U.S. patent application number 11/908527 was filed with the patent office on 2009-09-03 for dual-train wastewater reclamation and treatment system.
This patent application is currently assigned to NAVALIS ENVIRONMENTAL SYSTEMS, LLC. Invention is credited to Randall J. Jones, Stephen P. Markle.
Application Number | 20090218282 11/908527 |
Document ID | / |
Family ID | 37053690 |
Filed Date | 2009-09-03 |
United States Patent
Application |
20090218282 |
Kind Code |
A1 |
Markle; Stephen P. ; et
al. |
September 3, 2009 |
Dual-Train Wastewater Reclamation and Treatment System
Abstract
A wastewater treatment system for use on marine vessels or
land-based applications where wastewater is separated into two
separate sources as graywater and raw sewage (blackwater). For
blackwater, the treatment system incorporates five general phases
(or zones): (1) screening, (2) clarifying, (3) filtering, (4)
advanced oxidation, and (5) sludge reducing. For graywater, the
treatment system incorporates three general phases (or zones): (1)
screening (2) filtering, and (3) advanced oxidation. Each train of
the treatment system (blackwater and graywater) can operate as a
stand-alone system or can be assimilated into an integrated
treatment train for both graywater and blackwater. This system is
particularly useful in today's restrictive regulatory
environment.
Inventors: |
Markle; Stephen P.;
(Alexandria, VA) ; Jones; Randall J.; (Scottsdale,
AZ) |
Correspondence
Address: |
VENABLE, CAMPILLO, LOGAN & MEANEY, P.C.
1938 E. OSBORN RD
PHOENIX
AZ
85016-7234
US
|
Assignee: |
NAVALIS ENVIRONMENTAL SYSTEMS,
LLC
Scottsdale
US
|
Family ID: |
37053690 |
Appl. No.: |
11/908527 |
Filed: |
March 20, 2006 |
PCT Filed: |
March 20, 2006 |
PCT NO: |
PCT/US06/10165 |
371 Date: |
September 13, 2007 |
Related U.S. Patent Documents
|
|
|
|
|
|
Application
Number |
Filing Date |
Patent Number |
|
|
11276880 |
Mar 17, 2006 |
7534357 |
|
|
11908527 |
|
|
|
|
60665736 |
Mar 28, 2005 |
|
|
|
60777520 |
Feb 27, 2006 |
|
|
|
Current U.S.
Class: |
210/638 ;
210/150; 210/201; 210/202; 210/205; 210/537; 210/748.11; 210/758;
210/760; 422/186.3 |
Current CPC
Class: |
C02F 1/32 20130101; B63J
4/006 20130101; C02F 2103/002 20130101; C02F 11/06 20130101; C02F
2303/06 20130101; C02F 1/78 20130101; C02F 2303/16 20130101; C02F
2303/24 20130101; Y02W 10/10 20150501; C02F 9/00 20130101; C02F
2103/008 20130101; C02F 1/24 20130101; C02F 3/12 20130101; Y02W
10/15 20150501; C02F 1/72 20130101; C02F 2209/008 20130101; C02F
2305/023 20130101; C02F 1/001 20130101; C02F 2103/005 20130101;
C02F 2209/11 20130101; C02F 1/5236 20130101; C02F 1/444 20130101;
C02F 2209/04 20130101; C02F 3/1221 20130101; C02F 2301/08 20130101;
C02F 1/001 20130101; C02F 1/444 20130101; C02F 1/72 20130101; C02F
1/001 20130101; C02F 1/444 20130101; C02F 1/78 20130101; C02F 1/32
20130101 |
Class at
Publication: |
210/638 ;
210/758; 210/760; 210/748; 210/205; 210/201; 210/537; 210/202;
422/186.3; 210/150 |
International
Class: |
C02F 9/12 20060101
C02F009/12; C02F 1/72 20060101 C02F001/72; C02F 1/78 20060101
C02F001/78; C02F 1/32 20060101 C02F001/32; C02F 9/04 20060101
C02F009/04; C02F 11/00 20060101 C02F011/00 |
Claims
1. A method for treating wastewater comprising the acts (steps) of:
treating a first influent in a blackwater treatment train, the
blackwater treatment train comprising the acts (steps) of:
screening the first influent in a blackwater screening zone,
clarifying a blackwater screening zone effluent in a clarifying
zone, reducing sludge from the clarifying zone in a sludge
reduction zone, filtering clarification zone effluent in a
blackwater filtration zone, advanced oxidation of a blackwater
filtration zone effluent (permeate) in a blackwater advanced
oxidation zone, and discharging a blackwater advanced oxidation
zone effluent. treating a second influent in a graywater treatment
train, the graywater treatment train comprising the acts (steps)
of: screening the second influent in a graywater screening zone,
treating screened solids from the graywater screening zone in the
sludge reduction zone, filtering a graywater screening zone
effluent in a graywater filtration zone, treating filtered solids
(retentate) from the graywater filtration zone in the sludge
reduction zone, advanced oxidation of a graywater filtration zone
effluent (permeate) in a graywater advanced oxidation zone, and
reusing an advanced oxidation zone effluent.
2. The method for treating wastewater of claim 1, wherein the
blackwater advanced oxidation zone comprises a blackwater stirred
reactor.
3. The method for treating wastewater of claim 2, the blackwater
advanced oxidation zone further comprising the acts (steps) of:
infusing a clarification zone effluent with ozone prior to entering
the blackwater stirred reactor, and oxidizing the ozonated
clarification zone effluent in the blackwater stirred reactor.
4. The method for treating wastewater of claim 1, wherein the
blackwater advanced oxidation zone comprises the act (step) of
disinfecting with ultraviolet light.
5. The method of claim 1, the sludge reduction zone comprising the
acts (steps) of: adding a graywater filtration zone effluent
(retentate), oxidizing the sludge with ozone, removing an oxidized
sludge for disposal, and sending a sludge reduction zone effluent
to the blackwater clarifying zone.
6. The method for treating wastewater of claim 1 wherein the
graywater treatment train does not comingle with the blackwater
treatment train.
7. The method for treating wastewater of claim 1 wherein the first
influent comprises graywater from kitchen operations.
8. The method for treating wastewater of claim 1, further
comprising the act (step) of directing a second graywater
filtration zone effluent (permeate) to the blackwater treatment
train.
9. The method for treating wastewater of claim 1, the graywater
filtration zone comprises the act (step) of ultrafiltration.
10. The method for treating wastewater of claim 1, the graywater
advanced oxidation zone comprises a graywater stirred reactor.
11. The method for treating wastewater of claim 10, the graywater
advanced oxidation zone comprising the acts (steps) of: infusing
the graywater filtration zone effluent (permeate) with ozone prior
to entering the graywater stirred reactor, oxidizing the graywater
filtration zone effluent permeate) in the graywater stirred
reactor.
12. The method for treating wastewater of claim 1, the graywater
advanced oxidation zone comprising the act (step) of disinfecting
with ultraviolet light in a disinfection zone.
13. The method for treating wastewater of claim 1, further
comprising the act (step) of directing a second graywater advanced
oxidation zone effluent to the clarifying zone.
14. The method for treating wastewater of claim 1, further
comprising the act (step) of discharging a third graywater advanced
oxidation zone effluent.
15. A dual-train wastewater treatment system comprising: a
blackwater treatment train, the blackwater treatment train
comprising a blackwater advanced oxidation zone, and a graywater
treatment train, the graywater treatment train comprising a
graywater advanced oxidation zone.
16. The dual train wastewater treatment system of claim 15 further
comprising a sludge reduction zone.
17. A dual-train wastewater treatment system comprising: a
blackwater treatment train, a graywater treatment train and a
sludge reduction zone.
18. The dual train wastewater treatment system of claim 15, the
blackwater treatment train further comprising: a blackwater
screening zone in fluid communication with a blackwater clarifying
zone, the blackwater clarifying zone in fluid communication with a
blackwater filtration zone, and the blackwater filtration in fluid
communication with a blackwater advanced oxidation zone.
19. The dual train wastewater treatment system of claim 16, the
graywater treatment train further comprising: a graywater screening
zone in fluid communication with a graywater filtration zone, the
graywater filtration zone in fluid communication with a graywater
advanced oxidation zone, wherein effluent from the graywater
advanced oxidation zone is available for reuse as technical
water.
20. The dual train wastewater treatment system of claim 15 wherein
the blackwater treatment train and the graywater treatment train
are modular in design.
21. A dual train wastewater treatment system comprising: a
blackwater treatment train, the blackwater treatment train
comprising, a blackwater screening zone in fluid communication with
a clarifying zone, the clarifying zone in fluid communication with
a sludge reduction zone, the clarifying zone in fluid communication
with a blackwater filtration zone, and the blackwater filtration
zone in fluid communication with a blackwater advanced oxidation
zone, a graywater treatment train, the graywater treatment train
comprising, a graywater screening zone in fluid communication with
a graywater filtration zone the graywater filtration zone in fluid
communication with a graywater advanced oxidation zone, and a
conduit for sending filtered solids from the graywater filtration
zone to the sludge reduction zone.
22. The dual train wastewater treatment system of claim 21, wherein
the blackwater advanced oxidation zone comprises a blackwater
stirred reactor.
23. The dual train wastewater treatment system of claim 22, the
blackwater advanced oxidation zone further comprises infusing the
clarification zone effluent with ozone prior to entering the
blackwater stirred reactor, and oxidizing the clarified mixed
liquor in the blackwater stirred reactor.
24. The dual train wastewater treatment system of claim 21, wherein
the blackwater advanced oxidation zone comprises an ultraviolet
unit.
25. The dual train wastewater treatment system of claim 21, the
sludge reduction zone comprising: a sludge reduction tank, the
sludge reduction tank having a baffle that separates the interior
of the sludge reduction tank into a sludge reduction region and an
uptake region, wherein ozonated liquid enters the bottom of the
sludge reduction region and sludge enters the top of the sludge
reduction region, and wherein liquid in the uptake region can exit
an outfall, the outfall located near the top of the uptake
region.
26. The dual train wastewater treatment system of claim 21 wherein
the graywater treatment train does not commingle with the
blackwater treatment train.
27. The dual train wastewater treatment system of claim 21 wherein
the first influent comprises graywater from kitchen operations.
28. The dual train wastewater treatment system of claim 21, further
comprising the act (step) of directing a second graywater
filtration zone effluent to the blackwater treatment train.
29. The dual train wastewater treatment system of claim 21, the
graywater filtration zone comprises the act (step) of
ultrafiltration.
30. The dual train wastewater treatment system of claim 21, the
graywater advanced oxidation zone comprises a graywater stirred
reactor.
31. The dual train wastewater treatment system of claim 21, the
graywater advanced oxidation zone comprising the acts (steps) of:
infusing the graywater filtration zone effluent (permeate) with
ozone prior to entering the graywater stirred reactor, oxidizing
the graywater filtration zone effluent (permeate) in the graywater
stirred reactor.
32. The dual train wastewater treatment system of claim 21, the
graywater advanced oxidation zone comprising the act (step) of
disinfecting with ultraviolet light in a disinfection zone.
33. The dual train wastewater treatment system of claim 21, further
comprising the act (step) of directing a second graywater advanced
oxidation zone effluent to the clarifying zone.
34. The dual train wastewater treatment system of claim 21, further
comprising the act (step) of discharging a third graywater advanced
oxidation zone effluent.
35. The dual train wastewater treatment system of claim 21 wherein
the blackwater treatment train and the graywater treatment train
are modular in design
36. An apparatus to enhance oxidation of treated wastewater, the
apparatus comprising: an interior treatment chamber, the interior
treatment chamber further comprising a fluidized media chamber,
wherein the fluidized media chamber is located within the interior
treatment chamber, the fluidized media chamber houses fluidized
media, and the fluidized media chamber is in fluid communication
with the interior treatment chamber.
37. The apparatus to enhance oxidation of treated wastewater of
claim 35, fluidized media chamber further comprising a pair of
perforated plates that permit fluid communication between the
interior treatment chamber and the fluidized media chamber while
keeping the fluidized media inside the fluidized media chamber.
38. The apparatus to enhance oxidation of treated wastewater of
claim 35, the interior chamber further comprising a blade for
increasing circulation within the interior treatment chamber.
39. The apparatus to enhance oxidation of treated wastewater of
claim 35, wherein the treated wastewater contains dissolved
ozone.
40. The apparatus to enhance oxidation of treated wastewater of
claim 35, further comprising an inlet port, an outlet port, the
inlet port and outlet port being in fluid communication with the
interior treatment chamber, wherein the treated waste water enters
the apparatus through the inlet port, circulates through the
fluidized media chamber and exits the vessel through the outlet
port.
41. The apparatus to enhance oxidation of treated wastewater of
claim 35, wherein the interior treatment chamber further comprises
a cylindrical acceleration chamber.
42. A method of reducing sludge for use in a wastewater treatment
system comprising a clarifying zone and a filtration zone, the
method of reducing sludge comprising the acts (steps) of: reducing
sludge from the clarifying zone in a sludge reduction zone,
treating filtered solids from the filtration zone in the sludge
reduction zone, adding ozone-infused liquid to the sludge reduction
zone, removing reacted sludge from the sludge reduction zone, and
directing clarified mixed liquor from the sludge reduction zone
back to the clarifying zone.
43. A sludge reduction zone for reducing wastewater sludge, the
sludge reduction zone comprising a sludge reduction tank, the
sludge reduction tank having a baffle that separates the interior
of the sludge reduction tank into a sludge reduction region and an
uptake region, wherein ozonated liquid enters the bottom of the
sludge reduction region and sludge enters the top of the sludge
reduction region, and wherein liquid in the uptake region can exit
an outfall, the outfall located near the top of the uptake
region.
44. A method of graywater reclamation and re-use comprising the
acts (steps) of: first, screening graywater to remove solids,
second, filtering screened effluent by ultrafiltration, third,
treating filtered effluent (permeate) by advanced oxidation, and
fourth, selecting from the group consisting of re-using the
effluent and discharging the effluent.
45. The method of graywater reclamation and re-use of claim 44, the
advanced oxidation step further comprising the acts (steps) of:
clarifying ultrafiltration effluent by gravity infusing clarified
effluent with ozone oxidizing ozonated effluent by closed loop
circulation through fluidized media, and, treating oxidized
effluent with ultraviolet light.
46. A method of graywater reclamation and re-use comprising the
acts (steps) of: screening a graywater influent in a graywater
screening zone, treating screened solids from the graywater
screening zone in a sludge reduction zone, filtering a graywater
screening zone effluent in a graywater filtration zone, treating
filtered solids (retentate) from the graywater filtration zone in
the sludge reduction zone, treating a graywater filtration zone
effluent (permeate) in a graywater advanced oxidation zone, reusing
a first graywater advanced oxidation zone effluent, directing a
second graywater advanced oxidation zone effluent to the clarifying
zone, and discharging a third graywater advanced oxidation zone
effluent.
47. A graywater system for reclamation and re-use of graywater
comprising: a screening zone, the screening zone in fluid
communication with a filtration zone, the filtration zone in fluid
communication with an advanced oxidation zone, wherein effluent
from the advanced oxidation zone is re-used.
48. The graywater system for reclamation and re-use of claim 46,
the filtration zone further comprising ultrafiltration.
49. The graywater system for reclamation and re-use of claim 46,
the advanced oxidation zone further comprising ozone-infused
clarified effluent oxidized in closed loop circulation through
fluidized media, and, and wherein oxidized effluent passes though
ultraviolet light.
50. A graywater system for reclamation and re-use of graywater
comprising: graywater influent in fluid communication with a
graywater screening zone, screened solids from the graywater
screening zone in fluid communication with a sludge reduction zone,
a first graywater screening zone effluent in fluid communication
with a graywater filtration zone, filtered solids (retentate) from
the graywater filtration zone in fluid communication with the
sludge reduction zone, graywater filtration zone effluent permeate)
in fluid communication with a graywater advanced oxidation zone, a
first graywater advanced oxidation zone effluent is in fluid
communication with the clarifying zone, and wherein a second
graywater advanced oxidation zone effluent is reused.
51. A method of treating blackwater having total suspended solids
less than 500 parts per million (milligrams per liter), the method
comprising the acts (steps) of: first screening blackwater to
remove solids, second clarifying screened effluent, third treating
clarified effluent by advanced oxidation, and fourth filtering
screened effluent by ultrafiltration.
52. A method of treating blackwater having total suspended solids
greater than 500 parts per million (milligrams per liter), the
method comprising the acts (steps) of: first screening blackwater
to remove solids, second clarifying screened effluent, third
filtering clarified effluent by ultrafiltration, and fourth
treating permeate by advanced oxidation.
53. A method for reducing uncertainty of treatment compliance time
for wastewater comprising the following acts (steps): obtaining an
effluent sample from a wastewater treatment train, measuring
turbidity, measuring oxidation reduction potential (ORP),
Redirecting sampled effluent back into the wastewater treatment
train if measured ORP and measured turbidity fail to satisfy
pre-defined limits.
54. The method for reducing uncertainty of treatment compliance
time for wastewater of claim 53, wherein the redirecting step is
triggered when measured ORP is less than 200 mV and measured
turbidity is greater when 3 NTU.
55. A sludge separating apparatus comprising: a holding chamber,
the holding chamber comprising an inlet, a bottom outlet, and a top
outlet, the bottom outlet further comprising a bottom outlet valve,
wherein the bottom outlet can be closed so that wastewater flowing
into the holding tank through the inlet will ultimately fill the
holding chamber and be forced through the top outlet.
56. The sludge separating apparatus of claim 55, the holding tank
further comprising: a pipe diffuser having a first end connected to
an air dissolving pump and a second end located inside the holding
chamber.
57. The sludge separating apparatus of claim 55, wherein the
wastewater flowing into the holding tank is effluent from a
flocculator.
58. The sludge separating apparatus of claim 57, wherein the
wastewater flowing out of the top outlet flows without mechanical
assistance into a sludge reduction tank.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] The present application claims priority to co-pending United
States provisional patent application entitled "Advanced Oxidation
System For Wastewater Treatment," having Ser. No. 60/665,736, filed
by inventor Randall Jones on Mar. 28, 2005, which is entirely
incorporated herein by reference. The present application also
claims priority to co-pending United States provisional patent
application entitled "Dual-Train Wastewater Reclamation and
Treatment System," having Ser. No. 60/777,520, filed by inventors
Randall J. Jones and Stephen P. Markle on Feb. 24, 2006, which is
also entirely incorporated herein by reference. The present
application also claims priority to co-pending United States
non-provisional patent application entitled "Dual-Train Wastewater
Reclamation and Treatment System," having Ser. No. 11/276,880,
filed by inventors Randall J. Jones and Stephen P. Markle on Mar.
17, 2006, which is also entirely incorporated herein by
reference.
BACKGROUND OF THE INVENTION
[0002] 1. Field of the Invention
[0003] The present invention relates generally to wastewater
treatment systems, and more particularly wastewater treatment
systems where holding large volumes of sludge for later disposal is
difficult. As such, this invention particularly relates to waste
water treatment for ships, off-shore structures and platforms other
large transportation vehicles, mobile/portable treatment systems
(i.e., military support, disaster relief, etc.), remote treatment
systems (i.e. highway rest stops, campgrounds, etc.), industrial
wastewater treatment, food processing, dairy and other light
industrial wastewater treatment applications.
[0004] 2. Discussion of the Related Art
[0005] Land-based wastewater treatment solutions tend to occupy
relatively large spaces to effectuate wastewater treatment. Space,
however, is a premium on transportation vehicles (like cruise
ships), mobile treatment systems (such as used in military
support), and remote treatment systems (like campgrounds), as well
as other similarly situated treatment scenarios.
[0006] Ordinarily, wastewater systems combine blackwater and
graywater prior to treatment. Blackwater and graywater, however,
are very different in terms of chemical makeup (composition,
viscosity), volume, perception by passengers and crew, and
treatment under the law. For example, blackwater must be treated to
a higher standard in most operating areas. Most ships are fitted
with vacuum flush systems with blackwater pollutant concentrations
much greater than those found in graywater. Shipboard water
production, storage and management necessitates costly
infrastructure.
[0007] Shipboard wastewater systems are typically based on
biological treatment. While biological based systems can work,
biological systems are complicated to operate, have a large
footprint in terms of tankage and deck space, are susceptible to
periodic chemical upsets, can be expensive to operate due to costs
of chemicals, require provisioning of these chemicals, have long
start-up times (order of days) and produce large amounts of
sludge.
[0008] Finally, discharge of wastewater is regulated. Compliance
with regulations can be difficult and may require holding volumes
of wastewater for days to complete Biochemical Oxygen Demand (BOD)
testing and other compliance testing. If the treated wastewater
ultimately fails compliance testing, the process must be continued,
which results in lost time and requires larger holding tanks.
[0009] Wastewater treatment systems have been disclosed in the
following United States or foreign patents: U.S. Pat. No. 3,822,786
(Marschall), U.S. Pat. No. 3,945,918 (Kirk), U.S. Pat. No.
4,053,399 (Donnelly et al.), U.S. Pat. No. 4,072,613 (Alig), U.S.
Pat. No. 4,156,648 (Kuepper), U.S. Pat. No. 4,197,200 (Alig), U.S.
Pat. No. 4,214,887 (van Gelder), U.S. Pat. No. 4,233,152 (Hill et
al.), U.S. Pat. No. 4,255,262 (O'Cheskey et al.), U.S. Pat. No.
4,961,857 (Ottengraf et al.), U.S. Pat. No. 5,053,140 (Hurst), U.S.
Pat. No. 5,178,755 (LaCrosse), U.S. Pat. No. 5,180,499 (Hinson et
al.), U.S. Pat. No. 5,256,299 (Wang et al.), U.S. Pat. No.
5,308,480 (Hinson et al.), U.S. Pat. No. 6,811,705 (Puetter), EPO
261822 (Garrett), WO 93/24413 (Hinson) and U.S. Pat. No. 6,195,825
(Jones). None of these references, however, disclose the aspects of
the current invention.
[0010] What is needed is a wastewater treatment system that has a
small footprint, produces dischargeable effluent minutes after
startup, requires virtually no chemical additions, is simple to
operate, minimizes sludge production from biological activity, is
constructed of the most durable components, and produces a high
quality effluent exceeding most stringent effluent requirements
day-after-day. What is also needed is a wastewater treatment system
that can treat the same volume of wastewater in a smaller space
and/or in faster time than currently existing systems to reduce the
space occupied by holding tanks and treatment equipment.
[0011] What is also needed is a system that can accurately predict
treatment compliance results to enable more efficient and
predictable compliance success.
SUMMARY OF THE INVENTION
[0012] The invention is summarized below only for purposes of
introducing embodiments of the invention. The ultimate scope of the
invention is to be limited only to the claims that follow the
specification.
[0013] Generally, the present invention is incorporated in an
integrated, split treatment system that treats blackwater for
compliance and sludge reduction and treats graywater for reuse,
blending and compliance (referred herein as the "dual-train water
reclamation and treatment system" or "treatment system"). For
blackwater, the treatment system incorporates five general phases
(or zones): (1) screening, (2) clarifying, (3) filtering, (4)
advanced oxidation, and (5) sludge reducing. For graywater, the
treatment system incorporates three general phases (or zones): (1)
screening (2) filtering, and (3) advanced oxidation. Each train of
the treatment system (blackwater and graywater) can operate as a
stand-alone system or can be assimilated into an integrated
treatment train for both graywater and blackwater. This system is
particularly useful in today's restrictive regulatory
environment.
[0014] One advantage of the treatment system is the ability to
treat blackwater differently from graywater. Reuse of graywater is
becoming more socially acceptable; blackwater reuse is not.
Moreover, reuse of reclaimed sewage also bears the risk to human
health associated with equipment failure.
[0015] Another advantage of the treatment system is that it reduces
the space needed for wastewater treatment, and space is a premium
for mobile units like cruise ships and other aquatic vessels. The
system is compact in size, simple in design, inexpensive to
operate, built for long term reliable operation in the marine
environment, hatchable, and modular in construction affording ease
of tailoring with selection of correct number of standardized
modules.
[0016] Another advantage of the water reclamation and treatment
system is the use of turbidity, UV transmittance and ORP readings
to predict final BOD levels for compliance or non-compliance in
advance of the compliance test results to enable a more predictable
and efficient treatment. In addition, it affords reach-back,
real-time monitoring of effluent quality.
[0017] Another advantage of the water reclamation and treatment
system is the ability to handle wastewater that lacks predictable
levels of contamination and pH. Ferries or military vessels may
wait for many hours, days, weeks, or even months between heavy
loading events. This type of varied influent can greatly affect a
biological based treatment system. Among other things, a varied
influent causes a lengthy period of limited effectiveness while
biological colonies reform. Unlike the biological systems in use in
many of these applications, varied influent does not affect the
water reclamation and treatment system. In this case, the treatment
system immediately reacts and begins treatment without regard to
effluent strength or pH. In addition, biological treatment systems
typically require a fixed amount of time (1-2 weeks) to establish a
viable colony for wastewater treatment. In this case, the water
reclamation and treatment system begins treating wastewater
immediately after system startup.
[0018] The description of the invention that follows, together with
the accompanying drawings, should not be construed as limiting the
invention to the example shown and described, because those skilled
in the art to which this invention pertains will be able to devise
other forms thereof within the ambit of the appended claims.
BRIEF DESCRIPTION OF THE DRAWINGS
[0019] FIG. 1 illustrates an embodiment of an integrated water
reclamation and treatment system 10.
[0020] FIG. 2 is a flow chart that reflects an embodiment of a
blackwater treatment train 100.
[0021] FIG. 3 a flow chart that reflects an embodiment of a
graywater treatment train 200.
[0022] FIG. 4 illustrates an embodiment of a blackwater clarifying
zone 120 and a sludge reduction zone 170.
[0023] FIG. 5 illustrates an embodiment of a stirred reactor
300.
[0024] FIG. 6 illustrates an embodiment footprint/plan for a 20-gpm
blackwater treatment train 100.
[0025] FIG. 7 illustrates an embodiment footprint/plan for a 30-gpm
blackwater treatment train 100.
[0026] FIG. 8 illustrates an embodiment footprint/plan for a 25-gpm
graywater treatment train 200.
[0027] FIG. 9 illustrates an embodiment footprint/plan for a
100-gpm graywater treatment train 200.
[0028] FIG. 10 illustrates an embodiment of the modularity of the
system 10.
[0029] FIG. 11 is a flow chart that reflects an embodiment of an
alternate blackwater treatment train 100.
[0030] FIG. 12 is a flow chart that illustrates a functional
diagram of flow zones of the system.
DESCRIPTION OF PREFERRED EMBODIMENT
[0031] The descriptions below are merely illustrative of the
presently preferred embodiments of the invention and no limitations
are intended to the detail of construction or design herein shown
other than as defined in the appended claims. In this
specification, the term "graywater" refers to discarded liquid from
sources such as deck drains, lavatories, showers, dishwashers,
laundries, drinking fountains and potentially equipment cooling
water. "Graywater" does not include industrial wastes, infectious
wastes, human body wastes, and animal waste. In this specification,
the term "blackwater" refers to sources such as wastes of human
origin from water closets (toilets), urinals, and medical
facilities transported by the ships soiled drain system (a/k/a
sewage). It also includes animal wastes from spaces containing live
animals. When graywater is combined with blackwater, the waste
stream is characterized as blackwater. In this specification, the
term "technical water" includes water for laundry, flushing water,
cooling water, vehicle wash, etc. In this specification, the term
"advanced oxidation" refers to a process that typically involves
the generation and use of the hydroxyl free radical (OH.sup.-) as a
strong oxidant to destroy compounds that cannot be oxidized by
conventional oxidants such as oxygen, ozone, and chlorine.
[0032] General Design Overview
[0033] The water reclamation and treatment system 10 splits
treatment into a blackwater treatment train 100 and a graywater
treatment train 200. By splitting the treatment of blackwater and
graywater, the treatment system can reclaim graywater for reuse.
Reusing graywater offers several advantages. Among other things,
reusing graywater (1) reduces fresh water making
requirement/consumption, (2) reduces plant operating costs, (3)
reduces tankage requirement (and ultimately the treatment
footprint), (4) reduces ship propulsion plant costs by reduced ship
displacement resulting from smaller tankage requirements, (5)
protects the environment, and (6) reduces the volume of wastewater
needing to undergo blackwater treatment.
[0034] The graywater and blackwater treatment trains differ in
arrangement due to the unique differences of the influent treated.
The principle difference is the location where filtration occurs.
In graywater trains, filtration preferably occurs prior to advanced
oxidation. In blackwater trains, filtration preferably depends on
the level of total suspended solids (TSS). For blackwater with TSS
less than 500 parts per million (PPM), filtration preferably occurs
post-advanced oxidation. For blackwater with TSS greater than 500
parts per million (PPM), filtration preferably occurs prior to
advanced oxidation.
[0035] FIG. 1 provides an example embodiment of an integrated dual
train system designed for shipboard use. Of course, the system
shown in FIGS. 1-12 could be adapted for other uses (such as
land-based uses) as well as other wastewater volumes and loading
conditions. FIG. 12 illustrates the four principle zones of the
water reclamation and treatment system 10. Whether as an integrated
system or as a standalone system, the water reclamation and
treatment system 10 comprises: a solids separation zone, a
filtration zone, and an advanced oxidation zone, with the option of
adding a sludge reduction zone.
[0036] Preferred Blackwater Treatment Train
[0037] The blackwater treatment train 100 can be used as a
standalone system to treat wastewater. Alternatively, the
blackwater treatment train 100 can be used as a retrofit to enhance
existing systems. As illustrated in FIG. 1, the blackwater
treatment train 100 can treat raw wastewater or wastewater first
treated by an existing bioreactor.
[0038] As shown in FIGS. 1 and 2, a first influent 102 enters the
blackwater treatment train 100. Typically, this occurs directly
from an installed blackwater collection system by way of a positive
displacement pump. Alternatively, the first influent could enter
from existing bioreactors. Initially, the first influent 102 enters
a blackwater solids separation zone 108. While there are many ways
to achieve a solids separation zone, it is preferred that the
blackwater solids separation zone 108 further comprises a
blackwater screening zone 110 and a clarifying zone 120.
[0039] The blackwater screening zone 110 performs initial solids
separation. It is preferred that the blackwater screening zone 110
utilizes a 200-micron mesh rotary sieve 111 for initial solid
separation. Screened effluent 112 can be held in an aerated
equalization tank 114. Screened solids from the rotary sieve 111
are directed to either thermal destruction device or to the sludge
reduction zone 170 (discussed below).
[0040] The first influent 102 comprises traditional blackwater
sources, but could also include other sources. For example, in
shipboard designs, it is preferred to include galley wastewater
(sinks and grinders) as part of the first influent 102. In such
cases, it is preferred that galley wastewater enter the blackwater
treatment train 100 after first being directed through grease
traps. Sources such as galley wastewater can be added directly to
the aerated equalization tank 114 as shown in FIG. 1.
[0041] Next, blackwater screening zone effluent 118 is pumped to a
clarifying zone 120. A preferred embodiment of the clarifying zone
120 is shown in FIG. 4. It is preferred that the clarifying zone
120 include a macerating pump 121, a flocculator 122, a clarifier,
an air dissolving pump 130 and a blackwater intermediate tank 135.
The macerating pump 121 helps homogenize the incoming feed to an
optimum particle size compatible with the clarifier. An example of
a macerator pump 121 is Barnes model number DGV2042L. An example of
an air-dissolving pump 130 is made by Nukini, model M25NPD-15Z. It
is preferred that the air-dissolving pump 130 stream a small amount
of air into the wastewater as the wastewater passes through the
flocculator 122.
[0042] While many types of clarifiers are available, the preferred
clarifier is a stainless steel hydraulic-lift dissolved air
flotation device having a cone-shaped top, which is referred to in
this specification as a hydraulic separator 129. Effluent from the
flocculator 122 flows into the hydraulic separator 129 at the inlet
128. Air from the air-dissolving pump 130 is streamed through
diffusers 134. When released from the pipe diffusers 134, dissolved
air forms very fine bubbles that move upwards. This imparts an
upward velocity to the fluid. As this air contacts solid material
it tends to agglomerate onto its surface imparting a positive
buoyant force. This combination of upward fluid velocity and
positive buoyancy floats solids to the surface where they are
removed at specific intervals to the sludge reduction tank 172. It
is also preferred to add a solution of aluminum chlorohydrate by a
dosing pump to attain an optimum concentration (roughly 30 ppm),
which will assist flocculation and floatation of solids.
[0043] Closing outlet valve 132 permits liquid wastewater that
continues to flow through inlet 128 to raise the liquid wastewater
level in the hydraulic separator 129. Ultimately, the liquid
wastewater level will rise to the point that it force the separated
sludge 126 (for this specification, the term "separated sludge"
also includes water from the top of the hydraulic separator 129)
into the inverted cone region at the top of the hydraulic separator
129. When the level is sufficiently high, separated sludge 126
(which has formed a floating blanket) is directed through the
outfall pipe located at the top of the hydraulic separator 129 into
the sludge reduction tank 172. It is preferred to keep the
separated sludge in a liquid, flowable state so that it will flow
without need for mechanical means. With a flowable separated sludge
and having the top of the hydraulic separator 129 higher than the
sludge reduction tank 172 inlet and normal operating level, sludge
flows by gravity into the sludge reduction tank 172.
[0044] The sludge reduction tank 172 is segmented into two regions
by a baffle plate 171. The baffle is oriented to form a barrier at
the top of the tank and open at the bottom allowing communication
between the two tank regions. One side of the baffle plate 171
forms a sludge reduction region 173 and the other side of the
baffle plate 171 forms an uptake region 175. Separated sludge 126
from the hydraulic separator 129 enters the sludge reduction region
173 of the sludge reduction tank 172 near the top of the vessel.
Separated sludge 126, so introduced, will retain its buoyancy and
tend to rise to the top of the tank; while liquid is displaced
downward. Clarified water, which can pass under the baffle plate
171 collects in the uptake region 175 before flowing by gravity
into the blackwater intermediate tank 135.
[0045] Ozonated finishing tank effluent 182 can be introduced into
the sludge reduction tank 172, preferably in the sludge reduction
region 173 in sufficient quantity to oxidize the odoriferous
material. A simple smell test works here. The sludge reduction tank
172 treats sludge through advanced oxidation, with sludge
characteristics transformed by ozonation and oxidation. This
substantially reduces sludge volume by oxidation to carbon dioxide
gas, water and other materials. In addition, the sludge reduction
tank 172 promotes solid and liquid separation. This step also
further clarifies the sludge mixture, forcing clarified water
downward in the device, around the baffle and into the clarified
water uptake region 175. As additional sludge enters the sludge
reduction tank 172 from the hydraulic separator 129, an equal
amount of sludge reduction tank 172 clarified water flows under the
baffle and into the uptake region 175. When the water level reaches
the uptake outfall 177, it is directed to the blackwater
intermediate tank 135.
[0046] The preferred sludge reduction tank 172 is cylindrical in
shape. For separated sludge 126 flow rates of 0.5 gpm, the
preferred sludge reduction tank would be approximately 8 feet tall
and 3 feet in diameter, having a total ozonated volume of
approximately 320 gallons, and providing a total retention time of
10 hours. In addition, the preferred baffle plate 171 is a flat
plate that is positioned within the cylindrical tank as a chord,
running from inside wall to inside wall of the sludge reduction
tank 172.
[0047] Reacted sludge 174 is directed to an onboard disposal system
for thermal destruction or held for overboard discharge at-sea or
pumped ashore. Unlike most, if not all, sludge burning incinerators
in use today, which suffer from odor problems from incineration of
odiferous sludge from bioreactors, the sludge reduction zone 170
removes virtually all odors from the reacted sludge 174, making it
suitable for destruction by thermal devices.
[0048] When the outlet valve 132 is open, clarified water 124 flows
into the blackwater intermediate tank 135. Likewise sludge
reduction tank 172 clarified water 176 from the sludge reduction
zone 170 also flows into the blackwater intermediate tank 135 and
mixes with the clarified water 124.
[0049] Clarification zone effluent 138 proceeds to a blackwater
filtration zone 160. It is preferred that the blackwater filtration
zone 160 comprises blackwater ultrafilters 162 and a blackwater
flush tank 164. It is preferred that the blackwater ultrafilters
162 be pressure fed external plate and frame ultrafiltration
membranes, such as the Pleiade Series manufactured by Novasep
Orelis. This membrane system has approximately 753 square feet (70
square meters) of surface area/module, and can process up to 26.5
gallons-per-minute (6 m.sup.3/hr) per module. System capacity may
be increased by adding additional modules. The blackwater
ultrafilters 162 should be periodically flushed with water produced
by the blackwater ultrafilters 162 and stored in the blackwater
flush tank 164.
[0050] Blackwater retentate 192, comprised of solids and other
material that did not pass through the blackwater ultrafilters 162,
is directed to the sludge reduction zone 170 for treatment, or
bioreactor if installed. Blackwater permeate (i.e., effluent from
the filters) 190 is directed to a blackwater advanced oxidation
zone 140.
[0051] It is preferred that the blackwater advanced oxidation zone
140 comprises an ozone generator 180, at least one, but preferably
two blackwater stirred reactors 142, 144, a blackwater disinfecting
zone 150 and a finishing tank 154. Prior to entering a stirred
reactor, it is preferred to infuse blackwater permeate 190 with
ozone. Ozone can be produced in a blackwater ozone generation zone
180 from ship service oil free compressed air. Many different ozone
generators could work. For example, the 240-g/hr ozone generator
sold by Pacific Ozone, Model R-SGA642, is preferred for treating 30
gpm flows of blackwater. The ozone can be dissolved into a
pressurized stream of blackwater finishing tank effluent 156 for
circulation to the blackwater stirred reactors 142, 144 and the
sludge reduction tank 172.
[0052] The preferred design of the blackwater stirred reactors 142,
144 is shown in FIG. 5. It is preferred to have blackwater stirred
reactors 142, 144 arranged in series. Within each blackwater
stirred reactor 142, 144, neutrally buoyant media 310 provide
sufficient surface area for the interaction and oxidation of
dissolved ozone and soluble and insoluble organic material. For
treating 30 gpm flows, it is preferred to size each blackwater
stirred reactor 142, 144 to provide at least 11 minutes of
residence time for the ozone oxidation reaction to occur.
[0053] Next, blackwater stirred reactor effluent 146 is directed to
a blackwater disinfection zone 150 and treated with ultraviolet
light. Ultraviolet radiation is advantageous because it damages the
genetic structure of bacteria, viruses, and parasites, making them
incapable of reproducing and/or killing them. In addition,
ultraviolet radiation removes ozone. It is preferred that the
blackwater disinfection zone 150 comprises a UV unit 152. It is
preferred to use a medium pressure, high intensity UV unit 152 that
produces polychromatic light for destruction of residual organic
material, and disinfection. An example of such a unit is the Hyde
Marine Model QMD100B1. The UV unit 152 can feature an automatic
cleaning wiper, which can be controlled by the control system 450.
The UV unit 152 also transforms any residual ozone into fast
reacting species, such as hydrogen peroxide and hydroxyl radicals
further consuming any residual organic carbon based material. In
addition, the destruction of residual ozone through this process
allows for post-membrane filtration with ultra filtration where
such filters would not ordinarily tolerate ozone-enriched water
without damage. UV treated water is then directed to the finishing
tank 154.
[0054] Ozone infused water in the finishing tank 154 is
recirculated back to the stirred reactors and UV unit until the
level in the finishing tank 154 reaches a predetermined level.
Blackwater finishing tank effluent 157 is then either pumped
directly overboard if compliant, or pumped to onboard ship storage
tanks for eventual discharge.
[0055] Blackwater finishing tank effluent 157 is typically
colorless and odorless since ozone reaction with wastewater removes
color and odors. This phenomenon is unique and important since most
other technologies used for treating wastewater such as bioreactors
or membrane-bioreactors do not consistently produce effluent of
this visual and olfactory quality.
[0056] The use of gravity separation after grinding in this
application is unique owing to the sludge reduction capabilities of
the sludge holding and sludge reduction tank 172. This allows the
system to be operated in remote environments where sludge
limitations and disposal are major obstacles to system operation
and standard treatment methods would be undesirable in part due to
quantities of sludge produced
[0057] Alternate Embodiment of Blackwater Treatment Train
[0058] Alternatively, the blackwater filtration zone 160 could be
moved from its location prior to the blackwater advanced oxidation
zone 140 and after the clarification zone 120 to after the
blackwater stirred reaction zone 140 as shown in FIG. 11. This
alternate blackwater treatment train is preferred when the total
suspended solids (TSS) is less than 500 parts per million.
[0059] Preferred Graywater Treatment Train
[0060] The graywater treatment train 200 can be used as a
standalone system to treat and reuse graywater or discharge all or
part of the treated graywater. It is preferred to use the same
component design for any graywater treatment train component that
has a counterpart in the blackwater treatment train and vice versa.
The blackwater treatment train 100 and graywater treatment train
200, however, are separate treatment trains and wastewater is not
comingled between the two trains other than where expressly stated.
In other words, the two treatment trains share only component
design; they do not physically share components.
[0061] As shown in FIGS. 1 and 3, a second influent 202 enters the
graywater treatment train 200. Typically, the second influent 202
first enters a graywater solids separation zone 208. While there
are many ways to achieve a solids separation zone, it is preferred
to employ a screening zone 210 after being pumped from a graywater
holding tank (not shown). Preferably, the graywater screening zone
210 includes a resiliently mounted shaker screen 212 where
separation of larger material occurs. The screen is mounted on an
equalization tank 215. Screened solids 216 collected from the
graywater screening zone 210 are directed to the sludge reduction
zone 170.
[0062] Next, the graywater screening zone effluent 218 is directed
from equalization tank 215 to a graywater filtration zone 220. It
is preferred that the graywater filtration zone 220 include
pre-filters 222 graywater ultrafilters 226, a backwash tank 224 and
a graywater intermediate tank 235.
[0063] The pre-filters 222 are preferably skid mounted, stainless
steel vessels. The pre-filters 222 house polyethylene filter
sleeves that will remove particulate material, reducing suspended
solids and oil/grease in the graywater stream. The redundant nature
of the configuration ensures an uninterrupted flow of filtered
water to the graywater ultrafilters 226. The system self-cleans
using its own filtered water. In the preferred embodiment, the
pre-filters 222 are sized to remove particulate larger than 5
micron in size, filters with this capability are available from
Wastewater Resources, Inc, model number AQM 30.
[0064] Next, pre-filter effluent 223 is directed to the graywater
ultrafilters 222. The graywater ultrafilters 222 preferably use
20-nanometer ceramic membranes such as those manufactured by the
Novasep Orelis company of Lyon, France. When using ceramic
membranes, surface wash water is preferably ozonated and it is
preferred not to use chlorine. The preferred source of ozonated
surface wash water is from the graywater finishing tank 254. A pH
neutralization chemical is preferred to adjust the pH of the
reclaim water to a pH of 7.5. For a 25-gpm design, it is expected
that between 50 and 80 gallons per month of pH neutralizer will be
required, volume is dependent upon pH of influent graywater.
[0065] Alternatively, the graywater filters 222 can use
20-nanometer polysulfone synthetic membranes, such as those
manufactured by Wastewater Resources, Inc., model number PC1140.
When using polysulfone synthetic membranes (the alternative
ultrafilter embodiment), it is preferred to add chlorine to the
backwash water for disinfection of the modules. If polysulfone
synthetic membranes are used, it is preferred to add a backwash
tank 224 as shown in FIG. 3. Chlorine use for the backwash tank 224
should not exceed 20 gallons per month for a 25-gpm system. A pH
neutralization chemical is also preferred hereto adjust the pH of
the reclaim water to a pH of 7.5. It is expected that between 50
and 80 gallons per month of pH neutralizer will be required, volume
is dependent upon pH of influent graywater.
[0066] For a 25-gpm design using polysulfone synthetic membranes
(the alternative ultrafilter embodiment), a 94-gallon backwash tank
224 constructed from 1/4-inch polypropylene, such as the one
manufactured by Navalis Environmental Systems, LLC, model number
TK24-007-01, is preferred. For a 25-gpm design using polysulfone
synthetic membranes (the alternative ultrafilter embodiment), the
membranes are each 12-in in diameter and 36-in in height with 1,140
ft.sup.2 of surface area. The process is designed to filter
particles in the range of 0.02 to 0.04 microns at up to 130 degrees
F. with particulate loading not to exceed 750 ppm. This will allow
for backwashing at 24 to 30 minute intervals for two minutes. When
using polysulfone synthetic membranes (the alternative ultrafilter
embodiment), water for the backwash tank 224 is preferred from the
graywater finishing tank 254.
[0067] Graywater filter permeate 227 is collected in the graywater
intermediate tank 235. Graywater intermediate tank effluent 238
proceeds to a graywater advanced oxidation zone 240. It is
preferred that the graywater advanced oxidation zone 240 comprise
an ozone generator 280, at least one, but preferably two graywater
stirred reactors 242, 244, a graywater disinfecting zone 250 and a
graywater finishing tank 254. Prior to entering a graywater stirred
reactor, it is preferred to infuse intermediate tank effluent 238
with ozone. Ozone can be produced in a graywater ozone generation
zone 280 from ship service oil free compressed air. Many different
ozone generators could work. For example, the 120-g/hr ozone
generator sold by Pacific Ozone, Model R-SGA442, is preferred for
treating 100 gpm flows of graywater. The ozone can be dissolved
into a pressurized stream of graywater finishing tank effluent 256
for circulation to the graywater stirred reactors 240, 242. A
second graywater finishing tank effluent 258 can be directed to the
graywater backwash tank 224 in the alternative ultrafilter
embodiment that uses polysulfone ultrafilters.
[0068] The preferred design of the graywater stirred reactors 242,
244 is shown in FIG. 5. It is preferred to have graywater stirred
reactors 242, 244 arranged in series. Within each graywater stirred
reactor 242, 244, neutrally buoyant media 310 provide sufficient
surface area for the interaction and oxidation of dissolved ozone
and soluble and insoluble organic material. It is preferred to size
each graywater stirred reactor 242, 244 to provide at least 5
minutes of residence time for the ozone oxidation reaction to
occur.
[0069] Stirred reactor effluent 246 proceeds to a graywater
disinfection zone 250 and disinfected with ultraviolet light. It is
preferred that the graywater disinfection zone 250 comprises a UV
unit 252. It is also preferred to use a medium pressure, high
intensity UV unit 252 that produces polychromatic light for
destruction of residual organic material, and disinfection. An
example of such a unit is the Hyde Marine QMD100B1. The UV unit 252
can feature an automatic cleaning wiper (as controlled by the
control system 450). The UV unit 252 also transforms any residual
ozone into fast reacting species, such as hydrogen peroxide and
hydroxyl radicals further consuming any residual carbon based
material.
[0070] Graywater finishing tank effluent 290 may be reused 292
(e.g., directed back to laundry feed tanks for reuse as reclaimed
technical water), blended 294 with graywater screening zone
effluent 218, or discharged 296 where regulations permit. The
graywater finishing tank 254 also serves as source water of
backwash for the backwash tank 224.
[0071] Graywater retentate 228 from the graywater filtration zone
220 can be directed to the blackwater sludge reduction zone 170.
Alternatively, graywater retentate 228 could be directed to a ships
graywater transfer system (not shown).
[0072] Preferred Stirred Reactor
[0073] FIG. 5 illustrates the preferred stirred reactor 300. It is
preferred to use the stirred reactor 300 for the blackwater stirred
reactors 142, 144 and the graywater stirred reactors 242, 244.
Referring to FIG. 5, the stirred reactor 300 comprises two
cylindrically shaped chambers: a cylindrical acceleration chamber
302 and a fluidized media chamber 304. The two chambers are mounted
coaxially with respect to each other (i.e., one inside the other).
Two washer-shaped perforated plates 306 on either end cap the
fluidized media chamber 304. One perforated plate is mounted near
the top of the stirred reactor 300 and the other near the bottom.
The volume between the perforated plates 306 houses fluidized media
310. These upper and lower perforated plates 306 hold the fluidized
media 310 in place and away from inlet and outlet ports. It is
preferred that the perforations be sized to allow maximum flow
while retaining the fluidized media 310 between perforated plates
306.
[0074] The cylindrical acceleration chamber 302 is smaller in cross
section and mounted between the perforated plates 306. The
preferred stirred reactor 300 has inlet ports 308 and outlet ports
309 for admitting and exhausting the liquid. At the top of the
stirred reactor 300, a mixer 312 with a shaft 314 containing
multiple blades 316 passes down though the cylindrical acceleration
chamber 302. The mixer 312 moves fluid in the cylindrical
acceleration chamber 302 down and out to the fluidized media
chamber 304 through the bottom perforated plate 306. Ozone enriched
fluids react with dissolved ozone and tiny, outgassed ozone bubbles
which have formed on the fluidized bed, walls of the chamber, and
float freely within the chamber. This enhanced oxidation reactor
allows for advanced treatment in a small space.
[0075] The preferred stirred reactor 300 is for a 100-gpm graywater
or 30-gpm blackwater treatment train is constructed from 316
stainless steel, approximately 3 feet diameter, 8 feet tall, having
a fluidized media chamber 304 volume of 282 gallons and a combined
inside/outside chamber volume of 423 gallons. Thus, it is preferred
that the fluidized media chamber 304 be about 2/3 of the size of
the combined inside/outside chamber volume.
[0076] The preferred stirred reactor 300 is for a 25-gpm graywater
and 10 gpm blackwater treatment train is constructed from 316
stainless steel, approximately 2 feet diameter, 5 feet tall, having
a fluidized media chamber 304 volume of 79 gallons and a combined
inside/outside chamber volume of 118 gallons.
[0077] The stirred reactor 300 can be used alone, in series or in
parallel. FIG. 1 illustrates two stirred reactors 300 connected in
series. When connected in series, the outlet port 309 of one
stirred reactor 300 can be connected to the series inlet port 308
if the second stirred reactor 300.
[0078] The design of the advanced ozone reactor chambers and their
incorporation of fluidized media held in place by perforated plates
allows the process to reach maximum oxidation efficiency in order
to meet modern standards. Earlier use of ozone in other designs
limits the effectiveness of the process and may fail to meet these
more stringent standards.
[0079] System Modularity
[0080] The treatment system 10 is expandable by design. It is
preferred to construct a treatment system 10 from a standard family
of 24-inch and 36-inch diameter tanks. The 24 and 36 inch families
are directed to retrofit design applications. In addition, FIG. 10
discloses an embodiment of a forward-fit blackwater component
design. In a forward-fit design (i.e., new construction projects),
larger diameter tanks can be more easily assimilated into the ship
or other structure than in the typical retrofit situation. In this
way, system treatment capacity is a function of the number of
modular system components selected. Specific advantages of this
design flexibility include: [0081] 1. System capacity is related to
residence time in the reactor vessels. The 100-gpm graywater
treatment system shares common stirred reactor, tank, pumps and
system component (with exception of ultrafiltration units) designs
and materials with the 30-gpm blackwater treatment system. [0082]
2. System components are mounted on either 28-inch or 40-inch
stainless steel squares that afford ease of mounting on ship
foundations. [0083] 3. System blocks can be arranged in a variety
of configurations to optimally use the space available, from a very
compact square to open linear based on available footprint. [0084]
4. Ease of rigging to the designated system compartment: [0085]
24-inch diameter system components fit through a 28''.times.28''
square or 40'' (1 meter) round opening [0086] 36-inch diameter
system components fit through a 40''.times.40'' square or 57''(1.5
meter) round opening [0087] 5. The arrangement enables design for
easy access to areas requiring routine maintenance. [0088] 6. The
system is designed for growth. The modular nature of its components
enables ease of expansion. For example, the capacity of the 25-gpm
Graywater System could easily be increased by addition of a filter
module, and if necessary an additional reactor.
[0089] An illustration of the building block nature of system
capacity and inherent flexibility are provided in FIGS. 6-10.
[0090] Example: 25 gpm Graywater Embodiment
[0091] As previously noted, the water reclamation and treatment
system 10 can operate as a stand-alone system or as part or a more
comprehensive treatment train. The following sections describe
examples of how the treatment system 10 could be incorporated into
different treatment trains. These examples should not be construed,
however, as limiting the invention to the example shown and
described, because those skilled in the art to which this invention
pertains will be able to devise other forms thereof within the
scope of the disclosure set forth herein.
[0092] While a treatment system can be designed to meet existing
conditions and need, the following section summarizes an embodiment
of the treatment system sized to treat 25-gpm of graywater. A
plan/footprint of this embodiment is shown in FIG. 8. Referring now
to FIG. 8, a first modular group 400 and a second modular group 410
of modules house the treatment system. The first modular group 400
comprises two rows of five modules, where each module is 28-inches
square and constructed from stainless steel. The second modular
group 410 comprises one module 28-inches by 41-inches. The modular
sizing shown in this embodiment will permit a total footprint of 54
square feet.
[0093] This modular design can be arranged in a variety of
configurations to optimally use the space available. The modular
design enables ease of expansion. For example, the capacity of the
25-gpm system could easily be increased by addition of a filter
module, and if necessary an additional stirred reactor. System
components are mounted on 28-inch stainless steel squares that
afford ease of mounting on ships foundations, and make a variety of
configurations possible; from a very compact square to open linear.
For ship use, each component preferably fits through a 28-inch
opening for ease of rigging to the designated system compartment.
Further, the arrangement allows for easy access to areas requiring
routine maintenance. Other modular embodiments are shown in FIGS.
6, 7, and 9.
[0094] It is preferred that the treatment system be fully automated
and capable of remote control. It is preferred to use a control
system 450, such as an Allen Bradley Programmable Logic Controller
(PLC). The control system 450 can interface with most ship interior
communication and control systems providing system status where
desired throughout the ship. The control system 450 can alert
operational staff to issues requiring intervention. The control
system 450 can also be configured for reach-back monitoring of
system performance off ship through the addition of networking
components such as modems or ethernet connections. This permits
operators of the system to monitor and solve operational issues as
they arise.
[0095] In this example, treatment system components are preferably
fabricated from 316 Stainless Steel and should be impervious to
ozone. System tanks are preferably constructed from 1/4-inch 316
Stainless Steel. Internal piping should be press fit 316 Stainless
Steel or CPVC for the filter assembly only.
[0096] In this example, the graywater screening zone 210 uses a
shaker screen manufactured by Midwestern Industries, model Gyra-Vib
MR 24 and a shaker tank manufactured by Navalis Environmental
Systems, LLC ("Navalis"), model number TK24-008-01; graywater
ultrafilters 222 manufactured by Wastewater Resources, Inc., model
number PC1140; graywater intermediate tank 235 manufactured by
Navalis, model number TK24-001-01; graywater stirred reactors 242,
244 manufactured by Navalis, model number TK24-003-01; UV unit 252
manufactured by Hyde Marine, model number QMD100B1; a graywater
finishing tank manufactured by Navalis, model number TK24-002-01;
graywater backwash tank 224 manufactured by Navalis, model number
TK24-007-01; ozone generator 280 manufactured by Pacific Ozone,
model number SGA 24 (60 g/hr); control system 450 manufactured by
Navalis model number CP-GW-25; 30-gpm Process Pump manufactured by
Nikuni, model number M40NP; 50-gpm Transfer Pump manufactured by
Gould model number 11ASH262DO; 50-gpm Filter Charging Pump
manufactured by Gould, model number 4SH2E2CO; 100-gpm Filter
Backwash Pump manufactured by Gould, model number 8SH2H2CO; Ambient
Ozone Monitor/Alarm/Shutdown manufactured by IN USA, model number
IN-2000-L2-LC.
[0097] It has been found that during normal operation of the
treatment system, a system sized to handle 25-gpm of graywater
operated in the order of 18 hours a day can reclaim 100 m3/day of
graywater for reuse.
[0098] Elevated ORP Reading and Relationship to Turbidity
[0099] The water reclamation and treatment system 10 will produce
an effluent with elevated ORP (oxygen reduction potential) and a
lowered turbidity when in regulatory compliance as a by-product of
its design. The recirculation of final effluent through a stirred
reactor 300 and subsequently UV light in the disinfection zone
allows the process to be measured through ORP and turbidity scales.
Both of these effects can be measured and quantified by digital
instruments currently available. The preferred instruments are
George Fischer digital ORP meter and transmitter, and the HACH
1720E digital Turbidimeter. These instruments yield a 4-20 ma
output that can be monitored from the 450 (Program Logic
Controller), which controls overall system operations.
[0100] The regulatory environment for discharge of treated
wastewater into the ocean varies from location to location around
the world. Typically Total Suspended Solids (TSS), Biochemical
Oxygen Demand (BOD) and Fecal Coliform are the primary constituents
regulated. TSS may be measured directly and immediately, during,
and after treatment with existing instrumentation. Both Fecal
Coliform and BOD require sampling and laboratory testing after
waiting for a specified period of time. Thus wastewater treatment
operators must wait the specified period of time before learning
whether the treated wastewater has been sufficiently treated to
have permitted discharge. At least in part because of distrust in
technology prior to this invention, some operators have been known
to hold effluent until reaching water outside of regulatory
restrictions--even when using in a certified, properly functioning
treatment device. As a result, real time effluent quality
monitoring for these two constituents is not currently achievable,
creating uncertainty as to the real-time continuous quality of
effluent from wastewater treatment.
[0101] For example, United States 33 Code of Federal Regulations
Part 159 subpart E establishes perhaps the most restrictive treated
wastewater effluent discharge standards in the world today.
Applying to cruise vessels when in certain waters of the State of
Alaska, these ships must meet effluent quality standards of not
more than 30 milligrams per liter TSS, 20 colony forming units per
100 milliliters Fecal Coliform and 30 milligrams per liter BOD.
Typically ships with marine sanitation devices certified to meet
these standards as a result of testing are permitted to discharge
in these waters. However, spot-checking of ships by the State of
Alaska has revealed that numerous ships are out of compliance even
though they are operating certified systems, and they are prevented
from further discharge until corrective action is accomplished. The
causes for failure are numerous, but lack of real-time effluent
monitoring capability has prevented instantaneous recognition of
out-of-compliant system operation so that action might be taken to
cease discharging.
[0102] Given that a properly sized and properly functioning UV unit
operating in water of acceptable UV transmittance characteristics
will effectively destroy or reduce to acceptable levels harmful
bacteria, including the regulated Fecal Coliform, we have found
that measuring ORP and turbidity of treated wastewater as soon as
immediately after treatment can be used to forecast BOD. Measurable
indication of BOD treatment compliance effectiveness at the time of
discharge and displayed through the PLC control center 450 is now
possible because both ORP and turbidity can be monitored
immediately after treatment. Thus, to reduce the uncertainty of
treatment compliance time for wastewater, it is preferred to take
the following steps: (1) obtain a sample of effluent from a
wastewater treatment train, (2) measure Turbidity, and (3) Measure
Oxidation Reduction Potential (ORP), and (4) comparing that to
pre-determined levels based on site-specific regulations.
[0103] Continuous monitoring of ORP and Turbidity through installed
measurement devices connected to the PLC control center 450
indicates BOD levels within the effluent in real time. Indication
of BOD (30 milligrams per liter) concentration compliance with
33CF159 subpart E requirement is provided if ORP is greater than
200 mV and turbidity is less than 3 NTU. Compliance with the
international standard specified in International Convention for
the Prevention of Ships Annex IV at 50 milligrams per liter is also
indicated by ORP being greater than 200 mV and turbidity less than
3 NTU. This gives the operator an accurate active indication of
compliance with modern standards not available through another
means. Other BOD regulatory criteria can be achieved in a similar
manner on a case-by-case basis.
[0104] This unique relationship takes into account both the visible
(suspended solids) and the invisible (dissolved organics) through
the use of turbidity, UV transmittance, and ORP. While the exact
relationship between measured UV Transmittance and BOD not yet
known, it is expected that testing would shown it to be a critical
parameter that will be of more use than turbidity to predict BOD
compliance.
[0105] Visible organics will register in higher turbidity and
dissolved organics will register in lower transmittance and reduced
ORP levels. Biological treatment systems that do not use advanced
oxidation lack the necessary water chemistry to utilize this ratio
and therefore cannot be monitored for compliance in real time. The
use of the oxidation reaction in the configuration listed yield ORP
levels that are high enough to affect a readable ratio. Previous
attempts at this type of oxidation did not yield a readable,
repeatable ratio because the levels, if they were observed, were
not high enough to affect a ratio. Since the readings are both
digital and inferred electronically, effluent quality data can then
be easily transmitted from ship to shore for off ship effluent
quality monitoring and system troubleshooting.
[0106] An alternate method for predicting BOD levels would be to
recreate the unique advanced oxidation water chemistry by injecting
ozone or other oxidizer into the stream at the appropriate
location, expose to UV light, measure ORP and turbidity levels.
[0107] Although the invention has been described in detail with
reference to one or more particular preferred embodiments, persons
possessing ordinary skill in the art to which this invention
pertains will appreciate that various modifications and
enhancements may be made without departing from the spirit and
scope of the claims that follow.
* * * * *