NZ759710A - Solid waste treatment system and method - Google Patents
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Abstract
There are limited remediation options presently available for treatment of PFAS contaminated solid waste, other than landfill and encapsulation which are environmentally undesirable. Accordingly, an improved waste treatment system for separating contaminants including per-fluoroalkyl and poly-fluoroalkyl substances (PFAS) from bulk solid waste (12) is therefore proposed that does not require the contaminated soil to be discarded. The system includes a preparation module (9) having a bulk material separator separates oversize material (14) from bulk solid waste (12). A physical separation module (13), located down-stream of the preparation module (9), separates the bulk solid waste (12) based on particle size using physical and/or hydrodynamic and/or density separation techniques. An extraction/chemical separation module (19), located downstream of the physical separation module (13), adds leachate and/or extractant to separate the contaminants from a slurry output from the physical separation module (13), into a fines output and a contaminated water solution. A water circulation system (21) supplies water to the physical separation module (13) and the extraction/chemical separation module (19), the water circulation system including at least one water treatment process, the treated water being recycled and recirculated within the waste treatment system.
Description
Solid waste treatment system and method
Technical Field
The present disclosure relates to a solid waste treatment system and method. The
present invention relates to a system and method for removing per-fluoroalkyl and poly-
fluoroalkyl substances (PFAS) from contaminated solid waste such as soil, sediment,
concrete or other contaminated solid waste. However, it will be appreciated by those skilled
in the art that the present invention may be used to remove other contaminants from solid
waste.
Background of the Invention
Per-fluoroalkyl and poly-fluoroalkyl substances (PFAS) are a diverse group of
manufactured compounds which are not naturally occurring in the environment. PFAS are a
group of fluorinated organic compounds that were invented in 1938 and used heavily within
several industries from 1950 to about 2000 when phase out of several PFAS compounds
began due to health concerns. Perfluorooctane sulfonate (PFOS) and perfluorooctanoic acid
(PFOA) are two of the most well-known PFAS.
PFAS are resistant to heat, water, and oil. PFAS have been used in industrial
applications and consumer products such as carpeting, apparel, upholstery, food paper
wrappings and fire-fighting foams (aqueous film-foaming foams) and hydraulic fluid in
aircraft.
In Australia there are several instances in which fire-fighting facilities and fire-
fighting training grounds at airports have been found to be contaminated by PFAS. Solid
waste contaminated with PFAS may result in contamination of ground water and related
water courses.
Unfortunately PFAS are resistant to environmental degradation, meaning that
without suitable treatment, they can persist in contaminated solid waste for extended
periods of time. Studies indicate that continued exposure to sources of PFAS may result in
bioaccumulation of PFAS in living organisms, meaning their concentration increases over
time in the blood and organs. Exposure to certain PFAS have been linked to various adverse
health effects.
Due to the chemical properties of PFAS (low volatility and resistance to
biodegradation, photolysis and hydrolysis), there are limited remediation options currently
available for treatment of PFAS contaminated solid waste (soil, sediment, spent media,
concrete and all other PFAS impacted media). Available options include landfill disposal,
encapsulation in purpose built lined repositories and thermal desorption.
Various methods have been considered and studied for removing contaminants
including PFAS from solid waste. For example, physical barriers have been considered which
physically prevent ground water movement out of a contaminated area. Whilst such
approaches may have application in the containment of contaminants, they ultimately do not
achieve local decontamination of the solid waste.
Removal and disposal of contaminated solid waste may be possible in small scale
contamination sites, but this approach is expensive and the feasibility of the option is
controlled by state or federal regulators who may remove such options.
Some thermal processes, such as high temperature plasma arcs, have been found
to be successful in destroying PFAS. Alternatively, thermal desorption can be used to desorb
contaminants by evaporation. The contaminants can then be condensed and collected or
destroyed in a thermal oxidiser. Whilst thermal processes may be applied to remove PFAS
from solid waste, in practice these processes can be energy intensive, result in the
production of highly corrosive by-products and are expensive.
Object of the Invention
It is an object of the present invention to substantially overcome or at least
ameliorate one or more of the above disadvantages, or to provide a useful alternative.
Summary of the Invention
In a first aspect, the present invention provides a per-fluoroalkyl and poly-
fluoroalkyl substances (PFAS) waste removal system from bulk solid waste, the system
comprising:
a preparation module having a bulk material separator to separate oversize material
from the bulk solid waste;
a physical separation module, located down-stream of the preparation module, to
separate the bulk solid waste based on particle size using physical and/or hydrodynamic
and/or density separation techniques;
an extraction/chemical separation module, located downstream of the physical
separation module, to add leachate and/or extractant to separate the contaminants from a
slurry output from the physical separation module, into a fines output and a contaminated
water solution; and
a water circulation system supplying water to the preparation module and the
physical separation module and the extraction/chemical separation module, the water
circulation system including at least one water treatment process, the treated water being
recycled and recirculated within the waste treatment system.
Process water added to the physical separation module is preferably heated above
an ambient temperature and/or chemically amended.
Preferably wash-water and/or chemicals used in the extraction/chemical separation
module are heated above an ambient temperature.
Preferably wash-water and/or chemicals used in the extraction/chemical separation
module are modified by the addition of chemicals including surfactants, biosurfactants
and/or solvents and/or poly-valent cations.
Wash-water and/or chemicals used in the extraction/chemical separation module
are preferably pH modified. The pH is preferably in the range of 8-9.
Reverse osmosis is preferably used to generate de-ionised water for reuse as wash-
water in the extraction/chemical separation module and/or the water circulation system.
The physical separation module preferably includes:
a first linear screen deck configured to separate input slurry into output slurry and
organic material having a size generally larger than about 1mm; and
a hindered settling classifier and a sieve bend located down-stream of the first
linear screen deck and configured to separate organic material having a size of about
0.15mm to 1mm from the slurry.
The physical separation module further preferably includes a DAF or flotation cell to
remove organic material smaller than 0.15mm.
The physical separation module preferably includes a wet trommel screen down-
stream of and in communication with the preparation module, the wet trommel screen
having an oversize output, generally larger than about 50mm, and a gravel slurry output.
The gravel slurry output is preferably directed into a coarse material washer, the
coarse material washer having:
a slurry containing fine sand, silt, clay output;
an organic material output which is directed to the first linear screen deck; and
a gravel, sand, silt and clay slurry output which is directed to a second linear screen
deck.
The second linear screen deck preferably separates the gravel, sand, silt and clay
slurry output into a gravel output and a slurry output, the slurry output being in fluid
communication with an attrition scrubber.
The attrition scrubber preferably agitates an input liquid to disseminate solid waste
particles, a downstream side of the attrition scrubber being in fluid communication with a
cyclonic separator.
The cyclonic separator preferably has a cyclonic slurry output having a particle size
of less than about 0.15mm and a sandy slurry output which is in fluid communication with
the hindered settling classifier.
The hindered settling classifier preferably has a sandy slurry output which is
directed to a third linear screen deck.
The third linear screen deck preferably has a sand output being larger than about
0.15mm in size and a water output, the water output being in fluid communication with a
location upstream of the attrition scrubber.
The cyclonic slurry output preferably has a particle size of less than about 0.15mm
is in fluid communication with a polymer dispenser and an input port of a thickener.
The thickener preferably has a water output in fluid communication with a clarified
water tank and a slurry outlet in fluid communication with a dewatering press, the clarified
water tank being in fluid communication with a water treatment plant.
The dewatering press preferably has a press water outlet and a dewatered cake
fines outlet, the press water outlet being in fluid communication with a filtrate water tank,
the filtrate water tank being in fluid communication with the head of the thickener.
The waste treatment system further preferably comprises:
at least one primary filter;
at least one secondary filter; and
a filtered water tank located in between the primary and secondary filters.
The waste treatment system further preferably comprises a treated water tank
located down-stream of the secondary filter, the treated water tank being in fluid
communication with a recycled water supply line for supplying water to the waste treatment
system.
The treated water tank is preferably in fluid communication with a back wash pump,
the back wash pump being in fluid communication with downstream sides of the secondary
filter and the primary filter
Brief Description of the Drawings
A preferred embodiment of the invention will now be described by way of specific
example with reference to the accompanying drawings, in which:
Fig. 1 is a process flow diagram depicting a solid waste treatment system and
process according to the present invention;
Fig. 2 is a schematic diagram depicting physical separation modules of the solid
waste treatment system and process of Fig. 1; and
Fig. 3 is a schematic diagram depicting physical separation modules and extraction/
chemical separation modules and a wastewater treatment circuit of the solid waste
treatment system and process of Fig. 1.
Detailed Description of the Preferred Embodiments
There is disclosed herein a solid waste treatment system and process (Fig. 1, 2 and
3). The waste treatment system and process provides a washing process that treats and
separates per- and poly-fluoroalkyl substances (PFAS) contaminated bulk solid waste 12.
Bulk solid waste including but not limited to, sediment, concrete or other solid waste
material,
The waste treatment system and process is a physical and chemical treatment train
that incorporates size, density and chemical separation processes which will be discussed in
detail below.
Referring to Fig. 1, a process flow diagram is provided which identifies the overall
stages of the waste treatment system. The initial stage is solid waste 12 excavation followed
by solid waste 12 preparation to remove oversize material.
Physical separation modules
The subsequent stage includes physical separation modules 13, which may use a
variety of different equipment, as follows:
? Size Separation Modules – particle size separations are conducted on the bulk
contaminated solid waste 12 using physical or hydrodynamic separation techniques.
Examples of equipment utilised includes multi deck screens, hydro-cyclones and rising
current classifiers.
? Density Separation Modules – particles with different densities respond differently to
gravity and to one or more other forces applied simultaneously in opposition to gravity.
Although density difference is the main criterion for gravity separation, particle size
and shape also influence the separation. Utilising these techniques, contaminants with
a density difference from the bulk solid waste 12 can be effectively separated and
concentrated. Examples of equipment used in density separation include spirals and
shaking tables.
? Dewatering Modules – the dewatering modules are used to separate the wash water
from the treated solid waste 12 and contaminated sludge. These modules allow the
wash water to be recycled and utilised in a continuous closed loop process. Examples
of dewatering equipment include filter presses and linear motion screens.
? Within the physical separation modules, the process water can be heated or amended
with chemicals to enhance the separation of the PFAS components from the solid
waste 12.
It will be appreciated by those skilled in the art that the physical separation module may
deploy alternative equipment than the equipment described above.
Extraction / Chemical Separation modules
After processing through the physical separation modules 13, the remaining solid
waste 12 is processed with extraction / chemical separation modules 19, which are as
follows:
The leaching or extraction / chemical separation modules 19 differ from solid waste
washing, physical separation modules 13, in that they employ a leachate or extractant to
separate the contaminants from the bulk solid waste matrix 12. Like the physical separation
modules 13, the extraction / chemical separation modules 19 provide a separation process
that utilises an amended wash water to extract contaminants from the bulk solid waste 12.
Amendments within wash water may include acids, bases, surfactants,
biosurfactants, solvents or specific solutions (for example those containing poly-valent
cations) that are added to the water stream within the process to enhance the desorption of
PFAS from solid waste into the wash water. The surfactants may be biological surfactants or
cationic surfactants or anionic surfactants.
The wash water may also be corrected to an optimal pH range (typically 8-9 but
dependent on soil characteristics) with an acid or base and may also be heated. Both pH
correction and heating enhance PFAS desorption from solids.
However, it differs from solid waste washing in that the time within the extraction
system is in the order of magnitude of hours (or greater) as opposed to minutes allowing for
greater contact times and extraction efficiencies.
The technique operates on the principal that the contaminants will have a greater
solubility in the wash water solution than in the solid waste or mineral matter matrix. The
equilibrium concentration gradient drives the mass transport process such that the
contaminant transfers from the solid waste to the wash water. When the solid waste is
separated from the amended wash water, the contaminant concentrations present in the
solid waste or mineral matrix are reduced relative to the concentrations prior to the
extraction process.
Water Treatment modules
The waste treatment system (Figs. 1, 2 and 3) includes a wastewater treatment
module 21 that is used to treat the contaminant affected process water and extraction
solution and recycle the treated water in a closed loop process for the solid waste 12
washing circuit. The water treatment module 21 is designed specific to the contaminant
being treated, but typically incorporates precipitation and filter polishing elements. The water
treatment module 21 may also include equipment to generate deionised water which is
effective at extracting PFAS from solids.
In the preferred embodiment, the different fractions in the solid waste 12 that are
separated are as follows:
o Ferrous scrap metal this comprises tramp ferrous metal objects that may
be present in the bulk solid waste;
o Oversize material comprising mainly rocks > 50mm in the bulk solid
waste
o Gravel material comprising mainly stones with a fraction < 50mm
and >5mm;
o Sand material comprising mainly sand with a fraction < 5mm and
> 0.15mm;
o Fines material comprising mainly silt and clays with a fraction
< 0.15mm;
o Organics (1mm) material comprising mainly organic vegetation material such
as sticks, grass leaves etc. with a fraction > 1mm; and
o Organics (0.15m) material comprising mainly organic vegetation material such
as sticks, grass leaves etc. with a fraction < 1mm and >
0.15mm. However, it will be appreciated that finer grained
organics with a fraction less than 0.15mm may also be removed
by flotation or other suitable processes.
The waste treatment system (Figs. 1, 2 and 3) operates on the principal that
contaminants are associated with certain size fractions of a bulk solid waste 12 matrix and
that these contaminants can be desorbed from solid waste, dissolved or suspended in an
aqueous solution, removed by separating out clay and silt particles from the bulk solid waste
12 matrix, separated through physical differences between the contaminant and the solid
waste 12 particles and/or destroyed using chemical amendments such as oxidants separated
through the removal of specific components of the solid waste matrix 12 that the PFAS has
preferentially partitioned. In some embodiments, additives may also be added to the wash
water to enhance the separation between the contaminant and bulk solid waste 12. The pH
of waste water may also be amended to an optimal value and/or the waste water may be
heated.
As shown in Fig. 1, the first stage of the process involves solid waste 12
preparation. The process is designed to treat material up to about 1,200 mm in size.
Per the preferred embodiment described below, the bulk solid waste 12 is
transported to a starting point of the system (Figs. 1, 2 and 3). Referring to Figs. 1 and 2,
this may be conducted at the contamination site or alternatively at a remote location, and
requires the excavated, contaminated bulk solid waste 12 to be physically delivered to the
starting point of the system (Figs. 1, 2 and 3).
This may be done using various types of earth moving and/or transportation
equipment. In a preferred embodiment, contaminated bulk solid waste 12 is fed via a front
end loader 23 into a feeder bin 14. However, it will be appreciated that other materials
handing machinery may be deployed such as conveyor belts.
The feeder bin 14 is equipped with a grizzly screen, typically in the form of a static
or vibrating screen. The grizzly screen separates large, coarse material from the bulk solid
waste 12. Oversize material such as large boulders, are directed into a bunker and removed
with the front end loader 23.
The grizzly screen is preferably defined by angled bars which slope downwardly
toward the feed side. In a preferred embodiment, the bars are spaced at about 100mm from
adjacent bars. The grizzly screen preferably includes hungry boards or other such barriers to
reduce lateral spillage. The grizzly screen is preferably hinged so that it can be flipped open
for cleaning.
The feeder bin 14 is equipped with a feeder belt 17 that controls the feed rate of
the bulk solid waste 12 into the waste treatment system. The feeder bin 14 also preferably
includes a bin vibrator to manage and reduce material bridging. The drive unit for the feeder
belt 17 is equipped with a variable frequency drive that is integrated with the control system
allowing adjustment of the feed rate from a control panel, depending on bulk solid waste 12
input rates.
The feeder bin 14 is preferably lined with high density polyethylene (HDPE) to limit
the amount of material bridging, and reduce blockages and obstructions.
A magnet 18, located above the feeder belt 17, removes ferrous tramp metal
objects from the bulk solid waste 12 during transit along the feeder belt 17. Any collected
ferrous metal objects are removed from the magnet 18 and deposited into a skip bin for
recycling.
Rock and debris greater in size than this maximum limit are deemed oversize
material 14 which is separated from the bulk solid waste 12 using the grizzly screen and/or
other dry screening techniques. If required, the oversize material 14 is subsequently treated
using a hand held high pressure water spray device to clean the surface of the oversize
material 14.
On completion of the solid waste 12 preparation stage, once the oversize material
14 has been removed, the remaining bulk solid waste 12 is mixed with wash water and
enters several different stages of the waste treatment system as described in detail below.
Referring to Fig. 2, after the initial solid waste 12 preparation and removal of
oversize material 14, the bulk solid waste 12 is delivered by the feeder belt 17 to a rotating
trommel 20, such as a wet trommel screen 20. However, it will be appreciated by those
skilled in the art that other size dependent material screening devices can be utilised in place
of the rotating trommel 20.
High pressure water is injected into the trommel screen 20. The purpose of the wet
trommel screen 20 is to agitate the material under high pressure water jets to break up the
solid waste 12 into its constituent components and then sieve out the oversize fraction 30.
The clean oversize fraction 30, which is typically larger than 50mm, is ejected from the back
end of the trommel screen 20 into a bunker or other storage facility. The clean oversize
fraction 30 is unlikely to be contaminated, and does not require any further processing.
The wet trommel screen 20 also separates the solid waste 12 into a gravel slurry
output 40, which is generally under 50mm.
The gravel slurry output 40 from the wet trommel screen 20 is delivered to a coarse
material washer 50. The coarse material washer 50 provides a cleaning and scrubbing
process which typically removes soluble clays and dust. In a preferred embodiment, a single
or double Archimedean screw coarse material washer 50 is utilised. The Archimedean screw
transfers the gravel and a portion of the sand and fines fractions up an incline in the coarse
material washer 50. Fine sands, silts, clay and any organic fraction overtops a weir located at
one end of the coarse material washer 50, and is transferred to a first liner screen deck 80.
The coarse material washer 50 has two outputs 60, 70. A first output 60 is in the
form of a slurry including the organic fraction. A second output 70 is in the form of gravel
and a portion of the sand and silt/clay. The gravel typically has a size of about 5mm or
above.
The organic material and slurry output 60 is fed into a first linear screen deck 80,
such as a vibrating screen. The linear screen deck 80 separates the input slurry 60 into
organic material 90, typically having a size larger than 1mm, and slurry 85. The organic
material 90 may be removed from the system at this point. The liquor with the organic
material 90 (1mm) from the first linear screen deck 80 is washed with high pressure water
jets and is transferred into a skip bin or similar. The remaining undersize 85 and liquor is
transferred to an attrition scrubber 130 as discussed below.
The gravel sand and silt/clay output 70 from the coarse material washer 50 is
directed into a second linear screen deck 100, such as a vibrating screen. The second linear
screen deck 100 separates the gravel 70 into two outputs in the form of gravel 110, having a
size of about 5mm or larger. The second output from the second linear screen deck 100 is in
the form of a slurry 120. The liquor with the gravel/sand/fines fractions 110 from the second
linear screen deck 100 is washed with high pressure water jets and the gravel is screened
out and is transferred into a bunker. The remaining slurry containing undersize sand/fines
fraction 120 and liquor is transferred to the attrition scrubber 130.
The slurry output 85 of the first linear screen deck 80 and the slurry output 120 of
the second linear screen deck 100 converge before being fed into the attrition scrubber 130.
The attrition scrubber 130 provides a high-shear mixing environment to separate clays and
transfer to the aqueous phase other soluble impurities. In the preferred embodiment, the
attrition scrubber 130 is a vessel, such as an induced flotation cell, that agitates the
combined liquor streams to further disseminate the solid waste 12 particles. In one
embodiment, the attrition scrubber 130 may be used as a flotation cell to also remove iron
oxides.
The output from the attrition scrubber 130 is directed into a separator pump 140.
The output of the separator pump 140 is directed to a separator such as a cyclonic
separator 150. The cyclonic separator 150 is calibrated such that it separates the sand
fraction 170 from the fines. The sand liquor fraction 170 is pumped to a hindered settling
classifier 180 whilst the fines slurry fraction 160, which is likely to contain contaminants, is
pumped to a thickener 300. The fines slurry 160 generally has a particle size of 0.15mm and
smaller. The cyclonic separator 150 has an output typically in the range of 0.15mm to
0.04mm.
A further organics removal step is undertaken on the sand fraction within the
hindered settling classifier 180. The hindered settling classifier 180 operates with teeter
water added to create a density bed capable of further separation of organics. The rising
teeter water and solids 200 with a settling rate lower than the teeter water are carried out of
the top of the hindered settling classifier 180. The organics 200 and liquor are transferred to
a sieve bend 210.
The liquor with the organics (larger than about 0.15mm) 200 on the sieve bend 210
is screened by the sieve bend 210 with the organic fraction 220 transferred into a skip bin.
The undersize 222 and liquor is transferred back to a location upstream of the attrition
scrubber 130 as a recycle stream, being mostly water.
After settling into the dewatering cone of the hindered settling classifier 180, the
sand fraction slurry 190 is removed via the bottom vessel outlet. The sand fraction slurry 190
and liquor, being approximately 50% water and 50% solid, are transferred to a third linear
screen deck 230.
The sand fraction slurry 190 from the hindered settling classifier 180 is directed to a
third linear screen deck 230. The liquor with the sand fraction slurry 190 from the third linear
screen deck 230 is washed with high pressure water jets and the sand 240 is screened out
and is transferred into a bunker. The remaining undersize fraction 250 and liquor are
transferred back to the attrition scrubber 130 as a recycle stream.
A water source 270, such as recycled water, is supplied to the system. The water
270 is provided to various treatment sites within the system, including the wet trommel
screen 20, the first, second and third linear screen decks 80, 100, 230, and the hindered
settling classifier 180.
Referring to Fig. 3, the fines slurry 160 from the cyclonic separator 150 enters a
thickener 300 which is used to clarify the water and thicken the fines 160. Fines slurry 160
flows through a de-aeration vessel before entering the launder to the thickener 300 well.
The thickener 300 may be equipped with a mechanical sludge rake, moving sludge along a
sloped bottom to a central sludge outlet 305.
Preferably a drive motor of the thickener 300 is located at the centre, stilling well
and is accessible via a walkway. Motor speed for the thickener 300 may be controlled via a
variable frequency drive with torque limiting functionality.
Polymer 310, (for example polydiallyldimethyl ammonium chloride (polyDADMAC) or
non-ionic polyacrylamide based polymers) may be added to the inlet launder of the thickener
300 to assist in clarification and fines thickening in a sludge blanket.
The polymer 310 is normally injected into the launder leading up to the stilling well
of the thickener 300. The polymer 310 dosing rate is preferably controlled via an automatic
sampler. Automatic feedback from the auto sampler to adjust chemical pump speed is
required to control polymer 310 dosing rates.
The clarified water from the thickener 300 overflows the effluent launder and is
transferred into a clarified water tank 330.
The thickened fines slurry is delivered to a slurry tank 307 from the thickener 300
before being pumped into a plate and frame press or similar e.g. vacuum filter press, belt
press, centrifuge etc. An extraction additive (for example an acid or base) 311 may be added
to the slurry tank.
The slurry dewaters against the filter cloth in the press 320 and water is expelled
into a sump 308. This filtrate water is pumped with pump 309 to a filtrate water tank 340
from where it is recycled to a location upstream of the thickener 300.
Once the dewatering cycle of the plate and frame press 320 is complete, the press
320 is opened and the dewatered fines cake is discharged into a skip bin. The dewatered
fines cake typically retains higher residual levels of PFAS than the coarse fractions however
the removal efficiency is dependent on the specifics of the feed material being treated.
Water from the clarified water tank 330 undergoes water treatment. It will be
appreciated by those skilled in the art that the water treatment system described herein may
be replaced with alternative water treatment systems. Water is pumped to one or more
primary filters in the form of multi-media filters 350 to remove residual suspended solids.
The filtered water from the multi-media filters 350 is discharged into a filtered water
tank 360. After filtration, the water is pumped through at least one secondary filter in the
form of a granular activated carbon (GAC) filter 370 (or other selected media filter) to
remove the dissolved PFAS or other organic contaminants.
On the outlet side of the GAC filters 370, water is stored in a treated water tank
375. From the treated water tank 375, the treated water 270 is pumped back to the system
as a recycle stream as described earlier. Reverse osmosis or similar may be used to generate
de-ionised water for reuse as process water within the system, due to deionised water’s
effectiveness at extracting PFAS from solids.
The filtration system is set up so that both GAC filters 370 and/or multi-media filters
350 can be backwashed. Backwash water is pumped with a dedicated pump to the filtrate
water tank 340, through lines 390, 395 for reprocessing at the head of the thickener 300.
Additional water may be input into the system through the line 385.
During processing of the bulk solid waste 12, contaminants may be separated from
the bulk solid waste 12 in the following different forms:
1. Water-soluble contaminants are transferred to the wash water;
2. Insoluble contaminants are suspended as particulate in the wash water;
3. Clay and silt particles to which contaminants are adhered are separated from
the larger solid particles;
4. Contaminants are separated and concentrated and/or destroyed from the
bulk matrix based on physical or chemical differences; and
. Water soluble contaminants are adsorbed on granular activated carbon that
is disposed of.
6. Separated through the removal of specific components of the solid waste
matrix 12 that the PFAS has preferentially partitioned.
The water-soluble contaminants transferred to the wash water and contaminant
suspended as particulate in the wash water are sent to the wastewater treatment circuit
where these contaminants are removed from the water as “residuals” and dewatered. The
treated water is typically recycled back to the solid waste 12 washing system for further
treatment of solid wastes.
After the larger solid waste particles are washed and removed, the fines (clay and
silt particles) are typically sent for additional treatment, and eventually to the dewatering
modules where the free water is removed and reused. The treated solid waste is stockpiled
and analysed to confirm that the post-treatment environmental solid waste quality objectives
have been met. The concentrated contaminants and the dewatered residuals from the
wastewater treatment circuit are prepared either for off-site disposal or recycling / reuse at
an appropriately licensed facility.
The actual configuration of the solid waste washing process will be determined
based on the treatability testing.
The waste treatment system separates the input bulk solid waste 12 into oversize,
gravel, sand, fines and two organic fractions (>1mm and 0.15-1mm);
Advantageously, the waste treatment system enables the desorption of PFAS
from solid waste to water and the adsorption of PFAS onto an adsorbent media in the water
circuit.
Figs. 2 and 3 conceptually depict the hydraulic gradient through the waste
treatment system. Material is expected to cascade via conveyor belts or gravity from the feeder
bin 14 to the attrition scrubber 130. Beyond the attrition scrubber 130, the circuit is pressurised
with pumps allowing the organics (0.15mm) and sand circuits to be raised and flow under
gravity.
It is envisaged that variations may be made to the waste treatment system as
follows:
? A magnet 131 may be installed near the input to the attrition scrubber 130 to
separate ferrous material;
? The screening size of materials;
? The ratio of wash water to solid waste 12;
? The size of solid waste 12 particles that will enter the water treatment
process;
? Chemicals, temperature, retention time;
? The polymer used to remove solids from the liquid stream;
? Polymers or other electrochemical processes could also be used to remove
PFAS contamination directly from the liquid stream;
? The water treatment process depicted is generic and many other water
treatment processes could potentially be substituted, achieving the same or
better outcomes (including technologies such as foam fractionation, which
removes PFAS from water as a foam stream);
? Numerous other adsorbents (powdered activated carbon, modified clay,
polymers, ion exchange resins) or alternative water treatment technologies
(reverse osmosis, nano-filtration) may be used to remove PFAS from the
liquid stream; and
? The fines thickening and dewatering process is also generic. Alternative
dewatering devices such as belt filter presses and/or vacuum filters are
possible.
Advantageously, the system enables the treatment of multiple contaminant types
within one treatment system.
Advantageously, the process includes a three-step process for removal of organic
material (i.e. removal within a linear screen deck and the hindered settling classifier and DAF
or flotation cell).
Although the invention has been described regarding specific examples, it will be
appreciated by those skilled in the art that the invention may be embodied in many other
forms.
Claims (22)
1. A per-fluoroalkyl and poly-fluoroalkyl substances (PFAS) waste removal system from bulk solid waste, the system comprising: a preparation module having a bulk material separator to separate oversize material from the bulk solid waste; a physical separation module, located down-stream of the preparation module, to separate the bulk solid waste based on particle size using physical and/or hydrodynamic and/or density separation techniques; an extraction/chemical separation module, located downstream of the physical separation module, to add leachate and/or extractant to separate the contaminants from a slurry output from the physical separation module, into a fines output and a contaminated water solution; and a water circulation system supplying water to the preparation module and the physical separation module and the extraction/chemical separation module, the water circulation system including at least one water treatment process, the treated water being recycled and recirculated within the waste treatment system.
2. The waste removal system of claim 1, wherein process water added to the physical separation module is heated above an ambient temperature and/or chemically amended.
3. The waste removal system of claim 1 or 2, wherein wash-water and/or chemicals used in the extraction/chemical separation module is heated above an ambient temperature.
4. The waste removal system of any one of claims 1 to 3, wherein wash-water and/or chemicals used in the extraction/chemical separation module is modified by the addition of chemicals including surfactants, biosurfactants and/or solvents and/or poly-valent cations.
5. The waste removal system of either of claims 3 or 4, wherein wash-water and/or chemicals used in the extraction/chemical separation module is pH modified.
6. The waste removal system of claim 5, wherein the pH is in the range of 8-9.
7. The waste removal system of any one of the preceding claims, wherein reverse osmosis is used to generate de-ionised water for reuse as wash-water in the extraction/chemical separation module and/or the water circulation system.
8. The waste removal system of any one of claims 1 to 7, wherein the physical separation module includes: a first linear screen deck configured to separate input slurry into output slurry and organic material having a size generally larger than about 1mm; and a hindered settling classifier and a sieve bend located down-stream of the first linear screen deck and configured to separate organic material having a size of about 0.15mm to 1mm from the slurry.
9. The waste removal system of claim 8, further including a DAF or flotation cell to remove organic material smaller than 0.15mm.
10. The waste treatment system of claim 8 or 9, wherein the physical separation module includes a wet trommel screen down-stream of and in communication with the preparation module, the wet trommel screen having an oversize output, generally larger than about 50mm, and a gravel slurry output.
11. The waste treatment system of claim 10, wherein the gravel slurry output is directed into a coarse material washer, the coarse material washer having: a slurry containing fine sand, silt, clay output; an organic material output which is directed to the first linear screen deck; and a gravel, sand, silt and clay slurry output which is directed to a second linear screen deck.
12. The waste treatment system of claim 11, wherein the second linear screen deck separates the gravel, sand, silt and clay slurry output into a gravel output and a slurry output, the slurry output being in fluid communication with an attrition scrubber.
13. The waste treatment system of claim 12, wherein the attrition scrubber agitates an input liquid to disseminate solid waste particles, a downstream side of the attrition scrubber being in fluid communication with a cyclonic separator.
14. The waste treatment system of claim 13, wherein the cyclonic separator has a cyclonic slurry output having a particle size of less than about 0.15mm and a sandy slurry output which is in fluid communication with the hindered settling classifier.
15. The waste treatment system of claim 14, wherein the hindered settling classifier has a sandy slurry output which is directed to a third linear screen deck.
16. The waste treatment system of claim 15, wherein the third linear screen deck has a sand output being larger than about 0.15mm in size and a water output, the water output being in fluid communication with a location upstream of the attrition scrubber.
17. The waste treatment system of any one of claims 13 to 16, wherein the cyclonic slurry output having a particle size of less than about 0.15mm is in fluid communication with a polymer dispenser and an input port of a thickener.
18. The waste treatment system of claim 17, wherein the thickener has a water output in fluid communication with a clarified water tank and a slurry outlet in fluid communication with a dewatering press, the clarified water tank being in fluid communication with a water treatment plant.
19. The waste treatment system of claim 18, wherein the dewatering press has a press water outlet and a dewatered cake fines outlet, the press water outlet being in fluid communication with a filtrate water tank, the filtrate water tank being in fluid communication with the head of the thickener.
20. The waste treatment system of claim 18 or 19, further comprising: at least one primary filter; at least one secondary filter; and a filtered water tank located in between the primary and secondary filters.
21. The waste treatment system of claim 20, further comprising a treated water tank located down-stream of the secondary filter, the treated water tank being in fluid communication with a recycled water supply line for supplying water to the waste treatment system.
22. The waste treatment system of claim 21, wherein the treated water tank is in fluid communication with a back wash pump, the back wash pump being in fluid communication with downstream sides of the secondary filter and the primary filter. Excavated Contaminated Recycled Water Solid Waste Makeup Additives Water and Additives Treated Water for Water Physical Treatment Solid Waste Wastewater Separation Preparation Treatment Modules Additives Contaminated Extraction Precipitates to Solution Key Dewatering Extraction Solid Modules Clean Fines to Dewatering Liquid Slurry Clean Solid Waste Concentrated Contamination to Disposal/Recycling Clean Oversize
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2017902433A AU2017902433A0 (en) | 2017-06-23 | Solid waste treatment system and method | |
AU2017902433 | 2017-06-23 | ||
NZ75970918 | 2018-06-22 |
Publications (2)
Publication Number | Publication Date |
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NZ759710A true NZ759710A (en) | 2020-10-30 |
NZ759710B2 NZ759710B2 (en) | 2021-02-02 |
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