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TABLE 219
BLEACHED KRAFT MILLS
BEST OF THE BEST MILLS ( mg/L)
Mill
- — -
101
130
119
117
112
105
106
107
Subcategory
Fine-Mkt
Mkt
Fine
BCT
Fine
BCT
Fine-Mkt
Fine-Mkt
Treatment
C-ASB-PS
SB-ASB
C-A
C-ASB
C-ASB-C
C-ASB-PS
C-ASB-PS
C-A-PS
Average
Raw
Waste
BOD5
186
120
240
146
224
224
204
264
201
Final
BOD5
9
11
11
12
13
16
18
18
13.5
Effluent
TSS
I •<•/«••*
13
25
33
25
139N
.
20
71
31
66.
-------
mg/1 as discussed in Section VII. In addition to TSS reduction,
approximately 20% to 25% of the BOD5 is removed by filtration. The
effluent limitations were thereby based upon 15 mg/1 BOD5 and 10 mg/1
TSS.
Market Kraft Subcategory
The market kraft subcategory raw waste load was essentially based upon
three mills, 130, 114, and 140. Mills 140 and 139 have flow volumes
of 79.2 kl/kkg (19.0 kgal/ton) and 85.1 kl/kkg {20.4 kgal/ton),
respectively. The other market kraft mills cannot necessarily be
expected to achieve these flow values and thereby the flows used for
BATEA limitations were based upon mill 114 which had a flow of 172.6
kl/kkg (41.4 kgal/ton). Evaluation of the internal, controls in use
by mill 114 resulted in estimates of flow reductions of about 29.2
kl/kkg (7.0 kgal/ton). The BODj> raw waste load was based on mills 130
and 140. Evaluation of the inplant controls in use at mills 114, 130,
and 140 resulted in estimates that BOD5 reductions of 5.0 kg/kkg (10.0
Ibs/ton) could be achieved by BATEA internal controls not yet in use
by mill 130 and that the BOD5_ levels were achievable as demonstrated
by mill 140. The estimated raw waste loads for BATEA were the
following:
Flow: 141.8 kl/kkg (34.0 kgal/ton)
BOD5: 26.5 kg/kkg (53.0 Ibs/ton)
TSS: 65.0 kg/kkg (130 Ibs/ton)
The above estimated raw waste load is similar to that presently being
achieved by mill 185 as shown in Table 51 in Section V. The raw waste
flow at mill 185 is presently 143 kl/kkg (34.2 kg/kkg) and the raw
waste BOD5 is presently 32.4 kg/kkg (64.7 Ibs/ton). Application of
BATEA inplant controls not presently in use at mill 185 should allow
the mill to achieve a raw waste load lower than the above BATEA raw
waste load. The effluent limitations for BATEA were based upon 10
mg/1 TSS and 14 mg/1 BODj> in conduction with 141.8 kl/kkg (34.0
kgal/ton). As discussed previously, the capabilities of the
coagulation and filtration systems results in levels of TSS in
effluents of 5 - 10 mg/1 TSS. The average of mill 130 and mill 114
final effluent BOD5 values was 18 mg/1. Application of filtration
technologies will reduce effluent BOC5 by approximately 20% to 25%.
The BODJ5 effluent limitations were thereby based upon 14 mg/1. The
subcategory average BOD5 raw waste load is 187 mg/1 whereas the
average of mills 130 and 114 is 235 mg/1 indicating that the BODS^
levels are achievable.
Bleached Kraft - BCT Papers Subcategory
The BCT Papers Subcategory raw waste load was based upon mill 111
which had the following flow, BOD5, and TSS raw waste loads:
Flow: 134.7 kl/kkg (32.3 kgal/ton)
BOD5: 30.8 kg/kkg (61.6 Ibs/ton)
TSS: 51.5 kg/kkg (103 Ibs/ton)
666
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The internal controls presently in use by mill 111 are shown below:
Knots collection and disposal
Decker filtrate for brown stock washer showers
Jump stage countercurrent washing
Evaporator surface condenser
Evaporator boilout tank
Alarms on chemical tanks
Paper machine vacuum saveall
Paper machine high pressure showers
Paper machine white water showers
Vacuum pumps seal water reuse
Pulp mill spill collection from tanks, equipment, and drains
Mechanical conveyor for log transport
Fourth stage fcrown stock washer
Close-up screen room
Causticizing area spill collection system
Evaporator condensate for causticizing makeup
Lime mud storage pond
Cooling water segregation and reuse
Paper mill stock spill collection system
Pulp mill spill collection from washers
Evaluation of the internal controls in use by mill 111 in relationship
to the present raw waste loads and estimating the raw waste load
reductions possible by installation of any BATEA internal technologies
not used by mill 111 and by more intensive process control to further
reduce impacts or raw waste load resulted in the estimates of RWL
reductions for mill 111 are given below.
Flow: 20.9 kl/kkg (5.0 kgal/ton)
BOD5: 5.0 kg/kkg (10.0 Ibs/ton)
TSS: 5.0 kg/kkg (10.0 Ibs/ton)
Thus, the RWL for the BCT Papers Subcategory used in developing the
BATEA effluent limitations and the costs of achieving the limitations
are the following:
Flow: 112.6 kl/kkg (27.0 kgal/ton)
BOD5: 26.0 kg/kkg (52.0 Ibs/ton)
TSS: 46.5 kg/kkg (93.0 Ibs/ton)
The BATEA effluent limitations were based upon 10 mg/1 TSS, 15 mg/1
BOD5, and 112.6 kl/kkg (27.0 kgal/ton) as shown in Table 218. Use of
coagulation and filtration systems treating the biological treatment
effluent will achieve at least 10 mg/1 TSS as discussed in Section
VII. Mills 117 and 105 are presently achieving BOD5 effluent levels
of 16 mg/1 and 12 mg/1, respectively, with an average of 14 mg/1. The
average BOD5 raw waste for mills 117 and 105 is 185 mg/1 whereas the
subcategory average is 231 mg/1. Because the average raw waste load
for mills 117 and 105 is less than the subcategory average, the BOD5_
effluent limitations were based upon 15 mg/1 which takes into account
a 20% to 25% reduction in BOD5_ achieved by the application of
filtration technologies.
667
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Bleached Kraft - Fine Papers Subcategory
The bleached kraft fine papers subcategory raw waste loads which were
used in determining the BATEA effluent limitations and the costs of
achieving the limitations were based upon mill 119 which had the
following RWL:
Flow: 97.2 kl/kkg (23.3 kgal/ton)
BODJ5: 23. a kg/kkg (46.7 Ibs/ton)
TSS: 46.5 kg/kkg (92.9 Ibs/ton)
The internal controls presently in use by mill 119 are shown below:
Knots collection and disposal
Decker filtrate for brown stock washer showers
Jump stage countercurrent washing
Evaporator surface condenser
Evaporator boilout tank
Black liquor storage tank spill collection
Vacuum pumps seal water reuse
Alarms on chemical tanks
Paper machine high pressure showers
Paper machine white water showers
Use of steam in drum barkers
Fourth stage brown stock washer
Close-up screen room
Pulp mill spill collection from washers
Pulp mill spill collection from tanks, equipment, and drains
Causticizing area spill collection system
Evaporator condensate for causticizing makeup
Lime mud storage pond
Cooling water segregation and reuse
Paper mill stock spill collection system
Evaluation of the internal controls identified in Sections VII and
VIII as BATEA and those presently in use by the mill showed that the
mill was already achieving effluent raw waste loads representative of
the BATEA. Thus, the BATEA effluent limitations were based upon mill
119 and, the mill's RWL were rounded to the following:
Flow: 95.9 kg/kkg (23.0 kgal/ton)
BODJ5: 23.5 kg/kkg (47.0 Ibs/ton)
TSS: 46.5 kg/kkg (93.0 Ibs/ton)
The BOD5 and TSS concentrations on which the BATEA effluent
limitations were based were 15 mg/1 and 10 mg/1, respectively. The
TSS level of 10 mg/1 has been discussed previously. The BOD5 effluent
limitations were based upon evaluation of the effluent levels
presently being achieved by the following mills in conjunction witt
the application of filtration technologies which remove 20% to 25% of
the remaining BOD_5.
Raw Waste Final Effluent
Mill Treatment EOD5 (mg/1) BODS (mg/1)
-------
101 C-ASB-PS 186 9
119 C-A 240 11
112 OASB-C 224 13
106 C-ASB-PS 204 18
107 C-ASB-PS 264 18
Average 224 14
The average subcategory raw waste load is 245 mg/1 whereas the average
of above mills is 224 mg/1. The BOD5 effluent limitations were based
upon 15 mg/1 which takes into account the differences in raw waste
load and the BODJ5 reductions associated with the filtration
technologies.
Color Limitations
The color effluent limitations were based upon the color data
presented in Table 49 in Section V. Analysis of the data in the table
shows four significant levels of color: (1) Dissolving kraft, (2)
Market kraft, (3) BCT Papers, and (4) Fine Papers. The raw waste
color loads for the above subcategories are the following: 415 kg/kkg
(830 Ibs/ton) , 310 kg/kkg (620 Ibs/ton) , 225 kg/kkg (450 Ibs/ton) , and
150 kg/kkg (300 Ibs/ton), respectively. It should be pointed out that
the data used in determining these color RWL is the highest of stream
09 or stream 79 data per mill in Table 49. The dissolving kraft and
market kraft RWL were based upon mills 127 and 114, respectively,
whereas the BCT RWL was based upon mills 105, 125, and 117. Mills
101, 110, 106, 116, and 119 were used as the basis for the fine
paper's RWL.
As identified in Sections VII and VIII, the "minimum lime" process for
color removal was suggested for application to the caustic extraction
effluent and a portion of the decker effluent. Color data obtained
from surveyed mills were insufficient to establish reliable color
values for those streams. As discussed in Section VII, however, the
minimum lime process can attain a 90 to 94 percent color reduction
(260) (261). Comparable streams treated by the massive lime process
can achieve similar results (247).
At these levels of color reductions in the extraction and decker
effluents, total mill raw waste color is reduced approximately 72%
(232). By BATEA internal controls such as extensive spill control and
more efficient liquor recovery, it is estimated that at least 10%
additional color reduction will occur. Thus, minimum lime and BATEA
controls should reduce raw waste color loads by over 80%. Applying
QQ% reduction to the subcategory RWL given above resulted in the color
values based upon annual averages. Variability factors of 1.5 and 3.0
which were based upon full scale operations of color removal
technologies at kraft mills for maximum 30 consecutive days and
maximum day to annual average, respectively, were used to determine
the effluent limitations. The RWL used in calculating the limitations
for BCT and Fine sutcategories was based upon 212.5 kg/kkg (425
Ibs/ton) which was an average of six mills manufacturing various
proportions of BCT papers, fine papers, and market pulp. This RWL was
669
-------
used because of the relatively large range of color RWL for mills
producing varying proportions of fine papers and market pulp.
Soda Subcategorv
The soda subcategory raw waste load used in developing costs and in
determining the BATEA effluent limitations was based upon mills 151
and 152. The average flow for mill 151 and the average BODJ5 RWL for
mill 152 are shown below:
FLow: 117.6 kl/kkg (28.2 kgal/ton)
BOD5: 34.0 kg/kkg (68.0 Ibs/ton)
Evaluation of the internal controls used at these mills and those
additional internal controls identified in Section VIII as BATEA
resulted in the following estimates of flow and BOD5_ reductions:
Flow: 20.85 kl/kkg (5.0 kgal/ton)
EOD5: 4.0 kg/kkg (8.0 Ibs/ton)
The TSS RWL demonstrated by mill 150 was used as the basis for the TSS
RWL even though mill 150 has closed because TSS data was unavailable
for mill 151 and mill 152 had very high TSS losses. The resulting RWL
used in determining the BATEA effluent limitations and costs are given
below:
Flow: 95.9 kl/kkg (23.0 kgal/ton)
EOD5: 30.0 kg/kkg (60.0 Ibs/ton)
TSS: 65.0 kg/kkg (130 Ibs/ton)
As discussed previously in Section VII, the application of internal
controls are generally specific for the reduction of one pollutant
parameter (BOD5 and TSS) or for the reduction of flow. However, there
are controls, such as use of the decker filtrate on the brown stock
washers, that reduce both flow and BOD5. These points are briefly
discussed here in support of the determination of the soda subcategory
RWL which used three mills as the basis for the three respective
parameters. The internal controls for TSS reduction are very specific
for reduction of the loss of TSS and thus it would be expected that
relationships between TSS and flow or BOD5 would not generally exist.
Similarly, inplant controls can be applied which reduce flow without
impacting BOD5 (i.e., cooling water segregation) or reduce BODJ5
without impacting flow (i.e.r more efficient liquor recovery). The
wide variations in the RWL from the soda mills indicates that the
inplant controls at each of the mills are specific for reduction of
one of these parameters. Thus, application of the BATEA inplant
controls would reduce the RWL to at least the level of control
indicated by the flow, BOD5, and TSS levels presently achieved by the
three respective mills. Further support for this analysis is that the
estimated BATEA RWL for the soda subcategory are similar to the
bleached kraft fine papers subcategory RWL as would be expected since
the manufacturing processes are similar at mills within the two
subcategories.
670
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Mill 152 presently achieves 28 mg/1 BOD5 with an aerated stabilization
basin of five days of detention time. Increasing the extent of the
biological treatment will probably be necessary for mill 152 to
achieve BPCTCA TSS limitations and in so doing improved BODj> reduction
should occur. The BATEA limitations are based upon BODj> levels of 15
mg/1 as demonstrated by bleached kraft mills. The level of 15 mg/1
wag selected as a conservative estimate of the capabilities of the
BATEA external technologies including biological treatment and
coagulation and filtration. It should be pointed out that the average
of the top eight bleached kraft mills was 13.5 mg/1 as shown in Table
219. The TSS effluent limitations were based upon 10 mg/1 as
discussed previously for the bleached kraft subcategories.
The color limitations for the soda subcategory were the same as the
bleached kraft BCT and fine papers subcategories because the soda
manufacturing process is similiar to these two subcategories and color
raw waste load data was not available for mills in the soda
subcategory.
Groundwood Suhcategories
GW: Chemi-Mechanical Subcategory
The raw waste load for the chemi-mechanical subcategory used in
determining the BATEA effluent limitations and the costs were based
upon mill 001 which had the following RWL after adjusting for
purchased pulp:
Flow: 84.7 kl/kkg (20.3 kgal/ton)
BOD5: 48.5 kg/kkg (97.0 Ibs/ton)
TSS: 23.3 kg/kkg (46.6 Ibs/ton)
More recent data for mill 001 has shown significant decreases in flow
accomplished by in plant control measures and was used as the basis
for the BATEA RWL. BOD5 data was unavailable for the most recent
period but it is estimated that BOD5 would be reduced by the
additional BATEA internals by 3.5 kg/kkg (7.0 Ibs/ton). The BATEA raw
waste load for mill 001 is given below:
Flow: 75.1 kl/kkg (18.0 kgal/ton)
BOD5: 45.0 kg/kkg (90.0 Ibs/ton)
TSS: 22.5 kg/kkg (45.0 Ibs/ton)
The groundwood chemi-mechanical limitations are based upon 100% chemi-
mechanical production; therefore, contributions from purchased pulp
and waste paper were removed. Calculating the RWL due to chemi-
mechanical pulp and paper manufacturing, the basis for the BATEA
limitations was derived.
Flow: 91.3 kl/kkg (21.9 kgal/ton)
BOD5: 79.5 kg/kkg (159 Ibs/ton)
TSS: 22.5 kg/kkg (45 Ibs/ton)
During the most recent data period for which data were available
(April through August 1974), mill 001 has achieved an average of 5.6
671
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mg/1 BOD5 and 10.9 mg/1 TSS with a treatment system consisting of ai
aerated stabilization basin followed by chemical addition
coagulation, and clarification. The BATEA effluent limitations wer
based upon a reduction in the BOD5 concentration from 35 mg/1 (BPCTCA
to 30 mg/1 (estimated concentration for the best mill) and th
addition of filtration to achieve final effluent concentrations fo
BODJ5 of 24 mg/1 and TSS of 10 mg/1. These values are based upon
100% chemi-mechanical pulp and paper process.
GW: ihermo-mechanical Sutcategory
The thermo-mechanical subcategory raw waste load was based up<
estimates BOD5 loads for companies starting new mills and waste wat<
data developed from thermo-mechanical mills in Sweden. Data for
thermo-mechanical mill in Sweden showed flows and BOD5 loads of 17.
to 27.2 kl/kkg (4.1 to 6.6 kgal/ton) and 21.3 kg/kkg (42.5 Ibs/toi
were reported. Since the thermo-mechanical process will be install*
at existing GW Fine and CMN mills, the higher flow rate of GW CMN w«
transferred to the thermo-mechanical subcategory. Modified existii
plants are not expected to be able readily achieve the flow rates <
the new thermo-mechanical mills in Sweden. The following RWL valu<
were therefore selected as conservative estimates of the thermc
mechanical subcategory RWL:
Flow: 78.3 kl/kkg (19.0 kgal/ton)
BOD5: 26.5 kg/kkg (53.0 Ibs/ton)
TSS: 25.0 kg/kkg (50.0 Ibs/ton)
There are very few mills in this country presently using the thermc
mechanical pulping process and effluent data is not available from ar
mill operating biological treatment facilities which has a significai
portion of the total pulp production produced by the thermo-mechanic?
process. As demonstrated by mill 001 in the chemi-mechanicc
subcategory which has a substantially higher RWL of 529 mg/1 ai
achieves a final effluent BODJ5 of 5.6 mg/1 (based upon 5 months <
data, April thru August) using biological treatment followed by
clarifloculator, and by several mills in the bleached kra:
subcategories wi.ere effluent BOD5 qualities of 10 -17 mg/1 a:
achievable with biological treatment and thereby the BOD5_ BAT:
effluent limitations were based upon 15 mg/1. The TSS limitatio
were based upon 10 mg/1 as discussed previously.
GW: Fine Papers Sutcategory
The groundwood: fine papers subcategory raw waste load was based up
mill 13 which had a flow of 83.0 kl/kkg (19.9 kgal/ton) and a r
waste BOD5 of 13.5 kg/kkg (27.0 Ibs/ton). Two mills, 19 and 21, h
flows less than mill 13 but the C & F content of their final produ
was 35% and 20%, respectively, which could have the effect of loweri
their water use per kkg (ton) of product. Thus, the BATEA flow ra
was based upon mill 13. Evaluation of the inplant controls used
mill 13 and those additional controls identified as BATEA in Secti
VIII result in estimating that 74.9 kl/kkg (18.0 kgal/ton) w
achievable. Because mill 13fs BOD5 of 13.5 kg/kkg (27.0 Ibs/ton) w
significantly lower than the other mills with 10-15% C & F, the BAT
672
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raw waste BOD5 and TSS were estimated by the internal controls used by
mill 005 which used 10% C & F were evaluated. It was estimated that
the additional BATEA controls identified in Section VIII would reduce
the average BOD5 to 16.0 kg/kkg (32.0 Its/ton). The TSS raw waste
load was based on an estimate involving the TSS reduction capabilities
of the BATEA internal controls upon the average BPCTCA raw waste load.
It was estimated that the added controls could achieve at least 45.0
kg/kkg (90.0 Ibs/ton). Thus, the BATEA RWL are the following:
Flow: 74.9 kl/kkg (18.0 kgal/ton)
BOD5: 16.0 kg/kkg (32.0 Ibs/ton)
TSS: 45.0 kg/kkg (90.0 Ibs/ton)
Data for mill 005 shows that 13 mg/1 BODJ3 and 21 mg/1 TSS are
presently being achieved by the mill's aerated stabilization basin.
Addition of filtration systems will further decrease these levels.
The BATEA effluent limitations were thereby based upon 13 mg/1 BOD^
and 10 mg/1 TSS.
GW: CMN papers Subcategory
The groundwood: CMN papers subcategory was based upon an average of
mills 009 and 014 raw waste loads because of the relatively wide
spread between the raw waste loads, i.e. mill 009's flow and BOD5 RWL
was 52.9 kl/kkg (12.7 kgal/ton) and 19.6 kg/kkg (39.2 Ibs/ton) whereas
mill 014 «s RWL was 107.6 kl/kkg (25.8 kgal/ton) and 12.0 kg/kkg (24.0
Ibs/ton) . Evaluation of the in plant controls used by these mills and
those BATEA internal controls identified in Section VIII resulted in
selection of the following RWL:
Flow: 79.0 kl/kkg (19.0 kgal/ton)
BODJ5: 16.0 kg/kkg (32.0 Ibs/ton)
TSS: 45.0 kg/kkg (90.0 Ibs/ton)
Since none of the mills in the GW: CMN Subcategory have biological
treatment, the BOD5 concentration used for the BODj> effluent
limitations was based upon mill 014 in the GW: fine papers
subcategory which was achieving 13 mg/1 BOD5. The TSS effluent
limitation was based upon 10 mg/1 as discussed previously.
Groundwood subcategories Zinc Limitations
The zinc limitations for the groundwood subcategories are based upon
the BATEA flow values and 0.35 mg/1 zinc as in the BPCTCA limitations.
Sulfite Subcategories
Papergrade Sulfite Subcategory
The BATEA raw waste load for the papergrade sulfite subcategory was
based upon mill 062 which had raw waste flow and BOD5 values of 193
kl/kkg (46.2 kgal/ton) and 74.5 kg/kkg (149 Ibs/ton), respectively.
Mill 062 was determined to be the most representative papergrade
sulfite mill using BATEA inplant controls, some of which include
vacuum drum pulp washing, full SSL recovery, and surface condensers.
673
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Evaluation of the inplant controls in use by mill 062 and furthe:
possibilities of RWL reduction by installation of BATEA interna.
controls not in use by mill 062 resulted in the following BATEA RWL:
Flow: 167 kl/kkg (40.0 kgal/ton)
BOD5: 75.0 kg/kkg (150 Ibs/ton)
TSS; 75.0 kg/kkg (150 Ibs/ton)
The above TSS RWL was based
unavailable from mill 062.
upon mill 066 since TSS data wa
The effluent limitations were based upon BOD5 and TSS concentratioi
of 30 mg/1 and 10 mg/1, respectively. The application of filtratic
technologies achieves TSS levels in final effluents of 5 to 10 mg/
and removes 20-25% of the remaining BOD5.
Improved operation of the biological treatment facilities and tl
application of filtration technologies should allow effluent BO1
levels of 30 mg/1 to be achieved as shown by the relations!*.'
determined in Section VII. While some mills have stated that BOD5_ R\
of 75,0 kg/kkg (150 Ibs/ton) will be difficult to achieve even thou<
mill 062 is presently achieving that level, the mills can use mo:
effective external treatment to achieve the effluent limitation;
This is demonstrated by mill 053 which has a BOD5 RWL of 96.0 kg/kl
(192 Ibs/ton) and achieves a final effluent BOD5> of 3.45 kg/kkg (6.
Ibs/ton) using effective primary and biological treatment systei
which is substantially less than 5.0 kg/kkg (10.0 Ibs/ton) on whi<
the effluent limitations were based.
Papergrade Sulfite Market Pulp Subcategory
The BATEA raw waste load for the papergrade sulfite market pu.
subcategory was based upon evaluation of the internal controls in u
by mill 056 and estimating further reductions associated with BAT
internal controls not presently in use by mill 056. The BATEA RWL a:
shown below:
Flow: 188 kl/kkg (45.0 kgal/ton)
BOD5: 100 kg/kkg (200 Ibs/ton)
TSS: 30 Ibs/ton (60 Ibs/ton)
The BOD5_ and TSS effluent limitations were based upon 30 mg/1 and
mg/lr respectively, as discussed above for the papergrade sulfi
subcategory.
Low Alpha Dissolving Sulfite Pulp Subcategory
The BATEA raw waste load for the low alpha dissolving sulfite pv
subcategory was based upon an evaluation of the inplant controls
use at mill 512 and an estimation of the RWL reductions that could
achieved by application of BATEA inplant controls not presently in i;
by mill 512. The present RWL at mill 512 was the following:
Flow: 203 kl/kkg (48.6 kgal/ton)
BOD5: 136.5 kg/kkg (273 Ibs/ton)
674
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The above evaluation resulted in the following reductions in the
present RWL at mill 512:
Flow: 19.2 kl/kkg (4.6 kgal/ton)
BOD5: 21.5 Ibs/ton (43.0 Ibs/ton)
Thus, the BATEA RWL for the low alpha dissolving sulfite pulp
subcategory were the following:
Flow: 183 kl/kkg (44.0 kgal/ton)
BOD5: 115 kg/kkg (230 Ibs/ton)
The BATEA RWL TSS was based upon mill 511 since TSS data was not
available for mill 512. The TSS RWL was 85.0 kg/kkg (170 Ibs/ton).
The BOD5 and TSS effluent limitations were based upon 35 mg/1 and 10
mg/1, respectively. As discussed previously, the application of
filtration technologies results in TSS levels of 5 to 10 mg/1 in final
effluents and a 20 to 25% reduction in BOD5, An extensive biological
treatment pilot plant operation at mill 512 resulted in an average
final effluent BOD5 concentration of 47 mg/1. The relationship
determined in Section VII, the pilot plant data, and the application
of filtration shows that a level of 35 mg/1 BOD£> is achievable. Thus,
the BOD5 final effluent concentration of 35 mg/1 was used as the basis
of the effluent limitations.
High Alpha Dissolving Sulfite Pulp Sutcategory
The BATEA raw waste load for the high alpha dissolving sulfite pulp
subcategory was based upon mill 403 which is presently the one mill of
the three in the subcategory which has full SSL recovery using vacuum
drum washing and surface condensors. The present RWL at mill 403 is
shown below:
Flow: 258 kl/kkg (61.8 kgal/ton)
BOD5: 244 kg/kkg (487 Ibs/ton)
Evaluation of the inplant controls in use by mill 403 and estimating
the RWL reduction associated with the application of additional BATEA
controls not presently in use by the mill resulted in the following
BATEA RWL:
Flow: 172 kl/kkg (41.2 kgal/ton)
BOD5: 212.5 kg/kkg (425 Ibs/ton)
The BATEA controls at mill 403 include segregation of BODji bearing
streams from TSS bearing streams and cooling waters. The above flow
estimate accounts for the BOD5 bearing streams.
The fiber bearing streams not containing appreciable amounts of BODj[
are estimated to be 85.9 kl/kkg (20.6 kgal/ton) which is the
difference between the present RWL flow and the above BATEA flow. In
addition, it is estimated that 85.9 kl/kkg (20.6 kgal/ton) of non-
contact cooling waters are discharged from mill 403.
675
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The BOD5 and TSS effluent limitations were based upon 45 mg/1 and 10
mg/1, respectively. The application of filtration technologies
results in TSS levels in the final effluents of 5 to 10 mg/1 and
reduction of BOD5 by 20 to 25%. The BOD^ BATEA RWL is 1,237 mg/1
which is higher than the BPCTCA RWL of 986 mg/1. The relationship
determined in Section VII between influent BODjj concentrations and
effluent BOD5 concentrations for biological treatment systems at
sulfite mills shows that 62 mg/1 BOD5 would be achieved with an
influent BOD5_ of 1,237 mg/1. Improved operation of the biological
treatment facilities should allow a final BOD5 of 60 mg/1 or less to
be achieved and application of filtration technologies should reduce
the final effluent BOB5 to at least 45 mg/1. The BOD5_ effluent
limitations were determined using 45 mg/1 and the above BATEA RWL flov
of 172 kl/kkg (**1.2 kgal/ton) whereas the TSS effluent limitations
were determined using 10 mg/1 and the above BATEA flow plus the flot
representing the fiber bearing streams which equaled 258 kl/kkg (61.8
kgal/ton) .
Deink Subcategory
The deink subcategory flow used as the basis for BATEA effluenl
limitations was based upon mill 217 which deinks all of its pulp.
However, the use of 25% clays and fillers in the paper by mill 217 ma\
result in a lower flow (kl/kkg (kgal/ton) than deink mills makinc
tissue papers. Since the use of clays and fillers do not contribute
significantly to flow. Mill 217 «s flow of 55 kl/kkg (13.2 kgal/ton)
was recalculated excluding clays and fillers from the production ir
order to be comparable to mills producing tissue papers which do no!
use clays and fillers. The resulting flow value for mill 217 is 73.'
kl/kkg (17.6 kgal/ton). As discussed in Section V, the deink ra\
waste BOD5 and TSS are related to the type of waste paper used, anc
therefore BATEA BOD5 and TSS raw waste loads used were the same usec
as for BPCTCA. Thus, the BATEA RWL are the following:
Flow: 73.4 kl/kkg (17.6 kgal/ton)
BODJ5: 82.5 kg/kkg (165 Ibs/ton)
TSS: 178.5 kg/kkg (357 Ibs/ton)
The BATEA effluent limitations were based upon BOD5 and TSS levels o:
20 mg/1. This level of BOD5 and TSS takes into account the high RW:
and the variabilities of RWL associated with deinking operations.
Non-Integrated Paper Mills Segment
N.I. Fine Papers Subcategory
The Nl fine papers sufccategories raw waste loads were developed b
evaluation of the raw waste loads at 10 mills in relation to th
extent of internal controls at each mill. Since flow is an indicate
of the extent of in plant controls at NI paper mills, the mills whic
achieved lower flow rates than the BPCTCA average of 62.4 kl/kkg (15.
kgal/ton) were arranged in ascending order as shown below:
Mill Flow BOD5 TSS
kl/kkg (kgal/ton) kg/kkg (Ibs/ton) kg/kkg (Ibs/
676
-------
284 25.8 (6.2) 7.6 (15.2) 30.4 (60.7)
261 26.3 (6.3) 8.7 (17.3) - ( - )
279 37.5 (9.0) - ( - ) - ( - )
255 37.9 (9.1) - ( - ) - ( - )
272 37.9 (9.1) 10.9 (21.8) - ( - )
276 39.2 (9.4) 19.2 (38.3) 38.5 (76.9)
257 40.0 (9.6) 9.2 (18.3) - ( - )
266 49.2 (11.8) 12.8 (25.6) (22.9) (45.7)
250 53.8 (12.9) - ( - ) - ( - )
402 57.5 (13.8) 7.5 (15.0) (43.6) (87.1)
Ave 40.4 (9.7) 10.8 (21,6) 33.8 (67.6)
Examination of the flow values above show two definite breaks, below
37.5 kl/kkg (9.0 kgal/ton) and above 40.0 kl/kkg (9.6 kgal/ton).
The BATEA flow was thereby based upon an average of those mills within
that range, mills 279, 255, 272, 276, and 257. The average flow rate
was 38.3 kl/kkg (9.2 kgal/ton) which was used in determining the BATEA
effluent limitations and in determining the costs. The BATEA BOD5
raw waste load of 9.5 kg/kkg (19.0 Ibs/ton) was based upon an average
of all the mills presented above excluding mill 276 whose BOD5_ was
much higher than all of the other values. Because of a lack of data,
the BATEA TSS raw waste load of 30.0 kg/kkg (60.0 Ibs/ton) was
essentially the same as the BPCTCA TSS raw waste load. It should be
noted that this estimate was used for purposes of developing costs of
the BATEA external controls and does not necessarily reflect the
capabilities of the BATEA internal controls.
The BATEA effluent limitations were based upon 38.3 kl/kkg (9.2
kgal/ton) and BOD5 and TSS levels of 20 mg/1 and 10 mg/1,
respectively. BOD5 levels of 10 - 17 mg/1 have been shown to be
achievable by mills using biological treatment systems in other
subcategories. However, the effluent limitations were based upon a
conservative 20 mg/1. The rationale for the TSS level of 10 mg/1 has
been discussed previously.
NI Tissue Papers Subcategory
The BATEA raw waste load for the NJ tissue papers subcategory was
developed in a similar manner as the NI fine papers subcategory raw
waste load. The mills presently achieving lower flow rates than the
BPCTCA average of 95.7 kl/kkg (23.0 kgal/ton) were arrayed in
ascending order as shown below:
Mill Flow BOD5 TSS
kl/kkg (kgal/ton) kg/kkg (Ibs/ton) kg/kkg (Ibs/ton)
306 43.4 (10.4) - ( - ) - ( - )
252 48.0 (11.5) - ( - ) - ( - )
302 50.9 (12.2) 11.8 (23.5) - ( - )
208A 61.3 (14.7) 22.9 (45.7)* 72.5 (145)
315 66.3 (15.9) 8.7 (17.4) - ( - )
309A 69.6 (16.7) 14.7 (29.3)* - ( - )
677
-------
326 72.6 (17.4) - ( - ) - ( - )
259A 73.8 (17.7) 9.6 (19.2) 32,2 (64.3)
Ave 60.5 (14.5) 10.0 (20.0) - ( - )
*Not included in average
The BATEA flow was thus an average of eight mills with better than the
BPCTCA average flow rate. The BOD5 of 10.0 kg/kkg (20.0 Ibs/ton) was
based upon three of the above eight or.ills that were achieving better
than the average EPCTCA BOD5_ raw waste load were used as the basis for
the BATEA BOD5 raw waste load. The TSS raw waste load of 28.0 kg/kkg
(56.0 Ibs/ton) was based upon an average of mills 259A, 310, and 308
whose TSS levels demonstrated relatively high control of TSS.
The BATEA effluent limitations were based upon 60.5 kl/kkg (14.5
kgal/ton) and BOD5 and TSS levels of 20 mg/1 and 10 mg/lr
respectively. The rationale for selection of the BOD5_ and TSS levels
was as previously discussed for the NI fine papers subcategory.
NI Tissue Papers (fWP) Subcategory
The NI Tissue Papers (fwp) Subcategory BATEA flow was based upon the
average of the best two mills (of the four mills surveyed). Flow
rates for mill 330, 79.2 kl/kkg (19.0 kgal/ton), and mill 313, 27.9
kl/kkg (6.7 kgal/ton) were averaged to obtain the BATEA flow basis of
53.8 kl/kkg (12.9 kgal/ton). The BOD5 and TSS raw waste loads used in
developing the costs presented in Section VIII were based upon mills
330 and 313. The BATEA effluent limitations are based upon BOD5 and
TSS levels of 20 mg/1 and 10 mg/1, respectively. The rationale for
selection of the BOD5 and TSS levels was previously discussed for the
NI fine papers subcategory.
678
-------
SECTION XI
NEK SOURCE PERFORMANCE STANDARDS (NSPS)
INTRODUCTION
This level of technology is to be achieved by new sources. The term
"new source" is defined in the Act to mean "any source, the construc-
tion of which is commenced after the publication of proposed regula-
tions prescribing a standard of performance."
The New Source Performance Standards (NSPS) are predicated on the
application of the Best Available Demonstrated Technology (BADT).
These standards are thus not based upon an average of the best
performance within a given subcategory under study, but have been
determined by identifying the best demonstrated control and treatment
technology employed by mills in given subcategory. Consideration was
also given to:
a. The type of process employed and process changes;
b. Operating methods;
c. The engineering aspects of the application of control
technologies;
d. the cost of application (including energy requirements);
e. The non-water quality environmental impact;
f. Use of alternative raw materials and mixes of raw materials;
g. Use of dry rather than wet processes (including substitution
of recoverable solvents for water);
h. Recovery of pollutants as by-products.
EFFLUENT REDUCTIONS ATTAINABLE THROUGH THE APPLICATION OF NEW SOURCE
PERFORMANCE STANDARDS
Based upon the information available to the Agency, the point source
discharge standards for each identified pollutant are shown in Table
220 and can be attained through the application of appropriate
internal and external control technologies.
The average of daily values for 30 consecutive days should not exceed
the maximum 30 consecutive days average standards shown in Table 220.
The value for any one day should not exceed the daily maximum
standards shown in the table. The standards shown are in kilograms of
pollutant per metric ton of production (pounds of pollutant per ton of
production). Effluents should always be within the pH range of 5,0 to
9.0.
Production in kkg (tons) is defined as annual tonnage produced from
pulp dryers (in the case of market pulp) and paper machines (for
paper/ board) divided by the number of production days in the 12-month
period. Pulp production is to be corrected, if necessary, to the "air
dry" moisture basis.
679
-------
Subcategory
TABLE 220
NEW SOURCE PERFORMANCE STANDARDS
kg/kkg(1bs/ton)
Maximum 30 Day Average
Maximum Day
BOD5
Dissolving Kraft
Market Kraft
BCT Kraft
Fine Kraft
Papergrade Sulfite
Market Sulfite
Low Alpha
Dissolving Sulfite
High Alpha
Dissolving Sulfite
GW-Chemi -Mechanical
GW-Thermo-Mechanical
GW-CMN Papers
GW-Fine Papers
Soda
Deink
NI Fine Papers
NI Tissue Papers
NI Tissue Papers(FWP)
pH for all
Subcategory
GW:Chemi -mechanical
GW:Thermo-mechanical
GW:CMN Papers
GW:Fine Papers
6
2
3
2
4
4
11
13
3
2
2
1
3
3
1
2
1
.1 (12.2)
.65( 5.3)
.7 ( 7.4)
.55( 5.1)
.65( 9.3)
.65( 9.3)
.15(22.3)
.8 (27.6)
.9 ( 7.8)
.3 ( 4.6)
.0 ( 4.0)
.9 ( 3.8)
.15( 6.3)
.9 ( 7.8)
.35( 2.7)
.15( 4.3)
.9 ( 3.8)
8.
2.
5.
3.
2.
2.
10.
9.
3.
3.
3.
3.
4.
4.
1.
2.
1.
subcategories shall be within
Zinc *
TSS
35(16
9 ( 5
0 (10
75 ( 7
9 ( 5
9 ( 5
0 (20
45(18
3 ( 6
15( 6
15( 6
0 ( 6
3 ( 8
0 ( 8
4 ( 2
2 ( 4
95( 3
the
BOD
.7)
.8)
.0)
.5)
.8)
.8)
.0)
.9)
.6)
.3)
.3)
.0)
.6)
.0)
.8)
.4)
.9)
range
n
5
7
4
8
8
21
26
7
4
3
5
6
7
2
4
3
5.0 to
Maximum 30 Day Average
kg/kkg(lbs/ton)
0.048 (0.096)
0
0
0
.0455(0.091)
.0455(0.091)
.044 (0.088)
.75(23
.15(10
.05(14
.95( 9
.95(17
.95(17
.45(42
.5 (53
.5 (15
,45( 8
.85( 7
.6 ( 7
.0 (12
.5 (15
.6 ( 5
.15( 8
.7 ( 7
9.0.
.5)
.3)
.1)
.9)
.9)
.9)
.9)
.0)
.0)
.9)
.7)
.4)
.0)
.0)
.2)
.3)
.4)
TSS
15.5 (31
5
9
7
5
5
18
17
6
5
5
5
7
7
2
4
3
.35(10
.3 (18
.0 (14
.35(10
.35(10
.6 (37
.6 (35
.15(12
.85(11
.85(11
.6 (11
.95(15
.45(14
.6 ( 5
.1 ( 8
.65( 7
.0)
.7)
.6)
.0)
.7)
.7)
.2)
.2)
.3)
.7)
.7)
.2)
.9)
.9)
.2)
.2)
.3)
Maximum Day
kg/kkg(lbs/ton)
0.095 (0.19)
0.09
0.09
0.09
(0
(0
(0
.18)
.18)
.18)
*Applicable only to mills using zinc hydrosulfite.
680
-------
Performance standards will be established for ammonia nitrogen for
ammonia base mills in the sulfite and dissolving sulfite subcategories
at a later date. No specific standard has been developed because of
the limited availability at this time of meaningful data. Indications
are that discharges in the range of 1.0-3.0 kg/kkg (2.0-5.0 Ib/ton)
can occur. No technology for the removal of nitrogen has been applied
within the pulp and paper industry.
Performance standards for color established for BATEA are not
included for NSPS since the technology has not been demonstrated to
the degree necessary in terms of engineering and performance for the
subcategories included in these regulations.
IDENTIFICATION OF TECHNOLOGY FOR NEW SOURCE PERFORMANCE STANDARDS
The technology available for New Source Performance Standards consists
of the Best Available Demonstrated Technology (BADT) which includes
extensive application of internal control technologies and external
waste water treatment practices as identified in Sections VII and
VIII. Technology for nitrogen and color removal has not been
demonstrated to the degree necessary for application to the effluents
generated by mills in the pulp and paper industry. Such technologies,
therefore, are not included among those required to achieve NSPS.
BADT technology does include the utilization of mechanical
clarification and chemical coagulation equipment following biological
treatment and prior to discharge. The effectiveness of this external
technology has been demonstrated by at least one mill included in this
study. It should be pointed out that filtration of biological
treatment effluents is not included as a technology for NSPS because
filtration of biological treatment effluents has not been fully
demonstrated to the degree necessary at this time for general
application to new pulp and paper mills
Excluding the nitrogen and color removal technologies it is expected
that new source mills will be able to realize maximum efficiency in
the application of Best Available Demonstrated Technology. New source
mills have an advantage over existing mills in that implementing
internal control measures such as recovery, recycle, reuse, and spill
control systems can be more readily incorporated at the initial
engineering design stage than into existing mills.
RATIONALE FOR SELECTION OF TECHNOLOGY FOR NEW SOURCE PERFORMANCE
STANDARDS
Type of Process Employed and Process Changes
No new in-plant processes are proposed as a means of achieving New
Source Performance Standards for the sutcategories studied. It will
be mandatory, however, to use the well-known concepts associated with
selective water use, cascading reuse, and water segregation practices
at the engineering design stage if NSPS are to be achieved by a new
production facility.
681
-------
Operating Methods
Significant revisions in operating methods, both in-plant and at th
waste water treatment facility, beyond those normally practiced
mills representative of BPCTCA will te necessary. These improvemen
are not beyond the scope of well-trained personnel, and are current
being practiced in other industries. The primary areas of operation
change will be in the assignment of supervisory responsibility for t
performance of recycle, reuse, and spill control systems, as well
for achieving optimal performance of waste water treatment facilitie
Engineering Aspects of the Application of Control Technologies
Much of the technology to achieve these performance standards is pra
ticed within the pulp and paper industry by outstanding mills in
given subcategory. The technology level of the best availab
demonstrated technology will necessitate sophisticated monitorin
sampling, and control programs, as well as properly trained personne
Cost of Application Energy Reguirements)
The total projected costs of NSPS are shown in Tables 151 through 1
of Section VIII. These costs include both internal control a
external waste treatment improvements incorporated in the engineeri
design of the plant. They are based on 360 days of production p
year.
The energy reguirements associated with the application of polluti
control technologies are developed in Section VIII and shown in Tabl
197 to 201.
Non-water Quality Environmental Impact
The technology cited will not create any significant increase
odors, or in noise levels beyond those observed in well-design
municipal waste water treatment systems which currently are bei
approved by the federal government for construction in populat
areas. Further, no hazardous chemicals are required as part of th
technology. Further discussion of the non-water environmental impac
associated with the BADT is presented in Section VIII.
Use of Alternative Raw Materials and Mixes of Raw Materials
The raw materials reguirements for a given mill in each of t
subcategories studied do vary, depending upon supply and demar
desired end product, and other conditions. However, alteration of r
materials as a means of reducing pollutants is not considered feasit
over the long term even though such a change could possibly reali
benefits of short duration in a given instance. A possible except!
to this could be the development of alternatives for the use
ammonia as a base if an effective and economical method for removal
nitrogen does not become available through further study.
682
-------
Use of Dry Rather Than Wet Processes (Including Substitution of
Recoverable solvents for Water)
For the subcategories studied, it was determined that technology for
dry pulping or papermaking processes does not exist nor is it in a
sufficiently viable experimental stage to be considered here.
Recovery of Pollutants as Byproducts
As discussed in Sections VII and VIII of this report, recovery of some
potentially polluting materials as by-products is economically
feasible and is practiced to a limited extent by mills included in
this study. It is anticipated that these performance standards will
motivate increased research on recovering other materials for by-
product sale the recovery of which is not presently economically
feasible.
RATIONALE FOR SELECTION OF NEW SOURCE PERFORMANCE STANDARDS
The NSPS are based upon raw waste loads presently being achieved by
the best mill or mills within each subcategory and the application of
the best available demonstrated technology (BADT) presently being
operated by mills in each respective sutcategory. Where no mills are
operating treatment systems representative of BADT in a subcategory,
the standards are based upon the subcategories treating similar waste
waters and using technology representative of BADT. The NSPS were
determined use raw waste flow values and achievable effluent BOD5 and
TSS concentrations as demonstrated by the application of BADT. In
determining the appropriate achievable BOD5 levels which were used as
the basis of the BODji standards, the raw waste BOD5 levels were
carefully evaluated in order to take into account any impacts of the
raw waste BOD5 upon the final effluent BODf> levels. The BADT for all
subcategories includes internal controls, biological treatment, and
chemical addition, coagulation, and clarification technologies. The
TSS NSPS were based upon an effluent level of 20 mg/1 which has been
demonstrated to be achievable using chemical addition, coagulation,
and clarification technologies which also reduce the BOD5> levels in
biological treatment effluents by 20 to 25%.
It should be pointed out that no color standards were developed for
the bleached kraft and soda subcategories because the color removal
technology has not been fully demonstrated at this time. In addition,
the TSS standards were based upon chemical addition, coagulation, and
clarification technologies instead of filtration, because filtration
technologies treating biological treatment effluents which were
included in BATEA have not been demonstrated in the pulp and paper
industry.
Tables 221 and 222 summarize for each subcategory the BADT raw waste
loads and the flow, BOD5, and TSS values used as the basis of the
NSPS, respectively. The annual average values were multiplied by the
variability factors shown in Table 223 in order to determine the
maximum 30 consecutive days and iraximum day standards. The
determination of variability factors were discussed in Section VII.
683
-------
TABLE 221
SUBCATEGORY RAW WASTE LOADS
BEST AVAILABLE DEMONSTRATED TECHNOLOGY
(NSPS)
Subcategory
FLOW
k1/kkg(kgal/ton)
BOD5
kg/kkg(1bs/ton)
TSS
kg/kkg(1bs/ton) mg/
BK:Diss
BK:Mkt
BK:BCT
BK:Fine
Soda
GW:CMP
GW:TMP
GW:Fine
GW:CMN
Sulfite: Paper
Sulfite-.Mkt
Low Alpha
High Alpha
Deink
NI Fine
NI Tissue
NI Tissue (FWP)
229 (55.0)
79.2 (19.0)
138 (33.0)
103 (24.8)
117 (28.0)
91.3 (21.9)
86.3 (20.7)
83.0 (19.9)
86.3 (20.7)
79.2 (19.0)
79.2 (19.0)
157 (37.6)*
172 (41.2)**
73.4 (17.6)
38.4 ( 9.2)
60.5 (14.5)
53.8 (12.9)
40.0 ( 80.0)
27.5 ( 55.0)
29.5 ( 59.0)
22.0 ( 44.0)
34.0 ( 68.0)
79.5 (159 )
28.0 ( 56.0)
13.15( 26.3)
16.0 ( 32.0)
96.0 (192 )
96.0 (192 )
130 (260 )
244 (487 )
82.5 (165 )
9.5 ( 19.0)
10.0 ( 20.0)
13.0 ( 26.0)
174
347
214
213
291
871
324
158
185
1212
1212
829
1417
1124
248
165
242
87.0 (174 )
72.5 (145 )
53.0 (106 )
64.5 (129 )
65.0 (130 )
22.5 ( 45.0)
48.5 ( 97.0)
41.4 ( 82.8)
45.0 ( 90.0)
80.0 (160 )
80.0 (160 )
85.0 (170 1
85.0 (170 )
178.5 (357 )
30.0 ( 60.0)
28.0 ( 56.0)
110.5 (221 )
37
91
38
62
55
24
56
49
52
101
101
30
33
243
78
46
205
* BOD5 flow only, total flow = 275 kl/kkg (66.0 kgal/ton)
** BOD5 flow only, total flow = 258 kg/kkg (61.8 kgal/ton)
684
-------
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68S
-------
Table 223
BADT Variability Factors
Bleached Kraft Soda, Groundwood, Sulfite, Deink,
NI Fine Papers, and NI Tissue (fwp) Subcategories
Parameter Maximum 30 Days Maximum Day
BOD5_ 1.78 3.42
TSS 1.82 3.38
NI Tissue Papers Subcategory
Parameter Maximum 30 Days Maximum Day
BOD5_ 1.79 3.25
TSS 1.76 3.60
686
-------
Bleached Kraft Subcategories
Bleached Kraft Dissolving Pulp Subcategory
The raw waste load used as the basis for the NSPS for the bleached
kraft dissolving pulp subcategory was based upon mill 127 which has
the raw waste load shown below:
Flow: 230 kl/kkg (55.1 kgal/ton)
BOD5: 40.0 kg/kkg (80.0 Ibs/ton)
TSS: 87.0 kg/kkg (174 Ibs/ton)
Mill 127 is presently achieving a final effluent BOD5 value of 24 mg/1
with an influent raw waste BOD5 value of 174 mg/1 using an aerated
stabilization pond. Table 219 in Section X presents influent and
effluent BODJ5 data for bleached kraft mills considered to represent
the best of the best in effluent qualities. As shown in the table,
the eight mills achieve final effluent BOD5 levels averaging less than
14 mg/1 with an average BOD5 raw waste load of 201 mg/1. Improved
operation of the biological treatment facilities at mill 127 and the
application of chemical addition, coagulation, and clarification which
removes 20 to 25% of the remaining EOD5 should result in effluent
levels of 15 mg/1 of BOD.5. In addition, chemical addition,
coagulation, and clarification will reduce TSS levels to 20 mg/1 in
the final effluent.
The NSPS were therefore based upon the following:
Flow: 229 kl/kkg (55.0 kgal/ton)
EOL5: 15 mg/1
TSS: 20 mg/1
The above values were used to determine annual average values for BODI5
and TSS which were multiplied by the variability factors in Table 223
in order to determine the maximum 30 consecutive days and maximum day
standards.
Bleached Kraft Market Pulp Subcategory
The raw waste load used as the basis for the NSPS for the bleached
kraft market pulp subcategory were based upon mill 140 which has the
following raw waste load:
Flow: (18.9 kgal/ton)
BOD5: (55.4 Ibs/ton)
TSS: (145 Ibs/ton)
The external treatment system at irill 140 consists of an aerated
stabilization basin with approximately 21 days of detention time as
shown in Figure 44 in Section VII. However, the final effluent BOD5
level being achieved during the period for which data were available
averaged 98 mg/1 and it appears that the ASB was underaerated. The
mill has added additional aerators to ASB during more recent
operations. Two other bleached kraft market pulp mills, mills 130 and
114, use ASBs to achieve effluent BOD5 levels of 11 mg/1 and 26 mg/1.
687
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respectively. The average raw waste BOD5 for the two mills was 2(
mg/1 which is less than the NSPS bleached kraft market pu
subcategory BOD5 raw waste level of 317 mg/1. Mill 138 (20% mark
pulp, 80% BCT papers) uses an ASB to achieve final effluent BO
levels averaging 28 mg/1 with a raw waste BODjj level of 375 mg/1 whi
is slightly higher than the average subcategory BOD5 level of 3
mg/1. Based upon effluent reductions as demonstrated at mill 138, t
subcategory raw waste load, and applying chemical additio
coagulation, and clarification which rerroves 20-25% of the remaini
BOD5 in the biological treatment effluent, the BOD5 NSPS were bas
upon 19 mg/1. The 1SS NSPS were based upon 20 mg/1 becau
application of chemical addition, coagulation, and clarificati
results in effluent levels of 20 mg/1.
The NSPS were therefore based upon the following:
Flow: 79.2 kl/kkg (19.0 kgal/ton)
BOD5: 19 mg/1
TSS: 20 mg/1
The above values were used to determine annual average BOD5 and T
levels which were multiplied by the variability factors in Table 2
to determine the maximum 30 consecutive days and daily maxim
standards.
Bleached Kraft BCT Papers Subcategory
The raw waste load for the bleached kraft BCT papers subcategory vv
based upon mill 111 which had the following raw waste load:
Flow: 137 kl/kkg (32.9 kgal/ton)
BOD.5: 29.7 kg/kkg (59.3 Ibs/ton)
TSS: 53.0 kg/kkg (106 Ibs/ton)
Several mills in Table 52 in Section V have raw waste flow values le
than mill 111 but the other mills produce some market pulp in additi
to BCT papers. Mill 111 is therefore the most representative mi
producing BCT papers.
The treatment system at mill 111 consist of an ASB which achiev
effluent BOD5 levels averaging 22 mg/1. Two bleached kraft mil
producing BCT papers are shown in Table 219 which presents data f
mills with external treatment systems achieving effluent leve
considered to be the "best of the best." Mills 117 and 105 achie
average BODJ3 final effluent levels of 12 mg/1 and 16 mg/
respectively, with an average of 14 mg/1. The average BOD_5 raw was
load for the two mills was 185 mg/1 which is less than the Bf
bleached kraft BCT papers subcategory raw waste BODJ5 of 214 mg/
Improved operation of mill Ill's biglogical treatment system
comparable effluent reduction effectiveness as mills 117 and 105 c
application of chemical addition, coagulation, and clarification wh:'
reduces the remaining BOD5 in biological treatment effluents by 20
25% will allow achievement of 15 mg/1 BOD5. As discussed previous!
chemical addition, coagulation, and clarification will achie
effluent TSS levels averaging 20 mg/1.
688
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The NSPS were therefore based upon the following:
Flow: 138 kl/kkg (33.0 kgal/ton)
BOD5: 15 mg/1
TSS: 20 mg/1
The above values were used to determine annual average BODj> and TSS
levels which were multiplied by the variability factors shown in Table
223 in order to determine the maximum 30 consecutive days and maximum
day standards.
Bleached Kraft Fine Papers Subcategory
The raw waste load for the bleached kraft fine papers subcategory was
based on the following mills:
Mill Flow BODJ5 TSS
kl/kkg (kgal/ton) kg/kkg fibs/ton) kg/kkg (Ibs/ton)
118 107 (25.7) 20.3 (40.6)
119 97.2 (23.3) 23.4 (46.7) 46.5 (92.9)
134 106 (25.4) 35.9 (71.8)* 82.5 (165)
Average 103 (24.8) 21.9 (43.7) 64.5) (129)
*Not included in average
The BOD5_ raw waste load of mill 134 was not included in the
subcategory average because it was substantially higher than the raw
waste loads being achieved through inplant controls at mills 118 and
119.
As shown in Table 219 in Section X, five bleached kraft mills
producing fine papers achieve effluent levels representing the "best
of the best." The NSPS were based upon the BOD5_ levels presently being
achieved by the five mills which are shewn below:
RWL Final Effluent
Mill BODS (mq/1) BODS (rnq/1)
101 186 9
119 240 11
112 224 13
106 204 18
107 264 18
Average 224 14
The average subcategory RWL was 213 mg/1 and since the average of the
above mills was 224 mg/1, no adjustment for achievable effluent
concentrations was necessary. The above mills are presently achieving
effluent BOD5 levels which are better than most other bleached kraft
mills with comparable raw waste loads and because of this, the BOD5>
NSPS were based upon 14 mg/1. The level of 14 mg/1 BOD5 has been
689
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demonstrated to the achievable even without the added 20 to 25!
reduction in BOD5 which is achieved by application of chemica!
addition, coagulation, and clarification of biological treatmen1
effluents. In addition chemical addition, coagulation, an
clarification results in TSS effluent levels of 20 mg/1.
The NSPS were therefore based upon the following:
Flow: 103 kl/kkg (24.8 kgal/ton)
BODj>: 14 mg/1
TSS: 20 mg/1
The above values were used to determine annual average levels of BOD
and TSS which were multiplied by the variability factors in Table 22
to determine the maximum 30 consecutive day and daily maximv
standards.
Soda Subcategory
The BADT raw waste load for the soda subcategory was based primaril
upon mill 151 which the following raw waste load:
Flow: 118 kl/kkg (28.2 kgal/ton)
BOD5: 52.5 kg/kkg (105 Its/ton)
TSS data were unavailable for mill 151 and while the above flow valv
represents good inplant controls, the raw waste BOD5 represents
higher level than should be achieved using the inplant contro]
identified in Sections VII and VIII for new sources. Mill If
achieves a BOD5 raw waste load of 34.0 kg/kkg (68.0 Ibs/ton) whic
represents an acceptable level using inplant controls but has a n
waste flow of 170 kl/kkg (40.7 kgal/ton). The NSPS raw waste load we
based upon both mills and is shown belcw:
Flow: 117 kl/kkg (28.0 kgal/ton)
BOD5: 34.0 kg/kkg (68.0 Ibs/ton)
TSS: 65.0 kg/kkg (130 Ibs/ton)
The above TSS RWL was based upon mill 150 since the TSS RWL at mi;
151 was over twice the level achieved by mill 152 which represents
minimum of TSS inplant controls. Mill 152 presently achieves c
effluent BOD_5 averaging 28 mg/1 with an aerated stabilization basir
As discussed in Section VII, the primary clarifier and the ASB at mi;
152 were not representative of BPCTCA. Upgrading and improvi
operations of the treatment facilities at mill 152 and application <
chemical addition, coagulation, and clarification technologies whi<
reduce BOD5 in biological treatment effluents by 20 to 25% wou.'
result in an achievable BOD5 level of 15 mg/1. Chemical additio
coagulation, and clarification also reduces TSS levels to 20 mg/1.
The NSPS were therefore based upon the following:
Flow: 117 kl/kkg (28.0 kgal/ton)
BOD5: 15 mg/1
690
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1SS: 20 mg/1
The above values were used to determine annual average BOD5 and TSS
levels which were multiplied by the variability factors in Table 223
in order to determine the maximum 30 consecutive days and maximum day
standards.
Sulfite Subcategories
Papergrade Sulfite Sutcategory
The NSPS for the papergrade sulfite subcategory were based upon mill
053 which had the following raw waste load:
Flow: 79.2 kl/kkg (19.0 kgal/ton)
BOD5: 96.0 kg/kkg (192 Ibs/ton)
TSS: 80.0 kg/kkg (160 Ibs/ton)
Mill 053 is the newest existing papergrade sulfite mill, built in
1968, and produces tissue papers using inplant control technologies
which represent the best available demonstrated technology. Within
the process mill 053 uses two stages of vacuum drum pulp washing to
recover 95-98% of the spent sulfite liquor. The mill has segregated
process water systems for the pulp mill and for the paper mill and as
a result the waste waters from the two sources are treated in separate
treatment systems. The waste waters from the pulp mill are low in
volume and high in BOD5 concentration and are treated in an activated
sludge system. The waste waters from the paper mill are treated by
primary treatment since the BOD5_ in the waste waters is primarily
associated with the fibrous solids which are removed in primary
treatment. The combined discharge from both treatment systems
resulted in the following BOD5 and TSS values:
EOD5: 3.45 kg/kkg (6.9 Ibs/ton)
TSS: 7.45 kg/kkg (14.9 Ibs/ton)
Since mill 053 uses some purchased pulp in the manufacturing process
as a supplementary source of fiber, the raw waste and final effluent
flow, BODj>, and TSS values were adjusted to reflect on-site production
of 100% of the pulp used to make paper. This adjustment was necessary
because of the impact upon the waste water values when examined on a
kiloliters or kilograms per 1000 kilograms basis (kgal or Ibs per
ton). The above values of BOD5 and TSS correspond to the following
concentrations of 44 mg/1 and 94 mg/1, respectively. Application of
chemical additive, coagulation, and clarification should remove 20-25%
of the BOD5 and attain an TSS level of 20 mg/1. Thus, the NSPS were
based upon the following:
Flow: 79.2 kg/kkg (19.0 kgal/ton)
BOD5: 33 mg/1
TSS: 20 mg/1
The above values were used to determine annual average BODj> and TSS
levels which were multiplied by the variability factors in Table 223
691
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in order to determine the maximum 30 consecutive days and maximum
standards.
Papergrade Sulfite Market Pulp Subcategory
day
The papergrade sulfite market pulp sutcategory NSPS are the same as
the papergrade sulfite subcategory. As discussed in Section IV, the
major impact on sulfite mill raw waste loads is the degree of spent
liquor recovery and a new sulfite market pulp mill can include an
adequately sized recovery system which would minimize the raw waste
load. In addition, a new mill has the advantages of being able to
segregate the low volume, highly concentrated pulp mill waste waters
from the dilute white water system of the pulp dryers. Thus, similar
waste water systems and treatment systems as mill 053 can be installed
at new sulfite market pulp mills.
Low Alpha Dissolving Sulfite Pulp Subcategory
The NSPS raw waste load for the low alpha dissolving sulfite pulp
subcategory was based upon mill 511 which had the following raw waste
load:
Flow: 275 kl/kkg (66.0 kgal/ton)
BOD5: 130 kg/Jckg (260 Ibs/ton)
TSS: 92.5 kg/kkg (185 Ibs/ton)
Segregation of the BOD5 bearing waste waters from the TSS bearing
waste waters and cooling waters at mill 511 would allow a new mill to
treat the highly concentrated, low volume waste waters rather than
treating the entire mill effluent. The NSPS were thereby determined
using the following raw waste load for the BOD5 bearing streams:
Flow: 157 kl/kkg (37.6 kgal/ton)
EOD5: 130 kg/kkg (260 Ibs/ton)
The raw waste flow of the other waste waters was 118 kl/kkg (28. U
kgal/ton). The BADT TSS EWL was based on mill 511 which had a TSS RWL
of 85.0 kg/kkg (170 Ibs/ton).
The NSPS were determined using the relationship for sulfite waste
waters which was determined in Section VII. The influent BOD5 level
using the above values for segregated waste streams would be 829 mg/1
and application of biological treatment followed by chemical addition,
coagulation, and clarification which removes 20 to 25% of the BOD5_ in
the biological treatment effluent should result in an effluent BOD5_
level of approximately 40 mg/1. Chemical addition, coagulation, and
clarification also achieves effluent TSS levels of 20 mg/1.
The NSPS were therefore based upon the following:
Flow: 157 kl/kkg (37.6 kgal/ton)
BOD5: 40 mg/1
Flow: 275 kl/kkg (66.0 kgal/ton)
TSS 20 mg/1
692
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It should be pointed out that mill 512 had a comparable BOD5 raw waste
load to mill 511 and a substantially lower raw waste flow as showed in
Table 42 in Section V. However, information and data were unavailable
to determine the effluent raw waste values for segregating the waste
waters. The above values were used to determine annual average BOD5_
and TSS levels which were multiplied by the variability factors in
Table 223 in order to determine the maximum 30 consecutive days and
maximum day standards.
High Alpha Dissolving Sulfite Pulp Sutcategory
The NSPS for the high alpha dissolving sulfite pulp subcategory were
based upon segregation of BOD5 and TSS bearing streams from cooling
water streams similarly to the low alpha dissolving sulfite pulp
subcategory. Mill 403 which was used as the basis of the NSPS had the
following raw waste load:
Flow: 258 kl/kkg (61.8 kgal/ton)
BOD5: 244 kg/kkg (487 Ibs/ton)
Segregation of the waste streams would result in biological treatment
of 172 kl/kkg (41.2 kgal/ton) of the raw waste flow which would have a
BOD5I raw waste level of 1417 mg/1.
The relationship determined in Section VII shows that the application
of biological treatment to the waste water flow of 172 kl/kkg (41.2
kgal/ton) and chemical addition/ coagulation, and clarification to the
entire effluent flow of 258 kl/kkg (61.8 kgal/ton) should achieve BOD5_
and TSS levels of 45 mg/1 and 20 mg/1, respectively.
The NSPS were therefore based upon the following:
Flow: 172 kl/kkg (41.2 kgal/ton)
EOD5: 45 mg/1
Flow: 258 kl/kkg (61.8 kgal/ton)
TSS: 20 mg/1
The above values were used to determine annual average BOD5 and TSS
levels which were multiplied by the variability factors in Table 223
in order to determine the maximum 30 consecutive days and maximum day
standards.
Deink Subcateqory
As previously discussed, the deink manufacturing process can be
considered as a cleaning process in removing impurities from the waste
paper and as such relatively high BOC5 and TSS loadings can occur as a
function of the raw materials used therefore, BODJ5 and TSS raw waste
loads for NSPS are the same as BPCTCA raw waste loads. Mill 217
demonstrated the lowest flow rate of the three 100% deink mills and
was used as the flow basis for NSPS. Since the market for waste paper
can vary and the types of waste paper available to deink mills can
vary, the NSPS were increased slightly from the effluent levels
693
-------
normally considered achievable with the technology identified. Thus,
BOD5 and TSS levels of 30 mg/1 were used as the basis for NSPS for the
deink subcategory.
Groundwopd; Thermo-mechanical Subcategory
The groundwood: thermo-mechanical subcategory NSPS were based upon
the BPCTCA raw waste load rather than the BATEA raw waste load.
Thermo-mechanical pulping is relatively new in this country and thus
the BPCTCA raw waste load reflects the best demonstrated technology
presently used by thermo-mechanical mills.
Groundwood; Fine Papers Subcategory
The groundwood: fine papers subcategory NSPS flow, and BODjj were based
on the average of mills 13 and 20. TSS raw waste was based upon only
mill 20 since mill 13 did not have measured non-standard TSS.
Flow: 83.0 kl/kkg (19.9 kgal/ton)
BOD5: 13.2 kg/kkg (26.3 Ibs/ton)
TSS: 41.a kg/kkg (82.8 Ibs/ton)
Application of biological treatment and chemical addition,
coagulation, and clarification to the raw waste load should achieve
the following effluent basis:
Flow: 83.0 kl/kkg (19.9 kgal/ton)
BOD5: 13 mg/1
TSS: 20 mg/1
Groundwood; CMN Papers Subcategory
Raw waste load BOD5 and TSS are based upon an evaluation of the
subcategory and internal controls available for new sources. The NSPS
flow for the groundwood CMN subcategory is based upon mill 016, 86.3
kl/kkg (20.7 kgal/ton). The resultant raw waste load basis is:
Flow: 86.3 kl/kkg (20.7 kgal/ton)
BOD5: 16 kg/kkg (32.0 Ibs/ton)
TSS: 45 kg/kkg (90.0 Ibs/ton)
Since none of the mills in the GW: CMN subcategory have biological
treatment, the BOD5 concentration used for the BOD5 effluent
limitations was based upon mill 014 in the GW: fine papers subcategory
which was achieving 13 mg/1 BOD5. The TSS effluent limitation was
based upon 20 mg/1 as discussed previously.
The NSPS were therefore based upon the following:
Flow: 86.3 kl/kkg (20.7 kgal/ton)
BOD5: 13 mg/1
TSS: 20 mg/1
PRETREATMENT REQUIREMENTS
694
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No constituents of the effluents discharged from mills within the
bleached kraft, groundwood, sulfite, soda, deink, and non-integrated
paper mills segment of the pulp, paper, and paperboard point source
category have been identified which would interfere with, pass
through, or otherwise be incompatible with a well-designed and
operated publicly-owned biological waste water treatment plant. The
exception to this, however, is the discharge of zinc from groundwood
mills which use zinc hydrosulfite as a bleaching agent. Pretreatment
standards on zinc which are equal to the BPCTCA limitations are
proposed for groundwood mills using zinc hydrosulfite. The
pretreatment standards can be achieved by substituting sodium
hydrosulfite for zinc hydrosulfite in the bleaching process which is
commonly practiced by many groundwood mills.
695
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SECTION XII
ACKNOWLEDGEMENTS
The Environmental Protection Agency wishes to acknowledge the
contributions of WAPORA, Inc., E. C. Jordan Co., and General Data
Systems, Inc. The efforts of E. N. Ross, William Groff, and Dr. Harry
Gehm of WAPORA; James Vamvakias, Donald Cote, Richard Perrault, and
William Warren of E. C. Jordan; and John Rhinney of General Systems
Corporation (Maryland) are appreciated.
Appreciation is expressed for the contributions of several individuals
within the Environmental Protection Agency: John Riley, Effluent
Guidelines Division, Bruce Diamond, Office of General Counsel, Irving
Susel and Ed Brandt, Office of Planning and Evaluation, and Jeff
Denit, Effluent Guidelines Division. The continued support and
direction by Allen Cywin and Ernst Hall, Effluent Guidelines Division,
are certainly appreciated.
Efforts by several members of the EPA working group/steering committee
deserve special acknowledgement and the technical assistance and
support provided to the project officer are appreciated. Those
members include: Danforth Bodien, Region X, Joe Davis, Region III,
Tom Doane, Region It Frank Early, NEIC-Denver, John Moebes, Region IV,
John Schluter, Region II, and Ralph Scott and Kirk Willard, National
Environmental Research Center at Corvallis, Oregon.
The assistance of Fred Zaiss, Effluent Guidelines Division, in
providing timely computer support is very much appreciated.
Appreciation is extended to Charles G. Nichols, Effluent Guidelines
Division, for his assistance in revising portions of the original
draft report and in compiling the many tables and figures. The
efforts of Karla Jean Dolum for her continuous assistance throughout
the project were invaluable. Special recognition is given to Pearl
Smith who typed much of this document and has put up with the constant
harassment of the project officer. Assisting Pearl Smith were Jane
Mitchell, Doris Clark, Acqua Delaney, and Brenda Pinkney.
The cooperation of the National Council for Air and Stream Improvement
in providing liaison with the industry and technical assistance were
appreciated. Thanks are also extended to the American Paper Institute
for its assistance.
Appreciation is also extended to companies who granted access to their
mills and treatment works from field surveys and for the assistance
lent by mill personnel to field crews. The operation records
furnished by these manufacturers and information supplied by other
individuals in the industry contributed significantly to the project.
697
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SECTION XIII
REFERENCES
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4. Scott, R. H., and Willard, H. K., "The U.S. Sulfite Industry
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5. Gehm, H. W., State-of-the-Art Review of Pulp and Paper Waste
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699
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15. Waymanr M. , et al. , "Peracetic Acid Bleaching of Groundwood from
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700
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31. Slatin, B., "Paper." Book of Knowledge, 1966 Ed. Grolier Inc.,
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45. Private Communication, Nov. (1973) .
46. Rexfelt, J., and Samuelson, O., "The Composition of Condensates
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Swenska Papperstidning, 21, 689 (1970).
701
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47. Clark, L. H., and DeHaas, G. G., "Volatile Acid Recovery from
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48. Long, C. J., and DeHaas, G. G., "Conversion of Crude Acetates to
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50. Van Horn, W. M., "Aquatic Biology in the Pulp and Paper
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51. Van Horn, W. M., "Aquatic Biology in the Pulp and Paper
Industry," Part II, NCASI Technical Bulletin No. 251 (1971).
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Pulping Effluents and Available Treatment Methods," TAPPI, 56, 9
(1973).
53. Harrison, M., "A Critical Review of the Literature on Slime
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54. Cormack, J. B., and Amberg, H. R., "The Effects of Biological
Treatment of Sulfite Waste Liquor on the Growth of Sphaerotilus
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(1959) .
55. Edde, H., "A Critical Review of the Literature on Slime Infesta-
tions," Part II, NCASI Technical Bulletin No. 232 (1969).
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58. Kleppe, P. J., and Rogers, C. N., Survey of Water Utilization and
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59. Timpe, W. G., et al., "Kraft Pulping Effluent Treatment and Reuse
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Publishing Co., Inc., New York (1967).
702
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61. Gehn, W. H., and Gove, G. W. , "Kraft Mill Waste Treatment in the
U.S. - A Status Report," NCASI Technical Bulletin No. 221 (1968).
62. Burns, O. B., and Eckenfelder, W. W., Jr., "A Statistical Study
of Five Years of Operation of the West Virginia Pulp and Paper
Company"s Waste Treatment Plant," Purdue Univ. Industrial Waste
Conf. XVIII (1963).
63. Edde, H. , "Settleable solids Removal Practices in the Pulp and
Paper Industry," NCASI Technical Bulletin No. 198 (1964).
64. Follette, R., and Gehm, H. W., "Manual of Practice for Sludge
Handling in the Pulp and Paper Industry,"
NCASI Technical Bulletin No. 190 (1966).
65, Stovall, J. H., and Berry, D. A., "Pressing and Incineration of
Kraft Mill Primary Clarifier Sludge," TAPPI 6th Water and Air
Conf. (1969) .
66. Wilson, D. F., et al., "Methanol, Ethanol and Acetone in Kraft
Mill Streams," TAPPI, 55, 8 (1972).
67. Hrutfiord, B. F., and McCarthy, J. L. , "SEKOR-I Volatile Organic
Compounds in Kraft Mill Effluent Streams," TAPPI. 50. 2 (1967).
68. "Evaluation of Analytical Procedures for the Analysis of Selected
Organic Compounds in Kraft Mill Effluents,"
NCASI Technical Bulletin No. 258 (1972).
69. Davis, C. L., Jr., "Color Removal from Kraft Pulping Effluents by
Lime Addition," AIChE Chemical Engineering Symposium Series, 107,
67 (1971).
70. South, W. D., "Relating Kraft Waste Stream Properties to BOD,"
TAPPI, 54, 11 (1971).
71. Carpenter, W. L,, "COD and BOD Relationships of Raw and Biologi-
cally Treated Kraft Mill Effluents," NCASI Technical Bulletin
No. 193 (1966) .
72. "Oxidation Analysis of Pulp Mill Effluents," NCASI Technical
Bulletin No. 256 (1972).
73. Van Hall, C. E., and Stenger, V. A., "Use of Infrared Analyser
for Total Carbon Determination," Proceedings Symposium on Water
Renovation," Div. of Water and Waste Chemistry, ACS, Cincinnati
(1963) .
74. Hill, N. H., "Carbon Analysers for Contaminants in Water,"
Instrument Technology, March (1969).
703
-------
75. "The Toxicity of Kraft Pulping Wastes to Typical Fish Food
Organisms," NCASI Technical Bulletin No. 10 (1947).
76. Howard, T. E., and Walden, C. C., "Pollution and Toxicity Charac-
teristics of Kraft Mill Effluents," TAPPI,48, 3 (1965).
77. "The Effects of Sublethal Concentrations of Kraft Pulping Wastes
and their Components on Fish Organs," NCASI Technical Bulletin
No. J49, (1952) .
78. "Laboratory and Controlled Experimental Stream Studies of Effects
of Kraft Mill Effluents on Growth and Production of Fish," NCASI
Technical Bulletin No. 259 (1972).
79. Private Communication, Dissolving Pulp Manufacturers (1971).
80. Private Communication (1973).
81. Jamieson, A., and Smedman, L., "Oxygen Bleaching — A Mill Tested
Approach to Pollution Abatement," TAPPI, 56, 6 (1973).
82. Nicholls, G. A., "Kraft Multistage Bleach Plant Effluents,"
TAPPI. 56. 3 (1973).
83. Ota, M., et al., "Low Molecular Weight Compounds in Spent Chlori-
nation Liquors," TAPPI, 56. 6 (1973).
84. "Bleaching Effluents with Lime. I. Treatment of Caustic
Extraction Stage Bleaching Effluent,"
NCASI Technical Bulletin No. 239 (1970).
85. Ibid, "Part II. Treatment of Chlorination Stage Bleaching
Effluent," NCASI Technical Bulletin No. 242 (1970).
86. Gould, M., "Physical-Chemical Treatment of Pulp Mill Wastes,
Woodland, Maine". Purdue International Waste Conference, 1972.
87. Haynes, D. C., "Water Reuse - A Survey of the Pulp and Paper
Industry," TAPPI. 49, 9 (1966).
88. "Deinking Report," NCASI Technical Bulletin No. 5 (1946).
89. Hodge, W. W., and Morgan, P. F., "Characteristics and Methods of
Treatment of Deinking Wastes," Sewage Works Journal, 19, 5(1947).
90. Barton, C. A., et al., "Treatment of Sulfite Pulp and Paper Mill
Waste," Journal WPCF, 45, 1 (1973).
91. Morgan, O. P., "Biological Waste Treatment Histories in the Pulp
and Paper Industry," NCASI Technical Bulletin No. 220 (1968).
704
-------
92. Bystedt, M. I., "What is the Future of Thermomechanical Pulp?,"
Pulp 5 Paper. Dec. (1973).
93. Rysberg, G., "Thermo-mechanical Pulp Advancing Around the World,"
Paper Trade Journal, Dec. 24 (1973).
94. Marton, J., and Marton, T., "Mercury in the Pulp and Paper Mill
Environment — Appraisal and Perspective," TAPPI, 55, 11, (1972).
95. Mayer, C., "Water Quality Control Program at Publishers Paper
Co.," Presented at NCASI West Coast Regional meeting, Nov.
(1972) .
96. Hrutfiord, B. F., et al.. Steam Stripping Odorous Substances from
Kraft Effluent Streams, EPA-R2-73-196, Apr. (1973).
97. Matteson, M. J., et al., "SEKOR II: Steam Stripping of Volatile
Organic Substances from Kraft Pulp Mill Effluent Streams,"
TAPPI, 50, 2 (1967).
98. Maahs, H. C., et al., "SEKOR III: Preliminary Engineering Design
and Cost Estimates for Steam Stripping Kraft Pulp Mill
Effluents," TAPPI, 50, 6 (1967).
99. Bengkvist, S., and Foss, E., "Treatment of contaminated Conden-
sates in Kraft Pulp Mills," International Congress on Industrial
Waste Water, Stockholm (1970).
100. Estridge, R. B., et al., "Treatment of Selected Kraft Mill Wastes
in a Cooling Tower," TAPPI 7th Water and Air Conf. (1970).
101. Timpe, W. C., and Evers, W. J., "The Hydropyrolysis Recovery Pro-
cess," TAP_PIX_56, 8 (1973).
102. Fogman, C. B., "A Pollution-Controlled Polysulfide Recovery
Method," Paper Trade Journal, Oct. 9 (1972).
103. Worster, H. E.r and Pudek, M. F., "The Effects of Oxygen Pulping
on Toxicity and Color of Effluent," 58th Annual Meeting, Techni-
cal Section, CPPA (1972).
104. Nelson, G. G., et al., "Water Reuse in Bleaching — Panel Discus-
sion," TAPPI, 55, 6 (1972).
105. Yankowski, A. A., "Reducing the Water Consumption in a Kraft
Bleachery." TAPPI, 55. 6 (1973).
106. Rowlandson, G., "Continuous Oxygen Bleaching in Commercial Pro-
duction*" Paper Trade Journal, Dec. 21 (1970).
705
-------
107. "Oxygen Bleaching after Seventeen Months of Operation," Paper
Trade Journal, Dec. 13 (1971).
108. Land, J. G., and Campbell, R. T., "Rapid Chlorine Dioxide Bleach-
ing of Southern Pine Kraft Pulp," Paper Trade Journal, July 30
(1973).
109. Carpenter, W. L., et al.x, "Effluent Characteristics from Conven-
tional and Oxygen Bleaching," Paper Trade Journal, July 30
(1973).
110. Makkonen, H., et al., "Oxygen Bleaching as Critical Link between
Chemical Fiberization and Fully Bleached Pulp," Paper Trad*
Journal, July 30 (1973).
111. Christensen, P. K., "Oxygen Bleaching Sulphite Pulps," Papei
Trade Journal, July 30 (1973).
112. Rapson, W. H., and Reeve, D. W., "The Effluent-Free Bleache<
Kraft Mill," Southern Pulp and Paper Manufacturer, Nov. K
(1972) .
113. Reeve, D. W., and Rapson, W. H., "Recovery of Sodium Chlorid<
from Bleached Kraft Pulp Mills," Pulp and Paper Magazine gj
Canada, 71, 13 (1970).
114. "Stream Improvement by Recovery of Bleach Plant Liquors froi
Kraft Pulp Mills," Pulp and Paper Magazine of Canada, Jun<
(1968) .
115. Reeve, D. W., et al., "Effluent Free Bleached Pulp Mill — Par
IV Salt Recovery Process," Paper Trade Journal, July 30 (1973) .
116. "Rapping with Rapson," Pulp & Paper, Oct. (1973).
117. Rapson, W. H., "Effluent Free Bleached Kraft Pulp Mill — R-
Process for Chlorine Dioxide Manufacture," Paper Trade Journal
July 30 (1973) .
118. Waste Treatment Plant at ITT Rayonier, Inc. Mill Fernandin
Beach, Florida," Southern Pulp and Paper Manufacturer, July 1
(1972) .
119. Kleinau, J. H., "Toward a Pollution-Free System of Secondar
Fibre Usage," Pulp and Paper Magazine of Canada, March (1960).
120. Lardieri, N. J., "Recovery of Usable Solids," Pulp and Papg
Magazine of Canada, March (1960).
706
-------
121. Gavalin, G., "A New Concept in Papermaking — The Lean Water
System," Paper Trade Journal, March 5 (1973).
122. Nerou, J. M.t and Garrigues, Y., Sapoxal Oxygen Bleaching Goes On
Stream at Cellulose d' Aguitaine," TAPPI Annual Meeting, Jan. 16
(1974) .
123. Gould, M., and Walzer, J., "Mill Waste Treatment by Flotation,"
Chem 26/Paper Processing, Nov. (1972).
124. Fuller, R. S., "Screening of Effluents," TAPPI, 56. 6 (1973).
125. Warren, C.E., Biology of Water Pollution Control, W.B. Saunders,
Philadelphia (1971).
126. Carpenter, W. L., "Foaming Characteristics of Pulping Wastes Dur-
ing Biological Treatment", NCASI Technical Bulletin No. 195
(1966) .
127. Nowacki, J., "Nutrient Salt Reduction in the Biological Purifica-
tion of Kraft Mill Effluents," Fortachr Wassechen ihrev Grengzch
#11, 135 (1969).
128. Nowacki, J., "Influence of Addition of Phosphorus and Nitrogen to
Pulp and Paper Mill Effluents," Pregeglad Papier 25, (6), 211,
Poland, June (1969).
129. Tracy, J. C., "Secondary Waste Treatment Nutrient and Aerator
Studies", Southern Pulp and Paper Manufacturer, Feb. 1970.
130. Eckenfelder, W. W., Jr., Industrial Waste Water Control, McGraw-
Hill Book Co., New York (1966).
131. Edde, H., "Field Research Studies of Hydraulic Mixing Patterns in
Mechanically Aerated Stabilization Basins," Proceedings Interna-
tional Congress on Industrial Waste Waters, Stockholm (1970).
132. McKeown, J. J., and Buckley, D. B., "Mixing Characteristics of
Aerated Stabilization Basins," TAPPI 8th Water and Air conf.
(1971) .
133. Grader, R. J., et al., "The Activated Sludge Process Using High-
Priority Oxygen for Treating Kraft Mill Wastewater," TAPPI, 56, 4
(1973).
134. Ayers, K. C., and Patton, T. H., Jr., "Biological Treatment
Alternatives for Kraft Effluents," TAPPI 8th Water and Air Conf.
(1971) .
707
-------
135. Bennett, D. J., et al., "Pilot Application of the Rotating Bio-
logical Surface Concept for Secondary Treatment of Insulating
Board Mill Effluents," TAPPI, 56. 12 (1973).
136. Edde, H., "A Manual of Practice for Biological Waste Treatment in
the Pulp and Paper Industry," NCASI Technical Bulletin No. 190
(1966) .
137. "Temperature Relationships in Aerobic Treatment and Disposal of
Pulp and Paper Wastes," NCASI Technical Bulletin No. 191 (1966).
138. Pelzar, M.J., Jr., Reid, R.D., "Microbiology", McGraw-Hill Book
Company, 1972.
139. Benedict, A.H., and Carlson, D.A., "Temperature Acclimation in
Aerobic BlO-oxidation Systems," Journal Water Pollution Control
Fed. 4j5, 10 (1973) .
140. Serafin, J. F., and Axen, A., "Oxygen Bleaching at Aspa Bruk
Division of Munksjo A B, Sweden," TAPPI Annual Meeting, Jan. 1416
(1974) .
141. Oledal, J., "Use of the Multi-Roll Press for Dewatering Clarifier
Sludges," Paper Trade Journal, Jan. 7 (1974).
142. Carpenter, W. L.f "Mechanical Pressing of Primary Dewatered Paper
Mill Sludges," NCASI Technical Bulletin No. 174 (1964).
143. "Great Lakes Has Copeland System to Handle Bark Fines and
Sludge," Paper Trade Journal. Oct. 2 (1972).
144. Aspitarte, T. R., et al., "Pulp and Paper Mill Sludge Utilization
and Disposal," TAPPI Environmental Conf. (1973).
145. Harkin, J. M., and Crawford, D. L., "Bacterial Protein from Paper
Mill Sludges," TAPPI Environmental Conf. (1973).
146. Vercher, B. D., et al., "Paper Mill Waste Water for Crop Irriga-
tion and Its Effects on the soil," Louisiana State Univ. Agri-
cultural Experiment Station Bulletin No. 604 (1965).
147. Gehm, H. W., "Control of Sulfite Pulping Wastes in the United
States," Pure and Applied Chemistry, 29, 281 (1972).
148. Gehm, H. W., "Factors Affecting the Appearance of Surface
Waters," NCASI Technical Bulletin No. 227 (1969).
149. Palladino. A. J., "Final Report — Aeration Development Studies,"
NCASI Technical Bulletin No. 12 (1959).
708
-------
150. Blosser, R. O. , "Oxidation Pond Studies for Treatment of Deinking
Wastes," Purdue Univ. Industrial Waste Conf. XVII (1962).
151. Laing, W. M., "New Secondary Aerated Stabilization Basin at the
Morraine Division of Kimberly-Clark Corp.," Purdue Univ.
Industrial Waste Conf. XXIV (1969).
152. MacAleese, J. E., "How Newton Falls Solved a Clean Water
Problem," Paper Trade Journal. Nov. 14 (1966).
153. Flower, W. A., "Spray Irrigation for the Disposal of Effluent
Containing Deinking Waste," TAPPI. 52. 1267 (1969).
154. "Wisconsin Tissue Effluent Plant Pioneers European Process Here,"
Paper Trade Journal. March 11 (1970).
155. Nadelman, A. H. , "A Study of Practical Approaches to Utilization
of Solids from Deinking Mills," NCASI Technical Bulletin No. 67
(1964) .
156. Davis, W. S., et al., "Recycling Fine Paper Mill Effluent by
Means of Pressure Filtration," TAPPI Environmental Conf. (1972).
157. Aldrich, L. C., and Janes, R. L., "White Water Reuse on Fine
Paper Machines," TAPPI Environmental Conf. (1972).
158. "New Approaches to In-Plant Load Control and Monitoring," NCASI
Technical Bulletin No. 248 (1971).
159. Mason, O.A., Statement by Alaska Lumber and Pulp Co., Inc., for
EPA Public Meeting Concerning National Pollutant Discharge
Elimination System (NPDES), Application No. 071-OYD-2-000055 and
Proposed Permit.
160. "G-P«s 'Pipe Organ* Aeration System," Southern Pulp and Paper
Manufacturer. May 10 (1972).
161. "K-C to Spend $92 Million at Coosa Pines Mill to Boost Pulp Out-
put and Control Pollution," Paper Trade Journal, May 20 (1974).
162. Tall Oil and Its Uses. Pulp Chemicals Assn., New York (1965).
163. Ellerbe, R. W., "Why, Where and How U.S. Mills Recover Tall Oil
Soap," Paper Trade Journal. June 25 (1973).
164. "Resource Engineering Associates, "State-of-the-Art Review on
Product Recovery," FWPCA Contract No. 14-12-495, Nov. (1969).
165. Stengle, W. B., "Crude Tall Oil Manufacture," Southern Pulp and
Paper Manufacturer, Dec. 10 (1971).
709
-------
166. Drew, J., and Pylant, G. D. , Jr., "Turpentine from the Pulpwoods
of the United States and Canada," TAPPI, 49, 10 (1966).
167. Dres, J.,et al., Sulfate Turpentine Recovery, Pulp Chemicals
Assn., New York (1971).
168. "Tapping the Chemical Motherlode of the southern Pines," Chem 26/
Paper Processing, 9, 11 (1973) .
169. Hearon, K. H., "The Lignin Dimethyl Sulfide Process," Forest
Products Journal, 7, 13 (1957).
170. Barton, J. S., "Future Technical Needs and Trends of the Paper
Industry, By-Products Usages," TAPPI, 56, 6 (1973).
171. Elgee, H., "A View of the Ligno-Sulfonate Industry," AIChE Sym-
posium Series, 133, 69 (1973).
172. Craig, D., "Justification for Pulp and Paper By-Products Develop-
ment," AIChE Symposium Series, 133, 69 (1973).
173. Pearl, I. A., "Utilization of Ey-Products of the Pulp and Paper
Industry." TAPPI. 52, 7 (1969).
174. Wiley, A. J., and Holderby, J. M., VStrong Spent Sulfite Liquors:
Utilization, By-Products and Marketing," Pulp and Paper Magazine
of Canada, 61, 3 (1960).
175. "Chemicals from the Other Half of the Tree," Chemical and Engi-
neering News. 41, 6 (1963) .
176. Howard, G. C., U.S. Patent No. 1,699,815 (1929).
177. Serafin, J. F., and Axen, A., "Operating Experience of the
Chemetics* Oxygen Bleaching Systems," TAPPI Annual Meeting, Jan.
14-16 (1974) .
178. Robeson, J. S. , U.S. Patents No. 1,075,856; 1,075,857; 1,069,029;
and 1,069,030 (1913) .
179. Lang, C. J., and DeHaas, G. G., "Acetic Acid Recovery fron
Sulfite liquor," TAPPI, 53^ 6 (1970).
180. Testimony of Roland J. Stanton, Technical Director, Ketchikar
Pulp Co., Ketchikan, Alaska, EPA Hearing, EPDES Permit
Application No. 081-OY2-2-000094, Aug. 16 (1973).
181. Gehm, H. W., "An Overview of Water Reuse Potential in Pulp anc
Paper Manufacture," Paper presented to AIChE, Washington, D.C.,
April 26 (1973) .
710
-------
182. Hendrickson, E. R., and Oglesby, H. S., "Process Design and
Operation for zero Effluent Discharge," TAPPI, 57, 4 (1974).
183. Haynes, D. C., "Water Recycling in the Pulp and Paper Industry,"
TAPPI, 57, 4 (1974).
184. "Cost of Achieving EPA's BPCTCA and Zero Discharge," Paper Trade
Journal. April 15 (1974).
185. Gullichsen, J., "Status of Kamyr Displacement Bleaching Project,"
Paper Trade Journal. July 30 (1973).
186. "New Pulp Bleaching System to be Part of Eastex Mill Expansion,"
Paper Trade Journal, Apr. 29 (1974).
187. Serafin, J. F., and Andrews, D. H., "Oxygen Bleaching Development
from Laboratory Scale Experiments to Full Scale Commercial
Installation and Operation," TAPPI Annual Meeting, Jan. 14-16
(1974) .
188. Lowe, K. E., "Chesapeake Launches Oxygen Bleaching," Pulp and
Paper, Oct. (1973) .
189. Private communication (1974).
190. Fary, D. A., and Schmitt, "Oxygen Bleaching at Chesapeake
Corporation," TAPPI Environmental Conf., Apr. 17-19 (1974).
191. Standard Methods for the Examination of Water and Wastewater,
APHA, AWWA, and WPCF, American Public Health Assn., Inc., New
York (1971) .
192. "An Investigation of Improved Procedures for Measurement of Mill
Effluent and Receiving Water Color," NCASI Technical Bulletin
No. 253 (1971).
193. Kreissl, J. F., "Granular Media Filtration of Wastewater: An
Assessment," EPA, National Environmental Research Center, Ad-
vanced Waste Treatment Research Laboratory, Cincinnati, Ohio,
Jan. (1973) .
194. Cruver, J. E., "Reverse Osmosis fcr Water Reuse," Gulf Environ-
mental system Co., Paper presented at the National Conf. on Com-
plete Water Reuse, Washington, E.G., Apr. (1973).
195. Schwonke, P. A., and Davis, W. S., "Enzyme Enhanced Turbidity
Removal through Primary Treatment," TAPPI, 56, 1 (1973).
196. Baumann, E. R.,"Design of Filters for Advanced Wastewater Treat-
ment," Iowa State University, Department of Civil Engineering,
711
-------
Paper presented at EPA Technology Transfer Design Seminar, Ames,
Iowa, June (1973).
197. Weber, Walter J., Jr., Physico-chemical Processes for Water
Quality Control, Wiley-Interscience, New York 1972.
198. Pilot Plant Studies of Turbidity and Residual Cell Material
Removal from Mill Effluent by Granular Media Filtration. NCASI
Tech. Bull. No. 266, May 1973.
199. Tchobanoglous, G.r "Filtration Techniques in Tertiary Treatment,
Journal Water Pollution Control Federation. 42, April 1970.
200. Tchobanoglous, G., and Eliassen, R., "Filtration of Treated
Sewage Effluent," Journal of the Sanitary Engineering Division,
ASCE, April 1970.
201. Gulp, G.L., and Hansen, S.P., "Extended Aeration Polishing by
Mixed Media Filtration", Wajbgr and Sewage Works, February 1967.
202. Culp, R. L., and Gulp, C.L., Advanced Wastewater Treatment, Van
Nostrand Reinhold, New York, 1971.
203. Vecchiolo, Jr., et. al., "Wastewater Reclamation and Recharge,
Bay Park, New York, Journal Sanitary Engineering Division ASCE,
April 1975.
204. Middlebrooks, E.J., et. al., "Evaluation of Techniques for Algae
Removal from Wastewater Stabilization Ponds," Utah Water Research
Laboratory, Utah State University, Logan, Utah, January 1974.
205. Baumann, E.R., "Design of Filters for Advanced Waste Water
Treatment," Project 1002-S, Engineering Research Institute, Iowa
State University, Ames, Iowa, June 1973.
206. Leitner, G. F., "Reverse Osmosis For Waste Water Treatment -
What? When?," TAPPI 8th Water & Air Conf. (1971).
207. Morris, D. C., Nelson, W. R., and Walraven, G. O., Recycle of
Paper Mill Wastewaters and Application of Reverse Osmosis, Green
Bay Packaging. Inc.. EPA 12040 FEE, Jan. (1972).
208. Wiley, A. J., Dubey, G. A., and Eansal, J. K., Reverse Osmosis
Concentration of Dilute Pulp and Paper Effluents, The Pulp Manu-
facturers Research League and The Institute of Paper Chemistry,
EPA 12040 EEL, Feb. (1972).
209. Johnson, J. S., Jr., Minturn, R. E., and Moore, G. E., Hyperfil-
tration (Reverse Osmosis) of Kraft Pulp Mill and Bleach Wastes.
712
-------
Chemistry Division, Oak Ridge National Laboratory (unpublished)
(1973) .
210. Beder, H., and Gillespie, W. J., "The Removal of Solutes from
Pulp Mill Effluents by Reverse Osmosis," TAPPI, 53, 5 (1970).
211. Smith,R., and McMichael, W. F., Cost and Performance Estimates
for Tertiary Wastewater Treatment Processes, FWPCA, U.S. Dept.
of the Interior, June (1969).
212. Direct Filtration of Secondary Effluents, EPA Technology Transfer
Program, Engineering Research Institute; Iowa State University,
Ames, Iowa; Newark, N.J., Mar. 13-15 (1974).
213. Ultra High Rate Filtration of Activated Sludge Plant Effluent,
EPA Office of Research and Monitoring, Washington, D.C., Apr.
(1973) .
214. Nelson, W. R., Walraven, G. O., and Morris, D. C., "Process Water
Reuse and Upset Control Modification at an Integrated NSSC Mill,"
TAPPI, 56, 7 (1973).
215. McCuaig, W. B., Atkins, P. P., Jr., and Lueck, B. L., Physical-
Chemical Treatment of Combined Municipal Pulp and Paper Wastes,
TAPPI Environmental conf. (1974).
216. Bishop, H. K., Use of Improved Mecr.tranes in Tertiary Treatment by
Reverse Osmosis, McDonnell Douglas Astronautics Company, EPA
17020 DHR, Dec. (1970).
217. Kreusch, E., and Schmidt, K., Wastewater Demineralization by ion
Exchange, Culligan International Co., EPA 17040 EEE, Dec. (1971).
218. Herbert, A. J., "A Process for Removal of Color from Bleached
Kraft Effluents through Modification of the Chemical Recovery
System," NCASI Technical Bulletin No. 157 (1962), U.S. Patent #
3,120,464.
219. Berger, H. F., and Thibodeaux, L. J,, "Laboratory and Pilot Stu-
dies on Water Reclamation," NCASI Technical Bulletin No. 203
(1967) .
220. Linstedt, K. D., Houck, C. P., and O'Connor, J. T., "Trace
Element Removals in Advanced Wastewater Treatment Processes,"
Journal WPCF, 43, 7 (1971).
221. Gregory, J«» and Dhond, R. V., "Wastewater Treatment by Ion Ex-
change," Water Research (Great Britain), Pergamon Press (1973).
713
-------
222. Gulp, R. L., and Gulp, G. L., Advanced Waste Treatment, Van
Nostrand Reinhold, New York (1971).
223. Optimization of Ammonia Removal by Ion Exchange Using Clinoptilo-
lite. University of California, EPA 17080 DAP, Sept. (1971).
224. Wastewater Ammonia Removal by Ion Exchange, Battelle-Borthwest,
EPA 17010 EEZ, Feb. (1971).
225. Johnson, W. K., and Vania, G, B.,
Nitrification and Denitrification of Waste Water, University of
Minnesota, EPA Research Grant Number WP 01028, Jan. (1971).
226. Nitrogen Removal From Wastewaters, EPA Federal Water Quality Re-
search Laboratory, Advanced Waste Treatment Research Laboratory,
Cincinnati, Ohio, Oct. (1970).
227. Shindala, A., "Nitrogen and Phosphorus Removal From Wastewaters -
Part I," Water and Sewage Works, June (1971).
228. Shindala, A., "Nitrogen and Phosphorus Removal From Wastewaters -
Part II," Water and Sewage Works, July (1971).
229. Process Design Manual for Carbon Adsorption, EPA Technology
Transfer, Oct. (1973).
230. Hansen, S. P., and Eurgess, F. J., "Carbon Treatment of Kraft
Condensate Wastes." TAPPI, 51, 6 (1968).
231. Rimer, A. E., et al., "Activated Carbon System for Treatment of
Combined Municipal and Paper Mill Waste Waters in Fitchburg,
Mass.," TAPPI, 54, 9 (1971).
232. Smith, D. R., and Berger, H. F., "Waste Water Renovation," TAPPI,
51, 10 (1968).
233. Timpe, W. G., et al.. TherUse of Activated Carbon for Water
Renovation in Kraft Pulp and Paper Mills. 7th TAPPI Air and
Water Conf,, (1970).
2J4. Timpe, W. G., and Lang, E. w., "Activated Carbon Treatment: of
Unbleached Kraft Effluent for Reuse - Pilot Plant Results," TAPPI
Environmental Conf. (1973) .
235. Coates, J. and McGlasson, W. G., "Treatment of Pulp Mill
Effluents With Activated Carbon,"
NCASI Technical Bulletin No. 199 (1967).
236. Davies, D. S. and Kaplan, R. A., "Activated Carbon Eliminates
Organics," Chemical Engineering Progress, 60, 12 (1964).
714
-------
237. Bishop, D. F., et al.,"Studies on Activated Carbon Treatment,"
Journal WPCF. 39, 2 (1967).
238. Vanier, C., et al.. Carbon Column Operation in Waste Water Treat-
ment, Syracuse University, Syracuse, New York, Nov. (1970).
239. Weber, W. J., Jr., and Morris, J. C., "Kinetics of Adsorption in
Columns of Fluidized Media," Journal WPCF, 37, 4, (1965).
240. Beebe, R. L., and Stevens, J. I., "Activated Carbon System for
Wastewater Renovation," Water and Wastes Engineering, Jan.
(1967) .
241. Holm, J. D., "A Study of Treated Wastewater Chlorination," Water
and Sewage Works, Apr. (1973).
242. Meiners, A. F., Light-Catalyzed Chlorine Oxidation for Treatment
of Wastev>ater, EPA, Water Quality Office, Midwest Research Insti-
tute, Kansas City, Missouri, Sept. (1970).
243. Huibers, T. A., et al.. Ozone Treatment of Secondary Effluents
from Wastewater Treatment Plants, EPA, Robert A. Taft Water Re-
search center. Report No. TWRC-4, Apr. (1969).
244. Chen, J. W., and Smith, G. V.,
Feasibility Studies of Applications
of Catalytic Oxidation in Wastewater, EPA, Southern Illinois
University, Carbondale, Illinois, Nov. (1971).
245. Eckenfelder, W. W., Jr., Krenkel, P. A., and Adams, C. A., Ad-
vanced Waste Water Treatment, American Institute of Chemical
Engineers, New York (1972) .
246. Moggio, W. A., "Experimental Chemical Treatments for Kraft Mill
Wastes," NCASI Technical Bulletin No. 50 (1952).
247. Oswalt, J. L., and Lund, J. G., Jr., Color Removal from Kraft
Pulp Mill Effluents by Massive Lime Treatment, EPA 12040 DYD
(1973) .
248. Swanson, J. W., et al., Kraft Effluent Color Characterization
Before and After StQichiometric Lime Treatment, EPA 12040 DKD
(1973) .
249. Lowe, K. E., "Is Pulping Technology on Verge of Revolution,"
Pulp & Paper, July (1974) .
250. Private Communication, Interstate Paper Corporation (1973).
715
-------
251. Rapson, W. H., and Reeve, D. W., "Bleached Kraft Pulp Mills Can
be Made Free of Liquid Effluents," Paper Trade Journal, Oct. 16
(1972) .
252. Ranhagen, G., "The Entirely Closed Mill - A Utopia or a Realistic
Approach," Paper Trade Journal, Jan. 22 (1973).
253. Chang, H,, Reeves, R. H., McKean, W. T., and Gratel, J. S., "Sem-
inar on Soda-Oxygen Pulping Held by North Carolina State Univer-
sity," Paper_Trade Journal, Sept. 10 (1973).
254. Gilmont, P. L., "Water Requirements of Pulp Bleaching - Survey of
Mill Practice in the United States," TAPPI, 50, 10 (1967).
255. Histed, J. A., and Nicolle, F. M. A., "Water Reuse and Recycle in
Kraft Bleacheries," Pulp and Paper Magazine of Canada, 74, 12
(1973).
256. Histed, J. A., and Nicolle, F. M. A., "Water Reuse and Recycle in
the DcEDED Bleach Sequence," CPPA-TAPPI Conf., Vancouver, B.C.
Sept. (1973).
257. Gall, R. J., and Thompson, F. H., "The Anti-Pollution Sequence
A New Route to Reduce Pollutants in Bleach Effluent," TAPPI, 56,
11 (1973).
258. Improved Machinery, Inc., Impcp Papribleach Pulp Bleaching
Process, (Trade Pamphlet), Nashua, N.H. (1972).
259. Jamieson, A., Noreus, S., and Pettersson, B., "Advances in Oxygen
Bleaching III, Oxygen Bleaching Pilot Plant Operation,"
TAPPI, 54, 11 (1971) .
260. Lescot, J. C., "Oxygen Bleaching - A Flexible Process for Pollu-
tion Abatement," CPPA-TAPPI Conf., Vancouver, B.C., Sept. (1973).
261. Lowe, K. E., "Bleaching at Crossroads," Pulp & Paper. Aug.
(1973) .
262. Carpenter, W. L., McKean, W. T., Berger, H. F., and Gellman, I.,
"A Comparison of Effluent Characteristics from Conventional and
Oxygen Bleaching Sequences - Results of a Laboratory Study,"
CPPATAPPI Conf., Vancouver, B.C., Sept. (1973).
263. Berger, H. F., "Development of an Effective Technology for Pulp
and Bleaching Effluent Color Reduction," NCASI Technical Bulletin
No. 228, (1969) .
264. Spruill, E. L., Draft of Final Report, Color Removal and Sludge
Disposal Process for Kraft Mill Effluents, EPA 12040 DRY (1973) .
716
-------
265. "Treatment of Calcium-Organic Sludges Obtained From Lime Treat-
ment of Kraft Pulp Mill Effluents — Part I," NCASI Technical
Bulletin No. 62 (1955) .
266. "Treatment of Calcium-Organic Sludges Obtained From Lime Treat-
ment of Kraft Pulp Mill Effluents — Part II," NCASI Technical
Bulletin No. 75 (1955).
267. "Development Studies on the Removal of Color from Caustic Extract
Bleaching Effluent by the Surface Reaction Process — Part II,"
NCASI Technical Bulletin No. 107 (1958) .
268. Berger, H. F., and Brown, R. I., "The Surface Reaction Method for
Color Removal from Kraft Bleachery Effluents," NCASI Technical
Bulletin No. 119. (1959) .
269. "Development Studies on the Removal of Color from Caustic Extract
Bleaching Effluent by the Surface Reaction Process — Part II,"
NCASI Technical Bulletin No. 122 (1959).
270. Davis, C. L., Color Removal from Kraft Pulping Effluent by Lime
Addition, Interstate Paper Corporation, EPA 12040 ENC (1971).
271. Spruill, E.L., Color Removal and Sludge Recovery from Total Mill
Effluent, TAPPI Environmental Conf. (1972).
272. Gould, M., Color Removal from Waste Effluents, U.S. Patent
3,531,370 (1970) .
273. Spruill, E. L., "Color Removal from Paper Mill Waste," Proceed-
ings Purdue Univ. Industrial Waste Conf. XXV (1970).
274. Private Communication, Continental Can Company, Inc. (1973).
275. Gould, M., "Color Removal from Kraft Mill Effluent by an Improved
Lime Process," TAPPI, 56, 3 (1973),
276. Gould, M., "Physical - Chemical Treatment of Pulp Mill Wastes,
Woodland, Me.," Proceedings Purdue Univ. Industrial Waste Conf.
XXV (1970) .
277. Private Communication, Georgia Pacific Corporation (1974).
278. Private Communication, International Paper Company (1974).
279. Berov, M. B., et al., "pH and the Effectiveness of Effluent
Treatment," Bum. Prom. (USSR), No. 2, 6(1973);
Abs. Bull. Inst. Paper Chem., 44, 1561 (1973).
717
-------
280. Willard, H. K. , "Coagulation of Pulp and Paper Aerated Lagoon
Effluents for Color and Solids Removal," AIChE Symposium Series,
69 (1973).
281. Smith, S. E., and Christman, R. F., "Coagulation of Pulping
Wastes for the Removal of Color," Journal WPCF, 41, 2., Part I,
(1969) .
282. Middlebrooks, E. J., et al. , "Chemical coagulation of Kraft Mill
Wastewater," Water and Sewage Works, 116, 3, (1967).
283. Scott, R. H., "Sophisticated Treatment at Baikal Pulp Mill in
U.S.S.R.," Pulp and Paper, Apr. (1974).
281. Private Communication, Gulf States Paper, Tuscaloosa, Alabama
(1974) .
285. Fremont, H. A., Tate, D. C., and Goldsmith, R. L., "Color Removal
from Kraft Mill Effluents by Ultrafiltration," Environmental Pro-
tection Technology Series, EPA-660/2-73-019, Office of Research
and Development, EPA, Dec. (1973).
286. Private Communication, Union Carbide Corp., S. Charleston, W. Va.
(1974) .
287. Rock, S. L., Kennedy, D. C., and Brunner, A., "Decoloration of
Kraft Mill Effluents with Polymeric Adsorbents," TAPPI Environ-
mental conf., Apr. 17-19 (1974).
288. Anderson, L. G., Groddevall, B., Lindberg, S., and Phillips, Jr.,
"A New Color Removal Process: A Field Report," TAPPI, 57, 4
(1974) .
289. Sanks, R. L., "Ion Exchange Color and Mineral Removal from Kraft
Bleach Wastes," Environmental Protection Technology Series, EPA-
R2-73-255, Office of Research and Monitoring, EPA May (1973).
290. McGlasson, W. G., et al., "Treatment of Pulp Mill Effluents with
Activated Carbon," MCASI Bulletin No. 199 (1967).
291. Whittemore, R. C., "An Evaluation of the Adsorptive Properties of
Fly Ash and Bark-Derived Activated Char," NCASI Technical Bulle-
tin No. 267 (1973) .
292. Hanzawa, M., et al., "Clarification of NSSC Waste Liquor by
Active Carbon, etc.," Res. Bull. Coll. Expt. Forests Hokkaido
Univ.(Jup.), 29, 361 (1972); Abs. Bull Inst. Paper Chem.. 43,
11803 (1973).
718
-------
293. MacDonald, D. G., and Nguyen, T. , "Activated Carbon from Bark for
Effluent Treatment," Pulp S Paper, 75, 5 (1974).
294. Bauman, H. D., and Lutz, L. R., "Czonation of a Kraft Mill Efflu-
ent," TAFPI Environmental Conf., Apr. 17-19 (1974).
295. Rapson, B., Sullivan, D. P., and Brothers, J. A., "NSRF seawater-
Lime Clarification Process for Kraft Effluents," Paper Trade
journal. Feb. 25 (1974).
296. "Color Removal Process," Pulp and Paper International. May
(1973) .
297. Twitchell, J. P., and Edwards, L. L., "Kraft Mill Material
Balance Calculations for Brown Stock Washing, Screening and
Oxygen Bleaching,".TAPPI Environmental Conf. (1974).
298. Narrstrom, H,, "The Environmental Care Project of the Swedish
Pulp and Paper Industry," TAPPI environmental Conf. (1974).
299. Nichols, G. A., "Kraft Multistage Bleach Plant Effluents,"
TAPPI, 56, 3 (1973).
300. Chen, H. T., et al., "Evaluation of Four Biological Systems on
Integrated Paper Mill Effluent," TAPPI Enviornmental Conf.
(1974) .
301. Gillespie, W. J., et al., "A Pilot Scale Evaluation of the Effi-
cacy of Rotating Biological Surface Treatment of Pulp and Paper
Mill Wastes," TAPPI Environmental Conf. (1974).
302. MaAliley, J. E., "A Pilot Plant Study of a Rotating Biological
Surface for Secondary Treatment of Unbleached Kraft Mill Wastes,"
TAPPI Environmental Conf. (1974).
303. Gorham International Inc., Study of Solid Waste Management
Practices in the Pulp and Paper Industry, EPA, Office of Solid
Waste Management Program, Feb. (1974).
304. Tyler, M. A., and Fitzgerald, A. D., "A Review of Colour Re-
duction Technology in Pulp and Paper Mill Effluents," Presented
at the 58th Annual Meeting Technical Section, CPPA, Montreal,
Jan. 24-28 (1972) .
305. Vogt, C., Development Document for Effluent Limitations
Guidelines and New Source Performance Standards for the
Unbleached Kraft and semichemical Pulp Segment of the Pulpf
Paper, and Paperboard Point source Category, U. S. Environmental
Protection Agency, EPA-440/ 1-74-025-a, May 1974.
719
-------
306. TAPPI Mag., American Defibrator, Vol. 59, No. 2. February 1976.
307. American Paper Institute, Comments Concerning Effluent
Limitations and Guidelines for Existing Sources and Standards of
Performance and Pretreatment Standards for New Sources for The
Bleached Kraft, Groundwood, Sulfite, Soda, Deink, and Non-
Integrated Paper Mills Segment of the Pulp, Paper, and Paperboard
Point Source Category; Federal Register, September, 5, 1975, Vol.
40, No. 173.
308. Libby, Earl C.; Pulp and Paper Science and Technology; Vol. I
Pulp; McGraw - Hill Book Co., NY, NY. 1962.
309. Button, N.; ITT - Rayonier, Inc. Correspondence; December 1975.
310. Clark, J. W. and Viessman, W., Jr., Water Supply and Pollution
Control, International Textbook Company (1970).
311. McKinney, E. E., Microbiology for Sanitary Engineers, McGraw -
Hill Book Company (1962).
312. Brock, T. D., Biology of Microorganisms, Prentice-Hall, Inc.
(1970)
313. E. J. Kirsch, Private Communication, Purdue University.
314. Metcalf & Eddy, Inc., Wastewater Engineering, McGraw-Hill Book
Company, Chapter 10 (1972) .
315. Streeter, H. W. and Phelps, E. B., "A Study of the Pollution and
Natural Purification of the Ohio", Public Health Bulletin 146,
United States Public Health Service, February (1925).
316. Vamvakias, J. G. and Miller, J. P., "Temperature Response of
Aerated Stabilization Basins With and Without Nutrients," Fifth
Paper—Industry and Stream Improvement Conference, Canadian Pulp
and Paper Association, Technical Paper T87.
317. T. W. Beak Consultants Limited, "Biological Treatment Study,"
Government of Canada, Ottawa, Canada, September (1972) .
318. McKeown, J. J.; Buckley D. B.; and Gellman, I., "A Statistical
Documentary on the Performance of Activated Sludge and Aerated
Stabilization Basin Systems Operating in the Paper Industry,"
Purdue Industrial Waste Conference XXIX (1974) .
319. "A Manual of Practice for Biological Waste Treatment in the Pulp
and Paper Industry," NCASI Technical Bulletin f214.
720
-------
320. Burns, 0. B., Jr. and Eckenfelder, W. W., Jr., "A Statistical
Study of Five Years' Operation of West Virginia Pulp and Paper
Company's Waste Treatment Plant," Purdue Industrial Waste
Conference XVIII (1963).
321. Dorr Oliver, Inc., Stamford, Connecticut,
322. American Water Works Association, Water Treatment Plant Design,
AWWA, Inc. (1969).
323. Ford, D. L.; Shin, C. S.; and sebesta, E. C., "Temperature
Prediction in Activated Sludge Basins Using Mechanical Aerators,"
Purdue Industrial Waste Conference XXVII (1972).
324. Adams, C. E., Jr., et al, "The Development of Design Criteria for
Wastewater Treatment Processes," Proceedings of a Seminar,
Vanderbilt University, April (1975).
325. Eckenfelder, W. W. and Ford, D. L., Water Pollution Control,
Jenkins Book Publishing Company (1970).
326. Babcock & Wilcox, Inc.; Personnel Communication.
327. TAPPI Mag.; Vol. 54, No. 4 Page 564.
328. Amberg, H. Crown Zellerbach Corp.; Correspondence, Sept. 1975.
329. Brown, S., Philip, D.; "Color Removal from Bleached Kraft
Effluents." Dow Chemical Co.; Presented at TAPPI Envir.
Conference, May 1975.
721
-------
SECTION XIV
GLOSSARY
Active alkali
A measure of the strength of alkaline pulping liquor indicating the
sum of caustic soda and sodium sulfide expressed as Na20.
Air Dry (AD) Ton
Measurement of production including a moisture content of 10 percent
by weight.
Bark
The protective covering of a tree.
Barking
Removal of bark from logs in a wet or dry process.
Black Liquor
Spent liquor recovered from a kraft digester up to the point of its
introduction into the recovery plant.
Bleaching
The brightening and delignification of pulp by addition of chemicals
such as chlorine.
Blow
Ejection of the chips from a digester.
Boil-Out
A procedure, usually utilizing heat and chemicals, to clean equipment
such as evaporators, heat-exchangers, and pipelines.
Breaker Stack
Two rolls, one above the other, placed in the dryer section of a paper
machine to compact the sheet and smooth out its surface defects.
723
-------
Broke
Partly or completely manufactured paper that does not leave the
machine room as salable paper or board; also paper damaged in
finishing operations such as rewinding rolls, cutting, and trimming.
Calender Stack
Two or more adjacent and revolving rolls which provide even calipe:
control of the sheet and the final finishing of its surface.
Cellulose
The fibrous constituent of trees which is the principal raw material:
of paper and paperboard.
Chest (or Stock Chest)
Tank used for storage of wet fiber or furnish.
Chips
Small pieces cf wood used to make pulp.
Color Unit
A measure of color concentration in water using NCASI methods.
Consistency
A weight percent of solids in a solids-water mixture used in the manu
facture of pulp or paper.
Cooking
Heating of wood, water, and chemicals in a closed vessel unde
pressure to a temperature sufficient to separate fibrous portion o
wood by dissolving lignin and other nonfibrous constituents.
Cooking Liguor
The mixture of chemicals and water used to dissolve lignin in woo
chips.
Countercurrent Washing
Pulp washing in which fresh water is added only at the last stage an
the effluent from this stage is then used as wash water for tlr
previous stages.
Decker
A mechanical device used to remove water or spent cooking liquor frc
pulp, and to thicken pulp consistency.
724
-------
Digester
A pressure vessel used to cook wood chips in the presence of cooking
liquor and heat.
Digestion
Cooking of chips in the above manner.
Dregs
The inert rejects from the green liquor clarifier of a pulp mill.
Extraction Water
Water removed during a pulp manufacturing process.
Felt
The endless belt of wood or plastic used to convey and dewater the
sheet during the papermaking process.
Fiber
The cellulosic portion of the tree used to make pulp, paper, and
paperboard.
Fjnes
Fiber fragments produced by fiber cutting in beaters.
Furnish
The mixture of fibers and chemicals used to manufacture paper.
Gland
A device utilizing a soft wear-resistant material used to minimize
leakage between a rotating shaft and the stationary portion of a
vessel such as a pump.
Gland Water
Water used to lubricate a gland. Sometimes called "packing water."
Grade
The type of pulp or paper product manufactured.
Green Liquor
Liquor made by dissolving chemicals recovered from the kraft process
water and weak liquor preparatory to causticizing.
Grits
725
-------
Unreactive materials mechanically removed from the causticizing of
kraft and soda green liquor and disposed of as solid waste.
Headbox
The area of the paper machine from which the stock flows through a
sluice onto the wire.
Integrated
A term used to describe a pulp and paper mill operation in which all
or some of the pulp is processed into paper at the mill.
Lignin
A non-degradable organic compound of wood.
Newsprint
Paper made largely frcm groundwood pulp, with a small percentage o:
chemical pulp added for strength, used chiefly in the printing of
newspapers.
Packing Water
See Gland Water.
Prehydrolysis
Pre-steaming of chips in the digester prior to cooking; usually asso
ciated with improved bleaching of kraft pulp.
Pulp
Cellulosic fibers after conversion from wood chips.
Pulper
A mechanical device resembling a large-scale kitchen blender used t
separate fiber bundles in the presence of water prior to papermaking.
726
-------
Ray Cells
Cells which carry stored food (protein, starch, and fats) from the
bark to the wood of a tree and appear as impurities in the pulping
process, especially unbleached operations.
Rejects
Material unsuitable for pulp or papermaking which has been separated
in the manufacturing process.
Save-all
A mechanical device used to recover papermaking fibers and other
suspended solids from a waste water or process stream.
Screenings
Rejects separated from useable pulp by a device such as a screen.
Side-Hill Screens
Steeply sloped, 60-mesh screens.
Spent Cooking Liquor
Cooking liquor after digestion containing lignaceous as well as
chemical materials.
Stock
Wet pulp with or without chemical additions.
Suction Box
A rectangular box with holes or slots on its top surface, used to suck
water out of a felt or paper sheet by the application of vacuum.
Suction Couch Roll
A rotating roll containing holes through which water is sucked out of
a paper sheet on a fourdrinier machine, by the application of vacuum.
Sulfidity
Sulfidity is a measure of the amount of sulfur in kraft cooking
liquor. It is the percentage ratio of NaS, expressed as NaO, to
active alkali.
727
-------
1 Stainless Steel
1 Stainless Steel is steel with the following composition:
Carbon 0.08 percent maximum
Manganese 2.00 percent maximum
Silicon 1.00 percent maximum
Chromium 18.00-20.00 percent
Nickel 11.00-10.00 percent
Molybdenum 3.00- U.OO percent
Remainder iron
Virgin Wood Pulp (or fiber)
Pulp made from wood, as contrasted to waste paper sources of fiber.
Wet Laps
Rolls or sheets of pulp of 30-45 percent consistency prepared in a
process similar to papermaking; facilitates transportation of market
pulp.
Wet Strength Additives
Chemicals such as urea and melanine formaldehydes used in papermaking
to impart strength to papers used in wet applications.
White Liquor
Liquors made by causticizing green liquors; cooking liquor.
White Water
Water which drains through the wire of a paper machine which contains
fiber, filler, and chemicals.
Wire
An endless moving belt made of metal or plastic, resembling a window
screen, upon which a sheet of paper is formed on a fourdrinier
machine.
728
-------
A.
A.
AD Pulp
ADT
APHA
API
APS
ASB
atm
AWT
B.
BATEA
BCT
BK
BOD or BODj>
BPCTCA
BTU
C
C
°C
C+F
CMN
CMP
COD
cu m/min
SECTION XV
TERMINOLOGY INDEX
Activated Sludge
When associated with a mill code, refers to new data
Air Dried Pulp
Air dry tons
American Public Health Association
American Paper Institute
anti-pollution sequence
Aerated Stabilization Basin
atmospheres
Advanced Waste Treatment
Board or Paperboard
Best Available Technology Economically Achievable
Paperboard, Coarse, Tissue
Bleached Kraft
Biochemical Oxygen Demand (five-day)
Best Practicable Control Tehcnology Currently
Available
British Thermal Units
Clarifier
Coarse
degrees Centigrade
Clays and Fillers
Coarse, Molded, Newsprint
Chemi-mechanical Pulp
Chemical Oxygen Demand
Cubic meters per minute
729
-------
cu. m./kkg
D
DAF
Diss.
DO
E. Coli.
ENR
F
FACET
oF
Fwp
IIQII
gal
gpd/sq. ft.
gpm
GW
ha
hp
IDOD
IJC
in. Hg
JTU
kg
kg BOD/kg
MLUSS/day
kg/ha sur-
face area/
day
kg/kkg
Cubic meters per 1000 kilograms
De-ink
Dissolved Air Flotation
Dissolving
Dissolved Oyxgen
Escherica Coliform
Engineering News Record
Fine
Fine Activated Carbon Effluent Treatment
degrees Fahrenheit
from waste paper
Gravity
gallons
gallons per day per square foot
gallons per minute
Groundwood
hectare, 10,000 meter squared
horsepower
Immediate Dissolved Oxygen Demand
International Journal Commission
inches of Mercury
Jackson Turbitity Units
kilogram, 1000 grams
kilogram of BOD per kilograms of MLVSS per day
kilograms per hectare of surface area per day
kilograms per 1000 kilograms
730
-------
kg/sq cm
kgal
kgal/ton
kkg
kw
L
Lpd/sq. m.
L/kkg
L/min.
Liquor
Recovery
Ib
Ib/ac/day
mgd
mg/1
MKT
MLSS
MLVSS
MM
mu
N
N(NSM)
N.A.
NAB
NCASI
NI
nm
kilograms per square centimeter
1000 gallons
1000 gallons per ton
1000 kilograms, metric ton
kilowatt
liter
liters per day per square meter
liters per 1000 kilograms
liters per minute
C - Collected
B - By-products
I - Incinerated
pound
pound per acre per day
million gallons per day
milligrams per liter
market
Mixed Liquor Suspended Solids
Mixed Liquor Volatile Suspended Solids
Maximum Month
millimicrons
News
non-standard methods when associated with
data
Not Available
Natural Aeration Basin
National Council for Air and Stream Improvement
Non-Integrated
nano meters, 10- meters
731
-------
NOV
NPDES
NSPS
NSSC
P
PCB
PCU
PP
ppm
PS
psig
RBS
rpm
RWL
S
SB
Set Slds
SO
SSL
Std. Meth.
T
TAPPI
TC
TDS
Temp
TMP
TOC
Number of Values Reported
National Pollutant Discharge Elimination
System
New Source Performance standards
Neutral Sulfite Semi-chemical
Pulp
Polychlorinated biphenyl
Platinum Color Units
Purchased Pulp
parts per million
Post Storage
pounds per square inch gage
Rotating Biological Surface
revolutions per minute
Raw Waste Load(s)
Sulfite
Settling Basin
Settleable Solids
Soda
Spent Sulfite Liquor
Standard Methods
Tissue
Technical Association of the Pulp
and Paper Industry
Total Carbon
Total Dissolved Solids
Temperature
Thermo-mechanical Pulp
Total Organic Carbon
732
-------
TOD
TOM
ton
tpd
TS
TSS
turbid
TVS
Type
Condenser
UK
Total Oxygen Demand
Total Otganic Matter
1000 pounds (short ton)
tons per day
Total Solids
Total Suspended Solids
Turbitity
Total Volatile Solids
V - Vapor Recompression
S - Surface Condenser
B - Barometric Condenser
Unbleached Kraft
733
-------
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