Note: Descriptions are shown in the official language in which they were submitted.
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SINTERED WAVE MULTI-MEDIA POLARITY CONVERSION TREATMENT
APPARATUS AND PROCESS FOR NONDESTRUCTIVE REMOVAL AND
CONDENSATION OF PER- AND POLYFLUOROALKYL SUBSTANCES (PFAS)
AND OTHER DANGEROUS COMPOUNDS
Technical Field
The present disclosure relates to methods of environmental remediation, and in
particular to
methods of removing Per- and Polyfluoroalkyl Substances (PFAS) from soil,
sludge, colloids,
fluids, air, metallic objects, and hard surfaces.
Background
Per- and Polyfluoroalkyl Substances (PFAS) have become a global crisis over
the past few
years due to their extreme toxicity and the discovery of their presence
throughout the
environment including within food and drinking water supplies. There are over
5,000
compounds classified in the PFAS family of compounds. PFAS is found in human
blood in
practically all the population of the United States. Practically all babies
born today have PFAS
in their bodies. PFAS bioaccumulates in the human body and does not degrade.
PFAS is
present in consumer products, food packaging, water repellent, oil repellent,
industrial
processes, aqueous film forming foam (AFFF) for firefighting, TEFLON products
and other
common items. The waste infrastructure in the United States and globally was
not designed
to remove or contain PFAS; and PFAS passes through existing infrastructure
directly into the
environment. PFAS exposure pathways to humans are complete.
Thermal technologies applied for removal of amphiphilic PFAS and associated
mixtures have
special considerations associated with temperature application. Amphiphilic
compounds are
attracted to high energy interfaces. All polar mineral crystal systems
including certain
phyllosilicate minerals present in soil when heated are susceptible to
pyroelectrical current
generation; spontaneous polarity can occur or change when there is a
significant temperature
gradient across a soil bed. The change in temperature slightly modifies the
position of certain
atoms within the crystal structure, which result in a temporary change in
surface polarity. In
addition, thermal elasticity of a crystal lattice during heating causes stress
induced polarity or
piezoelectric currents. Pyroelectric and piezoelectric currents commonly occur
together.
Amphiphilic compounds react physiochemically; they relate physically not
chemically. The
momentary heat induced change in surface polarity causes a temporary voltage
across the
mineral crystal face causing movement of amphiphilic compounds. Uneven heating
can cause
amphiphilic compounds to move when pyroelectric and piezoelectric currents are
generated
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during the heating process. Once movement occurs, the amphiphilic compounds
will move to
cooler portions of the soil bed and accumulate. Even heat distribution is an
important aspect
of treatment. Incineration overcomes this phenomenon through the excessive
application of
high temperatures; however, HF is formed and is immediately dangerous to human
life and
damages equipment.
In situ thermal technologies create large thermal gradients in soil that
generate pyroelectric
and piezoelectric currents, which move amphiphilic compounds and mixtures away
from the
treatment area. Further, when naturally occurring organic compounds in soil
are heated, they
degrade to simple alcohols such as acetone and methyl ethyl ketone. These
alcohols act as
co-surfactants and will trigger liquid crystal formation at the outer edges of
the treatment zone.
The resulting liquid crystal structure serves as a source for continued
amphiphilic compound
groundwater contamination. Pyroelectric and piezoelectric currents are
important
considerations in designing a safe system to remove PFAS amphiphilic compounds
and
associated mixtures.
A variety of thermal treatments of soils have been previously described. US
Patent No.
4,738,206 (Noland), US Patent No. 4,864942 (Fochtman), US Patent No. 4,977,839
(Fochtman) and US Patent No. 7,618,215 (Haemers) describes continuous process
apparatus
that make use of combustion gas for heat. The processes vary greatly in the
temperature used
with US Patent No. 4,738,206 teaching a range of 120 to 450 degrees F and US
Patent Nos.
4,864,942 and 4,977,839 claiming a range of 300 to 400 degrees C, which is 572
to 752
degrees F. They also vary in the treatment gas with US Patent 4,738,206 using
combustion
gas and US Patent No. 4,864,942 and 4, 977,839 teaching the use of an inert
gas such as
Nitrogen and the addition of water. All these Patents rely on moving treatment
gases through
the soil under porous flow conditions to cause boiling and/or evaporation of
contaminants. In
addition, there is no mention in the prior art as to temperature limitation as
a means to prevent
unintended byproducts such as HF. Most prior art views higher application
temperatures to
heat porous media faster by increasing the thermal gradient.
A characteristic of continuous processes is the use of heavy material handling
equipment that
uses large amounts of energy in moving the material through the treatment
process. This
energy use is in addition to that expended in treating and in excavating the
material and
returning it to its final state. Further, continuous processes treat soil in a
very short period of
time (in minutes), which result is using large amounts of energy. There is no
precision in the
application of energy due to the short treatment times. The lack of precision
in energy
application creates a cumulative waste in energy through a large project and
creates the risk
of HF generation from thermal degradation of PFAS compounds. Steep thermal
gradients
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within porous media create pyroelectric and piezoelectric currents that can
redistribute PFAS
rather than remove PFAS.
Static thermal processes that use a pile arrangement are described in US
Patent No.
5,067,852 (Plunkett), US Patent No. 5,213,445 (Ikenberry), US Patent No.
5,228,804 (Balch),
US Patent No. 5,836,718 (Price), US Patent No. 6,000,882 (Bova) and US Patent
9,914,158
B2 (Baker et al). The apparatus of each of these consists of soil that is
placed on a treatment
surface then layered with differing configurations of piping until the desired
configuration is
attained. The pile is then covered with a vapor proof covering prior to
treatment. These
processes also vary greatly in temperature used. US Patent No. 5,067,852 uses
unheated air
as the treatment gas, but teaches some heat is advantageous. At the other end
of the
temperature range US Patent 5,228,804 teaches the use of air heated in a heat
exchanger to
1,200 to 1,400 degrees F. as a treatment gas. More moderate treatment gas
temperatures, to
300 degrees F, are used in US Patent No. 5,213,445 using the treatment gas of
combustion
products from recirculating the off gas, while US Patent No. 6,000,882 injects
combustion gas
of at least 800 degrees F and perhaps as high as 2,500 degrees F to raise the
soil temperature
to the 212 to 350 degrees F range, then exhausts the off gas through the same
piping. Another
approach is taken by US Patent No. 5,836,718 and 7,618,215 in that the soil is
heated by
conduction through the walls of the piping in the soil pile to a temperature
of 90 to 250 degrees
C (194 to 452 degrees F) and the fresh air treatment gas is not heated. US
Patent 9,914,158
B2 uses heaters attached to the walls and floor to distribute heat into porous
media. No
attempts are made to flatten thermal gradients to minimize pyroelectric and
piezoelectric
currents nor does the patent mention any method to treat PFAS vapor emissions.
Yet another approach is taken by US Patent No.10,016,795 (Rockwell et al.)
where a
smoldering process is enabled or enhanced by adding at least 25% total organic
carbon to the
soil and igniting the mixture to destroy contaminants. The smoldering process
can take place
in situ or ex situ. The range of treatment gas application temperatures and
lack of precise
energy application show a general lack of understanding of how hot air moves
through porous
media. Further, the application temperatures were not designed for removal of
PFAS as the
higher temperature ranges cause HF generation. No attempts are undertaken to
reduce
thermal gradients to reduce pyroelectric and piezoelectric current generation,
which can
redistribute PFAS within the porous media. All of the referenced patents do
not contain any
means to remove PFAS from their treatment gas emissions. Nor do these patents
contemplate
treatment of media other than porous media such as soil.
The pile arrangement processes do not require energy intensive material
handling during
treatment; however, they may be characterized as requiring labor intensive
setup and
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disassembly in the activity of layering the piping system within the soil pile
and removing it
after treatment and also covering and uncovering the completed pile.
Static processes that use container arrangements are not as prevalent in the
prior art. One
example is US Patent Reissue No. 36,222 (O'Ham) that has the contaminated soil
loaded into
a tray shaped treatment container, and then directs combustion heat and gases
on the surface
of the soil while the off gas is removed from the bottom of the container.
Temperatures are not
given, but the inlet gas temperatures may be assumed to be in the upper end of
the
temperature range. US Patent No. 6,296,815 (Walker) takes another approach.
The soil is
loaded into tall-insulated containers and then electric resistance heaters are
inserted into the
soil. The containers are moved into an insulated treatment vessel and the soil
heated directly.
The details of the process are not given. Another container arrangement is
described in US
Patent No. 6,829,844 B2 (Brady et al) describes the use of a thermally
conductive vessel that
fits within an insulated treatment chamber. Desiccated electrically heated air
is introduced to
the treatment chamber where the air is drawn through the thermally conductive
vessel via
vacuum lines located near the bottom; treatment gases are drawn through the
soil under
porous flow conditions. The electrically heated treatment gas is maintained
below 1,300 F to
prevent the formation of oxides of nitrogen and oxides of Sulphur. US Patent
No. 8,348,551
teaches a vehicle can drive in a treatment chamber where sacks, cartons and
drums can be
loaded and unloaded directly into a treatment chamber, which is subsequently
heated. Patent
9,914,158 B2 also teaches a moving vehicle can access the interior of the
treatment chamber
to facilitate loading and unloading. US Patent 9,636,723 (Brady) teaches bulk
soil in a
container can be treated in horizontal sections inside a thermally conductive
vessel placed
inside an evaporative desorption treatment chamber.
None of the previous evaporative desorption techniques contemplated treatment
of nonvolatile
amphiphilic PFAS contaminants, nor did they describe any emissions treatment
system or
treatment for anything other than porous media such as soil. Furthermore, the
steep thermal
gradients, the associated pyroelectric and piezoelectric currents and cooler
areas within the
soil box render it impossible for the conventional evaporative desorption
technology to remove
non-volatile amphiphilic PFAS and associated mixtures from porous media.
The review of the prior art summarized above indicates a need for a multimedia
technology
that can safely remove PFAS from porous media (soil, sediment, and other
porous media),
sludge, colloidal matter, biosolids, PFAS foams, PFAS fluids, metallic
objects, hard surfaces
and air.
Summary
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The present disclosure is directed to apparatus and methods for a non-
destructive recovery
of PFAS contaminants from a variety of media, the apparatus including 1) a
polarity conversion
unit for non-destructive PFAS removal from soil, sludges, filter media, and
objects; 2) a vapor
emissions treatment system that causes the formation of pre-nnicellar
aggregates and liquid
crystals; 3) a fluids treatment system for PFAS removal from water, brines,
foams and colloids;
and 4) an amphiphilic decontamination wand for PFAS removal from hard
surfaces.
In some embodiments, the disclosure can provide an apparatus for recovering
PFAS
contaminants, the apparatus including a vapor conversion assembly that
includes a cooling
chase that receives heated vapor containing PFAS from one or more sources of
PFAS-
containing vapor; a misting chamber that receives PFAS-containing vapor from
the cooling
chase; a cooling fluid line that injects droplets of cooling fluid into the
cooling chase and the
misting chamber to cool the PFAS-containing vapor, the cooling fluid having a
temperature
that is cooler than the incoming PFAS-containing vapor and warmer than ambient
temperature. The vapor conversion assembly can additionally include a
permeable Gibbs
energy curtain disposed so that the cooled PFAS-containing vapor passes
through the Gibbs
energy curtain before entering the vapor conversion tank, the Gibbs energy
curtain providing
an enhanced surface area configured to promote condensation of PFAS onto
and/or into the
Gibbs energy curtain; a supply of recycled cooling fluid disposed within the
vapor conversion
tank that is cooled and aerated by one or more internal purge lines delivering
outside air to
the cooling fluid, while maintaining a cooling fluid temperature above ambient
temperature; a
demister tower, including a demister screen, coupled to the vapor conversion
tank so that
droplets of fluid are removed from a mixture of treated PFAS-containing vapor
and air from
the one or more internal purge lines as the mixture passes through the
demister tower; and a
filter within a filter housing that removes PFAS pre-micellar aggregates and
liquid crystals from
the cooling fluid as it is cooled within the vapor conversion tank. The vapor
conversion
assembly can additionally include a brine pot evaporator assembly that
receives the PFAS
pre-micellar aggregates and liquid crystals removed by the vapor conversion
assembly filter,
in combination with additional PFAS-containing fluids and foams, and treats
the resulting
mixture with heated gas flow in combination with an applied vacuum in a batch
process that
yields dried PFAS-containing powder.
In some embodiments, the disclosure can provide a method for recovering PFAS
contaminants from a medium, the method including loading the medium into a
sealable media
treatment vessel of a polarity conversion unit, where the sealable media
treatment vessel
includes two pairs of opposed side walls, an upper lid including a plurality
of air injection heads,
a lower extraction pad, and a shaping screen assembly; where the plurality of
air injection
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heads are configured to deliver heated treatment air to the sealable treatment
vessel; the
shaping screen assembly includes a plurality of planar, vertically oriented,
and parallel shaping
screens; the extraction pad includes a plurality of vapor extraction lines
each extending across
a width of the extraction pad, each vapor extraction line being capable of
drawing heated
treatment from the sealable media treatment vessel, and each vapor extraction
line being
capable of being activated individually and in a sequence; and where when the
sealable media
treatment vessel is loaded with media to be treated the media is disposed
between adjacent
shaping screens of the plurality of shaping screens, and heated treatment air
delivered by the
plurality of air injection heads is is drawn by the vapor extraction lines
through the shaping
screen assembly within the media and removed from the vapor conversion
assembly. The
method can further include treating the medium in the sealable media treatment
vessel with
heated air and transporting the treatment air from the polarity conversion
unit to a vapor
conversion assembly; where the vapor conversion assembly can include a cooling
chase that
receives the treatment air from the polarity conversion unit; a misting
chamber that receives
the treatment air from the cooling chase; a cooling fluid line that injects
droplets of cooling fluid
into the cooling chase and the misting chamber to cool the treatment air,
where the cooling
fluid has a temperature that is cooler than the incoming treatment air and
warmer than ambient
temperature; a permeable Gibbs energy curtain disposed so that the cooled
treatment air
passes through the Gibbs energy curtain before entering a vapor conversion
tank, where the
Gibbs energy curtain provides an enhanced surface area that is configured to
promote
condensation of PFAS onto and/or into the Gibbs energy curtain; a supply of
recycled cooling
fluid that is disposed within the vapor conversion tank and that is cooled and
aerated by one
or more internal purge lines delivering outside air to the cooling fluid,
maintaining a cooling
fluid temperature above ambient temperature; a demister tower, including a
demister screen,
coupled to the vapor conversion tank so that droplets of fluid are removed
from a mixture of
purging air from the cooling fluid supply and treatment air as the mixture
passes through the
demister tower; and a filter within a filter housing that removes PFAS pre-
micellar aggregates
and liquid crystals from the cooling fluid as it is cooled within the vapor
conversion tank. The
method can further include drying the removed PFAS pre-micellar aggregates and
liquid
crystals using a brine pot evaporator assembly by treating the removed PFAS
pre-micellar
aggregates and liquid crystals with a heated gas flow in combination with an
applied vacuum
in a batch process to yield dried PFAS-containing powders.
In some embodiments, the disclosure can provide a method for recovering PFAS
contaminants from a contaminated surface, the method including treating the
contaminated
surface with heated treatment gas using a decontamination wand and recovering
a resulting
PFAS-containing vapor; transporting the PFAS-containing vapor to a vapor
conversion
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assembly to remove at least some PFAS from the PFAS-containing vapor and
generate a gas
mixture; and passing the gas mixture through a vapor phase galvanic separator
vapor phase
to promote amphiphilic self-assembly of PFAS monolayers from residual PFAS
present in the
received gas mixture to yield treated vapor.
Brief Description of the Drawings
Fig. 1: Sintered Wave Multimedia Polarity Conversion Apparatus
Fig. 2: General Cross Section Including Implements, Vapor Line and Fluids Line
Assembly
Fig. 3: General Map View including Implements, Vapor Line and Fluids Line
Assemblies
Fig. 4: Polarity Conversion Unit
Fig. 5: Polarity Conversion Unit w/ Soil Slip Assemblies Cross Section
Fig. 6: Modified Sintercraft Pad Perspective View
Fig. 7: Modified Sintercraft Pad Map View
Fig. 8: Soil Slip Base Framework Perspective View
Fig. 9: Soil Slip Base Framework Cross Section
Fig. 10: Soil Slip Base Framework Map View
Fig. 11: Soil Slip Perspective View
Fig. 12: Static Soil Shaping Screen Assembly Perspective View
Fig. 13: Static Soil Shaping Screen Assembly Cross Section
Fig. 14: Vapor Conversion Tank Perspective View
Fig. 15: Vapor Conversion Tank Entrance Cross Section
Fig. 16: Vapor Conversion Tank Front View Cross Section
Fig. 17: Vapor Conversion Tank Exit Cross Section
Fig. 18: Vapor Conversion Tank Rear Cross Section
Fig. 19: Vapor Conversion Tank Map View
Fig. 20: Vapor Conversion Tank Interior Elements Perspective View
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Fig. 21: Vapor Conversion Tank Interior Elements Cross Section
Fig. 22: Gibbs Energy Curtain Perspective View
Fig. 23: Vapor Phase Galvanic Separator Perspective View
Fig. 24: Vapor Phase Galvanic Separator Housing Cross Section
Fig. 25: Vapor Phase Galvanic Separator Housing Map View without Lid
Fig. 26: Vapor Phase Galvanic Separator Assemblies Cross Section
Fig. 27: Vapor Phase Galvanic Separator Filter Media Cross Section
Fig. 28: Brine Pot Evaporator Assembly Perspective View
Fig. 29: Brine Pot Evaporator Assembly Cross Section
Fig. 30: Brine Pot Evaporator Assembly Map View
Fig. 31: Brine Pot Evaporator Interior Elements Perspective View
Fig. 32: Brine Pot Evaporator Interior Elements Cross Section
Fig. 33: Surface Excess Concentrator Assemblies Perspective View
Fig. 34: Surface Excess Concentrator Assemblies Cross Section
Fig. 35: Surface Excess Concentrator Map View without Lid
Fig. 36: Surface Excess Concentrator Interior Elements Perspective View
Fig. 37: Surface Excess Concentrator Interior Elements Cross Section
Fig. 38: Aqueous Phase Galvanic Separator Perspective View
Fig. 39: Aqueous Phase Galvanic Separator Cross Section
Fig. 40: Aqueous Phase Galvanic Separator Map View without Lid
Fig. 41: Aqueous Phase Galvanic Separator Assemblies Cross Section
Fig. 42: Aqueous Phase Galvanic Separator Filter Media Cross Section
Fig. 43: Amphiphilic Decontamination Wand Perspective View
Fig. 44: Implement and Object Decontamination Base Framework Perspective View
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Detailed Description
PFAS has received significant public scrutiny especially over the past year.
To understand the
context of, and the need for, the presently disclosed apparatus and method, it
is necessary to
understand that PFAS behaves differently than classic regulated chemicals.
Further, it is
necessary to look at the evolution of the environmental regulations within the
United States
and how the PFAS crisis came to be. This current apparatus and method are
intended to
retrofit into existing classic regulated waste infrastructure. PEAS are
amphiphilic compounds,
which are invisible to the naked eye and are attracted to high energy
interfaces where they
self-assemble across those interfaces (forming films). The mere presence of
PFAS
compounds will cause water to move. PFAS formulations are created through a
physiochemical process, which means they associate physically and not
chemically. The
toxicity of PFAS is significantly higher than most classic regulated classic
chemicals.
PFAS were generally used for their surfactant (surface reactive agents)
characteristics, which
have a broad range of applications. Amphiphilic compounds like PFAS contain a
charged head
group with a lipophilic alkyl carbon tail (ball and stick structure); the head
group is attracted to
water (hydrophilic) while the alkyl carbon tail is attracted to oil/fat and
repulsive to water
(hydrophobic). The charged head group can have a negative charge, a positive
charge or both
a positive and negative charge, which depends on the ph. Surfactants reduce
the surface
tension of fluids. When surfactants reach a certain concentration (critical
micelle
concentration), surface tension stabilizes and micelles are formed in the bulk
of the fluids.
Micelles are aggregates with a hydrophobic nucleus; alkyl carbon tails point
inward with
charged heads facing outward in water. Micelles have the opposite structure
when immersed
in oil.
Perfluoroalkyl Substances are fully fluorinated compounds (fluorine atoms
attach to all carbon
atoms in the alkyl carbon tail structure) and are typically the end
degradation product of
precursor partially fluorinated PFAS. Polyfluoroalkyl Substances are partially
fluorinated
compounds where some hydrogens are bonded to the alkyl carbon chain structure.
Both
classes of PFAS can form linear and branched isomers.
When partially fluorinated compounds degrade in the environment the hydrogen-
carbon
structures (hydrocarbon portion) of the alkyl carbon tail structure typically
cleaves off. The
degradation process is not reversable in nature due to the extreme energy
requirement to fully
fluorinate a compound. This degradation phenomenon causes Perfluoroalkyl
Substances
(fully fluorinated compounds) to increase in concentration over time due to
hydrocarbon
cleaving during conventional classic contaminant treatment processes. With
thousands of
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PFAS compounds that can be partially fluorinated, there is a need for a
treatment technology
to remove both Perfluoroalkyl and Polyfluoroalkyl Substances along with
cleaved hydrocarbon
from a variety of media. Measurement of the cleaved hydrocarbon mass and the
increased
Perfluoroalkyl Substances concentration is an indirect method to quantify PFAS
mass that are
undetectable with modern analytical methods. Less than 29 individual PFAS out
of over 5,000
PFAS compounds have an analytical method to measure their presence and
concentration.
These undetectable PFAS are commonly referred to PFAS Dark Matter.
PFAS and PFAS mixtures interact with Gibbs free energy found on surfaces and
interfaces
through Van Der Waals forces. Gibbs free energy are uncompleted molecular
bonds found at
an interface that is characterized by the molecular structure of the bulk and
smoothness of the
interface. Van Der Waal forces are attractive and repulsive forces interacting
with atoms,
molecules and surface polarities (surface charges). Van Der Waal forces differ
from covalent
and ionic bonds as they are caused by correlations in fluctuating
polarizations (charges) of
nearby particles.
The intramolecular forces holding PFAS molecules together consist of the
strongest bonds in
nature (covalent bonds), which is why PFAS molecules are stable and resistant
to destruction.
The high Pauling Electronegativity of Fluorine contributes to the
extraordinary bond strength
with Carbon and the overall stability of PFAS molecules. The intermolecular
forces driving
PFAS interaction with other molecules, surfaces and interfaces are Van Der
Waals forces,
which are relatively weak. This significant aspect of PFAS characteristics
create the
opportunity to safely remove PFAS from various media without destroying the
PFAS molecule
and creating extremely dangerous by-product compounds.
Surfaces and interfaces have specific polar and dispersive energy ratios
specific to the surface
or interface. When a fluid and a solid have matching or closely matching polar
and dispersive
energy ratios, perfect wetting and adhesion occurs as a result. Surfactants
are used to
facilitate energy ratio matching for optimization of wetting and adhesion
properties.
PFAS behavior are largely Coulombs interactions at solid and liquid
interfaces. Coulombs
interactions are largely limited to the immediate area of the interface as
Coulombs law is an
inversed distance squared law where electrical forces quickly dissipate with
distance. Dynamic
surface energy on solid surfaces and surface tension on liquid surfaces are a
Gibbs free
energy phenomenon. Surfactants are commonly used to prevent corrosion on solid
metal
surfaces due to their self-assembly characteristics on high energy interfaces;
they reduce the
surface charge and form a layer preventing corrosion cells from forming on
metal surfaces.
Surfactants are also used to lower the surface tension in fluids. Certain PFAS
can reduce
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surface tension of fluids significantly lower than classic hydrocarbon
surfactant compounds;
nothing else can perform the way PFAS can perform.
Surfactants are typically used to combine compounds that do not mix
(immiscible), like oil and
water. For example, oil and water can be mixed when there is a physical
agitation; however,
the oil and water will separate into separate layers over time. When a
surfactant is added to
the oil and water mixture and physically agitated, the oil and water will not
separate; this
stabilized mixture is an emulsion. The PFAS molecule adheres to both water
(the hydrophilic
portion of the molecule) and oil (the hydrophobic portion of the molecule),
which allows
emulsions to be stable.
Microemulsions are different from emulsions as microemulsions are clear,
thermodynamically
stable, isotropic liquid mixtures of oil, water and surfactant. Cosurfactants
and the addition of
various salts are commonly used in microemulsions. The oil is typically a
complex mixture of
hydrocarbon and olefins (unsaturated hydrocarbon). Microemulsions are formed
through
simple mixing of components where simple emulsions are created through high
physical
shearing of the components. PFAS in the environment are largely mixtures
consisting of
stabilized emulsions or microemulsions.
The environmental regulations that govern chemical storage, wastes and
response to releases
to the environment were implemented on the federal level in the 1970s. Various
regulatory
agencies implemented the evolving environmental laws on the local, state and
federal level.
The vast majority of contaminated lands became contaminated as a result of
historical
practices before regulation. Spill rates for regulated substances dramatically
dropped in the
1980s and continue to drop to present day. Regulation has caused better
management of
regulated substances.
During the early years of regulation, the nation's waste infrastructure was
modernized to
prevent classic regulated chemicals from entering the environment. The
modernized
infrastructure largely included spill prevention structures/devices, lined
landfills, sewage
treatment facilities, drinking water treatment plants and vapor emissions
treatment, which
were all designed for classic regulated chemicals. Cleanup programs for pre-
regulation legacy
contamination were implemented on the local, state and federal level. During
the 1980s and
1990s, agency bureaucracy became the most significant challenge during site
remediation of
legacy contamination due to inconsistent enforcement and unclear cleanup
goals. The
bureaucracies greatly expanded regulation to include an ever-growing list of
chemicals.
During the mid-1990s, industry lobbyists seeking relief from burdensome and
sometimes
arbitrary legacy cleanup requirements and the expansion of regulated
substances lobbied for
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new laws that caused cleanup requirements to be less stringent and to slow or
stop the
expanding list of regulated chemicals by creating complexity in the law. For
example, the 1996
Safe Drinking Water Act (SDWA) was drafted in such a way that it produced a
complex and
cumbersome process. New drinking water standards for newly discovered
contaminants were
nearly impossible to develop and implement; even today. The few new drinking
water
standards developed after the 1996 SDWA were achieved mainly through Acts of
Congress,
by-passing the SWDA process. The current Congressional activities related to
PFAS are
designed to by-pass the 1996 SWDA. States are engaged in the same activity
where they are
developing their own regulation. PFAS remains unregulated even though PFAS has
been a
recognized toxin for almost 20 years. The United States Environmental
Protection Agency
(EPA) has recently set a PFAS action level but not an enforceable drinking
water standard.
In addition to the 1996 SDWA, other laws were passed making it easier to not
perform actual
cleanups of contaminated properties. Starting from 1994, institutional
controls became the
selected remedy for a growing number of sites. Institutional controls are
simply storing
contamination at the site by placing a cap over the top. Shallow groundwater
was generally
not considered worth protecting after the 1990s. With the 1990s cleanup law
evolution came
a general lack of enforcement for contaminated site cleanup. State and federal
agencies have
not had any meaningful enforcement actions for contaminated sites relative to
the number of
contaminated sites that exist within the United States. This has resulted in
thousands of
contaminated properties sitting idle for decades; either no cleanup actions or
conditionally
closed with a simple cap on the property. Investigations and cleanup of
environmental
contamination lasting decades were the norm. Some sites have been in active
investigation
and cleanup since regulation began with no meaningful results.
The new emerging contaminant class of PFAS, particularly fully fluorinated
Perfluorooctane
Sulfonate (PFOS) and Perfluorooctanic Acid (PFOA), has recently come to the
forefront of
public concern due to extreme toxicity, mobility and ubiquitous presence
throughout the globe.
PFAS has been unregulated since the environmental laws were first implemented
in the United
States. Private tort claim litigation filed shortly after the 1996 SWDA has
driven intense public
interest in PFAS and the general condition and effectiveness of current
environmental law.
Litigation across the country has uncovered documents that appear to indicate
that
manufacturers of PFAS products knew of its toxicity and did not disclose the
information to
the environmental agencies or the public. The EPA became aware of PFAS
toxicity through
documents obtained during litigation Discovery in the early 2000s. The EPA's
response to the
PFAS crisis has been bogged down due to the complexity of existing
environmental federal
law. Numerous water districts within the United States had their water
supplies contaminated
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with PFAS where they declared emergencies handing out bottled water to their
customers.
Discovery of PFAS contaminated areas caused new water systems to be installed
using
alternate clean water sources, which is essentially replacing existing
infrastructure. Some
states have filed lawsuits against PFAS manufacturers and have won large
settlements to pay
for resolution of the PFAS crisis.
Correlations have been found that show an association between PFAS exposure
and a variety
of diseases, birth defects and untimely deaths. In addition, some recent
studies seem to show
other associations between PFAS exposure and obstreperous and obesity. Maps
showing
obesity distribution throughout the United States correspond with maps showing
PFAS release
site distribution throughout the United States. Overall national obesity rates
increasing over
time appear to mirror the proliferation of PFAS products over the last 50
years. PFAS appears
to be impacting practically the entire population of the United States
(impacts ranging from
obesity to deaths).
New PFAS laws are under development on a federal and state level. These new
laws are
impacting the entire environmental industry. Properties believed to have been
cleaned up for
classic regulated compounds are no longer considered clean. PFAS groundwater
plumes are
miles long impacting vast areas having gone unregulated for the past 50 years.
One of the most significant routes for PFAS release to the environment is the
use of AFFF in
liquid hydrocarbon fire situations, which began in the 1960s. AFFF is a
microemulsion in its
concentrated form. VVhen mixed with water, using a special fire nozzle, foam
(an emulsion) is
created to cool and suffocate a fire. The interfacial energies of the foam
cause the foam to
float on top of fuel range liquid hydrocarbon. The AFFF foam sticks together;
when debris falls
into AFFF foam, the foam self-heals (the hole quickly closes up) preventing
reignition of the
fire. AFFF is used on petroleum fires especially around airports, plane crash
sites, bulk storage
facilities and oil refineries. AFFF is also used to prevent spilled petroleum
from igniting. The
foam prevents flammable vapors from forming around a spill. Bulk storage
facilities typically
have a mixture of petroleum and PFAS present in the soil and groundwater from
legacy spills.
The federal government required airports to have AFFF on hand for use on plane
crashes and
to routinely engage in live training exercises. The US Department of Defense
extensively used
AFFF in bases worldwide and used the foam in routine training exercises. AFFF
is by far the
best firefighting foam for liquid hydrocarbons fires ever made and was
distributed all over the
world. Researchers have been trying to find a replacement for years and had
not been
successful. For more than 50 years, AFFF waste was typically managed like
harmless water.
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This approach has resulted in significant groundwater PFAS contamination
around the nation
and the globe.
PFAS has also been found to accumulate in municipal landfills and wastewater
treatment
plants (sewage plants). Municipal waste contains large amounts of discarded
consumer
products, food packaging, biosolids, and flocculent sludges that contain PFAS.
Landfill
leachate, the fluids that come from the landfill debris, historically has been
directed to local
sewer plants, which were not designed to remove PFAS. In addition to
landfills, sewer plants
receive PFAS from industrial sources, chrome plating plants, dry cleaners,
human waste and
other sources. PFAS passes directly through sewer plants untreated into local
waterways. As
previously mentioned above, Perfluoroalkyl substances actually increase in
concentration as
a result of degradation of Polyfluoroalkyl substances. This is especially
problematic for the
eastern United States where drinking water is largely obtained locally through
surface water
or groundwater. There are a large number of PFAS sites in the eastern United
States where
obesity rates are the highest in the country. California has a large number of
PFAS
groundwater contamination sites also; however, the vast majority of drinking
water in California
is imported from the Sierra Nevada mountains and the Colorado River where
there is very little
PFAS contamination. The obesity rates in the California PFAS areas are orders
of magnitude
lower than the eastern United States PFAS areas.
Sewer plants generate biosolids that contain PFAS, which are typically
deposited on farm
fields for use as fertilizer. PFAS contaminated farm fields are known to
contaminate food
supplies including livestock and milk. There are now thousands of acres of
farmland
contaminated with PFAS due to biosolids spreading. PFAS is a global issue with
no
commercially available method to safely remove these compounds from soil,
sludge, high
concentrate PFAS fluids, metallic objects, hard surfaces and air. This present
disclosure is
intended to provide a multimedia non-destructive treatment process for PFAS on
cleanup spill
sites and from accumulation facilities such as landfills, sewer plants, water
treatment plants
and vapor emissions. The present disclosure is intended to be used to
modernize existing
waste infrastructure to safely remove PFAS preventing the unchecked spread of
PFAS into
the environment and sensitive receptors.
There are numerous ex situ treatment techniques available for petroleum
hydrocarbons,
solvents, PCBs and pesticides; however, safe ex situ treatment techniques are
not available
for PFAS. Current thinking calls for contaminant destruction. This line of
thinking has worked
well for classic regulated contaminants like petroleum hydrocarbons; however,
the carbon-
fluorine bond (C-F bond) in PFAS is among the strongest in nature. The high
electronegativity
of fluorine gives the C-F bond a significant polarity/dipole moment. The bond
disassociation
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energy is 5 to 10 times greater than other carbon halogen bonds. Destroying
PFAS results in
dangerous byproducts such as hydrofluoric acid (HF). HF dissolves glass, metal
and organic
matter. HF is immediately dangerous to life and health. Further, breaking the
C-F Bond
requires high energy and is expensive, significantly more costly than classic
regulated
compounds.
Incineration is the only technology commercially available to remove and
destroy PFAS. Any
incineration technology deployed on PFAS contaminated media requires HF
treatment where
calcium powder is sprayed into the effluent vapor stream to create calcium
fluoride. The
effectiveness of HF treatment is in question and there are attempts in
Congress to prohibit the
use of incineration for PFAS. Incinerators are complex, hard to permit and
costly. Only one
incinerator in the United States has been upgraded since the late 1990s. With
only 23 aging
hazardous waste incinerators in the United States, the incineration national
infrastructure is
not sufficient to satisfy the upcoming PFAS treatment needs. The majority of
PFAS
occurrences within the United States are located within non-attainment air
basins where
incinerators would not be allowed to operate. New incinerators will take
decades to permit,
construct and to begin operations. The Sintered Wave Technology is a flameless
emissions
friendly device that can be deployed throughout the United States in all air
basins. There are
approximately 16,000 sewer plants, 4,000 active landfills and up to 10,000
inactive landfills in
the United States today that have no cost-effective means to safely remove
PFAS from
wastewater, leachate, sludge, biosolids or vapor emissions.
Amphiphilic compounds like PFAS are weakly bonded to surfaces. Surface
polarity governs
the bonding capacity as the bonds are Van Der Waals forces. Thermal energy
will increase
entropy and disorganize surface polarity to a point where amphiphiles will be
released from
the surface. Even distribution of thermal energy is an important factor in
amphiphilic removal
from a surface.
The methods and apparatus of the present disclosure may be categorized as a
multimedia
polarity conversion technology where Gibbs free surface energy and Coulombs
interactions
are altered through static geometry, high surface area, treatment gas
velocity/temperature
modulation followed by a physiochemical PFAS vapor emissions treatment.
Coulombs
interaction forces play a significant role in adhesion of nonvolatile
amphiphilic compounds and
mixtures to porous media and other high energy interfaces. Traditional thermal
technologies
focus on boiling or evaporating volatile and semi volatile classic regulated
contaminants from
soil and then using commercially available vapor emissions treatment systems.
Commercially
available oxidizers dissolve when they are used for PFAS treatment due to HF
formation.
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The present disclosure recognizes the nonvolatile amphiphilic nature of PFAS
and the hazards
of destroying PFAS. Given Coulombs law, the inverse squared relationship
between charges
and distance, the PFAS Van Der Waal surface bonding is limited to surficial
charges at an
interface. Techniques used to reduce media thermal resistivity and flatten
thermal gradients
cause disorganization of surface polarity, which provide a reliable trigger to
non-destructively
remove nonvolatile amphiphilic PFAS compounds and associated mixtures from a
variety of
media. Temperature, velocity, geometry and high surface area are used to
disorganize surface
polarity, which safely removes PFAS while maintaining its molecular integrity
during the
process. The process is amenable to removal of other classic regulated
compounds and
cleaved hydrocarbon comingled with the nonvolatile amphiphilic PFAS compounds
and
mixtures.
The USPTO has no unique category for multimedia polarity conversion
decontamination
technologies. Prior art comparisons can be made with thermal technologies even
though the
actual physical functions (boiling/evaporating volatile and semi volatile
substances) are
different from the concept of multimedia polarity conversion decontamination.
All prior art
thermal technologies create thermal gradients within porous media capable of
producing
pyroelectric and piezoelectric currents. Techniques to lower thermal
resistivity, flatten thermal
gradients and disorganize surface polarity are critical in safe PFAS removal.
Prior art for ex situ thermal desorption technologies reveal that there are
two basic categories
of thermal desorption techniques: 1) techniques that involve mechanical
agitation of the soil
during the heating process and 2) techniques that are applied to static
configuration of soil.
Often the techniques that involve mechanical agitation also operate in a
continuous process
where soil is continuously introduced to the process and is mechanically moved
through the
process apparatus until treatment is complete, and then is continuously
discharged to a
container for disposal or reuse.
Alternatively, techniques that are applied to static configuration of soil are
generally treated in
batches where a batch or given amount of soil is introduced to the apparatus;
the treatment
process is started, and when complete, is stopped and the treated soil
removed. The next
batch of soil is then introduced to the treatment apparatus. Static
configuration techniques
may also be broken down into two subcategories: (a) pile arrangement and (b)
container
arrangement.
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Another characteristic of thermal desorption technology is the source of heat
and the gas used
to affect the decontamination. The exact mechanisms that occurs in thermal
desorption is not
well understood and a variety of techniques have been proposed in prior art.
The concept of
polarity conversion, reduction of thermal resistivity and the reduction of
pyroelectric and
piezoelectric currents is a new concept in this field of art. Some processes
use combustion
gases from the burning of fossil fuels as both a source of heat and the
treatment gas.
Sometimes the fuel is supplemented by recirculating the contaminated off gas
from the treated
soil to the burn chamber as additional fuel. Other processes have used fresh
air, or inert air
as the treatment gas, and heat the treatment gas indirectly in a heat
exchanger prior to
introducing the gas to the soil or heat the soil and not heat the treatment
gas.
Nearly all prior art processes use combustion of fossil fuel as a heat source.
This has
undesirable consequences of forming incomplete products of combustion, oxides
of nitrogen
and sulfur, and other greenhouse gases as a by-product. Combustion also has
the potential
to add unburned hydrocarbon to the process exhaust gas if strict control of
the combustion
process is not maintained.
A variety of temperatures have been used for the treatment and in control of
the off-gas
temperature, which is indicative of soil temperature. The temperature and time
at temperature
may be varied depending on the specific characteristics of the soil and
contaminants.
The advantages of a static process using a container are that the container
can provide for
ease of loading and unloading material reducing labor when compared with pile
arrangements,
and it does not require high energy costs for material handling when compared
to continuous
processing arrangements. A disadvantage of these prior art container
arrangements is they
require handling the soil to move it from the container in which it was placed
after excavation,
which presumably would be a dump truck hopper, load it into the treatment
container for
treatment, and then handle it again following treatment to put in back into
the dump truck
hopper disposition. Treatment containers are typically turned upside down to
empty treated
soils, which can create a physical hazard to site workers. The current
disclosure provides a
three-element flow through assembly to contain, transport and treat PFAS
contaminated soil
or sludge. The upper two elements of the assembly are simply lifted with a
forklift where the
treated soil falls out of the bottom of the assembly. The third flow through
element base is
lifted from the treated soil pile with a forklift making easy safe unloading
operations.
Static arrangements are perhaps the most cost-effective treatment option for
large scale
situations; however, static arrangements outlined in prior art have issues
related to treatment
gas and contaminant transport through porous media. This is especially true
for higher
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molecular weight compounds present in saturated fine grain soils. Static
arrangement
effectiveness is dependent on soil type, moisture concentration and type of
contaminant.
Saturated fine grain soil contaminated with a high molecular weight compounds
such as crude
oil or PFAS will not be effectively treated by static arrangements. Air flow
is minimal through
saturated fine grain soils rendering static arrangements not effective. In
drier more permeable
soils, high molecular weight compounds will evaporate then re-condense when
cooler portions
of the soil bed are encountered as the treatment gases move through the soil
bed (porous
flow conditions). Large thermal gradients in static arrangements cause
pyroelectric and
piezoelectric currents that impact PFAS removal effectiveness. These phenomena
result in
longer treatment times that increase energy consumption and incomplete
treatment. Bench
and pilot testing are required to assess static arrangement effectiveness for
each project.
Another issue related to static arrangements is the nature of treatment gas
movement through
the soil bed. All prior art technologies move treatment gases through the
porous media (porous
flow conditions) from an entry point to an exit point. The issue with the
concept is that soils
near the entry point are quickly treated while the exit point soils are
treated last. The entry
soils are continually heated beyond what is necessary for effective treatment,
which is a waste
of energy and can generate HF from PFAS soils. Soil is a poor conductor of
heat, which cause
large thermal gradients over significant distances and cause pyroelectric
current generation.
None of the prior art consider techniques to modify soil thermal resistivity
as a means of
efficient soil heating and flattening thermal gradients.
As mentioned above, moving hot air through soil creates re-condensation issues
within the
soil bed. Further, the pile arrangements typically treat the entire pile at
once, which require
larger blower, heater and vapor treatment apparatus. These larger equipment
requirements
create a limit of how large the pile arrangement can be, which in turn impacts
the scalability of
the device. There is no precision in the application of energy due to the
nature of treatment
gas flow through porous media. Soils at the entry point are repeatedly treated
when treatment
is complete and soils at the exit received minimal treatment. The lack of
precision in energy
application creates a cumulative waste in energy through a large project and
poses significant
risk of HF formation when removing PFAS.
The current disclosure contemplates fluids treatment as part of a multimedia
treatment system.
One aspect of the fluid treatment is the concept of concentrating surface
excess. Surface
excess is a term of art referring to amphiphilic compounds populating the
surface of a
fluid/water body interface (high energy surface). The vast majority of
amphiphilic mass is found
at or near the air/fluid interface. The presence of salts reduces repulsive
forces between the
amphiphilic polar heads, which allow a higher concentration of amphiphilic
compounds to
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occupy the interface. PFAS Micelles are also found near the surface. Residual
monomer
PFAS is found in the bulk of the fluid (away from the interface) in low
concentrations.
US Patent 10,259,730 (Ball, et al.) teaches that PFAS can be separated through
passing air
through a fluid to create a foam. The patent goes on to say that PFAS is
transferred to the
foam where the foam is separated from the fluids. The patent indicates that a
partial
destruction can be accomplished through oxidation. Foam fractionation has been
around for
decades. The Ball patent does not teach anything related to surface excess.
Further, the Ball
patent does not mention that PFAS released to the environment is a mixture and
not a pure
chemical. PFAS occur as microemulsions, which is the framework of foam
production.
Emulsions are created through physical shearing and introduction of air
bubbles into a
solution. Microemulsions are a mixture of salt, oil, and surfactants that can
support an
emulsion or foam. PFAS does not transfer to foam, it is the foam. AFFF
concentrate
microemulsions are designed to create foam.
The current disclosure uses a two-stage process to 1) create a surface excess
complex, which
is removed for drying/ultimate disposal and 2) a removal process for residual
PFAS
monomers. When creating a foam from PFAS contaminated water, long chain PFAS
generally
create the framework of the foam. When long chain PFAS form foams, short chain
and partially
fluorinated PFAS self-assemble on the foam/water interface. PFAS is present in
the foam, at
the foam/water interface and just below the foam/water interface. The Ball
patent only recovers
a portion of the PFAS population and does not include means or methods to
remove foam.
The Ball patent removes the foam for the purpose of partial destruction of
PFAS through
oxidation. The current disclosure uses the complete surface excess profile to
remove short
and long chain PFAS for drying and off-site disposal; no destruction of PFAS_
The fluids treatment line of the present disclosure uses system vacuum to draw
outside air
through the surface excess concentrator via vented purge lines where air
bubbles are formed
to create a foam. The foam, the foam/water interface and just below the
foam/water interface
together contain a saturated PFAS layer. The foam largely contains long chain
PFAS while
the interface largely contains shorter chain PFAS and micelles. A rotating
belt comprised of a
specific surface energy profile separates the foam, the interface and the
micelles from the bulk
of the fluids. The foam and fluids are drawn by the applied system vacuum into
the Brine Pot
Evaporator where they are dried to a powder. The treated bulk fluids exit the
Surface Excess
Separator from the bottom (below the surface) and are routed to the Aqueous
Phase Galvanic
Separator where galvanic currents offer high energy interfaces of varying
charges for
monomeric PFAS compounds to self-assemble. The galvanic filter media can be
recharged in
the Polarity Conversion Unit for reuse.
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The use of polarity conversion is a unique process to disconnect am phiphilic
nonvolatile PFAS
compounds from a variety of media. The polarity conversion process also can
remove classic
regulated organic compounds that are commonly found comingled with PFAS at
release sites.
The presently disclosed apparatus and method use a physiochemical PFAS vapor
emissions
treatment system to provide system vacuum and vapor conveyance for 1) a
Polarity
Conversion Unit for PFAS removal from soil, sludges, rechargeable PFAS
galvanic filter media
and objects, 2) a fluids treatment line for PFAS removal from water, brines,
foams and colloids,
and 3) a hard surface amphiphilic decontamination device for removal of PFAS
films. The
presently disclosed apparatus and methods can remove classic organic
contaminants mixed
with PFAS and cleaved hydrocarbons generated through degradation of partially
fluorinated
PFAS. The technology is intended to use the three implements outlined above
for cleaning
PFAS releases to the environment, providing a means to remove PFAS from
landfill leachate,
landfill gas, sewer plant waste water, sewer plant biosolids, and for hard
metal and concrete
surfaces.
The physiochemical emissions treatment system uses a combination of devices to
remove
PFAS and classic organic compounds from treatment gases coming from the
various
implements (Polarity Conversion Unit, fluids treatment, hard surface
Amphiphilic
Decontamination). The primary emissions treatment device for PFAS removal is
the Vapor
Conversion Tank where cooling fluids cause PFAS aggregation. The chemistry of
the cooling
fluids combined with rapid cooling through direct fine spray into the
treatment gas cause pre-
micellular aggregates and liquid crystals to form, which are removed through
physical filtration.
The cooling fluid temperature is regulated to remain above ambient outdoor
temperatures to
prevent water vapor condensation inside the vapor Conversion Tank. After vapor
cooling, the
Gibbs energy curtain situated inside the Vapor Conversion Tank is designed to
condense
compounds of matching energies (same or similar polar and dispersive surface
energy profile
as condensed compounds). The Gibbs Energy Curtain tines are removed when
completely
coated with contaminant for safe off-site disposal. Residual vapor phase PFAS
are removed
with the Vapor Phase Galvanic Separator, which uses adjustable granular metal
galvanic cells
of high surface area to offer high energy interfaces of varying charges for
PFAS to self-
assemble. The galvanic media is recharged in the Polarity Conversion Unit.
Other emissions
treatment elements include a cyclone dust separator, an electric catalytic
oxidizer and
granulated activated carbon vessels to remove classic contaminants prior to
discharge to the
atmosphere. The electric catalytic oxidizer and granulated activated carbon
vessels offer a
method to measure cleaved hydrocarbons, which offers an indirect measurement
of
Polyfluoroalkyl substances (fluorine unsaturated) or PFAS Dark Matter.
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The primary implement, Polarity Conversion Unit, is an automated, adjustable,
static, enclosed
arrangement that uses transportable "flow through" treatment vessels to
efficiently remove
PFAS (linear and branched isomers), PFAS amphiphilic stabilized emulsions,
microemulsions,
monomeric annphiphiles and classic organic contaminants and assorted mixtures
thereof from
a variety of media including 1) porous media such as a mixture of soil,
gravel, rocks, sediments
or other porous media, 2) colloidal sludges such as flocculent sludge,
wastewater biosolids,
paper sludges and other colloidal matter, 3) vapor and aqueous phase
rechargeable PFAS
galvanic filter media and 4) objects such as down hole drilling implements and
excavator
implements such as wheel loader buckets. The entire assembly uses static
geometry, high
surface area, treatment gas temperature and velocity modulation to reduce
thermal resistivity
of the media under treatment. Treatment gas is sequentially routed around
vertical shaped
media beds where efficient thermal energy distribution flattens thermal
gradients and
disorganizes surface polarities (Gibbs free energy/Coulombs interactions) that
disconnect
amphiphilic compounds and associated mixtures from high energy interfaces.
Soil and sludges are treated by using a three-element flow through assembly
for containment,
transport and treatment; Soil Slip Base Framework, Soil Slip, and Static Soil
Shaping Screen.
The loaded assembly is placed into the Polarity Conversion Unit. Treatment gas
is routed
around vertically shaped soil/sludge beds of high surface area in small
sections to alter surface
polarity within the bed. Treatment gas (air) is modulated for velocity and
temperature. In
combination with vertical and horizontal geometry of the open treatment gas
pathway, thermal
resistivity is reduced along the soil/sludge surfaces allowing fast
penetration of thermal energy
into the media under treatment. The thermal energy disorganizes surface
polarity within the
media releasing nonvolatile amphiphilic PFAS compounds. This is exactly what
happens when
metal reaches its curry point temperature; metal loses its magnetism at
specific temperature
due to disorganized polarity within the metallic crystal structure (within the
bulk and the
surface). Rechargeable galvanic PFAS filter media is the same size as the Soil
Slip assembly
and can be recharged the same method as the soil and sludge. Objects such as
drilling rod
and earth moving equipment implements (excavator buckets) can be placed on a
flow though
base and decontaminated in the Polarity Conversion Unit.
The fluids treatment line of the present apparatus uses system vacuum to draw
outside air
through fluids in the Surface Excess Concentrator where air bubbles are foamed
creating a
foam and a saturated PFAS interface (surface excess complex). The foam largely
contains
long chain PFAS while the saturated interface largely contains shorter chain
PFAS and
micelles just below the interface. A rotating belt comprised of a specific
surface energy profile
(polar and dispersive energy similar to PFAS contaminant) separates the foam,
the interface
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and the micelles from the bulk of the fluids. The foam and fluids are drawn by
the applied
system vacuum into the Brine Pot Evaporator where they are dried to a powder
in an isolated
batch process. The treated bulk fluids exit the Surface Excess Separator from
the bottom
(below the surface) and are routed to the Aqueous Phase Galvanic Separator
where galvanic
currents offer high energy interfaces of varying charges for residual
monomeric PFAS
compounds to self-assemble. The galvanic filter media can be recharged in the
Polarity
Conversion Unit for reuse.
The third implement of the present disclosure is the amphiphilic
decontamination on hard
surfaces and objects. Hard surfaces such as airport runways and dump truck
beds can be
decontaminated using the Amphiphilic Decontamination Wand where static
geometry, surface
area, treatment gas temperature and velocity modulation lowers thermal
resistivity and
disorganizes surface polarity. System vacuum contains and conveys PFAS to the
vapor
emissions treatment line.
Selected embodiments of the disclosure include the use of a multimedia
technology aspect to
serve safe treatment needs for PFAS, classic regulated organic compounds and
mixtures
thereof in soil, sludge, fluids, foams, metallic objects, hard surfaces and
air.
The present disclosure can also include the use of high surface area available
for treatment.
The present disclosure can also include the use of surface polarity (Gibbs
free
energy/Coulombs interactions) conversion to break adhesion of amphiphilic PFAS
compounds
from interfaces.
The present disclosure can also include the use of treatment gas temperature
modulation and
velocity modulation as a method to reduce surface thermal resistivity.
The present disclosure can also include the use of vertical and horizontal
geometry of open-
air gaps to further reduce the surface thermal resistivity.
The present disclosure can also include a flameless heat source allowing
temperature control
and the use of the apparatus in restrictive air basins
The present disclosure can also include non-destructive techniques to safely
remove and
condense PFAS from a variety of media.
The present disclosure can also include sequential treatment; treating small
sections at a time.
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The present disclosure can also include the three-element soil/sludge flow
through vessel
assembly that allows media transport, treatment, top loading and bottom empty
capabilities.
The present disclosure can also include the ability to perform fractional
treatment (different
application temperatures at different stages of treatment) of compound
mixtures.
The present disclosure can also include the ability to selectively treat
vapors of classic
regulated organic compounds separately from PFAS compounds.
The present disclosure can also include the condensation of PFAS vapors using
a
physiochemical direct fluid spray process creating PFAS pre-micellular
aggregates and liquid
crystals, which are removed through filtration of the recycled cooling fluid.
The present disclosure can also include the use of polar and dispersive
surface energy ratio
matching as a means of condensing compounds from vapors.
The present disclosure can also include the use of rechargeable galvanic
filter media to
remove amphiphilic PFAS compounds from air and fluids using galvanic currents
or impressed
currents.
The present disclosure can also include the use of replaceable and adjustable
granular
galvanic media for establishment of a galvanic cell.
The present disclosure can also include maintaining a vacuum over the entire
system.
The present disclosure can also include the use of a three-element soil slip
flow-through
assembly where portions of the assembly can be used for rechargeable filter
recharge and
metallic object decontamination.
The present disclosure can also include an adjustable vapor emission line
assembly.
The present disclosure can also include a fluids treatment line assembly.
The present disclosure can also include the ability to dry high concentrate
PFAS fluids and
foams while treating emissions generated from the drying process.
The present disclosure can also include the ability to concentrate long chain
PFAS, short chain
PFAS and PFAS micelles into foam and a high concentrate surface fluid layer
mixture.
The present disclosure can also include the use of a rotating belt to remove
PFAS foam and
surface fluids through rotation speed and surface energy (Gibbs surface
energy) matching.
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The present disclosure can also include the use of an amphiphilic
decontamination wand to
remove amphiphilic PFAS compounds from hard surfaces like metal and concrete.
The present disclosure can also include the safe and non-destructive removal
of PFAS, which
can then be dried to a powder for safe off-site disposal.
The present disclosure can also include the ability to use a system vacuum and
vapor
emissions treatment line assembly to safely remove dried PFAS powder and the
powder into
a standard disposal drum.
The present disclosure can also not produce oxides of nitrogen (Nox), oxides
of sulfur (Sox),
particulate matter (PM), HF or PFAS emissions allowing its use in restrictive
air basins.
The present disclosure can also include batch processing that allows
measurement of wet
density, dry density and contaminant intensity in treated media for every
batch allowing macro-
sampling and analysis maps to be generated in real time during site cleanup
operations.
The present dislcosure can also include the reduction of thermal gradients
within the media
under treatment as a means to reduce pyroelectric and piezoelectric currents;
currents caused
by steep thermal gradients that redistribute PFAS within the media under
treatment.
The present dislcosure can also include the ability to perform a macro Total
Oxidizable
Precursor Assay for unsaturated Polyfluoroalkyl Substances (PFAS Dark Matter)
using a
electric catalytic oxidizer exotherm to measure cleaved hydrocarbon mass
during fractional
treatment.
List of Reference Numbers
The following reference numbers are used in the drawings to refer to selected
components
and aspects of the present disclosure, including a brief description of their
purpose.
Ref. no. Component/Aspect Purpose
1 Polarity Conversion Unit Provides sealed contained
treatment,
sectional/sequential treatment, modulation of
treatment gas, and velocity modulation of the
treatment gas.
2 Blower Provides velocity modulation of
the treatment
gas.
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3 Heater Provides flanneless temperature
modulation of
the treatment gas.
4 Modified Sintercraft Pad Provides system vacuum,
sectional and
sequential treatment in concert with the Polarity
Conversion Unit.
Individual Extraction Line Provides applied vacuum to system and
treatment gas conveyance.
6 Vapor Extraction Isolation Isolates treatment gas flow
within the system;
Damper directs applied vacuum and
directional flow.
7 Vapor Extraction Manifold Creates isolated treatment
zones.
8 Cyclone Dust Separator Static in-line system that
removes fugitive dusts
from the extraction line prior to emissions
treatment system.
9 Catalytic Oxidizer Bypass Isolates Catalytic Oxidizer
in order for it to be
Damper on line or by-passed depending on
contaminant
under treatment or stage of treatment.
Electric Catalytic Oxidizer Destroys classic organic contaminants such as
fuel range hydrocarbons and cleaved
hydrocarbons using flameless oxidation and
measures contaminant mass through the
catalyst exotherm (temperature rise across the
catalyst through time).
11 Cooling Chase Cooling hot air through direct
injection of fluid of
varying droplet size.
12 Cooling Chase Cooling Cooling Fluid recirculated from
the Vapor
Fluid Line Conversion Tank.
13 Mist Chamber Small fluid droplets injected to
create an
evaporative environment for water
14 Vapor Conversion Tank Condenses PFAS through a
physiochemical
process.
Gibbs Energy Curtain Disposable curtain materials selected to match
Access energy of condensed contaminant;
matching
polar and dispersive energy profiles of
contaminant and curtain material
16 Purge Line Using system vacuum, ambient air
is drawn into
the Vapor Conversation tank to cool the fluid,
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create increased surface area within the fluid
and to maintain fluid temperature above
ambient temperature.
17 Vapor Conversion Tank Removes residual mists through
large cross-
Demister Tower sectional area of the tower,
tower height and a
demister screen.
18 Filter Housing Removes pre-micellular aggregate
and liquid
crystals precipitated within the cooling fluid.
19 Jet Pump Removes cooling fluid from the
Vapor
Conversion Tank and delivers the fluid to the
Cooling Chase and Mist Chamber.
20 First Vapor Extraction First system vacuum extraction
blower that
Blower (in series) provides system vacuum and
treatment gas
conveyance.
21 Bearing Cooling Water Stores water that is circulated
through the
Tank (First Blower) Vapor Extraction Blower to cool
the bearings
during operation.
22 Vapor Phase Galvanic Uses galvanic currents (galvanic
or impressed
Separator currents) to offer high energy
interfaces of
varying charges to cause amphiphilic PFAS
self-assembly on the galvanic media in vapor
phase.
23 Vapor Phase Granulated Uses vapor phase granular
activated carbon to
Activated Carbon Vessel (2 absorb residual PFAS as a final emissions
in series) treatment.
24 Second Vapor Extraction Second system vacuum
extraction blower in
Blower (in series) series that provides system
vacuum and
treatment conveyance for the vapor phase
galvanic separator and vapor phase granular
activated carbon treatment systems.
25 Bearing Cooling Water Stores water that is circulated
through the
Tank (Second Blower) Vapor Extraction Blower to cool
the bearings
during operatio.
26 Vent Stack Provides the final exit of
treated treatment
gases at elevation.
27 Vent Stack Weather Cover Protects vent Stack from weather
intrusion.
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28 Brine Tank Vapor System vacuum and vapor
conveyance is
Extraction Line (Connects applied to the fluids treatment
assembly line.
to 7)
29 Brine Pot Evaporator Assembly dries, in isolated batch
runs,
accumulated fluids/foams to a powder by
drawing hot treatment gases through fluids in
tank; tank connected to emission treatment
line.
30 Brine Pot Demister Tower Removes residual mists
through large cross-
sectional area of the tower, tower height and a
demister screen.
31 Blower Provides air to flameless heater.
32 Heater Provides flameless heat drawn
through fluids
for evaporation/drying.
33 Vapor/Foam/Fluids Provides system vacuum to Surface
Excess
Extraction Line/Valve Concentrator headspace and
conveyance of
foam/fluid mixture to the Brine Pot Evaporator.
34 Amphiphilic Provides connection to system
vacuum,
Decontamination Wand emissions treatment and
conveyance of PFAS
Flexible Extraction vapors from the Amphiphilic
Decontamination
Line/Valve Wand to the emissions treatment
line.
35 Amphiphilic Provides temperature and velocity
modulated
Decontamination Wand treatment gas directly to hard
surfaces under a
shroud to alter surface polarity for amphiphilic
PFAS removal.
36 First Fluids Pump (in series) Provide conveyance of
fluids to the fluid
treatment line assembly.
37 Surface Excess Provides mechanisms to
concentrate and
Concentrator remove surface excess in foam and
the upper
surface of the fluids; removes long chain PFAS
(in foam) and short chain PFAS (at fluid
surface) and PFAS micelles just below the
surface.
38 Surface Excess Using system vacuum, ambient air
is drawn
Concentrator Purge Lines through the purge lines and
through the fluids
tank to create bubbles, which in turn
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concentrates long chain PFAS in foam, short
chain PFAS at the fluid surface and PFAS
micelles just below the surface.
39 Aqueous Phase Galvanic Uses galvanic currents
(galvanic or impressed
Separator (2 in series) currents) to offer high energy
interfaces of
varying charges to cause amphiphilic PFAS
self-assembly on the galvanic media in
aqueous conditions.
40 Second Fluids Pump (in Provides conveyance of treated
fluids to final
series) discharge point.
41 Powder Vacuum Assembly Provides safe means to remove
dried PFAS
powder from the Brine Pot Evaporator or other
areas of the apparatus using the system
vacuum, vapor/powder conveyance and
emissions treatment. The powder is deposited
into a standard storage drum.
42 Catalytic Oxidizer Dilution In the event of an over-
temperature situation in
Valve the catalyst bed, the dilution
valve is opened
where system vacuum draws cool ambient
outside air into the catalyst bed for cooling.
High hydrocarbon concentration is the primary
cause for an over-temperature situation.
43 Blower/Heater Isolation Provides a means to isolate a
given
Damper Blower/Heater assembly from the
Polarity
Conversion Unit when the given Blower/Heater
assembly is not in operation.
44 Soil Slip Base Framework Provides a multi-purpose flow-
through
framework base for treatment of soil, sludges
and objects. The Base accommodates the Soil
Slip Assembly including the Soil Shaping
Screen or rechargeable filter media (from the
Galvanic Separators). The Base has forklift
pockets to accommodate transport of a variety
of assemblies for treatment.
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45 Soil Slip Base Framework Provides a transportable flow
through
used to Decontaminate framework base to accommodate
Objects decontamination of metallic
implements such
as drilling implements and excavator buckets.
Metallic surfaces are high energy interfaces
where amphiphilic PFAS will self-assemble;
disorganizing surface polarity removes
amphiphiles.
46 Vapor Extraction Trunk Provides vapor conveyance from
implements to
Line emissions treatment assembly and
provides
system vacuum.
47 Brine Pot Evaporator Provides system vacuum, vapor
conveyance
Connection Valve and emission treatment connection
for the
Brine Pot Evaporator and other fluid line
treatment elements.
48 Brine Pot Vapor Extraction Provides Brine Pot
Evaporator isolation when
Line Damper Valve off line.
49 Static Soil Shaping Screen Provides a means to create
shapes for soil or
Assembly sludge with specific shaped air
gaps where
treatment gas can be drawn around the shaped
vertical beds. The Static Soil Shaping Screen
geometry is designed to offer high surface area
and create low thermal resistivity along the soil
bed surfaces. Modulating treatment gas
temperature and velocity further reduces
thermal resistivity at the soil bed surfaces.
50 Soil Slip Provide four walls to contain
soil and sludge in
concert with the Static Soil Shaping Screen and
Soil Slip Base Framework; all flow-through
structures that can accommodate treatment,
top loading, transport and bottom empty
capability after treatment.
51 Isolated Vapor Extraction Provide a means to isolate
treatment to a small
Chamber section using damper valve.
52 Soil Retention Tab Within the Soil Slip Base
Framework, provides
a bottom to retain soil or sludge held in the
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Static Soil Shaping Screen and Soil Slip.
Accommodates treatment air flowing around
shaped vertical soil or sludge beds.
53 Flow through Air Gap Within the Soil Slip Base
Framework, provides
an air gap for treatment gases to freely flow
around shaped vertical soil or sludge beds.
54 Forklift Pockets Provides a means to transport a
variety of
assemblies for treatment.
55 Isolated Vapor Extraction Allows for Soil Slip
Assemblies to be placed
Chamber Register into the Polarity Conversion Unit
in either
direction; no front or back to Soil Slip assembly.
56 Soil Slip Open Top and The Soil Slip is part of a
three-element system
Bottom to contain, top load, transport,
treat and bottom
empty treated media. The Soil Slip is a flow
through device with on top and bottom; just four
walls.
57 Soil Slot Provides a space for soil or
sludge to occupy
during transport and treatment. The space
offers a high reactive surface area for
concentrated temperature and velocity
modulated treatment gas to flow across. The
surface area is designed in such a way to
reduce thermal resistivity, which in turn alters
surface polarity that triggers amphiphilic PFAS
to lose adhesion to surfaces.
58 Air Gap Provide a space for treatment gas
to flow
across vertical soil beds where temperature
and velocity can be modulated to reduce
thermal resistivity and in turn disorganize
surface polarity.
59 Air Gap Cover Prevent soil or sludge from
entering the air gap.
60 Soil Fill Line Designates the level for soil or
sludge to be
filled up to.
61 Vapor Conversion Tank Provides conveyance for cooling
fluid from the
Cooling Fluid Return Line bottom of the Vapor Conversion
Tank through
the Filter housing to the Jet Pump.
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62 Cooling Chase Spray Provides a fan spray array across
the vapor
Nozzle flow path for cooling.
63 Vapor Conversion Tank Provides visual observation
inside the Vapor
View Window Conversion Tank.
64 Vapor Conversion Tank Provides a means to sample the
cooling fluid at
Fluid Sample Port the bottom of the tank.
65 Vapor Conversion Tank Provides access to the inside of
the Vapor
Access Hatch Conversion Tank for maintenance.
66 Vapor Conversion Tank Provides surface area for
surface energy
Gibbs Energy Curtain matching condensation. The
curtain material is
designed to match the polar and dispersive
surface energy of the condensing contaminant.
67 Vapor Conversion Tank Provides a vapor pathway that
will shed mists
Vapor Diversion Baffle and further cool vapors prior to
exiting the
Vapor Conversion Tank.
68 Fluid Level The optimum level of cooling
fluid.
69 Vapor Conversion Tank The cooling fluid is primarily
water with
Cooling Fluid additives including alcohols,
salts, hydrocarbon
surfactant and urea (one or more of these
additives).
70 Gibbs Energy Curtain Tab The energy matching material
in which a
contaminant will condense due to polar and
dispersive energy matching.
71 Gibbs Energy Curtain Air Allows treatment gases to
pass through for
Gap further treatment.
72 Vapor Phase Galvanic Provides a vapor tight seal to
the Galvanic
Separator Tank Lid Separator Housing.
73 Vapor Phase Galvanic Provides an entrance to treatment
gas where
Separator Inlet the cross-sectional area
increases as the vapor
approaches the galvanic filter media to slow
gas velocity.
74 Vapor Phase Galvanic Provides an exit for the
treatment gas.
Separator Outlet
75 Vapor Phase Galvanic Provides a vertical bed for
granular metal
Separator Granular Metal particles of varying galvanic
energies. The
Slot granular nature of the metal
particles offers
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high surface area in a small space. Further, the
volume of the anodic metal particles can be
reduced in mass to increase the electrical
voltage across the galvanic cell.
76 Vapor Phase Galvanic Provides a vertical bed for
granular desiccant
Separator Granular media to bridge between the
various granular
Desiccant Bridge Slot metal vertical beds. Desiccant
absorbs water,
which will conduct electrical energy between
the galvanic cell members.
77 Vapor Phase Galvanic The filter media is rechargeable.
The charge
Separator Rechargeable distribution across the galvanic
cell offers
Filter Media multiple charge scenarios (high
energy
interfaces) for different charged amphiphilic
PFAS to occupy different portions of the cell. As
the surface area of the granular metallic media
becomes occupied with a self-assembled
amphiphilic PFAS monolayers, the voltage
decreases due to reduced galvanic potential.
Voltage drops across the galvanic cell indicates
the degree of amphiphilic PFAS self-assembly
that has occurred across the galvanic cell. The
media is recharged by placing the media in a
Soil Slip Assembly and treating the assembly in
the Polarity Conversion Unit.
78 Brine Pot Access Hatch Provides access to the interior
of the Brine Pot
Evaporator.
79 Brine Pot Fluid Level Provides a view of fluids level.
Window
80 Brine Pot Water Spray Provides a method to knock down
accumulated
Foam Knock Down foams for treatment. High
pressure bursts of
Assembly cooling fluid from the Vapor
Conversion Tank
provide a means to break down foam structure
and reduce foam levels.
81 Brine Pot Drain Valve Provides a means to drain the
brine Pot
Evaporator Tank.
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82 Brine Pot Purge Lines Provides the conveyance for
heated air to be
drawn through the fluids in the Brine Pot
Evaporator. Heated are, up to 1,100 F
evaporate the fluids in the tank.
83 Brine Pot Water Spray Provides a wide fan of high-
pressure cooling
Foam Knock Down Spray fluid from the vapor Conversion
Tank to break
Nozzle down accumulated foam structure
and reduce
foam levels.
84 Brine Pot Evaporator Fluid The optimal fluid level for
evaporation.
level
85 Surface Excess Provides entry of untreated
fluids into the
Concentrator Inlet Surface Excess Concentrator.
86 Surface Excess Provides an exit for treated
fluids. The intake of
Concentrator Outlet the exit is located at the bottom
of the Fluids
Process Tank (92), which is away from the
surface excess present in the resulting foam
and layer of fluids at the foam fluid interface.
The outlet is at the same elevation as the inlet
to maintain gravity flow.
87 Surface Excess Provide separation of the foam
and the
Concentrator Foam Belt foam/fluid interface through belt
rotation speed
and polar and dispersive energy matching the
belt media with the contaminant.
88 Surface Excess Provides space for fluids
treatment that
Concentrator Fluids concentrates surface excess
within the range of
Process Tank the belt (87).
89 Surface Excess Provides a means to apply system
vacuum
Concentrator Foam Tank over the entire unit and
vapor/foam/fluids
conveyance to the Brine Pot Evaporator. The
foam and fluid concentrate are drawn to the
Brine Pot Evaporator by the applied system
vacuum.
90 Surface Excess Provides a means to allow treated
fluids to exit
Concentrator Fluids Exit without contacting the
concentrated surface
Piping (bottom Intake in excess zones.
Fluids Process Tank)
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91 Surface Excess Provides access to the interior
of the vessel.
Concentrator Access Hatch
92 Surface Excess Provides bottom exit of the
Fluids Process
Concentrator Fluids Exit Tank, which is away from the
concentrated
Piping Bottom Intake in surface excess present in the
resulting foam
(88) and layer of fluids at the foam
fluid interface.
93 Foam Foam is generated by outside air,
drawn from
system vacuum, passing through the fluids.
Long chain PFAS are typically incorporated into
foams
94 Fluids Level in Fluids Provides a means to measure
fluids level in the
Process Tank tank.
95 Aqueous Phase Galvanic Provides access into the
Aqueous Phase
Separator Inlet Galvanic Separator.
96 Aqueous Phase Galvanic Provides access into Aqueous
Phase Galvanic
Separator Lid Separator.
97 Aqueous Phase Galvanic Provides an exit for treated
fluids.
Separator Outlet
98 Aqueous Phase Galvanic Provides a vertical bed for
granular metal
Separator Granular Metal particles of varying galvanic
energies. The
Slot granular nature of the metal
particles offers
high surface area in a small space. Further the
volume of the anodic metal particles can be
reduced in mass to increase the electrical
voltage across the galvanic cell.
99 Aqueous Phase Galvanic Provides a vertical bed for
granular molecular
Separator Granular sieve media to bridge between the
various
Molecular Sieve Bridge granular metal vertical beds.
Slot
100 Aqueous Phase Galvanic The filter media is
rechargeable. The charge
Separator Rechargeable distribution across the galvanic
cell offers
Filter Media multiple charge scenarios (high
energy
interfaces) for different charged amphiphilic
PFAS to occupy different portions of the cell. As
the surface area of the granular metallic media
becomes occupied with a self-assembled
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amphiphilic PFAS monolayers, the voltage
decreases due to reduced galvanic potential.
Voltage drops across the galvanic cell indicates
the degree of annphiphilic PFAS self-assembly
that has occurred across the galvanic cell. The
media is recharged by placing the media in a
Soil Slip Assembly and treating the assembly in
the Polarity Conversion Unit.
101 Amphiphilic Wand Hard Provides vacuum, vapor
conveyance and a
Pipe Vapor Extraction handle to manipulate the
Amphiphilic
Handle Decontamination Wand.
102 Amphiphilic Wand Provides treatment gas (air) to
the Amphiphilic
Heater/Blower Assembly Decontamination Wand. Treatment
gases are
modulated for velocity and temperature.
103 Amphiphilic Wand Shroud Provides an enclosed area for
decontaminating
hard surfaces.
104 Sediment Baffle Prevents sediment transport
across the floor of
the Vapor Conversion Tank.
105 Access Door into Polarity Provides access for loading
and unloading soil
Conversion Unit slip assemblies into and out of
the Polarity
Conversion Unit.
106 Light Port Provides a viewing window that
light can be
shined into the interior of the Vapor Conversion
Tank.
Description of an Illustrative Embodiment
1. Overview
Figure 1 presents a perspective view of an exemplary embodiment of an
apparatus according
to the present disclosure (the Sintered Wave Multimedia Polarity Conversion
Apparatus).
Figure 2 presents a General Cross Section Including Implements, Vapor Line and
Fluids Line
Assembly. Figure 3 presents a General Map View including Implements, Vapor
Line and
Fluids Line Assemblies. Other Figures present detailed views of the various
elements of this
apparatus.
The Polarity Conversion Unit (1) provides a means to use a contained
arrangement to treat
soils, sludges, rechargeable galvanic filter media, and objects. Treatment
gases (air) are
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drawn into the apparatus through a blower(s) (2), which then delivers the air
to an electric
heater(s) (3). The blower (2) and heater (3) work in conjunction to modulate
temperature and
velocity delivered into the Polarity Conversion Unit.
There are a number of blower (2) and heater (3) assemblies mounted on top of
the Polarity
Conversion Unit. Only selected blower (2) and heater (3) assemblies are in
operation at any
given time providing focused treatment gas delivery to small sections
delivered sequentially
across the Polarity Conversion Unit (1). Blower (2) and Heater (3) assemblies
are isolated
from the Polarity Conversion Unit (1) when not in operation by a Blower/Heater
assembly
Isolation Damper (43). The blower (2) and heater (3) assemblies operate in
tandem with the
Modified Sintercraft Pad (4) where an individual extraction line (5) can be
isolated with an
Vapor Extraction Isolation Damper (6). The Vapor Extraction Manifold (7)
connects an
individual Vapor Extraction Line (5) to the apparatus vapor extraction system
and Vapor Line
Assembly through the main Vapor Extraction Line to Emissions Treatment (46).
The Soil Slip
assembly that contains soil, sludge, galvanic filter media or objects are
placed inside the
Polarity Conversion Unit (1) for treatment through the Access Doors (105) are
not shown in
Figures 2 and 3 and are described in detail in Section 2 below.
As part of the emissions treatment, a Cyclone Dust Separator (8) removes any
fugitive dusts
that escaped the Polarity Conversion Unit (1). In the event that soils or
sludges contain PFAS
and Hydrocarbon as co-contaminants the Catalytic Oxidizer Bypass Damper (9)
causes the
treatment gases to flow through the Electric Catalytic Oxidizer (10) in order
to destroy and
measure hydrocarbons or cleaved hydrocarbons. An Electric Catalytic Oxidizer
is used to limit
production of oxides of Nitrogen (Nox) and oxides of Sulphur (Sox) in the
emissions. Flame
based oxidizers produce Nox and Sox. The electric oxidizer, which has no flame-
based heat
source, maintains operational temperature below the auto formation temperature
of Nox and
Sox. In a PFAS/Hydrocarbon co-contaminant situation or during a macro Total
Oxidizable
Precursor Assay, the Blower (2) and Heater (3) assemblies will operate at
lower temperatures
to remove the hydrocarbons or cleave hydrocarbons from unsaturated
Polyfluoroalkyls before
PFAS is released from the soil or sludge. If the concentration of hydrocarbon
exceeds a certain
pre-set concentration, which could cause the catalyst to over-heat, the
Electric Catalytic
Oxidizer will activate the Catalytic Oxidizer Dilution Valve (42) to open to
cool the catalyst. In
turn the Blower (2) and Heater (3) assemblies mounted on the Polarity
Conversion Unit (1)
will reduce flows and temperature to accommodate catalyst cooling.
When hydrocarbons and/or cleaved hydrocarbons have been removed from the media
under
treatment, the Blower (2) and Heater (3) assemblies will increase treatment
gas temperature
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and the Catalytic Oxidizer Bypass Damper (9) will be closed causing the
treatment gas to
bypass the Electric Catalytic Oxidizer (10).
Hot treatment gases enter the Cooling Chase (11) for cooling. The Cooling
Chase Cooling
Fluid Line (12) delivers cooling fluid through high pressure water jets and
misting nozzles
mounted in the Cooling Chase (11) and the Mist Chamber (13). Cooling fluids
are directly
sprayed into the treatment gas for cooling. The fine droplet size and the
pressurized delivery
cause an evaporative environment to exist within the Cooling Chase (11) and
the Mist
Chamber (13), which in turn dramatically and rapidly reduces temperature of
the treatment
gas. In order to prevent water from condensing out of the treatment gas, the
cooling fluid is
maintained above ambient outdoor temperature. The cooled treatment gas enters
the Vapor
Conversation Tank (14) where the gas encounters the Gibbs Energy Curtain (not
shown in
Figure 2 or 3). The Gibbs Energy Curtain Access (15) allows replacement of
disposable
elements of the curtain. Internal Purge Lines (16) are located at the bottom
of the Vapor
Conversion Tank (14) to allow outside air to be drawn into the tank by the
applied system
vacuum and bubble through the cooling fluid in the tank. The bubbles cool the
fluids just above
ambient outside temperature and promote mixing within the cooling fluid.
Treatment gases
flow through the Vapor Conversion Tank (14) around an internal baffle (not
shown in Figure 2
or 3) and up through the Vapor Conversion Tank Demister Tower (17) where the
gases flow
to other elements of the emissions treatment system. The cooling fluids are
continually
recycled from the Vapor Conversion Tank (14) where a Filter Housing (18)
removes PFAS
pre-micellular aggregate and liquids crystals that precipitate when the
cooling fluid causes a
sudden and rapid drop in temperature in the Cooling Chase (11). Certain
chemicals mixed
with the cooling fluids enhance the formation of PFAS aggregates and liquids
crystals. The
Jet Pump (19) draws the cooling fluids out of the Vapor Conversion Tank (14)
through the
Filter Housing (18) and pushes the filtered cooling fluid through the Cooling
Chase Cooling
Fluid Line (12) to the Cooling Chase (11) and Mist Chamber (13).
The First Vapor Extraction Blower (in series) (20) applies vacuum pressure and
provides
treatment gas conveyance for the entire apparatus. The First Vapor Extraction
Blower (in
series) (20) bearing assembly is cooled with water stored in the Bearing
Cooling Water Tank
(First Blower) (21). The bearing cooling system allows for a higher tolerance
in temperature of
the treatment gas.
Treatment gas is then routed into the Vapor Phase Galvanic Separator (22)
where residual
PFAS that escaped the Vapor Conversation Tank (14) encounter a galvanic
sequence of
granulated metal that offer high surface area, high energy interfaces of
varying charges for
amphiphilic self-assembly. The resulting voltage can be galvanic or impressed
generated
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currents. Voltage drops across the galvanic cell indicate active self-assembly
and provide an
indication of PFAS mass within the filter media. The galvanic filter media can
be recharged by
placing the filter assembly in the Polarity Conversion Unit (1). Traditional
Vapor Phase
Granular Activated Carbon Vessels (2 in series) (23) are used as a final
emission polishing
treatment.
The Vapor Phase Galvanic Separator (22) and the Vapor Phase Granular Activated
Carbon
Vessels (2 in series) (23) are maintained under vacuum pressure by a Second
Vapor
Extraction Blower (in series) (24) to prevent any leakage during treatment.
The Second Vapor
Extraction Blower (in series) (24) bearing assembly is cooled with water
stored in the Bearing
Cooling Water Tank (Second Blower) (25). The Second Vapor Extraction Blower
(in series)
(24) discharges the treated clean treatment gas to the Vent Stack (26) and
through the Vent
Stack Weather Cover (27) to the atmosphere at elevation.
The Fluids Line Assembly is connected to the Vapor Line Assembly through the
Brine Pot
Evaporator Connection Valve (47), which connects to the Vapor Extraction
Manifold (7).
System vacuum is used to contain, treat and convey PFAS saturated fluids and
foams while
providing a means for vapor phase treatment. The Brine Pot Vapor Extraction
Line (28) draws
PFAS vapors from the Brine Pot Evaporator (29). Vapors exit the Brine Pot
Evaporator (29)
through the Brine Pot Demister Tower (30), which is designed to remove any
mists from the
vapor stream before entry into the vapor line assembly. The Brine Pot
Evaporator (29) is
equipped with a Blower (31) and Heater (32) that provide hot air into the
vessel to facilitate
drying of PFAS fluids concentrate in an isolated batch process.
The Brine Pot Evaporator (29) has isolated two lines connected to downstream
implements.
The first line is the Vapor/Foam/Fluids Extraction Line (33) that provides
vacuum pressure to
the Surface Excess Concentrator (37) and a means of conveyance for separated
foam/fluid
PFAS concentrate. The second line is the Amphiphilic Decontamination Wand
Flexible
Extraction Line (34), which provides vacuum pressure and treatment gas
conveyance for the
Amphiphilic Decontamination Wand (35). The Amphiphilic Decontamination Wand
(35) is used
to decontaminate hard surfaces such as metal, concrete or other similar hard
surfaces where
amphiphilic PFAS self-assembly occurs. The Brine Pot Evaporator (29) creates a
pressure
drop in the vapor stream flow causing foams/fluids to drop out of the vapor
stream where all
emissions are routed to the vapor line assembly for emissions treatment.
Accumulated
foams/fluids are subsequently dried into a powder in the Brine Pot Evaporator
(29) in a batch
process. The Powder Vacuum Assembly (41) is used to remove dried PEAS powder
from the
Brine Pot Evaporator (29). The Powder Vacuum Assembly (41) is connected to the
Vapor
Extraction Line to Emissions Treatment (46). System vacuum provides vacuum and
powder
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conveyance into a disposal drum or vessel; the pressure drop in the drum
allows for powder
accumulation.
The fluids treatment of the disclosed apparatus begins with the First Fluids
Pump (in series)
(36) where raw untreated fluids such as landfill leachate or sewer plant waste
water is drawn
into the apparatus. The First Fluids Pump (in series) (36) discharges fluids
into the Surface
Excess Concentrator (37). Amphiphilic PFAS are attracted to high energy
interfaces such as
the air/water interface or an air/fluid interface. The accumulation of
amphiphilic compounds at
the interface is termed "Surface Excess". Once an interface area has been
covered by an
amphiphilic monolayer, amphiphilic micelles and monomers form within the bulk
of the fluids.
When the surface excess is removed, micelles and monomers in the bulk will
self-assemble
at the newly exposed interface. The Surface Excess Concentrator (37) takes
advantage of the
reliable self-assembly of amphiphilic PFAS compounds as a primary removal
technique.
System vacuum applied to the Surface Excess Concentrator (37) through the
Vapor/Foam/Fluids Extraction Line (33) draws outside air into the Surface
Excess
Concentrator Purge Lines (38) and through the fluids, which in turn causes
foam formation, a
saturated PFAS amphiphilic layer at the foam/fluid interface and a PFAS
micelle layer just
below the surface. The foam and the saturated PFAS amphiphilic layers are
removed by the
Foam Belt (43) for subsequent treatment. The Foam Belt (87) is designed to
have specific
polar and dispersive surface energies to match or nearly match PFAS
amphiphilic mixtures
for maximum adhesion to the belt. The belt speed is modulated to recover the
foam and the
upper layer of the fluids for removal of the entire surface excess column
around the interface.
Residual PFAS monomers are treated downstream of the Surface Excess
Concentrator (37)
The final treatment for the fluids line is the Aqueous Phase Galvanic
Separator (2 in series)
(39); two vessels are assembled in series. The Aqueous Phase Galvanic
Separator presents
a galvanic sequence of granulated metal that offer high surface area, high
energy interfaces
of varying charges for amphiphilic self-assembly. Voltage drops across the
galvanic cell
indicate active self-assembly and provide an indication of PFAS mass within
the filter media.
The galvanic filter media can be recharged by placing the filter assembly in
the Polarity
Conversion Unit (1). The Second Fluids Pump (in series) (40) provide enough
suction to the
fluids to overcome the applied vacuum in the Surface Excess Concentrator (37).
The Second
Fluids Pump (in series) (40) discharges clean treated fluids to an appropriate
discharge point.
Figure 2 presents the map view of the Soil Slip Base Framework (44), which is
a flow through
multipurpose device. All media arrangements treated in the Polarity Conversion
Unit (1) fit
onto the Soil Slip Base framework including soil, sludges, rechargeable
galvanic media (vapor
and aqueous phase) and objects. The Soil Slip Base Framework used to
Decontaminate
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Objects (45) is shown on Figure 2. Objects, mainly drill implements and
excavator implements,
are placed on the framework and inserted into the Polarity Conversion Unit (1)
where surface
polarities are thermally disorganized releasing PFAS amphiphilic films.
2. Detailed Description of Selected Elements of the Illustrative
Embodiment
Figure 4 presents "Polarity Conversion Unit Perspective View. The Polarity
Conversion Unit
(1) is shown in greater detail where the Blower (2) and Heater (3) assemblies
are shown.
There are a number of Blower (2) and Heater (3) assemblies mounted on top of
the Polarity
Conversion Unit. Each of those assemblies can be isolated from the Polarity
Conversion unit
through an Blower/Heater Assembly Isolation Damper (43) when the assembly is
off line. The
Blower (2) and Heater (3) assemblies work in tandem with the Modified
Sintercraft Pad (4).
The Modified Sintercraft Pad (4) has a sectionalized vapor extraction design
where small
sections can be treated sequentially in coordination with the Polarity
Conversion Unit (1).
Individual Extraction Lines (5) are isolated with Isolation Dampers (6) to
facilitate isolated
treatment zones. Dampers (6) are open when an array of Blower (2) and Heater
(3)
assemblies are in operation while at the same time a set of dampers (6) open
for Individual
Extraction Lines (5) directly below. The interior of the Polarity Conversion
Unit (1) is accessed
by the Access Door (105) for loading and unloading.
The Vapor Extraction Manifold (7) provides isolated Individual Extraction
Lines (5) a
connection to the Vapor Extraction Line to Emissions Treatment (46). In
addition, the Vapor
Extraction Manifold (7) provides a connection for the Brine Pot Evaporator
(29) through the
Brine Pot Evaporator Connection Valve (47). The Brine Pot Vapor Extraction
Line Damper
Valve (48) provides isolation during Brine Pot Evaporator (29) operations.
Figure 5 presents Polarity Conversation Unit w/ Soil Slip Assemblies Cross
Section. This
cross-sectional view illustrates how the various assemblies fit together when
in operation.
Mounted on top of the Polarity Conversion Unit (1) are a number of Blower (2),
Heater (3) and
Heater/Blower Isolation Damper (43) assemblies. These assemblies work in
tandem with the
Modified Sintercraft Pad (4) and assorted elements within the Pad. A
transportable flow
through treatment vessel consists of a Soil Slip Base Framework (44), a Static
Soil Shaping
Screen Assembly (49) and a Soil Slip (50). When combined together, all three
elements create
a transportable, flow though treatment vessel that is capable of treating
soil, other porous
media, sludges, colloidal matter and rechargeable galvanic filter media. The
vessel is loaded
from the top and empties from the bottom by simply using a forklift to lift
the Static Soil Shaping
Screen Assembly (49) and a Soil Slip (50) upwards together; the media falls
through the lifted
assembly. The Soil Slip Base Framework (44) is removed from the treated media
pile by a
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forklift in a separate lift operation; treated media flows through the base as
it is lifted from the
pile. Tabs in the Soil Slip Base Framework hold the media in place during
transport and
treatment as described below in Figure 8, 9, and 10. The vessels are loaded
and unloaded
from the Polarity Conversion Unit (1) through the Access Door (105).
Figure 5 also show different elements of the Modified Sintercraft Pad (4)
including the Vapor
Extraction Manifold (7), Individual Extraction Line (5), Vapor Extraction
Isolation Damper (6),
Vacuum Extraction Line to Emissions (46), Brine Pot Evaporator Connection
Valve (47) and
a partial view of the Brine Pot Vapor Extraction Line Damper Valve (48). All
of these elements
are designed to provide system vacuum and vapor conveyance to select portions
of the
system during various stages of operation.
Figure 6 presents Modified Sintercraft Pad Perspective View and Figure 7
presents Modified
Sintercraft Pad Map View. The Isolated Vapor Extraction Chamber (51) provides
a means to
isolate system vacuum and treatment gas flow to the area above through the use
of Individual
Extraction Lines (5) controlled by Vapor Extraction Isolation Dampers (6).
There are two
Individual Extraction Lines (5) located in each Isolated Vapor Extraction
Chamber (51). One
line is short while one line is longer to allow even flow through the
treatment vessel assembly.
Vapor Extraction Isolation Dampers (6) allow treatment to be focused on one
side of the
treatment vessel or the other within a given Isolated Vapor Extraction Chamber
(51). The Brine
Pot Evaporator Connection Valve (47) is clearly shown along with the Brine Pot
Vapor
Extraction Line Damper Valve (48); these elements provide system vacuum and
vapor
conveyance to the Fluids line assembly. Vapors are treated in the Emission
treatment
described above.
Figure 8 presents Soil Slip Base Framework Perspective View. Figure 9 presents
Soil Slip
Base Framework Cross Section. Figure 10 presents Soil Slip Base Framework
Cross Section.
The Soil Slip Base Framework (44) is a common element for a variety of
treatment
arrangements; the unit provides the base lifting apparatus, transport,
retainage of media
above, allows flow through treatment, top loading and bottom emptying
capability. The Base
is lifted with a forklift using the Forklift Pockets (54). The Soil Slip Base
Framework (44) also
serves as the base for object decontamination; typically drill rod and
excavator
buckets/implements. The Soil Slip Base Framework (44) has Soil Retention Tabs
(52) and
Flow Through Air Gaps (53) that line up with the Static Soil Shaping Screen
Assembly (49).
This arrangement along with the Soil Slip (50) allows media to be organized in
vertical beds
where temperature and flow modulated treatment gas can flow around the shaped
beds. The
arrangement allows for a high surface area for active treatment and minimizes
contaminant
travel distance within the vertical bed. Further, the arrangement allows for
an easy transport
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and easy top loading and bottom emptying operation. In addition, the Soil Slip
Base
Framework (44) is designed to insert into the Polarity Conversion Unit (1) in
either direction
through the use of the Isolated Vapor Extraction Chamber Register (55).
Figure 11 presents Soil Slip Perspective View. The Soil Slip (50) consists of
four walls with a
Soil Slip Open Top and Open Bottom (56). The purpose of the Soil Slip (50) is
to provide
horizontal retainage of the Static Soil Shaping Screen Assembly (49) and media
while
registered to the Soil Slip Base Framework (44). Both the Vapor Phase Galvanic
Separator
Rechargeable Filter Media (77) and the Aqueous Phase Galvanic Separator
Rechargeable
Filter Media (100) are designed to fit into the Soil Slip (50) for treatment
in the Polarity
Conversion Unit (1).
Figure 12 Presents Static Soil Shaping Screen Assembly Perspective View.
Figure 13
presents Static Soil Shaping Screen Assembly Cross Section. The purpose of the
Static Soil
Shaping Screen Assembly (49) is to provide a static means to organize media
into vertical
beds of high surface area and to provide an open flow path for treatment gas
to flow around
the vertical beds. Soil Slots (57) and Air Gaps (58) are constructed to line
up with Soil
Retention Tabs (52) and Flow Through Air Gaps (53) in the Soil Slip Base
Framework (44).
The Air Gap Covers (59) prevent soil, sludges or other media from entering the
Air Gaps (58).
Soil is filled to the Soil Fill Line (60), which corresponds with the height
of the Soil Slip (50)
wall height. Treatment gases enter the Air Gap (58) through the sides of the
Static Soil Shaping
Screen Assembly (49). The sides of the Air Gaps (58) are designed to increase
treatment gas
velocity by decreasing cross sectional area of flow in order to lower thermal
resistance.
Further, tabs perpendicular to flow located along the screen edge cause
turbulence along the
surface area, which in turn lowers thermal resistivity. VVire wrap well screen
can be used as
an alternative embodiment where the well screens are place adjacent to each
other in line
with the Air Gaps (58). The Air Gaps (58) can be a fin or pin heat sink
design. The well screens
can be spaced apart to allow additional room in the Soil Slip (50) assembly
for soil and sludge.
Figures 14 through 22 are all related to the Vapor Conversion Tank (14)
showing perspective,
map, cross sectional and internal element views. The Vapor Conversion Tank
(14) conditions
the treatment gas to facilitate rapid cooling, condensation of PFAS, removal
of residual
particulate matter and prevention of water condensation from the treatment
gas. Hot treatment
gases enter the Vapor Conversion Tank (14) through the Cooling Chase (11).
Cooling fluids
supplied by the Cooling Chase Cooling Fluid Line (12) are directly sprayed
into the treatment
gas using a variety of droplet sizes to create an evaporative environment.
High pressure
Cooling Chase Spray Nozzles (62), shown in Figure 18, apply a fan of cooling
fluid of varying
drop size directly into the treatment gas flow stream. Mist spray is injected
in the Mist Chamber
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(13) just prior to entry into the tank. Cooling Fluids drain into the Vapor
Conversion Tank (14)
and are then drawn out through the Vapor Conversion Tank Cooling Fluid Return
Line (61)
passing through the Filter Housing (18) to remove PFAS pre-micellular
aggregate and liquid
crystals from the cooling fluid. The Jet Pump (19) recirculates the cooling
fluid back to the
Cooling Chase (11) through the Cooling Chase Cooling Fluid Line (12). The
cooling fluid
contains water, alcohols, salts, urea and organic matter to enhance the
formation of pre-
micellular aggregate and liquid crystals.
In order to regulate cooling fluids temperature and maintain temperatures
above ambient
outdoor temperature, outside air is drawn through Purge Lines (16), which are
vented at the
top of the Vapor Conversion Tank (14) and equipped with a control valve that
regulates outside
air intake. The Purge Lines (16) are slotted at the bottom of the Vapor
Conversion Tank (14).
System vacuum causes outside air to enter the Purge Lines (16) and create
bubbles in the
cooling fluid. The Bubbles cool the cooling fluid, cause fluid mixing, and
maintains temperature
above ambient outside temperature. Maintaining temperatures above ambient
outside
temperature in the Vapor Conversion Tank (14) combined with cooling fluid
droplet size
prevent water condensation within the tank.
Treatment gas exit the Cooling Chase (11) and the Mist Chamber (13) and
encounter the
Vapor Conversion Tank Gibbs Energy Curtain (66). The Gibbs Energy Curtain (66)
consists
of Gibbs Energy Curtain Tabs (70) and Gibbs Energy Curtain Air Gaps (71). The
Tabs (70)
consist of materials with specific polar and dispersive Gibbs surface energy
profile to match
or closely match contaminants that facilitate condensation on to the tabs
(70). Treatment gas
flows through the device where the rapid cooling and physiochemical processes
cause the
tabs (70) to be coated with contaminant. The Gibbs Energy Curtain (66) is
removeable through
the Gibbs Energy Curtain Access (15). Figure 22 presents Gibbs Energy Curtain
Perspective
View.
Treatment gas flows through the Gibbs Energy Curtain (66), then downward under
the Vapor
Conversion Tank Vapor Diversion Baffle (67); as seen in Figure 21 The flow
path causes the
treatment gas to turn and flow close to the Fluid Level (68) in the tank,
which has a demisting
and cooling effect. In addition, any particulate matter drops out of the
treatment gas where it
accumulates on the tank bottom. A Sediment Baffle (104) located at the bottom
of the tank
prevents sediment from migrating into the Vapor Conversion Tank Cooling Fluid
Return Line
(61); seen in Figure 21. The treatment gas is drawn upwards into the Vapor
Conversion Tank
Demisting Tower (17) where a demister screen and the height of the tower
eliminates any
residual mists.
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The Vapor Conversion Tank (14) has various sampling, viewing and access ports
including
the Vapor Conversion Tank View Window (63) and Vapor Conversion Tank Access
Hatch (65)
as seen in Figure 16 and Vapor Conversion Tank Sample Port (64) as seen in
Figure 17. The
Vapor Conversion Tank Light Port (106) is located under the Mist Chamber (13)
to provide
lighting into the tank interior; as seen in Figure 15.
The vast majority of PFAS is removed from the treatment gas in the Vapor
Conversion Tank
(14). Amphiphilic PFAS compounds almost always have monomers that escape
primary
treatment mainly due to the weak Van Der Waals bonds. The Vapor Phase Galvanic
Separator
(22) is designed to remove residual monomer PFAS where a galvanic sequence
(galvanic or
impressed currents) of granulated metal that offer high surface area, high
energy interfaces of
varying charges for amphiphilic self-assembly. Voltage drops across the
galvanic cell indicate
active self-assembly and provide an indication of PFAS mass within the filter
media. The
galvanic filter media can be recharged by placing the filter assembly in the
Polarity Conversion
Unit (1). Figures 23 through 27 present perspective, cross sectional and map
views of the
assembly and various elements of the assembly. Figure 23 presents Vapor Phase
Galvanic
Separator Perspective View. The Vapor Phase Galvanic Separator (22) is the
same size as a
Soil Slip (50); it has a Vapor Phase Galvanic Separator Lid (72) that provides
a sealed
environment inside the vessel. The Vapor Phase Galvanic Separator Intake (73)
and Outlet
(74) are designed to expand the cross-sectional area of flow before and after
the Vapor Phase
Galvanic Separator Rechargeable Filter Media (77) as seen in Figure 24. The
entire assembly
can be moved with a forklift with the Forklift Pockets (54).
Figure 25 presents Vapor Phase Galvanic Separator Housing Map View without
Lid. Figure
shows the Vapor Phase Galvanic Separator Granular Metal Slot (75) and Granular
Desiccant Bridge Slot (76). Figure 26 also shows internal element through
cross sections.
25 Granular metal is used to provide high surface area and to allow easy
adjustment in metal
species or replenishment of the granular metal. Vertical granular metal beds
are placed across
the direction of treatment gas flow. Reducing the mass of the granulated
anodic metal slots
relative to the granular cathodic metal increase voltage across the galvanic
cell. Adjustable
granular metal mass allows adjustment in voltage across the galvanic cell. The
desiccant
media is also granular and acts as a bridge between the various granular metal
vertical beds.
When voltage readings indicate the Rechargeable Filter Media (77) is full, the
media is
removed from the Vapor Phase Galvanic Separator and placed in a Soil Slip
(50)/Soil Slip
Base Framework (44) for recharging in the Polarity Conversion Unit (1).
Figure 28 presents Brine Pot Evaporator Assembly Perspective View; Figures 29
and 30
present cross section and map views. The purpose of the Brine Pot Evaporator
(29) is to dry
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PFAS fluids and foams into a dry powder in isolated batch and to provide
system vacuum and
conveyance of vapor/foams/fluids from the Fluids Line Assembly. The Brine Pot
Evaporator
(29) connects the Fluids Line Assembly to the Vapor Line Assembly through the
Brine Pot
Evaporator Connection Valve (47), which connects to the Vapor Extraction
Manifold (7) as
shown in Figures 2, 3, and 4. System vacuum is used to contain, treat and
convey PFAS
saturated foams and fluids while providing a means for vapor phase treatment.
The Brine Pot
Vapor Extraction Line (28) draws PFAS vapors from the Brine Pot Evaporator
(29). Vapors
exit the Brine Pot Evaporator (29) through the Brine Pot Demister Tower (30),
which is
designed to remove any mists from the vapor stream before entry into the vapor
line assembly.
The Brine Pot Evaporator (29) is equipped with a Blower (31) and Heater (32)
that provide hot
air into the vessel to facilitate drying of PFAS fluids concentrate.
Figure 31 presents Brine Pot Evaporator Interior Elements Perspective View.
Figure 32
presents Brine Pot Evaporator Interior Elements Cross Section. Figures 31 and
32 show the
Brine Pot Purge Lines (82) where heated outside air is drawn through the
fluids by the applied
vacuum above the Brine Pot Evaporator Fluid Level (84). The Vapor Foam/Fluids
Extraction
Line/Valve (33) and the Amphiphilic Decontamination Wand Flexible Extraction
Line/Valve
(34) are closed during Brine drying operations in the Brine Pot Evaporator
(29).
The level of brine and foam inside the Brine Pot Evaporator (29) is monitored
through the
Brine Pot Fluid Level Window (79). In the event foam does not quickly decay
inside the Brine
Pot Evaporator (29), the Brine Pot Water Spray Foam Knock Down Assembly (80)
will direct
a blast of high-pressure water spray using the Brine Pot Water Spray Foam
Knock Down
Spray Nozzle (83) to knock down foam levels in the tank. Figures 31 and 32
also present the
Brine Pot Drain Valve (81) and the Fork Lift Pockets (54) to drain and move
the Brine Pot
Evaporator (29).
The Fluids Treatment Assembly line consists of two primary treatments in
series where the
initial treatment removes the majority of PFAS contaminants followed by a
polishing treatment
removing lower concentration monomeric PFAS as seen in Figures 2 and 3.
Figures 33, 34,
and 35 present the Surface Excess Concentrator Assembly in Perspective, Cross
Section and
Map View respectively. The Surface Excess Concentrator (37) concentrates short
and long
chain PFAS and associated mixtures as foam and surface excess layers. The
first Fluids
Pump (in series) (36) delivers PFAS contaminated fluids to the Surface Excess
Concentrator
(37) through the Surface Excess Concentrator Inlet (85). During active
treatment of fluids, the
Vapor/Foam/Fluids Extraction Line/Valve (33) is opened to provide system
vacuum and
vapor/foam/fluids conveyance from the Surface Excess Concentrator Assembly
(37) to the
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Brine Pot Evaporator (29). Treated Fluids exit through the Surface Excess
Concentrator Outlet
(86).
The raw PFAS contaminated fluids enter into the Surface Excess Concentrator
Fluids Process
Tank (88) where Surface Excess Concentrator Purge Lines (38) are vented to
outside air. The
vacuum applied the Surface Excess Concentrator Foam Tank (89) draws outside
air through
the Purge Lines (38), which are slotted at the bottom of the Process Tank
(88). The Outside
air creates bubbles in the raw fluids where foam is created at the surface,
which is the same
elevation as the inlet (85) and outlet (86). Long chain PFAS concentrate in
the foam allows
shorter chain PFAS to accumulate at the foam/fluid interface and PFAS micelles
just below
the fluid/foam interface. The fluid surface offers a high energy interface for
self-assembly.
PFAS mixtures create the foam framework lifting long chain compounds from the
fluid surface.
The Surface Excess Concentrator Foam Belt (87) removes the entire concentrated
surface
excess complex from the Process Tank (88) and delivers it to the Foam Tank
(89) where the
foam/fluid mixture is drawn into the Extraction Line (33) and subsequently
delivered to the
Brine Pot Evaporator (29). Treated fluids exit the Fluids Process Tank (88)
through the Surface
Excess Concentrator Fluids Exit Piping (bottom intake of Fluids Process Tank)
(90). The Fluids
Exit Piping Bottom Intake (92) is located the maximum distance below the
surface excess
formation occurring during treatment as seen in Figure 37 Surface Excess
Concentrator
Interior Elements Cross Section; Figure 36 offers a Perspective View.
The Foam Belt (87) uses a material that is designed to match or closely match
the polar and
dispersive energies associated with PFAS compounds and associated mixtures.
Perfect
wetting and adhesion occur when the fluids energy and solid surface energy
polar and
dispersive ratios match or closely match. The speed of the Foam Belt (87)
rotation also causes
the entire surface excess complex to be conveyed to the Foam Tank (89). The
Surface Excess
Concentrator Access Hatch (91) provides a means to change the Foam Belt (87)
and to
perform other maintenance tasks.
The second Fluids Treatment apparatus is intended to treat residual monomeric
PFAS that
passed through the Surface Excess Concentrator (37). The Aqueous Phase
Galvanic
Separator (39) is deployed, two in series, as seen in Figures 2 and 3. Figures
38, 39, and 40
present the Aqueous Phase Galvanic Separator (39) in Perspective, Cross
Section and Map
Views respectively. Figure 41 presents Aqueous Phase Galvanic Separator
Assemblies Cross
Section and Figure 42 presents Aqueous Phase Galvanic Separator Filter Media
Cross
Section. The Aqueous Phase Galvanic Separator is the same size as a Soil Slip
(50) where
fluids enter int o the Aqueous Phase Galvanic Separator Inlet (95) and exit
the Aqueous Phase
Galvanic Separator Outlet (97). The Aqueous Phase Galvanic Separator Lid (96)
secures the
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vessel providing a water tight seal and access to the Aqueous Phase Galvanic
Separator
Rechargeable Filter Media (100). The Galvanic Separator Rechargeable Filter
Media (100)
consists of alternating Aqueous Phase Galvanic Separator Granular Metal Slot
(98) and
Aqueous Phase Galvanic Separator Granular Molecular Sieve Bridge Slot (99).
The slot
design provides a flexible method to create a galvanic metal series of high
surface area for
amphiphilic PFAS self-assembly. Doubling the cathodic metal mass (more slots
filled with
cathodic granular metal) increases voltage across the galvanic cell. The
Second Fluids Pump
(in series) (40) as shown in Figures 2 and 3 provide vacuum pressure on the
fluids treatment
line to overcome the applied vapor vacuum in the Surface Excess Concentrator
(37). Fork
Pockets (54) allow easy transport of the unit.
Figure 43 presents Amphiphilic Decontamination Wand Perspective View. The
Amphiphilic
Decontamination Wand (35) is used to decontaminate hard surfaces such as
concrete airport
taxiways or dump truck beds. The Wand (35) can be made to any size ranging
from a walk
behind unit to a unit mounted on a vehicle. The Amphiphilic Decontamination
Wand (35)
assembly is connected to the Brine Pot Evaporator (29) through the Amphiphilic
Decontamination Wand Flexible Extraction Line/Valve (34) where system vacuum
provides
vapor conveyance for emissions treatment as shown in Figures 2, 3, 28, 30, and
31. The Wand
(35) is equipped with a Amphiphilic Wand Hard Pipe Vapor Extraction Handle
(101) to facilitate
easy movement of the device. The Amphiphilic Wand Heater/Blower Assembly (102)
provides
modulated heat and treatment gas velocity to a given treatment area. Hot air
is directed to the
area targeted for treatment within the Amphiphilic Wand Shroud (103) where
treatment gases
are promptly removed by the applied system vacuum. Treatment gas temperature
and velocity
are used to thermally disorganize surface polarity to release amphiphilic PFAS
and associated
mixtures and films. Treatment gas vapors are drawn into the Brine Pot
Evaporator (29) and
subsequently through the vapor treatment line assemble.
Figure 44 presents Implement and Object Decontamination Base Framework in
Perspective
(45). Objects are simply placed on the Soil Slip Base Framework (44),
transported with a
forklift and placed in the Polarity Conversion Unit (1) for treatment.
Treatment gas temperature
and velocity are used to convert the surface polarity of the objects releasing
amphiphilic PFAS
mixtures and films.
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