U.S. patent application number 17/061279 was filed with the patent office on 2021-01-21 for reverse osmosis system for use with a wellbore and methods of assembling the same.
The applicant listed for this patent is BL Technologies Inc.. Invention is credited to Hareesh Kumar Reddy KOMMEPALLI, Andrew Philip SHAPIRO, Hua WANG.
Application Number | 20210016227 17/061279 |
Document ID | / |
Family ID | 1000005123650 |
Filed Date | 2021-01-21 |
View All Diagrams
United States Patent
Application |
20210016227 |
Kind Code |
A1 |
WANG; Hua ; et al. |
January 21, 2021 |
REVERSE OSMOSIS SYSTEM FOR USE WITH A WELLBORE AND METHODS OF
ASSEMBLING THE SAME
Abstract
A reverse osmosis unit for processing a feed solution is
provided. The unit includes a pressure vessel includes an inlet
end, an outlet end, and a vessel body extending between the inlet
end and the outlet end. The reverse osmosis unit further includes a
plurality of first membrane modules positioned within the pressure
vessel. Each first membrane module of the plurality of first
membrane modules has a first salt permeance value. At least one
second membrane module is positioned within the pressure vessel and
coupled in flow communication to the plurality of first membrane
modules. The at least one second membrane module has a second salt
permeance value that is different from the first salt permeance
value.
Inventors: |
WANG; Hua; (Clifton Park,
NY) ; KOMMEPALLI; Hareesh Kumar Reddy; (Albany,
NY) ; SHAPIRO; Andrew Philip; (Schenectady,
NY) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
BL Technologies Inc. |
Minnetonka |
MN |
US |
|
|
Family ID: |
1000005123650 |
Appl. No.: |
17/061279 |
Filed: |
October 1, 2020 |
Related U.S. Patent Documents
|
|
|
|
|
|
Application
Number |
Filing Date |
Patent Number |
|
|
15125294 |
Sep 12, 2016 |
10828605 |
|
|
PCT/US2015/020448 |
Mar 13, 2015 |
|
|
|
17061279 |
|
|
|
|
61952674 |
Mar 13, 2014 |
|
|
|
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
B01D 61/02 20130101;
B01D 61/08 20130101; B01D 61/022 20130101; B01D 2317/02 20130101;
C02F 1/441 20130101; C02F 2209/005 20130101; B01D 2317/00 20130101;
E21B 43/20 20130101; B01D 61/025 20130101; C02F 1/008 20130101 |
International
Class: |
B01D 61/02 20060101
B01D061/02; B01D 61/08 20060101 B01D061/08; C02F 1/44 20060101
C02F001/44; E21B 43/20 20060101 E21B043/20; C02F 1/00 20060101
C02F001/00 |
Claims
1. A reverse osmosis unit for processing a feed solution, said unit
comprising: a pressure vessel comprising an inlet end, an outlet
end, and a vessel body extending between said inlet end and said
outlet end; a plurality of first membrane modules positioned within
said pressure vessel, each first membrane module of said plurality
of first membrane modules comprising a first salt permeance value;
and at least one second membrane module positioned within said
pressure vessel and coupled in flow communication to said plurality
of first membrane modules, said at least one second membrane module
comprising a second salt permeance value that is different from
said first salt permeance value by a difference of at least about
0.4.times.10.sup.-5 cm/sec.
2. The reverse osmosis unit of claim 1 wherein said second salt
permeance value is greater than said first salt permeance
value.
3. The reverse osmosis unit of claim 1 wherein said at least one
second membrane module is configured to facilitate processing the
permeate having a salinity of at least about 500 parts per
million.
4. The reverse osmosis unit of claim 1 wherein said at least one
said second membrane module is positioned within said pressure
vessel and between said inlet end and said plurality of first
membrane modules.
5. The reverse osmosis unit of claim 1 further comprising at least
one third membrane module coupled in flow communication to at least
one of said first membrane module and said second membrane module
and comprising a third salt permeance value which is greater than
said first salt permeance value and said second salt permeance
value.
6. The reverse osmosis unit of claim 1 wherein said plurality of
first membrane modules and said at least one second module comprise
at least one of spiral-wound configuration and a hollow fiber
configuration.
7. A reverse osmosis system for processing a feed solution, said
system comprising: a pump configured to discharge the feed
solution; and a first reverse osmosis unit coupled to said pump and
comprising: a pressure vessel coupled in flow communication to said
pump and configured to receive the feed solution, said pressure
vessel comprising an inlet end, an outlet end, and a vessel body
extending between said inlet end and said outlet end; a plurality
of first membrane modules positioned within said pressure vessel,
each first membrane module of said plurality of first membrane
modules comprising a first salt permeance value; and at least one
second membrane module positioned within said pressure vessel and
coupled in flow communication to said plurality of first membrane
modules, said at least one second membrane module comprising a
second salt permeance value that is different from said first salt
permeance value, the plurality of first membrane modules and the at
least one second membrane module are configured to process the feed
solution into a permeate having a salinity of at least about 500
parts per million.
8. The reverse osmosis system of claim 7 further comprising a
computing device coupled to said pump and configured to control
said pump to selectively discharge said feed solution into said
pressure vessel at least one of an adjustable flow rate and a
pressure rate.
9. The reverse osmosis system of claim 7 wherein said plurality of
first membrane modules and said at least one second membrane module
are coupled in flow communication together in series within the
pressure vessel.
10. The reverse osmosis system of claim 7 further comprising a
second reverse osmosis unit coupled in flow communication to said
first reverse osmosis unit and comprising a permeate-staged
unit.
11. The reverse osmosis system of claim 7 further comprising a
second reverse osmosis unit coupled in flow communication to said
first reverse osmosis unit and comprising a brine-staged unit.
12. A method of manufacturing a reserve osmosis unit for processing
a feed solution, said method comprising: positioning a pressure
vessel comprising an inlet end, an outlet end, and a vessel body
extending between the inlet end and the outlet end; coupling a
plurality of first membrane modules to the pressure vessel, each
first membrane module of the plurality of first membrane modules
comprising a first salt permeance value; and coupling at least one
second membrane module in flow communication to the plurality of
first membrane modules, the at least one second membrane module
comprising a second salt permeance value that is different from the
first salt permeance value by a difference of at least about
0.4.times.10.sup.-5 cm/sec.
13. The method of claim 12 further comprising coupling at least one
third membrane module in flow communication to at least one of the
plurality of first membrane modules and the at least one second
membrane module, the at least one third membrane module comprising
a third permeance value which is greater than the first salt
permeance value and the second salt permeance value.
14. The method of claim 12 wherein coupling the at least one second
membrane module comprises coupling the at least one second membrane
module between the inlet end and the plurality of first membrane
modules.
15. The method of claim 12 wherein coupling the at least one second
membrane module comprises coupling the at least one second membrane
module between the outlet end and the plurality of first membrane
modules.
16. A method of processing a feed solution, said method comprising:
discharging the feed solution into a pressure vessel comprising an
inlet end, an outlet end, and comprising a first membrane module
and a second membrane module coupled in series between the inlet
end and the outlet end; discharging the feed solution into the
first membrane module comprising a first salt permeance value and
configured to desalinate the feed solution into a first permeate
and a first concentrate; and discharging the first concentrate into
the second membrane module comprising a second salt permeance value
that is different from the first salt permeance value and
configured to desalinate the first concentrate into a second
permeate and a second concentrate wherein a collective permeate of
the first permeate and the second permeate has a salinity of at
least about 500 parts per million.
17. The method of claim 16 further comprising discharging the
concentrate into at least one third membrane module comprising a
third permeance value which is greater than the first salt
permeance value and the second salt permeance value.
18. A method of processing a feed solution into, said method
comprising: discharging the feed solution into a pressure vessel
comprising an inlet end, an outlet end, and comprising a first
membrane module and a second membrane module coupled in series
between the inlet end and the outlet end; discharging the feed
solution into the second membrane module comprising a second salt
permeance value and configured to desalinate the feed solution into
a permeate and a concentrate; and discharging the concentrate into
the first membrane module comprising a first salt permeance value
that is different from the second salt permeance value and
configured to desalinate the concentrate into another permeate and
another concentrate wherein a collective permeate of the permeate
and other permeate has a salinity of at least about 500 parts per
million.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application is a divisional of U.S. application Ser.
No. 15/125,294, filed Sep. 12, 2016, which is a National Stage
Entry of International Application No. PCT/US2015/020448, filed
Mar. 13, 2015, which is a non-provisional application of U.S.
Application Ser. No. 61/952,674, filed Mar. 13, 2014. Application
Ser. No. 15/125,294; PCT/US2015/020448; and 61/952,674 are
incorporated herein by reference.
BACKGROUND
[0002] The embodiments described herein relate generally to reverse
osmosis systems, and more particularly, to methods and systems for
recovering hydrocarbons from a porous subterranean geological
formation using a permeate generated by the reverse osmosis
systems.
[0003] In oil and/or gas wells, production fluid such as petroleum
can be recovered from a reservoir of a geological formation as a
result of the natural pressure of the reservoir. Due to a decline
in reservoir pressure, some enhanced recovery processes may be used
to extract more of the production fluid out of the geological
formation. Water-flooding is a common enhanced recovery process
wherein water is injected, under pressure, into the reservoir
forcing the production fluid from the geological formation and into
the well. Injection water may be supplied from rivers and aquifers
for land based wells and from water for offshore wells.
[0004] In some secondary recovery processes, controlled salinity of
the injection water may increase efficiency of the enhanced
recovery process. Moreover, low salinity water-flooding may
increase the efficiency of other chemical and/or polymer enhanced
recovery processes and may provide cost savings by reducing
chemical composition of the injection water. Depending on reservoir
factors such as, but not limited to, rock mineralogy, formation
water chemistry, production fluid composition, surface chemistry,
formation pressure and formation temperature, an optimal salinity
percentage of the injection water may be needed for specific
reservoirs.
[0005] Current reverse osmosis systems may produce water meeting
potable water requirements such as salinity having a range of 10 to
500 parts per million ("ppm"). For efficient and economical
enhanced recovery processes, however, an optimal salinity of over
500 ppm may be needed. Moreover, for reservoirs having different
fluid characteristics, controllable and/or adjustable salinity
amounts may be needed for suitable enhanced recovery processes.
BRIEF SUMMARY
[0006] In one aspect, a reverse osmosis unit for processing a feed
solution is provided. The unit includes a pressure vessel having an
inlet end, an outlet end, and a vessel body extending between the
inlet end and the outlet end. The reverse osmosis unit further
includes a plurality of first membrane modules positioned within
the pressure vessel. Each first membrane module of the plurality of
first membrane modules has a first salt permeance value. At least
one second membrane module is positioned within the pressure vessel
and coupled in flow communication to the plurality of first
membrane modules. The at least one second membrane module has a
second salt permeance value that is different from the first salt
permeance value.
[0007] In another aspect, a reverse osmosis system for processing a
feed solution is provided. The system includes a pump configured to
discharge the feed solution and a pressure vessel coupled in flow
communication to the pump and configured to receive the feed
solution. The pressure vessel includes an inlet end, an outlet end,
and a vessel body extending between the inlet end and the outlet
end. The reverse osmosis unit further includes a plurality of first
membrane modules positioned within the pressure vessel. Each first
membrane module of the plurality of first membrane modules has a
first salt permeance value. At least one second membrane module is
positioned within the pressure vessel and coupled in flow
communication to the plurality of first membrane modules. The at
least one second membrane module has a second salt permeance value
that is different from the first salt permeance the plurality of
first membrane modules and the at least one second membrane module
are configured to process the feed solution into a permeate having
a salinity of at least about 500 parts per million.
[0008] Still further, in one aspect, a method of manufacturing a
reserve osmosis unit for processing a feed solution is provided.
The method includes positioning a pressure vessel having an inlet
end, an outlet end, and a vessel body extending between the inlet
end and the outlet end. A plurality of first membrane modules is
coupled to the pressure vessel, each first membrane module of the
plurality of first membrane modules has a first salt permeance
value. The method includes coupling at least one second membrane
module in flow communication to the plurality of first membrane
modules, the at least one second membrane module has a second salt
permeance value that is different from the first salt permeance
value by a difference of at least about 0.4.times.10.sup.-5
cm/sec.
[0009] In one aspect, a method of processing a feed solution is
provided. The method includes discharging the feed solution into a
pressure vessel having an inlet end and an outlet end. The pressure
vessel further includes a first membrane module and a second
membrane module coupled in series between the inlet end and the
outlet end. The method includes discharging the feed solution into
the first membrane module having a first salt permeance value and
configured to desalinate the, fed solution into a first permeate
and a first concentrate. The method includes discharging the first
concentrate into the second membrane module having a second salt
permeance value that is different from the first salt permeance
value and configured to desalinate the first concentrate into a
second permeate and a second concentrate, wherein a collective
permeate of the first permeate and the second permeate has a
salinity of at least about 500 parts per million.
[0010] In another aspect, a method of processing a feed solution is
provided. The method includes discharging the feed solution into a
pressure vessel includes an inlet end and an outlet end. The
pressure vessel further includes a first membrane module and a
second membrane module coupled in series between the inlet end and
the outlet end. The method includes discharging the feed solution
into the second membrane module having a second salt permeance
value and configured to desalinate the feed solution into the a
permeate and a concentrate. The method includes discharging the
concentrate into the first membrane module having a first salt
permeance value that is different from the second salt permeance
value and configured to desalinate the concentrate into another
permeate and another concentrate, wherein a collective permeate of
the permeate and other permeate has a salinity of at least about
500 parts per million.
[0011] In one aspect, a method of processing a feed solution is
provided. The method includes discharging the feed solution into a
pressure vessel having an inlet end and an outlet end. The pressure
vessel further includes a first membrane module, a second membrane
module, and a third membrane module coupled in series between the
inlet end and the outlet end. The method includes discharging the
feed solution into the first membrane module having a first salt
permeance value and configured to desalinate the feed solution into
a first permeate and a first concentrate. The method includes
discharging the first concentrate into the second membrane module
having a second salt permeance value that is different from the
first salt permeance value and configured to desalinate the first
concentrate into a second permeate and a second concentrate. The
method includes discharging the second concentrate into the third
membrane modules having a third salt permeance value which is
greater than the first salt permeance value and the second salt
permeance value, the third membrane module configured to desalinate
the second concentrate into a third concentrate and a third
permeate, wherein a collective permeate of the first permeate, the
second permeate, and the third permeate has a salinity of at least
about 500 parts per million.
[0012] Still further, in one aspect, a method of recovering a
hydrocarbon fluid from a formation reservoir is provided. The
method includes discharging the feed solution into a pressure
vessel having an inlet end and an outlet end. The pressure vessel
further includes a first membrane module and a second membrane
module coupled in series between the inlet end and the outlet end.
The method includes discharging the feed solution into the first
membrane module having a first salt permeance value and configured
to desalinate the feed solution into a first permeate and a second
permeate. The method includes discharging the first concentrate
into the second membrane module having a second salt permeance
value that is different from the first salt permeance value and
configured to desalinate the first concentrate into a second
permeate and a second concentrate, wherein a collective permeate of
the first permeate and the second permeate has a salinity of at
least about 500 parts per million. The method includes controllably
discharging at least a portion of the collective permeate having
the salinity of at least about 500 parts per million into the
formation reservoir. The method includes forcing the hydrocarbon
fluid from the formation reservoir under pressure of the collective
permeate and into a well casing.
DRAWINGS
[0013] These and other features, aspects, and advantages will
become better understood when the following detailed description is
read with reference to the accompanying drawings in which like
characters represent like parts throughout the drawings, where:
[0014] FIG. 1 is a cross-sectional side view of a well assembly
having an exemplary reverse osmosis system coupled to a wellbore
via a wellhead;
[0015] FIG. 2 is a schematic view of the reverse osmosis system
shown in FIG. 1;
[0016] FIG. 3 is a schematic view of an exemplary arrangement of a
pressure vessel of reverse osmosis system shown in FIG. 2, the
pressure vessel having a plurality of first membrane modules and a
second membrane modules;
[0017] FIG. 4 is a schematic view of an alternative arrangement of
the pressure vessel having the plurality of first membrane modules
and second membrane module;
[0018] FIG. 5 is a schematic view of another alternative
arrangement of the pressure vessel having the plurality of first
membrane modules and the second membrane modules;
[0019] FIG. 6 is a schematic view of yet another alternative
arrangement of the pressure vessel having the plurality of first
membrane modules and the second membrane modules;
[0020] FIG. 7 is a schematic view of a further alternative
arrangement of the pressure vessel having the plurality of first
membrane modules, the second membrane modules, and a third membrane
module;
[0021] FIG. 8 illustrates another alternative arrangement of the
pressure vessel having the first membrane modules and second
membrane modules coupled in series within the pressure vessel of
the reverse osmosis system shown in FIG. 1;
[0022] FIG. 9 illustrates yet another alternative arrangement of
the pressure vessel having the first membrane modules and the
second membrane modules coupled in series within the pressure
vessel;
[0023] FIG. 10 illustrates another alternative arrangement of the
pressure vessel having the first membrane modules and the second
membrane modules coupled in series within the pressure vessel;
[0024] FIG. 11 illustrates another alternative arrangement of the
pressure vessel having the first membrane modules, the second
membrane modules, and a third membrane module coupled in series
within the pressure vessel;
[0025] FIG. 12 illustrates yet another alternative arrangement of
the pressure vessel having the first membrane modules, the second
membrane modules, and the third membrane modules coupled in series
within the pressure vessel;
[0026] FIG. 13 is a schematic of another alternative reverse
osmosis unit;
[0027] FIG. 14 is a schematic of another alternative reverse
osmosis unit;
[0028] FIG. 15 is a flowchart illustrating an exemplary method of
assembling the reverse osmosis system shown in FIG. 1 for
processing a feed solution;
[0029] FIG. 16 is a flowchart illustrating an exemplary method of
processing a feed solution into a permeate and a concentrate by the
reverse osmosis unit shown in FIG. 1;
[0030] FIG. 17 is a flowchart illustrating an alternative method of
processing a feed solution into a permeate and a concentrate by the
reverse osmosis unit shown in FIG. 1;
[0031] FIG. 18 is a flowchart illustrating an alternative method of
processing a feed solution into a permeate and a concentrate by the
reverse osmosis unit shown in FIG. 1; and
[0032] FIG. 19 is a flowchart illustrating an exemplary method of
recovering a hydrocarbon fluid from a formation reservoir.
[0033] Unless otherwise indicated, the drawings provided herein are
meant to illustrate features of embodiments of the disclosure.
These features are believed to be applicable in a wide variety of
systems comprising one or more embodiments of the disclosure. As
such, the drawings are not meant to include all conventional
features known by those of ordinary skill in the art to be required
for the practice of the embodiments disclosed herein.
DETAILED DESCRIPTION
[0034] In the following specification and the claims, reference
will be made to a number of terms, which shall be defined to have
the following meanings. The singular forms "a", "an", and "the"
include plural references unless the context clearly dictates
otherwise. "Optional" or "optionally" means that the subsequently
described event or circumstance may or may not occur, and that the
description includes instances where the event occurs and instances
where it does not.
[0035] Approximating language, as used herein throughout the
specification and claims, may be applied to modify any quantitative
representation that could permissibly vary without resulting in a
change in the basic function to which it is related. Accordingly, a
system modified by a term or terms, such as "about" and
"substantially", are not to be limited to the precise system
specified. Here and throughout the specification and claims, range
limitations may be combined and/or interchanged, such ranges are
identified and include all the sub-ranges contained therein unless
context or language indicates otherwise.
[0036] As used herein, the term "computer" and related terms, e.g.,
"computing device", are not limited to integrated circuits referred
to in the art as a computer, but broadly refers to a
microcontroller, a microcomputer, a programmable logic controller
(PLC), an application specific integrated circuit, and other
programmable circuits, and these terms are used interchangeably
herein. Further, as used herein, the terms "software" and
"firmware" are interchangeable, and include any computer program
stored in memory for execution by personal computers, workstations,
clients and servers.
[0037] As used herein, the term "non-transitory computer-readable
media" is intended to be representative of any tangible
computer-based device implemented in any method or technology for
short-term and long-term storage of information, such as,
computer-readable instructions, data structures, program modules
and sub-modules, or other data in any device. Therefore, the
methods described herein may be encoded as executable instructions
embodied in a tangible, non-transitory, computer readable medium,
including, without limitation, a storage device and/or a memory
device. Such instructions, when executed by a processor, cause the
processor to perform at least a portion of the methods described
herein. Moreover, as used herein, the term "non-transitory
computer-readable media" includes all tangible, computer-readable
media, including, without limitation, non-transitory computer
storage devices, including, without limitation, volatile and
nonvolatile media, and removable and non-removable media such as a
firmware, physical and virtual storage, CD-ROMs, DVDs, and any
other digital source such as a network or the Internet, as well as
yet to be developed digital means, with the sole exception being a
transitory, propagating signal.
[0038] The embodiments described herein relate to systems and
methods for performing a reverse osmosis process on an aqueous feed
solution to form a permeate for use in a well casing. More
particularly, the embodiments described herein enhance recovery of
production fluid from a geological formation. The embodiments also
relate to methods, systems, and/or apparatus for desalinating the
aqueous feed solution to form a permeate having a salinity range of
at least 1000 parts per million ("ppm") to facilitate improvement
of well production performance. It should be understood that the
embodiments described herein include a variety of types of well
assemblies, and further understood that the descriptions and
figures that utilize hydrocarbon formations are exemplary only. The
exemplary reverse osmosis system is configured to be a hybrid,
controllable reverse osmosis desalination system to produce
desalinated water with controlled salinity for low salinity
water-flooding to facilitate enhanced production fluid
recovery.
[0039] FIG. 1 is a cross-sectional side view of a well assembly 10
having an exemplary reverse osmosis system 12 coupled to a wellbore
14 via a wellhead 16. Reverse osmosis system 12 is configured to
process a feed solution 18 into a permeate 20 and concentrate 22.
For reverse osmosis system 12, fluid pressure is applied to the
high solute concentration side of a membrane to force flow of
solvent across the membrane, from high solute concentration side to
lower solute concentration side, which produces a purified solvent
solution. In the exemplary embodiments, the term "reverse osmosis"
includes both "tight" reverse osmosis, where all salts are
substantially rejected by the reverse osmosis membrane, and "loose"
reverse osmosis, where some salts such as, for example only,
monovalent salts, are substantially passed while other salts such
as, for example only, divalent salts, are selectively rejected by
the membrane. Both "tight" and "loose" reverse osmosis are based on
the same principal in that pressure is applied to the membrane to
overcome an osmotic pressure difference and forces solvent through
a membrane. Loose reverse osmosis may be known as
nanofiltration.
[0040] Reverse osmosis system 12 is configured to discharge
permeate 20 within wellbore 14 which is associated with a
geological formation 28 containing desirable production fluid 30,
such as, but not limited to, petroleum. Wellbore 14 is drilled into
geological formation 28 and lined with a well casing 32. Well
casing 32 includes an inner sidewall 34, an outer sidewall 36, and
a casing bore 38 defined by inner sidewall 34. Well casing 32 may
be positioned in any orientation within geological formation 28 to
enable reverse osmosis system 12 to function as described herein A
plurality of perforations 40 is formed through well casing 32 to
permit fluid 30 to flow from geological formation 28 and into well
casing 32.
[0041] Reverse osmosis system 12 is coupled, via a communication
wire 26, to a computing device 42 for use in analyzing fluid
characteristics 44 of feed solution 18, permeate 20, and
concentrate 22. Fluid characteristics 44 include, but are not
limited to, pressures 46, flow rates 48, fluid compositions 50, and
temperatures 52. Computing device 42 includes a processor 54 and a
memory 56. Processor 54 includes a processing unit, such as,
without limitation, an integrated circuit (IC), an application
specific integrated circuit (ASIC), a microcomputer, a programmable
logic controller (PLC), and/or any other programmable circuit.
Processor 54 may include multiple processing units (e.g., in a
multi-core configuration). Computing device 42 is configurable to
perform the operations described herein by programming processor
54. For example, processor 54 may be programmed by encoding an
operation as one or more executable instructions and providing the
executable instructions to processor 54 in memory 56 coupled to
processor 54. Memory 56 includes, without limitation, one or more
random access memory (RAM) devices, one or more storage devices,
and/or one or more computer readable media. Memory 56 is configured
to store data, such as computer-executable instructions. Memory 56
includes any device allowing instruction 58, such as executable
instructions and/or other data, to be stored and retrieved.
[0042] Stored in memory 56 are, for example, readable instructions
provided by for a user (not shown). Computing device 42 further
includes a user interface 60 and a presentation device 62. User
interface 60 may include, among other possibilities, a web browser
and/or a client application. Web browsers and client applications
enable users to display and interact with media and other
information. Exemplary client applications include, without
limitation, a software application for managing one or more
computing devices 42.
[0043] Computing device 42 includes at least one presentation
device 62 for presenting information to the user. Presentation
device 62 is any component capable of conveying information to the
user. Presentation device 62 includes, without limitation, a
display device (not shown) (e.g., a liquid crystal display (LCD),
organic light emitting diode (OLED) display, or "electronic ink"
display) and/or an audio output device (e.g., a speaker or
headphones). Presentation device 62 includes an output adapter (not
shown), such as a video adapter and/or an audio adapter. Output
adapter is operatively coupled to processor 54 and configured to be
operatively coupled to an output device (not shown), such as a
display device or an audio output device.
[0044] Moreover, computing device 42 includes input device 64 for
receiving input from the user. Input device 64 includes, for
example, a keyboard, a pointing device, a mouse, a stylus, a touch
sensitive panel (e.g., a touch pad or a touch screen), a gyroscope,
an accelerometer, a position detector, and/or an audio input
device. A single component, such as a touch screen, may function as
both an output device of presentation device 62 and input device
64. Computing device 42 can be communicatively coupled to a network
(not shown).
[0045] FIG. 2 is a schematic view of reverse osmosis system 12.
Reverse osmosis system 12 can include a land base system, a
subterranean system, an offshore platform system, and an underwater
system (none shown). Reverse osmosis system 12 can include any
configuration to enable desalinization of feed solution 18. Reverse
osmosis system 12 includes a feed solution source 66 such as, but
not limited to, a storage tank, a pipe line, an aquifer, and sea
water. A pump 68 is coupled in flow communication to feed solution
source 66. Feed solution source 66 is configured to hold and direct
an amount of feed solution 18 to pump 68. Reverse osmosis system 12
may further include other components such as, but not limited to,
pretreatment units, media filtration units, cartridge filtration
units, micro-filtration units, and ultra-filtration units. Reverse
osmosis system 12 further includes a reverse osmosis unit 70 having
a pressure vessel 74. Although four pressure vessels 74 are shown,
any number of pressure vessels 74 may be used. Each pressure vessel
74 includes an inlet end 76, an outlet end 78, and a vessel body 72
extending between inlet end 76 and outlet end 78. In an alternative
embodiment, a membrane housing 73 may enclose a plurality of
pressure vessels 74. Inlet end 76 is coupled in flow communication
to pump 68 and outlet end 78 is coupled in flow communication to
well casing 32 via wellhead 16 (both shown in FIG. 1).
Alternatively, inlet ends 76 may be coupled to outlet ends 78
and/or vice versa among the plurality of pressure vessels 74.
Moreover, each pressure vessel 74 includes another outlet end 80
coupled in flow communication to a concentrate storage 82 such as,
but not limited to, a storage tank, a piping system and/or a
discharge outlet. Outlet end 78 is configured to discharge permeate
20 out of pressure vessel 74 and into a well casing 32 (shown in
FIG. 1). Outlet end 80 is configured to discharge concentrate 22
from pressure vessel 74. In the exemplary embodiment, a plurality
of first membrane modules 84 is positioned within pressure vessel
74. Moreover, at least one second membrane module 86 is positioned
within pressure vessel 74.
[0046] In the exemplary embodiment, a permeate flux Jw through
reverse osmosis unit 70 is obtained from Eq. 1:
J.sub.w=ATCF(.DELTA.P-.DELTA..pi.) (Eq. 1)
where J.sub.w is a permeate 20 flux, A is the water permeance, or
"A-value" (with units of 10.sup.-5 cm.sup.2/cm.sup.2-s-atm), at
standard temperature of 25.degree. C., TCF is a temperature
correction factor for the water permeance, .DELTA.P is the
transmembrane pressure drop, and .DELTA..pi. is the osmotic
pressure difference across reverse osmosis unit 70. A salt flux Js
is given by Eq. 2:
J.sub.s=BTCF(C.sub.sf . . . C.sub.sp) (Eq. 2)
where B is a salt permeance, or "B-value" (with units of 10.sup.-5
cm/s), and C.sub.sf and C.sub.sp are the salt concentrations in
feed solutions and permeate solutions, respectively. A salt passage
SP and rejection R are calculated by Eqs. 3 and 4:
Salt passage SP = C sp C sf .times. 100 % , and ( Eq . 3 ) Salt
Rejection R = ( 1 - C sp C sf ) .times. 100 % ( Eq . 4 )
##EQU00001##
[0047] In the exemplary embodiment, each first membrane module 84
and second membrane module 86 include asymmetric membranes prepared
from a single polymeric material. Asymmetric membranes include a
dense polymeric discriminating layer supported on a porous support
formed from the same polymeric material. Alternatively, each first
membrane module 84 and second membrane module 86 may include
thin-film composite membranes prepared from a first and a second
polymeric material. Examples include asymmetric cellulose acetate
membranes. Thin-film composite membranes comprise a permselective
discriminating layer formed from a first polymeric material
anchored onto a porous support material formed from a second
polymeric material. The permselective discriminating layer includes
cross-linked polymeric material, for example, a cross-linked
aromatic polyamide. The porous support material includes a
polysulfone. Polyamide thin-film composite membranes have higher
water fluxes, salt and organic rejections and can withstand higher
temperatures and larger pH variations than asymmetric cellulose
acetate membranes. Moreover, the polyamide thin-film composite
membranes are also less susceptible to biological attack and
compaction. First membrane modules 84 and second membrane module 86
are configured to reduced and/or eliminate significant amounts of
dissolved solids from entering the treated low salinity water
concentrate stream while allowing the water solvent to pass. In the
exemplary embodiment, first membrane modules 84 and second membrane
module 86 include a spiral wound membrane located within pressure
vessel 74. Alternatively, first membrane module 84 and second
membrane module 86 can include a hollow fiber configuration.
Alternatively, first membrane 84 and second membrane 86 can include
reverse osmosis membrane and/or nanofiltration membranes. Still
farther, in an alternative embodiment, first membrane 84 and second
membrane 86 can include membranes that are configured to process
monovalent ions and/or divalent ions. First membrane modules 84 and
second membrane module 86 may include any membrane configuration to
enable reverse osmosis unit 70 to function as described herein.
[0048] The plurality of first membrane modules 84 and second
membrane module 86 are selectively arranged within pressure vessel
74 and with respect to each other to facilitate desalinating feed
solution 18 into permeate 20 and concentrate 22. Each first
membrane module 84 of the plurality of first membrane modules 84
has a first salt permeance value 88. Second membrane module 86 has
a second salt permeance value 90 that is different than first salt
permeance value. In the exemplary embodiment, the second salt
permeance value 90 is greater than first salt permeance value 88.
More particularly, second salt permeance value 90 is greater than
first salt permeance value 88 by a difference of at least about
0.4.times.10.sup.-5 cm/sec. Still further, in the exemplary
embodiment, second salt permeance value is greater than first salt
permeance value 88 by a difference having a range from about
0.4.times.10.sup.-5 cm/sec to 300.times.10.sup.-5 cm/sec.
Alternatively, second salt permeance value 90 may be less than
first salt permeance value 88. First salt permeance value 88 and
second salt permeance value 90 can include any value to enable
reverse osmosis system 12 to function as described herein.
[0049] The selective arrangement of the plurality of first membrane
modules 84 and second membrane module 86 within pressure vessel 74
and the difference between first salt permeance value 88 and second
salt permeance value 90 are configured to facilitate processing
wherein permeate 20 has a salinity of at least about 500 ppm as
described herein. More particularly, reverse osmosis unit 70 is
configured to process wherein permeate 20 has salinity from a range
from about 500 ppm to about 10,000 ppm. Still further, in the
exemplary embodiment, reverse osmosis unit 70 is configured to
process permeate 20 to have salinity having a range from about
10,000 ppm to about 30,000 ppm. Alternatively, reverse osmosis unit
70 is configured to process wherein permeate 20 has salinity of
less than 500 ppm and/or more than 30,000 ppm. Reverse osmosis unit
70 is configured to process permeate 20 to have any salinity amount
to facilitate enhancing recovery process from geological
formation.
[0050] In the exemplary embodiment, reverse osmosis of unit 70
includes at least one third membrane module 92 positioned within
pressure vessel 74 and selectively arranged among the plurality of
first membrane modules 84 and second membrane module 86. Third
membrane module 92 has a third salt permeance value 94 that is
different than first salt permeance value 88 and/or second salt
permeance value 90. In the exemplary embodiment, third salt
permeance value 94 is greater than first salt permeance value 88
and/or second salt permeance value 90. The selective arrangement of
the plurality of first membrane module 84, second membrane module
86, and third membrane module 92 and the differences between first
salt permeance value 88, second salt permeance value 90, and third
salt permeance value 94 facilitate processing wherein permeate 20
has a salinity of at least about 500 ppm as described herein.
[0051] During operation, computer device 42 is configured to
selectively activate pump 68 to discharge feed solution 18 from
feed solution source 66 into inlet end 76 of pressure vessel 74.
While pumping feed solution 18, computing device 42, via sensors
(not shown), monitors, measures, and/or analyzes fluid
characteristics 44 of feed solution 18 and adjust pressure rate 46
and/or flow rate 48 of feed solution 18 through pump 68. Computing
device 42 can control pump 68 to adjust and/or tune pressure rate
46 and/or flow rate 48 of feed solution 18 to predetermined
perimeters to facilitate desalinating feed solution 18. Pump 68
discharges feed solution 18 into pressure vessel 74. Inlet end 76
directs feed solution 18 into the plurality of first membrane
modules 84. First membrane modules 84, based at least on first salt
permeance value 88, removes salt 96 from feed solution 18 to form a
first permeate 23 and a first concentrate 25. After passing through
first membrane modules 84, first concentrate 25 is desalinated and
directed into second membrane module 86. Second membrane module 86,
based at least on second salt permeance value 90, removes
additional salt 96 to form a second permeate 27 and a second
concentrate 29. Collective permeate 20 which includes a combination
of first permeate 23 and second permeate 27 has a salinity of about
at least about 500 ppm. Outlet end 78 directs collective permeate
20 through wellhead 16 (shown in FIG. 1) and into well casing 32
(shown in FIG. 1) for enhanced recovery processes.
[0052] FIG. 3 is a schematic view of an arrangement 98 of pressure
vessel 74 having the plurality of first membrane modules 84 and
second membrane module 86. In the exemplary embodiment, second
membrane module 86 is positioned within pressure vessel 74 and
between inlet end 76 and the plurality of first membrane modules
84. Moreover, first membrane modules 84 and second membrane module
86 are coupled in series. Arrangement 98 is configured to
desalinate feed solution 18 into concentrate 22 and permeate 20,
wherein permeate 20 has salinity of at least about 500 ppm. More
particularly, during operation, inlet end 76 discharges feed
solution 18 initially into and through second membrane module 86,
and subsequently, concentrate 22 into and through the plurality of
first membrane modules 84.
[0053] FIG. 4 is a schematic view of an alternative arrangement 100
of pressure vessel 74 having the plurality of first membrane
modules 84 and second membrane module 86. In FIG. 4, similar
components include the same element numbers as is shown in FIGS.
1-3. In the exemplary embodiment, second membrane module 86 is
positioned within pressure vessel 74 and between outlet end 78 and
the plurality of first membrane modules 84. Moreover, first
membrane modules 84 and second membrane module 86 are coupled in
series. Arrangement 100 is configured to desalinate feed solution
18 into concentrate 22 and permeate 20, wherein permeate 20 has
salinity of at least about 500 ppm. More particularly, during
operation, inlet end 76 discharges feed solution 18 initially into
and through the plurality of first membrane modules 84, and
subsequently, concentrate 22 into and through second membrane
module 86.
[0054] FIG. 5 is a schematic view of an alternative arrangement 102
of pressure vessel 74 having the plurality of first membrane
modules 84 and second membrane modules 86. In FIG. 5 similar
components include the same element numbers as shown in FIGS. 1-4.
In the exemplary embodiment, second membrane module 86 is
positioned within pressure vessel 74 and between a pair of first
membrane modules 84 of the plurality of first membrane modules 84.
Moreover, first membrane modules 84 and second membrane module 86
are coupled in series. Arrangement 102 is configured to desalinate
feed solution 18 into concentrate 22 and permeate 20, wherein
permeate 20 has salinity of at least of about 500 ppm. More
particularly, during operation, inlet end 76 discharges feed
solution 18 initially into and through first membrane module 84,
and subsequently, concentrate 22 into and through second membrane
module 86. After passing through second membrane module 86,
concentrate 22 is discharged into subsequent first membrane modules
84.
[0055] FIG. 6 is a schematic view of an alternative arrangement 104
of pressure vessel 74 having the plurality of first membrane
modules 84 and second membrane modules 86. In FIG. 6 similar
components include the same element numbers as shown in FIGS. 1-5.
In the exemplary embodiment, a plurality of second membrane modules
86 is positioned within pressure vessel 74 and between a pair of
first membrane modules 84 of the plurality of first membrane
modules 84. Moreover, first membrane modules 84 and second membrane
module 86 are coupled in series. Arrangement 104 is configured to
desalinate feed solution 18 into concentrate 22 and permeate 20,
wherein permeate 20 has salinity of at least of about 500 ppm. More
particular, during operation, inlet end 76 discharges feed solution
18 initially into and through first membrane modules 84, and
subsequently, concentrate 22 into and through second membrane
modules 86. After passing through second membrane modules 86,
concentrate 22 is discharged into subsequent first membrane modules
84.
[0056] FIG. 7 is a schematic view of an alternative arrangement 106
of pressure vessel 74 having the plurality of first membrane
modules 84, second membrane modules 86, and third membrane module
92. In FIG. 7, similar components have the same element numbers as
shown in FIGS. 1-6. In the exemplary embodiment, secondary modules
86 are positioned within pressure vessel 74 and among the plurality
of first membrane modules 84. Moreover, first membrane modules 84
and second membrane module 86 are coupled in series. Moreover,
third membrane module 92 is positioned in series within pressure
vessel 74 and between second membrane modules 86 and outlet end.
More particularly, third membrane module 92 is positioned between
second membrane module 86 and subsequent first membrane modules 84.
Arrangement 106 is configured to desalinate feed solution 18 into
concentrate 22 and permeate 20, wherein permeate 20 has salinity of
at least of about 500 ppm, More particularly, during operation,
inlet end 76 discharges feed solution 18 initially into and through
first membrane modules 84. First membrane module 84 is configured
to desalinate feed solution 18 into first permeate 23 and first
concentrate 25. First concentrate 25 is discharged into second
membrane module 86 which is configured to desalinate first
concentrate 25 into second permeate 27 and second concentrate 29.
Second concentrate 29 is discharged into third membrane module 92
which is configured to desalinate second concentrate 29 into third
permeate 31 and third concentrate 33. Collective permeate 20 which
includes a combination of at least one of first permeate 23, second
permeate 27, and third permeate 31 has a salinity of at least about
500 ppm. Alternatively, third membrane module 92 may be positioned
between inlet end 76 and first membrane module 84 and/or second
membrane module 86.
[0057] Table 1 illustrates properties of first membrane modules 84,
second membrane modules 86, and third membrane modules 92 used in
the exemplary arrangements shown in FIGS. 8-12. In the exemplary
embodiments, water permeate values and salt permeate values are
measured at standard seawater reverse osmosis testing conditions
such as, but not limited to, 35,000 ppm NaCl, 25.degree. C., 800
psi, pH 8.0 and 8% recovery.
TABLE-US-00001 TABLE 1 Water Permeate value Salt Permeate value
Membrane (10.sup.-5 cm.sup.3/cm.sup.2-s-atm) (10.sup.-5 cm/s) First
Membrane 4 0.4 Module 84 Second membrane 6.8 6 module 86 Third
membrane 7.2 12 module 92
EXAMPLE 1: FIG. 8
[0058] FIG. 8 illustrates an alternative arrangement 108 of
pressure vessel 74 having first membrane modules 84 and second
membrane modules 86 coupled in series within pressure vessel 74.
Although a single pressure vessel 74 is shown in FIG. 8,
arrangement 108 includes thirty pressure vessels 74 (not shown)
position in parallel. In the exemplary embodiment, each pressure
vessel 74 includes five first membrane modules 84 having first salt
permeance value 88 of 0.4.times.10.sup.-5 cm/s. First membrane
modules 84 are positioned in series and adjacent inlet end 76.
Arrangement 108 further includes two second membrane modules 86
having second salt permeance value 90 of 6.times.10.sup.-3 cm/s.
Second membrane modules 86 are positioned between first membrane
modules 84 and outlet end 78. Feed solution 18 includes sea water
having fluid characteristics 44 such as, but not limited to, total
dissolved solids ("TDS") of 35,000 ppm, 25.degree. C., and
transmembrane pressure of 755 psi. Arrangement 108 is configured to
desalinate feed solution 18 into concentrate 22 and permeate 20,
wherein permeate 20 has salinity of about 1,442 ppm.
EXAMPLE 2: FIG. 9
[0059] FIG. 9 illustrates an alternative arrangement 110 of
pressure vessel 74 having first membrane modules 84 and second
membrane modules 86 coupled in series within pressure vessel 74.
Although a single pressure vessel 74 is shown in FIG. 9,
arrangement 110 includes thirty pressure vessels 74 (not shown)
positioned in parallel. In the exemplary embodiment, each pressure
vessel 74 includes four first membrane modules 84 having first salt
permeance value 88 of 0.4.times.10.sup.-5 cm/s. First membrane
modules 84 are positioned in series and adjacent inlet end 76.
Arrangement 110 further includes two second membrane modules 86 in
series having second salt permeance value 90 of 6.times.10.sup.-5
cm/s. Second membrane modules 86 are positioned between first
membrane modules 84 and outlet end 78. Arrangement 110 further
includes a single first membrane module having first salt permeance
value 88 of 0.4.times.10.sup.-5 cm/s. Single first membrane module
84 is positioned between second membrane modules 86 and outlet end
78. Feed solution 18 includes sea water having fluid
characteristics 44, such as, but not limited to, TDS of 35,000 ppm,
25.degree. C. and transmembrane pressure of 766 psi. Arrangement
110 is configured to desalinate feed solution 18 into concentrate
22 and permeate 20, wherein permeate 20 has salinity of about 1,433
ppm.
EXAMPLE 3: FIG. 10
[0060] FIG. 10 illustrates an alternative arrangement 112 of
pressure vessel 74 having first membrane modules 84 and second
membrane modules 86 coupled in series within pressure vessel 74.
Although a single pressure vessel 74 is shown in FIG. 10,
arrangement includes thirty pressure vessels 74 (not shown)
positioned and parallel. In the exemplary embodiment, each pressure
vessel 74 includes four first membrane modules 84 having first salt
permeance value 88 of 0.4.times.10.sup.-5 cm/s. First membrane
modules 84 are positioned in series and adjacent inlet end 76.
Arrangement 112 further includes three second membrane modules 86
having second salt permeance value 90 of 6.times.10.sup.-5 cm/s.
Second membrane modules 86 are positioned between first membrane
modules 84 and outlet end 78. Feed solution 18 includes sea water
having fluid characteristics 44 such as, but not limited to, TDS of
35,000 ppm, 25.degree. C., and transmembrane pressure of 732 psi.
Arrangement 112 is configured to desalinate feed solution 18 into
concentrate 22 and permeate 20, wherein permeate 20 has salinity of
about 1,954 ppm.
EXAMPLE 4: FIG. 11
[0061] FIG. 11 illustrates an alternative arrangement 114 of
pressure vessel 74 having first membrane modules 84, second
membrane modules 86, and third membrane module 92 coupled in series
within pressure vessel 74. Although a single pressure vessel 74 is
shown in FIG. 11, arrangement 114 includes thirty pressure vessels
74 (not shown) positioned and parallel. The exemplary embodiment,
each pressure vessel 74 includes four first membrane modules 84
having first salt permeance value 88 of 0.4.times.10.sup.-5 cm/s.
First membrane modules 84 are positioned in series and adjacent
inlet end 76. Arrangement 114 further includes two second membrane
modules 86 having second salt permeance of 6.times.10.sup.-5 cm/s.
Second membrane modules 86 are positioned between first membrane
modules 84 and third membrane module 92. Arrangement 114 further
includes third membrane module 92 having third salt permeance value
94 of 12.times.10.sup.-5 cm/s. Third membrane module 92 is
positioned between second membrane modules 86 and outlet end 78.
Feed solution 18 includes sea water having fluid characteristics 44
such as, but not limited to, TDS of 35,000 ppm, 25 degree
temperature and transmembrane pressure of 715 psi. Arrangement 114
is configured to desalinate feed solution 18 into a concentrate 22
and permeate 20, wherein permeate 20 has salinity of about 2,485
ppm.
EXAMPLE 5: FIG. 12
[0062] FIG. 12 illustrates an alternative arrangement 116 of
pressure vessel 74 having first membrane modules 84, second
membrane modules 86, and third membrane modules 92 coupled in
series within pressure vessel 74. Although a single pressure vessel
74 is shown in FIG. 12, arrangement 116 includes thirty pressure
vessels 74 (not shown positioned in parallel. In the exemplary
embodiment, each pressure vessel 74 includes four first membrane
modules 84 having first salt permeance value 88 of
0.4.times.10.sup.-5 cm/s. First membrane modules 84 are positioned
in series and adjacent inlet end 76. Arrangement 116 further
includes two second membrane modules 86 having second salt
permeance of 6.times.10.sup.-5 cm/s. Second membrane modules 86 are
positioned between first membrane modules 84 and a third membrane
modules 92. Arrangement 116 further includes two third membrane
modules 92 having third salt permeance value 94 of
12.times.10.sup.-5 cm/s. Third membrane modules 92 are positioned
between second membrane modules 86 and outlet end 78. Feed solution
18 includes sea water having fluid characteristics 44 such as, but
not limited to, TDS of 35,000 ppm, 25.degree. C., and transmembrane
pressure of 684 psi. Arrangement 116 is configured to desalinate
feed solution 18 into a concentrate 22 and permeate 20, wherein
permeate 20 has salinity of about 3,422 ppm.
[0063] FIG. 13 is a schematic view of an alternative reverse
osmosis system 118 such as, but not limited to, a permeate-staged
reverse osmosis system. In FIG. 13, similar components include the
same element numbers as shown in FIGS. 1-12. Reverse osmosis system
118 includes a first reverse osmosis unit 120 and a second reverse
osmosis unit 122 coupled in series and in flow communication to
first reverse osmosis unit 120. More particularly, outlet end 78 of
first reverse osmosis unit 120 is coupled in series and in flow
communication with inlet end 124 of second osmosis unit 122. Each
of first reverse osmosis unit 120 and second reverse osmosis unit
122 includes at least one of first membrane module 84, second
membrane module 86, and third membrane module 92. During operation,
feed solution 18 is discharged into and through pressure vessel 74
of first reverse osmosis unit 120. First reverse osmosis unit 120
discharges concentrate 22 out of outlet end 80. Moreover, first
reverse osmosis unit 120 discharges a first permeate 126 from
outlet end 78. First permeate 126 is discharged into inlet end 124
of second reverse osmosis unit 122. Second reverse osmosis unit 122
discharges concentrate 127 from an outlet end 128. Concentrate 127
has a different composition than concentrate 22. Moreover, second
reverse osmosis unit 122 discharges a second permeate 132 from an
outlet end 130, second permeate 132 includes a salinity of at least
about 500 ppm.
[0064] FIG. 14 is a schematic view of an alternative reverse
osmosis system 134 such as, but not limited to, a brine-staged
unit. In FIG. 14, similar components include the same element
numbers as shown in FIGS. 1-13. Reverse osmosis system 134 includes
a first reverse osmosis unit 136 and a second reverse osmosis unit
138 coupled in parallel and in flow communication to first reverse
osmosis unit 136. More particularly, outlet end 80 of first reverse
osmosis unit 136 is coupled in parallel and in flow communication
with inlet end 140 of second reverse osmosis unit 138. Each of
first reverse osmosis unit 134 and second reverse osmosis unit 138
includes at least one of first membrane module 84, second, membrane
module 86, and optionally third membrane module 92. During
operation, feed solution 18 is discharged into and through first
reverse osmosis unit 136. First reverse osmosis unit 136 discharges
a first concentrate 142 from outlet end 80. Moreover, first reverse
osmosis unit 136 discharges a first permeate 144 out of outlet end
78. First concentrate 142 is discharged into inlet end 140 of
second reverse osmosis unit 138. Second reverse osmosis unit 138
discharges a second concentrate 146 from outlet end 147. Moreover,
second reverse osmosis unit 138 discharges a second permeate 150
from an outlet end 148. Second permeate 152 is discharged into
first permeate 144 to form a combined permeate 154 having a
salinity of at least about 500 ppm.
[0065] FIG. 15 is a flowchart, illustrating an exemplary method
1500 of assembling a reverse osmosis system, such as reverse
osmosis system 12 (shown in FIG. 1), to well casing 32 (shown in
FIG. 1) for processing feed solution 18 (shown in FIG. 3). Method
1500 includes positioning 1502 pressure vessel 74 (show in FIG. 3).
Pressure vessel 74 includes inlet end 76, outlet end 78, and vessel
body 72 (all shown in FIG. 3) extending between the inlet end and
the outlet end. Method 1500 further includes coupling 1504 the
plurality of first membrane modules 84 (shown in FIG. 1) to the
pressure vessel. In the exemplary method 1500, each first membrane
module includes first salt permeance value 88 (shown in FIG.
3).
[0066] Method 1500 includes coupling 1506 at least one second
membrane module 86 (shown in FIG. 3) in flow communication to the
plurality of first membrane modules. In the exemplary method 1500,
the at least one second membrane module includes second salt
permeance value 90 (shown in FIG. 3) that is different from the
first salt permeance value to facilitate processing the feed
solution into permeate 20 and concentrate 22 (both shown in FIG.
3). Third membrane module 92 (shown in FIG. 2) is coupled 1508 in
flow communication to the second membrane module. In the exemplary
method 1500, third membrane module includes third permeance value
94 (shown in FIG. 2) which is greater than the first salt permeance
value and the second salt permeance value.
[0067] FIG. 16 is a flowchart illustrating an exemplary method 1600
of processing solution 18. Method 1600 includes discharging 1602
the feed solution into pressure vessel 74 having inlet end 76,
outlet end 78, and having first membrane module 84 and second
membrane module 86 coupled in series between the inlet end and the
outlet end (all shown in FIG. 3). Method 1600 includes discharging
1604 the feed solution into the first membrane module having first
salt permeance value 88 (shown in FIG. 3) and configured to
desalinate the feed solution into first permeate 23 and first
concentrate 25 (all shown in FIG. 2). Method 1600 includes
discharging 1606 the first concentrate into the second membrane
module having second salt permeance value 90 (shown in FIG. 3) that
is different from the first salt permeance value and configured to
desalinate the first concentrate into second permeate 27 and second
concentrate 29, wherein collective permeate 20 (all shown in FIG.
2) of the first permeate and the second permeate has a salinity of
at least about 500 parts per million.
[0068] FIG. 17 is a flowchart illustrating an exemplary method 1700
of processing feed solution 18. Method 1700 includes discharging
1702 the feed solution into pressure vessel 74 having inlet end 76,
outlet end 78, and having first membrane module 84 and second
membrane module 86 coupled in series between the inlet end and the
outlet end (all shown in FIG. 3). Method 1700 includes discharging
1704 the feed solution into the second membrane module having
second salt permeance value and configured to desalinate the feed
solution into permeate 27 and concentrate 29 (shown in FIG. 2).
Method 1700 further includes discharging 1706 the concentrate into
the first membrane module having first salt permeance value 88
(shown in FIG. 3) that is different from the second salt permeance
value and configured to desalinate the concentrate into another
permeate 23 and another concentrate 25 (shown in FIG. 2), wherein
collective permeate 20 of the permeate and other permeate has a
salinity of at least about 500 parts per million.
[0069] FIG. 18 is a flowchart illustrating an exemplary method 1800
of processing feed solution 18. Method 1800 includes discharging
1802 the feed solution into pressure vessel 74 having inlet end 76,
outlet end 78, and having first membrane module 84 and second
membrane module 86 coupled in series between the inlet end and the
outlet end (all shown in FIG. 3). Method 1800 includes discharging
1804 the feed solution into the first membrane module having first
salt permeance value 88 (shown in FIG. 3) and configured to
desalinate the feed solution into first permeate 23 and first
concentrate (shown in FIG. 7). Method 1800 includes discharging
1806 the first concentrate into the second membrane module having
second salt permeance value 90 (shown in FIG. 3) that is different
from the first salt permeance value and configured to desalinate
the first concentrate into second permeate 27 and second
concentrate 29 (shown in FIG. 7). Method 1800 includes discharging
1808 the second concentrate into third membrane modules 32 (shown
in FIG. 3) having a third salt permeance value 94 (shown in FIG. 3)
which is greater than the first salt permeance value and the second
salt permeance value, the third membrane module configured to
desalinate the second concentrate into third permeate 31 and third
concentrate 33 (shown in FIG. 7), wherein collective permeate 20
(shown in FIG. 7) of the first permeate, the second permeate, and
the third permeate has a salinity of at least about 500 parts per
million.
[0070] FIG. 19 is a flowchart illustrating an exemplary method 1900
of recovering a hydrocarbon fluid, such as fluid 30 (shown in FIG.
1), from a formation reservoir, for example formation 28 (shown in
FIG. 1). Method 1900 includes discharging 1902 feed solution 18
into pressure vessel 74 having inlet end 76, outlet end 78, and
having first membrane module 84 and second membrane module 86
coupled in series between the inlet end and the outlet end (all
shown in FIG. 2). Method 1900 includes discharging 1904 the feed
solution into the first membrane module having first salt permeance
value 88 (shown in FIG. 3) and configured to desalinate the feed
solution into first permeate 23 and first concentrate 25 (shown in
FIG. 2). Method 1900 includes discharging 1906 the first
concentrate into the second membrane module having second salt
permeance value 90 (shown in FIG. 3) that is different from the
first salt permeance value and configured to desalinate the first
concentrate into second permeate 25 and second concentrate 27,
wherein collective permeate 20 of the first permeate and the second
permeate has a salinity of at least about 500 parts per million.
Method 1900 further includes controllably discharging 1908 at least
a portion of the collective permeate having the salinity of at
least about. 500 parts per million into the formation reservoir.
Method 1900 further includes forcing 1910 the hydrocarbon fluid
from the formation reservoir under pressure of the collective
permeate and into a well casing.
[0071] The exemplary embodiments described herein provide for a
reverse osmosis system for cost effective and efficient recovery
processes for a production fluid. The exemplary embodiments
described herein provide for a reverse osmosis unit that
desalinates a feed solution into a concentrate and a permeate that
is optimal for enhanced recovery of production fluid. Moreover, the
embodiments described herein form a permeate having a salinity of
at least about 500 parts per million. The reverse osmosis system
includes controllably adjusting the feed solution trough reverse
osmosis units. The reverse osmosis system decreases design,
installation, operational, maintenance, and/or replacement costs
for a well site.
[0072] A technical effect of the systems and methods described
herein includes at least one of: (a) enhancing recovery of
production fluid from a geological formation; (b) discharging a
feed solution through different membrane modules having different
salt permeance values; (c) controlling fluid characteristics of a
feed solution while discharging the feed solution through a
pressure vessel; (d) forming a permeate having a salinity of at
least about 500 parts per million; and (e) decreasing design,
installation, operational, maintenance, and/or replacement costs
for a well site.
[0073] The term "processor" is not limited to just those integrated
circuits referred to in the art as a computer, but broadly refers
to a microcontroller, a microcomputer, a programmable logic
controller (PLC), an application specific integrated circuit, and
other programmable circuits, and these terms are used
interchangeably herein. In the embodiments described herein, memory
may include, but is not limited to, a computer-readable medium,
such as a random access memory (RAM), and a computer-readable
non-volatile medium, such as flash memory. Alternatively, a floppy
disk, a compact disc--read only memory (CD-ROM), a magneto-optical
disk (MOD), and/or a digital versatile disc (DVD) may also be used.
Also, in the embodiments described herein, additional input
channels may be, but are not limited to, computer peripherals
associated with an operator interface such as a mouse and a
keyboard. Alternatively, other computer peripherals may also be
used that may include, for example, but not be limited to, a
scanner. Furthermore, in the exemplary embodiment, additional
output channels may include, but not be limited to, an operator
interface monitor. The above examples are exemplary only, and thus
are not intended to limit in any way the definition and/or meaning
of the term processor.
[0074] Exemplary embodiments of a reverse osmosis system and
methods for assembling a deployment are described herein. The
methods and systems are not limited to the specific embodiments
described herein, but rather, components of systems and/or steps of
the methods may be utilized independently and separately from other
components and/or steps described herein. For example, the methods
may also be used in combination with other manufacturing systems
and methods, and are not limited to practice with only the systems
and methods as described herein, Rather, the exemplary embodiment
may be implemented and utilized in connection with many other fluid
and/or gas applications.
[0075] Although specific features of various embodiments of the
invention may be shown in some drawings and not in others, this is
for convenience only. In accordance with the principles of the
invention, any feature of a drawing may be referenced and/or
claimed in combination with any feature of any other drawing.
[0076] Some embodiments involve the use of one or more electronic
or computing devices. Such devices typically include a processor or
controller, such as a general purpose central processing unit
(CPU), a graphics processing unit (GPU), a microcontroller, a
reduced instruction set computer (RISC) processor, an application
specific integrated circuit (ASIC), programmable logic circuit
(PLC), and/or any other circuit or processor capable of executing
the functions described herein. The methods described herein may be
encoded as executable instructions embodied in a computer readable
medium, including, without limitation, a storage device and/or a
memory device. Such instructions, when executed by a processor,
cause the processor to perform at least a portion of the methods
described herein. The above examples are exemplary only, and thus
are not intended to limit in any way the definition and/or meaning
of the term processor.
[0077] This written description uses examples to disclose the
invention, including the best mode, and also to enable any person
skilled in the art to practice the invention, including making and
using any devices or systems and performing any incorporated
methods. The patentable scope of the invention is defined by the
claims, and may include other examples that occur to those skilled
in the art. Such other examples are intended to be within the scope
of the claims if they have structural elements that do not differ
from the literal language of the claims, or if they include
equivalent structural elements with insubstantial differences from
the literal language of the claims.
* * * * *