U.S. patent application number 14/719295 was filed with the patent office on 2016-08-11 for methods and systems for producing treated brines.
This patent application is currently assigned to Gradiant Corporation. The applicant listed for this patent is Gradiant Corporation. Invention is credited to Prakash Narayan Govindan, Steven Lam, Maximus G. St. John.
Application Number | 20160228795 14/719295 |
Document ID | / |
Family ID | 56565193 |
Filed Date | 2016-08-11 |
United States Patent
Application |
20160228795 |
Kind Code |
A1 |
St. John; Maximus G. ; et
al. |
August 11, 2016 |
METHODS AND SYSTEMS FOR PRODUCING TREATED BRINES
Abstract
Water treatment systems and associated methods are generally
described. Certain embodiments of the water treatment systems and
methods described herein may be used to treat water comprising one
or more contaminants (e.g., oil, grease, suspended solids,
scale-forming ions, volatile organic material) to remove at least a
portion of the one or more contaminants. In some embodiments, at
least a portion of the treated water may be used directly in
certain applications (e.g., oil and/or gas extraction processes).
In some embodiments, at least a portion of the treated water may
undergo desalination to produce substantially pure water and/or
concentrated brine.
Inventors: |
St. John; Maximus G.;
(Boston, MA) ; Lam; Steven; (Medford, MA) ;
Govindan; Prakash Narayan; (Melrose, MA) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Gradiant Corporation |
Woburn |
MA |
US |
|
|
Assignee: |
Gradiant Corporation
Woburn
MA
|
Family ID: |
56565193 |
Appl. No.: |
14/719295 |
Filed: |
May 21, 2015 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
62115120 |
Feb 11, 2015 |
|
|
|
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
C02F 1/5236 20130101;
C02F 1/56 20130101; C02F 1/40 20130101; C02F 1/42 20130101; C02F
2101/32 20130101; C02F 2101/10 20130101; C02F 1/66 20130101; C02F
2303/22 20130101; C02F 1/04 20130101; C02F 1/20 20130101; C02F
1/004 20130101; C02F 9/00 20130101; C02F 1/283 20130101; C02F 1/24
20130101; C02F 11/122 20130101; C02F 1/463 20130101; C02F 2103/10
20130101 |
International
Class: |
B01D 21/02 20060101
B01D021/02; C02F 1/40 20060101 C02F001/40; C02F 1/66 20060101
C02F001/66; B03D 1/14 20060101 B03D001/14; C02F 1/24 20060101
C02F001/24 |
Claims
1. A water treatment system, comprising: a clean brine system,
comprising: a separation apparatus configured to remove at least a
portion of at least one suspended and/or emulsified immiscible
phase from an aqueous input stream received by the separation
apparatus to produce an immiscible-phase-diminished stream
containing less of the immiscible phase relative to the aqueous
input stream received by the separation apparatus; an ion-removal
apparatus fluidically connected to the separation apparatus and
configured to remove at least a portion of at least one
scale-forming ion from an aqueous input stream received by the
ion-removal apparatus to produce an ion-diminished stream
containing less of the at least one scale-forming ion relative to
the aqueous input stream received by the ion-removal apparatus; a
suspended solids removal apparatus fluidically connected to the
separation apparatus and/or the ion-removal apparatus and
configured to remove at least a portion of suspended solids from an
aqueous input stream received by the suspended solids removal
apparatus to produce a suspended-solids-diminished stream
containing less suspended solid material relative to the aqueous
input stream received by the suspended solids removal apparatus;
and a storage tank fluidically connected to at least one component
of the clean brine system such that no intervening precipitation
apparatus is fluidically connected between the storage tank and the
component.
2. The water treatment system according to claim 1, wherein no
crystallization tank is fluidically connected between the storage
tank and the component.
3. The water treatment system according to claim 1, wherein no
intervening humidifier or dehumidifier apparatus is fluidically
connected between the storage tank and the component.
4. The water treatment system according to claim 1, wherein the
storage tank is directly fluidically connected to at least one
component of the clean brine system.
5. The water treatment system according to claim 1, wherein the
separation apparatus comprises an induced air flotation (IAF)
separator.
6. The water treatment system according to claim 1, wherein the
separation apparatus is configured to remove droplets of the
immiscible phase having an average droplet size of at least about
20 microns.
7. The water treatment system according to claim 1, wherein the
immiscible phase comprises oil and/or grease.
8. The water treatment system according to claim 1, wherein the
ion-removal apparatus comprises a chemical ion-removal
apparatus.
9. The water treatment system according to claim 8, wherein the
ion-removal apparatus is configured to add caustic soda, soda ash,
and/or an anionic polymer to the aqueous input stream received by
the ion-removal apparatus.
10. The water treatment system according to claim 1, wherein the
ion-removal apparatus is configured to remove at least about 5% of
the scale-forming ion from the aqueous input stream received by the
ion-removal apparatus.
11. The water treatment system according to claim 1, wherein the
ion-diminished stream contains the scale-forming ion in an amount
of about 5000 mg/L or less.
12. The water treatment system according claim 1, wherein the
suspended solids removal apparatus comprises a filter, a gravity
settler, and/or a coagulant-induced flocculator.
13. The water treatment system according to claim 12, wherein the
filter comprises a bag filter and/or a granular bed filter.
14. The water treatment system according to claim 1, further
comprising a pH adjustment apparatus fluidically connected to the
separation apparatus, ion-removal apparatus, and/or suspended
solids removal apparatus and configured to increase or decrease the
pH of an aqueous input stream received by the pH adjustment
apparatus to produce a pH-adjusted stream.
15. The water treatment system according to claim 1, further
comprising a VOM removal apparatus fluidically connected to the
separation apparatus, ion-removal apparatus, suspended solids
removal apparatus, and/or pH adjustment apparatus and configured to
remove at least a portion of VOM from an aqueous input stream
received by the VOM removal apparatus to produce a VOM-diminished
stream.
16. The water treatment system according to claim 15, wherein the
VOM removal apparatus comprises a carbon bed filter and/or an air
stripper.
17. The water treatment system according claim 1, further
comprising a filtration apparatus fluidically connected to the
separation apparatus, the ion-removal apparatus, the suspended
solids removal apparatus, the pH adjustment apparatus, and/or the
VOM removal apparatus.
18. The water treatment system according to claim 17, wherein the
filtration apparatus comprises a filter press.
19. A method for treating water, comprising: supplying an aqueous
input stream to a separation apparatus; removing, within the
separation apparatus, at least a portion of at least one suspended
and/or emulsified immiscible phase from the aqueous input stream to
produce an immiscible-phase-diminished stream containing less of
the immiscible phase relative to the aqueous input stream;
supplying at least a portion of the immiscible-phase-diminished
stream to an ion-removal apparatus; removing, within the
ion-removal apparatus, at least a portion of at least one
scale-forming ion from the immiscible-phase-diminished stream to
produce an ion-diminished stream containing less of the at least
one scale-forming ion relative to the immiscible-phase-diminished
stream; and directing at least a portion of the ion-diminished
stream to a storage tank.
20. The method for treating water according to claim 19, wherein
the directing step involves directing at least a portion of the
ion-diminished stream to the storage tank without first directing
the portion of the ion-diminished stream to any crystallization
tank, humidifier apparatus, or dehumidifier apparatus.
21-31. (canceled)
Description
RELATED APPLICATIONS
[0001] This application claims priority under 35 U.S.C.
.sctn.119(e) to U.S. Provisional Patent Application Ser. No.
62/115,120, filed Feb. 11, 2015, and entitled "Water Treatment
Systems and Associated Methods," which is incorporated herein by
reference in its entirety for all purposes.
TECHNICAL FIELD
[0002] Systems for the treatment of water, and associated methods,
are generally described.
BACKGROUND
[0003] Extraction of oil and gas from subterranean reservoirs may
produce contaminated water as a byproduct (e.g., produced water).
In some cases, it may be desirable to treat the contaminated water
to remove one or more contaminants. For example, treated water may
be useful as a drilling fluid and/or a fracking fluid in oil and
gas extraction operations. In certain cases, it may be desirable to
treat the contaminated water to comply with government
regulations.
[0004] In some cases, it may be desirable to feed the contaminated
water to a desalination system to remove an amount of salt to
produce fresh water suitable for human consumption, irrigation,
and/or industrial use. However, the presence of oils, suspended
solids, scale-forming ions, and other contaminants in the
contaminated water can complicate and impede the operation of a
desalination system. Accordingly, it may be desirable to pre-treat
a contaminated water stream to remove at least a portion of one or
more contaminants prior to feeding the contaminated water stream to
a desalination system.
[0005] Accordingly, improved systems for treating contaminated
water are needed.
SUMMARY
[0006] Water treatment systems and associated methods are generally
described. The subject matter of the present invention involves, in
some cases, interrelated products, alternative solutions to a
particular problem, and/or a plurality of different uses of one or
more systems and/or articles.
[0007] Certain aspects relate to a method for treating water. In
some embodiments, the method comprises supplying a saline water
input stream having a first concentration of a scale-forming ion to
an ion-removal apparatus; removing, within the ion-removal
apparatus, at least a portion of the scale-forming ion from the
saline water input stream to produce a first ion-diminished stream
having a second concentration of the scale-forming ion, wherein the
second concentration is lower than the first concentration;
collecting a product stream comprising at least a portion of the
first ion-diminished stream; removing, within the ion-removal
apparatus, at least a portion of the scale-forming ion from the
saline water input stream to produce a second ion-diminished stream
having a third concentration of the scale-forming ion, wherein the
third concentration is lower than the second concentration; and
feeding the second ion-diminished stream to a desalination system
to produce a substantially pure water stream having a lower
concentration of a dissolved salt than the second ion-diminished
stream and a concentrated brine stream having a higher
concentration of the dissolved salt than the second ion-diminished
stream.
[0008] In some embodiments, the method for treating water comprises
supplying a saline water input stream to a separation apparatus;
removing, within the separation apparatus, at least a portion of at
least one suspended and/or emulsified immiscible phase from the
saline water input stream to produce an immiscible-phase-diminished
stream containing less of the immiscible phase relative to the
saline water input stream; supplying at least a portion of the
immiscible-phase-diminished stream to an ion-removal apparatus;
removing, within the ion-removal apparatus, at least a portion of
at least one scale-forming ion from the immiscible-phase-diminished
stream to produce an ion-diminished stream containing less of the
at least one scale-forming ion relative to the
immiscible-phase-diminished stream; and directing at least a
portion of the ion-diminished stream to a storage tank.
[0009] Some aspects relate to a water treatment system. In some
embodiments, the system comprises an ion-removal apparatus
configured to remove at least a portion of a scale-forming ion from
a saline water input stream having a first concentration of the
scale-forming ion to produce a first ion-diminished stream having a
second concentration of the scale-forming ion under a first set of
operating conditions, wherein the second concentration is lower
than the first concentration, and a second ion-diminished stream
having a third concentration of the scale-forming ion under a
second set of operating conditions, wherein the third concentration
is lower than the second concentration, wherein the ion-removal
apparatus comprises an outlet configured to collect a product
stream comprising at least a portion of the first ion-diminished
stream; and a desalination system fluidically connected to the
ion-removal apparatus, wherein the desalination system is
configured to receive the second ion-diminished stream and produce
a substantially pure water stream having a lower concentration of a
dissolved salt than the second ion-diminished stream and a
concentrated brine stream having a higher concentration of the
dissolved salt than the second ion-diminished stream.
[0010] According to some embodiments, a water treatment system
comprises a clean brine system. In some embodiments, the clean
brine system comprises a separation apparatus configured to remove
at least a portion of at least one suspended and/or emulsified
immiscible phase from an aqueous input stream received by the
separation apparatus to produce an immiscible-phase-diminished
stream containing less of the phase relative to the aqueous input
stream received by the separation apparatus; an ion-removal
apparatus fluidically connected to the separation apparatus and
configured to remove at least a portion of at least one
scale-forming ion from an aqueous input stream received by the
ion-removal apparatus to produce an ion-diminished stream
containing less of the at least one scale-forming ion relative to
the aqueous input stream received by the ion-removal apparatus; a
suspended solids removal apparatus fluidically connected to the
separation apparatus and configured to remove at least a portion of
suspended solids from an aqueous input stream received by the
suspended solids removal apparatus to produce a
suspended-solids-diminished stream containing less suspended solid
material relative to the aqueous input stream received by the
suspended solids removal apparatus; and a storage tank fluidically
connected to at least one component of the clean brine system such
that no intervening precipitation apparatus is fluidically
connected between the storage tank and the component.
[0011] Certain aspects relate to a method for forming concentrated
brine. In some embodiments, the method comprises supplying a saline
water input stream comprising an amount of suspended solids to a
suspended solids removal apparatus; removing, within the suspended
solids removal apparatus, at least a portion of the suspended
solids from the saline water input stream to produce a
suspended-solids-diminished stream having a lower amount of
suspended solids relative to the saline water input stream and a
suspended-solids-enriched stream having a higher amount of
suspended solids relative to the saline water input stream;
supplying at least a portion of the suspended-solids-enriched
stream to a filtration apparatus and removing at least a portion of
liquid within the suspended-solids-enriched stream to form a filter
cake; and adding an acid to the filter cake to form a brine
solution comprising a dissolved salt and having a density of at
least about 9 pounds/gallon.
[0012] In some embodiments, the method for forming concentrated
brine comprises supplying a saline water input stream comprising an
amount of suspended solids to a suspended solids removal apparatus;
removing, within the suspended solids removal apparatus, at least a
portion of the suspended solids from the saline water input stream
to produce a suspended-solids-diminished stream having a lower
amount of suspended solids relative to the saline water input
stream and a suspended-solids-enriched stream having a higher
amount of suspended solids relative to the saline water input
stream; supplying at least a portion of the
suspended-solids-enriched stream to a filtration apparatus and
removing at least a portion of liquid within the
suspended-solids-enriched stream to form a substantially solid
material; and adding an acid to the substantially solid material to
dissolve substantially all of the substantially solid material to
form a brine solution comprising a dissolved salt.
[0013] Other advantages and novel features of the present invention
will become apparent from the following detailed description of
various non-limiting embodiments of the invention when considered
in conjunction with the accompanying figures. In cases where the
present specification and a document incorporated by reference
include conflicting and/or inconsistent disclosure, the present
specification shall control.
BRIEF DESCRIPTION OF THE DRAWINGS
[0014] Non-limiting embodiments of the present invention will be
described by way of example with reference to the accompanying
figures, which are schematic and are not intended to be drawn to
scale. In the figures, each identical or nearly identical component
illustrated is typically represented by a single numeral. For
purposes of clarity, not every component is labeled in every
figure, nor is every component of each embodiment of the invention
shown where illustration is not necessary to allow those of
ordinary skill in the art to understand the invention. In the
figures:
[0015] FIG. 1 shows a schematic flow diagram of an exemplary water
treatment system comprising a clean brine system, a desalination
system, and a mixing apparatus, according to some embodiments;
[0016] FIG. 2A shows, according to some embodiments, a schematic
flow diagram of an exemplary clean brine system comprising a
separation apparatus, an ion-removal apparatus, a suspended solids
removal apparatus, a pH adjustment apparatus, a VOM removal
apparatus, and a filtration apparatus;
[0017] FIG. 2B shows, according to some embodiments, a schematic
flow diagram of an exemplary clean brine system comprising a
separation apparatus, an ion-removal apparatus, a filtration
apparatus, a pH adjustment apparatus, and a VOM removal
apparatus;
[0018] FIG. 3 shows a schematic flow diagram of an exemplary
separation apparatus, according to some embodiments;
[0019] FIG. 4 shows, according to some embodiments, a schematic
flow diagram of an exemplary ion-removal apparatus;
[0020] FIG. 5 shows, according to some embodiments, a schematic
flow diagram of an exemplary pH adjustment apparatus;
[0021] FIG. 6 shows a schematic flow diagram of an exemplary
humidification-dehumidification system, according to some
embodiments;
[0022] FIG. 7 shows a schematic flow diagram of an exemplary water
treatment system, according to some embodiments;
[0023] FIG. 8 shows, according to some embodiments, a schematic
flow diagram of an exemplary water treatment system;
[0024] FIG. 9 shows a schematic flow diagram of an exemplary water
treatment system, according to some embodiments;
[0025] FIG. 10 shows, according to some embodiments, a schematic
flow diagram of an exemplary water treatment system; and
[0026] FIG. 11 shows a schematic flow diagram of an exemplary water
treatment system, according to some embodiments.
DETAILED DESCRIPTION
[0027] Water treatment systems and associated methods are generally
described. Certain embodiments of the water treatment systems and
methods described herein may be used to treat water comprising one
or more contaminants (e.g., oil, grease, suspended solids,
scale-forming ions, volatile organic material) to remove at least a
portion of the one or more contaminants. In some embodiments, at
least a portion of the treated water may be used directly in
certain applications (e.g., oil and/or gas extraction processes).
In some embodiments, at least a portion of the treated water may
undergo desalination to produce substantially pure water and/or
concentrated brine. In some embodiments, at least a portion of the
treated water may be used to produce concentrated brine without the
use of a desalination process.
[0028] It has been discovered within the context of this invention
that a single water treatment system may be capable of producing a
variety of products, including, but not limited to, clean brine,
concentrated brine, ultra-high-density brine, substantially pure
water, mixed water (e.g., a water product comprising a combination
of clean brine and substantially pure water), and/or solid salt. In
some embodiments, the water treatment system may comprise a clean
brine system. According to certain embodiments, the clean brine
system may be used to treat a saline water input stream comprising
one or more contaminants to produce clean brine (e.g.,
contaminant-diminished saline water). In some embodiments, the
clean brine may be collected as a product stream. In certain cases,
the clean brine product stream may be directly used in certain
applications (e.g., oil and/or gas extraction processes). In some
cases, the same clean brine system may be used to treat a saline
water input stream comprising one or more contaminants to produce
clean brine suitable for desalination in a desalination system.
According to some embodiments, desalination of clean brine in the
desalination system may produce substantially pure water and/or
concentrated brine. In some embodiments, the substantially pure
water may be collected as a product stream. In certain cases, the
substantially pure water product stream may be used for human
consumption, irrigation, industrial use, and/or other applications.
In some embodiments, the concentrated brine may be collected as a
product stream. In certain cases, the concentrated brine product
stream may be directly used in certain applications (e.g., as a
kill fluid and/or drilling fluid in oil and/or gas extraction
processes). In certain cases, at least a portion of the
substantially pure water may be mixed with at least a portion of
the clean brine (e.g., clean brine for direct use) to produce a
mixed water product, which may be collected as a product stream. In
some embodiments, one or more additional salts may be added to at
least a portion of the concentrated brine to produce an
ultra-high-density brine. In certain embodiments, one or more salts
may be precipitated from the concentrated brine to produce solid
salt. In some embodiments, the clean brine system may be used to
produce concentrated brine in the absence of desalination. For
example, in certain cases, a concentrated brine stream may be
produced by adding an acid to a solid-containing stream produced by
the clean brine system.
[0029] In some cases, it may be advantageous for a single water
treatment system to be capable of producing two or more product
streams. For example, it may advantageously reduce costs (e.g.,
capital costs) to have a single water treatment system instead of a
plurality of water treatment systems, each producing a particular
type of product. In addition, a single water treatment system may
have reduced maintenance requirements, fewer components, and a
smaller footprint than a plurality of water treatment systems.
Further, water treatment systems described herein may
advantageously have flexibility in producing different types of
products. This flexibility may be particularly desirable in the oil
and gas industries, in which frequent changes to system designs may
be necessary.
[0030] FIG. 1 is a schematic diagram of an exemplary water
treatment system, according to some embodiments. As shown in FIG.
1, water treatment system 100 comprises clean brine system 102,
desalination system 110, and mixing apparatus 116, all of which are
fluidically connected to one another. As described in further
detail herein, clean brine system 102 may comprise one or more
units configured to remove one or more contaminants from a saline
water input stream. For example, clean brine system 102 may
comprise a separation apparatus, an ion-removal apparatus, a
suspended solids removal apparatus, a pH adjustment apparatus, a
volatile organic material (VOM) removal apparatus, and/or a
filtration apparatus. Desalination system 110 may be any type of
desalination system known in the art, and mixing apparatus 116 may
be any type of mixing apparatus known in the art.
[0031] In operation, a saline water input stream 104 may enter
clean brine system 102 from a source of saline water comprising one
or more contaminants. Non-limiting examples of the source of
contaminated saline water include an oil or gas well, a separator
(e.g., a gravity separator) configured to separate oil (e.g.,
produced oil) and water (e.g., produced water), and one or more
tanks containing contaminated saline water. In some embodiments,
clean brine system 102 may be configured to produce first clean
brine stream 106 comprising a first concentration of one or more
contaminants. First clean brine stream 106 may, in some cases, be
suitable for direct use in certain applications. For example, first
clean brine stream 106 may be suitable for use in oil and/or gas
extraction operations as a drilling fluid (e.g., a fluid that aids
in drilling a wellbore) and/or a fracking fluid (e.g., a fluid that
is injected into a wellbore to assist in fracturing subterranean
rock formations). In some embodiments, clean brine system 102 may
be configured to produce second clean brine stream 108 comprising a
second concentration of one or more contaminants. In certain cases,
the second concentration may be lower than the first concentration,
and second clean brine stream 108 may be a suitable feed stream for
a desalination system. In certain cases, it may be desirable for
second clean brine stream 108 to have a lower concentration of one
or more contaminants than first clean brine stream 106. In some
cases, desalination system 110 may concentrate one or more salts
and may comprise one or more components (e.g., a heat exchanger)
vulnerable to fouling (e.g., by salt formation). Accordingly, it
may be preferred for a stream entering desalination system 110 to
have lower concentrations of contaminants (e.g., scale-forming
ions) to avoid forming scale within the desalination system. In
order to remove more contaminants for second clean brine stream
108, chemical loading rates and/or the order of chemical loading
may be modified in clean brine system 102.
[0032] Clean brine system 102 may, in some embodiments, produce
first clean brine stream 106 and second clean brine stream 108 in
an alternating manner (e.g., during a first period of time clean
brine system 102 may produce first clean brine stream 106, and
during a second period of time clean brine system 102 may produce
second clean brine stream 108). In some cases, producing one or
more clean brine streams in an alternating manner may
advantageously reduce costs (e.g., chemical costs). For example,
such a system may require a lower amount of expensive chemicals
than a system in which desalination-quality brine is continuously
produced.
[0033] In some embodiments, second clean brine stream 108 may enter
desalination system 110. In some cases, desalination system 110 may
produce substantially pure water stream 112. In certain
embodiments, a first portion of substantially pure water stream 112
may optionally be recycled back to the desalination system and/or
the clean brine system. In certain embodiments, a second portion of
substantially pure water stream 112 may optionally be discharged
from water treatment system 100 and collected as a product stream.
In certain cases, a third portion of substantially pure water
stream 112 may optionally be mixed with at least a portion of first
clean brine stream 106 in mixing apparatus 116 to produce mixed
water stream 118. In addition to substantially pure water stream
112, desalination system 110 may produce concentrated brine stream
114, which may be collected as a product stream. In some
embodiments, an amount of one or more salts may be added to at
least a portion of concentrated brine stream 114 to produce an
ultra-high-density brine stream. In certain embodiments, one or
more salts may be precipitated from the concentrated brine stream
to produce a solid salt. According to certain embodiments, a
precipitation apparatus (not shown in FIG. 1) may be fluidically
connected to desalination system 110 to produce the solid salt.
[0034] It should be noted that water treatment system 100 may
comprise additional components. For example, water treatment system
100 may further comprise one or more optional buffer tanks (not
shown in FIG. 1) positioned between clean brine system 102 and
desalination system 110. In some cases, the presence of one or more
optional buffer tanks may facilitate continuous operation of
desalination system 110. For example, the presence of a buffer tank
may allow desalination system 110 to continue operating when clean
brine system 102 is producing first clean brine stream 106 for
direct use instead of second clean brine stream 108 for
desalination.
[0035] Water treatment systems and methods described herein may be
used to treat water from a variety of sources. In some embodiments,
a saline water input stream comprises produced water (e.g., water
that emerges from oil or gas wells along with the oil or gas). Due
to the length of time produced water has spent in the ground, and
due to high subterranean pressures and temperatures that may
increase the solubility of certain salts and/or minerals, produced
water often comprises relatively high concentrations of dissolved
salts and minerals. For example, some produced water streams may
comprise a supersaturated solution of dissolved strontium sulfate
(SrSO.sub.4). In addition, produced water may comprise a variety of
other substances, including oil and/or grease, organic compounds
(e.g., benzene, toluene), scale-forming ions, and/or suspended
solids. In some embodiments, at least a portion of the saline water
input stream comprises and/or is derived from seawater, ground
water, brackish water, and/or wastewater (e.g., industrial
wastewater). Non-limiting examples of wastewater include textile
mill wastewater, leather tannery wastewater, paper mill wastewater,
cooling tower blowdown water, flue gas desulfurization wastewater,
landfill leachate water, and/or the effluent of a chemical process
(e.g., the effluent of a desalination system, or another chemical
process).
[0036] In certain systems described herein, a clean brine system is
configured to receive a stream of saline water comprising one or
more contaminants and remove at least a portion of the one or more
contaminants to produce a contaminant-diminished saline water
stream (e.g., a clean brine stream). FIG. 2A is a schematic diagram
of an exemplary clean brine system 102, according to some
embodiments. As shown in FIG. 2A, clean brine system 102 comprises
separation apparatus 202 configured to remove at least a portion of
a suspended and/or emulsified immiscible phase from an aqueous
stream, ion-removal apparatus 204 configured to remove at least a
portion of at least one scale-forming ion from an aqueous stream,
suspended solids removal apparatus 206 configured to remove at
least a portion of suspended solids from an aqueous stream, pH
adjustment apparatus 208 configured to increase or decrease the pH
of an aqueous stream, volatile organic material (VOM) removal
apparatus 210 configured to remove at least a portion of VOM from
an aqueous stream, and filtration apparatus 212 configured to
produce a solid product (e.g., filter cake).
[0037] In operation, saline water input stream 104 comprising a
suspended and/or emulsified immiscible phase, a scale-forming ion,
suspended solids, and/or a volatile organic material is flowed to
separation apparatus 202. Separation apparatus 202 removes at least
a portion of the immiscible phase to produce
immiscible-phase-diminished stream 214, which contains less of the
immiscible phase than stream 104. In certain embodiments,
separation apparatus 202 also produces immiscible-phase-enriched
stream 216, which contains more of the immiscible phase than stream
104. Immiscible-phase-diminished stream 214 is then flowed to
ion-removal apparatus 204. Ion-removal apparatus 204 removes at
least a portion of at least one scale-forming ion to produce
ion-diminished stream 218, which contains less of at least one
scale-forming ion than immiscible-phase-diminished stream 214. In
certain embodiments, ion-removal apparatus 204 also produces
ion-enriched stream 220, which contains more of at least one
scale-forming ion than immiscible-phase-diminished stream 214.
Ion-diminished stream 218 is then flowed to suspended solids
removal apparatus 206. Suspended solids removal apparatus 206
removes at least a portion of suspended solids from ion-diminished
stream 218 to produce suspended-solids-diminished stream 222, which
contains less suspended solids than ion-diminished stream 218.
Suspended solids removal apparatus 206 also produces
suspended-solids-enriched stream 228, which may be flowed to
filtration apparatus 212 to form solid stream 230 and filtered
liquid stream 232. Suspended-solids-diminished stream 222 may be
flowed to pH adjustment apparatus 208. pH adjustment apparatus 208
may increase or decrease the pH of stream 222 to produce
pH-adjusted stream 224. In some cases, chemicals 234 may be added
in pH adjustment apparatus 208 to increase or decrease the pH of
stream 222. Stream 224 may be flowed to VOM removal apparatus 210.
VOM removal apparatus 210 may remove at least a portion of VOM from
stream 224 to produce VOM-diminished stream 108. VOM removal
apparatus 210 may also produce VOM-enriched stream 226.
VOM-diminished stream 108 may be discharged from clean brine system
102 as clean brine stream 108. In some cases, clean brine stream
108 may be collected as a product stream for direct use (e.g., in
oil or gas extraction). In some cases, clean brine stream 108 may
be flowed to a desalination system configured to remove at least a
portion of at least one dissolved salt from clean brine stream
108.
[0038] It should be noted that each of the components of clean
brine system 102 shown in FIG. 2A is optional, and a clean brine
system may comprise any combination of the components shown in FIG.
2A. For example, FIG. 2B is a schematic diagram of exemplary clean
brine system 102 comprising separation apparatus 202 configured to
remove at least a portion of a suspended and/or emulsified
immiscible phase from an aqueous stream, ion-removal apparatus 204
configured to remove at least a portion of at least one
scale-forming ion from an aqueous stream, filtration apparatus 212
configured to remove at least a portion of suspended solids from an
aqueous stream and form a substantially solid material, pH
adjustment apparatus 208 configured to increase or decrease the pH
of an aqueous stream, and volatile organic material (VOM) removal
apparatus 210 configured to remove at least a portion of VOM from
an aqueous stream.
[0039] In operation, saline water input stream 104 comprising a
suspended and/or emulsified immiscible phase, a scale-forming ion,
suspended solids, and/or a volatile organic material is flowed to
separation apparatus 202. Separation apparatus 202 removes at least
a portion of the immiscible phase to produce
immiscible-phase-diminished stream 214, which contains less of the
immiscible phase than stream 104. In certain embodiments,
separation apparatus 202 also produces immiscible-phase-enriched
stream 216, which contains more of the immiscible phase than stream
104. Immiscible-phase-diminished stream 214 is then flowed to
ion-removal apparatus 204. Ion-removal apparatus 204 removes at
least a portion of at least one scale-forming ion from stream 214
to produce ion-diminished stream 218, which contains less of at
least one scale-forming ion than immiscible-phase-diminished stream
214. In certain embodiments, ion-removal apparatus 204 also
produces ion-enriched stream 220, which contains more of at least
one scale-forming ion than immiscible-phase-diminished stream 214.
Ion-diminished stream 218 is then flowed to filtration apparatus
212 (e.g., a filter press, a vacuum filter). Filtration apparatus
212 removes at least a portion of suspended solids from
ion-diminished stream 218 to form suspended-solids-diminished
stream 232 (e.g., a filtered liquid stream), which contains less
suspended solids than ion-diminished stream 218, and solid stream
230. Suspended-solids-diminished stream 232 may be flowed to pH
adjustment apparatus 208, which may increase or decrease the pH of
stream 232 to produce pH-adjusted stream 224. In some cases,
chemicals 234 may be added in pH adjustment apparatus 208 to
increase or decrease the pH of stream 232. Stream 224 may be flowed
to VOM removal apparatus 210. VOM removal apparatus 210 may remove
at least a portion of VOM to produce VOM-diminished stream 108. VOM
removal apparatus 210 may also produce VOM-enriched stream 226.
VOM-diminished stream 108 may be discharged from clean brine system
102 as clean brine stream 108.
[0040] A schematic diagram of an exemplary water treatment system
comprising exemplary clean brine system 102 (as shown in FIGS.
2A-B) and an exemplary desalination system is shown in FIG. 7, as
described in further detail below. Schematic diagrams of additional
exemplary water treatment systems are shown in FIGS. 8-10.
[0041] In some embodiments, the clean brine system comprises an
optional separation apparatus configured to receive a saline water
input stream and remove at least a portion of a suspended and/or
emulsified immiscible phase (e.g., a water-immiscible liquid phase)
to produce an immiscible-phase-diminished saline water stream,
which contains less of the immiscible phase than the saline water
input stream. As used herein, a suspended and/or emulsified
immiscible phase (e.g., a water-immiscible material) refers to a
material that is not soluble in water to a level of more than 10%
by weight at the temperature and under the conditions at which the
separation apparatus operates. In some embodiments, the suspended
and/or emulsified immiscible phase comprises oil and/or grease. As
used herein, the term "oil" refers to a fluid that is generally
more hydrophobic than water and is not miscible or soluble in
water, as is known in the art. Thus, the oil may be a hydrocarbon
in some embodiments, but in other embodiments, the oil may comprise
other hydrophobic fluids.
[0042] In certain embodiments, the separation apparatus is
configured to remove a relatively large percentage of
water-immiscible materials from the stream fed to the separation
apparatus. For example, in some embodiments, the amount (in weight
percentage, wt %) of at least one water-immiscible material within
the stream exiting the separation apparatus (e.g., stream 214 in
FIG. 2) is at least about 50%, at least about 75%, at least about
90%, at least about 95%, or at least about 99% less than the amount
of the at least one water-immiscible material within the stream
entering the separation apparatus (e.g., stream 104 in FIG. 2). To
illustrate, if the stream exiting the separation apparatus contains
5 wt % water-immiscible material, and the stream entering the
separation apparatus contains 50 wt % water-immiscible material,
then the stream exiting the separation apparatus contains 90% less
water-immiscible material than the stream entering the separation
apparatus. In certain embodiments, the sum of the amounts of all
water-immiscible materials within the stream exiting the separation
apparatus is at least about 50%, at least about 75%, at least about
90%, at least about 95%, or at least about 99% less than the sum of
the amounts of all water-immiscible materials within the stream
entering the separation apparatus.
[0043] In some embodiments, the separation apparatus comprises one
or more separators. FIG. 3 shows a schematic diagram of an
exemplary separation apparatus. As shown in FIG. 3, separation
apparatus 202 comprises optional strainer 302, primary separator
304, optional secondary separator 306, and optional water tank 308.
In operation, saline water input stream 104 (e.g., corresponding to
saline water input stream 104 in FIG. 2) flows through optional
strainer 302. Strainer 302 may be configured to prevent particles
having a certain size from passing through strainer 302 to primary
separator 304. Saline water stream 310, which is the portion of
saline water input stream 104 that passes through strainer 302, may
then flow to primary separator 304. In primary separator 304, water
may be substantially separated from a suspended and/or emulsified
immiscible phase to produce first immiscible-phase-diminished
stream 312, which contains less water-immiscible material than
stream 310, and first immiscible-phase-enriched stream 314, which
contains more water-immiscible material than stream 310.
Immiscible-phase-diminished stream 312 may flow to water tank
308.
[0044] In some cases, immiscible-phase-enriched stream 314 may flow
to optional secondary separator 306. In secondary separator 306,
water-immiscible materials may be separated from any water
remaining in stream 314 to produce second
immiscible-phase-diminished stream 316 and second
immiscible-phase-enriched stream 216. Second
immiscible-phase-enriched stream 216 may be discharged from
separation apparatus 202, and second immiscible-phase-diminished
stream 316 may be flowed to water tank 308.
Immiscible-phase-diminished stream 214 formed by combining streams
312 and 316 may then be discharged from separation apparatus
202.
[0045] In some embodiments, immiscible-phase-diminished stream 214
flows to another unit of a clean brine system (e.g., an ion-removal
apparatus, a suspended solids removal apparatus, a pH adjustment
apparatus, a volatile organic material removal apparatus, a
filtration apparatus). In some embodiments,
immiscible-material-diminished stream 214 is discharged from a
clean brine system as clean brine. In some cases, the clean brine
may be made to flow to a desalination system. In some cases, the
clean brine may be used directly in certain applications (e.g., oil
and gas extraction operations). In certain embodiments, the clean
brine may be made to flow to one or more storage tanks
[0046] The primary separator may be any type of separator known in
the art. In some cases, the primary separator may at least
partially separate a portion of a suspended and/or emulsified
immiscible phase from an aqueous stream via gravity, centrifugal
force, adsorption, and/or using a barrier.
[0047] According to certain embodiments, the primary separator is
an induced gas flotation (IGF) separator. An IGF separator
generally refers to a device configured to introduce bubbles of a
gas into a volume of a liquid, where the gas bubbles adhere to
particles (e.g., droplets of water-immiscible material, small solid
particles) within the liquid volume and cause the particles to
float to the surface of the liquid volume. In a particular
embodiment, the gas is air, and the IGF separator may be referred
to as an induced air flotation (IAF) separator. Other examples of
suitable gases include, but are not limited to, carbon dioxide
(CO.sub.2), nitrogen (N.sub.2), and/or natural gas.
[0048] In some embodiments, an IGF separator comprises a vessel
capable of holding a volume of liquid and a diffuser (e.g., a
mechanical device configured to distribute a gas flow through a
liquid volume). In certain embodiments, a low pressure zone (e.g.,
a zone having a pressure of about 100 kPa or less) that draws in
ambient air may be formed in the IGF separator. For example, in
certain cases, a low pressure zone may be formed by a rapidly
rotating paddle inside a stationary diffuser or by rapid rotation
of the diffuser itself. According to some embodiments, the diffuser
is capable of introducing relatively small gas bubbles (e.g., gas
bubbles having an average diameter of about 100 microns or less)
into the liquid volume. In some cases, the relatively small gas
bubbles adhere to particles (e.g., droplets of a water-immiscible
material, suspended solid particles) within the liquid volume and
cause the particles to float to the surface of the liquid volume.
In some embodiments, a portion of the liquid volume below the
surface (e.g., a portion of the liquid volume that is substantially
free of gas bubbles and associated particles) may exit the IGF
separator (e.g., through an underflow weir) as an
immiscible-phase-diminished stream. In some embodiments, a portion
of the material floating on the surface of the liquid volume may
exit the IGF separator (e.g., over an underflow weir) as an
immiscible-phase-enriched stream.
[0049] In some embodiments, use of an IGF separator may be
associated with certain advantages. For example, in addition to
removing at least a portion of a suspended and/or emulsified
immiscible phase, an IGF separator may be capable of removing at
least a portion of one or more volatile organic materials (VOMs)
from a saline water input stream. As used herein, the term
"volatile organic material" or "VOM" is used to describe organic
materials that at least partially evaporate at 25.degree. C. and 1
atmosphere. In some embodiments, the IGF separator is capable of
removing at least a portion of one or more dissolved gases from a
saline water input stream. A non-limiting example of a dissolved
gas that may be removed from a saline water input stream by an IGF
separator is hydrogen sulfide (H.sub.2S). Without wishing to be
bound by a particular theory, at least a portion of one or more
dissolved gases may be drawn out of solution by a low pressure zone
formed by a diffuser of the IGF separator and/or may diffuse into
the gas bubbles. In certain embodiments, gas exiting the IGF
separator may be vented to reduce the possibility of buildup of one
or more flammable gases.
[0050] Although the primary separator has been described as being
an IGF separator, it should be noted that the primary separator may
be any other type of separator known in the art. For example, the
primary separator may comprise a hydrocyclone (e.g., a de-oiling
hydrocyclone), a corrugated plate interceptor, an adsorption media
filter, a coalescing media filter, a membrane filter, a gravity
separator (e.g., an American Petroleum Institute (API) separator),
a dissolved gas flotation (DGF) separator, and/or a skimmer.
[0051] In some embodiments, an aqueous stream flowing through the
primary separator has a relatively short residence time in the
primary separator. In some embodiments, the residence time of an
aqueous stream flowing through the primary separator is about 30
minutes or less, about 20 minutes or less, about 10 minutes or
less, about 8 minutes or less, about 6 minutes or less, about 4
minutes or less, about 2 minutes or less, or about 1 minute or
less. In some embodiments, the residence time of the aqueous input
stream in the primary separator is in the range of about 1 minute
to about 30 minutes, about 1 minute to about 20 minutes, about 1
minute to about 10 minutes, about 1 minute to about 8 minutes,
about 1 minute to about 6 minutes, about 1 minute to about 4
minutes, or about 1 minute to about 2 minutes.
[0052] Those of ordinary skill in the art are capable of
determining the residence time of a volume of fluid in a vessel.
For a batch (i.e., non-flow) apparatus, the residence time
corresponds to the amount of time the fluid spends in the vessel.
For a flow-based apparatus, the residence time is determined by
dividing the volume of the vessel by the volumetric flow rate of
the fluid through the vessel.
[0053] In some embodiments, the separation apparatus further
comprises a secondary separator positioned downstream of a primary
separator. In some cases, the secondary separator is configured to
remove at least a portion of a suspended and/or emulsified
immiscible phase from an immiscible-phase-enriched stream received
from the primary separator.
[0054] The secondary separator may be any type of separator known
in the art. In some cases, the secondary separator may at least
partially separate a portion of a suspended and/or emulsified
immiscible phase from an aqueous stream via gravity, centrifugal
force, adsorption, and/or using a barrier.
[0055] According to certain embodiments, the secondary separator
comprises a dissolved gas flotation (DGF) separator. A dissolved
gas flotation apparatus generally refers to a device configured to
dissolve a gas into a liquid volume. In some cases, the gas may be
dissolved in the liquid volume through the generation of very high
pressure zones. In certain embodiments, the dissolved gas may
precipitate as small gas bubbles (e.g., having an average diameter
of about 10 microns or less). In some embodiments, the small gas
bubbles may nucleate on particles (e.g., droplets of
water-immiscible material, suspended solid particles), and the
bubbles and associated particles may float to the surface of the
liquid volume. In certain embodiments, the gas is air, and the DGF
separator may be referred to as a dissolved air flotation (DAF)
separator. In certain cases, the density of air bubbles in a liquid
volume may be relatively low. In some cases, the relatively low
density of air bubbles may advantageously increase the rate of
buoyancy-driven separation between water and water-immiscible
materials.
[0056] In certain embodiments, the secondary separator comprises a
gravity separator. In some cases, the gravity separator comprises a
settling tank, and water and water-immiscible material in an
immiscible-phase-enriched stream received by the gravity separator
may be at least partially physically separated within the settling
tank. In certain cases, water present in the
immiscible-phase-enriched stream received by the gravity separator
may settle at the bottom of a settling tank, while water-immiscible
material may float to the top of the settling tank. In certain
embodiments, this separation may be at least partially attributed
to differences in the specific gravity of water and
water-immiscible material. In certain cases, at least a portion of
the water-immiscible material (e.g., oil) may be recovered from the
settling tank. The water-immiscible material may subsequently be
stored and/or transported off-site.
[0057] In some embodiments, water recovered from the
immiscible-phase-enriched stream may be combined with the
immiscible-phase-diminished stream produced by the primary
separator. In certain cases, the immiscible-phase-diminished
streams may be made to flow into one or more buffer tanks and/or
storage tanks In certain cases, the immiscible-phase-diminished
streams may be made to flow to other components of a clean brine
system (e.g., ion-removal apparatus, suspended solids removal
apparatus, pH adjustment apparatus, volatile organic material
removal apparatus, filtration apparatus).
[0058] In some cases, the immiscible-material-diminished streams
may be discharged from the clean brine system as clean brine.
[0059] In some embodiments, an aqueous stream flowing through the
secondary separator has a relatively long residence time in the
secondary separating apparatus. In some embodiments, the residence
time of an aqueous stream in the secondary separator is at least
about 5 minutes, at least about 10 minutes, at least about 15
minutes, at least about 20 minutes, at least about 25 minutes, at
least about 30 minutes, at least about 40 minutes, at least about
50 minutes, or at least about 60 minutes. In some embodiments, the
residence time of an aqueous stream in the secondary separator is
in the range of about 5 minutes to about 30 minutes, about 10
minutes to about 30 minutes, about 15 minutes to about 30 minutes,
about 20 minutes to about 30 minutes, or about 25 minutes to about
30 minutes.
[0060] In some embodiments, the residence time of an aqueous stream
flowing through the secondary separator may be longer than the
residence time of an aqueous stream flowing through the primary
separator. In some cases, the residence time of an aqueous stream
flowing through the secondary separator may be larger than the
residence time of an aqueous stream flowing through the primary
separator by at least about 5 minutes, at least about 10 minutes,
at least about 15 minutes, at least about 20 minutes, at least
about 25 minutes, or at least about 30 minutes. In certain
embodiments, it may be advantageous for the secondary separator to
have a longer residence time than the primary separating apparatus.
For example, a longer residence time in the secondary separator may
facilitate more complete separation between water and a
water-immiscible material without significantly reducing the flow
rate of an aqueous stream through a clean brine system.
[0061] Although the secondary separator has been described as
comprising a DGF separator and/or a gravity separator, it should be
noted that the secondary separator may be any other type of
separator known in the art. For example, the secondary separator
may comprise a hydrocyclone (e.g., a de-oiling hydrocyclone), a
corrugated plate interceptor, an adsorption media filter, a
coalescing media filter, a membrane filter, an induced gas
flotation (IGF) separator, and/or a skimmer.
[0062] In some embodiments, the primary separator and/or secondary
separator may be configured to remove droplets of the immiscible
phase having relatively small diameters.
[0063] In certain embodiments, the primary separator and/or
secondary separator are configured to remove droplets of the
immiscible phase having a diameter of about 200 microns or less,
about 150 microns or less, about 100 microns or less, about 50
microns or less, about 20 microns or less, about 10 microns or
less, about 5 microns or less, or about 1 micron or less. In
certain cases, the primary separator and/or secondary separator are
configured to remove droplets of the immiscible phase having an
average diameter of at least about 1 micron, at least about 5
microns, at least about 10 microns, at least about 20 microns, at
least about 50 microns, at least about 100 microns, at least about
150 microns, or at least about 200 microns. Combinations of the
above-noted ranges (e.g., about 1 micron to about 200 microns,
about 1 micron to about 100 microns, about 1 micron to about 50
microns, about 1 micron to about 10 microns) are also possible.
[0064] In some embodiments, the separation apparatus comprises one
or more additional components. According to some embodiments, the
separation apparatus further comprises an optional strainer
positioned upstream of the primary separator and/or the secondary
separator. A strainer generally refers to a device configured to
prevent the passage of particles having a certain size through the
strainer. In some embodiments, the strainer is configured to
prevent the passage of particles having an average diameter of at
least about 0.1 mm, at least about 0.5 mm, at least about 1 mm, at
least about 2 mm, at least about 5 mm, at least about 10 mm, at
least about 15 mm, or at least about 20 mm. Non-limiting examples
of suitable strainers include basket strainers, duplex basket
strainers (e.g., twin basket strainers), Y-strainers, T-strainers,
inline strainers, automatic self-cleaning strainers, plate
strainers (e.g., expanded cross-section strainers), scraper
strainers, and/or magnetic strainers.
[0065] In some embodiments, the separation apparatus further
comprises one or more optional buffer tanks In some embodiments,
one or more buffer tanks are positioned between the primary
separator and/or secondary separator and other components of a
clean brine system.
[0066] In certain cases, the separation apparatus further comprises
one or more additional separators. In some embodiments, the one or
more separators are positioned upstream of the primary separator.
The one or more upstream separators may be any type of separator
known in the art. In some embodiments, the one or more upstream
separators at least partially separate the suspended and/or
emulsified immiscible phase from water via gas flotation, gravity,
centrifugal force, adsorption, and/or using a barrier. In some
embodiments, the one or more upstream separators comprise a
hydrocyclone (e.g., a de-oiling hydrocyclone), a corrugated plate
interceptor, an adsorption media filter, a coalescing media filter,
a membrane filter, an induced gas flotation (IGF) separator, or a
dissolved gas flotation (DGF) separator.
[0067] In certain embodiments, the one or more upstream separators
comprise a gravity separator. In some cases, the gravity separator
is an American Petroleum Institute (API) separator. An API
separator generally refers to a separator configured to separate
water and water-immiscible material based on the specific gravity
difference between the water and water-immiscible material (e.g.,
through settling). In some cases, an API separator may be used to
separate relatively large amounts of water and water-immiscible
material.
[0068] In certain embodiments, an API separator comprises
coalescing media. In some cases, an API separator comprises
parallel plates. In certain embodiments, the presence of parallel
plates in the API separator may advantageously reduce the residence
time required for separation by settling in the API separator.
[0069] It should be noted that the primary separator, optional
secondary separator, and/or one or more optional upstream
separators may be the same type of separator or different types of
separators.
[0070] In certain embodiments, the separation apparatus can be
configured to remove suspended solids. In some such embodiments,
the separation apparatus can be configured to perform any of the
functions described herein with respect to the suspended solids
removal apparatus. For example, in some such embodiments, the
separation apparatus can be configured to remove dirt, precipitated
salts, organic solids, and/or any other suspended solid material.
In some embodiments, the separation apparatus can be configured to
remove at least about 50%, at least about 75%, at least about 90%,
at least about 95%, or at least about 99% of the suspended solids
within the stream that is transported to the separation
apparatus.
[0071] The separation apparatus may be fluidically connected to one
or more other unit operations of the clean brine system, either
directly or indirectly. In some embodiments, the separation
apparatus may be fluidically connected to an optional ion-removal
apparatus. For example, in FIG. 2A, separation apparatus 202 is
fluidically connected to optional ion-removal apparatus 204,
described in more detail below, via stream 214. In some
embodiments, the separation apparatus may be fluidically connected
to an optional suspended solids removal apparatus. For example, in
FIG. 2A, separation apparatus 202 is fluidically connected to
optional suspended solids removal apparatus 206, described in more
detail below, via streams 214 and 218. The separation apparatus may
be, in some embodiments, fluidically connected to an optional pH
adjustment apparatus. For example, in FIG. 2A, separation apparatus
202 is fluidically connected to optional pH adjustment apparatus
208, described in more detail below, via streams 214, 218, and 222.
In some embodiments, the separation apparatus may be fluidically
connected to an optional VOM removal apparatus. For example, in
FIG. 2A, separation apparatus 202 is fluidically connected to
optional VOM removal apparatus 210 via streams 214, 218, 222, and
224. In some embodiments, the separation apparatus is fluidically
connected to a filtration apparatus, such as a filter press. For
example, in FIG. 2A, separation apparatus 202 is fluidically
connected to optional filtration apparatus 212 via streams 214,
218, and 228.
[0072] In some embodiments, the separation apparatus is directly
fluidically connected to an ion-removal apparatus. For example, in
FIG. 2A, separation apparatus 202 is directly fluidically connected
to ion-removal apparatus 204, described in more detail below, via
stream 214. It should be understood that the invention is not
limited to embodiments in which the separation apparatus is
directly fluidically connected to an ion-removal apparatus, and in
some embodiments, the separation apparatus can be directly
fluidically connected to one or more other unit operations. In some
embodiments, the separation apparatus is directly fluidically
connected to a suspended solids removal apparatus, described in
more detail below. In certain embodiments, the separation apparatus
is directly fluidically connected to a pH adjustment apparatus,
described in more detail below. According to some embodiments, the
separation apparatus is directly fluidically connected to a VOM
removal apparatus, described in more detail below. In some
embodiments, the separation apparatus is directly fluidically
connected to a filtration apparatus, described in more detail
below.
[0073] According to certain embodiments, the clean brine system
comprises an optional ion-removal apparatus. The ion-removal
apparatus can be configured to remove at least a portion of at
least one scale-forming ion from an aqueous feed stream received by
the ion-removal apparatus to produce an ion-diminished stream.
Generally, the ion-diminished stream contains less of the
scale-forming ion (e.g., a scale-forming cation and/or a
scale-forming anion) relative to the aqueous feed stream received
by the ion-removal apparatus. The use of the ion-removal apparatus
to remove scale-forming ions can reduce the level of scaling within
unit operations downstream of the ion-removal apparatus.
[0074] The ion-removal apparatus can be configured to remove any
scale-forming ion that is desired to be removed. Those of ordinary
skill in the art are familiar with scale-forming ions, which are
ions that tend to form solid scale when present in concentrations
exceeding their solubility levels. In some cases, the scale-forming
ion is a scale-forming cation (e.g., a multivalent cation).
Non-limiting examples of scale-forming cations include Mg.sup.2+,
Ca.sup.2+, Sr.sup.2+, and Ba.sup.2+. In some cases, at least one
scale-forming ion is a scale-forming anion (e.g., a multivalent
anion). Non-limiting examples of scale-forming anions include
carbonate anions (CO.sub.3.sup.2-), bicarbonate anions
(HCO.sub.3.sup.-), sulfate anions (SO.sub.4.sup.2-), bisulfate
anions (HSO.sub.4.sup.-), and dissolved silica (e.g.,
SiO.sub.2(OH).sub.2.sup.2-, SiO(OH).sup.3-,
(SiO.sub.3.sup.2-).sub.n). In certain embodiments, the ion-removal
apparatus is configured to remove at least a portion of at least
one scale-forming ion in an aqueous feed stream while allowing a
dissolved monovalent salt (e.g., NaCl) to remain dissolved in the
aqueous stream transported out of the ion-removal apparatus.
[0075] In some instances, the scale-forming ions that are removed
from the aqueous feed stream using the ion-removal apparatus are
sparingly soluble (e.g., having a solubility of less than about 1
gram per 100 grams of water, less than about 0.1 grams per 100
grams of water, or less than about 0.01 grams per 100 grams of
water (or lower) at 20.degree. C.). Therefore, according to some
embodiments, such scale-forming ions may be prone to scaling within
various parts of a water treatment system. Examples of sparingly
soluble salts containing scale-forming ions include, but are not
limited to, calcium carbonate (CaCO.sub.3), which has a solubility
of about 0.000775 grams per 100 grams of water at 20.degree. C.;
calcium sulfate (CaSO.sub.4), which has a solubility of about 0.264
grams per 100 grams of water at 20.degree. C.; magnesium hydroxide
(Mg(OH).sub.2), which has a solubility of about 0.0009628 grams per
100 grams of water at 20.degree. C.; and barium sulfate
(BaSO.sub.4), which has a solubility of about 0.000285 grams per
100 grams of water at 20.degree. C. The ion-removal apparatus can
be configured, according to certain embodiments, such that removal
of the scale-forming ions inhibits or prevents scaling of solid
salts comprising the scale-forming ions during operation of the
water treatment system.
[0076] In certain embodiments, the ion-removal apparatus is
configured to produce at least two ion-diminished streams
comprising different concentrations of one or more scale-forming
ions. In some embodiments, the ion-removal apparatus is configured
to produce a first ion-diminished stream comprising a first
concentration of one or more scale-forming ions and a second
ion-diminished stream comprising a second concentration of the one
or more scale-forming ions. In some cases, the first concentration
may be larger than the second concentration.
[0077] According to certain embodiments, the ion-removal apparatus
is configured to produce a first ion-diminished stream in which the
concentration, in milligrams per liter, of at least one
scale-forming ion (e.g., Ca.sup.2+) within the first ion-diminished
stream (e.g., stream 106 in FIG. 1) is about 5000 mg/L or less,
about 4000 mg/L or less, about 3000 mg/L or less, about 2500 mg/L
or less, about 2000 mg/L or less, about 1800 mg/L or less, about
1500 mg/L or less, about 1000 mg/L or less, about 500 mg/L or less,
about 200 mg/L or less, about 100 mg/L or less, about 50 mg/L or
less, about 20 mg/L or less, about 10 mg/L or less, about 5 mg/L or
less, about 2 mg/L or less, about 1 mg/L or less, or about 0.1 mg/L
or less. In some embodiments, the concentration of at least one
scale-forming ion within the first ion-diminished stream is in the
range of about 0.1 mg/L to about 5000 mg/L, about 0.1 mg/L to about
4000 mg/L, about 0.1 mg/L to about 3000 mg/L, about 0.1 mg/L to
about 2500 mg/L, about 0.1 mg/L to about 2000 mg/L, about 0.1 mg/L
to about 1800 mg/L, about 0.1 mg/L to about 1500 mg/L, about 0.1
mg/L to about 1000 mg/L, about 0.1 mg/L to about 500 mg/L, about
0.1 mg/L to about 200 mg/L, about 0.1 mg/L to about 100 mg/L, about
0.1 mg/L to about 50 mg/L, about 0.1 mg/L to about 20 mg/L, about
0.1 mg/L to about 10 mg/L, about 0.1 mg/L to about 5 mg/L, about
0.1 mg/L to about 2 mg/L, or about 0.1 mg/L to about 1 mg/L. In
some embodiments, the first ion-diminished stream is substantially
free of at least one scale-forming ion.
[0078] In some embodiments, the ion-removal apparatus is configured
to produce a first ion-diminished stream in which the total
concentration, in milligrams per liter, of scale-forming ions
within the first ion-diminished stream is about 5000 mg/L or less,
about 4000 mg/L or less, about 3000 mg/L or less, about 2000 mg/L
or less, about 1000 mg/L or less, about 500 mg/L or less, about 200
mg/L or less, 100 mg/L or less, about 50 mg/L or less, about 20
mg/L or less, about 10 mg/L or less, about 5 mg/L or less, about 2
mg/L or less, about 1 mg/L or less, or about 0.1 mg/L or less. In
some embodiments, the total concentration of scale-forming ions
within the first ion-diminished stream is in the range of about 0.1
mg/L to about 5000 mg/L, about 0.1 mg/L to about 4000 mg/L, about
0.1 mg/L to about 3000 mg/L, about 0.1 mg/L to about 2000 mg/L,
about 0.1 mg/L to about 1000 mg/L, about 0.1 mg/L to about 500
mg/L, about 0.1 mg/L to about 200 mg/L, about 0.1 mg/L to about 100
mg/L, about 0.1 mg/L to about 50 mg/L, about 0.1 mg/L to about 20
mg/L, about 0.1 mg/L to about 20 mg/L, about 0.1 mg/L to about 10
mg/L, about 0.1 mg/L to about 5 mg/L, about 0.1 mg/L to about 2
mg/L, or about 0.1 mg/L to about 1 mg/L. In some embodiments, the
first ion-diminished stream exiting the ion-removal apparatus is
substantially free of scale-forming ions.
[0079] In certain embodiments, the ion-removal apparatus is
configured to produce a first ion-diminished stream in which the
concentration, in moles per liter (i.e., molarity), of at least one
scale-forming ion within the first ion-diminished stream is at
least about 5%, at least about 10%, at least about 15%, at least
about 20%, at least about 25%, at least about 30%, at least about
40%, at least about 50%, at least about 60%, at least about 70%, or
at least about 75% less than the concentration of the at least one
scale-forming ion within the stream entering the ion-removal
apparatus. In certain embodiments, the sum of the concentrations,
in moles per liter, of all scale-forming ions within the first
ion-diminished stream is at least about 5%, at least about 10%, at
least about 15%, at least about 20%, at least about 25%, at least
about 30%, at least about 40%, at least about 50%, at least about
60%, at least about 70%, or at least about 75% less than the sum of
the concentrations of all scale-forming ions within the stream
entering the ion-removal apparatus.
[0080] According to certain embodiments, the ion-removal apparatus
is configured to produce a second ion-diminished stream in which
the concentration, in milligrams per liter, of at least one
scale-forming ion within the second ion-diminished stream (e.g.,
stream 108 in FIG. 1) is about 750 mg/L or less, about 500 mg/L or
less, about 200 mg/L or less, about 100 mg/L or less, about 50 mg/L
or less, about 20 mg/L or less, about 10 mg/L or less, about 5 mg/L
or less, about 2 mg/L or less, about 1 mg/L or less, about 0.1 mg/L
or less, or about 0 mg/L. In some embodiments, the concentration of
at least one scale-forming ion within the second ion-diminished
stream is in the range of about 0 mg/L to about 750 mg/L, about 0
mg/L to about 500 mg/L, about 0 mg/L to about 200 mg/L, about 0
mg/L to about 100 mg/L, about 0 mg/L to about 50 mg/L, about 0 mg/L
to about 20 mg/L, about 0 mg/L to about 10 mg/L, about 0 mg/L to
about 5 mg/L, about 0 mg/L to about 2 mg/L, or about 0 mg/L to
about 1 mg/L. In some embodiments, the second ion-diminished stream
is substantially free of at least one scale-forming ion.
[0081] In some embodiments, the ion-removal apparatus is configured
to produce a second ion-diminished stream in which the total
concentration, in milligrams per liter, of scale-forming ions
within the second ion-diminished stream is about 2600 mg/L or less,
about 2500 mg/L or less, about 2000 mg/L or less, about 1800 mg/L
or less, about 1500 mg/L or less, about 1000 mg/L or less, about
900 mg/L or less, about 800 mg/L or less, about 700 mg/L or less,
about 600 mg/L or less, about 500 mg/L or less, about 200 mg/L or
less, about 100 mg/L or less, about 50 mg/L or less, about 20 mg/L
or less, about 10 mg/L or less, about 5 mg/L or less, about 2 mg/L
or less, about 1 mg/L or less, about 0.1 mg/L or less, or about 0
mg/L. In some embodiments, the total concentration of scale-forming
ions within the second ion-diminished stream is in the range of
about 0 mg/L to about 2600 mg/L, about 0 mg/L to about 2500 mg/L,
about 0 mg/L to about 2000 mg/L, about 0 mg/L to about 1800 mg/L,
about 0 mg/L to about 1500 mg/L, about 0 mg/L to about 1000 mg/L,
about 0 mg/L to about 500 mg/L, about 0 mg/L to about 200 mg/L,
about 0 mg/L to about 100 mg/L, about 0 mg/L to about 50 mg/L,
about 0 mg/L to about 20 mg/L, about 0 mg/L to about 10 mg/L, about
0 mg/L to about 5 mg/L, about 0 mg/L to about 2 mg/L, or about 0
mg/L to about 1 mg/L. In some embodiments, the second
ion-diminished stream exiting the ion-removal apparatus is
substantially free of scale-forming ions.
[0082] In certain embodiments, the ion-removal apparatus is
configured to produce a second ion-diminished stream in which the
concentration, in moles per liter (i.e., molarity), of at least one
scale-forming ion within the second ion-diminished stream is at
least about 50%, at least about 75%, at least about 90%, at least
about 95%, or at least about 99% less than the concentration of the
at least one scale-forming ion within the stream entering the
ion-removal apparatus. In certain embodiments, the sum of the
concentrations, in moles per liter, of all scale-forming ions
within the second ion-diminished stream is at least about 50%, at
least about 75%, at least about 90%, at least about 95%, or at
least about 99% less than the sum of the concentrations of all
scale-forming ions within the stream entering the ion-removal
apparatus.
[0083] In some embodiments, the concentration, in moles per liter
(i.e., molarity), of at least one scale-forming ion within the
second ion-diminished stream is at least about 5%, at least about
10%, at least about 20%, at least about 50%, at least about 75%, at
least about 90%, or at least about 99% less than the concentration
of the at least one scale forming ion within the first
ion-diminished stream. In certain embodiments, the sum of the
concentrations, in moles per liter, of all scale-forming ions
within the second ion-diminished stream is at least about 5%, at
least about 10%, at least about 20%, at least about 50%, at least
about 75%, at least about 90%, or at least about 99% less than the
sum of the concentrations of all scale-forming ions within the
first ion-diminished stream.
[0084] In some cases, the two ion-diminished streams may be
suitable for different purposes. In some embodiments, the first
ion-diminished stream may be collected as a product stream. In
certain embodiments, the first ion-diminished stream may be
suitable for direct use in certain applications. For example, in
certain cases, the first ion-diminished stream may be used as a
drilling fluid and/or fracking fluid in oil and gas extraction
operations. In such applications, the first ion-diminished stream
may not encounter heat exchangers or other system components
vulnerable to scale formation, and a relatively high concentration
of one or more scale-forming ions may be acceptable. In certain
embodiments, the second ion-diminished stream may be suitable for
further processing in a desalination system. Accordingly, in some
cases, the second ion-diminished stream may be fed to a
desalination system to produce a substantially pure water stream
having a lower concentration of a dissolved salt than the second
ion-diminished stream and a concentrated brine stream having a
higher concentration of the dissolved salt than the second
ion-diminished stream. In such processing, the second
ion-diminished stream may come into contact with heat exchangers
and other system components vulnerable to scale formation.
Accordingly, to reduce or prevent formation of scale within a
desalination system, lower concentrations of one or more
scale-forming ions in the second ion-diminished stream may be
desirable.
[0085] A variety of types of ion-removal apparatuses may be used in
the embodiments described herein. In some embodiments, the
ion-removal apparatus comprises a chemical ion-removal apparatus.
According to certain embodiments, the chemical ion-removal
apparatus comprises one or more ion removal compositions configured
to induce precipitation of at least one scale-forming ion. For
example, the chemical ion-removal apparatus can be configured to
remove at least one ion using caustic soda (e.g., NaOH), soda ash
(e.g., Na.sub.2CO.sub.3), and/or a flocculent (e.g., an anionic
polymer). In some embodiments, the one or more ion removal
compositions can be configured to induce precipitation of at least
one scale-forming cation. For example, when caustic soda and/or
soda ash are added to a stream containing Ca.sup.2+ and/or
Mg.sup.2+, at least a portion of Ca.sup.2+ and/or Mg.sup.2+
contained within the stream may be precipitated as an insoluble
solid such as, for example, calcium carbonate (CaCO.sub.3) and/or
magnesium hydroxide (Mg(OH).sub.2). Without wishing to be bound by
a particular theory, the addition of caustic soda may induce
precipitation of certain scale-forming cations in a stream by
increasing the pH of the stream. In some cases, carbonate salts
and/or hydroxide salts of the scale-forming cations have relatively
low solubility at relatively high pH levels, and increasing the pH
of a stream containing scale-forming cations may induce
precipitation of such carbonate salts and/or hydroxide salts of the
scale-forming cations. In certain embodiments, the addition of soda
ash may facilitate precipitation of carbonate salts of certain
scale-forming anions by providing a supply of carbonate ions. In
some embodiments, the one or more ion removal compositions can be
configured to induce precipitation of at least one scale-forming
anion.
[0086] In some embodiments, the one or more ion removal
compositions comprise a flocculent. A flocculent generally refers
to a composition that causes relatively large particles to form
through aggregation of smaller particles. In some embodiments, the
relatively large particles may precipitate from a solution.
Non-limiting examples of suitable flocculents include ferric
chloride, polyaluminum chloride, activated silica, colloidal clays
(e.g., bentonite), metallic hydroxides with a polymeric structure
(e.g., alum, ferric hydroxide), starches and/or starch derivatives
(e.g., corn starch, potato starch, anionic oxidized starches,
amine-treated cationic starches), polysaccharides (e.g., guar gum),
alginates, polyacrylamides (e.g., nonionic, anionic, or cationic
polyacrylamides), polyethylene-imines, polyamide-amines,
polyamines, polyethylene oxide, and/or sulfonated compounds.
Without wishing to be bound by a particular theory, certain
flocculents may form large particles (e.g., large precipitates) by
enmeshing smaller particles on formation and/or entrapping smaller
particles through adhesion.
[0087] In some embodiments, the flocculent comprises a polymer. In
some cases, the flocculent may be a large-chain polymer. Without
wishing to be bound by a particular theory, a large-chain polymer
flocculent may facilitate the formation of large particles by
adhering to a plurality of smaller particles. In some cases, a
large-chain polymer flocculent may facilitate the formation of
large particles of increased size and/or increased mechanical
strength. In some cases, the flocculent may be an anionic polymer
flocculent. In some embodiments, an anionic polymer flocculent may
be used to remove scale-forming cations. In some cases, the
flocculent may be a cationic polymer flocculent. In some
embodiments, a cationic polymer flocculent may be used to remove
scale-forming anions.
[0088] It should be noted that mixtures of the above-mentioned ion
removal compositions and/or other ion removal compositions may also
be used. In addition, if two or more ion removal compositions are
added to an aqueous feed stream, the ion removal compositions may
be added in any order. According to certain embodiments, caustic
soda and a polymer flocculent (e.g., an anionic polymer flocculent)
may be added to an aqueous feed stream. In certain cases, caustic
soda, soda ash, and a polymer flocculent (e.g., an anionic polymer
flocculent) may be added to an aqueous feed stream. FIG. 4 shows a
schematic diagram of exemplary ion-removal apparatus 204. As shown
in FIG. 4, optional ion-removal apparatus 204 comprises first
reaction tank 402, second reaction tank 404, and third reaction
tank 406. In operation, an aqueous feed stream 214 (e.g.,
corresponding to immiscible-phase-diminished stream 214 in FIGS. 2
and 3) enters optional ion-removal apparatus 204. Aqueous feed
stream 214 initially enters first reaction tank 402. In first
reaction tank 402, a first ion removal composition (e.g., caustic
soda) may be added to stream 214 to produce stream 408. Stream 408
may then be made to flow to second reaction tank 404. In second
reaction tank 404, a second ion removal composition (e.g., soda
ash) may be added to stream 408 to produce stream 410. Stream 410
may then be made to flow to third reaction tank 406. In third
reaction tank 406, a third ion removal composition (e.g., an
anionic polymer flocculent) may be added to stream 410 to produce
ion-diminished stream 218. In some cases, ion-diminished stream 218
may be made to flow to another unit of the clean brine system
(e.g., suspended solids removal apparatus, pH adjustment apparatus,
VOM removal apparatus, filtration apparatus) for further treatment.
In certain cases, ion-diminished stream 218 may be discharged from
the clean brine system as clean brine. In some embodiments,
ion-diminished stream 218 may be made to flow to one or more
storage tanks In some cases, ion-diminished stream 218 may be made
to flow to a desalination system.
[0089] It should be noted that a chemical ion-removal apparatus may
comprise any number of reaction tanks In some embodiments, a
chemical ion-removal apparatus may comprise one reaction tank, two
reaction tanks, three reaction tanks, four reaction tanks, five
reaction tanks, or more. In some embodiments, the residence time of
an aqueous stream flowing through the reaction tanks may be
relatively short. According to some embodiments, the residence time
of an aqueous stream in at least one reaction tank is about 30
minutes or less, about 20 minutes or less, about 10 minutes or
less, about 5 minutes or less, about 2 minutes or less, or about 1
minute or less. In certain embodiments, the residence time of an
aqueous stream in each reaction tank is about 30 minutes or less,
about 20 minutes or less, about 10 minutes or less, about 5 minutes
or less, about 2 minutes or less, or about 1 minute or less. In
some embodiments, one or more of the reaction tanks comprise an
agitator.
[0090] In certain embodiments, a chemical ion-removal apparatus
further comprises an optional flocculation tank positioned
downstream of one or more reaction tanks According to some
embodiments, the flocculation tank may comprise an agitator (e.g.,
a slowly-rotating, low shear agitator). In some embodiments,
conditions in the flocculation tank may be selected to increase the
size of precipitates formed by chemical reactions in one or more
upstream reaction tanks For example, in some cases, a low shear
agitator may be configured to promote motion of precipitates within
the flocculation tank. In some cases, motion of the precipitates
may cause at least some of the precipitates to collide with each
other and adhere to each other, resulting in the formation of
larger precipitates. In some embodiments, it may be advantageous to
have larger precipitates, as they may have a reduced settling time.
In some embodiments, the flocculation tank may have a relatively
large volume. In some embodiments, the residence time of an aqueous
stream in the flocculation tank may be about 60 minutes or less,
about 50 minutes or less, about 40 minutes or less, about 35
minutes or less, about 30 minutes or less, about 25 minutes or
less, about 20 minutes or less, about 15 minutes or less, or about
10 minutes or less. In some embodiments, the residence time of an
aqueous stream in the flocculation tank is in the range of about 10
minutes to about 20 minutes, about 10 minutes to about 25 minutes,
about 10 minutes to about 30 minutes, about 10 minutes to about 35
minutes, about 10 minutes to about 40 minutes, about 10 minutes to
about 50 minutes, about 10 minutes to about 60 minutes, about 20
minutes to about 30 minutes, about 20 minutes to about 40 minutes,
about 20 minutes to about 50 minutes, about 20 minutes to about 60
minutes, about 30 minutes to about 40 minutes, about 30 minutes to
about 50 minutes, or about 30 minutes to about 60 minutes.
[0091] According to some embodiments, a chemical ion-removal
apparatus may be configured to produce two or more ion-diminished
streams by varying the amount of one or more ion removal
compositions added to an aqueous feed stream. Without wishing to be
bound by a particular theory, the amount of an ion removal
composition added to an aqueous stream may be proportional to the
amount of one or more scale-forming ions precipitated. In certain
embodiments, relatively large amounts of one or more scale-forming
ions may be precipitated from an aqueous feed stream received by a
chemical ion-removal apparatus by adding amounts of one or more ion
removal compositions (e.g., caustic soda) in excess of what is
required stoichiometrically. In some cases, adding excess amounts
of one or more ion removal compositions (e.g., caustic soda) may
advantageously speed up reaction kinetics and result in
precipitation of a relatively large amount of one or more
scale-forming ions. Accordingly, in some embodiments, a first
amount of one or more ion removal compositions may be added to an
aqueous feed stream to produce a first ion-diminished stream having
a first concentration of scale-forming ions. In some embodiments, a
second, larger amount of one or more ion removal compositions may
be added to an aqueous feed stream to produce a second
ion-diminished stream having a second, smaller concentration of
scale-forming ions. In some embodiments, a chemical ion-removal
apparatus may be configured to produce the first ion-diminished
stream and the second ion-diminished stream in an alternating
manner.
[0092] In certain embodiments, the ion-removal apparatus comprises
an electrocoagulation apparatus. The electrocoagulation apparatus
can be configured, in some embodiments, to remove at least a
portion of suspended solids from an aqueous stream rather than, or
in addition to, removing at least a portion of at least one
scale-forming ion from the aqueous stream. Those of ordinary skill
in the art are familiar with electrocoagulation, in which short
wave electrolysis can be used to remove at least a portion of
multivalent ions and/or suspended contaminants.
[0093] In certain embodiments, the ion-removal apparatus comprises
a resin bed. The resin bed contains, according to certain
embodiments, an ion-exchange resin. The resin bed can comprise, for
example, an anion-selective resin bed and/or a cationic-selective
resin bed. In certain embodiments, the ion-removal apparatus
comprises an ion-exchange apparatus. The ion-exchange apparatus may
contain, for example, an ion-exchange medium. Those of ordinary
skill in the art are familiar with the function of ion-exchange
media, which generally remove at least one scale-forming ion from a
solution and, in some but not all cases, replace the scale-forming
ion(s) with one or more monovalent ion(s). For example, in certain
embodiments, the ion-exchange medium functions by contacting the
aqueous solution containing the scale-forming ion(s), after which
at least a portion of the scale-forming ions are captured by the
ion-exchange medium and at least a portion of the monovalent ions
originally contained within the ion-exchange medium are released
into the aqueous solution. In some such embodiments, the
ion-exchange medium comprises an ion exchange resin.
[0094] Those of ordinary skill in the art would be capable of
selecting an appropriate ion removal medium (e.g., an ion-exchange
medium or other ion removal medium) for use in the ion-removal
apparatus based upon the types of scale-forming ions dissolved in
the stream fed to the ion-removal apparatus, the concentration of
said ions, and the flow rate at which one desires to operate the
ion-removal apparatus, among other factors. The ion-removal
apparatus can include one or more tanks and/or columns in which the
ion removal operation is performed. For example, in certain
embodiments, the ion-removal apparatus comprises one or more tanks
into which an aqueous feed stream and the ion removal medium are
transported. In one set of embodiments, the aqueous feed stream and
a precipitation-inducing ion removal medium are fed to a series of
tanks in which precipitation of scale-forming ions is allowed to
occur. In other embodiments, a column (e.g., a packed column) can
be used to perform the ion removal operation. For example, in some
embodiments, the aqueous feed stream can be fed to one or more
packed columns containing an ion-exchange resin or other ion
removal medium, which may be used to remove at least a portion of
the scale-forming ion(s) from the aqueous solution. One of ordinary
skill in the art, given the present disclosure, would be capable of
designing a variety of other suitable configurations for performing
the ion removal steps described herein.
[0095] The ion-removal apparatus may be fluidically connected to
one or more other unit operations of the clean brine system, either
directly or indirectly. In some embodiments, the ion-removal
apparatus may be fluidically connected to an optional suspended
solids removal apparatus. For example, in FIG. 2A, ion-removal
apparatus 204 is fluidically connected to optional suspended solids
removal apparatus 206, described in more detail below, via stream
218. The ion-removal apparatus may be, in some embodiments,
fluidically connected to an optional pH adjustment apparatus. For
example, in FIG. 2A, ion-removal apparatus 204 is fluidically
connected to optional pH adjustment apparatus 208, described in
more detail below, via streams 218 and 222. In some embodiments,
the ion-removal apparatus may be fluidically connected to an
optional VOM removal apparatus. For example, in FIG. 2A,
ion-removal apparatus 204 is fluidically connected to optional VOM
removal apparatus 210 via streams 218, 222, and 224. In some
embodiments, the ion-removal apparatus is fluidically connected to
a filtration apparatus (e.g., a filter press, a vacuum filter). For
example, in FIG. 2A, ion-removal apparatus 204 is fluidically
connected to optional filtration apparatus 212 via streams 218 and
228.
[0096] In some embodiments, the ion-removal apparatus is directly
fluidically connected to a suspended solids removal apparatus. For
example, in FIG. 2A, ion-removal apparatus 204 is directly
fluidically connected to suspended solids removal apparatus 206,
described in more detail below, via stream 218. It should be
understood that the invention is not limited to embodiments in
which the ion-removal apparatus is directly fluidically connected
to a suspended solids removal apparatus, and in some embodiments,
the ion-removal apparatus can be directly fluidically connected to
one or more other unit operations. In some embodiments, the
ion-removal apparatus is directly fluidically connected to a
separation apparatus. In some embodiments, the ion-removal
apparatus is directly fluidically connected to a suspended solids
removal apparatus, described in more detail below. In some
embodiments, the ion-removal apparatus is directly fluidically
connected to a pH adjustment apparatus, described in more detail
below. According to some embodiments, the ion-removal apparatus is
directly fluidically connected to a VOM removal apparatus,
described in more detail below. In some embodiments, the
ion-removal apparatus is directly fluidically connected to a
filtration apparatus, described in more detail below.
[0097] In some embodiments, the clean brine systems described
herein comprise an optional suspended solids removal apparatus. The
suspended solids removal apparatus can be configured, according to
certain embodiments, to remove at least a portion of suspended
solids from an aqueous feed stream received by the suspended solids
removal apparatus to produce a suspended-solids-diminished stream.
Generally, the suspended-solids-diminished stream contains a
smaller quantity of suspended solids than the input stream received
by the suspended solids removal apparatus.
[0098] The suspended solids removal apparatus can be configured to
remove any suspended solids that may be present in the stream fed
to the suspended solids removal apparatus. According to certain
embodiments, the suspended solids removal apparatus can be
configured to remove particles that remain in suspension in water
as a colloid or due to the motion of the water. In some
embodiments, the suspended solids removal apparatus can be
configured to remove dirt, precipitated salts, organic solids
(e.g., pathogens such as bacteria, Giardia, and the like), and/or
any other solid material. In some embodiments, the suspended solids
that are removed by the suspended solids removal apparatus comprise
particulate solids.
[0099] In certain embodiments, the suspended solids removal
apparatus is configured to remove a relatively large percentage of
the suspended solids from the stream fed to the suspended solids
removal apparatus. For example, in some embodiments, the amount (in
weight percentage, wt %) of at least one suspended solid material
within the stream exiting the suspended solids removal apparatus
(e.g., stream 222 in FIG. 2) is at least about 50%, at least about
75%, at least about 90%, at least about 95%, or at least about 99%
less than the amount of the at least one suspended solid material
within the stream entering the suspended solids removal apparatus
(e.g., stream 218 in FIG. 2). In certain embodiments, the sum of
the amounts of all suspended solid materials within the stream
exiting the suspended solids removal apparatus is at least about
50%, at least about 75%, at least about 90%, at least about 95%, or
at least about 99% less than the sum of the amounts of all
suspended solid materials within the stream entering the suspended
solids removal apparatus.
[0100] A variety of types of devices may be used in the suspended
solids removal apparatuses described herein. In some embodiments,
the suspended solids removal apparatus comprises a filter, a
gravity settler, and/or a coagulant-induced flocculator. A filter
generally refers a device configured to inhibit passage of certain
materials (e.g., particles of a certain size) from one side of the
device to the other side of the device. A gravity settler generally
refers to a device that promotes separation of suspended solids
from a liquid through gravity (e.g., a settling tank). A
coagulant-induced flocculator generally refers to a device in which
a coagulant is added to a volume of liquid to induce flocculation.
Non-limiting examples of coagulants include ferric chloride, alum,
ferrous sulfate, ferric sulfate, ferric chloride, cationic polymer,
calcium hydroxide (e.g., lime), calcium oxide (e.g., quicklime),
sodium aluminate, ferric aluminum chloride, ferric chloride
sulfate, magnesium carbonate, aluminum chlorohydrate, polyaluminum
chloride, polyaluminum sulfate chloride, polyaluminum silicate
chloride, forms of polyaluminum chloride with organic polymers,
polyferric sulfate and ferric salts with polymers, and/or
polymerized aluminum-iron blends.
[0101] According to some embodiments, the gravity settler comprises
a clarifier. A clarifier generally refers to a tank (e.g., a
settling tank) that is configured for substantially continuous
removal of solids. In some embodiments, the clarifier is an
inclined-plate clarifier (e.g., a lamella clarifier). An
inclined-plate clarifier generally refers to a device comprising a
plurality of inclined plates. In operation, an aqueous stream may
enter the inclined-plate clarifier, and solid particles may begin
to settle on one or more of the inclined plates. In some cases,
when a solid particle settles on an inclined plate, it adheres to
other particles that have settled on the plate, and the particles
slide down the inclined plate to the bottom of the clarifier, where
they are collected as a solid-containing stream. In some
embodiments, the solid-containing stream may be transported to a
filtration apparatus, as described in further detail herein. In
certain embodiments, the remaining water may exit the clarifier as
a suspended-solids-diminished stream.
[0102] According to some embodiments, the suspended solids removal
apparatus comprises a filter. In some embodiments, the filter is a
polishing filter. A polishing filter generally refers to a filter
configured to prevent passage of relatively small particles and/or
remove low concentrations of dissolved material. Examples of a
suitable polishing filter include, but are not limited to, a
granular bed filter (e.g., a media filter) and a bag filter. A
granular bed filter refers to a filter that comprises one or more
types of granular filtration media (e.g., sand, crushed anthracite
coal, garnet sand, granular activated carbon, diatomaceous earth
medium). In some embodiments, the polishing filter is configured to
remove particles having an average diameter of at least about 0.1
micron, at least about 0.5 micron, at least about 1 micron, at
least about 2 microns, at least about 5 microns, at least about 10
microns, at least about 15 microns, at least about 20 microns, or
at least about 25 microns. In some embodiments, the polishing
filter is configured to remove particles having an average diameter
in the range of about 0.1 micron to about 25 microns, about 0.1
micron to about 20 microns, about 0.1 micron to about 15 microns,
about 0.1 micron to about 10 microns, about 0.1 micron to about 5
microns, about 0.1 micron to about 2 microns, about 0.1 micron to
about 1 micron, about 0.1 micron to about 0.5 micron, about 1
micron to about 25 microns, about 1 micron to about 20 microns,
about 1 micron to about 15 microns, about 1 micron to about 10
microns, about 1 micron to about 5 microns, about 1 micron to about
2 microns, about 10 microns to about 25 microns, about 10 microns
to about 20 microns, or about 10 microns to about 15 microns.
[0103] The suspended solids removal apparatus may be fluidically
connected to one or more other unit operations of the clean brine
system, either directly or indirectly. In some embodiments, the
suspended solids removal apparatus may be fluidically connected to
an optional pH adjustment apparatus. For example, in FIG. 2A,
suspended solids removal apparatus 206 is fluidically connected to
optional pH adjustment apparatus 208, described in more detail
below, via stream 222. In some embodiments, the suspended solids
removal apparatus may be fluidically connected to an optional VOM
removal apparatus. For example, in FIG. 2A, suspended solids
removal apparatus 206 is fluidically connected to optional VOM
removal apparatus 210 via streams 222 and 224. In some embodiments,
the suspended solids removal apparatus is fluidically connected to
a filtration apparatus (e.g., a filter press, a vacuum filter). For
example, in FIG. 2A, suspended solids removal apparatus 206 is
fluidically connected to optional filtration apparatus 212 via
stream 228.
[0104] In some embodiments, the suspended solids removal apparatus
is directly fluidically connected to an ion-removal apparatus. For
example, in FIG. 2A, suspended solids removal apparatus 206 is
directly fluidically connected to ion-removal apparatus 204 via
stream 218. It should be understood that the invention is not
limited to embodiments in which the suspended solids removal
apparatus is directly fluidically connected to an ion-removal
apparatus, and in some embodiments, the suspended solids removal
apparatus can be directly fluidically connected to one or more
other unit operations. In some embodiments, the suspended solids
removal apparatus is directly fluidically connected to a separation
apparatus. In some embodiments, the suspended solids removal
apparatus is directly fluidically connected to an ion-removal
apparatus. In some embodiments, the suspended solids removal
apparatus is directly fluidically connected to a pH adjustment
apparatus, described in more detail below. According to some
embodiments, the suspended solids removal apparatus is directly
fluidically connected to a VOM removal apparatus, described in more
detail below. In some embodiments, the suspended solids removal
apparatus is directly fluidically connected to a filtration
apparatus, described in more detail below.
[0105] In certain embodiments, the clean brine apparatus comprises
an optional pH adjustment apparatus configured to receive an
aqueous input stream and increase or decrease the pH of the aqueous
input stream to produce a pH-adjusted stream. In certain
embodiments, increasing or decreasing the pH of the aqueous input
stream can be performed without dissolving any particles that
precipitated (e.g., due to addition of an ion removal composition
in the ion-removal apparatus). In some embodiments, the pH of the
aqueous input stream may be adjusted to a pH in the range of about
6 to about 8, about 6.5 to about 7.5, about 6.8 to about 7.2, or
about 6.9 to about 7.1. In some embodiments, the pH-adjusted stream
has a pH of about 7.0.
[0106] In some embodiments, the pH adjustment apparatus is
configured to reduce the pH of the aqueous input stream. In certain
embodiments, reducing the pH of the aqueous input stream can be
performed in order to inhibit scale-forming ions from
precipitating.
[0107] In some embodiments, the pH of an aqueous feed stream may be
reduced by adding a pH-adjusting composition to the feed stream.
For example, in certain embodiments, an acid may be added to the
feed stream to reduce the pH of the stream. Non-limiting examples
of suitable acids include hydrochloric acid, sulfuric acid,
phosphoric acid, nitric acid, and/or maleic acid. In some
embodiments, a base may be added to the feed stream to increase the
pH of the stream. Non-limiting examples of suitable bases include
caustic soda, potassium hydroxide, carbon dioxide, calcium
hydroxide (e.g., lime), and/or calcium oxide (e.g., quicklime).
[0108] In some embodiments, the pH adjustment apparatus comprises
one or more reaction tanks The reaction tanks may be configured to
facilitate the reaction of an aqueous stream and one or more
reagents (e.g., a pH adjustment composition). In some cases, for
example, one or more reaction tanks comprise a pH adjustment
composition inlet and/or an agitator. In some cases, one or more
reaction tanks comprise one or more pH sensors. In certain
embodiments, one or more reaction tanks may comprise two or more pH
sensors. In certain cases, the pH adjustment apparatus may further
comprise a pH adjustment composition tank fluidically connected
(e.g., directly fluidically connected) to one or more reaction
tanks The pH adjustment composition tank may, for example, be
configured to contain an amount of the pH adjustment composition.
In some cases, the pH adjustment composition may comprise an acid
(e.g., a strong acid) or a base (e.g., a strong base) having a
relatively high concentration. In some cases, the pH adjustment
composition tank may be a double-walled tank. It may be
advantageous, in some cases, for the pH adjustment composition tank
to be double-walled to reduce the risk of injury in the case of a
leak. For example, a leak in a first wall of a double-walled tank
may be contained by the second wall of the double-walled tank. In
some cases, the pH adjustment system further comprises a vapor
containment system fluidically connected to the pH adjustment
composition tank. In some cases, the vapor containment system may
comprise a water-containing tank. In certain cases, the
water-containing tank may comprise an amount of water, and vapor
from the pH adjustment composition tank may be bubbled through the
water of the water-containing tank. The pH adjustment apparatus may
further comprise one or more conduits connecting various components
of the pH adjustment apparatus. In some cases, one or more conduits
(e.g., conduits connecting the pH adjustment composition tank and
one or more reaction tanks) may be double-walled.
[0109] A schematic diagram of an exemplary pH adjustment apparatus
is shown in FIG. 5. In FIG. 5, pH adjustment apparatus 500
comprises first reaction tank 502, second reaction tank 504, pH
adjustment composition tank 506, and water-containing tank 508. In
some cases, pH adjustment composition tank 506 may be a
double-walled tank, a first conduit fluidically connecting pH
adjustment composition tank 506 and first reaction tank 502 may be
a double-walled pipe, and a second conduit fluidically connecting
pH adjustment composition tank 506 and second reaction tank 504 may
be a double-walled pipe. In some cases, first reaction tank 502
and/or second reaction tank 504 may comprise an agitator and/or at
least one pH sensor.
[0110] In some embodiments, a first amount of pH-adjusting
composition stream 234 is added to aqueous input stream 222 in
first reaction tank 502 to form stream 510. Stream 510 may be
directed to flow to second reaction tank 504, where a second amount
of pH-adjusting composition stream 234 may be added to stream 510.
It should be noted that in some cases, a first pH-adjusting
composition may be added to first reaction tank 502, and a second,
different pH-adjusting composition may be added to second reaction
tank 504. After an amount of a pH-adjusting composition has been
added to stream 510 in second reaction tank 504, the stream may be
directed to exit the pH adjustment apparatus as pH-adjusted stream
224.
[0111] In some cases, vapor from pH adjustment composition tank 506
is bubbled through water-containing tank 508 due to the volatility
of the pH-adjusting composition. In certain embodiments, as the pH
of the water in tank 508 is decreased (e.g., the water becomes more
acidic) or increased (e.g., the water becomes more basic), the
water is directed to flow to first reaction tank 502 for pH
adjustment.
[0112] The pH adjustment apparatus may be fluidically connected to
one or more other unit operations of the clean brine system, either
directly or indirectly. In some embodiments, the pH adjustment
apparatus may be fluidically connected to a VOM removal apparatus.
For example, in FIG. 2A, pH adjustment apparatus 208 is directly
fluidically connected to optional VOM removal apparatus 210 via
stream 224. In some embodiments, the pH adjustment apparatus is
fluidically connected to a filtration apparatus (e.g., a filter
press, a vacuum filter). For example, in FIG. 2A, pH adjustment
apparatus 208 is fluidically connected to optional filtration
apparatus 212 via streams 222 and 228.
[0113] In some embodiments, the pH adjustment apparatus is directly
fluidically connected to a VOM removal apparatus. For example, in
FIG. 2A, pH adjustment apparatus 208 is directly fluidically
connected to VOM removal apparatus 210, described in more detail
below, via stream 224. It should be understood that the invention
is not limited to embodiments in which the pH adjustment apparatus
is directly fluidically connected to a VOM removal apparatus, and
in some embodiments, the pH adjustment apparatus can be directly
fluidically connected to one or more other unit operations. In some
embodiments, the pH adjustment apparatus is directly fluidically
connected to a separation apparatus. In some embodiments, the pH
adjustment apparatus is directly fluidically connected to an
ion-removal apparatus. In some embodiments, the pH adjustment
apparatus is directly fluidically connected to a suspended solids
removal apparatus. In some embodiments, the pH adjustment apparatus
is directly fluidically connected to a filtration apparatus,
described in more detail below.
[0114] In certain embodiments, the water treatment system comprises
an optional volatile organic material (VOM) removal apparatus. The
VOM removal apparatus can be configured to remove at least a
portion of VOM from an input stream received by the VOM removal
apparatus to produce a VOM-diminished stream. Generally, the
VOM-diminished stream contains VOM in an amount that is less that
the amount of VOM in the input stream received by the VOM removal
apparatus.
[0115] In certain embodiments, the volatile organic material has a
boiling point of less than or equal to 450.degree. C. at 1
atmosphere. VOM includes volatile organic compounds (VOCs) and
semi-volatile organic compounds (SVOCs). Examples of VOCs that can
be at least partially removed by the VOM removal apparatus include,
but are not limited to, acetone; 1,1,1,2-tetrachloroethane;
1,1,1-trichloroethane; 1,1,2,2-tetrachloroethane;
1,1,2-trichloroethane; 1,1-dichloroethane; 1,1-dichloroethene;
1,1-dichloropropene; 1,2,3-trichlorobenzene;
1,2,3-trichloropropane; 1,2,4-trichlorobenzene;
1,2,4-trimethylbenzene; 1,2-dibromo-3-chloropropane;
1,2-dibromoethane; 1,2-dichlorobenzene; 1,2-dichloroethane;
1,2-dichloropropane; 1,3,5-trimethylbenzene; 1,3-dichlorobenzene;
1,3-dichloropropane; 1,4-dichlorobenzene; 2,2-dichloropropane;
2-butanone; 2-chloroethyl vinyl ether; 2-chlorotoluene; 2-hexanone;
4-chlorotoluene; 4-methyl-2-pentanone; benzene; bromobenzene;
bromochloromethane; bromodichloromethane; bromoform; carbon
disulfide; carbon tetrachloride; chlorobenzene; chloroethane;
chloroform; cis-1,2-dichloroethene; cis-1,3-dichloropropene;
dibromochloromethane; dibromomethane; dichlorodifluoromethane;
ethylbenzene; hexachlorobutadiene; isopropylbenzene; m-xylenes;
p-xylenes; bromomethane; chloromethane; methylene chloride;
n-butylbenzene; n-propylbenzene; naphthalene; o-xylene;
p-Isopropyltoluene; sec-butylbenzene; styrene; tert-butylbenzene;
tetrachloroethene; toluene; trans-1,2-dichloroethene;
trans-1,3-dichloropropene; trichloroethene; trichlorofluoromethane;
vinyl acetate; and vinyl chloride. Examples of SVOCs that can be at
least partially removed by the VOM removal apparatus include, but
are not limited to, 2,4,5-trichlorophenol; 2,4,6-trichlorophenol;
2,4-dichlorophenol; 2,4-dimethylphenol; 2,4-dinitrophenol;
2,4-dinitrotoluene; 2,6-dinitrotoluene; 2-chloronaphthalene;
2-chlorophenol; 2-methylnaphthalene; 2-methylphenol;
2-nitroaniline; 2-nitrophenol; 3,3'-dichlorobenzidine;
3-nitroaniline; 4,6-dinitro-2-methylphenol; 4-bromophenyl phenyl
ether; 4-chloro-3-methylphenol; 4-chloroaniline; 4-chlorophenyl
phenyl ether; 3 & 4-methylphenol; 4-nitroaniline;
4-nitrophenol; acenaphthene; acenaphthylene; anthracene;
benzo(a)anthracene; benzo(a)pyrene; benzo(b)fluoranthene;
benzo(g,h,i)perylene; benzo(k)fluoranthene; benzoic acid; benzyl
alcohol; bis(2-chloroethoxy)methane; bis(2-chloroethyl)ether;
bis(2-chloroisopropyl)ether; bis(2-ethylhexyl)phthalate; butyl
benzyl phthalate; chrysene; di-n-butyl phthalate; di-n-octyl
phthalate; dibenz(a,h)anthracene; dibenzofuran; diethyl phthalate;
dimethyl phthalate; fluoranthene; fluorene; hexachlorobenzene;
[0116] hexachlorocyclopentadiene; hexachloroethane;
indeno(1,2,3-cd)pyrene; isophorone; n-nitroso-di-n-propylamine;
n-nitrosodiphenylamine; nitrobenzene; pentachlorophenol;
phenanthrene; phenol; and pyrene.
[0117] Referring back to FIG. 2A, clean brine system 102 comprises
optional VOM removal apparatus 210. VOM removal apparatus 210 can
be configured to remove at least a portion of VOM from input stream
224 received by VOM removal apparatus 210 to produce a
VOM-diminished stream 108, which contains less of the VOM relative
to input stream 224 received by VOM removal apparatus 210. The VOM
removal apparatus can also produce a stream that is enriched in VOM
relative to the stream fed to the VOM removal apparatus. For
example, in FIG. 2A, VOM removal apparatus 210 can be configured to
produce stream 226, which is enriched in VOM relative to stream
224.
[0118] In certain embodiments, the VOM removal apparatus is
configured to remove a relatively large percentage of the VOM from
the stream fed to the VOM removal apparatus. For example, in some
embodiments, the amount (in weight percentage, wt %) of at least
one VOM within the stream exiting the VOM removal apparatus (e.g.,
stream 108 in FIG. 2) is at least about 50%, at least about 75%, at
least about 90%, at least about 95%, or at least about 99% less
than the amount of the at least one VOM within the stream entering
the VOM removal apparatus (e.g., stream 224 in FIG. 2). In certain
embodiments, the sum of the amounts of all VOM within the stream
exiting the VOM removal apparatus is at least about 50%, at least
about 75%, at least about 90%, at least about 95%, or at least
about 99% less than the sum of the amounts of all VOM within the
stream entering the VOM removal apparatus.
[0119] In some embodiments, the VOM removal apparatus does not
include any sources of thermal energy. For example, according to
certain embodiments, the VOM removal apparatus does not include any
steam input streams.
[0120] The VOM removal apparatus may be fluidically connected to
one or more other unit operations of the water treatment apparatus,
either directly or indirectly. In certain embodiments, the VOM
removal apparatus may also be, in certain embodiments, fluidically
connected to an optional separation apparatus. For example, in FIG.
2A, VOM removal apparatus 210 is fluidically connected to optional
separation apparatus 202 via streams 214, 218, 222, and 224. The
VOM removal apparatus may be, in some embodiments, fluidically
connected to an optional ion-removal apparatus. For example, in
FIG. 2A, VOM removal apparatus 210 is fluidically connected to
optional ion-removal apparatus 204 via streams 218, 222, and 224.
In some embodiments, the VOM removal apparatus may be fluidically
connected to an optional suspended solids removal apparatus. For
example, in FIG. 2A, VOM removal apparatus 210 is fluidically
connected to suspended solids removal apparatus 206 via streams 222
and 224. In certain embodiments, the VOM removal apparatus may be
fluidically connected to an optional pH adjustment apparatus. For
example, in FIG. 2A, VOM removal apparatus 210 is fluidically
connected to optional pH reduction apparatus 208 via stream 224. In
some embodiments, the VOM removal apparatus may be fluidically
connected to an optional filtration apparatus (e.g., a filter
press, a vacuum filter). For example, in FIG. 2A, VOM removal
apparatus 210 is fluidically connected to optional filtration
apparatus 212 via streams 222, 224, and 228.
[0121] In some embodiments, the VOM removal apparatus can be
directly fluidically connected to a pH adjustment apparatus. For
example, in FIG. 2A, VOM removal apparatus 210 is directly
fluidically connected to pH reduction apparatus 208 via stream 224.
In some embodiments, the VOM removal apparatus can be directly
fluidically connected to one or more other unit operations. In some
embodiments, the VOM removal apparatus is directly fluidically
connected to a separation apparatus. In some embodiments, the VOM
removal apparatus is directly fluidically connected to an
ion-removal apparatus. In some embodiments, the VOM removal
apparatus is directly fluidically connected to a suspended solids
removal apparatus. In some embodiments, the VOM removal apparatus
is directly fluidically connected to a filtration apparatus.
[0122] A variety of types of VOM removal apparatuses may be used in
the embodiments described herein. In some embodiments, the VOM
removal apparatus comprises a carbon bed filter and/or an air
stripper. In some embodiments, the air stripper comprises a packed
bed stripper, a low-profile air stripper, and/or an aeration
stripper. In certain embodiments, the carbon bed comprises
activated carbon.
[0123] According to some embodiments, the VOM removal apparatus is
configured to remove at least a portion of VOM from at least
partially desalinated water. For example, in some embodiments, the
input stream received by the VOM removal apparatus comprises at
least a portion of a water-containing stream produced by the
desalination system that contains a lower concentration of the
dissolved salt than the stream received by the desalination system,
as described in more detail below.
[0124] According to some embodiments, the clean brine system
comprises an optional filtration apparatus. In some embodiments,
the filtration apparatus may be configured to remove at least a
portion of water from a solid-containing stream to form a
substantially solid material and a filtered liquid stream. The
substantially solid material may, in some cases, comprise at least
a portion of a precipitated salt (e.g., a monovalent salt, a
divalent salt). In certain embodiments, the substantially solid
material may be a filter cake. In some embodiments, the filter cake
may comprise a plurality of solid particles, wherein at least a
portion of the solid particles are in direct contact with another
solid particle. In certain cases, at least about 60%, at least
about 70%, at least about 80%, at least about 90%, at least about
95%, or at least about 99% of the solid particles in the filter
cake are in direct contact with another solid particle. In some
cases, the filter cake has a relatively low liquid content. In some
embodiments, the filter cake has a liquid content of about 90 wt %
or less, about 85 wt % or less, about 80 wt % or less, about 75 wt
% or less, about 70 wt % or less, about 65 wt % or less, about 60
wt % or less, about 55 wt % or less, about 50 wt % or less, about
40 wt % or less, about 30 wt % or less, about 25 wt % or less,
about 20 wt % or less, about 15 wt % or less, or about 10 wt % or
less. In certain embodiments, the filter cake has a liquid content
in the range of about 10 wt % to about 90 wt %, about 10 wt % to
about 85 wt %, about 10 wt % to about 80 wt %, about 10 wt % to
about 75 wt %, about 10 wt % to about 70 wt %, about 10 wt % to
about 60 wt %, about 10 wt % to about 55 wt %, about 10 wt % to
about 50 wt %, about 10 wt % to about 40 wt %, about 10 wt % to
about 30 wt %, or about 10 wt % to about 20 wt %.
[0125] In some cases, the filtration apparatus comprises a filter
(e.g., a vacuum drum filter or a filter press) configured to at
least partially separate a precipitated salt from the remainder of
a suspension containing the precipitated salt. In some such
embodiments, at least a portion of the liquid within the
solid-containing stream can be transported through the filter,
leaving behind solid precipitated salt (e.g., a filter cake). As
one non-limiting example, a Larox FP 2016-8000 64/64 M40 PP/PP
Filter (Outotec, Inc.) may be used as the filter. The filter may
comprise, in certain embodiments, a conveyor filter belt which
filters the salt from a suspension containing the salt. In some
cases, for example, the filtration apparatus may be fluidically
connected (e.g., directly fluidically connected) to the suspended
solids removal apparatus. For example, in certain embodiments, a
solid-containing stream may be flowed (e.g., pumped) from the
suspended solids removal apparatus (e.g., a clarifier) to the
filtration apparatus.
[0126] In some embodiments, a solid-containing stream from the
suspended solids removal apparatus may be pumped to the filtration
apparatus by one or more pumps (e.g., air diaphragm pumps). In
certain embodiments, the one or more pumps may initially pump at a
relatively low pressure and may automatically increase the pressure
as flow rate drops due to collection of solids in the filtration
apparatus. In some cases, such a process may be advantageous. For
example, in embodiments where the filtration apparatus comprises
one or more filter presses, such a process may advantageously
reduce filter cloth blinding (e.g., embedding of particles in a
filter cloth) and result in formation of more consistent filter
cakes. In certain cases, a liquid component of the solid-containing
stream may be rejoined with other liquid streams in the clean brine
system after passing through the filtration apparatus.
[0127] In some cases, one or more buffer tanks may be positioned
between the suspended solids removal apparatus and the filtration
apparatus. The presence of one or more buffer tanks between the
suspended solids removal apparatus and the filtration apparatus
may, in some cases, advantageously provide buffer volume in the
event that components of the filtration apparatus (e.g., one or
more filter presses) are undergoing a cleaning cycle.
[0128] In some cases, a component of the filtration apparatus
(e.g., a filter press) may undergo a cleaning cycle when it is
full. In certain cases, a filtration apparatus component may be
considered to be full when the flow rate drops below a threshold
level at a certain pumping pressure. In certain cases, when a
filtration apparatus undergoes a cleaning cycle, flow may be
rerouted to one or more buffer tanks to continue fluid circulation
and prevent solid buildup. In some cases, the cleaning cycle begins
by pumping clean brine into the filtration apparatus component to
flush out soft filter cake. The filtration apparatus component may
then be blown down. In some cases, the filter cake may be dried.
For example, in certain cases, the filter cake may be air dried by
blowing compressed air through the cake. It may be advantageous in
some cases for the filter cake to be air dried in order to reduce
its liquid content. In some cases, compacted filter cake may be
stored and/or disposed (e.g., in a dumpster).
[0129] According to certain embodiments, substantially solid
material (e.g., filter cake) produced in a clean brine system may
be used to form a brine solution having a density of at least about
9 pounds/gallon. In some cases, substantially solid material
produced in a clean brine system may be used to form an
ultra-high-density brine solution (e.g., a brine solution having a
density of at least about 11.7 pounds/gallon). In certain
embodiments, the brine solution has a density (e.g., measured at
about 60.degree. F.) of at least about 9 pounds/gallon, at least
about 9.5 pounds/gallon, at least about 10 pounds/gallon, at least
about 10.5 pounds/gallon, at least about 11 pounds/gallon, at least
about 11.5 pounds/gallon, at least about 11.7 pounds/gallon, at
least about 11.8 pounds/gallon, at least about 12 pounds/gallon, at
least about 12.5 pounds/gallon, at least about 13 pounds/gallon, at
least about 13.2 pounds/gallon, at least about 13.5 pounds/gallon,
at least about 14 pounds/gallon, at least about 14.5 pounds/gallon,
or at least about 15 pounds/gallon. In some embodiments, the brine
solution has a density (e.g., measured at about 60.degree. F.) in
the range of about 9 pounds/gallon to about 9.5 pounds/gallon,
about 9 pounds/gallon to about 10 pounds/gallon, about 9
pounds/gallon to about 10.5 pounds/gallon, about 9 pounds/gallon to
about 11 pounds/gallon, about 9 pounds/gallon to about 11.7
pounds/gallon, about 9 pounds/gallon to about 11.8 pounds/gallon,
about 9 pounds/gallon to about 12 pounds/gallon, about 9
pounds/gallon to about 12.5 pounds/gallon, about 9 pounds/gallon to
about 13 pounds/gallon, about 9 pounds/gallon to about 13.2
pounds/gallon, about 9 pounds/gallon to about 13.5 pounds/gallon,
about 9 pounds/gallon to about 14 pounds/gallon, about 9
pounds/gallon to about 14.5 pounds/gallon, about 9 pounds/gallon to
about 15 pounds/gallon, about 9.5 pounds/gallon to about 11.8
pounds/gallon, about 10 pounds/gallon to about 11 pounds/gallon,
about 10 pounds/gallon to about 11.7 pounds/gallon, about 10
pounds/gallon to about 11.8 pounds/gallon, about 10 pounds/gallon
to about 12 pounds/gallon, about 10 pounds/gallon to about 12.5
pounds/gallon, about 10 pounds/gallon to about 13 pounds/gallon,
about 10 pounds/gallon to about 13.2 pounds/gallon, about 10
pounds/gallon to about 13.5 pounds/gallon, about 10 pounds/gallon
to about 14 pounds/gallon, about 10 pounds/gallon to about 14.5
pounds/gallon, about 10 pounds/gallon to about 15 pounds/gallon,
about 10.5 pounds/gallon to about 11.8 pounds/gallon, about 11
pounds/gallon to about 11.7 pounds/gallon, about 11 pounds/gallon
to about 11.8 pounds/gallon, about 11 pounds/gallon to about 12
pounds/gallon, about 11 pounds/gallon to about 12.5 pounds/gallon,
about 11 pounds/gallon to about 13 pounds/gallon, about 11
pounds/gallon to about 13.2 pounds/gallon, about 11 pounds/gallon
to about 13.5 pounds/gallon, about 11 pounds/gallon to about 14
pounds/gallon, about 11 pounds/gallon to about 14.5 pounds/gallon,
about 11 pounds/gallon to about 15 pounds/gallon, about 11.7
pounds/gallon to about 12 pounds/gallon, about 11.7 pounds/gallon
to about 12.5 pounds/gallon, about 11.7 pounds/gallon to about 13
pounds/gallon, about 11.7 pounds/gallon to about 13.2
pounds/gallon, about 11.7 pounds/gallon to about 13.5
pounds/gallon, about 11.7 pounds/gallon to about 14 pounds/gallon,
about 11.7 pounds/gallon to about 14.5 pounds/gallon, about 11.7
pounds/gallon to about 15 pounds/gallon, about 12 pounds/gallon to
about 12.5 pounds/gallon, about 12 pounds/gallon to about 13
pounds/gallon, about 12 pounds/gallon to about 13.2 pounds/gallon,
about 12 pounds/gallon to about 13.5 pounds/gallon, about 12
pounds/gallon to about 14 pounds/gallon, about 12 pounds/gallon to
about 14.5 pounds/gallon, about 12 pounds/gallon to about 15
pounds/gallon, about 13 pounds/gallon to about 14 pounds/gallon,
about 13 pounds/gallon to about 14.5 pounds/gallon, about 13
pounds/gallon to about 15 pounds/gallon, or about 14 pounds/gallon
to about 15 pounds/gallon.
[0130] In some cases, the density of the brine solution is measured
at a temperature of about 120.degree. F. or less, about 100.degree.
F. or less, about 80.degree. F. or less, about 72.degree. F. or
less, about 68.degree. F. or less, about 60.degree. F. or less,
about 50.degree. F. or less, or about 40.degree. F. or less. In
some embodiments, the density of the brine solution is measured at
a temperature of at least about 40.degree. F., at least about
50.degree. F., at least about 60.degree. F., at least about
68.degree. F., at least about 72.degree. F., at least about
80.degree. F., at least about 100.degree. F., or at least about
120.degree. F. In some embodiments, the density of the brine
solution is measured at a temperature in the range of about
40.degree. F. to about 120.degree. F., about 40.degree. F. to about
100.degree. F., about 40.degree. F. to about 80.degree. F., about
40.degree. F. to about 72.degree. F., about 40.degree. F. to about
68.degree. F., about 40.degree. F. to about 60.degree. F., about
40.degree. F. to about 50.degree. F., about 60.degree. F. to about
120.degree. F., about 60.degree. F. to about 100.degree. F., about
60.degree. F. to about 80.degree. F., about 60.degree. F. to about
72.degree. F., or about 60.degree. F. to about 68.degree. F.
[0131] In some cases, the brine solution comprises one or more
dissolved salts. Non-limiting examples of suitable dissolved salts
include sodium chloride (NaCl), calcium chloride (CaCl.sub.2),
and/or calcium nitrate (Ca(NO.sub.3).sub.2). In some cases, the
brine solution has a concentration of at least one dissolved salt
of at least about 10,000 mg/L, at least about 50,000 mg/L, at least
about 80,000 mg/L, at least about 85,000 mg/L, at least about
90,000 mg/L, at least about 100,000 mg/L, at least about 150,000
mg/L, at least about 180,000 mg/L, at least about 200,000 mg/L, at
least about 250,000 mg/L, at least about 270,000 mg/L, at least
about 300,000 mg/L, at least about 350,000 mg/L, at least about
380,000 mg/L, at least about 400,000 mg/L, at least about 450,000
mg/L, at least about 480,000 mg/L, or at least about 500,000 mg/L.
In some embodiments, the brine solution has a concentration of at
least one dissolved salt in the range of about 10,000 mg/L to about
500,000 mg/L, about 50,000 mg/L to about 500,000 mg/L, about 80,000
mg/L to about 500,000 mg/L, about 85,000 mg/L to about 500,000
mg/L, about 90,000 mg/L to about 500,000 mg/L, about 100,000 mg/L
to about 500,000 mg/L, about 150,000 mg/L to about 500,000 mg/L,
about 180,000 mg/L to about 500,000 mg/L, about 200,000 mg/L to
about 500,000 mg/L, about 250,000 mg/L to about 500,000 mg/L, about
280,000 mg/L to about 500,000 mg/L, about 300,000 mg/L to about
500,000 mg/L, about 350,000 mg/L to about 500,000 mg/L, about
380,000 mg/L to about 500,000 mg/L, about 400,000 mg/L to about
500,000 mg/L, or about 450,000 mg/L to about 500,000 mg/L. The
concentration of a dissolved salt generally refers to the combined
concentrations of the cation and anion of the salt. For example,
the concentration of dissolved NaCl would refer to the
concentration of sodium ions (Na.sup.+) in addition to the
concentration of chloride ions (CO. The concentration of a
dissolved salt may be measured according to any method known in the
art. For example, suitable methods for measuring the concentration
of a dissolved salt include inductively coupled plasma (ICP)
spectroscopy (e.g., inductively coupled plasma optical emission
spectroscopy). As one non-limiting example, an Optima 8300 ICP-OES
spectrometer may be used.
[0132] In some cases, the brine solution has a total dissolved salt
concentration of at least about 50,000 mg/L, at least about 80,000
mg/L, at least about 85,000 mg/L, at least about 90,000 mg/L, at
least about 100,000 mg/L, at least about 150,000 mg/L, at least
about 180,000 mg/L, at least about 200,000 mg/L, at least about
250,000 mg/L, at least about 270,000 mg/L, at least about 300,000
mg/L, at least about 350,000 mg/L, at least about 380,000 mg/L, at
least about 400,000 mg/L, at least about 450,000 mg/L, at least
about 480,000 mg/L, or at least about 500,000 mg/L. In some
embodiments, the brine solution has a total dissolved salt
concentration in the range of about 50,000 mg/L to about 500,000
mg/L, about 80,000 mg/L to about 500,000 mg/L, about 85,000 mg/L to
about 500,000 mg/L, about 90,000 mg/L to about 500,000 mg/L, about
100,000 mg/L to about 500,000 mg/L, about 150,000 mg/L to about
500,000 mg/L, about 180,000 mg/L to about 500,000 mg/L, about
200,000 mg/L to about 500,000 mg/L, about 250,000 mg/L to about
500,000 mg/L, about 280,000 mg/L to about 500,000 mg/L, about
300,000 mg/L to about 500,000 mg/L, about 350,000 mg/L to about
500,000 mg/L, about 380,000 mg/L to about 500,000 mg/L, about
400,000 mg/L to about 500,000 mg/L, or about 450,000 mg/L to about
500,000 mg/L. The total dissolved salt concentration generally
refers to the combined concentrations of all the cations and anions
of dissolved salts that are present. As a simple, non-limiting
example, in a water stream comprising dissolved NaCl and dissolved
MgSO.sub.4, the total dissolved salt concentration would refer to
the total concentrations of the Na.sup.+, Cl.sup.-, Mg.sup.2+, and
SO.sub.4.sup.2- ions. Total dissolved salt concentration may be
measured according to any method known in the art. For example, a
non-limiting example of a suitable method for measuring total
dissolved salt concentration is the SM 2540C method. According to
the SM 2540C method, a sample comprising an amount of liquid
comprising one or more dissolved solids is filtered (e.g., through
a glass fiber filter), and the filtrate is evaporated to dryness in
a weighed dish at 180.degree. C. The increase in dish weight
represents the mass of the total dissolved solids in the sample.
The total dissolved salt concentration of the sample may be
obtained by dividing the mass of the total dissolved solids by the
volume of the original sample.
[0133] In certain embodiments, the brine solution may be formed by
adding an amount of one or more acids to at least a portion of the
substantially solid material. Non-limiting examples of suitable
acids include hydrochloric acid (HCl) and nitric acid
(HNO.sub.3).
[0134] In a particular embodiment, at least a portion of the
substantially solid material formed in a clean brine system may
comprise calcium carbonate (CaCO.sub.3). According to some
embodiments, a concentrated brine comprising dissolved calcium
chloride (CaCl.sub.2) may be produced by adding an amount of
hydrochloric acid to the substantially solid material from the
clean brine system. The addition of hydrochloric acid may, in some
cases, result in the production of aqueous calcium chloride, water,
and CO.sub.2 (which separates from the aqueous CaCl.sub.2 and
H.sub.2O). In some cases, a brine solution comprising dissolved
CaCl.sub.2 may be formed. In some embodiments, addition of nitric
acid to a substantially solid material comprising calcium carbonate
can produce a brine solution (e.g., an ultra-high-density brine
solution) comprising dissolved calcium nitrate
(Ca(NO.sub.3).sub.2).
[0135] According to some embodiments, the water content of the
substantially solid material may be decreased prior to addition of
an acid. For example, in some cases, the substantially solid
material may be dried prior to addition of an acid. In certain
cases, the substantially solid material may be air dried (e.g, via
compressed air in a filter press) prior to addition of the acid. In
some cases, reducing the water content of the substantially solid
material prior to addition of the acid may advantageously increase
the density of the resultant brine solution.
[0136] In some embodiments, an amount of a salt may be added to a
brine solution and dissolved in the brine solution. In some cases,
addition of the additional salt may further increase the density of
the brine solution. Non-limiting examples of suitable salts include
sodium chloride (NaCl), calcium chloride (CaCl.sub.2), magnesium
chloride (MgCl.sub.2), copper (II) chloride (CuCl.sub.2), iron
(III) chloride hexahydrate (FeCl.sub.3.6H.sub.2O), iron (III)
chloride (FeCl.sub.3), lithium chloride (LiCl), manganese (II)
chloride (MnCl.sub.2), nickel (II) chloride (NiCl.sub.2), zinc
chloride (ZnCl.sub.2), calcium bromide (CaBr.sub.2), magnesium
bromide (MgBr.sub.2), potassium bromide (KBr), sodium bromide
(NaBr), copper (II) bromide (CuBr.sub.2), iron (III) bromide
(FeBr.sub.3), lithium bromide (LiBr), manganese (II) bromide
(MnBr.sub.2), nickel (II) bromide (NiBr.sub.2), zinc bromide
(ZnBr.sub.2), ammonium nitrate (NH.sub.4NO.sub.3), sodium nitrate
(NaNO.sub.3), lithium nitrate (LiNO.sub.3), calcium nitrate
(Ca(NO.sub.3).sub.2), magnesium nitrate (Mg(NO.sub.3).sub.2),
strontium nitrate (Sr(NO.sub.3).sub.2), calcium nitrate
tetrahydrate (Ca(NO.sub.3).sub.2.4H.sub.2O), copper (II) nitrate
(Cu(NO.sub.3).sub.2), iron (II) nitrate (Fe(NO.sub.3).sub.2), iron
(III) nitrate (Fe(NO.sub.3).sub.3), nickel (II) nitrate
(Ni(NO.sub.3).sub.2), and/or zinc nitrate (Zn(NO.sub.3).sub.2). In
some embodiments, at least one of the one or more additional salts
added to a brine solution comprising water and at least one
dissolved salt is different from the at least one dissolved salt.
In some embodiments, each of the one or more additional salts added
to the brine solution is different from the at least one dissolved
salt. In certain cases, at least one of the one or more additional
salts added to the brine solution is the same as the at least one
dissolved salt.
[0137] In certain embodiments, the brine solution with additional
salt has a density (e.g., measured at about 60.degree. F.) of at
least about 11 pounds/gallon, at least about 11.5 pounds/gallon, at
least about 11.7 pounds/gallon, at least about 12 pounds/gallon, at
least about 12.5 pounds/gallon, at least about 13 pounds/gallon, at
least about 13.2 pounds/gallon, at least about 13.5 pounds/gallon,
at least about 14 pounds/gallon, at least about 14.5 pounds/gallon,
at least about 15 pounds/gallon, at least about 20 pounds/gallon,
or at least about 25 pounds/gallon. In certain cases, the brine
solution with additional salt has a density (e.g., measured at
about 60.degree. F.) in the range of about 11 pounds/gallon to
about 12 pounds/gallon, about 11 pounds/ per gallon to about 12.5
pounds/gallon, about 11 pounds/gallon to about 13 pounds/gallon,
about 11 pounds/gallon to about 13.2 pounds/gallon, about 11
pounds/gallon to about 13.5 pounds/gallon, about 11 pounds/gallon
to about 14 pounds/gallon, about 11 pounds/gallon to about 14.5
pounds/gallon, about 11 pounds/gallon to about 15 pounds/gallon,
about 11 pounds/gallon to about 20 pounds/gallon, about 11
pounds/gallon to about 25 pounds/gallon, about 11.5 pounds/gallon
to about 12 pounds/gallon, about 11.5 pounds/gallon to about 12.5
pounds/gallon, about 11.5 pounds/gallon to about 13 pounds/gallon,
about 11.5 pounds/gallon to about 13.2 pounds/gallon, about 11.5
pounds/gallon to about 13.5 pounds/gallon, about 11.5 pounds/gallon
to about 14 pounds/gallon, about 11.5 pounds/gallon to about 14.5
pounds/gallon, about 11.5 pounds/gallon to about 15 pounds/gallon,
about 11.5 pounds/gallon to about 20 pounds/gallon, about 11.5
pounds/gallon to about 25 pounds/gallon, about 11.7 pounds/gallon
to about 12.5 pounds/gallon, about 11.7 pounds/gallon to about 13
pounds/gallon, about 11.7 pounds/gallon to about 13.2
pounds/gallon, about 11.7 pounds/gallon to about 13.5
pounds/gallon, about 11.7 pounds/gallon to about 14 pounds/gallon,
about 11.7 pounds/gallon to about 14.5 pounds/gallon, about 11.7
pounds/gallon to about 15 pounds/gallon, about 11.7 pounds/gallon
to about 20 pounds/gallon, about 11.7 pounds/gallon to about 25
pounds/gallon, or about 12 pounds/gallon to about 12.5
pounds/gallon, about 12 pounds/gallon to about 13 pounds/gallon,
about 12 pounds/gallon to about 13.2 pounds/gallon, about 12
pounds/gallon to about 13.5 pounds/gallon, about 12 pounds/gallon
to about 14 pounds/gallon, about 12 pounds/gallon to about 14.5
pounds/gallon, about 12 pounds/gallon to about 15 pounds/gallon,
about 12 pounds/gallon to about 20 pounds/gallon, about 12
pounds/gallon to about 25 pounds/gallon, about 13 pounds/gallon to
about 13.5 pounds/gallon, about 13 pounds/gallon to about 14
pounds/gallon, about 13 pounds/gallon to about 14.5 pounds/gallon,
about 13 pounds/gallon to about 15 pounds/gallon, about 13
pounds/gallon to about 20 pounds/gallon, about 13 pounds/gallon to
about 25 pounds/gallon, about 14 pounds/gallon to about 15
pounds/gallon, about 14 pounds/gallon to about 20 pounds/gallon,
about 14 pounds/gallon to about 25 pounds/gallon, about 15
pounds/gallon to about 20 pounds/gallon, about 15 pounds/gallon to
about 25 pounds/gallon, or about 20 pounds/gallon to about 25
pounds/gallon.
[0138] In some cases, the density of the brine solution with
additional salt is measured at a temperature of about 120.degree.
F. or less, about 100.degree. F. or less, about 80.degree. F. or
less, about 72.degree. F. or less, about 68.degree. F. or less,
about 60.degree. F. or less, about 50.degree. F. or less, or about
40.degree. F. or less. In some embodiments, the density of the
brine solution with additional salt is measured at a temperature of
at least about 40.degree. F., at least about 50.degree. F., at
least about 60 .degree. F., at least about 68.degree. F., at least
about 72.degree. F., at least about 80.degree. F., at least about
100.degree. F., or at least about 120.degree. F. In some
embodiments, the density of the brine solution with additional salt
is measured at a temperature in the range of about 40.degree. F. to
about 120.degree. F., about 40.degree. F. to about 100.degree. F.,
about 40.degree. F. to about 80.degree. F., about 40.degree. F. to
about 72.degree. F., about 40.degree. F. to about 68.degree. F.,
about 40.degree. F. to about 60.degree. F., about 40.degree. F. to
about 50.degree. F., about 60.degree. F. to about 120.degree. F.,
about 60.degree. F. to about 100.degree. F., about 60.degree. F. to
about 80.degree. F., about 60.degree. F. to about 72.degree. F., or
about 60.degree. F. to about 68.degree. F.
[0139] It may be advantageous, in certain cases, to form a brine
solution from the substantially solid material formed in the clean
brine system. In some cases, the brine solution may be used in
various applications (e.g., as a kill fluid in oil and gas
operations). In some embodiments, the formation of a brine solution
may avoid the expensive disposal of a solid material. According to
some embodiments, substantially no solid material is discharged
from the clean brine system. In certain cases, approximately about
70%, about 80%, about 90%, about 95%, about 99% or about 100% by
weight of the material discharged from the clean brine system is
substantially a liquid or a gas. In some embodiments, at least
about 70%, at least about 80%, at least about 90%, at least about
95%, at least about 99%, or about 100% by weight of the
substantially solid material is dissolved to form a brine solution.
In certain embodiments, substantially all of the substantially
solid material formed by the clean brine system is dissolved to
form a brine solution.
[0140] In some cases, CO.sub.2 resulting from the reaction of the
solid material and HCl may be collected. In some cases, the
CO.sub.2 may advantageously be used to increase the alkalinity of
an aqueous feed stream prior to the ion removal step, reducing the
amount of soda ash required. In some cases, the CO.sub.2 may be
used to decrease the pH of the feed stream prior to the pH
adjustment step, reducing the amount of additional acid (e.g., HCl)
required.
[0141] According to some embodiments, at least one component of the
clean brine system is fluidically connected to at least one storage
tank. A storage tank generally refers to any vessel (e.g.,
stainless steel tank or other vessel) that may be used to store a
liquid. The storage tank may have any shape (e.g, substantially
cylindrical, substantially rectangular prismatic, and the like) and
any size. In some embodiments, the storage tank may store an amount
of liquid (e.g., clean brine) until the liquid can be used in an
application (e.g., an oil or gas extraction process). In certain
cases, the storage tank may be fluidically connected (e.g.,
directly fluidically connected) to one or more water treatment
systems (e.g., a desalination system downstream of the clean brine
system).
[0142] In some embodiments, at least one storage tank is
fluidically connected to at least one component of the clean brine
system. In certain cases, at least one storage tank is directly
fluidically connected to at least one component of the clean brine
system. In certain embodiments, at least one storage tank is
fluidically connected to at least one component of the clean brine
system such that no intervening desalination system is fluidically
connected between the storage tank and the component. In certain
embodiments, at least one storage tank is fluidically connected to
at least one component of the clean brine system such that no
intervening precipitation apparatus (e.g., crystallization tank) is
fluidically connected between the storage tank and the component.
In some embodiments, at least one storage tank is fluidically
connected to at least one component of the clean brine system such
that no humidifier and/or dehumidifier is fluidically connected
between the storage tank and the component.
[0143] In some embodiments, at least one storage tank is
fluidically connected to a separation apparatus of the clean brine
system. In some cases, at least one storage tank is directly
fluidically connected to the separation apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the separation apparatus such that no intervening desalination
system is fluidically connected between the storage tank and the
separation apparatus. In some embodiments, at least one storage
tank is fluidically connected to the separation apparatus such that
no intervening precipitation apparatus (e.g., crystallization tank)
is fluidically connected between the storage tank and the
separation apparatus. In some embodiments, at least one storage
tank is fluidically connected to the separation apparatus such that
no humidifier and/or dehumidifier is fluidically connected between
the storage tank and the separation apparatus.
[0144] In some embodiments, at least one storage tank is
fluidically connected to an ion-removal apparatus of the clean
brine system. In some cases, at least one storage tank is directly
fluidically connected to the ion-removal apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the ion-removal apparatus such that no intervening desalination
system is fluidically connected between the storage tank and the
ion-removal apparatus. In some embodiments, at least one storage
tank is fluidically connected to the ion-removal apparatus such
that no intervening precipitation apparatus (e.g., crystallization
tank) is fluidically connected between the storage tank and the
ion-removal apparatus. In some embodiments, at least one storage
tank is fluidically connected to the ion-removal apparatus such
that no humidifier and/or dehumidifier is fluidically connected
between the storage tank and the ion-removal apparatus.
[0145] In some embodiments, at least one storage tank is
fluidically connected to a suspended solids removal apparatus of
the clean brine system. In some cases, at least one storage tank is
directly fluidically connected to the suspended solids removal
apparatus. In some embodiments, at least one storage tank is
fluidically connected to the suspended solids removal apparatus
such that no intervening desalination system is fluidically
connected between the storage tank and the suspended solids removal
apparatus. In some embodiments, at least one storage tank is
fluidically connected to the suspended solids removal apparatus
such that no intervening precipitation apparatus (e.g.,
crystallization tank) is fluidically connected between the storage
tank and the suspended solids removal apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the suspended solids removal apparatus such that no humidifier
and/or dehumidifier is fluidically connected between the storage
tank and the suspended solids removal apparatus.
[0146] In some embodiments, at least one storage tank is
fluidically connected to a pH adjustment apparatus of the clean
brine system. In some cases, at least one storage tank is directly
fluidically connected to the pH adjustment apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the pH adjustment apparatus such that no intervening desalination
system is fluidically connected between the storage tank and the pH
adjustment apparatus. In some embodiments, at least one storage
tank is fluidically connected to the pH adjustment apparatus such
that no intervening precipitation apparatus (e.g., crystallization
tank) is fluidically connected between the storage tank and the pH
adjustment apparatus. In some embodiments, at least one storage
tank is fluidically connected to the pH adjustment apparatus such
that no humidifier and/or dehumidifier is fluidically connected
between the storage tank and the pH adjustment apparatus.
[0147] In some embodiments, at least one storage tank is
fluidically connected to a VOM removal apparatus of the clean brine
system. In some cases, at least one storage tank is directly
fluidically connected to the VOM removal apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the VOM removal apparatus such that no intervening desalination
system is fluidically connected between the storage tank and the
VOM removal apparatus. In some embodiments, at least one storage
tank is fluidically connected to the VOM removal apparatus such
that no intervening precipitation apparatus (e.g., crystallization
tank) is fluidically connected between the storage tank and the VOM
removal apparatus. In some embodiments, at least one storage tank
is fluidically connected to the VOM removal apparatus such that no
humidifier and/or dehumidifier is fluidically connected between the
storage tank and the VOM removal apparatus.
[0148] In some embodiments, at least one storage tank is
fluidically connected to a filtration apparatus of the clean brine
system. In some cases, at least one storage tank is directly
fluidically connected to the filtration apparatus. In some
embodiments, at least one storage tank is fluidically connected to
the filtration apparatus such that no intervening desalination
system is fluidically connected between the storage tank and the
filtration apparatus. In some embodiments, at least one storage
tank is fluidically connected to the filtration apparatus such that
no intervening precipitation apparatus (e.g., crystallization tank)
is fluidically connected between the storage tank and the
filtration apparatus. In some embodiments, at least one storage
tank is fluidically connected to the filtration apparatus such that
no humidifier and/or dehumidifier is fluidically connected between
the storage tank and the filtration apparatus.
[0149] While separation apparatus 202, ion-removal apparatus 204,
suspended solids removal apparatus 206, pH adjustment apparatus
208, and VOM removal apparatus 210 are shown in FIG. 2A as being
arranged in a particular order, it should be understood that in
other embodiments, these components may be alternatively
arranged.
[0150] In certain embodiments, the input stream received by the
ion-removal apparatus comprises at least a portion of the
immiscible-phase-diminished stream produced by the separation
apparatus. That is to say, in certain embodiments, the ion-removal
apparatus can be located downstream of the separation apparatus.
Referring to FIG. 2A, ion-removal apparatus 204 receives at least a
portion of immiscible-phase-diminished stream 214 produced by
separation apparatus 202. In other embodiments, the input stream
received by the separation apparatus comprises at least a portion
of the ion-diminished stream produced by the ion-removal apparatus.
That is to say, in certain embodiments, the separation apparatus
can be located downstream of the ion-removal apparatus.
[0151] In some embodiments, for example, the input stream received
by the suspended solids removal apparatus comprises at least a
portion of the immiscible-phase-diminished stream produced by the
separation apparatus. That is to say, in certain embodiments, the
suspended solids removal apparatus can be located downstream of the
separation apparatus. Referring to FIG. 2A, for example, input
stream 218 received by suspended solids removal apparatus 206
comprises at least a portion of the immiscible-phase-diminished
stream (e.g., stream 214) produced by separation apparatus 202. In
other embodiments, the input stream received by the separation
apparatus comprises at least a portion of the
suspended-solids-diminished stream produced by the suspended solids
removal apparatus. That is to say, in certain embodiments, the
separation apparatus can be located downstream of the suspended
solids removal apparatus.
[0152] In certain embodiments, the input stream received by the pH
adjustment apparatus comprises at least a portion of the
immiscible-phase-diminished stream produced by the separation
apparatus. That is to say, in certain embodiments, the pH
adjustment apparatus can be located downstream of the separation
apparatus. Referring to FIG. 2A, for example, input stream 222
received by pH adjustment apparatus 208 comprises at least a
portion of immiscible-phase-diminished stream 214 produced by
separation apparatus 202. In other embodiments, the input stream
received by the separation apparatus comprises at least a portion
of the pH-adjusted stream produced by the pH adjustment apparatus.
That is to say, in certain embodiments, the separation apparatus
can be located downstream of the pH adjustment apparatus.
[0153] In some embodiments, the input stream received by the
volatile organic material (VOM) removal apparatus comprises at
least a portion of the immiscible-phase-diminished stream produced
by the separation apparatus. That is to say, in certain
embodiments, the VOM removal apparatus can be located downstream of
the separation apparatus. Referring to FIG. 2A, for example, input
stream 224 received by VOM removal apparatus 210 comprises at least
a portion of immiscible-phase-diminished stream 214 produced by
separation apparatus 202. In other embodiments, the input stream
received by the separation apparatus comprises at least a portion
of the VOM-diminished stream produced by the VOM removal apparatus.
That is to say, in certain embodiments, the separation apparatus
can be located downstream of the VOM removal apparatus.
[0154] In certain embodiments, the input stream received by the
suspended solids removal apparatus comprises at least a portion of
the ion-diminished stream produced by the ion-removal apparatus.
That is to say, in certain embodiments, the suspended solids
removal apparatus can be located downstream of the ion-removal
apparatus. Referring to FIG. 2A, for example, input stream 218
received by suspended solids removal apparatus 206 comprises at
least a portion of ion-diminished stream (also stream 218) produced
by ion-removal apparatus 204. In other embodiments, the input
stream received by the ion-removal apparatus comprises at least a
portion of the suspended-solids-diminished stream produced by the
suspended solids removal apparatus. That is to say, in certain
embodiments, the ion-removal apparatus can be located downstream of
the suspended solids removal apparatus.
[0155] In certain embodiments, the input stream received by the pH
adjustment apparatus comprises at least a portion of the
ion-diminished stream produced by the ion-removal apparatus. That
is to say, in certain embodiments, the pH adjustment apparatus can
be located downstream of the ion-removal apparatus. Referring to
FIG. 2A, for example, input stream 222 received by pH adjustment
apparatus 208 comprises at least a portion of ion-diminished stream
218 produced by ion-removal apparatus 204. In other embodiments,
the input stream received by the ion-removal apparatus comprises at
least a portion of the pH-adjusted stream produced by the pH
adjustment apparatus. That is to say, in certain embodiments, the
ion-removal apparatus can be located downstream of the pH
adjustment apparatus.
[0156] In some embodiments, the input stream received by the VOM
removal apparatus comprises at least a portion of the
ion-diminished stream produced by the ion-removal apparatus. That
is to say, in certain embodiments, the VOM removal apparatus can be
located downstream of the ion-removal apparatus. Referring to FIG.
2A, for example, input stream 224 received by VOM removal apparatus
210 comprises at least a portion of ion-diminished stream 218
produced by ion-removal apparatus 204. In other embodiments, the
input stream received by the ion-removal apparatus comprises at
least a portion of the VOM-diminished stream produced by the VOM
removal apparatus. That is to say, in certain embodiments, the
ion-removal apparatus can be located downstream of the VOM removal
apparatus.
[0157] In certain embodiments, the input stream received by the pH
adjustment apparatus comprises at least a portion of the
suspended-solids-diminished stream produced by the suspended solids
removal apparatus. That is to say, in certain embodiments, the pH
adjustment apparatus can be located downstream of the suspended
solids removal apparatus. Referring to FIG. 2A, for example, input
stream 222 received by pH adjustment apparatus 208 comprises at
least a portion of suspended-solids-diminished stream 222 produced
by suspended solids removal apparatus 206. In other embodiments,
the input stream received by the suspended solids removal apparatus
comprises at least a portion of the pH-adjusted stream produced by
the pH adjustment apparatus. That is to say, in certain
embodiments, the suspended solids removal apparatus can be located
downstream of the pH adjustment apparatus.
[0158] In some embodiments, the input stream received by the VOM
removal apparatus comprises at least a portion of the
suspended-solids-diminished stream produced by the suspended solids
removal apparatus. That is to say, in certain embodiments, the VOM
removal apparatus can be located downstream of the suspended solids
removal apparatus. Referring to FIG. 2A, for example, input stream
224 received by VOM removal apparatus 210 comprises at least a
portion of suspended solids-diminished stream 222 produced by
suspended solids removal apparatus 206. In other embodiments, the
input stream received by the suspended solids removal apparatus
comprises at least a portion of the VOM-diminished stream produced
by the VOM removal apparatus. That is to say, in certain
embodiments, the suspended solids removal apparatus can be located
downstream of the VOM removal apparatus.
[0159] In some embodiments, the input stream received by the VOM
removal apparatus comprises at least a portion of the pH-adjusted
stream produced by the pH adjustment apparatus. That is to say, in
certain embodiments, the VOM removal apparatus can be located
downstream of the pH adjustment apparatus. Referring to FIG. 2A,
for example, input stream 224 received by VOM removal apparatus 210
comprises at least a portion of pH-adjusted stream (also stream
224) produced by pH adjustment apparatus 208. In other embodiments,
the input stream received by the pH adjustment apparatus comprises
at least a portion of the VOM-diminished stream produced by the VOM
removal apparatus. That is to say, in certain embodiments, the pH
adjustment apparatus can be located downstream of the VOM removal
apparatus.
[0160] Each of separation apparatus 202, ion-removal apparatus 204,
suspended solids removal apparatus 206, pH adjustment apparatus
208, VOM removal apparatus 210, and filtration apparatus 212 is an
optional feature of the clean brine system. In some embodiments,
the clean brine system comprises only one of separation apparatus
202, ion-removal apparatus 204, suspended solids removal apparatus
206, pH adjustment apparatus 208, VOM removal apparatus 210, and/or
filtration apparatus 212. In some embodiments, the clean brine
system comprises any combination of two or more of separation
apparatuses 202, suspended solids removal apparatuses 206,
ion-removal apparatuses 204, pH adjustment apparatuses 208, VOM
removal apparatuses 210, and/or filtration apparatuses 212.
[0161] Various of the unit operations described herein can be
"directly fluidically connected" to other unit operations and/or
components. As used herein, a direct fluid connection exists
between a first unit operation and a second unit operation (and the
two unit operations are said to be "directly fluidically connected"
to each other) when they are fluidically connected to each other
and the composition of the fluid does not substantially change
(i.e., no fluid component changes in relative abundance by more
than 5% and no phase change occurs) as it is transported from the
first unit operation to the second unit operation. As an
illustrative example, a stream that connects first and second unit
operations, and in which the pressure and temperature of the fluid
is adjusted but the composition of the fluid is not altered, would
be said to directly fluidically connect the first and second unit
operations. If, on the other hand, a separation step is performed
and/or a chemical reaction is performed that substantially alters
the composition of the stream contents during passage from the
first component to the second component, the stream would not be
said to directly fluidically connect the first and second unit
operations.
[0162] It should be understood that, in embodiments in which a
single unit is shown in the figures and/or is described as
performing a certain function, the single unit could be replaced
with multiple units (e.g., operated in parallel) performing a
similar function. For example, in certain embodiments, any one or
more of the separation apparatus, suspended solids removal
apparatus, ion-removal apparatus, pH adjustment apparatus, VOM
removal apparatus, filtration apparatus, and/or desalination system
could correspond to a plurality of separation apparatuses,
suspended solids removal apparatuses, ion-removal apparatuses, pH
adjustment apparatuses, VOM removal apparatuses, filtration
apparatuses, and/or desalination systems (e.g., configured to be
operated in parallel).
[0163] It should also be understood that, where separate units are
shown in the figures and/or described as performing a sequence of
certain functions, the units may also be present as a single unit
(e.g., within a common housing), and the single unit may perform a
combination of functions. For example, in some embodiments, any two
or more of the separation apparatus, the ion-removal apparatus, the
suspended solids removal apparatus, the pH adjustment apparatus,
the VOM removal apparatus, and the filtration apparatus can be a
single unit which can perform each of the functions associated with
the combination.
[0164] As particular examples, in some embodiments, the system
comprises a single unit that acts as both an ion-removal apparatus
and a separation apparatus. In certain embodiments, the system
comprises a single unit that acts as both an ion-removal apparatus
and a suspended solids removal apparatus. In certain embodiments,
the system comprises a single unit that acts as both an ion-removal
apparatus and a pH adjustment apparatus. In certain embodiments,
the system comprises a single unit that acts as both an ion-removal
apparatus and a VOM removal apparatus. As additional examples, in
some embodiments, the system comprises a single unit that acts as
both a separation apparatus and a suspended solids removal
apparatus. In some embodiments, the system comprises a single unit
that acts as both a separation apparatus and an ion-removal
apparatus. In certain embodiments, the system comprises a single
unit that acts as both a separation apparatus and a pH adjustment
apparatus. In certain embodiments, the system comprises a single
unit that acts as both a separation apparatus and a VOM removal
apparatus. As still further examples, in some embodiments, the
system comprises a single unit that acts as both a suspended solids
removal apparatus and a pH adjustment apparatus. In some
embodiments, the system comprises a single unit that acts as both a
suspended solids removal apparatus and a VOM removal apparatus. In
some embodiments, the system comprises a single unit that acts as
both a pH adjustment apparatus and a VOM removal apparatus. Units
that perform three, four, or five of the functions outlined above
are also possible. Of course, the invention is not necessarily
limited to combination units, and in some embodiments, any of the
separation apparatus, the suspended solids removal apparatus, the
ion-removal apparatus, the pH adjustment apparatus, the VOM removal
apparatus, and/or the filtration apparatus may be standalone
units.
[0165] In some embodiments, one or more aqueous streams (e.g.,
clean brine streams) produced by a clean brine system described
herein may be collected as product streams. In some cases, one or
more aqueous streams produced by the clean brine system may be
further treated, for example by a desalination system. However, it
should be noted that any further processing of a clean brine stream
by a downstream system (e.g., a desalination system) is optional.
That is to say, in some embodiments, the clean brine system may be
used in association with a downstream apparatus, but in other
embodiments, the clean brine system may be used on its own, in the
absence of any downstream systems.
Desalination
[0166] In some embodiments, the water treatment system comprises an
optional desalination system fluidically connected to the clean
brine system. In some embodiments, the desalination system is
configured to remove water from an aqueous stream received by the
desalination system to produce a concentrated brine stream enriched
in a salt (e.g., a dissolved salt) relative to the aqueous stream
received by the desalination system. In certain embodiments, the
desalination system is also configured to produce a substantially
pure water stream lean in a dissolved salt relative to the aqueous
stream received by the desalination system. In some embodiments,
the desalination system is a system configured to remove at least a
portion of at least one dissolved salt from an aqueous stream.
[0167] According to some embodiments, at least one salt in an
aqueous stream received by the desalination system is a dissolved
salt (e.g., a salt that has been solubilized to such an extent that
the component ions of the salt are no long ionically bonded to each
other). In certain embodiments, at least one salt in the liquid
stream is a monovalent salt. As used herein, the term "monovalent
salt" refers to a salt that includes a monovalent cation (e.g., a
cation with a redox state of +1 when solubilized). Examples of
monovalent salts include, but are not limited to, salts containing
sodium, potassium, lithium, rubidium, cesium, and francium. In
certain embodiments, the monovalent salts include monovalent anions
comprising, for example, chlorine, bromine, fluorine, and iodine.
Non-limiting examples of monovalent salts include sodium chloride
(NaCl), sodium bromide (NaBr), potassium chloride (KCl), potassium
bromide (KBr), sodium carbonate, (Na.sub.2CO.sub.3), and sodium
sulfate (Na.sub.2SO.sub.4). In some cases, at least one salt is a
divalent salt. As used herein, the term "divalent salt" refers to a
salt that includes a divalent cation (e.g., a cation with a redox
state of +2 when solubilized). Non-limiting examples of divalent
salts include calcium chloride (CaCl.sub.2), calcium sulfate
(CaSO.sub.4), magnesium sulfate (MgSO.sub.4), strontium sulfate
(SrSO.sub.4), barium sulfate (BaSO.sub.4), and/or barium-strontium
sulfate (BaSr(SO.sub.4).sub.2). In some cases, at least one salt in
the liquid stream is a trivalent salt (e.g., a salt that includes a
trivalent cation having a redox state of +3 when solubilized) or a
tetravalent salt (e.g., a salt that includes a tetravalent cation
having a redox state of +4 when solubilized). Non-limiting examples
of trivalent salts or tetravalent salts include iron (III)
hydroxide (Fe(OH).sub.3), iron (III) carbonate
(Fe.sub.2(CO.sub.3).sub.3), aluminum hydroxide (Al(OH).sub.3),
aluminum carbonate (Al.sub.2(CO.sub.3).sub.3), boron salts, and/or
silicates.
[0168] In some embodiments, the desalination system is a thermal
desalination system. According to certain embodiments, the
desalination system is a humidification-dehumidification (HDH)
desalination system. An HDH desalination system generally refers to
a system comprising a humidifier and a dehumidifier. In some
embodiments, the humidifier is configured to receive a liquid feed
stream comprising water and at least one dissolved salt and to
transfer at least a portion of the water from the liquid feed
stream to a carrier gas through an evaporation process, thereby
producing a humidified gas stream and a concentrated brine stream.
In certain embodiments, the carrier gas comprises a non-condensable
gas. Non-limiting examples of suitable non-condensable gases
include air, nitrogen, oxygen, helium, argon, carbon monoxide,
carbon dioxide, sulfur oxides (SO.sub.x) (e.g., SO.sub.2,
SO.sub.3), and/or nitrogen oxides (NO.sub.x) (e.g., NO, NO.sub.2).
In some embodiments, the dehumidifier is configured to receive the
humidified gas stream from the humidifier and to transfer at least
a portion of water from the humidified gas stream to a stream
comprising substantially pure water through a condensation
process.
[0169] FIG. 6 shows an exemplary schematic illustration of HDH
desalination system 600, which may be used in association with
certain inventive systems and methods described herein. In FIG. 6,
desalination system 600 comprises humidifier 602 and dehumidifier
604. As shown in FIG. 6, humidifier 602 comprises liquid inlet 606
and liquid outlet 608. In FIG. 6, humidifier 602 is fluidically
connected to dehumidifier 604 via gas conduits 610 and 612. As
shown in FIG. 6, dehumidifier 604 comprises liquid inlet 614 and
liquid outlet 616.
[0170] In operation, a liquid stream comprising water and a
dissolved salt at an initial concentration may enter humidifier 602
through liquid inlet 606. Humidifier 602 may also be configured to
receive a carrier gas stream comprising a non-condensable gas.
According to some embodiments, humidifier 602 is configured such
that the liquid stream comes into contact (e.g., direct or indirect
contact) with the carrier gas stream, and heat and water vapor are
transferred from the liquid stream to the carrier gas stream
through an evaporation process, thereby producing a humidified gas
stream. In some embodiments, the remaining portion of the liquid
stream that is not transported to the carrier gas stream forms a
concentrated brine stream enriched in the dissolved salt relative
to the liquid stream (e.g., the concentration of the dissolved salt
in the concentrated brine stream is greater than the initial
concentration of the dissolved salt in the liquid stream). In some
embodiments, the concentrated brine stream exits humidifier 602
through liquid outlet 608.
[0171] According to some embodiments, the humidified gas stream
exits humidifier 602 and flows through gas conduit 610 to
dehumidifier 604. A stream comprising substantially pure water may
enter dehumidifier 604 through liquid inlet 614. In dehumidifier
604, the humidified gas stream may come into contact (e.g., direct
or indirect contact) with the substantially pure water stream, and
heat and water may be transferred from the humidified gas stream to
the substantially pure water stream through a condensation process,
thereby producing a dehumidified gas stream. The stream comprising
substantially pure water may exit dehumidifier 604 through liquid
outlet 616; in some cases, at least a portion of the substantially
pure water stream may be discharged from HDH desalination system
600, and at least a portion of the substantially pure water stream
may be recirculated to liquid inlet 614. The dehumidified gas
stream may exit dehumidifier 604, and at least a portion of the
dehumidified gas stream may flow to humidifier 602 through gas
conduit 612. In some embodiments, at least a portion of the
dehumidified gas stream may be transported elsewhere within the
system and/or vented.
[0172] The humidifier may have any configuration that allows for
the transfer of water vapor from a liquid feed stream to a carrier
gas stream (e.g., through an evaporation process). In certain
embodiments, the humidifier comprises a vessel (e.g., a stainless
steel tank, a fiber-reinforced plastic tank, or other vessel). The
humidifier vessel can comprise a liquid inlet configured to receive
a liquid feed stream comprising water and at least one dissolved
salt and a gas inlet configured to receive a carrier gas stream. In
some embodiments, the humidifier can further comprise a liquid
outlet and a gas outlet.
[0173] The dehumidifier may have any configuration that allows for
the transfer of water from a humidified gas stream to a stream
comprising substantially pure water (e.g., through a condensation
process). In certain embodiments, the dehumidifier comprises a
vessel (e.g., a stainless steel tank or other vessel). The
dehumidifier vessel can comprise a liquid inlet configured to
receive a stream comprising substantially pure water and a gas
inlet configured to receive the humidified gas stream. In some
embodiments, the dehumidifier can further comprise a liquid outlet
for the stream comprising substantially pure water and a gas outlet
for the dehumidified gas stream.
[0174] According to some embodiments, the humidifier is a bubble
column humidifier (e.g., a humidifier in which the evaporation
process occurs through direct contact between a liquid feed stream
and bubbles of a carrier gas) and/or the dehumidifier is a bubble
column dehumidifier (e.g., a dehumidifier in which the condensation
process occurs through direct contact between a substantially pure
liquid stream and bubbles of a humidified gas). In some cases,
bubble column humidifiers and bubble column dehumidifiers may be
associated with certain advantages. For example, bubble column
humidifiers and dehumidifiers may exhibit higher thermodynamic
effectiveness than certain other types of humidifiers (e.g., packed
bed humidifiers, spray towers, wetted wall towers) and
dehumidifiers (e.g., surface condensers). Without wishing to be
bound by a particular theory, the increased thermodynamic
effectiveness may be at least partially attributed to the use of
gas bubbles for heat and mass transfer in bubble column humidifiers
and dehumidifiers, since gas bubbles may have more surface area
available for heat and mass transfer than many other types of
surfaces (e.g., metallic tubes, liquid films, packing material). In
addition, bubble column humidifiers and dehumidifiers may have
certain features that further increase thermodynamic effectiveness,
including, but not limited to, relatively low liquid level height,
relatively high aspect ratio liquid flow paths, and multi-staged
designs.
[0175] In certain embodiments, a bubble column humidifier comprises
at least one stage comprising a chamber and a liquid layer
positioned within a portion of the chamber. The liquid layer may,
in some cases, comprise a liquid comprising water and at least one
dissolved salt. The chamber may further comprise a gas distribution
region occupying at least a portion of the chamber not occupied by
the liquid layer. In addition, the chamber may be in fluid
communication with a bubble generator (e.g., a sparger plate). In
some embodiments, a carrier gas stream flows through the bubble
generator, forming bubbles of the carrier gas. The carrier gas
bubbles may then travel through the liquid layer. The liquid layer
may be maintained at a temperature higher than the temperature of
the gas bubbles, and as the gas bubbles directly contact the liquid
layer, heat and/or mass may be transferred from the liquid layer to
the gas bubbles. In some cases, at least a portion of water may be
transferred to the gas bubbles through an evaporation process. The
bubbles of the humidified gas may exit the liquid layer and enter
the gas distribution region. The humidified gas may be
substantially homogeneously distributed throughout the gas
distribution region. The humidified gas may then exit the bubble
column humidifier as a humidified gas stream.
[0176] In some embodiments, a bubble column dehumidifier comprises
at least one stage comprising a chamber and a liquid layer
positioned within a portion of the chamber. The liquid layer may,
in some cases, comprise substantially pure water. The chamber may
further comprise a gas distribution region occupying at least a
portion of the chamber not occupied by the liquid layer. In
addition, the chamber may be in fluid communication with a bubble
generator (e.g., a sparger plate). In some embodiments, the
humidified gas stream flows from the humidifier through the bubble
generator, forming bubbles of the humidified gas. The bubbles of
the humidified gas may then travel through the liquid layer. The
liquid layer may be maintained at a temperature lower than the
temperature of the humidified gas bubbles, and as the humidified
gas bubbles directly contact the liquid layer, heat and/or mass may
be transferred from the humidified gas bubbles to the liquid layer
via a condensation process.
[0177] Suitable bubble column condensers that may be used as the
dehumidifier in certain systems and methods described herein
include those described in U.S. Pat. No. 8,523,985, by Govindan et
al., issued Sep. 3, 2013, and entitled "Bubble-Column Vapor Mixture
Condenser"; U.S. Pat. No. 8,778,065, by Govindan et al., issued
Jul. 15, 2014, and entitled "Humidification-Dehumidification System
Including a Bubble-Column Vapor Mixture Condenser"; U.S. Patent
Publication No. 2013/0074694, by Govindan et al., filed on Sep. 23,
2011, and entitled "Bubble-Column Vapor Mixture Condenser"; U.S.
Patent Publication No. 2015/0129410, filed on Sep. 12, 2014, and
entitled "Systems Including a Condensing Apparatus such as a Bubble
Column Condenser"; U.S. patent application Ser. No. 14/538,619,
filed on Nov. 11, 2014, and entitled "Systems Including a
Condensing Apparatus such as a Bubble Column Condenser"; U.S.
Provisional Patent Application No. 61/877,032, filed on Sep. 12,
2013, and entitled "Systems Including a Bubble Column Condenser";
and U.S. Provisional Patent Application No. 61/881,365, filed on
Sep. 23, 2013, and entitled "Desalination Systems and Associated
Methods," each of which is incorporated herein by reference in its
entirety for all purposes. Suitable bubble column humidifiers that
may be used as the humidifier in certain systems and methods
described herein include those described in International Patent
Publication No. WO 2014/00829, by Govindan et al., filed Jun. 6,
2014, as International Patent Application No. PCT/US2014/41226, and
entitled "Multi-Stage Bubble Column Humidifier," which is
incorporated herein by reference in its entirety for all
purposes.
[0178] In some embodiments, the humidifier and/or dehumidifier
comprise a plurality of stages. For example, the stages may be
arranged such that a gas (e.g., a carrier gas, a humidified gas)
flows sequentially from a first stage to a second stage. In some
cases, the stages may be arranged in a vertical fashion (e.g., a
second stage positioned above a first stage) or a horizontal
fashion (e.g., a second stage positioned to the right or left of a
first stage). In some cases, each stage may comprise a liquid
layer. In embodiments relating to a humidifier comprising a
plurality of stages (e.g., a multi-stage humidifier), the
temperature of the liquid layer of the first stage (e.g., the
bottommost stage in a vertically arranged bubble column) may be
lower than the temperature of the liquid layer of the second stage,
which may be lower than the temperature of the liquid layer of the
third stage (e.g., the topmost stage in a vertically arranged
bubble column). In embodiments relating to a dehumidifier
comprising a plurality of stages (e.g., a multi-stage
dehumidifier), the temperature of the liquid layer of the first
stage may be higher than the temperature of the liquid layer of the
second stage, which may be higher than the temperature of the
liquid layer of the third stage.
[0179] The presence of multiple stages within a bubble column
humidifier and/or bubble column dehumidifier may, in some cases,
advantageously result in increased humidification and/or
dehumidification of a gas. In some cases, the presence of multiple
stages may advantageously lead to higher recovery of substantially
pure water. For example, the presence of multiple stages may
provide numerous locations where the gas may be humidified and/or
dehumidified (e.g., treated to recover substantially pure water).
That is, the gas may travel through more than one liquid layer in
which at least a portion of the gas undergoes humidification (e.g.,
evaporation) or dehumidification (e.g., condensation). In addition,
the presence of multiple stages may increase the difference in
temperature between a liquid stream at an inlet and an outlet of a
humidifier and/or dehumidifier. This may be advantageous in systems
where heat from a liquid stream (e.g., dehumidifier liquid outlet
stream) is transferred to a separate stream (e.g., humidifier input
stream) within the system. In such cases, the ability to produce a
heated dehumidifier liquid outlet stream can increase the energy
effectiveness of the system. Additionally, the presence of multiple
stages may enable greater flexibility for fluid flow within an
apparatus. For example, extraction and/or injection of fluids
(e.g., gas streams) from intermediate humidification and/or
dehumidification stages may occur through intermediate exchange
conduits.
[0180] In some cases, a bubble column humidifier and/or a bubble
column dehumidifier is configured to extract partially humidified
gas from at least one intermediate location in the humidifier
(e.g., not the final humidification stage) and to inject the
partially humidified gas into at least one intermediate location in
the dehumidifier (e.g., not the first dehumidification stage). In
some embodiments, extraction from at least one intermediate
location in the humidifier and injection into at least one
intermediate location in the dehumidifier may be thermodynamically
advantageous. Because the portion of the gas flow exiting the
humidifier at an intermediate outlet (e.g., the extracted portion)
has not passed through the entire humidifier, the temperature of
the gas flow at the intermediate outlet may be lower than the
temperature of the gas flow at the main gas outlet of the
humidifier. The location of the extraction points (e.g., outlets)
and/or injection points (e.g., inlets) may be selected to increase
the thermal efficiency of the system. For example, because a gas
(e.g., air) may have increased vapor content at higher temperatures
than at lower temperatures, and because the heat capacity of a gas
with higher vapor content may be higher than the heat capacity of a
gas with lower vapor content, less gas may be used in higher
temperature areas of the humidifier and/or dehumidifier to better
balance the heat capacity rate ratios of the gas (e.g., air) and
liquid (e.g., water) streams. Extraction and/or injection at
intermediate locations may therefore advantageously allow for
manipulation of gas mass flows and for greater heat recovery.
[0181] The humidifier and/or dehumidifier may be of any size. In
some cases, the size of the humidifier and/or dehumidifier will
generally depend upon the number of humidifier units and/or
dehumidifier units employed in the system and the total flow rate
of the liquid that is to be desalinated. In certain embodiments,
the total of the volumes of the humidifiers used in the
desalination system can be at least about 1 gallon, at least about
10 gallons, at least about 100 gallons, at least about 500 gallons,
at least about 1,000 gallons, at least about 2,000 gallons, at
least about 5,000 gallons, at least about 7,000 gallons, at least
about 10,000 gallons, at least about 20,000 gallons, at least about
50,000 gallons, or at least about 100,000 gallons (and/or, in some
embodiments, up to about 1,000,000 gallons, or more).
[0182] In some embodiments, the desalination system may have a
relatively high liquid feed rate (e.g., amount of liquid feed
entering the system per unit time). In certain embodiments, the
desalination system has a liquid feed rate of at least about 5
barrels/day, at least about 10 barrels/day, at least about 20
barrels/day, at least about 50 barrels/day, at least about 100
barrels/day, at least about 200 barrels/day, at least about 300
barrels/day, at least about 400 barrels/day, at least about 500
barrels/day, at least about 600 barrels/day, at least about 700
barrels/day, at least about 800 barrels/day, at least about 900
barrels/day, at least about 1,000 barrels a day, at least about
2,000 barrels/day, at least about 5,000 barrels/day, at least about
10,000 barrels/day, at least about 20,000 barrels/day, at least
about 30,000 barrels/day, at least about 35,000 barrels/day, at
least about 50,000 barrels/day (and/or, in some embodiments, up to
about 100,000 barrels/day, or more).
[0183] In some embodiments, the desalination system may have a
relatively high production rate (e.g., amount of substantially pure
water produced per unit time). In certain cases, the desalination
system has a production rate of at least about 10 barrels/day, at
least about 50 barrels/day, at least about 100 barrels/day, at
least about 200 barrels/day, at least about 300 barrels/day, at
least about 400 barrels/day, at least about 500 barrels/day, at
least about 600 barrels/day, at least about 700 barrels/day, at
least about 800 barrels/day, at least about 900 barrels/day, at
least about 1,000 barrels a day, at least about 2,000 barrels/day,
at least about 5,000 barrels/day, or at least about 10,000
barrels/day (and/or, in some embodiments, up to about 100,000
barrels/day, or more).
[0184] It should be recognized that other types of humidifiers
and/or dehumidifiers may be used in systems and methods described
herein. For example, in some embodiments, the humidifier is a
packed bed humidifier. In certain cases, the humidifier comprises a
packing material (e.g., polyvinyl chloride (PVC) packing material).
The packing material may, in some cases, facilitate turbulent gas
flow and/or enhanced direct contact between the liquid stream
comprising water and at least one dissolved salt and the carrier
gas stream within the humidifier. In certain embodiments, the
humidifier further comprises a device configured to produce
droplets of the liquid feed stream. For example, a nozzle or other
spraying device may be positioned at the top of the humidifier such
that the liquid feed stream is sprayed downward to the bottom of
the humidifier. The use of a spraying device can advantageously
increase the degree of contact between the liquid feed stream fed
to the humidifier and the carrier gas stream into which water from
the liquid feed stream is transported.
[0185] In some embodiments, the desalination system further
comprises one or more additional devices. According to some
embodiments, for example, the desalination system further comprises
a heat exchanger in fluid communication with the humidifier and/or
dehumidifier. In certain cases, the heat exchanger advantageously
facilitates transfer of heat from a liquid stream exiting the
dehumidifier to a liquid stream entering the humidifier. For
example, the heat exchanger may advantageously allow energy to be
recovered from a dehumidifier liquid outlet stream and used to
pre-heat a humidifier liquid inlet stream prior to entry of the
humidifier liquid inlet stream into the humidifier.
[0186] In certain embodiments, the desalination system further
comprises an optional heating device arranged in fluid
communication with the humidifier. The optional heating device may
be any device capable of transferring heat to a liquid stream. The
heating device may be a heat exchanger, a heat collection device
(e.g., a device configured to store and/or utilize thermal energy),
or an electric heater. In certain cases, the heating device may be
arranged such that a liquid feed stream is heated prior to entering
the humidifier. Heating the liquid feed stream may, in some cases,
increase the degree to which water is transferred from the liquid
feed stream to the carrier gas stream within the humidifier.
[0187] In some embodiments, the desalination system further
comprises an optional cooling device arranged in fluid
communication with the dehumidifier. In certain cases, a stream
comprising substantially pure water may be cooled by the cooling
device prior to entering the dehumidifier. A cooling device
generally refers to any device that is capable of removing heat
from a fluid stream (e.g., a liquid stream, a gas stream). The
cooling device may be a heat exchanger (e.g., an air-cooled heat
exchanger), a dry cooler, a chiller, a radiator, or any other
device capable of removing heat from a fluid stream.
[0188] It should be understood that the inventive systems and
methods described herein are not limited to those including a
humidification-dehumidification desalination system, and that in
other embodiments, other desalination system types may be employed.
Non-limiting examples of suitable desalination systems include a
mechanical vapor compression system, a multi-effect distillation
system, a multi-stage flash system, and/or a vacuum distillation
system. In some embodiments, the desalination system is a hybrid
desalination system comprising a first desalination unit and a
second desalination unit, each of which may be any type of
desalination system. The first desalination unit and second
desalination unit may be the same or different types of
desalination systems. Certain of the systems described herein can
be configured to desalinate saline solutions entering at relatively
high flow rates, and, accordingly, can be configured to produce
relative pure water streams at relatively high flow rates. For
example, in some embodiments, the systems and methods described
herein may be configured and sized to operate to receive an aqueous
feed stream at a flow rate of at least about 1 gallon/minute, at
least about 10 gallons/minute, at least about 100 gallons/minute,
or at least about 1000 gallons/minute (and/or, in certain
embodiments, up to about 10,000 gallons/minute, or more).
[0189] In some embodiments, the dehumidifier is configured to
produce a stream comprising water of relatively high purity (e.g.,
a substantially pure water stream). For example, in some
embodiments, the dehumidifier produces a stream comprising water in
an amount of at least about 95 wt %, at least about 99 wt %, at
least about 99.9 wt %, or at least about 99.99 wt % (and/or, in
certain embodiments, up to about 99.999 wt %, or more). In some
embodiments, the percentage volume of a liquid feed stream that is
recovered as fresh water is at least about 40%, at least about 45%,
at least about 50%, at least about 55%, at least about 58%, at
least about 60%, or at least about 70%.
[0190] In some embodiments, the substantially pure water stream has
a relatively low concentration of one or more dissolved salts. In
some cases, the concentration of at least one dissolved salt in the
substantially pure water stream is about 500 mg/L or less, about
200 mg/L or less, about 100 mg/L or less, about 50 mg/L or less,
about 20 mg/L or less, about 10 mg/L or less, about 5 mg/L or less,
about 2 mg/L or less, about 1 mg/L or less, about 0.5 mg/L or less,
about 0.2 mg/L or less, about 0.1 mg/L or less, or about 0.01 mg/L
or less. According to some embodiments, the concentration of at
least one dissolved salt in the substantially pure water stream may
be substantially zero (e.g., not detectable). In certain cases, the
concentration of at least one dissolved salt in the substantially
pure water stream is in the range of about 0.01 mg/L to about 500
mg/L, about 0.01 mg/L to about 200 mg/L, about 0.01 mg/L to about
100 mg/L, about 0.01 mg/L to about 50 mg/L, about 0.01 mg/L to
about 20 mg/L, about 0.01 mg/L to about 10 mg/L, about 0.01 mg/L to
about 5 mg/L, about 0.01 mg/L to about 2 mg/L, about 0.01 mg/L to
about 1 mg/L, about 0 mg/L to about 500 mg/L, about 0 mg/L to about
200 mg/L, about 0 mg/L to about 100 mg/L, about 0 mg/L to about 50
mg/L, about 0 mg/L to about 20 mg/L, about 0 mg/L to about 10 mg/L,
about 0 mg/L to about 5 mg/L, about 0 mg/L to about 2 mg/L, about 0
mg/L to about 1 mg/L, about 0 mg/L to about 0.1 mg/L, or about 0
mg/L to about 0.01 mg/L. The concentration of a dissolved salt may
be measured according to any method known in the art. For example,
suitable methods for measuring the concentration of a dissolved
salt include inductively coupled plasma (ICP) spectroscopy (e.g.,
inductively coupled plasma optical emission spectroscopy). As one
non-limiting example, an Optima 8300 ICP-OES spectrometer may be
used.
[0191] In some embodiments, the substantially pure water stream
contains at least one dissolved salt in an amount of about 2 wt %
or less, about 1 wt % or less, about 0.5 wt % or less, about 0.2 wt
% or less, about 0.1 wt % or less, about 0.05 wt % or less, or
about 0.01 wt % or less. In some embodiments, the substantially
pure water stream contains at least one dissolved salt in an amount
in the range of about 0.01 wt % to about 2 wt %, about 0.01 wt % to
about 1 wt %, about 0.01 wt % to about 0.5 wt %, about 0.01 wt % to
about 0.2 wt %, or about 0.01 wt % to about 0.1 wt %.
[0192] In some embodiments, the substantially pure water stream has
a relatively low total dissolved salt concentration. In some cases,
the total dissolved salt concentration in the substantially pure
water stream is about 500 mg/L or less, about 200 mg/L or less,
about 100 mg/L or less, about 50 mg/L or less, about 20 mg/L or
less, about 10 mg/L or less, about 5 mg/L or less, about 2 mg/L or
less, about 1 mg/L or less, about 0.5 mg/L or less, about 0.1 mg/L
or less, or about 0.01 mg/L or less. According to some embodiments,
the total dissolved salt concentration in the substantially pure
water stream may be substantially zero (e.g., not detectable). In
certain embodiments, the total dissolved salt concentration in the
substantially pure water stream is in the range of about 0.01 mg/L
to about 500 mg/L, about 0.01 mg/L to about 200 mg/L, about 0.01
mg/L to about 100 mg/L, about 0.01 mg/L to about 50 mg/L, about
0.01 mg/L to about 20 mg/L, about 0.01 mg/L to about 10 mg/L, about
0.01 mg/L to about 5 mg/L, about 0.01 mg/L to about 2 mg/L, about
0.01 mg/L to about 1 mg/L, about 0 mg/L to about 500 mg/L, about 0
mg/L to about 200 mg/L, about 0 mg/L to about 100 mg/L, about 0
mg/L to about 50 mg/L, about 0 mg/L to about 20 mg/L, about 0 mg/L
to about 10 mg/L, about 0 mg/L to about 5 mg/L, about 0 mg/L to
about 2 mg/L, about 0 mg/L to about 1 mg/L, about 0 mg/L to about
0.1 mg/L, or about 0 mg/L to about 0.01 mg/L. Total dissolved salt
concentration may be measured according to any method known in the
art. For example, a non-limiting example of a suitable method for
measuring total dissolved salt concentration is the SM 2540C
method. According to the SM 2540C method, a sample comprising an
amount of liquid comprising one or more dissolved solids is
filtered (e.g., through a glass fiber filter), and the filtrate is
evaporated to dryness in a weighed dish at 180.degree. C. The
increase in dish weight represents the mass of the total dissolved
solids in the sample. The total dissolved salt concentration of the
sample may be obtained by dividing the mass of the total dissolved
solids by the volume of the original sample.
[0193] In some embodiments, the total dissolved salt concentration
of the substantially pure water stream is substantially less than
the total dissolved salt concentration of an aqueous feed stream
received by the desalination system. In some cases, the total
dissolved salt concentration of the substantially pure water stream
is at least about 0.5%, about 1%, about 2%, about 5%, about 10%,
about 15%, or about 20% less than the total dissolved salt
concentration of the aqueous feed stream.
[0194] According to some embodiments, the substantially pure water
stream has a relatively low salinity (e.g., weight percent of all
dissolved salts). In some embodiments, the substantially pure water
stream has a salinity of about 5% or less, about 2% or less, about
1% or less, about 0.5% or less, about 0.2% or less, about 0.1% or
less, about 0.05% or less, or about 0.01% or less. In some
embodiments, the substantially pure water stream has a salinity in
the range of about 0.01% to about 5%, about 0.01% to about 2%,
about 0.01% to about 1%, about 0.01% to about 0.5%, about 0.01% to
about 0.2%, or about 0.01% to about 0.1%. Salinity may be measured
according to any method known in the art. For example, a
non-limiting example of a suitable method for measuring salinity is
the SM 2540C method. According to the SM 2540C method, a sample
comprising an amount of liquid comprising one or more dissolved
solids is filtered (e.g., through a glass fiber filter), and the
filtrate is evaporated to dryness in a weighed dish at 180.degree.
C. The increase in dish weight represents the mass of the total
dissolved solids in the sample. The salinity of the sample may be
obtained by dividing the mass of the total dissolved solids by the
mass of the original sample and multiplying the resultant number by
100.
[0195] According to some embodiments, the humidifier is configured
to produce a concentrated brine stream (e.g., a stream comprising a
relatively high concentration of at least one dissolved salt). The
concentrated brine stream may, in some cases, have a relatively
high salinity. In some cases, the salinity of the concentrated
brine stream is at least about 10%, at least about 15%, at least
about 20%, at least about 25%, at least about 26%, at least about
27%, at least about 28%, at least about 29%, or at least about 30%.
In some embodiments, the salinity of the concentrated brine stream
is in the range of about 10% to about 20%, about 10% to about 25%,
about 10% to about 26%, about 10% to about 27%, about 10% to about
28%, about 10% to about 29%, about 10% to about 30%, about 15% to
about 20%, about 15% to about 25%, about 15% to about 26%, about
15% to about 27%, about 15% to about 28%, about 15% to about 29%,
about 15% to about 30%, about 20% to about 25%, about 20% to about
26%, about 20% to about 27%, about 20% to about 28%, about 20% to
about 29%, about 20% to about 30%, about 25 wt % to about 26 wt %,
about 25 wt % to about 27 wt %, about 25 wt % to about 28 wt %,
about 25 wt % to about 29 wt %, or about 25% to about 30%.
[0196] The concentrated brine stream may, in some cases, have a
relatively high concentration of at least one dissolved salt (e.g.,
NaCl). In certain cases, the concentration of at least one
dissolved salt in the concentrated brine stream is at least about
100 mg/L, at least about 200 mg/L, at least about 400 mg/L, at
least about 500 mg/L, at least about 800 mg/L, at least about 1,000
mg/L, at least about 2,000 mg/L, at least about 4,000 mg/L, at
least about 5,000 mg/L, at least about 8,000 mg/L, at least about
10,000 mg/L, at least about 20,000 mg/L, at least about 40,000
mg/L, at least about 45,000 mg/L, at least about 50,000 mg/L, at
least about 80,000 mg/L, at least about 100,000 mg/L, at least
about 150,000 mg/L, at least about 200,000 mg/L, at least about
250,000 mg/L, at least about 300,000 mg/L, at least about 350,000
mg/L, at least about 400,000 mg/L, at least about 450,000 mg/L, or
at least about 500,000 mg/L (and/or, in certain embodiments, up to
the solubility limit of the salt in the concentrated brine stream).
In some embodiments, the concentration of at least one dissolved
salt in the concentrated brine stream is in the range of about
10,000 mg/L to about 20,000 mg/L, about 10,000 mg/L to about 40,000
mg/L, about 10,000 mg/L to about 45,000 mg/L, about 10,000 mg/L to
about 50,000 mg/L, about 10,000 mg/L to about 80,000 mg/L, about
10,000 mg/L to about 100,000 mg/L, about 10,000 mg/L to about
150,000 mg/L, about 10,000 mg/L to about 200,000 mg/L, about 10,000
mg/L to about 250,000 mg/L, about 10,000 mg/L to about 300,000
mg/L, about 10,000 mg/L to about 350,000 mg/L, about 10,000 mg/L to
about 400,000 mg/L, about 10,000 mg/L to about 450,000 mg/L, about
10,000 mg/L to about 500,000 mg/L about 20,000 mg/L to about 50,000
mg/L, about 20,000 mg/L to about 80,000 mg/L, about 20,000 mg/L to
about 100,000 mg/L, about 20,000 mg/L to about 150,000 mg/L, about
20,000 mg/L to about 200,000 mg/L, about 20,000 mg/L to about
250,000 mg/L, about 20,000 mg/L to about 300,000 mg/L, about 20,000
mg/L to about 350,000 mg/L, about 20,000 mg/L to about 400,000
mg/L, about 20,000 mg/L to about 450,000 mg/L, about 20,000 mg/L to
about 500,000 mg/L about 50,000 mg/L to about 100,000 mg/L, about
50,000 mg/L to about 150,000 mg/L, about 50,000 mg/L to about
200,000 mg/L, about 50,000 mg/L to about 250,000 mg/L, about 50,000
mg/L to about 300,000 mg/L, about 50,000 mg/L to about 350,000
mg/L, about 50,000 mg/L to about 400,000 mg/L, about 50,000 mg/L to
about 450,000 mg/L, about 50,000 to about 500,000 mg/L, about
100,000 mg/L to about 150,000 mg/L, about 100,000 mg/L to about
200,000 mg/L, about 100,000 mg/L to about 250,000 mg/L, about
100,000 mg/L to about 300,000 mg/L, about 100,000 mg/L to about
350,000 mg/L, about 100,000 mg/L to about 400,000 mg/L, about
100,000 mg/L to about 450,000 mg/L, or about 100,000 mg/L to about
500,000 mg/L.
[0197] In some embodiments, the concentrated brine stream contains
at least one dissolved salt (e.g., NaCl) in an amount of at least
about 1 wt %, at least about 5 wt %, at least about 10 wt %, at
least about 15 wt %, at least about 20 wt %, at least about 25 wt
%, at least about 26 wt %, at least about 27 wt %, at least about
28 wt %, at least about 29 wt %, or at least about 30 wt % (and/or,
in certain embodiments, up to the solubility limit of the salt in
the concentrated brine stream). In some embodiments, the
concentrated brine stream comprises at least one dissolved salt in
an amount in the range of about 1 wt % to about 10 wt %, about 1 wt
% to about 20 wt %, about 1 wt % to about 25 wt %, about 1 wt % to
about 26 wt %, about 1 wt % to about 27 wt %, about 1 wt % to about
28 wt %, about 1 wt % to about 29 wt %, about 1 wt % to about 30 wt
%, about 10 wt % to about 20 wt %, about 10 wt % to about 25 wt %,
about 10 wt % to about 26 wt %, about 10 wt % to about 27 wt %,
about 10 wt % to about 28 wt %, about 10 wt % to about 29 wt %,
about 10 wt % to about 30 wt %, about 20 wt % to about 25 wt %,
about 20 wt % to about 26 wt %, about 20 wt % to about 27 wt %,
about 20 wt % to about 28 wt %, about 20 wt % to about 29 wt %,
about 20 wt % to about 30 wt %, about 25 wt % to about 26 wt %,
about 25 wt % to about 27 wt %, about 25 wt % to about 28 wt %,
about 25 wt % to about 29 wt %, or about 25 wt % to about 30 wt
%.
[0198] In some embodiments, the total dissolved salt concentration
of the concentrated brine stream may be relatively high. In certain
cases, the total dissolved salt concentration of the concentrated
brine stream is at least about 100 mg/L, at least about 200 mg/L,
at least about 500 mg/L, at least about 1,000 mg/L, at least about
2,000 mg/L, at least about 5,000 mg/L, at least about 10,000 mg/L,
at least about 20,000 mg/L, at least about 50,000 mg/L, at least
about 75,000 mg/L, at least about 100,000 mg/L, at least about
150,000 mg/L, at least about 200,000 mg/L, at least about 250,000
mg/L, at least about 300,000 mg/L, at least about 350,000 mg/L, at
least about 400,000 mg/L, at least about 450,000 mg/L, at least
about 500,000 mg/L, at least about 550,000 mg/L, or at least about
600,000 mg/L (and/or, in certain embodiments, up to the solubility
limit of the salt(s) in the concentrated brine stream). In some
embodiments, the total dissolved salt concentration of the
concentrated brine stream is in the range of about 10,000 mg/L to
about 20,000 mg/L, about 10,000 mg/L to about 50,000 mg/L, about
10,000 mg/L to about 100,000 mg/L, about 10,000 mg/L to about
150,000 mg/L, about 10,000 mg/L to about 200,000 mg/L, about 10,000
mg/L to about 250,000 mg/L, about 10,000 mg/L to about 300,000
mg/L, about 10,000 mg/L to about 350,000 mg/L, or about 10,000 mg/L
to about 400,000 mg/L, about 10,000 mg/L to about 450,000 mg/L,
about 10,000 mg/L to about 500,000 mg/L, about 10,000 mg/L to about
550,000 mg/L, about 10,000 mg/L to about 600,000 mg/L, about 20,000
mg/L to about 50,000 mg/L, about 20,000 mg/L to about 100,000 mg/L,
about 20,000 mg/L to about 150,000 mg/L, about 20,000 mg/L to about
200,000 mg/L, about 20,000 mg/L to about 250,000 mg/L, about 20,000
mg/L to about 300,000 mg/L, about 20,000 mg/L to about 350,000
mg/L, about 20,000 mg/L to about 400,000 mg/L, about 20,000 mg/L to
about 450,000 mg/L, about 20,000 mg/L to about 500,000 mg/L, about
20,000 mg/L to about 550,000 mg/L, about 20,000 mg/L to about
600,000 mg/L, about 50,000 mg/L to about 100,000 mg/L, about 50,000
mg/L to about 150,000 mg/L, about 50,000 mg/L to about 200,000
mg/L, about 50,000 mg/L to about 250,000 mg/L, about 50,000 mg/L to
about 300,000 mg/L, about 50,000 mg/L to about 350,000 mg/L, about
50,000 mg/L to about 400,000 mg/L, about 50,000 mg/L to about
450,000 mg/L, about 50,000 mg/L to about 500,000 mg/L, about 50,000
mg/L to about 550,000 mg/L, about 50,000 mg/L to about 600,000
mg/L, about 100,000 mg/L to about 200,000 mg/L, about 100,000 mg/L
to about 250,000 mg/L, about 100,000 mg/L to about 300,000 mg/L,
about 100,000 mg/L to about 350,000 mg/L, about 100,000 mg/L to
about 400,000 mg/L, about 100,000 mg/L to about 450,000 mg/L, about
100,000 mg/L to about 500,000 mg/L, about 100,000 mg/L to about
550,000 mg/L, or about 100,000 mg/L to about 600,000 mg/L.
[0199] In some embodiments, the concentrated brine stream contains
a total amount of dissolved salts of at least about 1 wt %, at
least about 5 wt %, at least about 10 wt %, at least about 15 wt %,
at least about 20 wt %, at least about 25 wt %, at least about 26
wt %, at least about 27 wt %, at least about 28 wt %, at least
about 29 wt %, or at least about 30 wt %. In some embodiments, the
concentrated brine stream comprises a total amount of dissolved
salts in the range of about 1 wt % to about 10 wt %, about 1 wt %
to about 20 wt %, about 1 wt % to about 25 wt %, about 1 wt % to
about 26 wt %, about 1 wt % to about 27 wt %, about 1 wt % to about
28 wt %, about 1 wt % to about 29 wt %, about 1 wt % to about 30 wt
%, about 10 wt % to about 20 wt %, about 10 wt % to about 25 wt %,
about 10 wt % to about 26 wt %, about 10 wt % to about 27 wt %,
about 10 wt % to about 28 wt %, about 10 wt % to about 29 wt %,
about 10 wt % to about 30 wt %, about 20 wt % to about 25 wt %,
about 20 wt % to about 26 wt %, about 20 wt % to about 27 wt %,
about 20 wt % to about 28 wt %, about 20 wt % to about 29 wt %,
about 20 wt % to about 30 wt %, about 25 wt % to about 26 wt %,
about 25 wt % to about 27 wt %, about 25 wt % to about 28 wt %,
about 25 wt % to about 29 wt %, or about 25 wt % to about 30 wt
%.
[0200] In some embodiments, the total dissolved salt concentration
of the concentrated brine stream is significantly higher than the
total dissolved salt concentration of an aqueous feed stream
received by the desalination system. In some cases, the total
dissolved salt concentration of the concentrated brine stream is at
least about 5%, at least about 6%, at least about 10%, at least
about 14%, at least about 15%, at least about 20%, or at least
about 25% greater than the total dissolved salt concentration of
the aqueous feed stream.
[0201] According to some embodiments, one or more additional salts
may be added to the concentrated brine stream to produce an
ultra-high-density concentrated brine stream. Non-limiting examples
of suitable salts to add to a concentrated brine stream to produce
an ultra-high-density concentrated brine stream include sodium
chloride (NaCl), calcium chloride (CaCl.sub.2), magnesium chloride
(MgCl.sub.2), copper (II) chloride (CuCl.sub.2), iron (III)
chloride hexahydrate (FeCl.sub.3.6H.sub.2O), iron (III) chloride
(FeCl.sub.3), lithium chloride (LiCl), manganese (II) chloride
(MnCl.sub.2), nickel (II) chloride (NiCl.sub.2), zinc chloride
(ZnCl.sub.2), sodium bromide (NaBr), calcium bromide (CaBr.sub.2),
magnesium bromide (MgBr.sub.2), potassium bromide (KBr), copper
(II) bromide (CuBr.sub.2), iron (III) bromide (FeBr.sub.3), lithium
bromide (LiBr), manganese (II) bromide (MnBr.sub.2), nickel (II)
bromide (NiBr.sub.2), zinc bromide (ZnBr.sub.2), ammonium nitrate
(NH.sub.4NO.sub.3), sodium nitrate (NaNO.sub.3), lithium nitrate
(LiNO.sub.3), calcium nitrate (Ca(NO.sub.3).sub.2), magnesium
nitrate (Mg(NO.sub.3).sub.2), strontium nitrate
(Sr(NO.sub.3).sub.2), calcium nitrate tetrahydrate
(Ca(NO.sub.3).sub.2.4H.sub.2O), copper (II) nitrate
(Cu(NO.sub.3).sub.2), iron (II) nitrate (Fe(NO.sub.3).sub.2), iron
(III) nitrate (Fe(NO.sub.3).sub.3), nickel (II) nitrate
(Ni(NO.sub.3).sub.2), and/or zinc nitrate (Zn(NO.sub.3).sub.2). In
some embodiments, at least one of the one or more additional salts
added to a concentrated brine stream comprising water and at least
one dissolved salt is different from the at least one dissolved
salt. In some embodiments, each of the one or more additional salts
added to the concentrated brine stream is different from the at
least one dissolved salt. In certain cases, at least one of the one
or more additional salts added to the concentrated brine stream is
the same as the at least one dissolved salt.
[0202] In some embodiments, the ultra-high-density concentrated
brine stream has a density (e.g., measured at about 60.degree. F.)
of at least about 11.7 pounds/gallon, at least about 12
pounds/gallon, at least about 12.5 pounds/gallon, at least about 13
pounds/gallon, at least about 13.2 pounds/gallon, at least about
13.5 pounds/gallon, at least about 14 pounds/gallon, at least about
14.5 pounds/gallon, at least about 15 pounds/gallon, at least about
20 pounds/gallon, or at least about 25 pounds/gallon. In certain
cases, the ultra-high-density concentrated brine stream has a
density (e.g., measured at about 60.degree. F.) in the range of
about 11.7 pounds/gallon to about 12.5 pounds/gallon, about 11.7
pounds/gallon to about 13 pounds/gallon, about 11.7 pounds/gallon
to about 13.2 pounds/gallon, about 11.7 pounds/gallon to about 13.5
pounds/gallon, about 11.7 pounds/gallon to about 14 pounds/gallon,
about 11.7 pounds/gallon to about 14.5 pounds/gallon, about 11.7
pounds/gallon to about 15 pounds/gallon, about 11.7 pounds/gallon
to about 20 pounds/gallon, about 11.7 pounds/gallon to about 25
pounds/gallon, about 12 pounds/gallon to about 12.5 pounds/gallon,
about 12 pounds/gallon to about 13 pounds/gallon, about 12
pounds/gallon to about 13.2 pounds/gallon, about 12 pounds/gallon
to about 13.5 pounds/gallon, about 12 pounds/gallon to about 14
pounds/gallon, about 12 pounds/gallon to about 14.5 pounds/gallon,
about 12 pounds/gallon to about 15 pounds/gallon, about 12
pounds/gallon to about 20 pounds/gallon, about 12 pounds/gallon to
about 25 pounds/gallon, about 12.5 pounds/gallon to about 13
pounds/gallon, about 12.5 pounds/gallon to about 13.2
pounds/gallon, about 12.5 pounds/gallon to about 13.5
pounds/gallon, about 12.5 pounds/gallon to about 14 pounds/gallon,
about 12.5 pounds/gallon to about 14.5 pounds/gallon, about 12.5
pounds/gallon to about 15 pounds/gallon, about 12.5 pounds/gallon
to about 20 pounds/gallon, about 12.5 pounds/gallon to about 25
pounds/gallon, about 13 pounds/gallon to about 13.2 pounds/gallon,
about 13 pounds/gallon to about 13.5 pounds/gallon, about 13
pounds/gallon to about 14 pounds/gallon, about 13 pounds/gallon to
about 14.5 pounds/gallon, about 13 pounds/gallon to about 15
pounds/gallon, about 13 pounds/gallon to about 20 pounds/gallon,
about 13 pounds/gallon to about 25 pounds/gallon, about 13.5
pounds/gallon to about 14 pounds/gallon, about 13.5 pounds/gallon
to about 14.5 pounds/gallon, about 13.5 pounds/gallon to about 15
pounds/gallon, about 13.5 pounds/gallon to about 20 pounds/gallon,
about 13.5 pounds/gallon to about 25 pounds/gallon, about 14
pounds/gallon to about 15 pounds/gallon, about 14 pounds/gallon to
about 20 pounds/gallon, about 14 pounds/gallon to about 25
pounds/gallon, about 15 pounds/gallon to about 20 pounds/gallon,
about 15 pounds/gallon to about 25 pounds/gallon, or about 20
pounds/gallon to about 25 pounds/gallon.
[0203] In some cases, the density of the ultra-high-density
concentrated brine stream is measured at a temperature of about
120.degree. F. or less, about 100.degree. F. or less, about
80.degree. F. or less, about 72.degree. F. or less, about
68.degree. F. or less, about 60.degree. F. or less, about
50.degree. F. or less, or about 40.degree. F. or less. In some
embodiments, the density of the ultra-high-density concentrated
brine stream is measured at a temperature of at least about
40.degree. F., at least about 50.degree. F., at least about
60.degree. F., at least about 68.degree. F., at least about
72.degree. F., at least about 80.degree. F., at least about
100.degree. F., or at least about 120.degree. F. In some
embodiments, the density of the ultra-high-density concentrated
brine stream is measured at a temperature in the range of about
40.degree. F. to about 120.degree. F., about 40.degree. F. to about
100.degree. F., about 40.degree. F. to about 80.degree. F., about
40.degree. F. to about 72.degree. F., about 40.degree. F. to about
68.degree. F., about 40.degree. F. to about 60.degree. F., about
40.degree. F. to about 50.degree. F., about 60.degree. F. to about
120.degree. F., about 60.degree. F. to about 100.degree. F., about
60.degree. F. to about 80.degree. F., about 60.degree. F. to about
72.degree. F., or about 60.degree. F. to about 68.degree. F.
[0204] In some embodiments, the water treatment system includes an
optional disinfection unit. The disinfection unit may be, for
example, a chlorination system configured to add chlorine to the
water. According to some embodiments, the disinfection unit can be
configured to receive at least a portion of a substantially pure
water stream produced by the desalination system.
[0205] In some embodiments, the water treatment system comprises an
optional precipitation apparatus. The precipitation apparatus may
be, in certain embodiments, fluidically connected to the
desalination system. In some such embodiments, the precipitation
apparatus is configured to receive at least a portion of a
concentrated brine stream output by the desalination system.
[0206] The precipitation apparatus is, in certain embodiments,
configured to precipitate at least a portion of the dissolved salt
(e.g., dissolved monovalent salt) from the concentrated brine
stream to produce a product stream containing less of the dissolved
salt relative to the concentrated brine stream.
[0207] The precipitation apparatus can be manufactured in any
suitable manner. In certain embodiments, the precipitation
apparatus comprises a vessel, such as a crystallization tank. The
vessel may include an inlet through which at least a portion of the
concentrated brine stream produced by the desalination system is
transported into the precipitation vessel. The precipitation vessel
may also include at least one outlet. For example, the
precipitation vessel may include an outlet through which the
substantially pure water stream (containing the dissolved salt in
an amount that is less than that contained in the inlet stream) is
transported. In some embodiments, the precipitation vessel includes
an outlet through which solid, precipitated salt is
transported.
[0208] In some embodiments, the crystallization tank comprises a
low shear mixer. The low shear mixer can be configured to keep the
crystals that are formed mixed (e.g., homogeneously mixed) in the
brine stream. According to certain embodiments, the vessel is sized
such that there is sufficient residence time for crystals to form
and grow. In certain embodiments, the precipitation apparatus
comprises a vessel which provides at least 20 minutes of residence
time for the concentrated brine stream. As one non-limiting
example, the vessel comprises, according to certain embodiments, a
6000 gallon vessel, which can be used to provide 24 minutes of
residence in a 500 US barrel per day fresh water production
system.
[0209] In some embodiments the crystallization tank is followed by
a storage tank. The storage tank may have, in some embodiments, a
capacity that is substantially the same as the capacity of the
crystallization tank. In certain embodiments, the crystallization
tank and/or the storage tank can be configured to accommodate batch
operation of the downstream solid handling apparatus, which can be
fluidically coupled to the precipitation apparatus.
[0210] In some embodiments, the precipitation apparatus comprises
at least one vessel comprising a volume within which the
concentrated brine stream is substantially quiescent. In some
embodiments, the flow rate of the fluid within the substantially
quiescent volume is less than the flow rate at which precipitation
(e.g., crystallization) is inhibited. For example, the flow rate of
the fluid within the substantially quiescent volume may have, in
certain embodiments, a flow rate of zero. In some embodiments, the
flow rate of the fluid within the substantially quiescent volume
may have a flow rate that is sufficiently high to suspend the
formed solids (e.g., crystals), but not sufficiently high to
prevent solid formation (e.g., crystal nucleation). The
substantially quiescent volume within the vessel may occupy, in
some embodiments, at least about 1%, at least about 5%, at least
about 10%, at least about 25%, at least about 50%, at least about
75%, at least about 90%, or at least about 100% of the volume of
the vessel. As one particular example, the precipitation apparatus
can comprise a vessel including a stagnation zone. The stagnation
zone may be positioned, for example, at the bottom of the
precipitation vessel. In certain embodiments, the precipitation
apparatus can include a second vessel in which the solids
precipitated in the first vessel are allowed to settle. For
example, an aqueous stream containing the precipitated solids can
be transported to a crystallization tank, where the solids can be
allowed to settle. The remaining contents of the aqueous stream can
be transported out of the crystallization tank. While the use of
two vessels within the precipitation apparatus has been described,
it should be understood that, in other embodiments, a single
vessel, or more than two vessels may be employed. In certain
embodiments, the desalination system can be operated such that
precipitation of the salt occurs substantially only within the
stagnation zone of the precipitation vessel. In certain
embodiments, the precipitation apparatus is directly fluidically
connected to the desalination system. It should be understood,
however, that the invention is not limited to embodiments in which
the precipitation apparatus and the desalination system are
directly fluidically connected, and in other embodiments, the
precipitation apparatus and the desalination system are fluidically
connected but are not directly fluidically connected.
[0211] In some embodiments, the precipitated salt from the
precipitation apparatus is fed to a solids-handling apparatus. The
solids-handling apparatus may be configured, in certain
embodiments, to remove at least a portion of the water retained by
the precipitated salt. In some such embodiments, the
solids-handling apparatus is configured to produce a cake
comprising at least a portion of the precipitated salt from the
precipitation apparatus. As one example, the solids-handling
apparatus can comprise a filter (e.g., a vacuum drum filter or a
filter press) configured to at least partially separate the
precipitated salt from the remainder of a suspension containing the
precipitated salt. In some such embodiments, at least a portion of
the liquid within the salt suspension can be transported through
the filter, leaving behind solid precipitated salt. As one
non-limiting example, a Larox FP 2016-8000 64/64 M40 PP/PP Filter
(Outotec, Inc.) may be used as the filter. The filter may comprise,
in certain embodiments, a conveyor filter belt which filters the
salt from a suspension containing the salt.
[0212] In some embodiments, the desalination system comprises a
transport device configured to transport precipitated salt away
from the precipitation apparatus. For example, in certain
embodiments, a pump is used to transport a suspension of the
precipitated salt away from the precipitation apparatus. In other
embodiments, a conveyor could be used to transport precipitated
salt away from the precipitation apparatus. In certain embodiments,
the transport device is configured to transport the precipitated
salt from the precipitation apparatus to a solids-handling
apparatus.
[0213] In certain embodiments, the water treatment system is
operated such that little or no brine is left to be disposed from
the system (also sometimes referred to as a "zero liquid discharge"
system). In some such embodiments, the system produces a salt
product and a fresh water product. The salt product can be
produced, for example, as a product of a crystallization or other
precipitation step.
[0214] Certain of the water treatments described herein comprise a
desalination system configured to remove water from an aqueous
stream to produce a concentrated brine stream enriched in a
dissolved salt relative to the aqueous stream received by the
desalination system. According to some embodiments, the
desalination system can be configured to produce a water-containing
stream that contains a lower concentration of the dissolved salt
than the stream fed to the desalination system (e.g., a
substantially pure water stream).
[0215] In some embodiments, water treatment systems and methods
described herein may be used to produce two or more product
streams. In some embodiments, a water treatment system may produce
a first stream comprising a first concentration of one or more
contaminants. In some embodiments, the water treatment system may
produce a second stream comprising a second concentration of the
one or more contaminants, wherein the second concentration is lower
than the first concentration.
[0216] In some embodiments, the desalination system is separate
from each of the separation apparatus, the suspended solids removal
apparatus, the ion-removal apparatus, the pH adjustment apparatus,
the VOM removal apparatus, and the filtration apparatus.
[0217] In some embodiments, the desalination system is fluidically
connected to one or more components of the clean brine system. In
certain embodiments, the desalination system is directly
fluidically connected to one or more components of the clean brine
system. The desalination system may be, in some cases, upstream or
downstream of one or more components of the clean brine system.
[0218] In some embodiments, for example, a desalination system can
be fluidically connected to a separation apparatus. In certain
cases, the desalination system is directly fluidically connected to
the separation apparatus. In some embodiments, the input stream
received by the desalination system comprises at least a portion of
the immiscible phase-diminished stream produced by the separation
apparatus. That is to say, in certain embodiments, the desalination
system is downstream of the separation apparatus. In other
embodiments, the input stream received by the separation apparatus
comprises at least a portion of the concentrated brine stream
and/or substantially pure water stream produced by the desalination
system. That is to say, in certain embodiments, the separation
apparatus can be located downstream of the desalination system.
[0219] In some embodiments, for example, a desalination system can
be fluidically connected to an ion-removal apparatus. In certain
cases, the desalination system is directly fluidically connected to
the ion-removal apparatus. In some embodiments, the input stream
received by the desalination system comprises at least a portion of
the ion-diminished stream produced by the ion-removal apparatus.
That is to say, in certain embodiments, the desalination system is
downstream of the ion-removal apparatus. In other embodiments, the
input stream received by the ion-removal apparatus comprises at
least a portion of the concentrated brine stream and/or
substantially pure water stream produced by the desalination
system. That is to say, in certain embodiments, the ion-removal
apparatus can be located downstream of the desalination system.
[0220] In some embodiments, for example, a desalination system can
be fluidically connected to a suspended solids removal apparatus.
In certain cases, the desalination system is directly fluidically
connected to the suspended solids removal apparatus. In some
embodiments, the input stream received by the desalination system
comprises at least a portion of the suspended-solids-diminished
stream produced by the suspended solids removal apparatus. That is
to say, in certain embodiments, the desalination system is
downstream of the suspended solids removal apparatus. In other
embodiments, the input stream received by the suspended solids
removal apparatus comprises at least a portion of the concentrated
brine stream and/or substantially pure water stream produced by the
desalination system. That is to say, in certain embodiments, the
suspended solids removal apparatus can be located downstream of the
desalination system.
[0221] In some embodiments, for example, a desalination system can
be fluidically connected to a pH adjustment apparatus. In certain
cases, the desalination system is directly fluidically connected to
the pH adjustment apparatus. In some embodiments, the input stream
received by the desalination system comprises at least a portion of
the pH-adjusted stream produced by the pH adjustment apparatus.
That is to say, in certain embodiments, the desalination system is
downstream of the pH adjustment apparatus. In other embodiments,
the input stream received by the pH adjustment apparatus comprises
at least a portion of the concentrated brine stream and/or
substantially pure water stream produced by the desalination
system. That is to say, in certain embodiments, the pH adjustment
apparatus can be located downstream of the desalination system.
[0222] In some embodiments, for example, a desalination system can
be fluidically connected to a VOM removal apparatus. In certain
cases, the desalination system is directly fluidically connected to
the VOM removal apparatus. In some embodiments, the input stream
received by the desalination system comprises at least a portion of
the VOM-diminished stream produced by the VOM removal apparatus.
That is to say, in certain embodiments, the desalination system is
downstream of the VOM removal apparatus. In other embodiments, the
input stream received by the VOM removal comprises at least a
portion of the concentrated brine stream and/or substantially pure
water stream produced by the desalination system. That is to say,
in certain embodiments, the VOM removal apparatus can be located
downstream of the desalination system.
Mixing Apparatus
[0223] In some embodiments, the water treatment system comprises an
optional mixing apparatus fluidically connected to the clean brine
system and the desalination system. A mixing apparatus generally
refers to a device configured to mix a first fluid with a second
fluid to form a fluid mixture (e.g., a substantially homogeneous
fluid mixture). In some embodiments, the mixing apparatus is
configured to receive at least a portion of a clean brine stream
from a clean brine system described herein. In some embodiments,
the mixing apparatus is also configured to receive at least a
portion of a substantially pure water stream from a desalination
system described herein. According to some embodiments, the mixing
apparatus is configured to mix at least a portion of the clean
brine stream and at least a portion of the substantially pure water
stream to form a mixed water stream.
[0224] In some embodiments, the mixed water stream has a mixing
ratio by mass of the substantially pure water stream to the clean
brine stream of at least about 1:1, at least about 2:1, at least
about 3:1, at least about 4:1, at least about 5:1, at least about
10:1, at least about 20:1, at least about 50:1, at least about
100:1, at least about 150:1, or at least about 200:1. In some
embodiments, the mixed water stream has a mixing ratio by mass of
the substantially pure water stream to the clean brine stream of
about 1:1 or less, about 1:2 or less, about 1:3 or less, about 1:4
or less, about 1:5 or less, about 1:10 or less, about 1:20 or less,
about 1:50 or less, about 1:100 or less, about 1:150 or less, or
about 1:200 or less. In certain cases, the mixed water stream has a
mixing ratio by mass of the substantially pure water stream to the
clean brine stream in the range of about 1:200 to about 200:1,
about 1:150 to about 150:1, about 1:100 to about 100:1, about 1:50
to about 50:1, about 1:20 to about 20:1, about 1:10 to about 10:1,
about 1:5 to about 5:1, or about 1:2 to about 2:1. In some
embodiments, the mixed water stream has a mixing ratio by mass of
the substantially pure water stream to the clean brine stream in
the range of about 1:1 to about 200:1, about 1:1 to about 150:1,
about 1:1 to about 100:1, about 1:1 to about 50:1, about 1:1 to
about 20:1, about 1:1 to about 10:1, about 1:1 to about 5:1, about
1:1 to about 4:1, about 1:1 to about 3:1, about 1:1 to about 2:1,
about 2:1 to about 5:1, about 2:1 to about 4:1, about 2:1 to about
3:1, about 3:1 to about 10:1, about 3:1 to about 5:1, or about 5:1
to about 10:1. The mixing ratio by mass may be calculated by
dividing the mass of the amount of substantially pure water by the
mass of the amount of clean brine in a mixed water stream.
[0225] In some embodiments, the concentration of at least one salt
(e.g., NaCl) in the mixed water stream is at least about 1,000
mg/L, at least about 2,000 mg/L, at least about 5,000 mg/L, at
least about 10,000 mg/L, at least about 20,000 mg/L, at least about
50,000 mg/L, at least about 100,000 mg/L, or at least about 150,000
mg/L. In some embodiments, the concentration of at least one salt
(e.g., NaCl) in the mixed water stream is about 150,000 mg/L or
less, about 100,000 mg/L or less, about 50,000 mg/L or less, about
20,000 mg/L or less, about 10,000 mg/L or less, about 5,000 mg/L or
less, about 2,000 mg/L or less, or about 1,000 mg/L or less. In
certain cases, the concentration of at least one salt in the mixed
water stream is in the range of about 1,000 mg/L to about 5,000
mg/L, about 1,000 mg/L to about 10,000 mg/L, about 1,000 mg/L to
about 15,000 mg/L, about 1,000 mg/L to about 20,000 mg/L, about
1,000 mg/L to about 50,000 mg/L, about 1,000 mg/L to about 100,000
mg/L, about 1,000 mg/L to about 150,000 mg/L, about 5,000 mg/L to
about 10,000 mg/L, about 5,000 mg/L to about 15,000 mg/L, about
5,000 mg/L to about 20,000 mg/L, about 5,000 mg/L to about 50,000
mg/L, about 5,000 mg/L to about 100,000 mg/L, about 5,000 mg/L to
about 150,000 mg/L, about 10,000 mg/L to about 20,000 mg/L, about
10,000 mg/L to about 50,000 mg/L, about 10,000 mg/L to about
100,000 mg/L, about 10,000 mg/L to about 150,000 mg/L, about 20,000
mg/L to about 50,000 mg/L, about 20,000 mg/L to about 100,000 mg/L,
about 20,000 mg/L to about 150,000 mg/L, about 50,000 mg/L to about
100,000 mg/L, or about 50,000 mg/L to about 150,000 mg/L.
[0226] In some embodiments, the total salt concentration in the
mixed water stream is at least about 10,000 mg/L, at least about
20,000 mg/L, at least about 50,000 mg/L, at least about 100,000
mg/L, at least about 110,000 mg/L, at least about 120,000 mg/L, at
least about 150,000 mg/L, or at least about 200,000 mg/L. In some
embodiments, the total salt concentration in the mixed water stream
is about 200,000 mg/L or less, about 150,000 mg/L or less, about
120,000 mg/L or less, about 100,000 mg/L or less, about 100,000
mg/L or less, about 50,000 mg/L or less, about 20,000 mg/L or less,
or about 10,000 mg/L or less. In certain cases, the total salt
concentration in the mixed water stream is in the range of about
10,000 mg/L to about 20,000 mg/L, about 10,000 mg/L to about 50,000
mg/L, about 10,000 mg/L to about 100,000 mg/L, about 10,000 mg/L to
about 110,000 mg/L, about 10,000 mg/L to about 120,000 mg/L, about
10,000 mg/L to about 150,000 mg/L, about 10,000 to about 200,000
mg/L, about 20,000 mg/L to about 50,000 mg/L, about 20,000 mg/L to
about 100,000 mg/L, about 20,000 mg/L to about 150,000 mg/L, about
20,000 to about 200,000 mg/L, about 50,000 mg/L to about 100,000
mg/L, about 50,000 mg/L to about 150,000 mg/L, or about 50,000 mg/L
to about 200,000 mg/L.
[0227] In some embodiments, the mixed water stream comprises at
least one salt (e.g., NaCl) in an amount of at least about 0.1 wt
%, at least about 0.5 wt %, at least about 1 wt %, at least about 2
wt %, at least about 5 wt %, at least about 10 wt %, or at least
about 15 wt % (and/or, in certain embodiments, up to the solubility
limit of the salt in the mixed water stream). In some embodiments,
the mixed water stream comprises at least one salt in an amount in
the range of about 0.1 wt % to about 1 wt %, about 0.1 wt % to
about 2 wt %, about 0.1 wt % to about 5 wt %, about 0.1 wt % to
about 10 wt %, about 0.1 wt % to about 15 wt %, about 1 wt % to
about 5 wt %, about 1 wt % to about 10 wt %, about 1 wt % to about
15 wt %, about 2 wt % to about 5 wt %, about 2 wt % to about 10 wt
%, about 2 wt % to about 15 wt %, about 5 wt % to about 10 wt %,
about 5 wt % to about 15 wt %, or about 10 wt % to about 15 wt
%.
[0228] In some embodiments, the mixed water stream has a total salt
concentration of at least about 1 wt %, at least about 5 wt %, at
least about 10 wt %, at least about 15 wt %, at least about 20 wt
%, at least about 25 wt %, at least about 26 wt %, at least about
27 wt %, at least about 28 wt %, at least about 29 wt %, or at
least about 30 wt %. In some embodiments, the mixed water stream
has a total salt concentration in the range of about 1 wt % to
about 10 wt %, about 1 wt % to about 20 wt %, about 1 wt % to about
25 wt %, about 1 wt % to about 26 wt %, about 1 wt % to about 27 wt
%, about 1 wt % to about 28 wt %, about 1 wt % to about 29 wt %,
about 1 wt % to about 30 wt %, about 10 wt % to about 20 wt %,
about 10 wt % to about 25 wt %, about 10 wt % to about 26 wt %,
about 10 wt % to about 27 wt %, about 10 wt % to about 28 wt %,
about 10 wt % to about 29 wt %, about 10 wt % to about 30 wt %,
about 20 wt % to about 25 wt %, about 20 wt % to about 26 wt %,
about 20 wt % to about 27 wt %, about 20 wt % to about 28 wt %,
about 20 wt % to about 29 wt %, about 20 wt % to about 30 wt %,
about 25 wt % to about 26 wt %, about 25 wt % to about 27 wt %,
about 25 wt % to about 28 wt %, about 25 wt % to about 29 wt %, or
about 25 wt % to about 30 wt %.
[0229] The mixing apparatus may be any type of mixing apparatus
known in the art. Non-limiting examples of suitable types of mixing
apparatuses include static inline mixers, stirred tanks (e.g.,
tanks comprising an agitator), eductors, venturi mixers, plate-type
mixers, and/or wafer inline static mixers.
Water Treatment System
[0230] FIG. 7 is a schematic diagram of an exemplary water
treatment system 700, according to certain embodiments. The water
treatment system shown in FIG. 7 includes a number of components
that can be used to treat an aqueous stream containing at least one
dissolved salt. According to FIG. 7, water treatment system 700
comprises optional separation apparatus 702 configured to receive
aqueous input stream 704 comprising a suspended and/or emulsified
immiscible phase. Optional separation apparatus 702 can be
configured to remove at least a portion of the suspended and/or
emulsified immiscible phase to produce immiscible-phase-diminished
stream 706, which contains less of the suspended and/or emulsified
immiscible phase than stream 704. Separation apparatus 702 can also
be configured to produce stream 705, which is enriched in the
suspended and/or emulsified water-immiscible phase relative to
stream 704.
[0231] In FIG. 7, system 700 further comprises optional suspended
solids removal apparatus 708, which can be configured to remove at
least a portion of suspended solids from input stream 706 to
produce a suspended-solids-diminished stream 710. Suspended solids
removal apparatus 708 can be configured to produce stream 709,
which is enriched in the suspended solids relative to stream
706.
[0232] According to FIG. 7, system 700 further comprises optional
ion-removal apparatus 712. Ion-removal apparatus 712 can be
configured, according to certain embodiments, to remove at least a
portion of at least one scale-forming ion from stream 710 received
by ion-removal apparatus 712. Ion-removal apparatus 712 can be
configured to produce ion-diminished stream 714, which contains
less of the scale-forming ion relative to input stream 710 received
by ion-removal apparatus 712. Ion-removal apparatus 712 can also be
configured to produce stream 713, which is enriched in at least one
scale-forming ion relative to stream 710.
[0233] In FIG. 7, system 700 includes optional pH adjustment
apparatus 716, which can be configured to receive aqueous input
stream 714, which can comprise scale-forming ions. pH adjustment
apparatus 716 can be configured to increase or decrease the pH of
aqueous input stream 714 to produce a pH-adjusted stream 718. In
certain cases, the pH of input stream 714 may be reduced to inhibit
the precipitation of scale-forming ions. In some cases, the pH of
input stream 714 can be increased or decreased, for example, by
adding chemicals via stream 717, according to some embodiments. For
example, an acidic composition can be added to the pH adjustment
apparatus to reduce the pH of stream 714, in certain
embodiments.
[0234] According to FIG. 7, system 700 further comprises optional
VOM removal apparatus 720. VOM removal apparatus 720 can be
configured to remove at least a portion of VOM from input stream
718 received by VOM removal apparatus 720 to produce a
VOM-diminished stream 722, which contains less of the VOM relative
to input stream 718 received by VOM removal apparatus 720. VOM
removal apparatus 720 can be configured to produce stream 721,
which is enriched in VOM relative to stream 718.
[0235] In FIG. 7, water treatment system 700 further comprises an
optional desalination system 724, which is configured to remove
water from aqueous stream 722 received by desalination system 724
to produce a concentrated brine stream 726 enriched in a dissolved
salt relative to aqueous stream 722 received by desalination system
724.
[0236] Water treatment system 700 may also comprise optional
precipitation apparatus 734. For example, in FIG. 7, precipitation
apparatus 734 is fluidically connected to desalination system 724
and configured to receive concentrated brine stream 726 from
desalination system 724. Precipitation apparatus 734 can be
configured such that at least a portion of the dissolved salt
within concentrated brine stream 726 precipitates within
precipitation apparatus 734 to produce water-containing product
stream 736, which contains less dissolved salt than concentrated
brine stream 726, and solid salt stream 738.
[0237] According to FIG. 7, water treatment system 700 can comprise
an optional disinfection unit 730. Disinfection unit 730 can be
configured to receive at least a portion of water-containing stream
725 from desalination system 724. In some embodiments, disinfection
unit 730 can be configured to receive disinfectant stream 731,
which can contain, for example, chlorine. Disinfection unit 730 can
be configured to produce disinfected water-containing stream
732.
[0238] FIG. 8 is a schematic illustration of an exemplary water
treatment system 800, according to certain embodiments. In FIG. 8,
aqueous input stream 804 is transported to optional tank 806. In
some embodiments, chemicals are added to optional tank 806 via
stream 808. The chemicals can be selected to aid in a downstream
apparatus, according to certain embodiments. For example, in some
embodiments, a skimmer (which can be part of a dissolved gas
flotation apparatus, for example) can be positioned downstream of
tank 806, and the chemicals added to tank 806 are selected to aid
in operation of the skimmer (e.g., in a dissolved gas flotation
process). Aqueous stream 810 can be transported out of tank 806.
Aqueous stream 810 can be transported to skimmer 814. In some
embodiments, skimmer 814 can be configured to remove at least a
portion of a suspended and/or emulsified water-immiscible phase
within stream 810 to produce an immiscible-phase-diminished stream
822 (and, in some embodiments, immiscible-phase-diminished stream
818). The water-immiscible phase from skimmer 814 can be
transported, for example, to a recovery tank 826 via stream 820. In
some embodiments, skimmer 814 is part of a dissolved gas flotation
apparatus. In some such embodiments, compressed gas (e.g., air) can
be added, via stream 812, to a tank containing the treated water,
which can aid in the transport of immiscible material to the top of
the tank. Gas can subsequently be transported out of the tank via
stream 816.
[0239] In some embodiments, ion-removal apparatus 828 can be
configured to receive at least a portion of
immiscible-phase-diminished stream 822. In some embodiments,
ion-removal apparatus 828 is configured to remove at least a
portion of scale-forming ions within stream 822 to produce an
ion-diminished stream 832. In some such embodiments, ion-removal
apparatus 828 produces ion-diminished stream 832 using a chemical
reagent. For example, in FIG. 8, chemical reagent can be
transported to ion-removal apparatus 828 via stream 830. The
chemical reagent can be, for example, soda ash, caustic soda, and
the like.
[0240] In certain embodiments, a portion of the
immiscible-phase-diminished stream produced by skimmer 814 can
bypass ion-removal apparatus 828. For example, in FIG. 8, at
portion of the immiscible-phase-diminished stream from skimmer 814
bypasses ion-removal apparatus 828 via stream 818. The contents of
bypass stream 818 may be merged with the contents of stream 832
downstream of ion-removal apparatus 828.
[0241] In some embodiments, a filter is configured to receive at
least a portion of the immiscible-phase-diminished stream and/or at
least a portion of the ion-diminished stream. For example, in FIG.
8, filter 834 is configured to received ion-diminished stream 832
and/or immiscible-phase-diminished stream 818. In certain
embodiments, filter 834 is configured to remove at least a portion
of suspended solids from the immiscible-phase-diminished stream
portion and/or the ion-diminished stream portion received by the
filter to produce a suspended-solids-diminished stream. For
example, in FIG. 8, filter 834 is configured to remove at least a
portion of suspended solids from stream 832 to produce
suspended-solids-diminished stream 838. In addition, in FIG. 8,
filter 834 is configured to produce solids-containing stream
836.
[0242] In certain embodiments, a pH adjustment step can be included
in the process. For example, in FIG. 8, optional tank 840 can be
configured to receive suspended-solids-diminished stream 838 and to
output pH-adjusted (e.g., pH-reduced) stream 844. Tank 840 can be
configured, in some embodiments, to receive an acid and/or a base
via stream 842. In some such embodiments, an acid and/or base may
be added to tank 840 until the pH of the contents of tank 840
reaches a desired level. According to certain embodiments, the
contents of tank 840 may be output via stream 844, once the pH has
reached a desired level. In certain embodiments, tank 840 is a
reactor, such as a continuous flow stirred tank reactor. In some
such embodiments, acid and/or base can be constantly fed at a rate
such that the reactor effluent reaches a desired pH level.
[0243] In some embodiments, optional filter 846 can be included in
the system. Filter 846 can be used to remove one or more solid
materials from pH-adjusted stream 844 to produce filtered stream
848.
[0244] According to certain embodiments, a carbon bed is configured
to receive at least a portion of the filtered stream. For example,
in FIG. 8, carbon bed 850 is configured to receive filtered stream
848 produced by filter 846. Carbon bed 850 can be configured to
remove at least a portion of VOM from the filtered stream portion
received by the carbon bed to produce a VOM-diminished stream. For
example, in FIG. 8, carbon bed 850 is configured to produce
VOM-diminished stream 852.
[0245] In some embodiments, a desalination system is configured to
receive at least a portion of the VOM-diminished stream and to
remove at least a portion of water from the VOM-diminished stream
received by the desalination system. For example, in FIG. 8
desalination system 854 is configured to receive VOM-diminished
stream 852. In addition, desalination system 854 is configured to
produce concentrated brine stream 856, which is enriched in at
least one dissolved salt (e.g., dissolved monovalent salt) relative
to VOM-diminished stream 852. In some embodiments, the desalination
system can also produce a water-containing stream that contains a
lower concentration of the dissolved salt (e.g., dissolved
monovalent salt) than the stream fed to the desalination system.
For example, in FIG. 8, desalination system 854 can be configured
to produce water-containing stream 858, which contains less of a
dissolved salt (e.g., less of a dissolved monovalent salt) than
stream 852 fed to desalination system 854.
[0246] In certain embodiments, the order of the desalination system
and the carbon bed can be switched, relative to the order shown in
FIG. 8. For example, in some embodiments, the desalination system
is configured to receive at least a portion of the
suspended-solids-diminished stream, and to remove at least a
portion of water from the suspended-solids-diminished stream
portion received by the desalination system to produce a
concentrated brine stream enriched in a dissolved salt relative to
the suspended-solids-diminished stream portion received by the
desalination system. The desalination system can also be configured
to produce a water-containing stream containing less of the
dissolved salt than the suspended-solids-diminished stream. In some
such embodiments, the carbon bed can be configured to receive at
least a portion of the water-containing stream produced by the
desalination system, and to remove at least a portion of VOM from
the water-containing stream portion received by the carbon bed to
produce a VOM-diminished stream.
[0247] FIG. 9 is a schematic illustration of another exemplary
water treatment system 900, according to certain embodiments. In
FIG. 9, aqueous input stream 904 is transported to optional tank
906. In some embodiments, chemicals are added to optional tank 906
via stream 908. The chemicals can be selected to aid in a
downstream apparatus, according to certain embodiments. For
example, in some embodiments, a skimmer (which can be part of a
dissolved gas flotation apparatus, for example) can be positioned
downstream of tank 906, and the chemicals added to tank 906 are
selected to aid in operation of the skimmer (e.g., in a dissolved
gas flotation process). Aqueous stream 910 can be transported out
of tank 906. Aqueous stream 910 can be transported to skimmer 914.
In some embodiments, skimmer 914 can be configured to remove at
least a portion of suspended and/or emulsified water-immiscible
phase within stream 910 to produce an immiscible-phase-diminished
stream 922 (and, in some embodiments, immiscible-phase-diminished
stream 918). The water-immiscible phase from skimmer 914 can be
transported, for example, to a recovery tank 926 via stream 920. In
some embodiments, skimmer 914 is part of a dissolved gas flotation
apparatus. In some such embodiments, compressed gas (e.g., air) can
be added, via stream 912, to a tank containing the treated water,
which can aid in the transport of immiscible material to the top of
the tank. Gas can subsequently be transported out of the tank via
stream 916.
[0248] In some embodiments, electrocoagulation apparatus 928 can be
configured to receive at least a portion of water-immiscible
phase-diminished stream 922. Electrocoagulation apparatus 928 can
be configured to remove at least a portion of scale-forming ions
within stream 922 to produce an ion-diminished stream 932.
[0249] In certain embodiments, a portion of water-immiscible
phase-diminished stream produced by skimmer 914 can bypass
electrocoagulation apparatus 928. For example, in FIG. 9, a portion
of the immiscible phase-diminished product from skimmer 914
bypasses electrocoagulation apparatus 928 via stream 918. The
contents of bypass stream 918 may be merged with the contents of
stream 932 downstream of electrocoagulation apparatus 928.
[0250] Filter 934 can be configured to receive ion-diminished
stream 932 and/or immiscible-phase-diminished stream 918. Filter
934 can be configured to remove at least a portion of suspended
solids from stream 932 to produce suspended-solids-diminished
stream 938. In addition, filter 934 can be configured to produce
solids-containing stream 936.
[0251] In certain embodiments, a pH adjustment step can be included
in the process. For example, in FIG. 9, optional tank 940 can be
configured to receive suspended-solids-diminished stream 938 and to
produce pH-adjusted stream 944. Optional tank 940 can be
configured, in some embodiments, to receive an acid and/or a base
via stream 942. In some such embodiments, an acid and/or base may
be added to tank 940 until the pH of the contents of tank 940
reaches a desired level. In certain embodiments, tank 940 is a
reactor, such as a continuous flow stirred tank reactor. In some
such embodiments, an acid and/or base can be constantly fed at a
rate such that the reactor effluent reaches a desired pH level.
According to certain embodiments, the contents of tank 940 may be
output via stream 944, once the pH has reached a desired level.
[0252] In some embodiments, optional filter 946 can be included in
the system. Filter 946 can be used to remove one or more solid
materials from pH-adjusted stream 944 to produce filtered stream
948.
[0253] Carbon bed 950 can be configured to receive filtered stream
948 produced by filter 946. Carbon bed 950 can be configured to
remove at least a portion of VOM from the filtered stream portion
received by the carbon bed to produce a VOM-diminished stream
952.
[0254] Desalination system 954 can be configured to receive
VOM-diminished stream 952. Desalination system 954 can be
configured to produce concentrated brine stream 956, which is
enriched in at least one dissolved salt (e.g., dissolved monovalent
salt) relative to VOM-diminished stream 952. Desalination system
954 can also be configured to produce water-containing stream 958,
which contains less of a dissolved salt (e.g., dissolved monovalent
salt) than stream 952 fed to desalination system 954.
[0255] In certain embodiments, the order of the desalination system
and the carbon bed can be switched, relative to the order shown in
FIG. 9. For example, in some embodiments, the desalination system
is configured to receive at least a portion of the
suspended-solids-diminished stream, and to remove at least a
portion of water from the suspended-solids-diminished stream
portion received by the desalination system to produce a
concentrated brine stream enriched in a dissolved salt (e.g.,
dissolved monovalent salt) relative to the
suspended-solids-diminished stream portion received by the
desalination system. The desalination system can also be configured
to produce a water-containing stream containing less of the
dissolved salt (e.g., dissolved monovalent salt) than the
suspended-solids-diminished stream. In some such embodiments, the
carbon bed can be configured to receive at least a portion of the
water-containing stream produced by the desalination system, and to
remove at least a portion of VOM from the water-containing stream
portion received by the carbon bed to produce a VOM-diminished
stream.
[0256] FIG. 10 is a schematic illustration of another exemplary
water treatment system 1000, according to certain embodiments. In
FIG. 10, aqueous input stream 1004 is transported to optional tank
1006. In some embodiments, chemicals are added to optional tank
1006 via stream 1008. The chemicals can be selected to aid in a
downstream apparatus, according to certain embodiments. For
example, in some embodiments, a skimmer (which can be part of a
dissolved gas flotation apparatus, for example) can be positioned
downstream of tank 1006, and the chemicals added to tank 1006 are
selected to aid in operation of the skimmer (e.g., in a dissolved
gas flotation process). Aqueous stream 1010 can be transported out
of tank 1006. Aqueous stream 1010 can be transported to skimmer
1014. In some embodiments, skimmer 1014 can be configured to remove
at least a portion of suspended and/or emulsified water-immiscible
phase within stream 1010 to produce an immiscible-phase-diminished
stream 1022 (and, in some embodiments, immiscible-phase-diminished
stream 1018). The water-immiscible phase from skimmer 1014 can be
transported, for example, to a recovery tank 1026 via stream 1020.
In some embodiments, skimmer 1014 is part of a dissolved gas
flotation apparatus. In some such embodiments, compressed gas
(e.g., air) can be added, via stream 1012, to a tank containing the
treated water, which can aid in the transport of immiscible
material to the top of the tank. Gas can subsequently be
transported out of the tank via stream 1016.
[0257] In certain embodiments, a portion of water-immiscible
phase-diminished stream produced by skimmer 1014 can be transported
to filter 1019, for example, via stream 1018. Filter 1019 can be
configured to remove at least a portion of suspended solids from
immiscible-phase-diminished stream portion 1018 received by filter
1019 to produce a suspended-solids-diminished stream 1024. Filter
1019 can also be configured to produce a solids-containing stream
1036.
[0258] In some embodiments, a portion of the water-immiscible
phase-diminished stream produced by skimmer 1014 can bypass filter
1019. For example, in FIG. 10, a portion 1022 of the immiscible
phase-diminished product from skimmer 1014 bypasses filter 1019 via
stream 1022. The contents of bypass stream 1022 may be merged with
the contents of stream 1024 downstream of filter 1019 and skimmer
1014 to produce stream 1023.
[0259] In certain embodiments, an optional pH adjustment step can
be included in the process. For example, in FIG. 10, optional tank
1040 can be configured to receive suspended-solids-diminished
stream 1023 and to produce pH-adjusted stream 1044. Optional tank
1040 can be configured, in some embodiments, to receive an acid
and/or a base via stream 1042. In some such embodiments, an acid
and/or base may be added to tank 1040 until the pH of the contents
of tank 1040 reaches a desired level. In certain embodiments, tank
1040 is a reactor, such as a continuous flow stirred tank reactor.
In some such embodiments, an acid and/or base can be constantly fed
at a rate such that the reactor effluent reaches a desired pH
level. According to certain embodiments, the contents of tank 1040
may be output via stream 1044, once the pH has reached a desired
level.
[0260] In some embodiments, media filter 1034 can be configured to
receive pH-adjusted stream 1044 (and/or suspended-solids-diminished
stream 1023). Media filter 1034 can be configured to remove at
least a portion of suspended solids from stream 1044 to produce
stream 1038.
[0261] In some embodiments, a carbon bed can be included in the
system. For example, referring to FIG. 10, carbon bed 1050 can be
configured to receive stream 1038, which contains at least a
portion of the stream produced by filter 1034. Carbon bed 1050 can
be configured to remove at least a portion of VOM from the stream
received by the carbon bed to produce a VOM-diminished stream
1052.
[0262] In some embodiments, a resin bed can be included in the
system. For example, in FIG. 10, resin bed 1060 can be configured
to receive at least a portion of VOM-diminished stream 1052. Resin
bed 1060 can be configured to remove at least a portion of at least
one scale-forming ion from VOM-diminished stream portion 1052
received by resin bed 1060 to produce ion-diminished stream 1062
containing less of the scale-forming ion relative to input stream
1052 received by resin bed 1060.
[0263] In some embodiments, desalination system 1054 can be
configured to receive ion-diminished stream 1062. Desalination
system 1054 can be configured to produce concentrated brine stream
1056, which is enriched in at least one dissolved salt (e.g.,
monovalent salt) relative to ion-diminished stream 1062.
Desalination system 1054 can also be configured to produce
water-containing stream 1058, which contains less of a dissolved
salt (e.g., a dissolved monovalent salt) than stream 1062 fed to
desalination system 1054.
[0264] In certain embodiments, the order of the desalination system
and the carbon bed can be switched, relative to the order shown in
FIG. 10. For example, in some embodiments, the desalination system
is configured to receive at least a portion of the
suspended-solids-diminished stream, and to remove at least a
portion of water from the suspended-solids-diminished stream
portion received by the desalination system to produce a
concentrated brine stream enriched in a dissolved salt relative to
the suspended-solids-diminished stream portion received by the
desalination system. The desalination system can also be configured
to produce a water-containing stream containing less of the
dissolved salt than the suspended-solids-diminished stream. In some
such embodiments, the carbon bed can be configured to receive at
least a portion of the water-containing stream produced by the
desalination system, and to remove at least a portion of VOM from
the water-containing stream portion received by the carbon bed to
produce a VOM-diminished stream.
[0265] Certain of the systems described herein can be configured to
desalinate saline solutions entering at relatively high flow rates,
and accordingly, can be configured to produce relative pure water
streams at relatively high flow rates. For example, in some
embodiments, the systems and methods described herein may be
operated to receive an aqueous saline feed stream (e.g., streams
104 in FIG. 1, 804 in FIG. 8, 904 in FIG. 9, and/or 1004 in FIG.
10) at a flow rate of at least about 1 gallon/minute, at least
about 10 gallons/minute, at least about 100 gallons/minute, or at
least about 1000 gallons/minute (and/or, in certain embodiments, up
to about 10,000 gallons/minute, or more).
EXAMPLE 1
[0266] In this example, a water treatment system comprising a clean
brine system, a desalination system, and a mixing apparatus is
described.
[0267] As shown in FIG. 1, water treatment system 100 comprises
clean brine system 102, humidification-dehumidification
desalination system 110, and mixing apparatus 116. In operation,
saline water input stream 104 (e.g., a produced water stream)
having a dissolved NaCl concentration of 140,000 ppm enters clean
brine system 102 at a flow rate of 12,000 barrels/day. In clean
brine system 102, a first clean brine stream 106 having a dissolved
NaCl concentration of 140,000 ppm is produced at a rate of 4,000
barrels/day. A second clean brine stream 108, which has a lower
concentration of at least one scale-forming ion than first clean
brine stream 106, is produced at a rate of about 8,000 barrels/day
and is fed into desalination system 110. In desalination system
110, at least a portion of water is removed from clean brine stream
108 to produce a substantially pure water stream 112 and a
concentrated brine stream 114. Substantially pure water stream 112,
which has a dissolved NaCl concentration of less than about 500
ppm, is produced at a rate of about 4,000 barrels/day. Concentrated
brine stream 114, which has a dissolved NaCl concentration of
260,000 ppm, is produced at a rate of about 4,000 barrels/day.
Approximately 1,000 barrels/day of first clean brine stream 106 are
mixed with about 3,000 barrels/day of substantially pure water
stream 112 in mixing apparatus 116 to produce about 4,000
barrels/day of mixed water product 118 having a dissolved NaCl
concentration of about 35,000 ppm.
EXAMPLE 2
[0268] In this example, a water treatment system as in Example 1
was used to treat produced water from Midland, Tex. and obtain
clean brine for direct use, clean brine for desalination,
substantially pure water, and concentrated brine. Table 1 lists the
concentrations of various constituents of the different water
streams. Concentrations for a mixed water product comprising 3:1
pure water to clean brine for direct use were estimated based on
the concentrations obtained for substantially pure water and clean
brine for direct use. In Table 1, ND stands for "not detected." To
calculate hardness, the molar concentration of various divalent
ions was measured, then mg/L concentration was calculated as if
each of those ions were a calcium ion.
[0269] FIG. 11 shows a schematic diagram of the clean brine system
used. As shown in FIG. 11, clean brine system 1100 comprised buffer
tanks 1102A and 1102B, reaction tanks 1104A, 1104B, and 1104C,
clarifier 1106, polishing filter 1108, resin beds 1110, pH
adjustment tank 1112, holding tank 1114, and filter 1116. In
operation, aqueous feed stream 1118 (e.g., produced water) was
pumped to buffer tanks 1102A and 1102B, each of which had a height
of about 15 feet and a volume of about 3,000 gallons. The presence
of buffer tanks 1102A and 1102B assisted in mitigating any
unsteadiness in the flow rate of aqueous feed stream 1118. In
buffer tanks 1102A and 1102B, a small amount of floating oil was
removed by a belt oil skimmer. The residence time of aqueous feed
stream 1118 in buffer tanks 1102A and 1102B was about 10 minutes.
From buffer tanks 1102A and 1102B, a stream 1120 was directed to
first reaction tank 1104A. In first reaction tank 1104A, soda ash
and a coagulant comprising barium chloride were added to stream
1120 to produce stream 1122. The coagulant comprising barium
chloride was added to precipitate sulfate ions present in the
stream as barium sulfate. Stream 1122 was then directed to flow to
second reaction tank 1104B. In second reaction tank 1104B, caustic
soda was added to stream 1122 to produce stream 1124. Stream 1124
was then directed to flow to third reaction tank 1104C, where a
polymer flocculent was added to stream 1124 to produce stream 1126.
Stream 1126 was directed to flow to clarifier 1106. Clarifier 1106
was a lamella plate clarifier configured to remove solids by
settling. An amount of oil was also removed (e.g., through
entrapment of oil droplets by solid precipitates, through adhesion
of oil droplets with solid precipitates as a result of collisions).
As a result, clarifier 1106 produced a solid-diminished stream 1128
and a solid-containing stream 1130.
[0270] Solid-diminished stream 1128 was directed to flow to
polishing filter 1108 to further remove solids from stream 1128 and
produce filtered stream 1134. In this embodiment, the polishing
filter was a multi-media filter. When too many particles collected
in filter 1108, flow through filter 1108 slowed, and filter 1108
was automatically cleaned by backwashing. In the backwashing
process, clean brine and hydrochloric acid were flushed through
filter 1108 in opposite directions, fluidizing and suspending the
media and freeing collected particles. Backwash was reintroduced
into the aqueous stream upstream of filter 1108.
[0271] Filtered stream 1134 was then directed to flow to
ion-exchange resin beds 1110 to form stream 1136. Stream 1136 was
then flowed to pH adjustment tank 1112. In pH adjustment tank 1112,
hydrochloric acid was added to stream 1136 to produce pH-adjusted
stream 1138, which had a pH around 7. During the precipitation step
in reaction tanks 1104A-C, the pH was raised to 10 or 11 to
decrease the solubility of calcium carbonate and magnesium
hydroxide.
[0272] In one case, at least a portion of pH-adjusted stream 1138
was discharged from system 1100 as a clean brine stream for reuse.
In another case, at least a portion of pH-adjusted stream 1138 was
subsequently flowed to a humidification-dehumidification
desalination system to produce a substantially pure water stream
and a concentrated brine stream. Significantly less (or
substantially no) soda ash was added to the produced water to
produce the clean brine stream for reuse compared to the amount of
soda ash added to produce the clean brine stream for desalination.
The concentrations of various constituents in the clean brine for
reuse, clean brine for desalination, substantially pure water, and
concentrated brine are shown in Table 1.
[0273] Solid-containing stream 1130 produced by clarifier 1106 was
initially directed to flow from clarifier 1106 to holding tank
1114, and then from holding tank 1114 to filter 1116. Filter 1116
was a rotary vacuum drum filter comprising a round drum covered in
a filter cloth. Diatomaceous earth was applied to the filter cloth
as a precoat to aid filtration. The drum, covered in diatomaceous
earth, was partially submerged in solid-containing stream 1130 and
rotated slowly. A vacuum was applied to the interior of the drum,
causing liquid to be drawn through the drum and solid material to
form a cake around the outside of the drum. What the cake was
sufficiently large, it was removed by scraping with a stationary
blade. This process resulted in substantially solid material
1132.
TABLE-US-00001 TABLE 1 Clean Clean Brine Produced Brine for for
Pure Concentrated Mixed Constituent Water Reuse Desalination Water
Brine Water Barium 3.78 mg/L 16.1 mg/L 6.55 mg/L 0.017 mg/L 1.51
mg/L 4.04 mg/L Bromide 1390 mg/L 1360 mg/L 1350 mg/L 2.78 mg/L 3960
mg/L 342 mg/L Calcium 2350 mg/L 1720 mg/L 121 mg/L 1.85 mg/L 345
mg/L 431 mg/L Chloride 70100 mg/L 76400 mg/L 65800 mg/L 130 mg/L
159000 mg/L 19200 mg/L Sulfate 282 mg/L 222 mg/L 255 mg/L ND 710
mg/L 55.5 mg/L Magnesium 375 mg/L 359 mg/L ND ND 61.6 mg/L 89.8
mg/L Oil & 22.5 mg/L ND ND ND ND ND Grease Sodium 41700 mg/L
43100 mg/L 46000 mg/L 89.3 mg/L 96400 mg/L 10800 mg/L Strontium 712
mg/L 586 mg/L 101 mg/L 0.379 mg/L 277 mg/L 147 mg/L Benzene 1960
.mu.g/L 1560 .mu.g/L 88.4 .mu.g/L ND ND 390 .mu.g/L Toluene 1230
.mu.g/L 929 .mu.g/L 50.8 .mu.g/L ND ND 232 .mu.g/L pH 6.55 7.15
7.75 8.18 5.55 8.03 Hardness 7420 mg/L 5780 mg/L 303 mg/L 4.61 mg/L
1120 mg/L 1450 mg/L expressed as mg/L Ca.sup.2+ Total 125000 mg/L
121000 mg/L 113000 mg/L 234 mg/L 320000 mg/L 30400 mg/L Dissolved
Solids Total 535 mg/L 410 mg/L 246 mg/L ND 636 mg/L 102.5 mg/L
Suspended Solids
[0274] While several embodiments of the present invention have been
described and illustrated herein, those of ordinary skill in the
art will readily envision a variety of other means and/or
structures for performing the functions and/or obtaining the
results and/or one or more of the advantages described herein, and
each of such variations and/or modifications is deemed to be within
the scope of the present invention. More generally, those skilled
in the art will readily appreciate that all parameters, dimensions,
materials, and configurations described herein are meant to be
exemplary and that the actual parameters, dimensions, materials,
and/or configurations will depend upon the specific application or
applications for which the teachings of the present invention
is/are used. Those skilled in the art will recognize, or be able to
ascertain using no more than routine experimentation, many
equivalents to the specific embodiments of the invention described
herein. It is, therefore, to be understood that the foregoing
embodiments are presented by way of example only and that, within
the scope of the appended claims and equivalents thereto, the
invention may be practiced otherwise than as specifically described
and claimed. The present invention is directed to each individual
feature, system, article, material, and/or method described herein.
In addition, any combination of two or more such features, systems,
articles, materials, and/or methods, if such features, systems,
articles, materials, and/or methods are not mutually inconsistent,
is included within the scope of the present invention.
[0275] The indefinite articles "a" and "an," as used herein in the
specification and in the claims, unless clearly indicated to the
contrary, should be understood to mean "at least one."
[0276] The phrase "and/or," as used herein in the specification and
in the claims, should be understood to mean "either or both" of the
elements so conjoined, i.e., elements that are conjunctively
present in some cases and disjunctively present in other cases.
Other elements may optionally be present other than the elements
specifically identified by the "and/or" clause, whether related or
unrelated to those elements specifically identified unless clearly
indicated to the contrary. Thus, as a non-limiting example, a
reference to "A and/or B," when used in conjunction with open-ended
language such as "comprising" can refer, in one embodiment, to A
without B (optionally including elements other than B); in another
embodiment, to B without A (optionally including elements other
than A); in yet another embodiment, to both A and B (optionally
including other elements); etc.
[0277] As used herein in the specification and in the claims, "or"
should be understood to have the same meaning as "and/or" as
defined above. For example, when separating items in a list, "or"
or "and/or" shall be interpreted as being inclusive, i.e., the
inclusion of at least one, but also including more than one, of a
number or list of elements, and, optionally, additional unlisted
items. Only terms clearly indicated to the contrary, such as "only
one of" or "exactly one of," or, when used in the claims,
"consisting of," will refer to the inclusion of exactly one element
of a number or list of elements. In general, the term "or" as used
herein shall only be interpreted as indicating exclusive
alternatives (i.e. "one or the other but not both") when preceded
by terms of exclusivity, such as "either," "one of," "only one of,"
or "exactly one of." "Consisting essentially of," when used in the
claims, shall have its ordinary meaning as used in the field of
patent law.
[0278] As used herein in the specification and in the claims, the
phrase "at least one," in reference to a list of one or more
elements, should be understood to mean at least one element
selected from any one or more of the elements in the list of
elements, but not necessarily including at least one of each and
every element specifically listed within the list of elements and
not excluding any combinations of elements in the list of elements.
This definition also allows that elements may optionally be present
other than the elements specifically identified within the list of
elements to which the phrase "at least one" refers, whether related
or unrelated to those elements specifically identified. Thus, as a
non-limiting example, "at least one of A and B" (or, equivalently,
"at least one of A or B," or, equivalently "at least one of A
and/or B") can refer, in one embodiment, to at least one,
optionally including more than one, A, with no B present (and
optionally including elements other than B); in another embodiment,
to at least one, optionally including more than one, B, with no A
present (and optionally including elements other than A); in yet
another embodiment, to at least one, optionally including more than
one, A, and at least one, optionally including more than one, B
(and optionally including other elements); etc.
[0279] In the claims, as well as in the specification above, all
transitional phrases such as "comprising," "including," "carrying,"
"having," "containing," "involving," "holding," and the like are to
be understood to be open-ended, i.e., to mean including but not
limited to. Only the transitional phrases "consisting of" and
"consisting essentially of" shall be closed or semi-closed
transitional phrases, respectively, as set forth in the United
States Patent Office Manual of Patent Examining Procedures, Section
2111.03.
[0280] In cases where the present specification and a document
incorporated by reference, attached as an appendix, and/or referred
to herein include conflicting disclosure, and/or inconsistent use
of terminology, and/or the incorporated/appended/referenced
documents use or define terms differently than they are used or
defined in the present specification, the present specification
shall control.
* * * * *