8 6 38"
4 2 10j
83 69 384
1 $ 2,058
10 27,616
1 3,131
2 1,431
3,873
2 540
6,340
1 2,435
3 6,993
3 4,979
f 1,204
23 $60,600
$ 14,
195,
22,
10,
27,
3,
44,
17,
49,
35,
8,
$429,
600
957
219
153
482
835
986
276
619
329
541
997
INSTALLATION
TOTAL
INSTALLED COST (PER TRAIN)
$ 16,
223,
25,
11,
31,
4,
51,
19,
56,
40,
9,
$ 490,
613,
$1,103,
658
573
350
584
355
375
326
711
612
308
745
597
246
843
Temperature point count is for temperature recorders (TR's) only.
Temperature points for temperature recorder/controllers (TRC's) a
included with the TRC's.
are
-------
10.4 REACTION SYSTEMS
The reactor system was given thorough mathematical modeling
which was discussed in Section 4.2.
10.4.1 Computer Programs for Reaction Systems
Computer programs for the various reactor configurations
are listed in the following pages.
Reaction system calculations were done on an EAI #640 dig-
ital computer with a 16,000 word memory and eight sense
switches. The programs were written in-standard Fortran
IV computer language except for the use of logical vari-
able SENSW. In these programs SENSW(N) is interpreted by
the compiler to check the Nth sense switch for a true or
false condition. To use these programs with other machines
the variable SENSW(N) will have to be assigned a true or
false value before it can be used in a logical expression.
Proper units for data input are specified on comment cards
in the program. Concentrations used in calculating chemical
reaction rates are in units of Ib moles/cu ft. Molecular
weight and density data were taken from "The Handbook of
(25)
Chemistry and Physics" with the exception of the molec-
ular weight of coal. A value of 13 was used for the molec-
ular weight of pyrite-free coal to maintain consistency
between this report and the TRW report
In the batch reactor and the plug flow reactor programs
(programs A and C) the reaction rate equations in Section
4.2.1 are integrated directly with the fourth order Runge-.
Kutta integration subroutine. For well mixed tanks or well
-385-
-------
mixed sections in series (Program B) the steady state
equation
input + generation by reaction = output
is solved by an iterative method.
In Section 4.2 four reactor systems are summarized. Pro-
grams A-C were employed for these evaluations as follows:
Table 5 Batch Reactors
Table 6 Continuous Reactors,
-with External Regeneration
Table 7 Continuous Reactors
in Series
Table 8 Continuous Reactors in
Parallel
Program A
Program B
Program C
Program B
Program B
-386-
-------
PROGRAM A - BATCH REACTORS
PAGE 1 C BATCH REACTOR FOR FERRIC SULFATE LEACHING OF PYRITIC SULFUR
C FROM COAL WITH OXYGEN RECIRCULATION — 0, FEAR
C
C
C 1«COAL SOLIDS FREE OF FES2
C 2»FES2
C 3«S
C 4»FE2(S04>3
C 5sFES04
C 6*H2S04
C 7»H20
C 6*02
C 9«INERT GAS
C 10=H20 VAPOR
C
C REACTIONS AREl 4,6FE2(S04>3+4.8H20+FES2=10.2FESp4*4.8H2S04*.85
C FES04t,5H2S04*,2502 = '.'5FE2,M0<10),NAME<10,3>,STF2(8).STF5(8>.W{10),W0<10),MW(
Sl0),DERlV(ll),FEED{8),MFEED(8)
DATA MW(l)iMW(2>,MW(3>,MW<4),MW(5),MW<6),MWC7).MW<8).MW{9).MW<10)/
S13,, 119,96,32. 06.399,86,151, 90i 98'. 08,18.02,32.. 35., 18.02/
DATA RHos/90,/
DATA STF2(1),STF2(2),STF2(3),STF2(4),STF2(5).STF2(6).STF2(7),STF2(
SB)/,0,1,,-.8,4.6,-10,2.-4.8,4.8,,0/
DATA STF5{1),STF5(2).STF5(3),STF5(4)ISTF5(5),STF5(6).STF5<7),STF5(
S8)/',0, ,0;.0,-'.5,l.'0( »5.-,5,-,01l842l/
DATA NAME(1,1),NAME(1.2).NAME(1.3)/4HCOAL,4H(PUR'.4HE) /
DATA NAME(2,1).NAME(2,2),NAME(2,3)/4HFES2,4H .4H /
DATA NAME(3.1),NAME(3,2>.NAMfcC3.3)/4HS ,4H ,4H /
DATA NAME(4,1).NAME(4,2) .NAME(4.3)/4HFE2(.4HS04),4H3 /
DATA NAME(5.1),NAME(5.2),NAME(5,3)/4HFES0.4H4 ,4H /
DATA NAME(6,1),NAME(6.2>,NAME{6,3)/4HH2S0.4H4 ,4H /
DATA NAME(7,1),NAME(7.2),NAME(7.3)/4HH20 ,4H ,4H /
DATA NAME(8,1),NAME(8,2),NAME(8,3)/4H02 ,4H ,4H /
DATA NAME(9,1).NAME(9,2),NAME(9,3)/4HINER.4HT GA.4HS /
DATA NAME(10,1),NAME(10,2) ,NAME(10,3)/4HH20 .4HVAP0.4HR
FLAGI*.-FALSE.
PF LA G«,FALSE.
!F
-------
PAGE 2 c BATCH REACTOR FOR FERRIC SULFATE LEACHING OF PYRITIC SULFUR
DH5»0,0
C READ INPUTS IN TONS/HR AND TOTAL TONS OF OXYGEN TO BE FED IN
4 IN«6
READUN,100XFEED(n,I=lf7)iHBTOT
02FAC*0t0
lF/MW
10 TIME30.0
TPRINT»0,0
TEMP0=TEMP
WRITE(6, 101)
IF(,NOT,PFLAG)GO TO 13
WRITE(6,113)
NRITE(6,114)
GO TO 24
11 KL«2.E05«EXP(-3524,67/(TEMP*273,2)>
KR«6,439E08«EXP(-6646,5/(TEMP*273. 2) )
RATEle-Cl*KL/M(l)*Y«V«M(2)*»2
IF(M(1),LE,0.0)RATE1=0,0
RATE2«-KR#P8/VL«M<5)»*2
IF(VL,LE.0,0)RATE2»0,0
DO 12 I'l,6
12 DERIV( DsMFEEDd )*RATE1»STF2DH5«RATE2-U*AREA»(TEMP-TA)
VT0»VT
13 CALL RUNGE(ll.M,DERlV,TlMEiDT,IFLAG,MFLAG)
Y«2i»M{4)/(2>M(4)*M(5))
MST*0,0
DO 14 I«lV3
14 WST*HST*M(I)*MH(I)
-388-
-------
PAGE 3 C BATCH REACTOR FOR FERRIC SULFATE LEACHING OF PYRIT1C SULFUR
WLT»0,0
DO 15 I«4,6
15 WLT«WLT*MU)«MWU)
W7«M<7)*MW(7)
HCPT = 1,8««WST*WLT)»,3*W7>
C CALC TEMPERATURE
TEMP*M<11)/WCPT
IF(WCPT,LE,0.0)TEMP«TEMP0
WLT»WLT*W7
WFLS«1,-M<7)*MW<7)/WLT
IF(WLT,LE.0.0)WFLS»0.0
C CALC LIQUID DENSITY IN LB/CU FT
RHOLs62,43*<1.001*.72434*WFLS*.94305«WFLS»«2 + .108
C
VP70=EXP<13,6953-3215.4/(TEMp*273.2>-333070, /< TEMP*273 .2
VP7«VP70*<,99973-.0863*WFLS-.16059*WFLS**2)
C
C CALC LIQUID VOLUME AND TOTAL VOLUME IN CU FT
VLsWLT/RHOL
VT«VL»WST/RHOS
C
C CALC AVG DENSITY OF REACTOR MIXTURE IN L8/CU FT
RHOAVG=(Wl_T + WST)/VT
C
C CALC HEIGHT OF LIQUID IN REACTOR
HsVT/AREA0
C CALC AREA FOR HEAT TRANSFER
AREA«AREA0*C1R»H
C
C CALC PRESSURE OF LIQUID HEAD IN PS I
DPL*H»RHOAVG/144.
C
PG«PRESS*DPL/2.-VP7
IF(PG,GE.0,0)GO TO 18
PG«0,0
PRESS»VP7-DPL/2.
18 P8«PG*,9»02FAC
IF
W0(I)sTlME*FEED( D/2000,
20 MFEED-0,0
WCPF"0i0
GO TO 25
22 IF
-------
PAGE 4 C BATCH REACTOR FOR FERRIC SULFATE LEACHING OF PYRlTIC SULFUR
IF(FLAG1)GO TO 26
WRITE(6,116)
GO TO 27
26 WRITE<6,117)
27 WR1TE<6,1.02)TEMP0,TEMP
C CONVERT VT FROM CU FT TO GAL
VT*VT«7.48
WRITE(6,112)VT»TIME
WRITE(6,103)PRESS.CONV
WR1TE<6,104>
WT80.0
W0T*0.0
00 30 I«l,10
H
35 WRlTE<6,105)(NAME< I,K) ,Ksl,3),M0(I ),M( I)
WRJTE(6il09)
WRITE(6ill0)M0T.MT
1F(FLAG1)GO TO 40
FLAG IB .TRUE,
GO TO 10
40 CALL EXIT
100 FORMAT(11F10.0)
101 FORMAT<1H1«3X,70HF£RRIC SULFATE LEACHING OF PYRITIC SULFUR FROM CO
SAL IN A BATCH REACTOR.///)
102 FORMAT
112 FORMAT(/,5X,21HREACTOR VOLUME, GAL « ,F9, 0. 11X, 20HRES I DENCE TIME, H
SR »,F6,2) •
113 FORMAT<5X,5HTIME..4X,4HFES2,4X.9HFE2(S04)3,4X,5HFES04.4X,5HH2S04.4
SX.2H02.4X.9HH20 VAPOR)
114 FORMAT(7X,2HHR,1X>2K1H-),16HQUANTITY* LB MOL* 2K1H*),/)
115 FORMAT(1X,F9.1,F9.2,F10,2,F11.2,F9,2,F8.2,F9.2>
116 FORMAT(33X,10HFlLL CYCLE)
117 FORMAT<33X,11HBATCH CYCLE)
END
-390-
-------
SUB-ROUTINE A-l
PAGE i c RUNGE.KUTTA INTEGRATION SUBROUTINE
SUBROUTINE RUNGE
-------
PROGRAM B - RECIRCULATING REACTORS
PAGE 1
RECIRCULATING FLOW REACTOR CALCULATIONS
D, FEAR
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
Mi* ******
• *
* *
*****
* *
JMAX * NO, OF REACTORS IN SERIES
NMAX * NO. OF CSTR'S IN SERIES PER REACTOR
RR t RECIRCULATION RATIO
NPR « NO. OF PARALLEL REACTOR TRAINS
« *
***•*
•*•**••*»*«»M
1*R 1
R
LOGICAL SENSW
LOGICAL FLAGI
INTEGER DFAC
REAL M0,M,MW,MT.MI,MIT,NAME,MI02
DIMENSION M0<10>,M{10),MW(10),M!(10),NAME<10,3>.W<10).WI(10)
DIMENSION OLDM<7>.-W8C10).W9<10>
COMMON /COMMl/QLOSS
DATA UP.DOWN/4HUP .4HDOWN/
DATA RHOS/90./
DATA MW<1),MW<2>,MW(3)»MW<4) ,MW<5).MW(6).MWm.MW<8),MW<9),MWU0)/
S13,1119,96,32.06.399.86,151.90.98.08,18.02,32.•35.•18.027
DATA NAMEC1,1>,NAME(1.2>,NAME<1,3)/4HCOAL.4H(PUR,4HE> /
DATA NAME<2,1),NAME<2,2>,NAME<2,3)/4HFES2,4H ,4H /
DATA NAME(3,1) ,NAME(3,2) .NAME(3,3)/4HS , 4H i4H /
DATA NAME(4,1),NAME(4,2),NAME(4,3)/4HFE2(,4HS04).4H3 /
DATA NAME(5,1).NAME{5.2),NAME(5,3)/4HFESO,4H4 ,4H /
DATA NAME<6,1),NAME<6.2>,NAMEC6,3)/4HH2SO,4H4 ,4M /
DATA NAME(7,1),NAME(7,2),NAME(7,3)/4HH20 ,4w ,4H /
DATA NAME(8,1),NAME(8,2).NAME(8,3)/4H02 .4M ,'4H /
DATA NAME(9I1),NAME(9,2),NAME(9.3)/4HINER,4MT GA.4HS /
DATA NAME(10.1),NAME(10,2),NAME(10,3)/4HH20 .4HVAP0.4HR /
READ INPUTS IN TONS/HR
IN*6
READ=WI(I
H(I)»NIfI)
10 M0(I)»MI(IJ
-392-
-------
PAGE 2 C RECIRCULATING FLOW REACTOR CALCULATIONS — Di FEAR
MI02=MI<2)
T0»TM
C CALC REACTION PROM MIXING TANK
J'0
IF(SENSW(4))GO TO 11
CALL CSTR(1,TM,PM,VM,,0,1,M0,M;HW;RESTIM,HODM)
GO TO 25
11 DO 999 I*li7
MCI>sM(l>/FLOATCNPR)
M0U>«M0
999 MI(I)sM0(I)
12 J»J*1
T0»TEMP
ir
M(8)=M0(8)
MI(9)=W9(J)«2000,/MW(9)/FLOAT
WRJTE(6,101)J
IF(J.EQ,0)GO TO 28
HRITE(6,113)NMAX
WRJTE(6,114)RR,DIR
26 HR1TE(6,102)T0.T
WR1TE(6,111)P,QLOSS
WRITE(6,112)RV,RESTIM
-393-
-------
PAGE 3 C RECIRCULATING FLOW REACTOR CALCULATIONS •• 0, FEAR
WRITE(6,103)CONV,CONV0
IF *MW
35 WRITE(6,105)(NAME( I,K).Ksl,3).MI
116 FORMAT
-------
SUB-ROUTINE B-l
PAGE 1
SUBROUTINE CSTR(NMAX,TEMP,PRESS,VOL»02FAC,DFACiM0,M';MW,RESTIM,HOD)
C CSTR CALCULATIONS FOR FERRIC SULFATE LEACHING OF PYRJTIC SULFUR
c FROM COAL --- D, FEAR
c
C 1'COAL SOLIDS FREE OF FES2
C 2« FE S2
C 3»S
C 4»FE2 ,0,.0. -.5.1.0, ,5,-,5,,25/
DATA RHOS/90,/
C
TA*21,
U«2,
DH2«99000.
DH5«33480.
TFLAGs.TRUE.
PASSl'.TRUE,
IF(,NOT.SENSM(7))GO TO 5
TFLAG», FALSE*
M0(10)=0.0
QLOSS«0,0
WCPG0=,403»M0(8)»MWt8)*,225*M0(9)«MW(9)
C CONVERT VOLUME FROM GAL TO CU FT
RVL«VOL/7.48
C CALC REACTOR HEIGHT AND DIAMETER IN FT
DIA«««.3333
H»HOD»DIA
-395-
-------
PAGE 2
Ci«MW<2)/MW
WSTs0,0
DO 14 1=1,3
14 WST«WST*M( D*MW( n
WL T« 0. 0
DO 15 1*4,6
15 WLTsWiT+MU>«MW< I)
W7sM(7)»MW<7)
IF(,NOT,PASS1)GO TO 16
WCPT0=WCpT
PASSls, FALSE.
16 WLT=WLT*W7
WFLS=1.-M(7)»MW(7)/WLT
RHOL=62,43»(l,00l*,72434«WFLS*.94305«WFLS*«2*.10874*WFLS*«3>
VP7BVP70*{, 99973-. 08 63*WFLS-,16059*WFLS*»2)
CALC LIQUID FLOW RATE IN CU FT/HR
FL»WLT/RHOL
TAU«(FL*WST/RHOS)/RVL
CALC AVG DENSITY OF REACTOR MIXTURE IN LB/CU FT
RHOAVG»(WLT*WST)/TAU/RVL
CALC PRESSURE OF LIQUID HEAD IN PS I PER STAGE
DPU«H*RHOAVG/144 ./RNMAX
PTAVG=PRESS*DPL«(FLOAT(N)-,5)
CONSTsK«»(pTAVG-VP7)/FL/TAU
17 BsM(9)-M0(8)*STF5(0)*CONST»OLDM5««2
C«4,*M0(8)*M(9)/(8««2)
IF(C,GE, ,00005)60 TQ 18
M(8)*M0(8)*M{9)/B
GO TO 19
18 SIGN=1,D00
IF(B,LT,0. 0) SIGNS- 1.D00
eOBL'B
CDBL»C
M(8)aBD8L«(SlGN»DSQRT(l.D00*CD8L)-l,D00)/2.De0
19 A*CONST«STF5(5)*M(8)/(M(8)*M(9)>
IF(M(8),|.E,0.0)A = 0.0
C5 »M 0( 5) *S TF 2( 5J »0 LD DM 2
-396-
-------
PAGE 3
C«4,*A*C5
IFCC.GE, ,00005)GO TO 20
M(5>=C5
GO TO 21
20 ADBL=A
CDBLsC
M<5)=/ADBL/2,D00
21 CONTINUE
lF{SENSW(l))WRITE(6,109)M0(5),OLDM5,M(5),C5iDM2,A,C;M(8)
CALL CONV(OLDM5.M(5)tl.NC,,00002)
IFfNC.EQ.DGO TO 22
FLAG1=,TRUE,
GO TO 17
22 DM5«s-A/STF5(5)*M(5)»»2
CONST=C1«KL/TAU
AsM0(4)*DM5*STF5(4)
24 B=A*OLDDM2*STF2(4)
Y=2,»B/<2.»B*M<5»
SIGN=1,
IF(B,LT.0.0)SIGN=-1.
DM2»-SIGN»CONST*Y»»2*(M0(2)*OLDDM2)»»2
IF(SENSW(l»WRlTE(6.109)OLnDM2fDM2.M0(2)tM0(4)
CALL CONV(OLDDM2,DM2,2,NC, .00002)
!F{NC,EQ.1)GO TO 28
FLAG1»,TRUE,
GO TO 24
28 IF{,NOT.TFLAG)GO TO 30
WCPGs,403»M(8)*MW(8)*.225»M(9)«MW(9)
TEMP=(WCPT0-*T0*WCPG0»TG-DH2»DM2"DH5»DM5*U»AREA»TA)/(WCPT»WCPG*U»AR
SEA)
DQsU*AREA»(TEMP-TA)
30 DO 31 1=2.7
31 M( 1) sM0( I) +DM2«STF2( I) *DM5«STF5< 1)
IF(FLAG1)GO TO 12
OLOSS=QLOSS*DQ
IF(SENSW(3))WRITE(6,109)DM5,DPL,DQ.QLOSS
1F(SENSW(3))WRITE(6,108)(M
-------
PAGE 4
SUBROUTINE CONVCX. Y. NR.NCi TOD
C HEGSTEIN METHOD FOR ALGEBRAIC CONVERGENCE
C X « TRIAL VALUE
c Y « CALCULATED VALUE
c NR * ROUTINE CALL NUMBER
C NC * CONVERGE INDEX GO TO 6
lFtNC,LE.l>(30 TO 5
XT«(XA(NR)»Y-YA(NR)*X)/(XA(NR)»X*Y-YA(NR»
XA(NR>=X
YA(NR)SY
X*XT
RETURN
5 XA(NR)=X
YA(NR)=Y
NC*2
RETURN
6 X=Y
NC»1
RETURN
END
-398-
-------
PROGRAM C
PLUG FLOW REACTOR, USED FOR EXTERNAL REGENERATION CALCULATIONS
PAGE 1 C PLUG FLOW REACTOR FOR FERRIC SULFATE LEACHING OF PYRITJC SULFUR
C FROM COAL — D. FEAR
C
C
C 1«COAL SOLIDS FREE OF FES2
C 2»FES2
C 3»S
C 4=FE2(S04)3
C 5sFES04
C 6>H2S04
C 7»H20
C 8*02
C 9slNERT GAS
C 10=H20 VAPOR
C
C REACTIONS ARE! 4,6FE2(S04)3+4,8H20+FES2sl0.2FES04+4.8H2S04+.85
C FES04*.5H2S04*.2502 = '.5FE2(S04)3+.5H20
C
C 02FAC=1.0 IF OXYGEN IS USED, OTHERWISE 02FAC=0.0
C
C VFACsl.0 IF REACTOR IS VERTICAL. OTHERWISE VFAC=0.0
C
C
C
LOGICAL SENSW.PFLAG
REAL M,M0,MT,M1T.MW,NAME,KL,KR.MI
DIMENSION M<10).M0(10>,NAME(10,3).STF2(8).STF5<8>,W<1B).W0(10),MW(
$10)iDEL<2),DERlV{2),WK10),Ml(10)
DATA MW<1),MW<2),MW(3>,MK(4).MW(5),MW<6),MW<7),MW(8),MW(9),MW(10)/
$13,,119,96,32,06.399.86,151,90.98.08,18,02,32.,35.,18.02/
DATA RHOS/90./
DATA STF2(l).STF2(2).STF2(3).STF2(4>.STF2(5>tSTF2(6).STF2(7).STF2(
$8)/,0.1.V"•8,4.6,-10.2,-4.8,4.8,.0/
DATA STF5(l),STF5t2),STF5(3),STF5(4),STF5(5>.STF5(6).STF5(7>,STF5(
S8)/,0,,0,,0.-.5,1.0,.5,",5.,25/
DATA NAME(1,1),NAME(1,2),NAME(1,3)/4HCOAL,4H(PUR.4HE) /
DATA NAME(2,1) ,NAME(2,2),NAME(2,3)/4HFES2,4H .4H /
DATA NAME(3,1),NAME(3,2),NAME(3,3)/4HS ,4H ,4H /
DATA NAME(4,l),NAMEf4,2),NAME(4,3)/4HFE2<.4HS04),4H3 /
DATA NA«E{5,1).NAME<5,2),NAME(5,3)/4HFESO,4H4 ,4H /
DATA NAME(6,1),NAME(6,2),NAME(6.3)/4HH2SO,4H4 ,4H /
DATA NAME(7,1),NAME(7,2),NAME(7',3)/4HH20 , 4H ,4H /
DATA NAME(B,D ,NAME(S, 2) .NAMECB, 3>/4Ho2 ,4H ,4H /
DATA NAME(9,1),NAME(9.2),NAME(9.3)/4HINER,4HT GA.4HS /
DATA NAME(10,1).NAME(10,2)>NAME(10,3)/4HH20 ,4HVAPO,4HR /
PFLAG=.FALSE.
IF
-------
PAGE 2 C PLUG FLOW REACTOR FOR FERRIC SULFATE LEACHING OF PYRITIC SULFUR
ZPRINT*0.0
AREA«,785»DIA*«2
KLs2.E05*EXP(-3524,67//W(1)*AREA
C2*KR»AREA
WRITE<6, 101)
IF(,NOT,pFLAG)GO TO 11
WRITE<6,113>
WR!TE(6,114)
GO TO 24
11 DO 12 I«1.10
W0+M(9))#02FAC
DERlV(l)s-Cl«Y*Y/FT«M<2)»*2
DERIV(2)*-C2*P8/FT/FL»M(5)«*2
20 CALL RUNGE(2.DEL.DERIV,Z,DZf IFLAG.MFLAG)
IF(IFLAG.EQ,1)GO TO 20
DO 22 1=2,8
M{I)=M0(I)*STF2(I)«DEL(1)+STF5(I)*DEL(2>
22 W(D = H(I)«MW(1)
IF(SENSW(3))WRlTE(6il08)DERIV(l).DERlV(2).DEL(l).DEL(2).P8iFT,FL
IF(MFLAG.LT.2)GO TO 13
M(10)«VP7/(PRESS*DPL-VP7)*(M(8)*M(9))
W(10)=M(10)«MW(10)
M(7)SM(7)*M0(10)-M(10)
W(7>sM(7)*MW(7)
IF(Z.GE.ZMAX)GO TO 25
IF(Z.LT,ZPRINT)GO TO U
IF(,NOT,PFLAG)GO TO 11
24 WRITE(6,115)Z,M(2),M(4),M(5).M(6).M(8),M(10)
ZPRINT«ZPRINT+PINT
-4OO-
-------
PAGE 3 C PLUG FLOW REACTOR FOR FERRIC SULFATE LEACHING OF PYRITIC SULFUR
GO TO 11
25 CONV«<1,*W(2)/W1 (2)1*100,
IF(MI(2) .LE,0.0)CONV=0,0
IF(PFLAG)WRITE(6.101)
WRITE(6.102)TEMP.PRESS
WRITE<6,112)DIA.ZMAX
WRITE<6,103)CONV
WR ITE( 6,104)
WT.0.0
Hlt'0.0
DO 30 I«1,10
W( I)=W(I )/2000,
WT«WT*W( I)
WIT"WIT*WI (I )
30 WRITE(6,105)(NAME(JjK),K=1,3),WI(I ),W( I)
WRITE<6,109>
WRITE(6,110)WIT,WT
WRITE<6,106>
WRITE16.107)
MIT=0.0
MT«0,0
DO 35 I«l',10
MIT*MIT*MI(I)
MT«MT*M
-------
SUB-ROUTINE C-l
PAGE 1 C RUNQE-KUTTA INTEGRATION SUBROUTINE
SUBROUTINE RUNGE(NUMBER,RESULT.DERIV.X.H,I PLAGiMFLAQ)
C NUMBER = NUMBER OF EQUATIONS..
C RESULT s INTEGRAND ARRAY WHERE RESULTS ARE STORED
C DERIV = DERIVATIVE ARRAY
C X • LENGTH OR TIME POSITION-—THE INDEPENDANT VARIABLE
C H « INCREMENT SIZE
c IFLAG s FLAG TO THE SUBROUTINE FOR MULTI-PASSES
C IFLAG MUST BE PRESET TO ZERO BEFORE THE FIRST ENTRY
c IF MFLAG = i THEN CALCULATE DERIVATIVES
C IF MFLAG s g THEN INCREMENT IS FINISHED
C DERIVATIVES ARE CALCULATED FOUR TIMES FOR EACH TIME-STEP
DIMENSION RESULT(30),DERIV(30>,SAVE(30),PHI(30)
IFLAG « IFLAG * 1
C PASS 1
GO TO (100,200.300,400,500), IFLAG
100 MFLAG = 1
GO TO 600
200 DO 201 J « 1. NUMBER
SAVE(J)=RESULT(J)
PHKJ) s DERlV(J)
201 RESULTSA VE (J )*0. 5«H»DERI V( J)
GO TO 600
C PASS 4
400 DO 401 J « 1, NUMBER
PHKJ) * PHKJ) * 2,0 • DERIV(J)
401 RESULT(J)«SAVE(J)*H«DERIV( J)
X a X * ,5»H
GO TO 600
500 DO 501 J « 1, NUMBER
501 RESULT{J)«SAVE(J)*fPHKJ)*DERIV(J))»H/6.0
MFLAG * 2
IFLAG = 0
600 RETURN
END
-402-
-------
10.4.2 Computer Printout for Reaction Systems
The data used for Summary Tables 5-8 in Section 4.2.4 are
presented here in full. In addition, the printouts from a
number of other runs are included to illustrate the effects
of conditions somewhat different from those summarized in
the main text. These other runs were used to help determine
the ranges of interest of system variables such as reactor
size, feed temperature and liquid to solids ratio. For
continuous reactors with external regeneration a number of
runs are presented to show the effect of regeneration
temperature on regeneration reactor volume.
For continuous reactors in parallel the alternative runs
given are printouts from a series of early exploratory runs
wherein the ratio of liquid to coal solids and the concen-
tration of iron ion were changed, and the mixer and reactor
volumes were adjusted correspondingly to accommodate the new
solution conditions. The residence times, reactor temperature,
% conversion of FeS2 in the reactor, and the amounts of iron
sulfate solution, acid, and water removed or added were
altered, partially by cut-and-try methods, to get a meaning-
ful output. The program used for these alternative runs
was an early version arranged so that all of the oxygen was
introduced in the mixer but did not participate in the
reactions until the slurry reached the reactors. Also,
conditions had not been optimized to give a 102°C mixer
outlet temperature.
-403-
-------
BATCH REACTORS
DATA CORRESPONDING TO TABLE 5 SECTION 4.2.4
MIXER
TEMPERATURE. DEG C = 102,0
REACTOR VOLUME, GAL ~ 25000.
% CONV OF FES2 INPUT s 9,70
PRESSURE. PS1A = 14.7
RESIDENCE TIME. HR = ,25
* OF INITIAL FES2 CONV s 9,70
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE2
-------
BATCH REACTORS
DATA CORRESPONDING TO TABLE 5 SECTION 4.2.4
REACTOR FILL CYCLE
INITIAL TEMPERATURE. DEG C » 125.0
REACTOR VOLUME. GAL « 101028.
PRESSURE. PSIA = 80,0
QUANTITY, TONS
COAL(PURE)
FES2
S
FE2
-------
BATCH REACTORS
DATA CORRESPONDING TO TABLE 5 SECTION 4.2.4
REACTOR BATCH CYCLE
INITIAL TEMPERATURE, DEC C = 141,0
REACTOR VOLUME. GAL = 100697,
PRESSURE, PSIA = 80,0
FINAL TEMPERATURE. DEG C = 150.4
RESIDENCE TIME. HR * 7,99
% CONV OF FES2 INPUT » 93.87
QUANTITY, TONS
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
95.87
5,51
;«i2
49,31
18.79
5.89
334.42
3.80
.02
.00
OUTPUT
95,87
.33
1.22
60.59
16.78
3.97
334.59
.17
.02
.17
TOTAL
513.78
513.76
** *• •* •# ** »•'** »# •* •» ** •» »» •» •• »• •• *« »• •• •* «• »* •» •• »* »* *« •• *• *« ** »• ** *• ** ** ••
QUANTITY, LB MOL
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
14750.75
92.00
7.63
246.67
247.51
120.22
37117.31
237'.59
1,19
.00
OUTPUT
14750.75
5.63
76,72
303.07
221.05
81.07
37135.72
10.74
1.19
19.08
TOTAL
52820.87
52605.03
-406-
-------
BATCH REACTORS
DATA FOR ALTERNATIVE RUN NO.
REACTOR FILL CYCLE
INITIAL TEMPERATURE, DEG C s 102.0
REACTOR VOLUME, GAL = 101041,
PRESSURE, PSIA = 50,0
FINAL TEMPERATURE, DEG C = 113.1
RESIDENCE TIME, HR * 1,02
X CONV OF FES2 INPUT = 27,52
QUANTITY, TONS
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
95.87
5.51
.12
49.31
18,79
5.89
334.42
1.69
.01
.00
OUTPUT
95.87
3,99
.44
66.42
7,72
1.94
'335.12
.07
.01
.02
TOTAL
511.66
511.66
QUANTITY, LB
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
14750.75
92.00
7,63
246.67
247.51
120,22
37117'.31
105.82
.53
,00
OUTPUT
14750.75
66.67
27.89
332.26
101.65
39,69
37194.73
4,78
.53
3,05
TOTAL
52688,44
52522,02
>***•**•»••*»*•
-4O7-
-------
BATCH REACTORS
DATA FOR ALTERNATIVE RUN NO. 1
REACTOR BATCH CYCLE
INITIAL TEMPERATURE, DEC C » 113,1
REACTOR VOLUME, GAL = 100755.
PRESSURE, PSIA * 50.0
FINAL TEMPERATURE, DEG c = 127,7
RESIDENCE TIME. HR = 7,99
X CONV OF FES2 INPUT s 91.06
QUANTITY, TONS
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA CORRESPONDING TO TABLE 6 SECTION 4.2.4
SETTLER #1
TEMPERATURE, DEC C s 102.0 PRESSURE. PSIA * 14.7
REACTOR VOLUME. GAL = 5000000. RESIDENCE TIME. HR = 18.40
% CONV OF FES2 INPUT s 72.86 % OF INITIAL FES2 CONV = 72'.'86
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE23 1719.60 1384.33
FES04 382.09 1125,51
H2S04 190.04 539.89
H20 109311.87 108962.03
02 .00 .00
INERT GAS '.'00 .00
H20 VAPOR .00 .00
TOTAL
126165.17
126558.76
-4O9-
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA CORRESPONDING TO TABLE 6 SECTION 4.2.4
SETTLER #2
TEMPERATURE. OE6 C a 102.0 PRESSURE. PSlA = 14.7
REACTOR VOLUME. GAL * 5000000. RESIDENCE TIME. HR = 18.36
X CONV OF FES2 INPUT = 59.62 * OF INITIAL FES2 CONV = 59.'62
FLOWRATE. T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
94.00
...
347.18
34.38
8.36
984.89
'.'00
.00
OUTPUT
94.00
.'65
1.13
332.37
46,85
12.15
984.31
•.00
.00
,00
TOTAL
1471.37
1471.48
FLOWRATE. LB MOL/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
•H20 VAPOR
INPUT
14461.53
27.00
58.01
1736.55
452.66
170.47
109311.87
.00
.00
.00
OUTPUT
14461.53
10.90
70.89
1662.45
616.91
247.76
109247.26
.00
,00
.00
TOTAL
126218.12
126317.71
i •• *•
-410-
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA CORRESPONDING TO TABLE 6 SECTION 4.2.4
REGENERATION TANK
TEMPERATURE? DEG C « 130,0
REACTOR DIAMETER. FT « 2,00
X CONV OF FES2 INPUT * ',00
PRESSURE, PSIA = 200,0
REACTOR LENGTH. FT « 147,5
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
'.'00
,00
',00
522,55
113.59
34.39
1708.31
3.64
.02
.00
OUTPUT
',00
,00
',00
609,32
47',65
13,10
1712,12
,16
.02
.02
TOTAL
2382.51
2382.41
FLOWRATE. LB MOL/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
.00
'.00
,00
2613,71
1495.58
701.26
189602.65
227.49
1,14
,00
OUTPUT
,00'
.00
,00
3047;67
627,49
267i2l
190024.71
10.47
1.14
2.71
TOTAL
194641.81
193981.37
' »•**••*»**••
-411-
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA FOR ALTERNATIVE RUN NO. 1
SETTLER #1
TEMPERATURE, DEC C s 102','0 PRESSURE, PSIA a 14.7
REACTOR VOLUME, GAL « 3000000, RESIDENCE TIME, HR * ll',03
X CONV OF FES2 INPUT = 66,92 % OF INITIAL FES? CONV 9 66.92
FLOHRATE, T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
94.'00
6,00
A00'
343.79
29,02
9'.'32
9 84 ,'89
'.'00
.00
',00
OUTPUT
94,00
1,98
,85
282,22
80,88
25.07
982,14
.00
,00
','00
TOTAL
1467.03
1467.17
FLOWRATE. LB MOL/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
14461.53
100.03
.00
1719.60
382.09
190.04
109311.87
^00
'.00
,00
OUTPUT
14461.53
33.08
53.55
1411.62
1064.94
511,39
109006 .'46
,00
.00
,00
TOTAL
126165.17
126542,59
-412-
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA FOR ALTERNATIVE RUN NO. 1
SETTLER #2
TEMPERATURE. DEG C = 102.0 PRESSURE. PSJA * 14.7
REACTOR VOLUME. GAL * 3000000. RESIDENCE TIME. HR = 11.03
X CONV OF FES2 INPUT » 54'.'58 % OF INITIAL FES2 CONV * 54,'58
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
94A00
1.97
.86
335.60
35 '.B 4
11.39
984'.'21
.00
.00
.00
OUTPUT
94.00
.89
1.08
319.12
49.72
15.61
983'.'44
.00
.00
.(10
TOTAL
1463.88
1463.88
•* #» «* ** ** *« *« •» »* *» #» •» *» *» *» »« •• »• ** *« •» «* «* «• *« *****«•*•»*****««*****»• •<
FLOWRATE, LB MOL/HR
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA FOR ALTERNATIVE RUN NO. 1
REGENERATION TANK
TEMPERATURE* DEG C « 102,0
REACTOR DIAMETER, FT • 2,00
% CONV OF FES2 JNPUT « ,00
PRESSURE, PSIA » 200.0
REACTOR LENGTH. FT * 444,0
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE23
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
.00
,00
.00
522,55
113.59
34.39
I708'.3l
3.64
.02
.00
OUTPUT
,00
,00
.00
609.40
47.59
13.08
1712.16
.16
.02
,01
TOTAL
2382.51
2382.44
FLOWRATE, LB MOL/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
,00
.00
,00
2613.71
1495,58
701.26
169602.65
227.49
1.14
.00
OUTPUT
.00
.00.
.00
3048.11
626.67
266.60
190029.53
10.27
1.14
.93
TOTAL
194641.81
193983.43
-414-
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA FOR ALTERNATIVE RUN NO. 2
REGENERATION TANK
TEMPERATURE. DEG C ' 120,0
REACTOR DIAMETER, FT » 2,00
% CONV OF FES2 INPUT • .00
PRESSURE, PSIA = 200,0
REACTOR LENGTH, FT » 211,0
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES 04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
,00
.00
.00
522.55
113,59
34.39
1708,31
3,64
.02
.00
OUTPUT
,00
,00
',00
609.28
47.68
13.11
1712.15
.16
.02
.01
TOTAL
2382.51
2382.44
FLOWRATE, LB MOL/HR
COAL
-------
CONTINUOUS REACTORS WITH EXTERNAL REGENERATION
DATA FOR ALTERNATIVE RUN NO. 3
REGENERATION TANK
TEMPERATURE, DEC C * 140,0
REACTOR DIAMETER. FT * 2,30
* CONV OF FES2 INPUT • ,00
PRESSURE, PSIA * 200,0
REACTOR LENGTH, FT « 107,5
FLOWRATE, T/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
.00
,00
,00
522,55
113.59
34.39
1708.31
3,64
.02
,00
OUTPUT
,00
,00
',00
609,34
47>64
13.09
1712.13
,16
,02
,03
TOTAL.
2382.51
2382.44
FLOWRATE, LB MOL/HR
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
INPUT
,00
.00
.00
2613.71
1495,58
701.26
189602.65
227,49
1.14
OUTPUT.
100
;00
•00
3047*79
627,31
267i!2
190025,96
10,43
1,14
3,92
TOTAL
194641.81
193983.62
-416-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
MIXER
TEMPERATURE IN, DEG C = 102.0
PRESSURE, PSIA « H,7
REACTOR VOLUME, GAL * 50000,
% CONV OF FES2 INPUT « 14.34
TEMPERATURE OUTi DEG C « 102,0
HEAT LOSS, BTU/HR = 0.
RESIDENCE TIME, HR f ,50
x OF INITIAL FES2 CONV » 14,34
FLOWRATE, T/HR
TOTAL
INPUT
499,99975
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
5,99999
.00000
57,29998
10,89999
3,49999
328,29986
,00000
.00000
,00000
93.99998
5.13928
.18402
44.10256
22.01683
6.87788
327,67926
.00000
.00000
,00000
499,99975
i •*
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51500.335
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES 04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461.537
100.033
.000
286,600
143.515
71.370
36437.289
,000
.000
1000
14461.537
85,683
11.480
220.590
289,885
14B.250
36368,406
.000
.000
.000
51577.828
-417-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4'
REACTOR NO,
EACH REACTOR is
RECIRCULATION RATIO » ,00
TEMPERATURE IN, DEC C « 150,0
PRESSURE, PS IA * 80,0
REACTOR VOLUME, GAL » 100000,
X CONV OF FES2 INPUT » 59,35
4 CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TSMPERATURE OUTi" DEC C s 150,0
HEAT LOSS, BTU/HR * 0,
RESIDENCE TIME, HR = 1,01
-J4 OF INITIAL FES2 CflNV » 50,84
FLOWRATE, T/HR
TOTAL
INPUT
502,41290
OUTPUT
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO i 2
EACH REACTOR is
RE CIRCULATION RATIO « ,00
TEMPERATURE IN, DEG C a 150, 0
PRESSURE, PSIA e 80,0
REACTOR VOLUME, GAL * 100000,
% CONV OF FES2 INPUT * 43,22
4 CSTRS IN SERIES
DIRECTION OF FLOW is UP
TEMPERATURE b UT, DEG C » 150.0
HEAT LOSS. BTU/HR * 0.
RESIDENCE TIME, HR • 1,01
* OF INITIAL FES2 CONV = 15.04
FLOWRATE. T/HR
TOTAL
INPUT
503,36767
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
2,08868
,83625
57,30612
15,84803
4,13807
326,14508
1,00000
,00550
,00000
93,99998
1,18591
1.02927
68.45527
8.52238
1.55095
328.60467
.00000
.00550
.01553
503.36743
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51611.125
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461.537
34.822
52.168
286.630
208,664
84.381
36420,109
62.500
,314
,'000
14461,537
19.771
64.209
342.396
112,184
31.626
36471.117
.000
.314
1,724
51504.867
-419-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO, 3
EACH REACTOR IS
RECIRCULAT10N RATIO « ,00
TEMPERATURE IN, DEG C = 150,0
PRESSURE. PSIA > 80,0
REACTOR VOLUME. GAL * 100000,
X CONV OF FES2 INPUT « 32,39
A CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TEMPERATURE QUTi DEC C = 150,0
HEAT LOSS, BTU/HR « 0.
RESIDENCE TIME. HR * 1,01
X OF INITIAL FES2 CONV s 6.40
FLOWRATE, T/HR
TOTAL
INPUT
503,74859
OUTPUT
COAL(PURE)
FES2
S
F62(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
1,18591
1,02927
68,45527
8,52038
1,55095
328,60467
,39999
,002212
,00000
93.99998
.80170
1.11141
72.56022
5,88808
.60688
328,77172
.00000
. 00 22 0
.00620
503.7482-9
•••»*•*•**»*«• •*••••**«•*•«»**»•*«••*•••••*•»•**•••»»« •»**•••*•*•*•**• •»*••»
PLOHRATE. LB MOL/HR
INPUT
TOTAL
51527,953
OUTPUT
COAL(PURE)
FES2
S
FE2(S04}3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461,537
19,771
64.209
342,396
112.184
31.626
36471.117
24.999
,125
. .000
14461.537
13.366
69.333
362.928
77,525
12,375
36489.656
.000
,125
i689
•••••»«•••
51487,531
-420-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO. 4
EACH REACTOR is
REclRCULATjON RATIO « ,00
TEMPERATURE IN, DEC C s 150,0
PRESSURE, PS IA s 80,0
REACTOR VOLUME, GAL * 100000.
« CONV OF FES2 INPUT » 23,09
4 CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TEMPERATURE OUT, DEG C « 150,0
HEAT LOSS, 8TU/HR = 0.
RESIDENCE TIME. HR • 1,01
K OF INITIAL FES2 CQNV «= 3,06
FLOWRATE, T/HR
TOTAL
INPUT
503,73992
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
,80170
1.11141
72,56022
5,88808
,60688
328,77172
,00000
.00000
,00000
93.99998
,61651
1.15101
69,72070
8.27993
1.33366
328.63793
.00000
.00000
,00000
503.73968
FLOWRATE, LB MOL/HR
INPUT
TOTAL
91486.716
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461.537
13.366
69.333
362.928
77.525
12.375
36489.656
.000
.000
,000
14461.537
10.278
71; 80 3
348.725
109.018
27.195
36474.812
.000
.000
,000
51503,367
-421-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO,
EACH REACTOR is
RECIRCULATION RATIO s ,00
TEMPERATURE IN, DEG C * 150.0
PRESSURE, PSIA = 80,0
REACTOR VOLUME, GAL s 100000,
% CONV Or FES2 INPUT * 18,03
4 CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TEMPERATURE OUT, DEG C 5 150,0
HEAT LOSS. BTU/HR a 0,
RESIDENCE TIME, HR = 1,01
% OF INITIAL FES2 CONV s i.ss
FLOWRATE, T/HR
TOTAL
INPUT
503,73968
OUTPUT
COAL
FES2
s
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93.99998
,61651
1,15101
69.72070
8,27993
1,33366
328,63793
,00000
,00000
,00000
93.99998
,50531
1,17478
68,01562
9.71618
1.77006
328.55767
, 00 00 a
,00000
.00000
503.73956
•* •• «* #• *« ** •* •• *» •• *« •• ** •• «• *• •* •« *» ** «* *• ** ** *« ** •« •* «• *• «* «* •* •* ** •* »• *•
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51503,367
OUTPUT
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO,
EACH REACTOR is
RECIRCULATION RATIO « ,00
TEMPERATURE IN, DEG C = 150,0
PRESSURE, PS IA = 80,0
REACTOR VOLUME, GAL ' 100000,
* CONV OF FES2 INPUT » 14,85
4 CSTRS IN SERIES
DIRECTION or FLOW is up
TEMPERATURE 0 UT. DEG C = 150,0
HEAT LOSS. 8TU/HR * 0',
RESIDENCE TIME, HR * 1,01
% OF INITIAL FES2 CONV = 1,25
FLQWRATE. T/HR
TOTAL
INPUT
503,73956
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
,50531
1,17478
68,01562
9,71618
1.77006
328,55767
,00000
,00000
,00000
93.99998
.43023
1.19083
66.86445
10,68584
2.06470
328.50335
.00000
,00000
,00000
503.73937
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51513.359
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461.537
8,424
73,286
340.197
127,928
36,094
36465.898
,000
.000
,000
14461,537
7.173
74.288
334.439
140,695
42.102
36459; 875
.000
,000
.000
51520,101
-423-
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO,
EACH REACTOR IS
RECIRCULATION RATIO » ,00
TEMPERATURE IN. DEG C = 150,0
PRESSURE. PS IA 3 80,0
REACTOR VOLUME, GAL = 100000,
% CONV OF FES2 INPUT « 12,66
4 CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TEMPERATURE OUT* DEG C =.150,0
HEAT LOSS, BTU/HR = 0.
RESIDENCE TIME. HR * 1,01
* OF INITIAL FES2 CONV = .90
FLOWRATE, T/HR
TOTAL
INPUT
503,73937
OUTPUT
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS IN SERIES
DATA CORRESPONDING TO TABLE 7 SECTION 4.2.4
REACTOR NO, 8
EACH BEACTOR IS
RECIRCULATION RATIO = ,00
TEMPERATURE IN, DEC C s 150,0
PRESSURE, PSIA = 30,0
REACTOR VOLUME, GAL • 100000.
« CONV OF FES2 INPUT » 11,05
4 CSTRS IN SERIES
DIRECTION OF FLOW IS UP
TEMPERATURE OUT, DEG C = 150.2
HEAT LOSS, BTU/HR = 0,
RESIDENCE TIME, HR « 1,01
% Of INITIAL FES2 CONV = ,69
FLOWRATE. T/HR
TOTAL
INPUT
503,73925
OUTPUT
COAL(PURE)
FES2
S
FE23
FES 04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
,37574
1,20248
66 ,028 '93
11,38961
2 ,2 78 54
328,46398
,00000
,00000
,00000
93,99998
.33420
1.21136
65.39186
11.92622
2. 44 15 9
.328,43389
.00000
.00000
.00000
503,73907
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51524.992
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
14461.537
6.264
75,014
330.260
149.962
46,463
36455.500
.000
.000
,000
14461.537
5.571
75,568
327,073
157,027
49.787
36452'.'164
.000
.000
,000
51528,718
-425-
-------
CONTINUOUS REACTORS IN PARALLEL
DATA CORRESPONDING TO TABLE 8 COLUMNS 1&2 SECTION 4.2.4
MIXER
TEMPERATURE IN, DEC C = 101.1
PRESSURE. PSIA a 14,7
REACTOR VOLUME, GAL • 50000.
« CONV OF FES2 INPUT * 14,35
TEMPERATURE OUT. DEC C = 102.0
HEAT LOSS. BTU/HR = 242910.
RESIDENCE TIME. HR « ,50
* OP INITIAL FES2 CQNV = 14.35
FLOWRATE. T/HR
TOTAL
INPUT
499,99975
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
93,99998
5,99999
.00000
57,29998
10.89999
3,49999
328.29986
,00000
,00000
,00000
93.99998
5.13843
k 18420
44.08956
22.02778
6.88121
327.67858
.00000
,00000
,00000
499.99969
FLOWRATE, LB MOL/HR
INPUT
TOTAL
51500.335
OU TP UT
COAL(PURE)
FES2
S
FE2
-------
CONTINUOUS REACTORS IN PARALLEL
DATA CORRESPONDING TO TABLE 8 COLUMNS 3&4 SECTION 4.2.4
EACH REACTOR is 10 CSTRS IN SERIES
RECIRCULATION RATIO = .00 DIRECTION OF FLOW IS UP
TEMPERATURE IN, DEG C = 130,0 TEMPERATURE OuT, DEG C = 146.7
PRESSURE, PSIA a 80,0 HEAT LOSS. BTU/HR sl028849,
REACTOR VOLUME, GAL » 100000, RESIDENCE TIME, HR « 10.11
% CONV OF FES2 INPUT » 93,46 % OF INITIAL FES2 CONV » 80,04
ONE OF 10 PARALLEL REACTORS
FLOWRATE, T/HR
TOTAL
INPUT
50,36676
•OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
9.39999
,51384
.01842
4,40895
2,20277
,68812
32,76786
,36479
,00200
,00000
9.39999
.03358
.12110
6.162213
1.47896
.33664
32.82887
.00000
.00200
,00354
50.36673
FLOWRATE, LB MOL/HR
INPUT
TOTAL
5180,704
OUTPUT
COAL
-------
CONTINUOUS REACTORS IN PARALLEL
DATA CORRESPONDING TO TABLE 8 COLUMNS 5, 6 & 9 SECTION 4.2.4
MIXER
TEMPERATURE IN, DEG C s 100.4
PRESSURE. PSIA = 14,7
REACTOR VOLUME. GAL = 83525,
% CONV OF FES2 INPUT = 13.86
TEMPERATURE OUT, DEG C = 102,0
HEAT LOSS, BTU/HR = 341927.
RESIDENCE TIME, HR = 1,04
* OF INITIAL FES2 CONV = 13.86
FLOWRATE, T/HR
TOTAL
INPUT
OUTPUT
REMOVE
ADD
COAL(PURE)
FES2
S
FE2(S04)3
FESQ4
H2S04
H20
02
INERT GAS
H20 VAPOR
113,49996
8,14999
,00000
34,84999
6.62999
2,12999
238.97973
,00000
.00000
,00000
113.49996
7.02036
.24151
17.52930
21.22006
6.56323
238.16522
.00000
.00000
.00000
4.983
6.032
1.866
39.2897
1.821
2.293
404,23962
404.23962
52.1707
4.114
FLOWRATE, LB MOL/HR
INPUT
TOTAL
44426.261
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
17461.535
135.878
,000
174.310
87.294
43.433
26523.839
.000
.000
.000
17461.535
117,045
15.066
87.677
279.395
133.834
26433.437
.000
.000
,000
44527,984
-428-
-------
CONTINUOUS REACTORS IN PARALLEL
DATA CORRESPONDING TO TABLE 8 COLUMNS 7 & 8 SECTION 4.2.4
ONE OF TEN PARALLEL REACTORS
EACH REACTOR is 10 CSTRS IN SERIES
REC1RCULATION RATIO = ,00 DIRECTION OF FLOW IS UP
TEMPERATURE IN. DEC C = 102,0 TEMPERATURE OllT, DE6 C • 145,4
PRESSURE, PSIA s 80,0 HEAT LOSS'," BTu/HR = 775635.
REACTOR VOLUME, GAL = 67780, RESIDENCE TIME, HR s 9,67
% CONV OF FES2 INPUT = 94,36 « OF INITIAL FE$2 CQNV = 94,36
ONE OF 10 PARALLEL REACTORS
FLOWRATE. T/HR
TOTAL
INPUT
36,11669
OUTPUT
COALCPURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
11.34999
,70203
.02415
1,25462
1.51880
,65182
20.11684
,49569
.00272
,00000
11,34999
.03955
.16579
3.48513
,66301
.21304
20.19325
.00000
,00272
.00418
36.11667
FLOWRATE, LB MOL/HR
INPUT
TOTAL
4062,789
OUTPUT
COALCPURE)
FES2
S
FE2(S04)3
FES04 '
H2S04
H20
02
INERT GAS
H20 VAPOR
1746.153
11.704
1,506
6,275
19,997
13.291
2232,724
30.981
,155
,000
1746.153
,659
10.342
17.431
8.729
4.344
2241.205
,000
.155
,464
4029,484
-429-
-------
CONTINUOUS REACTORS IN PARALLEL
DATA FOR ALTERNATIVE RUN NO. 1
MIXER
TEMPERATURE IN. DEC C = 102. B
PRF.SS'JKO, PS 14 = 14.7
REACTOR VOLUME, GAL = 7?6fi4,
'A CONV OF FES? INPUT = 13.66
5% IRON SOLUTION
TEMPERATURE OUT, DFG C * 103.7
HEAT LOSS. "3Ti;/->* = 312426.
RESIDENCE TIME. HR = l.£»
% OF INITIAL FFS? CONV = 13.86
2# LIQUID/0COAL SOLIDS
FLOWRATE, T/HR
INPUT
OUTPUT
REMOVE
COAL(PURE)
FES 2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
113,4999
6.1499
.tfUfiH
34.6499
6.6299
2.1299
199.6899
4.9569
.0272
.0300
113.4999
7. 0 20 3
.2415.
17.5295
21.2197
6.5631
198.P751
4.9569
.M272
,0(?0fl
4.983
6.032
0.045
TOTAL
369.9339
369.9335
11.060
CONTINUOUS REACTORS IN PARALLEL
EACH reAcTOf; is ir CSTSS IN SERIES
RECIRCULAT ION RATIO = .*? DIRECTION OF FLOW IS UP
TEMPERATURE IN, DEC C = 102. d TEMPERATURE OUT, BEG C = 152.'3
PRESSURE, PSIA = 80.? HEAT LOSS, 9TU/HR = 794489.
REACTOR VOLUME, GAL = 68640.' RESIDENCE TMF. HR = 9,88
S CONV OF FES2 INPUT = 94.36 X OF INITIAL FES2 CONV = 94.36
ONE OF If PARALI EL REACTORS
FLOWRATE, T/HR
INPUT
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
TOTAL
11.3499
.7020
.0241
1.2546
1,5187
.6518
19.8875
.4957
.0027
.00H0
35.6873
-4 SO-
11 .3499
.B395
.1657
3.4849
.6630
.2130
19.9548
.OB00
.1?027
.0128
35.8867
-------
CONTINUOUS REACTORS IN PARALLEL
DATA FOR ALTERNATIVE RUN NO. 2
MIXER
TEMPERATURE IN. DEG C = 102.0
PRESSURE, PSIA = 14.7
REACTOR VOLUME. GAL = 70390.
« CONV OF FES2 INPUT = 13.86
5% IRON SOLUTION
TEMPERATURF OUT. DEG C = 103,9
HEAT LOSS. BTU/HR = 140469'.
RESIDENCE TIME. HR = ' 1 .00
« OF INITIAL FES2 CONV = 13.86
2# LIQUID/# COAL SOLIDS
FLOWRATE, T/HR
INPUT
0 UT PU T
REMOVE
COAL(PURF)
FES2
S
FE2(S04)3
FES 04
H2SQ4
H20
02
INERT GAS
H20 VAPOR
113.4999
8,1499
.0005*
34 .8499
6 ,6299
2 .1299
199.6899
4.9569
.0272
.0000
113 .4999
7.2203
.2415
17.5295
21 .2197
6.5631
193.8752
4.9569
.3272
.2000
4.983
6.032
0.045
TOTAL
3 69 .9 33 9
369 .9335
11.060
CONTINUOUS REACTORS IN PARALLEL
EACH REACTOR IS 10 CSTRS IN SERIES
RECIRCULATION RATIO = .00 DIRECTION OF FT OW IS UP
TEMPERATURE IN. DEfi C = 102.0 TEMPERATURF 0 yT, DEG C = 152,4
PRESSURE, PSIA = 80.0 HEAT LOSS. BTU/HR = 791988.
REACTOR VOLUME. GAL = 68340. RESIDENCE TIME. HR = 9.90
% CONV OF FES2 INPUT = 94.36 « OF INITJAL FES? CONV = 94.36
ONE OF 13 PARALLEL REACTORS
FLOWRATE. T/HR
INPUT
OUTPUT
COAL(pURE)
FES 2
S
FE2(S04)3
FES04
H2S04
H20
02
INERT GAS
H20 VAPOR
TOTAL
11.3*99
,7020
.0 24 1
1.2546
1.5187
.6518
19.8075
.4957
.0027
.£000
35.8873
-431-
11.3499
.0395
.1657
3.4849
.6630
.2130
19.6.682
.0C100
.0027
.0132
35.6006
-------
CONTINUOUS REACTORS IN PARALLEL
DATA FORxALTERNATIVE RUN NO. 3
MIXER
TEMPERATURE IN. DEC C = 1? 2.0
PR ES SU RE . PS IA = . 14 .7
REACTOR VOLUME. GA L = 170170,'
% COW OF FES2 INPUT = 20.79 .
5% IRON SOLUTION
TEMPERA TURF OUT. DEC C = 10 3. 6
H EA T LO SS . BT U/ HR = 5 61 49 3'.
RES IDENCE T iMEi HR » 1 ,78
« OF. INITIAL FPSZ CONV = 20,79
3#LIQUID/# COAL SOLIDS
FLOWRATE. T/HR
INPUT
OUTPUT
REMOVE
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
K20
02
INERT GAS
H20 VAPOR
113.4999
8.1499
.0000
52.2749
9.9449
3.1949
299.5349
4.9569
.0272
,0000
113.4999
6.4555
.3622
26.2939
31.8299
9.8448
298.3121
4.9569
.0272
.0000
4.983
6.032
0.045
TOTAL
491,5839
491.5827
11.060
CONTINUOUS REACTORS IN PARALLEL
EACH REACTOR is 10 CSTRS IN SERIES
RE CIRCULATION RATIO s .00 DIRECTI ON OF FL OW I S UP
TEMPERATURE IN. DEG C = 119.0 TEMPERATURE Out. DEG C = 152,'2
PRESSURE. PSIA = 80.0 HEAT LOSS. BTU/HR = 960383.
REACTOR VOLUME. GAL = 88352. RESIDENCE TIME, HR = 9,38
'A CONV OF FES2 INPUT = 93,37 % OF INITIAL FES2 CONV s 93.87
ONE OF 10 PARALLEL REACTORS
FLOWRATE. T/HR
INPUT
OUTPUT
COAL(PURE)
FES2
S
FE2(S04)3
FES04
H2S04
H20
02
.INERT GAS
H20 VAPOR
TOTAL
11.3499
.6455
.0362
2.1310
2.5797
.9799
29.8311
.4957
.0027
.0000
48.0522
-432-
11.3499
.0395
.1657
5.2274
.9945
.3195
29.7023
.0003
.0027
.0124
47.8144
-------
TEMPERATURE IN. DEC C = 102.0
PRESSURE, PS IA s 14 ,7
'RE AC TO R VO LU ME , GA L = 50 00 0.
% CONV OF FES2 INPUT = 14,08
5.61 IRON SOLUTION
CONTINUOUS REACTORS IN PARALLEL
DATA FOR ALTERNATIVE RUN NO. 4
MIXER
TEMPERA TURF OUT. DEC C = 103.2
HEAT LOSS. BTU/HR = 110676'.'
RESIDENCE TlMEi HR = ',42
« OF INITIAL FFS2 CONV = 14',08
4# LIQUID/* COAL SOLIDS
FLOWRATE. T/HR
INPUT
OUTPUT
COAL(PURE)
FES 2
S
FE2(S04)3
FES 04.
H2S04
H20
02
INERT GAS
H20 VAPOR
113 ,4999
8,1499
,0000
77,8299
14.8H99
4,7499
389.2058
4 ,9569
,0272
,0000
113.4999
7.0019
.2454
60,2272
29.6375
9.2554
388.3777
4 .9569
.0272
,0000
TOTAL
613,2297
613.2292
CONTINUOUS REACTORS IN PARALLEL
EACH REACTOR IS 10 CSTRS IN SERIES
RECIRCULAT ION RA TI 0 = ,00 DIRECTION OF Fl. OW IS UP
TEMPERATURE IN. DEG C = 126,0 TEMPERATURE OUT, DEG C = 15 4', 7
PRESSURE, PSIA = 80.0 HEAT LOSS. 8TU/HR = 539885.
REACTOR VOLUME, GAL. = 120000. RESIDENCE TIME. HR = i0','i6
X CONV OF FES2 INPUT = 94.32 % OF INITIAL FES2 CONV = 81.03
ONE OF 10 PARALLEL, REACTORS
FLOWRATE, T/HR
INPUT
OUTPUT
COAL (PURE )
FES2
S
FE2(S04)3
FES 04
H2S04
H20
02
INERT GAS
H 20 VAPOR
11,3499
,7001
.0245
6,0227
2,9637
,9255
38 .8 37 7
.4957
.0027
,0000
11.3499
.0397
.1657
8.2846
2.0814
.4786
38.7567
.0000
.0027
.0295
TOTAL
61.3229
61.1892
-433-
-------
CONTINUOUS REACTORS IN PARALLEL
DATA FOR ALTERNATIVE RUN NO. 5
MIXER
TEMPERATURE IN, DEC C = 102,0
PRESSURE, PS IA = 14,7
REACTOR VOLUME, GAL s 50000.
% CONV OF FES2 I NPUT = 12, 42
TEMPERA TURF OUT, DEC C = 103,7
HEAT LOSS, BTU/HR = 111568.
RESIDENCE TIME. HR = ,71
•/. OF INITIAL FES2 CONV = 12,42
IRON SOLUTION
FLOWRATE. T/HR
INPUT
2.04# LIQUID/* COAL SOLIDS
OUTPUT
COAL
-------
tuNTINUOUS REACTORS IN PARALLEL
DATA ?OR ALTERNATIVE RUN NO. 6
MIXER
TEMPERATURE IN, DEC C = 102.0
PRESSURE, PS 1A = 14 ,7
REACTOR VOLUME, GAL = 50000,
% CONV OF FES2 INPUT = 16,36
7.5% IRON SOLUTION
TEMPERA TURF OUT, DEC C = 1M3.7
H EA T LO SS . BT U/ HR = 111 57 9'.
RESIDENCE T IME. HR = ,56
« OF INITIAL FFS2 CONV = 16.36
3.02# LIQUIDS/0 COAL SOLIDS
FLOWRATE, T/HR
INPUT
OUTPUT
COAL(PURE)
FES 2
S
FE2
-------
CONTINUOUS REACTORS IN PARALLEL
DATA FOR ALTERNATIVE RUN NO. 7
MIXER
TEMPERATURE IN, DEG C = 102.0
PRFSSURE, PSIA s 14.7
REACTOR VOLUME, GAL = 50000,
K CONV OF FES2 INPUT = 13.27
5% IRON SOLUTION
TEMPERATURE OUT, DEG C = 1M2.9
HEAT LOSS, BTU/HR = 113432.
RESIDENCE TIME, HR = .37
X OF INITIAL FES2 CONV = 13.27
4.51 LIQUID/0 COAL SOLIDS
FLOWRATE, T/HR
INPUT
0 UT PU T
C OA L( PU RE )
FES 2
S
FE2(S04)3
FES 04
H2S04
H20
02
1 NE RT G AS
H20 VAPOR
113,4999
8.1499
.0000
77.8299
14.8099
4.7499
445 .9398
4 .9 56 9
,0272
.3000
113 .4999
7.0679
.2313
61.2394
23 .7849
8.9963
445 .1594
4 .9569
.0272
,0000
TOTAL
669,9636
669 .9633
CONTINUOUS REACTORS IN PARALLEL
EACH REACTOR I S 10 CSTRS IN SERIES
RECIRCULATION RATIO = ,00 DIRECTION OF FLOW IS UP
TEMPERATURE IN, DEG C = 130.0 TEMPERA TURF OUT, DEG C = 15 5'.'5
PRESSURE, PSIA =80.0 . HEAT LOSS. BTU/HR = 542684.
REACTOR VOLUME, GAL = 120030. RESIDENCE TIME, HR = 9.11
« CONV OF FES2 INPUT - 93.95 % OF INITIAL FES2 CONV = 81.46
ONE OF 10 PARA LI EL REACTORS
FLOWRATE, T/HR
INPUT
OUTPUT
COAL(PUR'E)
FES2
S
FE2(S04)3
FES 04
H2S04
H20
02
INERT GAS
H20 VAPOR
TOTAL
11.3499
.7067
.0231
6,1239
2 ,8 78 4
,8 99 6
44 .5 15 9
.4957
.0027
.0000
m mm mm mm *
66 .9 96 3
-436-
11.3499
.0427
,1651
8.3309
2 .0 42 4
.4668
44.3613
.0000
t0027
.0655
•» mm mm mm m
66 .8 27 6
-------
10.5 MATERIAL AND ENERGY BALANCE
The computer program for calculating the material and energy
balance is the proprietary information of The Dow Chemical
Company and accordingly cannot be included in this report.
The stream numbers, their description, and the results of
the material and energy balance computations are presented
in the following pages.
-437-
-------
10.5.1 Stream List and Descriptions
STREAM
NUMBER DESCRIPTION
1 Pulverized Coal to 100-V-l Mixer
2 Filtrate (Sulfates) from 400-F-1A-D to Stream #4
3 Vent from 100-V-l to 1500-V-l Scrubber
4 Sulfates Return to 100-V-l Mixer
5 Slurry from 100-V-l to Streams #16 and #105
6 Oxygen to Reactors 200-R-1A-K
7 Slurry from Streams #23 and #105 to Reactors 200-
R-1A-K
8 Vent from Reactors 200-R-1A-K to 1500-V-l Scrubber
9 Leached Coal Slurry from Reactors to 200-E-l
Cooler
10 Leached Coal Slurry from Cooler 200-E-l to Filter
400-F-1A-D
11 Steam from Line #24 to 100-V-l Mixer
12 Water from 1100-P-3A&B to Stream #4 (startup only)
14 Sulfates from Stream #40 to 100-V-l Mixer
15 Coal Filter Cake from 400-F-1A-D to 500-V-l
Extractor
16 Slurry from Stream #5 to 1100-F-1A&B Filters
17 Steam from Stream #25 to 1100-V-2 Reslurry Tank
18 Coal Filter Cake from 1100-F-1A&B Filters to
1100-V-2 Reslurry Tank
19 Sulfates from 1100-F-1A&B Filters to 1100-V-l
Concentrator
20 Sulfates from 1100-V-l Concentrator to 1100-E-l
Reboiler
21 Sulfates from 1100-V-l Concentrator to 1100-E-2
Cooler
22 Iron Sulfates Waste from 1100-F-2 Filter &
1100-ME-2 Dryer
-438-
-------
STREAM
NUMBER DESCRIPTION
23 Slurry from 1100-V-2 Reslurry Tank to Stream #105
24 Sulfates from Stream #123 to 1100-ME-2 Dryer
25 Steam from 1100-V-l Concentrator
26 Steam from Line #25 to 1100-ME-l Water Heater
27 Extracted Coal Slurry from 500-V-l Extractor to
600-F-1A-D Filters
28 Water from 100-ME-l Heater to 1100-T-l Water Surge
29 Washed Coal Filter Cake from 600-F-1A-D Filters to
700-V-l Water Wash Tank
30 Filtrate from 600-F-1A-D Filters to 600-V-l
Decanter
31 Distilled Solvent from 1400-T-2 Surge to Stream #37
32 Sulfates from 600-V-l Decanter to Stream #4
33 Solvent from 800-V-l Decanter to 1400-T-l Still
Feed Tank
34 Solvent from 1400-T-l Feed Tank to Streams #72 & #73
35 Sulfur Product from 1400-V-l Still to 1400-T-3
Sulfur Storage
36 Distilled Solvent from 1400-E-4 Cooler to 1400-T-2
Surge
37 Solvent from Streams #31 and #73 to 500-V-l
Extractor
38 Solvent from 600-V-l Decanter to 1400-T-l Still
Feed Tank
39 Washed Coal Slurry from 700-V-l Water Wash Tank
to 800-F-1A-D Filters
40 Weak Sulfates from 800-V-l Decanter to Streams
#14 and #43
41 Wash Water from 800-F-1A-D Filter to Stream #44
42 Filtrate from 800-F-1A-D Filters to 800-V-l
Decanter
43 From Stream #40 to Stream #44
44 From Streams #41 and #43 to 700-V-l Water Wash
Tank
-439-
-------
STREAM
NUMBER DESCRIPTION
45 Washed Coal Filter Cake from 800-F-1A-D to
900-ME-l Dryer
46 Water and Solvent Vapors from 900-ME-l Dryer to
900-E-l Condenser
47 Wash Water from 1100-T-l Surge to 800-F-1A-D
Filters
48 Condensate from 900-E-l Condenser to 900-V-l
Decanter
49 Vent from 900-E-l Condenser to 1500-V-l Scrubber
50 Solvent from 900-V-l Decanter to 1400-T-l Still
Feed Tank
51 Water from 900-V-l Decanter to 1100-T-l Water
Surge
52 Vapor from 1100-ME-2 Dryer to 1100-T-l Water
Surge
53 Product Coal from 900-ME-l Dryer to Storage and
Shipping
54 Solvent from Unloading to 1400-T-4 Solvent Storage
and to 1400-T-2 Recovered Solvent Storage
55af(b) Water Makeup to (or Waste from) 1100-T-l Water
Surge
56 Sulfuric Acid from Unloading to 1100-T-2 Storage
and to 100-V-l Mixer
57 Reflux to 1400-V-l Still from Stream #58
58 Distilled Solvent from 1400-E-3 Condenser to 1400-
V-2 Accumulator and to Stream #57 and to 1400-E-4
Cooler
60 Cooling Water Supply to 200-E-l Cooler
61 Cooling Water Return from 200-E-l Cooler
62 Cooling Water Supply to 1400-E-4 Cooler
63 Cooling Water Return from 1400-E-4 Cooler
-440-
-------
STREAM
NUMBER DESCRIPTION
64 Cooling Water Supply to 1400-E-3 Condenser
65 Cooling Water Return from 1400-E-3 Condenser
66 Cooling Water Supply to 900-E-l Condenser
67 Cooling Water Return from 900-E-l Condenser
68 Cooling Water Supply to 1100-E-5 Condenser
69 Cooling Water Return from 1100-E-5 Condenser
70 Cooling Water Supply to 1100-E-2 Cooler
71 Cooling Water Return from 1100-E-2 Cooler
72 Solvent from Stream #34 to 1400-E-2 Interchanger
73 Solvent from Stream #34 to Stream #37
74 Solvent from 1400-E-2 Interchanger to 1400-V-l
Still
75 Vapor from 1400-V-l Still to 1400-E-2 Interchanger
76 Condensate from 1400-E-2 Interchanger to 1400-E-3
Condenser
77* 50% NaOH to 1500-V-2 Surge-Decanter
78* Process Water to 1500-V-2 Surge-Decanter
79* Recovered Naphtha from 1500-P-2 to 1400-T-l
80* Scrubber Liquor from 1500-V-2 to 1500-P-l
81* Waste Sulfates and Caustic from 1500-P-l
82* Scrubber Liquor from 1500-P-l to 1500-E-l
83* Scrubber Liquor from 1500-E-l to 1500-V-l
84* Vent from 1500-V-l to Adsorption Unit
85* Vent from Adsorption Unit
86* Recovered Naphtha and Water to 900-V-l
88 Cooling Water Supply to 1500-E-l
89 Cooling Water Return from 1500-E-l
90 Steam to 1400-V-l Still Jacket
91 Condensate from 1400-V-l Still Jacket
*Streams marked with an asterisk require further
data to quantify.
-441-
-------
STREAM
NUMBER
DESCRIPTION
92 Steam to 1400-E-l Reboiler
93 Condensate from 1400-E-l Reboiler
94 Steam to 900-ME-l Dryer
95 Condensate from 900-ME-l Dryer
96 Steam to 1100-E-l Heater
97 Condensate from 1100-E-l Heater
98 Steam (125 psi) to Train
100 Steam (400 psi) to 1100-ME-2 Dryer
101 Condensate from 1100-ME-2 Dryer
105 From Stream #5 to Stream #7
114 Sulfates from Stream #40 to 100-V-l Mixer
118 From Stream #123 to 1100-V-2 Reslurry Tank
119 Water from 1100-P-3A&B to 1100-V-2 Reslurry Tank
120 Sulfates from 1100-E-l Heater to 1100-V-l
Concentrator
121 Sulfates from 1100-E-2 Cooler to 1100-F-2 Filter
122 Sulfates Waste from 1100-F-2 to Line #22
123 Filtrate from 1100-F-2 to Streams #24 and #118
124 Sulfates Waste from 1100-ME-2 Dryer to Stream #22
145 Dummy Stream (Internal in 800-F-1A-D)
146* Water from Stream #147 to 1100-ME-l
147* Water from 1100-P-3A&B to Streams #12, #47, #119,
and #146 See the first three of these for the
net amount.
201* Vent from 500-V-l to 1500-V-l Scrubber
202* Vent from 600-V-l to 1500-V-l Scrubber
*Streams marked with an asterisk require further
data to quantify.
-442-
-------
STREAM
NUMBER
203*
204*
205*
206*
207*
208*
209*
210*
211*
212*
Vent
Vent
Vent
Vent
Vent
Vent
Vent
Vent
Vent
Vent
from
from
from
from
from
from
from
from
from
from
DESCRIPTION
700-V-l to 1500-V-l Scrubber
800-V-l to 1500-V-l Scrubber
900-V-l to 1500-V-l Scrubber
1400-V-2 to 1500-V-l Scrubber
1400-T-l to 1500-V-l Scrubber
1400-T-2 to 1500-V-l Scrubber
1400-T-3 to 1500-V-l Scrubber
1400-T-4 to 1500-V-l Scrubber
1100-V-2 to 1500-V-l Scrubber
1100-E-5 to 1500-V-l Scrubber
*Streams marked with an asterisk require further
data to quantify.
-443-
-------
10.5.2 Computer Printout for Material and Energy Balance
-445-
-------
-UNIT OPERATIONS SIMULATOR
COAL-PYRITIC SULFUK REMOVAL
MREAM NUMBER
PULVERIZED COAL TO 100-V-l MIXER
o
on
tx)
COMPONENT NO.
1 COAL
2 FES2
7 H20
TOTALS
MOl.ES/HR
17461.5312
135.8700
1354..0500
18951.4453
MOLE FRACTION
0.921382546
0.007169373
0.071448326
TEMPERATURE 70.0000
PRESSURE 14.7000
HEAT CONTENT 3.3920
FRACI ION VAPOR 0.0
AVG. MOLECULAR WEIGHT 14.13
LBS/HR
226999.875
16301.6797
24393.6641
267695.125
L)EG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.84797907
0.06089644
0.09112477
21.1111 DEG. C)
TIJ N S / H R
113.4999
8.1508
12.1968
133.8476
o
o
3
13
C
rt
H
H-
0)
CU
X
T)
CU
3
O
0)
-------
STREAM NUMBER
VENT FROM 100-V-l TO 1500-V-l SCRUBBER
COMPONENT NO.
TOTALS
MOLES/HR
0.0
MOLE FRACTION
LBS/HR
0.0
WGT FRACTION
TONS/HR
0.0
TEMPERATURE 212.1000
PRESSURE 14.7000
HEAT CONTENT 0.0
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 0.0
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
( 100.0555 DEG. C)
STREAM NUMBER
SULFATES RETURN TO 100-V-l MIXER
COMPONENT NO.
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
8 ?.3239
174.2880
43.0247
24327.3398
24631.9727
MOLE FRACTION
0.003545144
0.007075679
0.001746703
0.987632573
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
13264.7578
69691.1250
4219.8633
438265.125
525440.812
207.7197
35.0000
79.6794
0.0
21.33
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.02524501
0.13263363
0.00803109
0.83409035
97.6221 DEG. C)
TONS/HR
6.6324
34.8456
2.1099
219.1326
262.7202
-------
STREAM NUMBER
SLURRY rROM 100-V-l TO STREAMS #16 AND #105
COMPONENT NO.
1
2
3
4
5
6
7
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
17461.5312
0400
0640
3899
6700
8300
117
115
279
87
133
26433
.4062
44527.9219
MOLE FRACTION
0.392147899
0.002628463
0.000338305
0.006274484
0.001968877
0.003005530
0.593636632
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
226999.875
14042.4570
482.9517
42440.1602
35055.9023
13126.0430
476206.625
808353.875
215.6000
154.7000
102.4605
0.0
DEG F (
PSIA.
MMBTU/HR
WGT FRACTION
0.28081745
0.01737167
0.00059745
0.05250195
0.04336702
0.01623799
0.58910662
102.0000 DEG. C)
TONS/HR
113.4999
7.0212
2415
2201 -
5279:-
5630.
1033
0
21
17
6
238
404.1768
18.15
LBS/MOLE
I
*>.
4*.
00
STREAM NUMBER
OXYGEN TO REACTORS 200-R-1A-K
COMPONENT NO.
9 OXYGEN
10 INERT
TOTALS
MOLES/HR
309.8101
1.5500
311.3599
MOLE FRACTION
0.995022416
0.004978161
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
9913.5469
54.2500
9967.7969
70.0000
154.7000
0.0733
1.0000
32.01
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.99455744
0.00544253
21.1111 DEG. CJ
TONS/HR
4.9568
0.0271
4.9839
-------
STREAM NUMBER
SLURRY FROM STREAMS 23 AND 105 TO REACTORS 200-R-1A-K
IPO
1
2
3
4
5
6
7
NENT NO.
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
17461 .5273
117.0400
15.0640
200.2999
64.7602
133.3035
22438.7617
40430.7383
MOLE FRACTION
0.431887388
0.002894826
0.000372588
0.004954148
0.001601757
0.003297082
0.554992616
LBS/HR
226999.812
14042.4531
482.9517
30426.1523
25895.1602
13074.4023
404241.750
715162.562
TEMPERATURE 215.6034 DEG F
PRESSURE 154.7000 PSIA.
HEAT CONTENT 88.6385 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 17.69 LBS/MOLE
WGT FRACTION
0.31741005
0.01963533
0.00067530
0.04254438
0.03620877
0.01828172
0.56524456
TONS/HR
( 102.0019 DEG. C)
7.0212
0.2415
15.2131
12.9476
6.5372
202.1209
357.5813
STREAM NUMBER 8 VENT FROM REACTORS 2OO-R-1 A-K TO 1500-V-l SCRUBBER
COMPONENT NO.
7 H20
10 INERT
TOTALS
MOLES/HR
11.5900
1.5500
13.1400
MOLE FRACTION
0.882039547
0.117960393
TEMPERATURE 306.1399
PRESSURE 14.7000
HEAT CONTENT 0.2492
FRACIION VAPOR 1.0000
AVG. MOLECULAR WEIGHT 20.02
LBS/HR
208.7977
54.2500
263.0476
DEG F
PSIA.
MMBTU/HR
LBS/MULE
WGT FRACTION
0.79376400
0.20623642
( 152.2999 DEG. C)
TONS/HR
0.1044
0.0271
0.1315
CO
-------
STREAM NUMBER
LEACHED COAL SLURRY FROM REACTORS TO 200-E-l COOLER
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04}3
6 H2S04
7 H20
TOTALS
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE?(S04)3
6 H2S04
7 H20
TOTALS
8
MOLES/HR
17461 .5312
6.5900
103.4200
8/.6260
174.9800
43.8430
22516.6562
40394,6367
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
MOLE FRACTION
0.432273448
0.000163140
0.002560241
0.002169248
0.004331760
0.001085368
0.557416975
304.9102
80.0000
132.9398
0.0
WEIGHT 17.93
LBS/HR
226999.875
790.6680
3315.6448
13310.6523
69967.8125
4300.1250
405645.062
724329.750
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
STREAM NUMBER 10 LEACHED COAL SLURRY FROM
MOLES/HR
17461.5312
6.5900
103.4200
87.6260
174.9800
43.8430
22516.6562
40394.6367
TEMPERATURE
PRESSURE
HEAT CONTENT
FRAC i ION VAPOR
AVG. MOLECULAR
MOLE FRACTION
0.432273448
0.000163140
0.002560241
0.002169248
0.004331760
0.001085368
0.557416975
215.6655
80.0000
89.0054
0.0
WEIGHT 17.93
LBS/HR
226999.875
790.6680
3315.6448
13310.6523
69967.8125
4300.1250
405645.062
724329.750
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.31339300
0.00109159
0.00457753
0.01837651
0.09659660
0.00593669
0.56002814
151.6167 DEG. C)
COOLER 200-E-l TO FILTER
WGT FRACTION
0.31339300
0.00109159
0.00457753
0.01837651
0.09659660
0.00593669
0.56002814
102.0364 DEG. C )
TUMS/HR
1 13.4999
0.3953
1.6578
6.6553
34.9839
2.1501
202.8225
362.1648
400-F-1A-D
TOMS/HR
113.4999
0.3953
1.6578
6.6553
34.9839
2.1501
202.8225
362.1648
-------
STREAM NUMBER 11
STEAM FROM LINE #24 TO 100-V-l MIXER
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
0.4213
842.3984
842.8196
MOLE FRACTION
0.000499811
0.999500275
LBS/HR
41.3162
15176.0898
15217.4023
WGT FRACTION
0.00271506
0.99728513
TONS/HR
0.0207
7.5880
7.6087
TEMPERATURE 290.0000
PRESSURE 35.0000
HEAT CONTENT 17.8643
FRACTION VAPOR 0.9992
AVG. MOLECULAR WEIGHT 18.06
DEG F
PSIA.
MMB1U/HR
LBS/MOLE
( 143.3333 DEG. C)
STREAM NUMBER 12 WATER FROM 1100-P-3-A&B TO STREAM #4 (STARTUP ONLY)
COMPONENT NO.
TOTALS
MOLES/HR
0.0
MOLE FRACTION
TEMPERATURE 77.0000
PRESSURE 14.7000
HEAT CONTENT 0.0
FRACflUN VAPOR 0.0
AVG. MOLECULAR WEIGHT 0.0
LBS/HR
0.0
WGT FRACTION
TUNS/HR
0.0
OEG F ( 25.0000 OEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
-------
STREAM NUMBER 14
SULFATES FROM STREAM #40 TO 100-V-l MIXER
COMPONENT NO.
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
0.7877
1.5730
1.5033
2102.7383
2106.6021
MOLE FRACTION
0.000373931
0.000746700
0.000713596
0.998165846
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
119.6576
628.9332
147.4400
37881.5312
38777.6094
173.5363
54.7000
5.3840
0.0
18.41
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00308574
0.01622026
0.00380219
0.97689182
78.6312 D6G. C)
TONS/HR
0.0598
0.3145
0.0737
18.9408
19.3888
01
-------
STREAM NUMBER 15 COAL FILTER CAKE FROM 400-F-1A-D TO 500-V-l EXTRACTOR
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
17461.5273
6.5900
103.4200
8.. 2 116
16.3978
4.1086
2110.0916
19710.3359
MOLE FRACTION
0.885907114
0.000334342
0.005246989
0.000416616
0.000831938
0.000208451
0.107055068
LBS/HR
226999.812
790.6677
3315.6443
1247.3740
6556.8477
402.9751
38014.0039
277327.125
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.2102
14.7000
18.8784
0.0
14.07
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.81852722
0.00285103
0.01195572
0.00449784
0.02364301
0.00145307
0.13707274
101.7834 DEG. C)
TONS/HR
113.4999
0.3953
1.6578
0.6237
3.2784
0.2015
19.0070
138.6636
STREAM NUMBER 16 SLURRY FROM STREAM #5 TO 1100-F-1ASB FILTERS
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
5479.4297
36.7272
4.7271
87.6725
27.5108
41.9959
8294.8047
13972.8594
MOLE FRACTION
0.392148018
0.002628464
0.000338305
0.006274488
0.001968877
0.003005531
0.593636870
LBS/HR
71232.5625
4406.5234
151.5503
13317.7227
11000.5430
4118.9531
149433.625
253661.312
01
CO
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.6000
154.7000
32.1521
0.0
18.15
DEG F (
PSIA.
MMBTU/HR
LBS/MULE
WGT FRACTION
0.28081757
0.01737168
0.00059745
0.05250198
0.04336705
0.01623800
0.58910686
102.0000 OEG. C)
TONS/HR
35.6163
2.2033
0.0758
6.6589
5.5003
2.0595
74.7168
126.8307
-------
STREAM NUMBER 17
STEAM FROM STREAM #25 TO 1100-V-2 RESLURRY TANK
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
0.1831
366.0676
366.2505
MOLE FRACTION
0.000499814
0.999500692
TEMPERATURE 290.0000
PRESSURE 35.0000
HEAT CONTENT 7.7626
FRACTION VAPOR 0.99*2
AVG. 'MOLECULAR WEIGHT 18.06
LBS/HR
17.9542
6594.8281
6612.7812
WGT FRACTION
0.00271508
0.99728507
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
( 143.3333 OEG. C)
TONS/HR
0.0090
3.2974
3.3064
STREAM NUMBER 18 COAL FILTER CAKE FROM 1100-F-1ASB FILTERS TO 1100-V-2 RESLURRY TANK
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
5479.4258
36.7271
4.7271
7.4714
2.3445
3.5789
706.8806
6241.1484
MOLE FRACTION
0.877951503
0.005884673
0.000757406
0.001197125
0.000375647
0.000573432
0,113261282
LBS/HR
71232.5000
4406.5195
151.5502
1134.9329
937.4634
351.0159
12734.6875
90948.5000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.6000
154.7000
6.1547
0.0
14.57
OEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.78321797
0.04845071
0.00166633
0.01247885
0.01030763
0.00385950
0.14002085
102.0000 DEG. C)
TONS/HR
35.6162
2.2033
0.0758
0.5675
0.4687
0.1755
6.3673
45.4743
-------
STREAM NUMBER 19 SULFATES FROM 1100-F-1-A§B FILTERS TO 1100-V-l CONCENTRATOR
COMPONENT NO.
1 COAL
2 FES2
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
0.0039
0.0000
2011
1664
4170
9219
80
25
38
7587
7731.7109
MOLE FRACTION
0.000000505
0.000000002
0.010373008
0.003254956
0.004968751
0.981402636
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
0.0508
0.0018
12182.7891
10063.0781
3767.9370
136698.937
162712.750
215.6000
54.7000
25.9974
0.0
21.04
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000031
0.00000001
0.07487297
0.06184566
0.02315699
0,84012431
102.0000 DEG. C)
TONS/HR
0.0000
0.0000
6.0914
5.0315
1.8840
68.3495
81.3564
STREAM NUMBER 20 SULFATES FROM 1100-V-l CONCENTRATOR TO 1100-E-l REBOILER
COMPONENT NO.
1 COAL
2 FES2
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
0.0391
0.0002
80^.0110
25!.6638
350.4695
848/.6172
9891.7969
MOLE FRACTION
0.000003949
0.000000015
0.081078351
0.025441665
0.035430312
0.858045995
LBS/HR
0.5078
0.0183'
121827.812
100630.812
34374.0469
152907.250
409740.375
I
£>.
Oi
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
290.0000
50.0000
51.8622
0.0
41.42
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000124
0.00000004
0.29732925
0.24559647
0.08389223
0.37318081
143.3333 DEG. C)
TONS/HR
0.0003
0.0000
60.9139
50.3154
17.1870
76.4536
204.8702
-------
STREAM NUMBER 21
SULFATES FROM 1100-V-l CONCENTRATOR TO 1100-E-2 COOLER
COMPONENT NO.
1 COAL
2 FES2
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
0.0039
0.0000
80.2011
21?. 1664
3-5.0470
84H.7617
989. 1836
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
MOLE FRACTION
0.000003949
0.000000015
0.081078053
0.025441565
0.035430193
0.858042598
290.0000
50.0000
5.1862
0.0
WEIGHT 41.42
LBS/HR
0.0508
0.0018
12182.7891
10063.0781
3437.4065
15290.7266
40974.0508
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000124
0.00000004
0.29732937
0.24559635
0.08389223
0.37318069
143.3333 DEG. C)
TONS/HR
0.0000
0.0000
6.0914
5.0315
1 . 7 1. M 7
7.6454
20.4870
STREAM NUMBER 22
IRON SULFATES WASTE FROM 1100-F-2 § 1100-ME-2 DRYER
COMPONENT NO.
1 COAL
2 FES2
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
I
*.
en
o
ij
7V
2^
3/
398
,0035
.0000
,0900
.9097
.0104
.4204
532.4343
MOLE FRACTION
0.000006603
0.000000026
0.148544073
0.043028299
0.060120765
0.748299599
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
0.0457
0.0016
12014.0039
9160.7344
3139.5762
7177.6758
31492.0352
77.0000
14.7000
0.0
0.0
59.15
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000145
0.00000005
0.38149339
0.29089051
0.09969425
0.22792029
25.0000 DEG. C)
TUNS/HR
0.0000
0.0000
6.0070
4.5804
1.5698
3.5888
15.7460
-------
STREAM NUMBER 23
SLURRY FROM 1100-V-2 RESLURRY TANK TO STREAM #105
COMPONENT NO.
1
2
3
4
5
6
7
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
5479.4258
7271
7271
5825
6011
36
4
8
4
41
4300
,4693
1602
MOLE FRACTION
0.554840147
0.003718947
0.000478659
0.000869059
0.000465901
0.004199136
0.435429096
9875.6836
LBS/HR
71232.5000
4406.5195
151.5502
1303.7146
1839.8010
4067.3132
77468.8125
160470.062
WGT FRACTION
0.44389898
0.02746007
0.00094441
0.00812435
0.01146507
0.02534624
0.48276174
TOMS/HR
35.6162
.2033
,0758
,6519
,9199
.0337
,7344
2
0,
0,
0.
2
38.
80.2350
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.6000
14.7000
18.3284
0.0
16.25
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
102.0000 DEG. C)
STREAM NUMBER 24
SULFATES FROM STREAM #123 TO 1100-ME-2 DRYER
COMPONENT NO.
1
2
4
5
6
7
COAL
FES2
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0035
0.0000
10.0042
20.3179
24.9008
569.0696
624.2959
MOLE FRACTION
0.000005632
0.000000022
0.016024716
0.032545280
0.039886143
0.911538184
LBS/HR
0.0457'
0.0016
1519,
8124,
2442,
10251
,6626
,3516
,2661
.9766
WGT FRACTION
0.00000205
0.00000007
0.06802940
0.36369604
0. 10933083
0.45894164
22338.3008
TUNS/HR
0.0000
0.0000
0.7598
4.0622
1.2211
5.1260
11. 1692
tn
-4
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACITON VAPOR
AVG. MOLECULAR WEIGHT
215.0000
14.7000
2.3261
0.0
35.78
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
101.6666 IJEG. C)
-------
STREAM NUMBER 25
STEAM FROM 1100-V-l CONCENTRATOR
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
3.3700
6739.1602
6742.t>273
MOLE FRACTION
0.000499812
0.999500573
LBS/HR
330.5295
121408.187
121738.687
WGT FRACTION
0.00271507
0.99728513
TEMPERATURE 290.0000
PRESSURE 35.0000
HEAT CONTENT 142.9143
FRACTION VAPOR 0.9992
AVG. MOLECULAR WEIGHT 18.06
DEG F { 143.3333 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
TUNS/HR
0. 1653
60.7041
60.8693
STREAM NUMBER 26 STEAM FROM LINE #25 TO 1100-ME-l WATER HEATER
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
2.7657
5530.6914
5533.4531
MOLE FRACTION
0.000499813
0.999500871
LBS/HR
271.2590
99637.2500
99908.5000
TEMPERATURE 290.0000
PRESSURE 35.0000
HEAT CONTENT 117.2868
FRACIION VAPOR 0.9992
AVG. MOLECULAR WEIGHT 18.06
DEG F
PSIA,
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00271507
0.99728501
TONS/HR
0.1356
49.8186
49.9542
( 143.3333 DEG. C)
Ol
00-
-------
STREAM NUMBER 27 EXTRACTED COAL SLURRY FROM 500-V-l EXTRACTOR TO 600-F-1A-D FILTERS
COMPONENT NO.
1
2
3
4
5
6
7
8
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H2U
SOLVENT
TOTALS
MOLES/HR
17461.5273
6.5900
206.8400
B-.2116
16.3978
4.1086
2110.0916
298^.0078
22795.7617
MOLE FRACTION
0.765998840
0.000289089
0.009073611
0.000360227
0.000719334
0.000180237
0.092565060
0.130814075
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
226999.812
790.6677
6631.2852
1247.3740
6556.8477
402.9751
38014.0039
276303.875
556946.625
162.0000
54.7000
34.3561
0.0
24.43
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.40757906
0.00141965
0.01190650
0.00223967
0.01177284
0.00072354
0.06825429
0.49610472
72.2222 DEG. C)
TONS/HR
113.4999
0,
3
0,
3
0,
19
138,
3953
.3156
6237
.2784
2015
.0070
1519
278.4731
STREAM NUMBER 28
WATER FROM 1100-ME-l HEATER TO 1100-T-l WATER SURGE
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
b.5314
13030.6133
13036.1406
MOLE FRACTION
0.000424311
0.999575973
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
542.5181
234750.812
235293.312
212.0402
14.7000
141.0213
0.4330
DEG
PSI
MMB
F (
A.
TU/HR
WGT FRACTION
0.00230571
0.99769431
( 100.0223 DEG. C)
TONS/HR
0.2V13
117.3754
117.6467
18.05
LBS/MOLE
01
to
-------
STREAM NUMBER 29
COMPONENT MO.
1 COAL
2 FFS2
3 SULFUR
4 FFS04
5 FE2(S04)3
6 H2S04
7 H20
8 SOLVENT
TOTALS
MOI hS/HR
1746! .3234
6.5900
2M.6284
I. 1366
i). 5687
29/.0547
41/.7354
18205.4961
WASHED COAL FILTER CAKE FROM 600-F-1A-D FILTERS TO
700-V-l WATER WASH TANK
MOLE FRACTION
0.959134698
0.000361978
0.001572513
0.000062430
0.000124665
0.000031236
0.016042113
0.022670917
LBS/HR
226999.750
790.6675
917.8259
172.6472
907.5234
55.7752
5261.4609
38242.8164
273348.312
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACiION VAPOR
AVG. MOLECULAR WEIGHT
161.3279
14.7000
11.7441
0.0
15.01
DEG F (
PSIA.
MMRTU/HR
LBS/MOLE
WGT FRACTION
0.83044136
0.00289253
0.00335772
0.00063160
0.00332003
0.00020404
0.01924819
0.13990504
71.8488 DEG. C)
TOMS/HK
1 13.4999
0.3953
0.4589
0.0863
0.4538
0.0279
2.6307
19.1214
136.6742
STREAM NUMBER 30 FILTRATE FROM 600-F-1A-D FILTERS TO 600-V-l DECANTER
COMPONENT NO.
1 COAL
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
8 SOLVENT
TOTALS
o
MOLES/HR
l).0039
178.2116
f.0751
14.1282
3.5400
181M.0369
2564.2725
4590.^656
MOLE FRACTION
0.000000851
0.038823802
0.001541324
0.003077859
0.000771190
0.396063507
0.559721947
LBS/HR
0.0508
5713.4609
1074.7268
5649.3242
347.2000
32752.5430
238061 .062
283598.312
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACIION VAPOR
AVG. MOLECULAR WEIGHT
161.3795
14.7000
22.4284
0.0
61.78
DEG F (
PSIA.
MMRTU/HR
LBS/MOLE
WGT FRACTION
0.00000018
0.02014631
0.00378961
0.01992016
0.00122427
0.11548918
0.83943045
71.8775 DEG. C)
TONS/HR
0.0000
,8567
.5374
,8247
.1736
,3/63
.0305
7991
2.
0,
2.
0,
16.
119,
141
-------
STREAM NUMBER 31 DISTILLED SOLVENT FROM 1400-T-2 SURGE TO STREAM #37
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
1465.5002
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
135788.812
135788.812
93.2871
54.7000
4.4861
0.0
92.66
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
34.0484 DEG. C)
TONS/HR
67.8944
67.8944
STREAM NUMBER 32
SULFATES FROM 600-V-l DECANTER TO STREAM #4
IPO
1
4
5
6
7
NENT NO.
COAL
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0039
7.0751
14.1282
3.5400
1818.0369
1842.7817
MOLE FRACTION
0.000002120
0.003839352
0.007666770
0.001920991
0.986571968
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
0.0508
1074.7268
5649.3242
347.2000
32752.5430
39823.8437
161.3795
54.7000
4.3921
0.0
DEG F (
PSIA.
MMBTU/HR
WGT FRACTION
0.00000128
0.02698702
0.14185780
0.00871839
0.82243550
71.8775 DEG. C)
TONS/HR
0.0000
0.5374
2.8247
0.1736
16.3763
19.9119
21.61
LBS/MOLE
*>.
-------
STREAM NUMBER 33 SOLVENT FROM 800-V-l DECANTER TO 1400-T-l STILL FEED TANK
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
26.6792
384.6340
411.3132
MOLE FRACTION
0.064863443
0.935136497
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG.'MOLECULAR WEIGHT
LBS/HR
855.3350
35639.0312
36494.3633
173.5363
14.7000
2.9949
0.0
88.73
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.02343745
0.97656262
78.6312 DEG. C)
TONS/HR
0.4277
17.8195
18.2472
STREAM NUMBER 34
SOLVENT FROM 1400-T-l FEED TANK TO STREAMS #72 S #73
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
204.8908
297V.4670
3184.3577
MOLE FRACTION
0.064342856
0.935657144
LBS/HR
6568.7969
276068.437
282637.187
WGT FRACTION
0.02324109
0.97675902
TEMPERATURE 165.0525
PRESSURE 54.7000
HEAT CONTENT 21.5978
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 88.76
DEG F ( 73.9180 DEG. Cj
PSIA.
MMBTU/HR
•LBS/MOLE
TONS/HR
3.2844
138.0342
141.3186
to
-------
STREAM NUMBER 35 SULFUR PRODUCT FROM 1400-V-l STILL TO 1400-T-3 SULFUR STORAGE
COMPONENT NO.
3 SULFUR
TOTALS
MOLES/HR
101.4748
101.4748
MOLE FRACTION
1.00000000
TEMPBRATURE 266.0000
PRESSURE 14.7000
HEAT CONTENT 0.2248
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 32.06
LBS/HR
3253.2815
3253.2815
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
130.0000 DEG. C)
TONS/HR
1.6266
1.6266
STREAM NUMBER 36
DISTILLED SOLVENT FROM 1400-E-4 COOLER TO 1400-T-2 SURGE
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
1462.9595
1462.9595
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
135553.375
135553.375
93.3285
14.7000
4.4815
0.0
92.66
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
34.0714 DEG. C)
TONS/HR
67.7767
67.7767
w
-------
STREAM NUMBER 37 SOLVENT FROM STREAMS #31 AND #73 TO 500-V-l EXTRACTOR
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
103.4200
2982.0078
3085.4277
MOLE FRACTION
0.033518847
0.966481149
LBS/HR
3315.6443
276303.875
279619.500
WGT FRACTION
0.01185770
0.98814231
TONS/HR
1.6578
138.1519
139.8098
i
*>.
Oi
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG.'MOLECULAR WEIGHT
131.2932
54.7000
15.4784
o.o -
90.63
DEC F (
PSIA.
MMBTU/HR
LBS/MOLE
55.1629 DEG. C)
STREAM NUMBER 38 SOLVENT FROM 600-V-l DECANTER TO 1400-T-l STILL FEED TANK
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLfcS/HR
178.2116
2569.2725
2747.4839
MOLE FRACTION
0.064863503
0.935136497
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
5713.4609
238061.062
243774.500
161.3795
14.7000
18.0363
0.0
88.73
DEG F (
PSIA.
MMBTU/HR
•LBS/MOLE
WGT FRACTION
0.02343748
0.97656256
71.8775 DEG. C)
TONS/HR
2.8567
119.0305
121.8872
-------
STREAM NUMBER 39
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
8 SOLVENT
TOTALS
MOLES/HR
1746).5234
6.5900
31.9733
5.7214
1!.4251
10.9186
1527^.7187
460.9595
33261.8164
WASHED COAL SLURRY FROM 700-V-l WATER WASH TANK TO
800-F-1A-D FILTERS
MOLE FRACTION
0.524972022
0.000198125
0.000961262
0.000172012
0.000343490
0.000328261
0.459166706
0.013858516
LBS/HR
226999.750
790.6675
1025.0652
869.1033
4568.4648
1070.8936
275143.125
42711.1172
553178.000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
173.8569
54.7000
51.7248
0.0
16.63
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTIUN
0.41035569
0.00142932
0.00185305
0.00157111
0.00825858
0.00193589
0.49738622
0.07721043
78.8094 DEG. C)
TONS/HR
113.4999
0
0
3953
5125
4346
2842
5354
5715
?1.3555
276.bH89
0
2
0
137
STREAM NUMBER 40 WEAK SULFATES FROM 800-V-l DECANTER TO STREAMS #14 AND #43
COMPONENT NO.
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
4.7741
9.5333
9.1107
12743.8672
12767.2812
MOLE FRACTION
0.000373931
0.000746701
0.000713596
0.998166084
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
725.1975
3812.0217
893.5757
229585.000
235015.750
173.5363
54.7000
32.6305
0.0
18.41
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00308574
0.01622028
0.00380219
0.97689193
78.6312 DEG. C)
TUNS/HR
0.3626
1.9060
0.4468
114.7925
1 17.5079
-------
STREAM NUMBER 41
WASH WATER FROM 800-F-1A-D FILTER TO STREAM #44
COMPONENT NO.
3 SULFUR
4 FES04
5 FE2
-------
STREAM NUMBER 43
FROM STREAM #40 TO STREAM #44
COMPONENT NO.
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
3.9864
7.9603
7.6074
1064T.1289
10660.6797
MOLE FRACTION
0.000373931
0.000746701
0.000713596
0.998166084
LBS/HR
605.5398
3183.0383
746.1357
191703.500
196238.187
TEMPERATURE 173.5363 DEC F
PRESSURE 24.7000 PSIA.
HEAT CONTENT 27.2465 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.41 LBS/MOLE
WGT FRACTION
0.00308574
0.01622028
0.00380219
0.97689188
( 78.6312 DEG. C)
TONS/HR
0.3028
1.5915
0.3731
95.8517
98.1191
STREAM NUMBER 44 FROM STREAMS #41 AND #43 TO 700-V-l WATER WASH TANK
COMPONENT NO.
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
8 SOLVENT
TOTALS
MOLES/HR
3.3449
4.5849
9.1556
10.3500
14980.7695
48.2239
15056.4258
MOLE FRACTION
0.000222160
0.000304515
0.000608085
0.000687413
0.994975150
0.003202876
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
107.2385
696.4622
3660.9741
1015.1260
269883.562
4468.2773
279831.562
178.1713
24.7000
39.9824
0.0
18.59
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00038323
0.00248886
0.01308278
0.00362763
0.96445000
0.01596774
81.2062 DEG. C)
TONS/HR
0.0536
0.3482
1.8305
0.5076
134.9418
2.2341
139.9158
en
«j
i
-------
STREAM NUMBER 45 WASHED COAL FILTER CAKE FROM 800-F-1A-D TO 900-ME-l DRYER
PO
1
2
3
4
5
6
7
8
NENT NO.
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H20
SOLVENT
TOTALS
MOLES/HR
17461.5234
6.5900
1.9492
0.3488
0.6965
0.6656
252H.8494
28.. 1016
20028.7148
MOLE FRACTION
0.871824443
0.000329027
0.000097320
0.000017415
0.000034776
0.000033234
0.126261175
0.001403064
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
226999.750
790.6675
62.4913
52.9834
278.5083
65.2851
45558.0664
2603.8076
276411.312
189. 1000
14.7000
17.3074
0.0
13.80
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.82123899
0.00286047
0.00022608
0.00019168
0.00100759
0.00023619
0.16481978
0.00942004
87.2778 DEG. C)
TONS/HR
113.4999
0.3953
.0312
,0265
1393
,0326
.7790
,3019
0,
0.
0,
0.
22
1.
138.2057
STREAM NUMBER 46 WATER AND SOLVENT VAPORS FROM 900-ME-l DRYER TO 900-E-l CONDENSER
COMPONENT NO.
7 H20
8 SOLVENT
TOTALS
MOLES/HR
2023.0737
28.1016
2051.1753
MOLE FRACTION
0.986299753
0.013700232
LBS/HR
36446.3477
2603.8076
39050.1523
TEMPERATURE 212.1000 DEG F
PRESSURE 14.7000 PSIA.
HEAT CONTENT 42.5804 MMBTU/HR
FRACIION VAPOR 1.0000
AVG. MOLECULAR WEIGHT 19.04 LBS/MOLE
WGT FRACTION
0.93332148
0.06667852
( 100.0555 OEG. C)
TONS/HR
18.2232
1.3019
19.5251
00
-------
STREAM NUMBER 47
WASH WATER FROM 1100-T-l SURGE TO 800-F-1A-D FILTERS
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
I.6003
4339.6445
4341.2422
MOLE FRACTION
0.000368627
0.999631941
LBS/HR
156.9573
78180.1250
78337.0625
WGT FRACTION
0.00200361
0.99799663
TEMPERATURE 212.0028
PRESSURE 54.7000
HEAT CONTENT 14.0914
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.04
DEG F
PSIA.
MM8TU/HR
LBS/MOLE
( 100.0015 DEG. C)
TOMS/HR
0.0785
39.0901
39.1685
STREAM NUMBER 48
CONDENSATE FROM 900-E-l CONDENSER TO 900-V-l DECANTER
COMPONENT NO.
7 H20
8 SOLVENT
TOTALS
MOI.ES/HR
2009.7637
2b.5606
2035.3242
MOLE FRACTION
0.987441480
0.012558479
LBS/HR
36206.5625
2368.3662
38574.9258
WGT FRACTION
0.93860352
0.06139652
TONS/HR
18.1033
1.1842
19.2874
TEMPERATURE 200.0000
PRESSURE 14.7000
HEAT CONTENT 6.3258
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.95
DEG F ( 93.3333 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
-------
STREAM NUMBER 49
VENT FRUM 900-E-l CONDENSER TO 1500-V-l SCRUBBER
COMPONENT NO.
7 H20
8 SOLVENT
TOTALS
MOLES/HR
13.3100
?.5410
15.8510
MOLE FRACTION
0.839694619
0.160305321
TEMPERATURE 212.1000
PRESSURE 14.7000
HEAT CONTENT 0.3338
FRACTION VAPOR 1.0000
AVG. 'MOLECULAR WEIGHT 29.98
LBS/HR
239.7841
235.4415
475.2253
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.50456923
0.49543113
( 100.0555 DEG. C)
TONS/HR
0.1199
0.1177
0.2376
STREAM NUMBER 50 SOLVENT FROM 900-V-l DECANTER TO 1400-T-l STILL FEED TANK
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
2b.5606
25.5606
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
2368.3662
2368.3662
200.0000
14.7000
0.5664
1.0000
92.66
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
93.3333 DEG. C)
TONS/HR
1.1842
1.1842
-------
STREAM NUMBER 51 WATER FROM 900-V-l DECANTER TO 1100-T-l WATER SURGE
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
2009.7637
2009.7637
MOLE FRACTION
1.00000000
TEMPE-RATURE
PRESSURE
HEAT CONTENT
FRACI ION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
36206.5625
36206.5625
200.0000
14.7000
6.0839
0.0
18.02
DEG F {
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
93.3333 DEG. C)
TONS/HR
18.1033
18.1033
-4
M
STREAM NUMBER 52 VAPOR FROM 1100-ME-2 DRYER TO 1100-T-l WATER SURGE
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
0.2710
38/.1372
387.4080
MOLE FRACTION
0.000699511
0.999301076
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACViON VAPUk
AVG. MOLECULAR WEIGHT
LBS/HR
26.5793
6974.4-062
7000.9844
353.0200
14.7000
8.3318
1.0000
18.07
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00379651
0.99620360
178.3444 DEG. C)
TONS/HR
0.0133
3.4872
3.5005
-------
STREAM NUMBER 53 PRODUCT COAL FROM 900-ME-l DRYEP.TO STORAGE
COMPONENT NO.
1 COAL
2 FES2
3 SULFUR
4 FES04
5 FE2(S04)3
6 H2S04
7 H20
TOTALS
MOLES/HR
17461.5234
5900
.9492
,3488
.6965
,6656
6,
1,
0.
U,
0.
505,
7756
17977.5391
MOLE FRACTION
0.971296608
0.000366568
0.000108424
0.000019402
0.000038743
0.000037026
0.028133750
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACT ION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
226999.750
790.6675
62.4913
52.9834
278.5083
65.2851
9111.7148
237361.187
160.0
14.7000
12.9980
0.0.
13.20
DEG F (
PSIA.
MMBTU/HR
LBS/MULE
WGT FRACTION
0.95634735
0.00333107
0.00026327
0.00022322
0.00117335
0.00027505
0.03838755
71.1
DEG. C)
TONS/HR
113.4999
0.3953
,0312
,0265
1393
,0326
,5559
0,
0,
0,
0,
4,
1 18.6806
STREAM NUMBER 54
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
/.5410
2.5410
SOLVENT FROM UNLOADING TO 1400-T-4 SOLVENT STORAGE AND TO
1400-T-2 RECOVERED SOLVENT STORAGE
MOLE FRACTION
1.00000000
TEMPERATURE 70.0000
PRESSURE 54.7000
HEAT CONTENT 0.0047
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 92.66
LBS/HR
235.4415
235.4415
DEG F (
PSIA.
MMBTU/HR
LBS/MGLE
WGT FRACTION
1.00000000
'1.1111 DEG. C)
TONS/HR
0.1177
0.1177
to
-------
STREAM NUMBER 55
WATER MAKEUP TO (OR WASTE FROM) 1100-T-l WATER SURGE
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
-0.2710
-427.6704
•427.9412
MOLE FRACTION
0.000633255
0.999367297
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
-26.5793
-7704.6250
-7731.2031
212.0028
54.7000
-1.3894
0.0
18.07
DEG F (
PSIA.
MMttTU/HK
LBS/MOLE
WGT FRACTION
0.00343792
0.99656218
100.0015 DEG. C)
TONS/HR
-0.0133
-3.8523
-3.8656
STREAM NUMBER 56
SULFURIC ACID FROM UNLOADING TO 1100-T-2 STORAGE AND TO
100-V-l MIXER
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
33.7764
3.7519
37.5283
MOLE FRACTION
0.900025368
0.099974751
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
L6S/HR
3312.7905
67.5914
3380.3818
70.0000
54.7000
0.0446
0.0
90.08
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.98000479
0.01999521
21.1111 DEG. C)
TUNS/HK
1.6564
0.0338
1.6902
CO
I
-------
STREAM NUMBER 57 REFLUX TO 1400-V-l STILL FROM STREAM #58
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
731.4797
731.4797
MOLE FRACTION
1.00000000
LBS/HR
67776.6875
67776.6875
WGT FRACTION
1.00000000
TEMPERATURE 248.0000 DEG F
PRESSURE 60.0000 PSIA.
HEAT CONTENT 9.4368 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 92.66 LBS/MOLE
TONS/HR
33.8883
33.8883
( 120.0000 DEG. C)
STREAM NUMBER 58
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
2194.4392
2194.4392
DISTILLED SOLVENT FROM 1400-E-3 CONDENSER TO 1400-V-2 ACCUMULATOR
AND TO STREAM #57 AND TO 1400-E-4 COOLER
MOLE FRACTION
1.00000000
LBS/HR
203330.125
203330.125
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
248.0000
60.0000
28.3105
0.0
92.66
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
120.0000 DEG. C)
TONS/HR
101.6651
101.6651
-------
STREAM NUMBER 59
COMPONENT NO.
TOTALS
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
0.0
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
MOLE FRACTION LBS/HR WGT FRACTION
0.0
77.000.0 DEG F ( 25.0000 DEG. C)
14.7000 PSIA.
0.0 MMBTU/HR
0.0
WEIGHT 0.0 LBS/MOLE
STREAM NUMBER 60 COOLING WATER SUPPLY TO 200-E-l COOLER
MOLES/HR
121904.500
121904.500
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
MOLE FRACTION LBS/HR WGT FRACTION
1.00000000 2196150.00 1.00000000
2196150.00
85.0000 DEG F ( 29.4444 DEG. Cl
54.7000 PSIA.
116.4228 MMBTU/HR
0.0
WEIGHT 18.02 LBS/MOLE
TOMS/HR
0.0
TONS/HR
1098.0750
1098.0750
I
rfk
^i
01
-------
STREAM NUMBER 61 COOLING WATER RETURN FROM 200-E-l COOLER
COMPONENT NO.
7 H20
TOTALS
MOL6S/HR
121904.500
121904.500
MOLE FRACTION
1.00000000
LBS/HR
2196150.00
2196150.00
WGT FRACTION
1.00000000
TEMPERATURE 105.0350
PRESSURE 54.7000
HEAT CONTENT 160.3509
FRAClION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02
DEG F ( 40.5750 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
TOMS/HK
1098.0750
1098.0750
STREAM NUMBER 62
COOLING WATER SUPPLY TO 1400-E-4 COOLER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
52368.5977
52368.5977
MOLE FRACTION
1.00000000
LBS/HR
943437.812
943437.812
WGT FRACTION
1.00000000
TONS/HR
471.7187
471 .7187
TEMPERATURE 85.0000
PRESSURE 54.7000
HEAT CONTENT 50.0133
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02
DEG F ( 29.4444 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
I
*>.
Ol
-------
STREAM NUMBER 63 COOLING WATER RETURN FROM 1400-E-4 COOLER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
52368.5977
52368.5977
MOLE FRACTION
1.00000000
LBS/HR
943437.812
943437.812
WGT FRACTION
1.00000000
TONS/HR
471 .7187
471.7187
COMPONENT NO.
7 H20
TOTALS
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
105.0350 DEG F ( 40.5750 DEG. C)
54.7000 PSIA.
68.8842 MMBTU/HR
0.0
WEIGHT 18.02 LBS/MOLE
STREAM NUMBER 64 COOLING WATER SUPPLY TO 1400-E-3 CONDENSER
MOLES/HR
4972/.55S6
49722.5586
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR
MOLE FRACTION LBS/HR WGT FRACTION
1.00000000 895768.500 1.00000000
895768.500
85.0000 DEG F ( 29.4444 DEG. C)
54.7000 PSIA.
47.4863 MMBTU/HR
0.0
WEIGHT 18.02 LBS/MOLE
TONS/HR
447.8840
447.8840
-------
STREAM NUMBER 65
COOLING WATER RETURN FROM 1400-E-3 CONDENSER
COMPONENT MO.
7 H2U
TOTALS
MOLES/HR
4972/.5S86
49722.5586
MOLE FRACTION
1.00000000
LBS/HR
895768.500
895768.500
TEMPERATURE 105.0350 DEG F
PRESSURE 54.7000 PSIA.
HEAT CONTENT 65.4037 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02 LBS/MOLE
WGT FRACTION
1.00000000
TONS/HR
447.8840
447.8840
( 40.5750 DEG. C)
STREAM NUMBER 66
COOLING WATER SUPPLY TO 900-E-l CONDENSER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
99669.3125
99669.3125
MOLE FRACTION
1.00000000
LBS/HR
1795576.00
1795576.00
WGT FRACTION
1.00000000
TOMS/HR
897.7878
897.7878
TEMPERATURE 85.0000
PRES>URE 54.7000
HEAT CONTENT 95.1877
FRACfION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02
DEG F ( 29.4444 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
oo
-------
STREAM NUMBER 67 COOLING WATER RETURN FROM 900-E-l CONDENSER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
99669.3125
99669.3125
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
1795576.00
1795576.00
105.
54.
131.
0.
0350
7000
1033
0
DEG
PSI
MMB
F (
A.
TU/HR
18.02
LBS/MGLE
WGT FRACTION
1.00000000
40.5750 DEG. C)
TONS/HR
897.7878
897.7878
STREAM NUMBER 68 COOLING WATER SUPPLY TO 1100-E-5 CONDENSER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
294004.812
294004.812
MOLE FRACTION
1.00000000
LBS/HR
5296595.00
5296595.00
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACI ION VAPOR
AVG. MOLECULAR WEIGHT
85.0000
54.7000
280.7822
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
29.4444 DEG. C)
TONS/HR
2648.2974
2648.2974
I
£>
-4
-------
STREAM NUMBER 69
COOLING WATER RETURN FROM 1100-E-5 CONDENSER
COMPONENT NO.
7 H20
TOTALS
MQl.ES/HR
294004.812
294004.812
MOLE FRACTION
1.00000000
TEMPtKATURE
PRESSURE
.HEAT CONTENT
FRACIION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
5296595.00
5296595.00
105.3040
54.7000
388.1489
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTIUN
1.00000000
40.7245 DEG. C)
TUMS/HR
2648.2974
2648.2974
I
*.
oo
STREAM NUMBER 70
COOLING WATER SUPPLY TO 1100-E-2 COOLER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
424b.0078
4245.0078
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
76475.1875
76475.1875
85.0000
54.7000
4.0542
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
29.4444 DEG. C)
TONS/HR
38.2376
38.2376
-------
STREAM NUMBER 71 COQUNG WATER RETURN FROM 1100-E-2 COOLER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
4245.0078
4245.0078
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRAC1ION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
76475.1875
76475.1875
105.0350
54.7000
5.5838
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
40.5750 DEG. C)
TONS/HR
38.2376
38.2376
I
>Ct
00
STREAM NUMBER 72
SOLVENT FROM STREAM #34 TO 1400-E-2 INTERCHANGER
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
101.4708
146^.9595
1564.4302
MOLE FRACTION
0.064861178
0.935138822
LBS/HR
3253.1533
135553.375
138806.500
WGT FRACTION
0.02343661
0.97656357
TONS/HR
1.6266
67.7767
69.4032
TEMPERATURE 165.0525 DEG F
PRESSURE 54.7000 PSIA.
HEAT CONTENT 10.6055 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 88.73 LBS/MOLE
( 73.9180 DEG. C)
-------
STREAM NUMBER 73
SOLVENT FROM STREAM #34 TO STREAM #37
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
103.4200
1516.5076
1619.9275
MOLE FRACTION
0.063842297
0.936157644
TEMPt-RATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. 'MOLECULAR WEIGHT
LBS/HR
3315.6443
140515.000
143830.625
165.0525
54.7000
10.9923
0.0
88.79
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.02305242
0.97694767
73.9180 DEG. C)
TONS/HR
1.6578
70.2575
71 .9153
00
N>
I
STREAM NUMBER 74 SOLVENT FROM 1400-E-2 INTERCHANGE!* TO 1400-V-l STILL
COMPONENT NO.
3 SULFUR
8 SOLVENT
TOTALS
MOLES/HR
101..4708
146^.9595
1564.4302
MOLE FRACTION
0.064861178
0.935138822
LBS/HR
3253.1533
135553.375
138806.500
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
246.0000
40.0000
18.7851
0.0
88.73
DEG F {
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.02343661
0.97656357
118.8889 DEG. C)
TONS/HR
1.6266
67.7767
69.4032
-------
STREAM NUMBER 75 VAPOR FROM 1400-V-l STILL TO 1400-E-2 INTERCHANGER
COMPONENT NO.
8 SOLVENT
TOTALS
MOI.ES/HR
2194.4392
2194.4392
MOLE FRACTION
1.00000000
TEMPEKATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
203330.125
203330.125
250.0000
40.0000
54.4101
1.0000
92.66
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
121.1111 DEG. C)
TONS/HR
101.6651
101.6651
00
CO
STREAM NUMBER 76
CONDENSATE FROM 1400-E-2 INTERCHANGER TO 14QO-E-3 CONDENSER
COMPONENT NO.
8 SOLVENT
TOTALS
MOLES/HR
2194.4392
2194.4392
MOLE FRACTION
1.00000000
LBS/HR
203330.125
203330.125
WGT FRACTION
1.00000000
TONS/HR
101.6651
101.6651
TEMPERATURE 246.8251
PRESSURE 40.0000
HEAT CONTENT 46.2305
FRACTION VAPOR 0.6993
AVG. MOLECULAR WEIGHT 92.66
DEG F ( 119.3472 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
-------
STREAM NUMBER 77 50% NAOH TO 1500 V-2 SURGE-DECANTER
COMPONENT NO.
TOTALS
MOLES/HR
0.0*
MOLE FRACTION
TEMPERATURE 77.0000
PRESSURE 14.7000
HEAT CONTENT 0.0
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 0.0
LBS/HR
0.0*
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
( 25.0000 DEG. C)
TONS/HR
0.0*
STREAM NUMBER 90
STEAM TO 1400-V-l STILL JACKET
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
14.3670
14.3670
MOLE FRACTION
1.00000000
TEMPERATURE 353.0095
PRESSURE 140.0000
HEAT CONTENT 0.3089
FRACTION VAPOR 1.0000
AVG. MOLECULAR WEIGHT 18.02
LBS/HR
258.8264
258.8264
WGT FRACTION
1.00000000
DEG F
PSIA.
MMBTU/HR.
LBS/MOLE
( 178.3386 DEG. C)
TONS/HR
0.1294
0.1294
'QUANTITY NOT DETERMINABLE
-------
STREAM NUMBER 91 CONDENSATE FROM 1400-V-l STILL JACKET
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
14.3670
14.3670
MOLE FRACTION
1.00000000
TEMPEKATURE 353.0000
PRESSURE 140.0000
HEAT CONTENT 0.0841
FRAC1ION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02
LBS/HR
258.8264
258.8264
WGT FRACTION
1.00000000
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
( 178.3333 DEG. C)
TONS/HR
0.1294
0.1294
STREAM NUMBER 92 STEAM TO 1400-E-l REBOILER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
1673.9421
1673.9421
MOLE FRACTION
1.00000000
LBS/HR
30156.6250
30156.6250
WGT FRACTION
1.00000000
TONS/HR
15.0783
15.0783
TEMPERATURE 353.0095 DEG F
PRESSURE 140.0000 PSIA.
HEAT CONTENT 35.9861 MMBTU/HR
FRACIION VAPOR 1.0000
AVG. MOLECULAR WEIGHT 18.02 LBS/MOLE
( 178.3386 DEG. C)
00
-------
STREAM NUMBER 93
CONDENSATE FROM 1400-E-l REBQILER
COMPONENT NO.
7 H20
TOTALS
COMPONENT NO.
7 H20
TOTALS
MOI.ES/HR
1673.9421
1673.9421
MOLE FRACTION
1.00000000
LBS/HR
30156.6250
30156.6250
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. .MOLECULAR
353.0000
140.0000
9.7974
0.0
WEIGHT 18.02
STREAM NUMBER 94 STEAM TO
MOLES/HR
2446.2734
2446.2734
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACT ION VAPOR
AVG. MOLECULAR
MOLE FRACTION
1.00000000
353.0095
140.0000
52.5895
1.0000
WEIGHT 18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
900-ME-l DRYER
LBS/HR
44070.4336
44070.4336
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
178.3333 DEG. C)
WGT FRACTION
1.00000000
178.3386 DEG. C)
TONS/HR
15.0783
15.0783
TONS/HR
22.0352
22.0352
I
4*.
00
-------
STREAM NUMBER 95 CONDENSATE FROM 900-ME-l DRYER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
2446.2734
2446.2734
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRAC1ION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
44070.4336
44070.4336
353.0000
140.0000
14.3177
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
178.3333 DEG. C)
TONS/HR
22.0352
22.0352
I
*».
00
-4
I
STREAM NUMBER 96
STEAM TO 1100-E-l HEATER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
7805.0859
7805.0859
MOLE FRACTION
1.00000000
LBS/HR
140611.187
140611.187
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACIION VAPOR
AVG. MOLECULAR WEIGHT
353.0095
140.0000
167.7923
1.0000
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
178.3386 DEG. C)
TONS/HR
70.3056
70.3056
-------
STREAM NUMBER 97
CONDENSATE FROM 1100-E-l HEATER
COMPONENT NO.
7 H20
TOTALS
MOLhrS/HR
780b.0859
7805.0859
MOLE FRACTION
1.00000000
LBS/HR
140611.187
140611.187
TEMPERATURE 353.0000 DEC F
PRESSURE 140.0000 PSIA.
HEAT (.ONTENT 45.6821 MMBTU/HR
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 18.02 LBS/MOLE
WGT FRACTION
1.00000000
( 178.3333 DEG. C)
TONS/HR
70.3056
70.3056
STREAM NUMBER 98 STEAM (125 PSI) TO TRAIN
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
11939.6680
11939.6680
MOLE FRACTION
1.00000000
LBS/HR
215097.062
215097.062
TEMPERATURE 353.0095 DEG F
PRESSURE 140.0000 PSIA.
HEAT CONTENT 256.6768 MMBTU/HR
FRACTION VAPOR 1.0000
AVG. MOLECULAR WEIGHT 18.02 LBS/MOLE
WGT FRACTION
1.00000000
{ 178.3386 DEG. C)
TONS/HR
107.5485
107.5485
00
00
-------
00
<£>
I
STREAM NUMBER 100 STEAM (400 PSI) TO 1100-ME-2 DRYER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
563.3384
563.3384
MOLE FRACTION
1.00000000
TEMPERATURE 448.2000
PRESSURE 415.0000
HEAT CONTENT 12.2232
FRACTION VAPOR i.OOOO
AVG. MOLECULAR WEIGHT 18.02
LBS/HR
10148.7266
10148.7266
DEG F
PSIA.
MMBTU/HR
L8S/MOLE
WGT FRACTION
1.00000000
( 231.2222 DEG. C)
TONS/HR
5.0744
5.0744
-------
STREAM NUMBER 101 CONDENSATE FROM 1100-ME-2 DRYER
COMPONENT NO.
7 H20
TOTALS
MOLES/HR
563.3384
563.3384
MOLE FRACTION
1.00000000
TEMPERATURE
PRESSURE
HEAT CONTENT
FRAC I ION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
10148.7266
10148.7266
448.2000
415.0000
4.3473
0.0
18.02
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
1.00000000
231.2222 DEG. C)
TONS/HR
5.0744
5.0744
STREAM NUMBER 105
FROM STREAM #5 TO STREAM #7
COMPONENT NO.
MOLES/HR
1
2
3
4
5
6
7
COAL
FES2
SULFUR
FES04
FE2(S04)3
H2S04
H20
TOTALS
1198^.1016
80.3128
10.3369
191.7173
60. 1591
91 .8341
1813H.6016
30555.0547
MOLE FRACTION
0.392147899
0.002628463
0.000338305
0.006274488
0.001968877
0.003005530
0.593636632
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACI1UN VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
155767.312
9635.9336
331.4014
29122.4375
24055.3594
9007.0898
326772.937
554692.312
215.6000
154.7000
70.3084
0.0
18.15
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.28081745
0.01737167
0.00059745
0.05250197
0.04336703
0.01623799
0.58910662
102.0000 DEG. C)
TONS/HR
77.8837
4.8180
0.1657
14.5612
12.0277
4.5035
163.3865
277.3462
I
*.
-------
STREAM NUMBER
COMPONENT NO.
4 FES04
5 FE2(S04)3
7 H20
TOTALS
MOLES/HR
0.8344
1.5776
2102.7405
2104.8901
SULFATES FROM STREAM #40 TO 100-V-l MIXED
(CHECK STREAM #14)
MOLE FRACTION
0.000396430
0.000749495
0.998978674
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
LBS/HR
126.7544
630.8245
37881.5742
38639.1523
77.0000
35.0000
0.0
0.0
18.36
DEG F (
PSIA.
MMBTU/HR
LBS/WOLE
WGT FRACTION
0.00328047
0.01632604
0.98039347
25.0000 DEG. C)
TONS/HR
0.0634
0.3154
18.9408
19.3196
STREAM NUMBER 118 FROM STREAM #123 TO 1100-V-2 RESLURRY TANK
IPO
1
4
5
6
7
NENT NO.
COAL
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0004
1.1111
2.2566
2.7656
63.2039
69.3376
MOLE FRACTION
0.000005632
0.016024720
0.032545440
0.039886154
0.911538184
LBS/HR
0.0051
168.7818
902.3376
271.2510
1138.6384
2481.0139
to
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.0000
14.7000
0.2583
0.0
35.78
OEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000205
0.06802934
0.36369711
0.10933065
0.45894074
101.6666 DEG. C)
TONS/HR
0.0000
0.0844
0.4512
0.1356
0.5693
1.2405
-------
STREAM NUMBER 119 WATER FROM 1100-P-3-ASB TO 1100-V-2 RESLURRY TANK
COMPONENT NO.
6 H2S04
7 H20
TOTALS
MOLES/HR
I.1654
316U.2808
3161.4460
MOLE FRACTION
0.000368626
0.999631405
LBS/HR
114.3017
56933.5156
57047.8164
WGT FRACTION
0.00200361
0.99799639
TONS/HR
0.0572
28.4668
28.5239
I
i^
<0
CO
TEMPERATURE 212.0132
PRESSURE 54.7000
HEAT CONTENT 10.2624
FRACTION VAPOR 0.0
AVG. 'MOLECULAR WEIGHT 18.04
DEG F
PSIA.
MMBTU/HR
LBS/MOLE
( 100.0073 DEG. C)
STREAM NUMBER 120
SULFATES FROM 1100-E-l HEATER TO 1100-V-l CONCENTRATOR
IPO
1
2
4
5
6
7
NENT NO.
COAL
FES2
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0391
0.0002
80/.0110
251 .6638
350.4695
8487.6172
9891.7969
MOLE FRACTION
0.000003949
0.000000015
0.081078351
0.025441665
0.035430312
0.858045995
LBS/HR
0.5078
0.0183
121827.812
100630.812
34374.0469
152907.250
409740.375
WGT FRACTION
0.00000124
0.00000004
0.29732925
0.24559647
0.08389223
0.37318081
TEMPERATURE 307.7864
PRESSURE 35.0000
HEAT CONTENT 173.9696
FRACTION VAPOR 0.7347
AVG. MOLECULAR WEIGHT 41.42
•DEG F ( 153.2146 DEG. C)
PSIA.
MMBTU/HR
LBS/MOLE
TONS/HR
0.0003
0.0000
,9139
.3154
1870
.4536
60.
50,
17.
76,
204.8702
-------
STREAM NUMBER 121
SULFATES FROM 1100-E-2 COOLER TO 1100-F-2 FILTER
IPO
1
2
4
5
6
7
NENT NO.
COAL
FES2
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0039
0.0000
80.2011
25.1664
35.0470
848.7617
989. 1799
MOLE FRACTION
0.000003949
0.000000015
0.081078351
0.025441661
0.035430323
0.858045816
LBS/HR
0.0508
0.0018
12182.7891
10063.0781
3437.4065
15290.7266
40974.0508
WGT FRACTION
0.00000124
0.00000004
0.29732937
0.24559635
0.08389223
0.37318069
TONS/HR
0.0000
0.0000
6.0914
5.0315
1.7187
7.6454
20.4870
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.0000
14.7000
3.6563
0.0
41.42
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
101.6666 DEG. C)
STREAM NUMBER 122 SULFATES WASTE FROM 1100-F-2 TO LINE #22
COMPONENT NO.
4 FES04
5 FE2(S04)3
6 H2S04
7 H2C)
TOTALS
MOLES/HR
69.0858
^.5919
7.3806
216.4882
295.5464
MOLE FRACTION
0.233756244
0.008769732
0.024972729
0.732501626
TEMPERATURE 215.0000
PRESSURE 14.7000
HEAT CONTENT 1.0719
FRACTION VAPOR 0.0
AVG. MOLECULAR WEIGHT 54.66
. LBS/HR
10494.3437
1036.3877'
723.8892
3900.1077
16154.7227
WGT FRACTION
0.64961457
0.06415385
0.04480975
0.24142212
DEG F ( 101.6666 DEG. C)
PSIA.
MMBTU/HR
L8S/MOLE
TONS/HR
5.2472
0.5182
0.3619
1.9501
8.0774
CO
-------
STREAM NUMBER 123
FILTRATE FROM 1100-F-2 TO STREAMS #24 AND #118
PO
1
2
4
5
6
7
NENT NO.
COAL
FES2
FES04
FE2(S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0039
0.0000
11.1153
2^.5745
2 f .6664
63->.2734
693.6335
MOLE FRACTION
0.000005632
0.000000022
0.016024712
0.032545295
0.039886139
0.911538124
LBS/HR
0.0508
0.0018
1688.4443
9026.6875
2713.5171
11390.6172
24819.3164
WGT FRACTION
0.00000205
0.00000007
0.06802940
0.36369604
0.10933083
0.45894158
TONS/HR
0.0000
0.0000
0.8442
4.5133
1.3568
5.6953
12.4097
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACTION VAPOR
AVG. MOLECULAR WEIGHT
215.0000
14.7000
2.5845
0.0
35.78
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
101.6666 DEG. C)
STREAM NUMBER 124 SULFATES WASTE FROM 1100-ME-2 DRYER TO STREAM #22
IPO
1
2
4
5
6
7
NENT NO.
COAL
FES2
FES04
FE2!S04)3
H2S04
H20
TOTALS
MOLES/HR
0.0035
0.0000
10.0042
2U.3179
24.6298
181.9324
236.8879
MOLE FRACTION
0.000014841
0.000000058
0.042231631
0.085770011
0.103972197
0.768010259
LBS/HR
0.0457
0.0016
1519.6626
8124.3516
"2415.6868
3277.5725
15337.3125
TEMPERATURE
PRESSURE
HEAT CONTENT
FRACIIUN VAPOR
AVG. MOLECULAR WEIGHT
353.0200
250.0000
1.8702
0.0
64.75
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.00000298
0.00000011
0.09908271
0.52971154
0.15750390
0.21369922
178.3444 DEG. C)
TONS/HR
0.0000
0.0000
0.7598
4.0622
1.2078
1.6388
7.6687
-------
.STREAM NUMBER 145 DUMMY STREAM (INTERNAL IN 800-F-1A-D)
COMPONENT NO.
1
2
3
4
5
6
7
8
COAL
FES2
SULFUR
FES04
FF2(S04)3
H2S04
H20
SOLVENT
TOTALS
MOl frS/HR
17461 .5234
6.5900
•5.2941
0.9474
L .8918
t .8079
252«.8494
76.3254
20083.2187
TEMPERATURE
PRESSURE
HEAT CONTENT
FRAC(ION VAPOR
AVG. MOLECULAR
MOLE FRACTION
0.869458377
0.000328134
0.000263609
0.000047171
0.000094196
0.000090020
0. 125918508
0.003800458
173.5540
14.7000
15.9829
0.0
WEIGHT 14.03
LBS/HR
226999.750
790.6675
169.7298
143.9057
756.4441
177.3180
45558.0664
7072.0859
281667.812
DEG F (
PSIA.
MMBTU/HR
LBS/MOLE
WGT FRACTION
0.80591297
0.00280709
0.00060259
0.00051091
0.00268559
0.00062953
0. 16174394
0.02510789
78.6411 DEG. C)
TONS/HR
113.4999
0.3953
0.0849
0.0720
0.3782
0.0887
22.7790
3.5360
140.8339
I
CD
T
HEAT LOSSES FROM FILTRATION UNITS IN MM BTU/HR
400-F-l =
600-F-l =
800-F-l =
0.2178
0.1840
0.1440
-------
THE QUANTITIES AND CONDITIONS OF STREAMS 201 to 212 ARE NOT DETERMINABLE AT
PRESENT.
STREAM NUMBER 201 VENT FROM 500-V-l TO 1500-V-l SCRUBBER
STREAM NUMBER 202 VENT FROM 600-V-l TO 1500-V-l SCRUBBER
STREAM NUMBER 203 VENT FROM 700-V-l TO 1500-V-l SCRUBBER
STREAM NUMBER 204 VENT FROM 800-V-l TO 1500-V-l SCRUBBER
STREAM NUMBER 205 VENT FROM 900-V-l TO 1500-V-l SCRUBBER
STREAM NUMBER 206 VENT FROM 1400-V-2 TO 1500-V-l SCRUBBER
STREAM NUMBER 207 VENT FROM 1400-T-l TO 1500-V-l SCRUBBER
CO
STREAM NUMBER 208 VENT FROM 1400-T-2 TO 1500-V-l SCRUBBER
-------
I
*t
CD
^
I
STREAM NUMBER 209 VENT FROM 1400-T-3 TO 1500-V-l SCRUBBER
STREAM NUMBER 210 VENT FROM 1400-T-4 TO 1500-V-l SCRUBBER
STREAM NUMBER 211 VENT FROM 1100-V-2 TO 1500-V-l SCRUBBER
STREAM NUMBER 212 VENT FROM 1100-E-5 TO 1500-V-l SCRUBBER
-------
10.5.3
Calculation of Sulfur Forms in the Product Coal
Utilizing the detail from the foregoing section and the
sulfur forms analyses from Table 2 in Section 4.1.1, the
residual sulfur in the product coal, Stream #53/ may be
calculated as follows:
Basis: One hour of operation for one train (tons/hr column
in Section 10.5.2, Stream #53).
Total weight less moisture,
(118.6806 - 4.5559 = 114.1247 or 114.1 T
Initially present in feed coal
(Stream #1 & Table 2):
Organic sulfur,
(113.5 + 8.15) x 0.0067
Sulfate sulfur,
(113.5 + 8.15) x 0.0004
Sulfur forms present,
T %
0.8150
0.0487
0.714
0.043
Residual compounds in product coal
(Stream #53):
Iron pyrites,
0.3953 x (2 x 32.1/119.8)
Elemental sulfur,
0.0312
Ferrous sulfate,
0.0265 x 32.1/151.9
Ferric sulfate,
0.1393 x (3 x 32.1/399.9)
Sulfuric acid,
0.0326 x'(32.1/98.1)
Subtotal from feed or reactions
Added as binder during compaction:
Lignin sulfonate,
1.71 x 0.05
0.2118
0.0312
0.0056
0.0335
0.0107
0.185
0.027
0.005
0.029
0.009
1.1565
0.0855
TOTAL, based on Stream #53, dry 1.2420
1.012
0.075
1.087
-498-
-------
Note that 0.67% organic sulfur in the feed coal containing
6.7% FeS2 becomes 0.714% in the product coal because the
denominator in the fraction, S/coal, has been reduced by
the amount of FeS2 converted less other residual compounds
remaining. Similarly, when 95% of the initial 6.7%
is removed the residual FeS- is more than 0.05 x 6.7 or
0.335%. Excluding other residuals it would be,
0.05 x 6.7 x TOO 0.335 X 100 n -jc^oa
- = - = U.jD/0%.
100 -(0.95 x 6.7) 93.635
-499-
-------
10.6 CAPITAL COSTS
-501-
-------
10.6.1 Capital Cost Estimate Summary
Table 26. Summary of Capit a 1 Cost s by Sector
SECTOR
000 Coal Handling & Preparation
100 Mixing
200 Reaction
400 Filtration
500 Extraction
600 Filtration/Decantation
700 Water Washing
800 Filtration/Decantation
900 Drying, Decantation, Compacting
1000 Product Coal Handling
1100 Iron Sulfates Removal
1400 Distillation
1500 Vent Scrubbing
1900 Building & Miscellaneous
SUB-TOTAL PROCESSING
2000 Utilities
3000 Site Development & General
SUB-TOTAL
Allowances (10%)
TOTAL
M$ (1975)
8,800.0
1,044.5
23,960.1
6,906.1
1,010.1
7,338.2
1,126.3
8,630.6
6,984.9
3,770.0
13,891.3
4,931.7
642.0
10,864.3
99,900.1
28,251.8
4,503.9
132,655.8
13,344.2
146,000.0
PROBABILITY-- 80%
Maximum (+22%) $180,000.OM
Minimum (-18%) $120,000.OM
-502-
-------
10.6.2 Capital Cost Estimate Details
The following detail sheets substantiate the sector totals
on the capital cost estimate summary. Costs for the vari-
ous items were estimated by one or more of the following
methods:
1. Unit operations data, proprietary information
of Dow.
2. Vendor quotations.
3. Popper, H., Ed., "Modern Cost-Engineering
Techniques," McGraw-Hill, New York,•1970 * .
4. Factors and/or allowances for installation and
indirect costs.
-5O3-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SECTION NUMBER 1 NAME
OOO
SECTOR NUMfcCft 4 NAME
FACTOR!
BASE X ESC. X CAPACITY
XQUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= M$(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
5s fi
Ool
f
Goo.! £-e.c.Js.\
' *?O00.O
031
re
'ft 4* P»+S
ool <*ar Pamptr
A//
,
tfo
00 to
S'SZ.O
a// /rt
on
/00.O
/v'-re
72) /
row Jwso PKINTCO IN u.sjt OKI
-5O4-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
SECTION NUMBER 4 NAME
/CO- M
SECTOR NUMBER 1 NAME
FACTORS
BASE X ESC. X CAPACITY X QUANT. X [MATERIAL + CONDITION + COMPLEXITY]
= MJ{19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
jao-
/oo-
eal
/.o
Lot
. £3
MS
ram iNM rrnMTEo w U.J.A. ni-«>
-5O5-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e oow CHEMICAL COHPAHY
MIDLAND. MICHIGAN
, ..DON MUUBEX 1 NAMC
/CO-
FACTOR:
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
=MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
Z&Z.3
7&Z 2+
I MM rMHTTO IN UAA. HKI
-506-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DO* CHEMICAL COMPANY
MIDLAND. MICHIGAN
•MAS!
oX7e~
EF NUMBER
SECTION NUMBER » NAME
T/
SECTOR NUMBER * NAME
FACTOR
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONSTRUCTION
MATERIAL
CONDITION + COMPLEXITY]
= MJ(W
ITEM
NAME OF FACILITY
QUANT.
DESCRIPTION
Feed
..S88
(7.25} x
Z-/
A-K
/
ft 3* 4.
sit,
\,0 y
£-/
row JNM nmTEO w OAA. RMI
/.£>
MS
-5O7-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
5
SOLFOZ
Wo ^3
tCCTION NUMBER » NAUC
SECTOR NUIMEII A NAME
FACTOR!
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
. 6
I MM PRKTU III U4JC 01-tl
-5O8-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPAHY
MIDLAND, MICHIGAN
£.
4ECTION NUMBE* 1 NAUt
- P/L
SECTOR NUMBED » NAME
FACTORS
BASE X ESC. X CAPACITY
x QUANT, x MATERIAL + CONDITION + COMPLEXITY]
M$(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
4*
F-t
4-D
/2V22
m
4
V
'4
juef-e. far 4-)
n
&
4.
'rje./ i
Lcto
4-
* O
y / b~ 2 - 6 5, z
'± V
no £ ~" f-'j ^
10 «•* 3-3 ,
Z • °
£/eci-ricaf / 7 ^'
£> d> 1
ME-
<£>0f-/-
J -
Zo
n.i
"7
'on
j / <8
503?.**
£,.!
FOM JNM POINTEO M U.J.A. Hi-el
•5O9-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
65?
SECTION NUMBER * NAME
£00-
c ri
SECTOR NUMBER A NAME
FACTOR
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
I/-/
1"
f/.te-t/.f
'.0
$e>4.
'.?£. 7$
Bo
fy a
_T/7
rOlM »•» miNTEO IN OAA, RKI
16/0, 1
-51O-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
4ECTION NUMBER 4 NAME
- Fi L
- I*
SECTOR NUMBER & NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
&£>£>>-
I.71Z
/. o
A-D
II 2.0
4.2Q. 0
104-i-e-
* * * *
Sie&l
J723.4-
772^4..-
rr>
4-
4-
nne.
(fSof-/'n£,/ ./
4}
Sc r e-t^ Con
4--- S
no < ft
ram 3NM raiHTco IN UAA. KI-M
/- O i 's*r/?
& -/
77/
-511-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAMD. MICHIGAN
. F
2-2t,-74-
ft CTIOM NUMKE* t NAMt
SECTOR NUMBER & HAMC
P ACTOR!
BASE x ESC. x CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(1S
mn
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
X77.5
r-t
/.O
/).
&OG-
P-I
/£>, 0 y /,
( ft Tr* in 3
35*1
7238,2.
19MM rmNTCO M U.tA. «I-M
-512-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
1035
*
JT
SECTION NUMBER 1 NAME
SECTOR NUMBER 1 NAME
c*
FACTORS
BASE X ESC. X CAPACITY
XQUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(«
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
700
v-t
Wafer Wash
3
71-7
J^ns i~ru ft) e^ fa ft 01
1 TV
""
ram MM miNTeo m UAA. RI-M
-513-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE oow CHEMICAL COMPANY
MIDLAND. MICHIGAN
//
OF
SuLf=U£
7^23
SECTION NUMBER i NAME
&GO • F/LT/SA T'W-
SECTOR NUMBER A NAME
FACTOR!
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
/£"<=? .e^
. 0 V //
4- / ^ - /3
/•o
52-2-
&&>
F-J
Quot
/ / 2 »
t s 23
/142,0
~tt~r8
S/**/
. 7
Z.067, 7
s
4*
S
Qup/c •&/- 4)
**
& retry)
&
'.4-
/• //?<:/ /'
* )
Boo-
J
4- i
PCm 996W flllNTCO III U4.A. RKI
lsc />
15.0
/ /
-514-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPAMY
MIDLAND. MICHIGAN
HlAlf
. F
DAlT
NGN NUUBE* 4 NAME
&00 • Ft L
FACTORS
BASE X ESC. X CAPACITY
X QUANT.
X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
/ Center- //?/ en
JA tie
o
Su.t>Te** 10 Train]
1 AY
-515-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
SECTION NUMBER I NAME
SECTOH NUMBER 4 NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= M$(19
ITEM
NAME OF FACILITY
OUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
2>7<1-O
/
MS
DCS
A/
'*/
-4-
1,0
POM IMU PRINTED III UJ.A. RUt
-516-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DO. CHEMICAL COMPANY
MIDLAND. MICHIGAN
0,
35
JT
TION NIWBER 4 NAME
SECTOR NUMBER & NAME
TJ
r ACTORS
BASE X ESC. X CAPACITY
XQUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19 )
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
300.
4-
Draco
ZZ7-0
127-0
S
/£"+&
be,
*3
/-
t'n /ei c/w-te.
T-l
gttitfer 2/f ft 01
.z
300-
2
1,778
ram auo fnwrtu m u A*. RMI
- 517-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
TION NUMBER 4 NAME
SECTOR NUMBER & NAME
FACTORS
BASE X ESC, X CAPACITY
X QUANT. X [MATERIAL
COKDITION + COMPLEXITY]
= MJ(l9
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
v-t
'-2"
A
A/)
i8jn.8_
Bolt. I
o ramreo m UJLA, nut
-518-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™E °°» CHEMICAL COMPANY
MIDLAND, MICHIGAN
JOBNUMBER
X"
SECTION NUMBER * NAME .
SECTOR NUMBER I NAME
FACTORS
BASE X ESC. X CAPACITY X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
ICG I
(Leaf
PMC
/Oft
r
PI' re Prt>
From Meet
/OOO
/Z,570
377^
POM SM90 PRINTED IN O.tX MK*
-519-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
X*
tECTION NUMBER I NAME
SE.CTOK NUMBED 1 H«1E
FACTORS
BASE X ESC. X CAPACITY
XQUANT. [MATERIAL +
CONDITION + COMPLEXITY]
= M$(19 )
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
fi-t
A46
'O If 3.Z
cJr
50,
-7
y acuu
2
^
™
7f • 7
3*9.2-
60/- 5
j-hra t~* Fluffs
Drum
4
Z.
z
X-2.
//#?•
/^-/
Heofirefit
/.O j
POW MM PRINTED IK UAA. Bl-41
-52O-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e oo» CHEMICAL COMPANY
MIDLAND. MICHIGAN
FACTOR!
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
P'/
/??*
/.o
/.
i
' ''•>'<-/ fits rp.fi
T-Z.
> O
/.a
//#&•
/?,
Jlron
Ao
1-7.0
fOill MM PffiNTCO IN UJJl KI-CI
-521-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
T/C
JT
£.
657
..TION HUHIER 4 NAME
//oO-
» ACTOR*
SECTOR NUMIER 4 NOME
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
.SQ5
f
l.o
/
"
4.3
ZA'/g
/IOC-
304.
tST.G
1100-
7
Sfae/
TTP-&Z
- 4.
1.0
I MM ntlNTCO IN OAA. «l-tl
-522-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
/f75
/•o
£00 /&r*
£-2.
/.o
. 3
5# me.
$00.7
row 3HW niNTco m
-523-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e oo» CHEMICAL COMPANY
MIDLAND. MICHIGAN
..TION NUUIE* t HAKE
IIQO-
SECTOR NUMBER » HAKE
FACTOR
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= M$(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
3£>4>
8 ft
M£-Z
.£>
X n
fn+4-b'ir>
Pcsr&h
'* 8
375^ ^
KM! MM ritMTEO M UAA. Rt-U
-524-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e °°» CHEMICAL COMPANY
MIDLAND, MICHIGAN
353^25
X
2-2(0-74-
«_wTION NUMBER 1 NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL V
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
3 A £
p-l
/.o -
IMG-
F-t
Ft'/ -
B&4-
ft/fie. - • /GO
1.0
/.o
301
/be
/JG
2-3
2./3J
Woo-
1 6 7- /" Y 11 f A. x 2£> ' /o r*=?
'
to
t;
10
c?
S
1.0
i MM mnitTeo "• U.LA. m-4i
-525-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
.- TION HUU1ER » NAME
D/S T/LL/l T/0tf
SECTOR NUMSEII A NAUE
f ACTOR
BASE X ESC. X CAPACITY
X QUANT.
X [MATERIAL
CONDITION + COMPLEXITY]
= MJ{19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
moo-
y,/
'Sac-Lei- £'
/.o
IWO-
1.0
(/, 0+0,3
M
Xr&o
/.o
*A
/&.
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
.--TION NUMBER * NAME
T/LL/}
SECTOR NUMBER 1 NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= M$(l3
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
Selvznf
A5
$e It/c h
feed
Duc+ife.
1,0
ho
1700
'.(.j-o.l)
c, a
r
-------
PRELIMINARY CAPITAL - DETAIL SHEET
DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
ttCTION NU»«E» I NAME
ICCTOV NUMACR * NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
M$(!9
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
Tourer
S-feef
20 '- / " 5 t~
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
,TION NUMftER 4 NAME
I5OO-
SECTOR NUMBER 4 NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
-ZV?5:/TV/
rc r> a $
/ .< I f/ fa > ft )
TOM «uo ncnTto IH U4JL RMI
-529-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
2?
OF
77
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
JOB NUMBER
Task 2.
. /=;
DATE
£57
SECTION NUMBER 1 NAME
SECTOR NUMBER «• NAME
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= HJ(19 )
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
60' */&>' 1 5'
/"Z.
/
FORM 1%!0 PRINTED IN U.S.*. Rl-69
-531-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE D°» CHEMICAL COMPANY
MIDLAND. MICHIGAN
T j
COAL-
JOBNUMBER
730
2-
4ECTION NUMBER t NAME
2000 • OT/L./ T/ £^5
SECTOR NUMBER I N4UE
FACTOR!
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MS(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
2-160
to
3 7,
5-0
) X /,SW/*/. 1.
US,
P'T
F&C./ /I'TJ'*
P/etr?
fCKW MUD PftinrEO III UJJk. «!•«>
-532-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
TN« DO. CHEMICAL COMPANY
MIDLAND, MICHIGAN
JOB NUMBER
..iTION NUU6ES » NAME
2 000 - OT/L./ T/ &S
FACTORS
BASE X ESC. X CAPACITY
X QUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19 )
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
2-162.
get /
tS.o.
&;£> Co
"
2)r>
121.4-
£> /??
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™e °°* CHEMICAL COMPANY
MIDLAND. MICHIGAN
OF
35
657
• ..CTIOH NUMBER 4 NAME
2 000 -
TV
SECTOR NUMBER * NAME
MCTOR:
BASE X ESC. X CAPACITY X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
. s .
^ />-?
2. £"
C£>
fyfa Meufi -Pre m
w
th
d&nir
/ V $;
y / JTV ^ / /. 3
• MM ntmTU M UAX HI-M
-534-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE BOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
31*35
JOOHUMBtO
750
OTION NUMBER 1 NAME
SECTO* NUMBER 4 NAME
MCTORi
BASE X ESC. X CAPACITY
xQUANT, x [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
OUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
^ en//// '
00
/ o u h
0*1
• nmrco M DJJ. «i«
-535-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
™E BOW CHEMICAL COMPANY
MIDLAND, MICHIGAN
..TIOM NUMBER A NAME
20(00 -
MCTOR:
BASE X ESC. X CAPACITY
XQUANT. X [MATERIAL
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
OUAHT
CONSTRUCTION
MATERIAL
DESCRIPTION
t
"f-
c.
rr>
MS* J/fi InJ
on Vo
/Zo.a
S
3
Tf
-
Crusher^ S 1 1 a
ar Dt/n*~pir>ij £0 ^
re
/- 3
t MM ntwreo M UAA. «i-«
-536-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE DOW CHEMICAL COMPANY
MIDLAND. MICHIGAN
35
•SECTION NUMBER A NAME
7~
FACTORS
BASE X ESC. X CAPACITY X QUANT. X [MATERIAL +
CONDITION + COMPLEXITY]
= MJ(19
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
2..O
A3 * /f/S
&.0
3/
zee./-
r
I.I
>r
VSY
3,
' 70 /7f
en
POmi WiO PRINTEO IN U.S.A. «!•<(
-537-
-------
PRELIMINARY CAPITAL - DETAIL SHEET
THE °°» CHEMICAL COMPANY
MIDLAND. MICHIGAN
T^Z - '
7^23
»£.'« NUMBER * NAME
$000* S/
SECTOR NUMBER A NAME
FACTORS
BASE X ESC. X CAPACITY
XQUANT. x [MATERIAL
CONDITION + COMPLEXITY]
= MJU9
ITEM
NAME OF FACILITY
QUANT.
CONSTRUCTION
MATERIAL
DESCRIPTION
S
/S38.4-
A?
"
' IS fas'* V*
•*- rft
m# / '/•)
row MU nmrco IN UJLA. RUI
-538-
-------
10.7 ECONOMICS
-539-
-------
10.7.1. Manpower Requirements
Table 27. JOB LISTINGS BY DEPARTMENT,
SECTION AND JOB TITLE OR FUNCTION
(Secondary function in parentheses)
Administration
Plant Manager 1
Admin. Assistant (Ecology) 1
Senior Secretary (Public Relations) 1
Supervisor, Accounting and Purchasing 1
Senior Accountant (Office Manager) 1
f
Accountants 2
Purchasing Agents 2
Secretaries (Receptionists) 3
Traffic Manager 1
Traffic Ass't, Rail Equipment Supervisor 2
Teletype Operator, Secretary (Plant Phone) 2
Industrial Relations Manager 1
Labor Relations, Employment 2
Safety Engineer, Security Officer (Fire Chief) 1
Plant Guards, 3/shift (Indus. Hygiene, Firemen) jj:
TOTAL, Administration 33
The following job listings were developed by Process Engi-
neering and extended after consultation with N. W. Miller,
Dow Michigan Division Plant Engineering, Chlor-Alkali Section,
and H. E. Chinworth, Dow Plant, Ludington, Michigan.
-54O-
-------
Production
Production Manager and Secretary 2
Maintenance, Service and Development Engineers 4
Coal Receiving and Unloading, day shift 2
Coal Crushing and Pulverizing, 3/shift 12
Coal Loading, Misc. Handling, Yard Work 4
Process Superintendents I/train 4
Production Engineers (Dev.) I/train 4
Process Foremen I/train 4
Clerks, Janitors 2/train 8
Operating Personnel 184
(Example duties are given in the next table.)
No. per shift No. for
Job per train 4 trains
Foremen 1 16
Control Operators 1 16
Reactor Operators 2 32
Filter Operators 2 32
Dryer Operators 2 32
Extractor Operators 2 32
Waste Sulfate Operators 1 16
Spare Operators 8
TOTAL, Production 228
Services
Engineering
Plant Engineer and Secretary 2
Engineers—Process, Mechanical, Civil,
Electrical/Instrument 6
Project Engineers (Development) 4
Draftsmen 4
-541-
-------
Quality Control
Director and Secretary 2
Chemists and Chemical Engineers 4
Laboratory Technicians 16
Utilities
Utilities Manager and Office Ass't 2
Superintendents and Assistants for Steam
Plant, Oxygen Plant, Water Supply and
Treatment, Cooling Towers, Waste Control 6
Power Specialist, Maintenance Foreman,
Shift Supervisors 6
Operating Personnel 4/shift, Spare, Janitor 18
Service Section
Garage Supt., Warehouse Supt., Foreman 3
Mechanics, Drivers, Equipment Operators 10
Clerks 3
Laborers, Janitors 12
TOTAL, Services 98
TOTAL, Administration, Production, Serv. 359
Maintenance
Maintenance Manager and Office Assistant 2
Supervisors and Engineers 5
Scheduling and Stock Clerks (Orderers) 5
Foremen and Crew Leaders 8
Journeymen and Helpers, Other Maintenance 150
Instrument Men 20
Oilers 10
Plant Mechanics 8
Electricians 12
Pipe Fitters and Coverers, Plumbers 10
-542-
-------
Machinists, Bench Repairmen 6
Welders, Boilermakers, Tinsmiths 18
Millwrights, Riggers 17
Masons 6
Carpenters 8
Painters, Sandblast Men 12
Road and Yard Crew 16
Track Maintenance 7
TOTAL, Maintenance 170
TOTAL, All Departments 529
-543-
-------
Table 28. EXAMPLE DUTIES OF PRODUCTION OPERATING PERSONNEL
For each, train and on each shift there are a number of
duties for which someone must be available and responsible.
Examples of these are given below, following a listing of
the major equipment items in a given operator's area of
(27)
responsibility . The;
Personnel from Table 27.
(27)
responsibility . These are for the 184 Operating
Foreman I/shift
a. Supervise and schedule operating personnel.
b. Be responsible for safety, quality,
production, maintenance, and housekeeping.
c. Write operating instructions and train personnel.
d. Schedule and conduct safety meetings. Write and
maintain safety procedures and check lists.
e. Transmit information to operating employees and
to supervision.
f. Schedule maintenance, communicate problems and
maintain a log of maintenance details.
g. Request and oversee ordering of materials
and supplies.
Control Operator I/shift
a. Monitor all indicating charts, meters,
indicators, and lights on the master control
panel.
b. Communicate control needs and conditions, and
maintenance needs to foreman and operators as
necessary. Direct operators.
c. Maintain log
d. Communicate with coal crushing and pulverizing
crew, coal loading crew, and services personnel.
Anticipate and initiate changes in control levels,
and coordinate start-ups, changes, and shut-downs
relating to these non-process personnel as well
as changes occurring within the process train.
-544-
-------
Reactor Operators 2/shift
Equipment
100 ME-1 Bucket Elevator
100 V-l Mixer
Agitator
Pump
Absorber
200 R-l A-K Reactors
200 E-l Cooler
Duties
a. Start elevator, mixer, pump
b. Switch to spare pump
c. Valve in absorber, reactors, cooler
d. Prepare equipment for maintenance
e. Shut down equipment for load variations
f. Start up equipment for load variations
g. Check operation, make field readings
h. Take samples
i. Adjust packing, tighten leaks
j. Report to Control Operator
k. Coordinate with Filter Operator
1. Coordinate side stream of coal and iron sulfate to
and from iron sulfate removal step
m. Clean area
-545-
-------
Filter Operators
Equipment
400 F-1A-D
Vacuum pumps
Receivers
Pumps
400 ME-1
600 P-l
600 F-1A-D
Vacuum pumps
Receivers
Pumps
600 ME-1
800 F-1A-D
Vacuum pumps
Receivers
Pumps
800 ME-1
800 V-l & 800 P-2
2/shift
Drum Filters
Conveyor
Pump
Drum Filters
Conveyor
Drum Filters
Conveyor
Filtrate Decanter & Pump
Duties
a. Start up filters, vac. pumps, pumps, reslurry tank
b. Shut down filters, vac. pumps, pumps, reslurry tank
c. Switch to spare pump
d. Prepare equipment for maintenance
e. Check equipment
f. Take field readings
g. Get samples
h. Coordinate with other operators
i. Wash filters
j. Clean area
k. Unplug lines
-546-
-------
Dryer Operators 2/shift
Equipment
900 ME-1A, IB Dryers
Fans
Ducts
Coolers
900 ME-2A, 2B Conveyors
900 ME-3 Conveyor
900 ME-4 Compactor
900 T-l Binder Tank
900 P-l, P-2 Pumps
900 ME-5 Elevator
Duties
a. Start up dryer
b. Shut down dryer
c. Prepare equipment for maintenance
d. Switch pumps
e. Check equipment
f. Take samples
g. Coordinate with other operators
h. Start up & shut down compactor
i. Attention to equipment operation
j. Take field readings
k. Clean area
-547-
-------
Extractor Operators
2/shift
Equipment
500 V-l & A-l
700 V-l
Pumps
Decanters
Extractor with Agitator
Water Wash Tank w/Agitator
1400 T-l, P-l Evaporator Feed Tank and Pump
1400 F-l Filter
1400 V-l Distillation column
1400 E-l, E-2, E-3 Reboiler, Interchanger, Condenser
1400 V-2
1400 E-4
1400 T-2f T-4
Pumps
Accumulator
Cooler
Solvent Surge and Storage
1500 V-l, V-2
1500 E-l
Scrubber and Decanter
Cooler
Pumps
Tracing System (Dowtherm®* SR-1)
Duties
a.
b.
c.
d.
e.
f.
Operate, shut down, start up, check equipment
Take field readings, get samples
Switch pumps, prepare equipment for maintenance
Attention to operation
Coordinate with other operators
Clean area
Make periodic inspections of sulfur storage tank
1400 T-3 and loading pump 1400 P-4. Prime
responsibility for these will be with truck
driver who hauls sulfur.
^Trademark of The Dow Chemical Company.
-548-
-------
Waste Sulfate Operators I/shift
Equipment
1100 T-2 Sulfuric Acid Storage Tank
1100 F-l Filter
1100 V-2 Slurry Tank w/Agitator
1100 V-l Evaporator
1100 E-l Reboiler
Pumps
Cooler, Condenser
Water Heater
1100 T-l Water Surge Tank
1100 F-2 Filter
1100 ME-2 Sulfate Waste Dryer
Duties
a. Operate, start up, & shut down equipment
b. Prepare equipment for maintenance
c. Take samples, get field readings
d. Clean area
e. Monitor storage and loading of solid waste into
trucks (Waste hauling truck driver will load
truck.)
-549-
-------
10.7.2 Computer Printout for Economics Program
-551-
-------
INPUT DATA
UEEP 11 PYRITIC SULFUR FROM COAL, (S04) 1302 PENN.,W. VA.
NEKERVIS TON 50
1. BASE CASEt 95X SULFUR REMOVED FROM ALL OF THE COAL
2, COAL FEED RATE IS 122 TONS/MR, PRODUCT: 104.8(PER TRAIN, DRY)
3. SEE CHAPTER 5, FINAL REPORT FOR OTHER ASSUMPTIONS AND BASES
CLEANED COAL, IX S 28.00 24
14 l,«jlj701RCOAL- RECVG
0.0801RASH/COAL LOSS
1 .0481ROXYGEN
-1 -0.1401RNITRCGEN
301200. 00101RCHEM AGT.CWT
5 0.01601RH2SQ4
-7 -.015 1RSULFUR
5 0.00121RNAPHTHA
38 27.02LMAMAGEMENT
80 68.02LTECHNICAL
58 253.02LOPERATING
90 11. 2LCLERICAL
4.004MMAINTENANCE
120 0.7501UWATER.M GAL
120 54.0Q1UPOWER,AC KWH
3 .0901UFUEL COAL
0.15 1XREFUSE.TONS
0.3401RBINDER.CWT
0 OOVERHEAD
003ERESEARCH
2703GG 6 A
2503TM £ S
7.05CCASH 6 ACC.
2.04IINS. £ TAXES
0003SSELLING
13900 311
4900 4 11
22200 411
9000 31 1
95900 311
100 5 1 1
000 3 1 1
.00 33
8.80
.0001
0.70
50.0
36.0
12.0
45.0
0.2
0.009
.010
4.50
5.00
0
0
0
0
1
1
0
0
1
1
.00 3300.0 11 3
8.80
.0001
.0001
0.70
50.0
36.0
12.00
45.00
32000
23000
17000
12000
0.0 «1.0
.011
.012
.0001
5.00
5.05
.02 1.00.3300 00.3333
0000 1.00
0 1.00 1.00
0 1.0 000
20
25
20
20
10
51
15
01
02
04
6
8
25
40
41
42
43
45
46
47
48
49
50
51
52
53
54
55
56
58
60
70
71
72
73
74
75
77
89
90
91
92
93
94
95
-552-
-------
INPUT DATA
B 11 0 0 PYfUTIC SULFUR FROM COAL,(S04» 1302 PENN..W. VA. I
8 30 74 NEKERVIS TON 0000000000 50.0 ECONOMIC EVALUATION 2
1. BASE CASE, 95% SULFUR REMOVED FROM ALL OF THE COAL 4
2. COAL FEED RATE IS 122 TONS/HR, PRODUCT: 104.3(PER TRAIN, DRY) 6
3. SEE CHAPTER 5, FINAL REPORT FOR OTHER ASSUMPTIONS AND BASES 8
OCLEANED COAL, U S28. 00024.
0
0
0
0 -
3100 1
0100 0
1100 0
1100-0
0 30120 0
0
5100 0
0 -7100-0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
13900
4900
22200
9000
95900
100
0
5100 0
0 88
0 80
.1701RCOAL RECVG
.0301RASH/COAL LOSS
.0481ROXYGEN
.1401RNITROG6N
.0011RCHEM AGT,CWT
.0161RH2S04
.0151RSULFUR
.0011RNAPHTHA
27.02LMANAGEMENT
68.02LTECHNICAL
00033.000
8.
0.
0.
0.
50.
36.
12.
45.
0 58 253.02LOPERATING
0 90
0 0
0120 0
012054
3100 0
0100 0
0100 0
0 0
0 0
11.02LCLERICAL
4.004MMAINTENANCE
.7501UWATER.M GAL
.0001UPOWER.AC KWH
.OgOlUFUEL COAL
.1501XREFUSE,TONS
.3401RBINDER,CWT
0.0 400VERHEAD
0.0 3ERESEARCH
0 0270.003GG £ A
0 0250.003TM £ S
0 0
0 0
0 0
3 1
4 1
4 1
3 1
3 1
5 1
3 1
0 48.0 0
0
0 0
7.005CCASH £ ACC.
2.004IINS. £ TAXES
0.0 3SSELLING
1 11 09
1 12 0 20
1 12 0 20
1 11 09
1 11 09
1 11 09
1 11 09
.0 0 0 14
0.0 7LLABOR ASSESS.
0.
0.
0.
0.
4.
5.
0.
0.
0.
0.
0.
0.
800
001
0
700
000
000
000
000
0
0
0
0
200
009
010
0
500
000
200
200
0
0
0
0
0.200
12
0.
0
1
1
0
0
1
1
200
0.0
0.0
0.0
0.0
0.0
0.0
0.0
3300
8.800
0.000
0.000
0.700
50.000
36.000
12.000
0.0 45.000
0
0
0
0
0.0
0.0
0.0
0.0
0.0
0.0
0.087
0.086
0.020
0.0
0.0
0.0
0.026
0
0
0
0
0
0
0
0 20
0.0
32000
23000
17000
12000
1.000
0.011
0.012
0.000
5.000
5.000
1.000
1.000
1.000
0.0
0.0
1.000
1.000
18 20
18 25
18 20
18 20
18 10
18 51
18 15
1
1.000
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1
1
0
0
0
0
0
0
1
.0
.0
.0
.0
.0
.0
.0
.0
0
0
0
0
.0
.0
.0
.0
.0
.0
.217
.200
.330
.0
.0
.0
.367
11
.0
1 0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0
0
0
0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
1.000
0.0
0.0
0
0
0
0
0
0
0
0
0.0
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.
1.
0.
1.
1.
0.
0.
9
0.
3 25
0 040
0 041
0 042
0 043
0 045
0 046
0 047
0 048
0 049
0 050
0 051
0 052
0 053
0 054
0 055
0 056
0 058
0 060
2171470
2001471
333 072
000 073.
000 074
0 075
3671477
089
090
091
092
093
094
095
1 99
0 076
-553-
-------
THE DOW CHEMICAL COMPANY PAGE:
BASES
AREA: u.s. DEPARTMENT: ECONOMIC EVALUATION
PROJECT NO.: 1302 EVALUATOR: NEKERVIS
LOCATION: PENN..W. VA. DATE: 8/30/74
PYRITIC SULFUR FROM COALf(S04)
1. BASE CAStf 95X SULFUR REMOVED FROM ALL OF THE COAL
2. COAL FEED RATE IS 122 TONS/HR, PRODUCT: 104.8(PER TRAINtORY)
3. SEE CHAPTER 5, FINAL REPORT FOR OTHER ASSUMPTIONS AND BASES
PYRITIC SULFUR FROM COAL,(S04) 8/30/74
-554-
-------
THE DOW CHEMICAL COMPANY
ECONOMIC PROFILE
PAGE:
AREA: U.S.
PROJECT NO.: 1302 DEPARTMENT: ECONOMIC EVALUATION
LOCATION: PENN..W. VA. EVALUATOR: NEKERVIS
CAPACITY: 3300 M TON/YR DATE: 8/30/74
PYRITIC SULFUR FROM COAL,(S04)
PRODUCTS
M TON/YR s/TON
BY-PRODUCTS M TON/YR S/TON
3300 28.0000
3300 28.0000
NONE
CLEANED COAL
TOTAL PROD.
BASES:
1. BASE CASE, 95X SULFUR REMOVED FROM ALL OF THE COAL
0 0.0
2. COAL FEED RATE IS 122 TONS/HR, PRODUCT: 104.8(PER TRAIN,DRY)
3. SEE CHAPTER 5, FINAL REPORT FOR OTHER ASSUMPTIONS AND BASES
COST ESTIMATE CAPITAL ESTIMATE
U.R. U.COST s/TON MS/YR MsFIXED MS WORK TOTAL S/U./YR
COAL RECVG U170
ASH/COAL LOS0.080
OXYGEN 0.048
OTHER R.M.
TOTAL R.M.
LABOR
MAINTENANCE
UTILITIES
DEPR. & OFC
TAXES & MISC
R.M. INV.
IN-PROC. INV
TOTAL BULK
TOTAL PLANT
G AND A
CASH £ ACC.
INV FOR SALE
TOTAL FOR SALE
8.800010.2960
0.0001 0.0000
0.0001 0.0000
2.1020
12.3980
2.0791
1.7697
0.6563
3.6494
1.6348
0.0
0.0
22.1872
22.1872
0.0818
0.0
0.0
22.2690
33977
0
0
6937
40913
6861
5840
2166
12043
5395
0
0
73218
73218
270
0
0
73488
0
0
0
0
0
0
0
0
146000
0
0
0
146000
146000
89
0
0
146089
PROFIT SUMMARY AT CAPACITY
NET SALES
COST FOR SALE
PROFIT BT
PROFIT AT 348X,
DEPREC. TOTAL
MS/YR
92400
73488
18912
9834
12048
S/TON
28.0000
22.2690
5.7310
2.9801
3i6510
PCT ROI
PCT ROS
TURNOVER
PROFIT RATIOS
B/T A/T
12.3 6.4
20.5 10.6
0.601
p
c
T
R
0
I
B
T
0
0
0
0
0
0
0
0
0146000
250 250
334 334
140 140
723146723
723146723
1 90
6468 6468
503 503
7695153784
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
44.2424
0.0758
0.1011
0.0424
44.4616
44.4616
0.0273
1.9600
0.1524
46.6012
NET SALES s/TON
PYRITIC SULFUR FROM COAL,(S04)
-555-
8/30/74
-------
THE DOW CHEMICAL COMPANY
PLANT AND TOTAL COST ESTIMATE
PAGE:
AREA: U.S.
PROJECT NO.: 1302 DEPARTMENT: ECONOMIC EVALUATION
LOCATION: PENN..W. VA. EVALUATOR: NEKERVIS
CAPACITY: 3300 M TON/YR DATE: 8/30/74
PYRITIC SULFUR FROM COAL,(S04)
RAW MATERIALS
COAL RECVG 1
ASH/COAL LOS 0
OXYGEN 0
NITROGEN -0
CHEM AGT,CWT 0
H2S04 0
SULFUR -0
NAPHTHA 0
BINDER, CWT 0
TOTAL RAW
MANAGEMENT
TECHNICAL
OPERATING
CLERICAL
MAINTENANCE
WATER, M GAL 0
POWER, AC KWH54
FUEL COAL 0
INS. G TAXES
REFUSE, TONS 0
DEPRECIATION
TOTAL BULK
G £ A
TOTAL COST
UNIT
RATIO
.1700
.0800
.0480
.1400
.0010
.0160
.0150
.0012
.3400
M UNITS
PER
YEAR
3861 8
264 0
158 0
-462 0
350
5336
-5012
445
1122 5
MATERIALS
.7500
.0000 1
.0900
.1500
COST
2475 0
78200 0
297 0
495 5
FOR SALE
COST
PER
UNIT
.800010
.0001 0
.0001 0
.7000-0
.0000 0
.0000 0
.0000-0
.0000 0
.0000 1
12
0
0
0
0
0
.0110 o
.0120 0
.0001 0
0
.0000 0
0
13
0
13
COST
V CASH
.29600
.00001
.0
.09800
.04000
.57600
.18000
.05400
.70000
.38808
.0
.0
.0
.0
.35394
.00540
.43200
.0
.0
.67500
.0
.85441
.0
.85441
F
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.
0.
1.
0.
0.
0.
0.
0.
0.
4.
0.
4.
PER
CASH
0
00000
0
01000
0
0
0
0
00993
26182
47394
30333
04000
41576
002.85
21600
00001
88485
07500
0
68348
08018
76366
TON
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3
3
0
3
DEPR.
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
,64938
10.
0.
0.
-0.
0.
0.
-0.
0.
1.
12.
0.
0.
1.
0.
1.
0.
0.
0.
0.
0.
3.
.6493822.
.00164
0.
.6510122.
TOTAL
29600
00001
00000
09800
05000
57600
18000
05400
70000
39801
26182
47394
30333
04000
76970
00825
64800
00001
88485
75000
64938
18726
08182
26907
TOTAL
MS/YR
33977
0
0
-323
165
1901
-594
178
5610
40913
864
1564
4301
132
5840
27
2138
0
2920
2475
12043
73218
270
73488
PYRITIC SULFUR FROM COAL,(S04)
8/30/74
-556-
-------
THE oow CHEMICAL COMPANY PAGE: <
CAPITAL SUMMARY
AREA: U.S.
PROJECT NO.: 1302 DEPARTMENT: ECONOMIC EVALUATION
LOCATION: PFNN..W. VA. EVALUATOR: NEKERVIS
CAPACITY: 3300 M TON/YR DATE: 8/30/74
PYRITIC SULFUR FROM COAL,(S04)
UNIT S/UNIT UNIT CAPITAL S/TON/YR M * CAPITAL
RATIO PER YR FIXED V.WORK F.WORK TOTAL FIXED TOTAL
EQUIPMENT 35.99998 35.99998 118800 118800
BUILDING 8.21212 8.21212 27100 27100
LAND 0.03030 0.03030 100 100
TOTAL DFC 44.24239 44.24239 146000 146000
M £, S 0.0 0.0 0.07576 0.07576 0 250
R.M. INV. 0.0 0.0 0.10108 0.10108 0 334
IN-PROC. INV 0.0 0.0 0.04238 0.04238 0 140
TOTAL BULK MFG 44.24239 0.0 0.2192244.46159 146000 146723
INV FOR SALE 0.0 0.0 0.15237 0.15237 0 503
G t A 0.02700 0.0 0.00.027 0.02727 89 90
CASH & ACC. 0.0 1.96000 0.0 1.96000 0 6468
TOTAL CAPITAL FOR SALE44.26938 1.96000 0.3718646.60121 146089 153784
PYRITIC SULFUR FROM COAt,(S04) 8/30/74
-557-
-------
THE DOW CHEMICAL COMPANY
PROFIT CALCULATIONS
PAGE:
AREA: U.S.
PROJECT NO.: 1302 DEPARTMENT: ECONOMIC EVALUATION
LOCATION: PENN.IW. VA. EVALUATOR: NEKERVIS
CAPACITY: 3300 M TON/YR DATE: 8/30/74
PYRITIC SULFUR FROM COAL,(S04)
M TON/YR
MAIN PRODUCT 3300
TOTAL SALES 3300
COST FOR SALE
PROFIT BEFORE TAXES
PROFIT AFTER TAXES
WORKING CAPITAL
TOTAL CAPITAL
PRICE 1
S/TON MS/YR
28.0000 92400
28.0000 92400
22.2691 73488
5.7309 13912
2.9801 9834
2.3319 7695
46.6012153784
PRICE 2
S/TON MS/YR
PRICE 3
S/TON MS/YR
24.0000
24.0000
22.2691
1.7309
0.9001
2.0519
46.3212.
79200
79200
73488
5712
2970
6771
152860
33.0000
33.0000
22.2691
10.7309
5.5801
2.6819
46.9512
108900
108900
73488
35412
18414
8850
154939
PROFIT RATIOS AT CAPACITY
PERCENT ROTCBT
PERCENT ROTCAT
PERCENT ROTSBT
PERCENT ROTSAT
TURNOVER
SENSITIVITY
PCT ROTCBT
PCT ROTCAT
3 50X CAPACITY
a 50% CAPACITY
PCT ROTCBT 3120X DFC
PCT ROTCBT 3 SOX DFC
12.3
6.4
20.5
10.6
0.601
-2.9
-1.5
8.1
18.5
3.7
1.9
7.2
3.8
0.518
-7.3
-3.8
0.9
8.0
22.9
11.9
32.5
16.9
0.703
2.5
1.3
17.0
31.5
SALES INCOME a PRICE 1
2
3
BREAKEVEN DATA
PRICES,S/TON
PRODUCT BY-PROD
28.0000 0.0
24.0000 0.0
33.0000 0.0
THOUSANDS OF s
350X CAP. aiOOXCAP.
46200
39600
54450
92400
79200
108900
TOTAL COST/YR.+ 10X ROI 26.9292 0.0
* 20X ROI 31.5893 0.0
*. 30X ROI 36.2495 0.0
VARIABLE COST/YEAR - TOTAL
TOTAL COST/YEAR (EXCLUDING DEPRECIATION)
TOTAL COST/YEAR (INCLUDING DEPRECIATION)
66007
81385
96763
22860
38580
50628
88866
104245
119623
45720
61440
73488
UNIT COST £ CAPITAL SUITABLE FOR CASH FLOW INPUT
VARIABLE COST 13.85441
DEPRECIATION 3.65101
TOTAL CST(LESS EXP. CONST) 22.26906
FIXED ALLOC. CAPITAL
VAR. WORKING/TON/YR
VAR. WORKING - XREV
FIXED WORKING
PYRITIC SULFUR FROM COAL,(S04)
-558-
0.02700
0.0
6.99999
0.37186
8/30/74
-------
10.7.3 Chemical Leaching Added to an Existing Coal
Preparation Plant ^ '
One interesting alternative is the incorporation of chemical
leaching in conjunction with inorganic sulfur and ash re-
moval by conventional coal washing equipment. This write-
up describes how such conventional coal preparation might
be used and provides a hypothetical basis from which an
optimized assembly of processes can be structured.
A number of coal companies produce a primary product of low
ash and low sulfur values in their preparation plants. The
premium product may be sold as metallurgical grade coal, or
it may be blended with other grades for various uses. The
heavier fraction is reprocessed, using a higher specific
gravity for the separation and giving a lower quality prod-
uct, but one that can be used in some areas or recombined
with primary product for use as a steam coal.
A block flowsheet is given in Figure 53, showing in general
terms primary and secondary washing where just the best 20%
of the float coal and the worst 7% of refuse are separated,
while the bulk of the coal, as middlings, is forwarded to the
chemical leaching process for upgrading. The TPH figures
are representative only. The proportions would vary in
accordance with the particular coal, the equipment used,
the desired product specifications, and the economics. The
coal leaving the leach process has the initial pyritic sul-
fur content reduced by 90 to 95% as needed to meet product
specifications.- This is blended with the previously sepa-
rated float coal for a greater overall yield than could be
obtained by washing alone.
-559-
-------
FIGURE 53
COAL PREPARATION AS AN ADJUNCT
TO PYRITIC SULFUR REMOVAL BY LEACHING
R.O.M. Coal
Coarse Preparation:
Picking Table
Scalping Grid
Breaker
Screens
Heavy 1
and Sii
Succesi
Washini
Crushii
Screen
Rock and
2.4 Sink
Refuse
•<
Fraction
ak -
sive
?,
ig,
Ing:
<—
1 ^
1-1/2" x
1
3/8" x 0
\
3/8"
a
Primary Preparatic
Washing, Crushing,
Screening -v-
Light, Float
f Fraction -
Successive
Washing,
Crushing,
Screening:
— »•
I ^S
<1.25 sp.gr.
Dewatered
Float Coal
3/8" x
14 m «.
.90 Sink
Refuse
14 m
x 0-"i
Refuse:
Coal Fines,
Iron Sulfate,
Sulfur
*Boxed figures are
tons per hour
(TPH) moisture-
free coal.
Secondary Preparation:
3/8"xl4 mesh
Washing, Grinding,
Screening.
14 mesh x 100 mesh
Washing, Pulverizing,
Dewatering (Optional
Flotation)
100 m x 0-
Leach Process:
Leaching, Extract-
ing, Washing,
Dewatering, Drying
Fuel Coal
sp.gr.
Dewatered
Fine Float
Coal^t-
or Process Steam
•Dewa tered and/or
Dried Low Pyrite
Compacted or
Loose Coal
Blended Low Sulfur
Coal to Storage,
Utilization or
Shipping
-56O-
-------
The coarse preparation includes a picking table and
scalper grizzlies on 8-inch centers to remove large pieces
of rock or large pieces of coal which are broken with a
sledge hammer and then added to the bulk of the coal being
conveyed to coarse screens and a breaker. This would
ordinarily be done at mine mouth.
The coarse screens make a three-way split: Undersize,
below 3/8 in., is advanced to the secondary preparation.
Oversize is crushed to 1 1/2 in. topsize, and this is combined
with the 1 1/2 in. x 3/8 in. midscreen fraction and is
conveyed to the primary preparation step.
In the primary preparation a light fraction, e.g. <1.25
specific gravity, is separated. Some product is withdrawn
from this, and the remaining float material is ground and
moved to the light end of the secondary preparation circuit.
A very heavy sink fraction, e.g. >2.4 specific gravity,
is removed and discarded and the somewhat lighter fraction
of this high density material is ground and fed to the
heavy end of the secondary preparation.
Data are given in Table 29 and Figure 54 for Lower
Kittanning coal float-sink tests. The specific gravities
and sizes discussed here are taken from these data. These
parameters are adjusted to fit the data for the coal being
handled.
The equipment in the primary preparation section is
assembled from an assortment of jigs, cones and cyclones
and is operated with water, a heavy liquid, or a suspen-
sion to produce the desired light skimming and discharge
of stone for the relatively coarse material.
-561-
-------
,(2)
I
£
to
TABLE 29
FLOAT AND SINK ANALYSIS, DRY BASIS'
(LOWER KITTANNING COAL. DATA BELOW 1.30 SP. GR. ARE EXTRAPOLATED)
CUMULATIVE FLOAT RECOVERY
Specific
1 1/2" x
1OO m
3/8"
x
1OO m 14 m x 0
Gravity % % % % ' % %
Sink
_ _
1.22
1.25
1.27
1.30
1.40
1.6O
l.SO
Float
1.22
1.25
1.27
1.30
1.4O
1.6O
1.9O
—
Wt. %
171
30
4O
59.5
86.8
92.7
94.4
100. O
Ash
4.2
4. 5
4.8
5.14
6.98
8.45
8.96
12.14
Pyr.
S
O.76
O.8O
O.85
O.91
1.63
1.77
1.87
2.72
FRACTION
Total
S
1
1
1
1
2
2
2
3
.56
.60
.65
.78
.42
. 55
.63
.46
Wt.
8
202
30
57.
85.
91.
94.
100.
% Ash
4
O
9
2
0
3.
3.
4.
4.
8.
9.
9.
12.
5
8
O
60
38
35
72
50
ANALYSIS
Spec i± ic To
Gravity
Sink
1.22
1.25
1.27
1.30
1.4O
1.60
1.9O
Float
1.22
1.25
1.27
1.30
1.4O
1.6O
1.90
Approximate %
Size Consist
1 1/2'
3/8"
14m x
14m x
IT It
M 11
M fT
TI rT
'xlOOm
x 14m
lOOm
0
T!
ft
ft
ft
Wt. %
7
13
6
16.3
34.9
12.3
4.1
6.4
Ash
4.5
3.8
3.2
3.6
7.82
19.48
38.19
64.13
Pyr
S
0.
O.
0.
0.
1.
2.
3.
21.
Total
76
70
64
50
44
97
91
64
S
1.
1.
1.
1.
2.
3.
4.
21.
56
31
30
26
15
42
20
91
Pyr. Total % Pyr. Total
S S Wt. % Ash S S
O.69 1.30 0 3.O O.35 1.O5
O.7O 1.31 1O 3.0 O.36 1.08
0.74 1.35 2O3 3.2 0.4O 1.12
O.89 1.46 42.3 3.62 O. 5O 1.26
1.55 2.14 77.2 5.52 O.92 1.66
1.69 2.27 89.5 7.44 1.21 1.9O
1.76 2.34 93.6 8.78 1.32 2.0O
2.71 3.27 1OO.O4 12.33 2.62 3.28
Rough estimate of coal preparation,
based on 680 TPH:
1 Separate 7% (50 TPH) for fuel coal.
Forward remainder to light end of (2)
2Assume 13% after the above 7% is
gone. Separate 6% (40 TPH). For-
ward 7% to light end of next grind.
3Assume about 7% left <1.27 after
9O TPH are removed. Separate 6%
(4O TPH)
4Assume 7% is discarded. This could
be reprocessed by the Bureau of
Mines two-stage froth flotation
method and the coal fraction for-
warded to the leach step.
-------
Figure 54
Float and Sink Analysis Plot, Dry Basis
(Data for <1.30 sp.gr. are extrapolated)
Lower Kittanning Coal
Fox Mine, Clarion County, Pennsylvania
EPA Report 650/2-74-025(2)
1.0 2.0
% Total Sulfur
4.0
-563-
-------
The secondary preparation also uses cones, cyclones, and
heavy media on the smaller sized material. Additionally,
concentrating tables are used to good advantage on the plus
28 mesh fine coal and froth flotation on the under 28 mesh
fines. A complete study is needed to determine proper equip-
ment to fae installed for coals in a given region. A typical
arrangement of circuits involves crushing, screening and
skimming. Part of the undersize from each crushing is
advanced to the next circuit and part of the lightest and
heaviest material is removed for blending (in the case of
float coal) or discard (heavy), while the remainder of the
light ends and heavy ends receives additional processing.
The bulk of the crushed material at each step moves to the
next size reduction. Some of the relatively dry, coarse
float coal with just above 1.25 specific gravity is pulver-
ized in this section and added to the dewatered coal to
increase the average dryness.
The washed, pulverized middlings from the secondary prep-
aration could be fed to the mixing tank for processing
through the leach system. Meeting fuel coal needs from the
float coal would increase the usable product from the proc-
ess. The leach process product could be blended in with
the remaining float coal to increase the overall plant
output. Where a utility is located adjacent to the prep-
aration plant, waste heat or steam and cooling tower service
could be obtained from the power generating facility.
The leach plant could also share with the preparation plant
or utility and possibly not be debited for the following:
site preparation; general administrative, shops, warehouse,
service and yard facilities; coal handling facilities and
-564-
-------
personnel. The leached, dewatered product could be blended
with the ground dewatered, float coal, and the installation
could be adapted such that no further drying nor compaction
was required. Existing storage silos and conveyors could
be used.
-565-
-------
10.7.4 Calculations For Alternative Cases in Chapter 6
The base capital cost was taken from the stated sheet in
Section 10.6.2 or other table or section listed. The cost
or equivalent value of the base facilities is given and the
method or reasoning used to determine the revised cost or
allocation is given. This is used to estimate the approxi-
mate reduction that was chosen for the example. Cost units
are $M and $M/yr.
Case 2 CH
Capital Reduction, $M
Process Capital,
Receiving(a) and Preparation(b) 3,000
Sheet 1, 8800 x 2°'7/2 = 7172 — the approximate
value of the Base Case size facilities in a
plant twice this size. Allocate '70% to the
desulfurization process, 7172 x 0.7 = 5020,
8800-5020 = 3780
Drying(b) 2,600
Sheets 13 & 15, first 2 dryers & decanters = 1412
Eliminate 4 of the next 6, 3812 x 4/6 = 2554.
Some drying facilities already exist. Plus other
economies because product is not shipped.
Compaction(a,d) 1,200
Eliminate compactor, use smaller tank and
pumps. Sheet 14, (476-135) x 6985/1888 = 1262
Product Coal Handling(b) 1,700
Sheet 16, 3770. n qKeep about 50% of the equip-
ment 3770 x (0.5) *y = 3770 x 0.535 = 2017,
3770-2017 = 1753
Other Capital,
Site, Building, General(c) 2,800
Table 20, 3882. Allocate 25% of existing
site and building to desulfurization
3882 (1-0.25) = 2912
-566-
-------
Utilities(b)
Less steam, lower unit capital 1,700
Table 20, 2730. Steam use is about half and
is supplied from the large utility boilers.
2730 x (1.0-(0.5x0.7)) = 1774
Allowances, 4% of reductions 500
Total Fixed Capital Reduction 13,500
Ratio to Base Case Coal Handling 0.47
Table 20, 28,702. 13,500/28,702 = 0.47
Working Capital, $M
Cash and Accounts Receivable(a,d) 6,000
Section 5.1.1.2, 6470. There are no accounts
receivable for the treated coal so reduce by
95% or about 6147.
Coal Inventories(d) 600
Section 5.1.1.2 & Table 17B. Product
inventory = 500, coal portion of raw material (RM)
inventory = ca 1500. Product inventory is not for
sale so value is lessened by 500 (25-8.80)/25 = 324.
RM inventory is shared with utility, subtract
another 276 for 600.
Other Materials and Supplies(b) 100
Section 5.1.1.2, 250. Assume this is shared
with the large utility at a 40% capital savings.
Total Working Capital Reduction 6,700
-567-
-------
Operating Costs Reduction, $M/yr
Capital Related,
Labor (a,b,c):
Base
Case
Case
1 CH
Decrease in No.
of Men x $/yr\
1,200
Administration
Production
12
8 x 20 = 160
Managers
Foremen, leaders
Labor, Spares
Labor, Rec'g & ship
Labor, Dry & Compact
Services
Eng'g, PD, QC
Util. & 0-
Other
TOTAL Men
Labor, $M
G&A, $M
TOTAL, $M
3
4
2
18
32
5
3
6
85
1655
54
1709
Use exist-
ing sup'vn
0
0
16
2
2
1
25
485
24
509
3
4.
36
3
1
5
60
x
X
X
X
X
X
30
22
.18
24
22
18
90
88
= 648
72
22
= 90
1170
3£
1200
Other Capital Related
Table 20, Capital Related Costs less labor and
G&A,, 5153-1709 = 3444. Reduce by fraction
of capital reduction: (3444) x (0.47) = 1619
1,620
Unit Ratio Based,
Binder(d)
Table 20, 5610/3300 = $1.70/T. Section 4.4.2.4
& Case 4. Stabilization could cost from 5$ to
50C/short ton. Use 43.5C.
3300 (1.70-0.435) = 4175
Other Unit Ratioed; Services and
fuel coal equivalent (c)
Table 20, 1067. Charge 70% for services and
utilities, 1067 (1.0-0.7) = 320
4,170
320
Total Operating Costs Reduction
Effect on Coal Handling Region
7310 r 3300 = 2.215
7,310
-$2.22/T
Alternative Unit Cost
Base Case Coal Handling
Less Reductions
Case 2 CH, Coal Handling
-568-
3.59
-2.22
$ 1.37/T
-------
Case 2 CP
The capital and operating cost reductions for the Chemical
Processing steps are somewhat speculative but illustrate the
impact of reductions of a given magnitude. The case descrip-
tion is given in Section 6.2.2. The base case values are
totalled from the Chemical Processing regions of Table 20
and the fraction to be eliminated is described in Section 6.2.2,
Capital Reduction, $M
Process Capital,
Leaching 15,000
31,911 x 0.5 = 15,956
Extraction, Sector 1400 2,500
4,932 x 0.5 = 2,466
Waste Sulfates 6,500
13,891 x 0.5 = 6,946
Subtotal, Process 24,000
Other Capital,
Site, Buildings, General 3,400
11,486 x 0.30 = 3,446
Utilities
Waste Sulfates 4,490
8,981 x 0.5 = 4,490
Remainder x 0.3 2,520
8,410 x 0.3 = 2,522
-569-
-------
Allowances
Above Process and Other Capital 2,750
Reductions x 0.08
34,410 x 0.08 = 2,753
Subtotal-, Other 13,160
Total Fixed Capital Reductions 37,160
Ratio to Base Case Chemical Processing 0.32
Table 20, 117,298. 37,160/117,298 = 0.317
Operating Costs Reduction, $M/yr
Capital Related,
Labor and G&A 1,360
5446 x 0.25 = 1,362
Other Capital Related 5,550
17,359 x 0.32 = 5,555
Unit Ratio Based, 1,550
Utilities, Waste Disposal, Coal
Equivalent to Fuel & Ash Loss, Less
Reduced Sulfur Credit
6,212 x 0.3 - (594/2) = 1,567
TOTAL, Operating Cost Reduction 8,460
Effect on Chemical Processing Regions -$2.56/T
8460 r 3300 = 2.564
Alternative Unit Cost
Base Case Chemical Processing $9.88/T
Less Reductions -'2.56
Case 2 CP, Chemical Processing $7.32/T
(This is further reduced in Section 6.2.2 due
to increased product tonnage when fuel coal
requirements are met otherwise).
-570-
-------
Case 3 CP
Discussion — This case illustrates a method of assessing
the value of being able to apply chemical desulfurization to
middlings coal from a gravity separation process. With
chemical desulfurization, a hypothetical 680 TPH preparation
plant could be operated as in Figure 53, Section 10.7.3 to
obtain high quality float coal with sequential grinding and
separating yielding 500 TPH of middlings to the chemical
process. Without chemical desulfurization, the tendency would
be to grind the coal more fine to maximize the float coal and
minimize the refuse and poor middlings quality that would have
to be discarded because they could not meet present fuel
source performance standards for air quality in the vicinity
of the coal combustion plant.
The disposition of the coal is given below for 680 TPH, 7920
hr/yr operation for two such cases:
Sp. Gr. Control <1.27 Float <1.35 Float
Coal size consist 1-1/2" x 28 mesh Thru 14 mesh
Pyritic/Total S, % 0.7/1.4 0.7/1.4
R.O.M. Coal
Float Coal
Middlings
Refuse, >1.9 sp. gr.
An estimate of costs for coal receiving and complete
preparation is summarized here. Further details follow the
discussion.
%
100
19
74
7
M TPY
5386
1030
3960
396
%
100
63
30
7
M TPY
5386
3374
1616
396
-571-
-------
Preparation Plant Capital, $M
Receiving, Handling, Pulverizing 11,000
Primary and Secondary Washing 5,000
Other—Site, Bldgs., Util., etc. 4,000
20,000
Operating Costs, $M/yr
Preparation Plant
Labor and G&A 600
Other capital related 3,600
Utilities etc. 1,000
Subtotal, Preparation 5,200
Disposal ($0.40/T)
High ash refuse 160
Middlings, <1.35 sp. gr. case 640
Subtotal, Disposal 800
TOTAL Operating Costs 6,000
Unit operating cost
assigned to 3374M TPY of
float coal, $/T 1.78
A meaningful estimate of the value of reprocessing the
middlings in a chemical desulfurization plant would require
a much more exhaustive study of plant data and- economics for
a well defined preparation plant, various alternative methods
of operating a complete facility, waste disposal methods and
accounting practices for a particular organization. The
following assumptions and calculations indicate the impact of
one interpretation of the value to the Chemical Processing
plant.
a. Existing Plant, Costs
1) Preparation plant and high ash residue disposal
costs spread to the float coal:
(5200 + 160) ? 3374 = $1.60/T
-572-
-------
b. Chemical Processing, Credits
1) Credit from existing plant for
avoiding cost of middlings disposal: 640
2) Middlings are available to Chemical
Processing at nil cost thus saving
the raw material cost of $8.80/T
8.80 x 1616 = $14,220 M/yr 14,220
TOTAL Operating Cost Reduction 14,860
Effect on Chemical Processing Regions -$4.50/T
14860 f 3300 = 4.50
Refuse disposal might cost less. The comparable coal
value is indeterminate — alternative R.O.M. coal
grades would have a lower value but receiving and grind-
ing costs would need to be added. Tax and accounting
practices would need to be considered. Use a conservative
credit of $2.00/T.
Case 2 CP, Chemical Processing $6.85/T
Less the above credits -2.00
Case 3 CP, Chemical Processing $4.85/T
Calculations — The costs related to the existing coal
handling facilities were approximated. Units are generally
$M for capital, $M/yr for costs and $/T for unit costs.
Example costs expended to separate float coal;
a. Scale-up Factor
Base Case, 121.65 TPH/train x 4 x 24 x 330 = 3854M TPY
This Case, 680 TPH x 7920 hrs/yr = 5385M TPY
680 TPH is 5385/3854 = 1.4 x Base Case
-573-
-------
Capital (excluding drying, compacting & shipping)
Process 11,000
Table 13, Sector 000, 8800.
8800 x (1.4)0'7 = 11,100
Other 4,000
Table 20, Coal Handling Total less Process
28,702 - 19,555 = 9,147
Proportion for Sector 000
9147 x 8800/19555 = 4116
Preparation 5,000
Section 10.7.3. The initial reference* '
gave an approximation of <5000. '
TOTAL 20,000
Operating Costs
Labor and G&A 600
Case 2 CH, 1,200. Proportioned for Sector 000
1200 x 8800/19555 = 540
Other Capital Related 3,600
Table 13, Coal Handling, 0.18
20,000 x 0.18 = 3,600
Utilities 1,000
Table 13, utilities, 727. Increase for
preparation plant power, coal stabilization;
to 1000.
Subtotal Preparation 5,200
Disposal 800
Table 17B, Steam plant ash disposal $1.50/T.
Disposal of inert residue could cost up to
$1.50/T; however, $0.40/T was used.
Refuse 396 x 0.40 = 158
Middlings 1616 x 0.40 = 646
804
TOTAL Operating Costs 6,000
-574-
-------
Case 3 U
The case described in 3 CP is approached from the standpoint
of the coal cost for the entire complex. The increasing
costs accompanying improved coal quality are shown.
a. Purchased coal, 3.3% total S
5386M TPY x $8.80/T = $47,397 M/yr
b. Add part of the preparation plant-receiving, handling,
refuse separation, grinding, half of site, building
and utility capital.
Fixed CH Capital, $M
Receiving, handling, grinding 9,000
Other — site, bldgs., util., etc. 2,000
11,000
Handling Cost, $M/yr
Coal lost as refuse
390 M TPY x $8.80/T 3,485
Refuse disposal 160
Other operating (proportioned from 3 CP)
5200 x 11/20 2,860
TOTAL Handling Costs 6,505
Unit Handling Cost, $/T 1.30
4990M TPY, 2.0% total S
c. Extend primary washing with wet grinding.
Add secondary washing & pulverizing, site,
buildings, utilities (final drying not
included).
Fixed CH Capital added, $M
Conveying, centrifuging, pulverizing 2,000
Primary and secondary washing 5,000
Other — site, bldgs., util., etc. 2,000
9,000
-575-
-------
Washing Costs added, $M/yr
5200 x 9/20 2,340
Summary of (b) and (c)
Fixed CH Capital, $M 20,000
Preparation Costs $M/yr
Coal lost, disposal 3,645
Receiving and handling 2,860
Washing and pulverizing 2,340
TOTAL Operating Cost 8,845
Unit Preparation Cost, $/T 2.62
3374M TPY, 1.4% total S
The increase from (b) cost to (c) cost might be gradual
as sulfur content is incrementally lowered. For a time
it may be possible to sell the 1.4 to 2% S middlings to
another processor. Eventually, it is assumed here, the
entire 4990M TPY would be upgraded for use on-site.
d. Install Chemical Processing, adapt preparation
plant to produce 1030M TPY float coal with
<1.3% S and feed the remaining 396OM TPY to
chemical processing to produce 3480M TPY of
-------
Summary of (a), (b), (c) and (d)
Fixed Capital, $MM
CH, drying, and transferring 25.3
CP 80.1
TOTAL Fixed Capital 105.4
Operating Costs, $MM/yr
Purchased coal 47.4
CH less value of coal lost (already
included in purchased cost) 5.4
CP 24.2
77.0
Unit Operating Cost, $/T 17.07
1030M TPY, <1.3% S
3480M TPY, <1.1% S
4510M TPY, <1.2% S
Apparent Treating Cost, $/T 8.27
Case 4 CP — Merchant Coal
No reduction in utilities, 25% reduction in all else. See
Case 4 CP, Section 6.2.2.
Capital Reduction, $M
Process Capital
See 2 CP, this section
24,000 x 0.25/0.5 12,000
Other Capital
Site, Bldgs., General. See 2 CP.
3,400 x 0.25/0.5 2,830
Utilities nil
Allowances 1,170
14,830 x 0.08
TOTAL Fixed Capital Reductions 16,000
-577-
-------
Ratio to Base Case Chemical Processing 0.14
16,000/117,298 = 0.136
Operating Costs Reduction, $M/yr
Capital Related, See 2 CP.
Labor and G&A 1,360
Other Capital Related, new ratio 4,330
5550 x 0.14/0.32
Unit Ratio Based 1,400
(6212 x 0.25) - (594 x 0.25) = 1,404
TOTAL Operating Cost Reduction 7,090
Effect on Chemical Processing Region -$2.15/T
7090 f 3300 = 2.15
Did not use the increase in product tonnage described
for 2 CP in Section 6.2.2. However the type of
credits shown in 3 CP would also be applicable here.
Alternative Unit Cost
Base Case Chemical Processing $9.88/T
Less reductions calculated above -2.15
Less Case 3 CP credits -2.00
Case 4 CP, Chemical Processing $5.73/T
-578-
-------
10.8 CONTINUOUS SIMULATION MODELING PROGRAM (CSMP)
10.8.1 CSMP Listing
This program was developed for the purpose of looking at
the process chemistry using a transient state material
balance as a basis for chemical calculations. The reaction
kinetics configurations are those presented in Section 4.2.
The CSMP program was run on an IBM 370/155 computer. CSMP
is a program package that was developed by IBM for the
simulation of continuous systems.
The minimum machine configuration for CSMP is a System/360
Model 40G CPU(2040) with Floating Point Arithmetic (#4427).
The minimum partition or region size is 102K when using
FORTRAN IV (G) Compiler and Linkage Editor Level F (88K).
One IBM 2311 Disk Storage Drive or equivalent (in addition
to the operating system residence DSPD) is required to install
CSMP, but this need not be dedicated disk storage. While not
necessary for execution, one 2400 series tape drive is
required for system installation.
The partition or region size required for execution of CSMP,
is determined by the largest of the four phases: translator,
FORTRAN IV compiler, linkage editor and execution.
-579-
-------
$$$CONTINUOUS SYSTEM MODELING PROGRAM III V1M1 TRANSLATOR OUTPUT$$$
*
* CSMP COAL CESULFUSIZAT10N TRANSIENT STATE MASS BALANCE
*
*
* INTEGER VARIABLE SPECIFICATION
*
FIXF.O If JtK, I FLAG, IN IT 1 , IMT2, KFL AG, LFLAG, NMAX
FIXED IF1.MF1
*
* MACRO PRF.CLUCES THE OCCURENCE CF NEGATIVE MOLAR QUANTITIES
* IN MIXE^ AND «EACTORS(NEGATIVE RESULTS MAY ARISE IF THE INTEGRATION
* STEP SIZE IS LARGE AMD THE DERIVATIVE IS LARGE).
Y =LIMINT( ICtYDOT, PI)
PROCEDURE OYCT=LIM(Y,YDQT,P1 )
DYCT=YDt
-------
* IN THF MIXF" AND REACTORS FCF A SPECIAL CASF
* NOT HANDLED BY THE MACRO
*
DYNAMIC
NGSUPT
FEPYR = LIMH (0.0,FEPYR,FEPYR)
H20MX=LIHMT(C.CtH2CMXtH2CfX)
FE2MX=LIMIT(C.O,FE2MX,FE2MX)
COAL=LIMIT(O.OfCCAL,COAL)
FF3MX=LIMIT(C.C,FE3MX,FE3MX)
ACXX = LIV, IT (0.0, ACVXt ACVX )
= LIf'IT(C.CtSC4NX,SC4KX)
=L IMIT(0.0,SULFMX,SLLFMX)
IF(TIMP.GT.20)F12=1AO.
IF( TIME.GT.30)F12=145.
SORT
H=3. 5* (^.* VOL/7 .48/3. 14/3. 5)**. 333
KST=F41*MW1*F42*MW2*F43*MW3+F11*MW1+F12*MW2
PROCEDU"E VOL,TOTFLO = PES.(HLMXf V»SVXtWLTtWST)
!F(LFLO.EQ.1.0)GO TO 358
LFLO=1.0
TOTFLO=WLT/9.98+WST/12.032
358 CONTINUE
FNOP-OCEDUnF
FWATR=F18^F48
VP7=VP70=M .99973-.0863*hFLS-.16C59*KFLS**2)
RHOAVG=(WLMX+KSMX)/VOL
DPL=H*FHGAVG*7.48/144.
PTAVG=p:>ESMX-«-OPL/2
P8=(PT AVG-VP7)*.9*02FAC
PROCEDURE Y=INT(FE3VX,FE2"X)
IF(FE3MX.LT..CC0001)CALL CEBUG(2tO.O)
IF(FE2MX.LT.. 0000000 1 )CALL DEBUG (2, 0.0)
ENDPROCECURE
DM2=-KL*yW2*Y**2*FEPYR**2/(CCAL*NWl I
DM5=C.C
CC.OAL=F11-F51
DS04DT=F44-F54+0V2*SL4
= LIMINT( IC1 , DCOAL , P 1 )
FEPYR=LININT(IC2,CFESDT,P1)
SULFyx=INTf,=1L(IC3,CSnT)
S04MX=IM1 GPL
FC?MX=LIMINT(IC6,OFE3DT,P1»
-581-
-------
ACMX=IIMINT( IC7,OHDT,P1)
H20MX=INTGPL( IC8,DH2UMX)
PROCEDURE IC51,IC52tIC53=LJK(Fll,F12tlW)
IFdW.EQ.l.OJGO TO 69
LW=1.0
IC51=F11
IC52=F12
IC53=.0001
69 CONTINUE
ENOPROCECURE
PROCEDURE IC54, IC55 , IC56 , IC57, IC58=HT (F44 i FA5f F^6, FAT ,FA8t LID )
IF(LID.E0.1.C)GO TC 25
LID=1.0
IC55=F45
IC56=F46
IC57=F47
IC58=F48
25 CONTINUE
ENDPROCEDURF
A5l=COAL*TOTFLO/VCl
A52=FEPYR*TOTFLO/VCL
A53=SULFVX*TCTFLCXVCL
A5A=S04MX*TOTFLQ/VGl.
A55=FE2MX*TCTFLQ/VOL
A56=Ff:3MX*TQTFLO/VCL
A57=ACMX*TOTFLO/VOL
A58=H?CMX*TCTFLO/VCL
PROCEDURE F51,F52,F53=THAT(RESTIM,A51,A52tA53,IC51tIC52,IC53)
F51=A51
F52=A52
F53=A53
IF(TIME.GT.RESTIM)GO TO 182
IF(F51.EQ.O.C)F51=IC51
IF(F52.EO.O.C)F52=IC52
IF(F53.EQ.O.O)F53=IC53
182 CONTINUE
ENDPROCECURE
PROCEDURE F5A,F55,F56,F57,F58=THAX(RESTIM,IC5«t,IC55,...
IC56,IC57, !C58i A5^,A55,A56tA57,A58)
F55=A55
F56=A56
F57=A57
F58=A58
IF(TIME.GT.RESTIM)GO TO 181
IF(F5A.EQ.O.C)F54=IC54
IF
-------
F164=.31379*F54
F165=.31379*F55
F166=.31379*F56
F168=.31379*F58
F51A=.68621*F51
F52A=.68621*F52
F53A=.68621*F53
.68621*FE4
,68621*F55
.68621*F56
F57A=.6b621*F57
F58A=.68621*F58
F181=F161
F132=F162
F133=F1^3
F184=.085?.2*F164
F185=.08522*F165
F186=.03522*F166
F187=.085?2*F167
F183=.08522*F168
<=.9M78*F164
F195 = .'
*
* 1100 V-l EVAFCRATOP-1200 F-l FILTER
F214=.9985*F194
F215=F195
F216=F196
F217=.9925*F197
F218=.5866*F1S8
F267=.0075*F197
F225=.9861*F215
F226=.96A*F216
F227=.01835*F217
F228=.2758*F218
F246A=.036*F216
F247A=.V816*F217
F?4RA=.72':»2*F2ia
P»CCEDURE F244,F245tF246,F247,F248 = REflCT(FILTIMf IC54 , 1C 55, IC56, ,
IC57,IC5S,F24*A,F245A,F246A,F247A,F?48A)
F245=DLLAY(15,FILTIM,F245A)
F246=DTLAY( 15,FILTIM,F246A)
F2 -V7 = Of-L AY (lt3,FILTI",F2't7A)
IF(TI'-"E.GT.FILTIM>Gi; TO 321
-583-
-------
IF(F244.EQ.O.O)F244=.06105*IC54
IF(F245. EQ.O.O)F245=.0039H*IC55
IF(F246.EQ.C.O)F246=.01033*IC56
IF(F247.EQ.O.O)F247=.27965*IC57
IF(F24ft.FQ.O.O)F248=.12194*IC58
321 CONTINUE
ENCPRQCECURE
*
F71=(F51A+Fiei)/NMAX
F72=(F52A+F182)/NMAX
F73=(F53A+Fie3)/NMAX
F74=
-------
AREA=.785*CIA**2
C22=KR.1*APBA
C11=KL1*MW2/(F71*MW1)*AREA
WSTi=MWl*F91*MW2*F92+MW3*F93
WFLSl=l-MWb*F56/WLTl
VD71=VP72*(.99973-.0863*WFLS1-.16C59*WFLS1**3)
FLl=WLTl/RhOLl
FTl-FLl+hSTl/RHCS
"HOAVF^MULTl+kSTD/FTl
DPL1=(ZMAX-Z)*RHOAVE/144*VFAC
P81=(PRESS+DPL1-VP71)
CEP1=-C11*Y1*Y1/FT1*F92**2
IF«Y1.LT.O.O)CER1=0.0
IF(F92.LT.C.C)DER1=0.0
OER2=-C22*P81/FT1/FLI*F95**2
IF(F99.LT.O.O>OER2=0.0
IF(F97.LT.O.C)DER2=0.0
IF(F95.LT.O.C)CER2=0.0
2C GO TC 30
21 IF( IF1.EQ.DGO TO 20
CALL DEBUG(2»0.0)
F93=F93A+SL3*RES1+SR3*RES2
F96=F96A+SL6*RES1+SR6*RES2
F97=F97A+SL7*KES1+SR7*PES2
F98=F9fiA4-SL8*PESl + SR8*RES2
F99 = F99A-»-SR9*RES2
IF(F96.LE.O.C)ZSTA=> = Z
IF(F92.LE.O.C)GO TO 125
IF(F96.LE.O.O)GC TC 125
IF(VF1.LT.2)GO TO 15
1F(Z.GE.ZMAX)GC TO 125
GO TO 10
30 IF1 = !FH-1
GO T0( 100, 2CC, 300, 400, 500) ,IF1
100 MF1=1
GO TC 600
200 S1=^ES1
S2=RES2
PHI l=OtRl
PHI2=DER2
RES1=S1*.5*OZ*CER1
GO TC 600
?CC °HI1=CHIH-2.C*DEC1
PHI2=PHI2+2.C*CER2
RESl=Sl+.5'=OZ*nERl
GO TC 600
AOC PHIl=OH
PHI2=PH12+2.C*nFR2
RES1=S1+.5*D7*OER1
-585-
-------
Z=Z+.5*DZ
GO TO 600
500 RES1=S1*(PHI1+CER1)*DZ/6.0
RES2=S2-HPHI2+DE°.2)*DZ/6.0
MF1 = 2
IF1=0
60C GO TO 21
125 F91A=F91*NMAX
F92A=F92*NVAX
F93A=F93*NMAX
F96A=F96*NMAX
F97A=F97*N^AX
F98A=F98*NMAX
IFF97A=. 00001
IF (F98A.LE.C.O)F98A=. 00001
Z=0.0
SORT
PFOCEOU~sE F91,F92,F93 = SUL(^EST,JC51,JC52,JC53fF91A,F92A,F93A>
F91=CFLAY( 15,RESTt F91A1
F92=OELAY(15,REST,F92A)
F93^=DELAY( 1 5,R EST, F93A )
IF(TIME.GT.REST)GO TO 19
IF(F91.LE.O.C)F91=JC51*NfAX
IF(F92.LE.O.O)F92=JC52*NMAX
IF(F93.LE.O.C)F93=JC53*NMAX
19 CONTINUE
EKOPROCECURE
PROCEDURE F94,F95,F96,F97tF98 = f-/STX(REST,JC5A»JC55f JC56, JC57, . ..
JC58tF94A,F95A,F96A,F97A,F98A»
F94=CELAY(15,REST,F94A)
F95=OELAY( 1 5.P.EST ,F95A )
F96=CELAY(15,REST,F96A)
F97=OELAY(15fREST,F97A)
F98=OrLAY( 15t»EST,F98A)
IF(TIME.GT.P.EST)GO TO 281
IF(F95.LF.C.C)F05=JCSS*NMAX
IF(F96.LE.O.O)F96=JC56*NyAX
281
t
* 400 F-I FILTER
-586-
-------
PROCEDURE F24,F25,F26,F27iF28=R2FILT
F327=DELAY(15,F32T^,F307)
F 328= DEL AY ( 1 5, F 32TM.F 3C8 I
IF(TI«E.GT.F?2TM)GG TO 369
-587-
-------
IF(F3?6.EO.O.C)P?26=.7eO7=.78043*JC57*NWAX
369 CONTINUE
CALL CESUr,(2fO.O)
F3B-3=F303
*
* 7CC V-l kASH TANK
*
F474=F264
F3C1=F291
F392=F292
F393=111247*F293
F395=5.094*F295
F397=4.3A18*F267+5.3418*F297
F398=fc.729*F298+5.726fl*F268+£.7268*F558
#
* 300 F-l FILTER
*
F478=.10945*F3Sa+1.109*F268+1.109*F558
F454=.0573*(
F456=. 0576*^396
F457=.0548*(F397+F267)
F4?3=.8414*F393
F425=.8414*F295
F426=.8414*F396
F427=.8023*(F397*F267)
F428=.6577*(F398+F478I
F414 = .1049=!--(F394*F474)
F415=.1011*F295
F416=.1011*F396
F417=.1429*(F3S7*F267)
F413=.1011*F393
*
*
* 900 NE-1 DRYER (F53-CLEAN CCAL PRODUCT)
*
F521=F451
F532=F452
F533=F453
F535=F455
F517=F457
F538=.20*F458
F46£=.80*F456
1600 E-l CCNCCNiSE0 1600 V-l TECAMTE9
-588-
-------
F488=.9Q37*F468
F518=F4P6
*
* 1500 V-l DECANTER
*
F403=F423
F404=F424
F405=F425
F406=F426
F407=F427
F408=F42fi
F333=F423
F438=.835*F4C9
F144A=.165*F4C4
F147A=.165*FAC7
F148A=.165*F4C8
PROCEDURE ri44,F145,F146,F147,FlAe=HI'S(F14TM,F144A,F145A,F146#f ,
F147A,F148A,JC54tJC55tJC56,JC57fJC58)
F144=Df:LAY( 1 5 , F 14T V ,F144 A )
F145=DELAY(15,F14TM,F145A)
F147=DELAY( 15tF14TM,F147A)
F148 = PirLAY(15,F14TMtF148A)
IF( TIME.GT.F14T?')GC TO 199
IF(F144.EO.O.O)F144=.121*JC54*NMAX
1F(F145.EQ.O.O)F145=.0615*JC55*N^AX
IF(F146.EQ.O.O)F146=.1612*JC56*N^AX
IF(F147.EQ.C.O)F147=.0588*JC57*NMAX
IF(F148.EQ.O.O)F148=1.437*JC58*N^AX
199 CONTINUF
ENDPROCECUPE
F433=.035*F4C3
F434=.835*F4C4
F435=.835*F4C5
F436=.835*F4C6
F437=.835*F4C7
«
* KAIN RECYCLE
F46=F26+F1464F326
F47=F27*F147+F327
*
*
* STREAM 4 CHEMST^Y
*
F44VCL=2.157692*F48*3.785
H48PCT=F48*MW6/F44C*100.+F47*MU8/(2.*F44C»*108.
TOTAL=S44PCT+H43PCT+F46PCT
-589-
-------
F46PCT=100*F46PCT/ TOTAL
S44CN=F'. 4*453. /F44VHL
F45CN=F45*453./F44VCL
K S 4 6 = ( F 4 6 C N <• 1 . C E - 4 2 ) / ( H 4 7 C N * * 3 )
KFI
*
v MIXEP CHEMISTRY
#
FMXVCL=2.1576<92*hi2C^X*3.785
PHA7=-ALnG10(HA7CN)
FMXPCT=FF3MX*MW6/FMX*100./.7
SMXPCT=1 00* SMXPCT/ TOTAL
FMXPCT-100*FMXPCT/TOTAL
HM X°C T= 100#H,vx PC T/ TOTAL
F2MXCN=FE2f'XM53./F.vxVOL
F3MXCN=FE3MX*A£3./FMXVOL
KSMX=(F3MXCN*1.0E-A2)/(HyxCN**3)
KFIIMX=F2MXCN*SMXCN/HMXCN
PHMX=-ALOG1C(HMXCN)
EHMX=.771*.059*ALOG10(F3MXCN/F2MXCN>
SO^SMX=EXP(2.3025v{9.83E-03*(Ehf/X-.338+.0688*PHMX» J
*
* STREAM 5 CHEMISTRY
*
F5AVOL=2.157692*F5e*3.7S5
F56PCT=F56*M'rt6/F54C*LOO./.7
TOTAL=S54PCT+F56PCT*H58PCT
S54PCT=S54PCT*100/TOTAL
F56PCT=F56PCT*10C/TCTAL
H58PCT=H58PCT* ICO /TOTAL
S54CN=F54*453./F54VOL
F55CN=F55*453./F54VOL
F56CN=F56*453./F54VGL
H57CN=F57*453./F54VCL
KS56=(F56CN*1.0E-42)/(H57CN**3)
KF I I55=.F55CN*S'54CN/H57CM
PH57=-ALUG10(H57CN)
EH55=.771+.059*ALCG10(F56CN/F55CN»
*
* STREAM 9 OFMISTRY
*
F98VOl=F 98*?. 157^92*3. 785
-59O-
-------
F95CON=F95*453./F98VGL
F96CrN=F96*453./F98VOL
F94PCT=(F94*fW4)/F9C*33.3/.4
F98PCT=F9n*Mfc8/F9C*100.+F97*fV>8/(2.*F9C)*100
TUTAL = F94PCT4F96Pr.T4-F98»CT
F94PCT=1CO*F54PCT/TCTAL
F96PCT=100*F<;6PCT /TOTAL
F98PCT=1 00* F9 SPOT/TOTAL
KF 1 1 95-=F95CCN*F94CCN/F97CCN
KS96=(F96CON*1.0E-42)/(F97CCN**3)
FH9 = -AL':G1P(F97CCN)
V=(F96CnN*9.+F95CON*4.4-F94CCN*4.4-F97CCN)/2.
EH95=.77H-.059*ALOG10(F96CON/F95CON)
* STREAM 16 CHEMISTRY (IRON SLLFATE RE^CVAL)
*
Fl 6 VCL=2.1 5 7692*^1 63*3. 7 85
F16C=F164*MWA+F166*MW6*-F167-«-F168*MW8
Fl 64PT=F 16A*^WA/ F16O33 . 33/ .4
F168PT=F 167*100/1 2. *F16C)/. 11 11+F 168*MW8* LOC/F1 6C
TOTAL=f 16APT+F166PT+F16BPT
F16APT=F164PT*100/TOTAL
Fl 6ft PT = F1 66 PT*1'00/ TOTAL
F165CN=F165*A53./F16VOL
F166CN=F166^«53./F16VOL
F167CN=F167*A53./F16VCL
KS166 = (F166CM1.0E-42)/(F167CN**3)
KF2165=F164CN*F165CN/F167CN
PH167=-AL3G10(F167CN)
EH16=.771+.C59*ALOGIO(F166CN/F165CN)
*
* STREAM 18 ChEMISTRYdlOO F-l FILTER RESIDUE)
<<
Fl 8 VOL =2.1 57692 *F 188*3. 785
./F18C + F187*100./(2.*F18C)/.1H1
F184PT=F18APT*100/ TOTAL
F186PT=F186PT*100/TCTAL
Fl 88DT=F 16 PPT* ICO/ TOTAL
F184CN=F1 84*453. /F18VOL
F186CN=F-136*«53. /F18VOL
F137CN=F 187*453. /F18VOL
KS186=(F18fcCN*1.0F-42)/(Fl87CN**3l
KF2185=F184CN*Fia5CN/F187CN
PH187=-ALOG10(Fia7CN)
FH18=.771+-.C59*ALGGlC(F18ftCN/F185CNI
*
* STPEAV 19 CHEMSTPY (1100 F-l FILTPATF)
A
Fl 9VOL=2. 15 7692 *F 198*3.78'=
'
-591-
-------
F194PT=F194*NW4/F19C*33.33/.4
F 1 T=F 1 9f "N W6/F19C"! 00. /. 6904
= F198*ivV.8*100/F19C+F197*10C/(2.*F19C)/.llll
94PT + F196PT«-F198PT
F194PT=F19'.PT*1CC/TPTAL
Fl 96PT = F 196 PT*100/ TOTAL
F198PT=Fl<;ePT*iaO/TCTAL
F194CNI = F194*453./F19VOL
F195CN=F1 95*45 3./F19VOL
F196CN=F196*453./F19VOL
F197CN=F197*453./F19VOL
KS19t> = (F196CN*1.0c-42)/(F197CN**3.)
KF2195=F194Cf\*F155CN/Fl97CI\
P4197=-ALC!G10(F197CN»
FH19=.771^.C59*ALCG10(F196CN/F195CN)
*
* STEAM 21/24 CHEMISTRY (1200 F-l FILTRATE)
*
18*3.785
F218PT=F218*NW3*100/F21C+F217*10C/(2.*F21C)/.llll
F214PT=F?14PT*10C/TOTAL
F216PT=F216PT*100/TOTAL
F213PT=F218PT*lCC/Tr.TAL
F215Cfg=F21?>!;453./F21VOL
F216CN=F 21 6*453. /F21 VOL
F217CN=F217*453./F21VOL
KS216=(F216CN*1 .OE-42 ) / ( F2 17CN**3 )
KF2215=F214CN*F215CN/F217CN
PH217=-ALCG10(F217CN)
EH21=.771+.C59*ALCG10(F216CN/F215CN)
*
* STREAM 7 OEVISTRY (INPUT TO FLUIDIZED BED)
#
F7VOL=2. 1576?2*F78*3.785
F740T=F74*MU4/F7C*33.33/.4
F76PT=F76*MW6*100./F7C/.fc994
F78PT=F78*NW8*100./F7OF77*100./(2.*F7C)/.llll
TGTAL=F74PT+F76PT+F78PT
F74PT=100'!--F74PT/ TOTAL
F76PT=100*F76PT/TCTAL
F73PT=100*F7£PT /TOTAL
F74CN' = F74*453./F7VGL
F75CN=F75*453./F7VOL
F76CN=F76*453./F7VCL
F77CN=F77*453./F7VCL
KF27'5=F7<.CN*F75CN/F77CN
KS76=(F76CN*1.0E-42)/(F77CN**3)
I7=(F74CN*4+F75CN*4+F76CN*9+F77CN)/2.
PH7=-ALOGIO(F77CN)
EH7=.771*.059*ALGG10(F76CN/F75CN)
* •
* STRFAM 2 CHFMISTPY (400F-1 FILTRATE (RECYCLE))
-592-
-------
. /F2C/. 6994
F28PT=F28*NWe*10C/F2C+F27*lCO./(2.*F2C)/.llll
F24PT=F24PT* 100 /TOTAL
F26PT=F26PT* 100 /TOTAL
F28PT-F28PT*100/TOTAL
F24CN=F24*^53./F2VCL
F25CN=F?5*453./F2VCL
F26Cr>:=F26*453./F2VCL
F27CN=F27*453./F2VCL
KS26=(F26CN*1.0E-42)/(F27CN**3)
I2=(F24CN*4+F25CN*4+F26CN*9+F27CN)/2.
PH2=-ALQG10(F27CN)
EH2=.771+.C59*ALCG10(F26CN/F25CN)
*
* STREAM 32 CHEMISTRY (FILTRATE FROM 600 F-l AND
* AQUEOUS PRODUCT OF 1AOO V-l
* DECANTER (RECYCLE) )
*
F32Vn_=2.157692*F323*3.785
F32C=F324*flrj4+F326*MW6*-F
F324PT=F324*fW4/F32C*33.33/.^»
F328PT=F327*100./(2.*F32C)/.1111*F328*^W8*100./F32C
TOTAL=F324PTtF326PT*F323PT
F324PT=F224PT* IOC/TOTAL
F326PT = !=326PT*100/TGTAL
F328PT=F328PT*10C/TOTAL
F324CN=F324*453./F32VOL
F325CN=F325*453./F32VCL
F326CN=C326*453./F32VOL
F327CN=F327*453./F32VQL
KS326=(F226CN*1.0E-42»/(F327CN**3l
KF2325=F325CN*F324CN/F327CN
PH32=-ALrG10(F327CN)
EH32=.771+.C59*ALOG10(F326CN/F325CN)
*
*
* STt>EA*l 14 CHEMISTRY (FRACTICN CF 1500 V-l PRODUCT (FECYCLEJ)
*
PI 4 VCL=2.1 57692 *F 148*3. 785
FltC = F144*MW4 + F146*MW6+F 1 47+F 148*MV»8
F144PT=F144*23.33*MW4/F14C/.4
F146PT=F146*KV»6*10C./F14C/.6994
FU8PT=FlA6*MVi8*10C/F14C+F 147*100. /(2.*F14C)/. 11 11
=F 1 44° T* IOC /TOTAL
F146PT=F146PT* 100 /TOTAL
F148PT=F148PT*100/TOTAL
CN = F 14 5*453. /F14VOL
P146CN=F146*453./F14VCL
F147CN=F 147*453./F14VOL
KS146=(F146CN*1 .0 E-42 )/ ( F147CN **3 )
-593-
-------
STAF-TL'P
PH14=-ALOG1C(F1A7CM
EH14=.77H-.059*ALaG10(F146C\'/F145CN)
TF.°MINAL
yETHCD RtCT
TIMFR OFLT=.
TITLE COAL DESUl.FUR IZ AT ION
OUTPUT ZSTAR ,F99
* SULFATFj ST'TAPS
OUTPUT FAAtSCAMXtF5A,F74,F9A
OUTPUT FlfiA,F19A,F21A,F26A,F?2A,F2AA
OUTPUT F1A^,F?2A,F24,F3<;4
* FERROUS STREAMS
OUTPUT F
F156t'Pl96,F216iF226,F246
FlAfc,F3?6,F26tF396
* ACID STREAMS
OUTPUT F^7tACN'X,F57,F77fF97
F187,F1<;7,F217,F227,F267,F2A7
F1A7,F327,F27,F3<37
KATEF STREAMS
FA8fH20MX,F58,F78f F98
F328,F28,F1A3
OUTPUT
OUTPUT
*
OUTPUT
OUTPUT
*
OUTPUT
*
OUTPUT
*
OUTPUT
OUTPUT
OUTPUT
*
*
OUTPUT
OUTPUT
OUTPUT
*
F12,FEPYR,F52,F72,F92
IRON CHEMSTRY EH-PH
EHCX,Eh55,tH95
PH
HNXfPH57tPH7fPH9
PH2,PH1A,PH32,PHA7
PHI 67 ,PH187iPH217fPH32
IRON' CHEMISTRY FE(OH)3 SOLUBILITY PRODUCT
KSAA,KSNX,KS5C:,KS76,KS96
KS166fKSl£6,KS196,KS216
KS26,KS326,KS1A6,KSA6
IRON CHfMISTPY (FESOA SOLUBILITY PRODUCT)
OUTPUT KFIK5,KFIII'X»KFII55,KFII95
OUTPUT KF226.,KF21A5tKF2325,KFIIA5
OUTPUT KF2165,KF21£5,KF2195,KF2215
*• TERNARY DATA
OUTPUT S^PCT ,FA6PCT,H43PCTfSCXFCT,F»'XPCTf HCXPCT
OUTPUT S5APCT,F56PCT,H58PCT
^UTPUT F7APT,F76PT,F7HPTtF2':>PT,c26PTiF28PT
OUTPUT F94PCT,F9tPCT,F98°CT
OUTPUT F16APT,Flfc6PTfFl68PTfFl8APT,F186PT,FlB3PT
OUTPUT F19/.PT,F196PT , F1Q8PT , F2 14PT ,F 2 16PT , F2 18PT
OUTPUT F32-DT,F?26DT,P3?fiPT
OUTPUT F1AAPT,F1^6PT,F1A8PT
FND
STOP
•594-
-------
10.8.2 Conditions of Iron Precipitate Formation
In the coal desulfurization process there are three types
of precipitate that can form: (1) ferrous sulfate, (2) ferric
hydroxide/ and (3) a solid solution of acidic to basic ferric
sulfate. The purpose of this section is to discuss the
conditions where these precipitates will form and indicate
where additional data will be required to better define
the process.
(1) Ferrous Sulfate
(29)
Sources in the literature report the solubility of
ferrous sulfate in terms of grams of H^SO. and grams of
FeSO, per fixed volume of solution. In.order to interpolate
and possibly extrapolate to different conditions, a relation-
ship had to be developed to fit these data. The general form
selected was
K-L = [Fe2+] [S042~] (16)
Since many of the streams are quite acidic an additional
relation was included:
[HSO. ".]
2 [H+][S042~] (17)
The value of the equilibrium constant, K~, is known to be
1
(10 ). Therefore, for pH values above pH 1.9, form
(16) was used. Below pH 1.9 [Fe2+][HSO4~]/IH+] was used as
a relative indicator of ferrous sulfate solubility. Plots
of K, and K,/K2 did not remain constant across the range
-595-
-------
of solubility data. If forms (16) and (17) are correct for
ferrous sulfate precipitation, then the variability must be
due to variations of activity coefficients. Since activity
coefficients vary in magnitude with ionic strength, it was
decided to make ionic strength corrections. However, the
determination of mean activity coefficients is quite dif-
ficult and it would require extensive experimentation.
A less accurate but reasonable alternative that was used
relates the constants directly to ionic strength using
polynomial regression. CSMP was then used to calculate
stream and vessel ionic strengths. These ionic strengths
were used as input to determine the constants K, and K,/K2.
The results were realistic when the ionic strengths calculated
by the CSMP were within the range of the existing solubility
data; however, the majority of desulfurization ionic strengths
were beyond the range of the data. Extrapolation beyond
the data yielded unrealistic results so the approach was
2+ 2-
limited in its usefulness. However, the terms [Fe ][SO. ]
2+ - +
and [Fe ][HSO. ]/[H ] are useful as relative indicators of
ferrous sulfate solubility. More data will definitely
have to be generated to define the ferrous sulfate system.
(2) Ferric Hydroxide
The precipitate ferric hydroxide or ferric oxyhydroxide has
a solubility product constant that varies with time and
conditions of precipitation. Actually, many of the re-
ported values are "apparent" solubility product constants
rather than a solubility product constant in the thermody-
namic sense. The solubility product relation is
-596-
-------
K = Kw3 [Fe3+] [H+]~3 (18)
where Kw = [H+][OH~] = 1 x 10~14
(22) —17
Values of K reported in the literaturev ' vary from 10
—44 —17
to 10 at 25°C. In this process 10 will probably be
most realistic because it corresponds to a value reported
2+
where rapid oxidation of Fe occurs. There are several
other factors that must be considered in arriving at a K
for the coal desulfurization process: (1) K will vary
with ionic strength in an inverse manner. (2) K is in-
versely proportional to temperature. (3) Laboratory values
of K may not predict process conditions' if the forward rate
is slow. Further experimental data will be required to
fill these gaps. Yet, the CSMP calculated quantity (18)
will provide a relative indication of conditions in the
process.
(3) Acidic-Basic Ferric Sulfate
The iron (III)-sulfate-water system has been well defined
(21)
across the region of interest by Posnjak and Merwin
who experimentally developed a ternary diagram for the
Fe20_-S0^-H20 system. Theoretically, there should be
little influence of the ferrous sulfate system on the
structure of this ternary diagram. This appears to be
true as indicated by a plot of FeO-Fe_O_-SO-,-H90 data from
(29)
Seidell on a ternary diagram (Figure 55). The solu-
bility limits plotted on this curve agree with those of
Figure 46. This form of diagram was used in conjunction
with CSMP molar amounts in an effort to determine where
ferric sulfates would form in the process.
-597-
-------
Figure 55. Solubility Diagram for the
FeO-Fe203-S03-H20 System(29) at 5O°C
© Fe203-SO3-H2O system
B FeO-Fe2O3-S03-H20 system
en
to
X^sSv^A'/y^-xSV^'^^XrA^'-y'^V^
'*$$^&£^^w&w&
. rf <--7v«?vv\ xV-v-A x-Vx'A' v-vv-A'-y-i-v.
SO,
-------
10.8.3 Construction of Eh~pH Diagrams for Sulfur Species
The following reactions are those that should be considered
in the oxidation of pyrite
(19)
2S°s) + 2eT (20)
S2" + H+ —-^~ HS (21)
HS + H * H0S /__\ (^2)
H2S(aq) Z^±S° + 2H+ + 2e- (23)
i 0(*^ + H + 2e~ (24)
(aq) -< - (s)
S° . + 4H20 < ^ S042~ + 8H+ + 6e~ (25)
S042~ + H+ < * HS04" (26)
4H20 < ^ S042" + 10H+ + 8e~ (27)
HS~ + 4H20 • ^' > S042 + 10H+ + 9e" (28)
S2~ ; ~^r*~ S(. + 2e~ (29)
(aq) -< (s)
-599-
-------
The equilibrium constants for reactions (21) and (22) are
-14 —7
10 and 10 respectively. Hence the stable regions for
2- -
S , HS and H2S can easily be determined.
Species Stable pH Range
S2~ >14 (at pH=14,tHS~] = [S2"])
HS 7-14
HO y/ 1
«o v /
Therefore, Equations (24), (28), and (29) can be neglected
in a study of pyrite oxidation in acid solutions.
19 -
Also, KHSQ- = 10 , which implies that HS04 is the
stable species below pH 1.9. The equations listed above
can be used in conjunction with free energy data to de-
termine the regions of stability for aqueous solutions.
From fundamental thermodynamics
AFr = AFr° + RTlnQ (30)
where AFr s? free-energy change of the reaction .
AFr° = standard free energy for the reaction
Q = reaction quotient
T = temperature, °K
R = gas constant, 0.001987 kcal/°k
-60O-
-------
and
AF° = nE°f (31)
r = nEhf (32)
where n = number of electrons transferred
f = Faraday constant, 23.06
E = standard reaction voltage at unit
activity (reference: hydrogen)
E, = total emf.
Then
E
Equation (33) is the relation used to determine regions
where certain species predominate in aqueous solutions.
An example of how the actual equation is developed will be
shown using Equation (27). The first step involves the
determination of the standard free energy change for the
reaction
AFr° = AFS042- + 10AFH+ + 8AFe- - AFH2S " 4AFH20
= -177.34 +0+0 -(-6.54)-4(-56.69)
= 55.96
Then
E° = 0.303
and
E
h = 0.303 + InQ
= 0.303 + 'a logQ
-6O1-
-------
Q =
[SO,2 .].[H+]10
- 2 -
[H2S]
Then [so.2-]
E. = 0.303 + 0.00738 log ( ) - 0.0738 pH
[H2S]
An E, -pH curve for this equation is drawn for the condition
2-
[SO. ] = [H^S] which reduces the equation to:
E = 0.303 - 0.0738 pH
Since equation (27) shows the transition from the -2 to
+6 valence state, it will not be useful to isolate the
stable region of sulfur. The equations that can be used
to isolate the stable sulfur region are (23) , (25) , and
(26). Equation (19) can be neglected because it has no
E,-pH dependency. Equations (21) and (22) were already
used to isolate regions of sulfide ion stability. Finally,
equation (20) has an E, of approximately -0.44 in all
regions of interest. The E, equations are plotted in
Figure 56. Superimposed on the E, lines are regions of
process operation when ferric ions are regenerated in the
mixer.
-602-
-------
1.0
0.6
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a
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o
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K
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i
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vtfZMZ'.l
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Elemental
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•r Operating Re
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,+1-dii f
»n
iviiAcr^
TTTtr! — H — — : 1 ' i ,.—., 5*
ileactor Effluent Operating j
Region (Ferric Regeneration- 4
Mixer) :
'l • l 1 • 1 ' ; '
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7
Hydrogen Ion Concentration, pH
Figure 56. Mixer and Reactor Operating Regions on a
Sulfur-Water Eh-pH Stability Diagram
-603-
-------
10.8.4 Calculations of the Effect of Ferric Ion
Regeneration in the Mixer
As indicated in Section 7.3.1 the small improvement in
overall product quality resulting from adding oxygen and
make-up acid to the Mixer becomes more significant when
viewed from the standpoint of residence time. The
relationship developed was
KLY
(14)
where f = reactor influent weight ratio, pyrite/coal
f. = reactor effluent weight ratio, pyrite/coal
t = time in reactor
The "reactor" system here is intended to be the entire Mixer-
Reactor system of the design.
Assume:
(1) Influent weight of coal/hour = 17,461 Ib mol/hr
(2) Influent weight of pyrite/hour = 135.87 Ib mol/hr
(3) KTY2 = (31.81) (0.7)2 = 15.59, held constant
Ju
Then
f0 = 100 x ' = 0.0718 Ib pyrite/lb coal
where 119.9 = molecular weight of pyrite
13.0 = molecular weight of coal
Examine three different levels of ft: 5.0%, 4.4% and 5.5% of
the initial level.
Then f = 0.050 x 0.0718 = 0.00359 for 5.0%
f , = 0.044 x 0.0718 = 0.00315 for 4.4%
f „ = 0.055 x 0.0718 = 0.00395 for 5.5%
-604-
-------
Case 1 — Change in residence time to reduce pyrite effluent
from 5.0% to 4.4% of initial:
= 16'97 hrs
15.59 0.00359 0.0718
t' = 15.59 0.00315 ~ 0.0718 = 19'47 hrs
c. 19'4L"ai6'97 x 100 = 14.73% increase
ID . y /
Case 2 — Change in residence time to reduce pyrite effluent
from 5.5% to 4.4% of initial:
a. t1 = 19.47 hrs.f from above
b> tM = 15.59 0.00395 ~ 0.0718 = 15*35 hrs
c. 19'4~5'35 x 10° = 26.84% increase
-6O5-
-------
TECHNICAL REPORT DATA
(Please read Inslmctions on the reverse before completing)
1. REPO.RT NO.
EPA -600/2 -7 5- 051
2.
3. RECIPIENT'S ACCESSIQN>NO.
4. TITLE AND SUBTITLE
Conceptual Design of a Commercial Scale Plant for
Chemical Desulfurization of Coal
5. REPORT DATE
September 1975
6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
8. PERFORMING ORGANIZATION REPORT NO.
W.F. Nekervis and E.F. Hensley
J. PERFORMING ORGANIZATION NAME AND ADDRESS
Dow Chemical, U.S.A.
Michigan Division
Midland, Michigan 48640
10. PROGRAM ELEMENT NO.
1AB013; ROAP 21ADD-097
11. CONTRACT/GRANT NO.
68-02-1302
12. SPONSORING AGENCY NAME AND ADDRESS
EPA, Office of Research and Development
Industrial Environmental Research Laboratory
Research Triangle Park, NC 27711
13. TYPE OF REPORT AND PERIOD COVERED
Final; 6/73-9/75
14. SPONSORING AGENCY CODE
15. SUPPLEMENTARY NOTES
16. ABSTRACT,
The report presents a conceptual design and an economic evaluation of a
9070 metric ton per day plant for the chemical removal of pyritic sulfur from coal.
All supporting facilities are included for a self-sufficient operating complex with
purchased water and power. The process engineering is complete through a capital
cost estimate. Computer augmented studies are included for the material and energy
balances, selection of the reactor systems, monitoring of operating parameters, and
economic sensitivity studies of process alternatives.
7.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTlFIERS/OPEN ENDED TERMS
c. COS AT I Field/Group
Air Pollution
Chemical Cleaning
Coal Preparation
Design
Desulfurization
Economic Analysis
Pyrite
Air Pollution Control
Stationary Sources
Meyers Process
Ferric Sulfate Extrac-
tion
13B
13H, 07A
081
07D
05C
08G
8. DISTRIBUTION STATEMENT
Unlimited
19. SECURITY CLASS (ThisReport)
Unclassified
21. NO. OF PAGES
607
20. SECURITY CLASS (Thispage)
Unclassified
22. PRICE
EPA Form 2220-1 (9-73)
-607-
-------