U.S. patent number 5,538,598 [Application Number 08/115,921] was granted by the patent office on 1996-07-23 for liquid purifying/distillation device.
This patent grant is currently assigned to FSR Patented Technologies, Ltd.. Invention is credited to Harold Rapp, Barry Schlesinger.
United States Patent |
5,538,598 |
Schlesinger , et
al. |
July 23, 1996 |
Liquid purifying/distillation device
Abstract
Disclosed herein is a distillation purifying system. The device
has a section which creates a vacuum pressure that is transmitted
throughout the system, a distillation/purification zone in which
fluids to be distilled/purified are treated, and a collection zone
in which the distilled/purified liquids are transferred. The device
is effective for certain liquids, solutions, and the like and can
be used for water treatment, petroleum processes, and bodily fluid
treatment.
Inventors: |
Schlesinger; Barry (Las Vegas,
NV), Rapp; Harold (Marina Del Rey, CA) |
Assignee: |
FSR Patented Technologies, Ltd.
(Las Vegas, NV)
|
Family
ID: |
27377355 |
Appl.
No.: |
08/115,921 |
Filed: |
September 1, 1993 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
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913694 |
Jul 14, 1992 |
5441606 |
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855979 |
Mar 23, 1992 |
5248394 |
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Foreign Application Priority Data
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Mar 3, 1993 [WO] |
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PCT/US93/02412 |
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Current U.S.
Class: |
202/206; 202/197;
202/202; 202/205 |
Current CPC
Class: |
B01D
1/0017 (20130101); B01D 3/007 (20130101); B01D
3/10 (20130101); B01D 3/103 (20130101); B01D
3/106 (20130101); B01D 5/0039 (20130101); B01D
5/0045 (20130101); B01D 5/009 (20130101); B09C
1/06 (20130101); C02F 1/04 (20130101); B01D
1/0035 (20130101); B01D 1/0058 (20130101); B01D
1/305 (20130101) |
Current International
Class: |
B01D
5/00 (20060101); B01D 3/10 (20060101); B01D
3/00 (20060101); B09C 1/06 (20060101); B09C
1/00 (20060101); C02F 1/04 (20060101); B01D
1/00 (20060101); B01D 1/30 (20060101); B01D
003/10 (); B01D 003/42 () |
Field of
Search: |
;202/205,206,160,197,182,176,202 ;203/11,2,21,25,91,DIG.8 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
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829487 |
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Jun 1938 |
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FR |
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2505968 |
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Aug 1976 |
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DE |
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Primary Examiner: Warden; Robert J.
Assistant Examiner: Snider; Theresa T.
Attorney, Agent or Firm: Ladas & Parry
Parent Case Text
CROSS REFERENCE TO RELATED APPLICATION
This is a continuation in part of U.S. Ser. No. 07/913,694, filed
on Jul. 14, 1992 now U.S. Pat. No. 5,441,606, which is a
continuation in part of U.S. Ser. No. 07/855,979, filed Mar. 23,
1992, now U.S. Pat. No. 5,248,394, both incorporated herein by
reference. This invention is reflected at least in part in U.S.
Disclosure Document No. 301003 received by the U.S. Patent Office
on Feb. 10, 1992 and incorporated herein by reference. Applicant
claims foreign priority benefits from applicant's International
Appln. No PCT/US93/92412, filed Mar. 16, 1993.
Claims
The present invention is claimed as follows.
1. A distillation system for distilling a fluid, said system being
comprised of:
a vacuum device;
a purifying device comprised of an evaporator and a condenser, said
evaporator being connected to said condenser so that said fluid to
be distilled passes to said evaporator for evaporation and then to
said condenser for condensation; and
a trap having a first end and a second end, said first end
connecting to said condenser, said second end leading to a
collection outlet at one point and to said vacuum device at another
point wherein said fluid which is condensed in said condenser flows
as distillate from said condenser to and through said trap to said
collection outlet, vacuum pressure in said system from said vacuum
being controllably communicated at least in part to said purifying
device through said trap and to said collection outlet at said one
point.
2. The system of claim 1 further comprising: a computer control for
automated operation of said system;
a heating mechanism for heating and vaporizing said fluid when in
said system, said heating mechanism being activated for use in said
purifying device only after the vacuum level in said system
corresponds to a latent heat of vaporization point which represents
a set relationship with respect to the temperature of the fluid to
be distilled; and
a degassification tank connected to said vacuum at one point and to
said evaporator at a second point, such that said fluid which is to
be distilled passes through said degassification tank to be exposed
to the vacuum pressure of said vacuum and then into said evaporator
chamber.
3. The system of claim 1 further comprising a heat recovery and
reuse device associated with said system.
4. A distillation system for distilling a fluid, said system being
comprised of:
a vacuum device;
a purifying device having a heating mechanism therein, said
purifying device being in fluid communication with said vacuum and
comprising an evaporator and a condenser, said evaporator being
connected to said condenser so that fluid to be distilled passes to
said evaporator for evaporation and then to said condenser for
condensation; and
a trap having a first end and a second end, said first end
connecting to said condenser, said second end leading to a
collection outlet at one point and to said vacuum device at another
point wherein
said heating mechanism is activated for use in said purifying
device only after the vacuum level in said system corresponds to a
latent heat of vaporization point which represents a set
relationship with respect to the temperature of the fluid to be
purified, said fluid being condensed in said condenser flowing from
said condenser as distillate to and through said trap to said
collection outlet, the vacuum pressure from said vacuum being
controllably communicated at least in part to said purifying device
through said trap.
5. A distillation and purifying system for treating a fluid, said
system being comprised of:
a vacuum for generating a vacuum pressure throughout said
system;
a distillation and purifying unit, said distillation and purifying
unit comprising an evaporator and a condenser, said evaporator
being connected to said condenser;
a degassification device connected at one end to said vacuum and at
another end to said evaporator; and
a trap directly connected to said vacuum at one point and directly
connected to said condenser at another point, said distillation and
purifying unit being in fluid communication with said vacuum
through said trap; and a collection device in fluid communication
with said vacuum and said distillation and purifying unit, wherein
said fluid is brought into said degassification device and then
into said evaporator where it is evaporated into vapor, said vapor
then passing into said condenser to be condensed as a distillate,
said distillate then passing through said trap into said collection
device.
6. A distillation system for distilling fluid, said system being
comprised of:
a computer control for controlling said system;
a vacuum for generating a vacuum pressure in said system and
controlled by said computer control;
a distillation and purifying device controlled by said computer
control and comprising an evaporator and a condenser, said
evaporator being directly connected to said condenser;
a single trap, said trap being directly connected to said vacuum at
one point and directly connected to said condenser at another
point, said distillation and purifying device being in fluid
communication with said vacuum through said trap; and
a collection outlet in fluid communication with said trap and said
vacuum, said condenser communicating distilled fluid to said
collection outlet through said trap, such that when said trap fills
with said distilled the vacuum requirement of said system
diminishes, the vacuum pressure generated by said vacuum means
acting on said distilled fluid to facilitate the continual flow of
said distilled fluid into said collection outlet from said trap,
said vacuum generating a vacuum that is controlled such that the
latent heat of vaporization point under vacuum pressure corresponds
to a temperature greater than the temperature of the fluid in said
trap so that the fluid in said trap remains in a condensed state
and does not vaporize, said vacuum being effectively applied only
to the fluid in said trap once said trap is filled with said
fluid.
7. The system of claim 6 further comprised of heaters in said
distillation and purifying device and controlled by said computer
and connectors to connect the parts of said system; and a
degassification tank connected to said vacuum at one point and to
said evaporator at a second point, such that said fluid which is to
be distilled passes through said degassification tank to be exposed
to the vacuum pressure of said vacuum and then into said evaporator
chamber, said trap, distillation and purifying device, said
collection outlet, said degassification tank and said connectors
being insulated and atmospherically sealed.
8. The system of claim 7 wherein said vacuum is comprised of: at
least two atmospherically closed towers; a vented tank connected to
said towers; a pump connected between said vented tank and said
towers; and valves associated with said towers whereby a fluid is
pumped and drained alternately between said towers from said tank
to create a vacuum pressure which is transmitted through said
system.
9. The system of claim 8 wherein said fluid is polyalpholefin oil
or a synthetic oil at ambient temperature in said tank and in said
towers.
10. A distillation system for distilling a fluid, said system being
comprised of:
a computer control for controlling said system;
a vacuum for generating a vacuum pressure in said system and
controlled by said computer control;
a distillation unit controlled by said computer control;
a single trap, said trap being directly connected to said vacuum at
one point and directly connected to said distillation unit at
another point, said distillation unit being in fluid communication
with said vacuum through said trap; and
a collection device in fluid communication with said trap and said
vacuum, said distillation unit communicating distilled fluid to
said collection device through said trap, such that when said trap
fills with said distilled fluid the vacuum requirement of said
system diminishes, the vacuum pressure generated by said vacuum
acting on said distilled fluid to facilitate the continual flow of
said distilled fluid into said collection device from said trap,
said vacuum generating a vacuum that is controlled by said computer
control such that the latent heat of vaporization point under
vacuum pressure corresponds to a temperature greater than the
temperature of the fluid in said trap so that the fluid in said
trap remains in a condensed state and does not vaporize, said
vacuum being effectively applied only to the fluid in said trap
once said trap is filled with said fluid, said distillation unit,
and said collection device being insulated and atmospherically
sealed, said vacuum being comprised of at least two atmospherically
closed towers; a vented tank connected to said towers; a pump
connected between said vented tank and said towers; and valves
associated with said towers whereby a fluid is pumped and drained
alternately between said towers from said tank to create a vacuum
pressure which is transmitted through said system, said towers
being between 35 to 50 feet in height and 6 to 14 inches in
diameter, said distillation unit being 42 to 50 feet in height.
11. A distillation and purifying system comprised of:
a computer control for controlling said system;
vacuum means for generating a vacuum pressure in said system and
controlled by said computer control;
a distillation and purifying device controlled by said computer
control;
a single trap, said trap being directly connected to said vacuum at
one point and directly connected to said distillation and purifying
device at another point, said distillation and purifying device
being in fluid communication with said vacuum through said trap;
and
a collection device in fluid communication with said trap and said
vacuum means, said distillation and purifying device communicating
distilled and purified fluid to said collection device through said
trap, such that when said trap fills with said distilled and
purified fluid the vacuum requirement of said system diminishes,
the vacuum pressure generated by said vacuum acting on said
purified and distilled fluid to facilitate the continual flow of
said purified and distilled fluid into said collection device from
said trap, said vacuum generating a vacuum that is controlled by
said computer control such that the latent heat of vaporization
point under vacuum pressure corresponds to a temperature greater
than the temperature of the fluid in said trap so that the fluid in
said trap remains in a condensed state and does not vaporize, said
vacuum being effectively applied only to the fluid in said trap
once said trap is filled with said fluid, said distillation and
purifying device, and said collection device being insulated and
atmospherically sealed, said collection device comprised of at
least two closed tanks, valves, said tanks being directly connected
through said valves to said trap and said vacuum and also directly
connected through said valves to atmosphere and to a collection
conduit open to atmosphere, wherein said distilled and purified
fluid continually flows from said trap to said at least two closed
tanks, said tanks alternately filling and emptying.
12. A distillation system for distilling a fluid, said system being
comprised of:
a computer control for controlling said system;
vacuum for generating a vacuum pressure in said system, said vacuum
being controlled by said computer control;
a distillation device controlled by said computer control;
a single trap, said trap being directly connected to said vacuum at
one point and directly connected to said distillation device at
another point, said distillation device being in fluid
communication with said vacuum through said trap; and
a collection device in fluid communication with said trap and said
vacuum, said distillation device communicating distilled and
purified fluid to said collection device through said trap, such
that when said trap fills with said distilled fluid the vacuum
requirement of said system diminishes, the vacuum pressure
generated by said vacuum acting on said distilled fluid to
facilitate the continual flow of said distilled fluid into said
collection device from said trap, said vacuum generating a vacuum
that is controlled by said computer control such that the latent
heat of vaporization point under vacuum pressure corresponds to a
temperature greater than the temperature of the fluid in said trap
so that the fluid in said trap remains in a condensed state and
does not vaporize, said vacuum being effectively applied only to
the fluid in said trap once said trap is filled with said fluid,
said collection device comprises a rotating vane device.
13. A vacuum distillation system for distilling fluid comprised
of:
vacuum for generating vacuum pressure in said device;
an insulated distillation and separation device having an
evaporator chamber and a condensing unit, said condensing unit
being in communication with said evaporator chamber;
a vapor separation device and heating device associated with said
evaporator chamber, said evaporator chamber defining an outlet for
nonvaporized materials remaining after vaporizing said fluid;
an open tube bundle heat exchanger associated with said condensing
unit of said distillation and separation chamber;
a fluid transfer pipe having a first end extending into fluid to be
distilled and a second end opening into said evaporator
chamber;
an insulated single trap connected between said condensing unit of
said distillation and separation chamber and said vacuum, said
distillation and separation device being in fluid communication
with said vacuum through said trap; and
an insulated collection device connected to said trap, where said
fluid to be distilled passes through said fluid transfer pipe into
said evaporator chamber to be turned to vapor, said vapor passing
into said condensing unit to become distillate as said vapor passes
over said heat exchanger, said distillate passing into said
collection device through said trap.
14. The system of claim 13 wherein said fluid transfer pipe has a
third end opening into said heat exchanger and wherein said heat
exchanger has an exit outlet extending into said fluid such that a
portion of said fluid enters said fluid transfer pipe and passes
into at least one of said evaporator chamber or said heat
exchanger, said fluid entering said heat exchanger passing out said
outlet to return to the main body of fluid.
15. The system of claim 14 wherein said outlet in said evaporator
chamber opens into said exit outlet of said heat exchanger.
16. The system of claim 14 further comprises a degassification tank
connected between said fluid transfer pipe and said evaporator
chamber, said degassification tank connected to said vacuum such
that said fluid which is to be distilled passes through said
degassification tank prior to passing to said evaporator
chamber.
17. The system of claim 13 further comprising a degassification
tank connected between said fluid transfer pipe and said evaporator
chamber, said degassification tank connected to said vacuum such
that said fluid which is to be distilled passes through said
degassification tank prior to passing into said evaporator chamber;
and a refrigeration device, said heating device in said evaporator
chamber being connected to said refrigeration device, said open
tube bundle heat exchanger being connected at one end to said
heating device in said evaporator chamber and at another end to
said refrigeration device through said open tube bundle heat
exchanger to said refrigeration device.
18. The system of claim 17 further comprising a non vaporized
matter collection device connected to said outlet, said non
vaporized, matter collection device comprising a closed and
insulated tank for collection of non vaporized materials which have
collected in the base of said insulated evaporator chamber, said
insulated tank comprising valves and a sensor, said tank being
connected through said valves to said evaporator chamber, the
atmosphere, and said vacuum pressure from said vacuum whereby when
said sensor indicates that the concentration in said insulated
evaporator chamber is at a certain level, said valve to said
evaporator chamber is opened to allow the non vaporized materials
to drain into said tank, and upon completion of said draining, said
valve to said evaporator chamber closes and said valve to the
atmosphere opens so that said non vaporized materials valve to the
atmosphere is closed, said valve to said vacuum is opened to return
said tank to vacuum pressure at which time said valve to said
vacuum is closed and said tank is again ready to receive non
vaporized materials from said evaporator chamber.
19. The system of claim 13 further comprising a supplemental
heating electrode located between said heating device and said
vapor separation device.
20. The system of claim 13 wherein said fluid transfer pipe has a
third end opening into said heat exchanger; said heat exchanger has
a first exit outlet extending into said fluid and a second exit
outlet extending into said open tube bundle heat exchanger; said
open tube bundle having a drain pipe joining said first exit outlet
such that fluid passing through said fluid transfer pipe into said
third end opening passes through said heat exchanger to at least
one of said first exit outlet or said second exit outlet, said
fluid passing through said second exit outlet or said second exit
outlet, said fluid passing through said second exit outlet passing
into and through said open tube bundle heat exchanger and out said
drain pipe, said system also comprising a degassification tank
connected to said evaporate chamber and said vacuum such that said
fluid which is to be distilled passes through said degassification
tank prior to passing into said evaporator chamber.
21. The system of claim 13 wherein the location of said open tube
bundle heat exchanger is such that the fluid exiting therefrom
offers power which is converted into usable energy.
22. The system of claim 13 wherein said vacuum acts as a structural
support for said system.
23. A system comprised of:
a vacuum, said vacuum providing vacuum pressure to said system at
specialized levels;
a liquid vaporization device;
a vapor condensing device attached to said liquid vaporization
device;
a degassification device connected to said liquid vaporization
device at one point and to said vacuum at another point, and
a trap connected at one end to said vapor condensing device and at
another end to said vacuum and at another point to a collection
point, wherein said vacuum acts on said condensing device and said
liquid vaporization device through said trap and said
degassification tank.
24. The system of claim 23 further comprising a control device for
controlling said system including said vacuum such that said vacuum
level corresponds to the latent heat of vaporization for liquid
which is vaporized and brought into said vapor condensing
device;
a filter within said liquid vaporization device such that said
liquid which is vaporized in said vaporization device passes
through said filter before entering said vapor condensing
device;
a heater associated with said liquid vaporization device for
creating heat therein;
a heat exchanger associated with said vapor condensing device;
and
first and second connecting lines located between said heat
exchanger and said liquid to be distilled and said vaporization
device, said first line extending from said liquid to be distilled
to both said heat exchanger and said vaporization device so that as
controlled by said control means at least a portion of said liquid
will enter said vaporization device and another portion said heat
exchanger, said second line extending from said vaporization device
and said exchanger to an exit point, wherein said liquid to be
distilled passes through said first line in one instance to said
vaporization device to be turned into vapor therein and pass
through said filter and in a second instance to said heat exchanger
to pass therethrough to said second line and to said exit point,
materials in said vaporization device which are not turned into
vapor move in a controlled manner as controlled by said control
device to said second line to said exit point.
25. The system of claim 23 further comprising: a control device for
controlling said system including said vacuum, such that said
vacuum level corresponds to the latent heat of vaporization for
liquid which is vaporized and brought into said vapor condensing
device;
a filter within said liquid vaporization device such that said
liquid which is vaporized in said vaporization device passes
through said filter before entering said vapor condensing
device;
a heater connected in said vaporization device for facilitating
vaporization of liquid therein;
a reclaim device associated with said liquid vaporization
device;
a heat exchanger associated with said vapor condensing device;
and
first, second and third connecting lines located between said heat
exchanger, said heat reclaim device, said degassification device,
and said liquid to be cleansed such that said liquid to be cleansed
passes through said first connecting line to in part flow to said
degassification device and to in other part flow to said heat
exchanger device as controlled by said control device, said fluid
which flows to said degassification device passing through said
liquid vaporization device to said condensation device to said trap
and to said collection point, said fluid which flows to said heat
exchange device passing therethrough to said second connecting
line, said second connecting line branching into said heat reclaim
device and to a section for controlled bypass of said system, said
control device operating said controlled bypass, such that said
liquid in said first connecting line passes at least in part into
said reclaim device and when so controlled at least in part to said
section for controlled bypass, said third line connecting to said
heat reclaim device, said bypass section and an exit point such
that liquid which passes from said second line into said heat
reclaim device, passes from said heat reclaim device to said exit
point and fluid which passes through said controlled bypass section
passes to said third line and to said exit point.
26. The system of claim 23 further comprising a control device for
controlling said system including said vacuum, such that said
vacuum level corresponds to the latent heat of vaporization for
liquid which is vaporized and brought into said vapor condensing
device;
a filter within said liquid vaporization device such that said
liquid which is vaporized in said vaporization device passes
through said filter before entering said vapor condensing
device;
a heater connected in said vaporization device for facilitating
vaporization of liquid therein;
a heat condenser associated with said liquid vaporization
device;
a heat exchanger associated with said vapor condensing device and
fluidly connected at one end to said heat condenser;
a supplemental heat exchanger fluidly connected to said heat
condenser at one end and to said heat exchanger at another end,
such that heat provided by said supplemental heat exchanger to said
heat condenser to facilitate the vaporization process to be
accomplished in said vaporization device, is thereafter passes to
said heat exchanger where it is now of such a temperature to
facilitate the condensation process to be accomplished in said
condensing device and thereafter returns to said supplemental heat
exchanger.
27. The system of claim 23 wherein said vacuum is comprised of: at
least two atmospherically closed towers; a vented tank connected to
said towers; a pump connected between said vented tank and said
towers; and valves associated with said towers whereby an oil is
pumped and drained alternately between said towers from said tank
to create a vacuum pressure which is transmitted through said
system.
28. The system of claim 23 further comprising a collection device
for non vaporized material fluidly attached to said vapor
condensing device, said collection device for non vaporized
material comprising a closed tank, valves for opening and closing
said tank, and a sensor associated with said valves and said vapor
condensing device, said tank being connected through said valves to
said vapor condensing device and the outside of said system and
opening and closing in response to said sensor to allow non
vaporized materials which collect in said vapor condensing device
to pass into said tank for removal from said system.
29. The system of claim 23 wherein said collection point comprises
at least two closed tanks, valves for opening and closing said
tanks and sensors for operating with said valves to control the
opening and closing of said tanks, said tanks being connected
through said valves to said trap and said vacuum and also through
said valves to atmosphere, wherein materials which pass through
said trap flow to said tanks to be alternately collected and
drained from each tank.
30. A system comprised of:
a vacuum, said vacuum providing vacuum pressure to said system at
specified levels;
a liquid vaporization device;
vapor condensing device attached to said liquid vaporization
device; and
a generally u-shaped generally tubular trap connected at one end to
said vapor condensing device and at another end to said vacuum such
that said vacuum acts on said condensing device and said liquid
vaporization device through said trap.
Description
BACKGROUND OF THE INVENTION
There is a recognized need to convert undrinkable water to potable
water and to have the ability to cleanse liquids in general. Many
inventions have been created to attend to this need. A list of such
inventions includes the following.
U.S. Pat. No. 5,064,505 (Borgren)
U.S. Pat. No. 4,770,748 (Cellini)
U.S. Pat. No. 4,954,223 (Leary)
U.S. Pat. No. 4,696,718 (Lasater)
U.S. Pat. No. 4,525,243 (Miller)
U.S. Pat. No. 4,585,524 (Hoiss)
U.S. Pat. No. 4,595,460 (Hurt)
U.S. Pat. No. 4,248,672 (Smith)
U.S. Pat. No. 4,267,022 (Pitcher)
U.S. Pat. No. 4,269,664 (Younger)
U.S. Pat. No. 4,282,070 (Egosi)
U.S. Pat. No. 3,597,328 (Michels)
U.S. Pat. No. 3,489,652 (Williamson)
U.S. Pat. No. 3,425,235 (Cox)
U.S. Pat. No. 3,440,147 (Rannenberg)
U.S. Pat. No. 3,236,748 (Pottharst, Jr.)
U.S. Pat. No. 3,203,875 (Sturtevant)
U.S. Pat. No. 4,555,307 (Hagen)
U.S. Pat. No. 4,686,009 (McCabe)
U.S. Pat. No. 4,285,776 (Atwell)
U.S. Pat. No. 4,366,030 (Anderson)
U.S. Pat. No. 3,248,305 (Williamson)
U.S. Pat. No. 3,390,057 (Day)
U.S. Pat. No. 3,140,986 (Hubbard)
The S-200 Vapor Compression Water Processor.TM. produced by
Superstill Technology Inc.
U.S. Congress, Office of Technology Assessment, "Using Desalination
Technologies for Water Treatment", OTA-BP-O-46 (Washington, D.C.:
U.S. Government Printing Office, March 1988).
Unfortunately, many of these inventions are unduly complex,
ungainly, uneconomical, unworkable, and/or not as efficient or as
effective as they might be. The present invention attempts to
overcome these drawbacks and to disclose an advance to the art. The
present invention is essentially a closed loop system recycling
heat, energy, and fluid.
BACKGROUND OF THE INVENTION
The purpose of the first embodiment of this invention is to convert
salt water, brackish water, contaminated ground water, or
contaminated water from large bodies of water to potable quality
water which can be used for irrigation, human and animal
consumption, or industrial or manufacturing needs. The device
employs a vacuum distillation process which is believed to remove
virtually all dissolved solids, particulates, bacteria, and organic
matter from contaminated water. The device is environmentally
desirable in that it does not concentrate brine residues or
discharge high temperature water. While the following description
directs itself to the cleansing of water, the cleansing of other
liquids or fluids is also contemplated.
The purpose of the second embodiment of this invention is to
separate certain specific fluids in solution and to separate
certain fluids from contaminants and solids, such as salts and
bacteria. The second embodiment is directly applicable to the
separation of water from ethylene glycol solutions (aircraft
de-icing solutions), and to the separation and vapor distillation
of certain fluids, including but not limited to the separation of
fluids for medical purposes and petroleum processes. The second
embodiment of this invention offers great versatility through the
use of a computer controlled system which allows the separation and
purification of various fluids or liquids based upon their
vaporization points under vacuum conditions. The device removes
unwanted liquids such as water, from solutions to enable the
economical transport of the remainder of the solution. It also
enables one to separate a specific fluid, such as glycol, from a
solution. For the purpose of explanation only, the removal of water
from a solution of ethylene glycol and water is primarily discussed
herein.
The purpose of the third embodiment is to cleanse liquids with a
device which utilizes heat recovery and can be lower in profile
than the device described in the first embodiment. This third
embodiment is used for the same purposes as the device described in
the first embodiment, and in certain installations will be
preferred where there is not abundant heat sources from outside
processes available, and where a device of smaller proportion is
required.
All embodiments make use of unshown sensor means and computers
which sense and activate portions of the invention. These are well
known to those skilled in the art. All embodiments operate on
various liquids and fluids and are not limited to the examples
disclosed herein.
SUMMARY OF THE INVENTION
Disclosed herein is a distillation/purifying system comprised
of:
a vacuum means;
a distillation/purifying means in fluid communication with said
vacuum means; and
a collection area in fluid communication with said vacuum means and
said distillation/purifying means, said distillation purifying
means communicating distilled/purified fluid to said collection
area and comprising a trap through which said distilled/purified
fluid flows to said collection area.
Also disclosed herein is a distillation/purifying system comprised
of:
a vacuum means;
a distillation/purifying means having heating means therein, said
distillation/purifying means being in fluid communication with said
vacuum means; and
a collection area in fluid communication with said vacuum means and
said distillation/purifying means, said distillation purifying
means communicating distilled/purified fluid to said collection
area and while separating and disposing of the fluids in which said
distilled/purified fluid was mixed, said heating means being
activated for use in said distillation/purifying means only after
said computer control system ensures that the vacuum level in said
system corresponds to a latent heat of vaporization point which
represents a set relationship with respect to the temperature of
the fluid to be distilled/purified.
IN THE DRAWINGS
FIG. 1 is a diagrammatic view of a first embodiment of the
invention.
FIG. 2 is a diagrammatic view of a second embodiment of the
invention.
FIG. 3 is a diagrammatic view of a third embodiment of the
invention.
DETAILED DESCRIPTION OF THE INVENTION
The present invention as first disclosed in FIG. 1, may be broadly
broken into three areas of study. These are the Vacuum Generating
Section (100), the Liquid Cleansing Area (200), and the End
Collection Zone (300).
Vacuum Generating Section (100)
In FIG. 1, the Vacuum Generating Section (100) is defined by
reference numerals (1) through (9). Two oil-filled towers (1) used
to create a vacuum, are situated side by side and connected in
parallel as further described herein. More than two oil-filled
towers (1) can be included. The oil-filled towers (1) are
preferably 35 to 50 feet in height and preferably 6 to 14 inches in
diameter. Greater diameters are, however, within the contemplation
of this invention. The oil-filled towers (1) are filled with a
synthetic oil (polyalphaolefin) or other similar liquid exhibiting
similar physical characteristics. The oil-filled towers (1) chosen
for use are preferably made of steel pipe or similar material that
is: a) capable of sustaining the vacuum levels that are generated
within each tower, and b) able to function as structural support
for the insulated evaporator chamber (21) and insulated vapor
condensing tower (20) discussed with respect to the Liquid
Cleansing Area (200).
Extending from the lower portion of each oil-filled tower (1) are
two pipes, an oil feeder pipe (OFP) and an oil drain pipe (ODP).
The oil drain pipe (ODP) is situated below the oil feeder pipe
(OFP). Extending from the top of each oil-filled tower(1) are also
two pipes, a return pipe (RP) and a vacuum pipe (9). The oil feeder
pipe (OFP), the oil drain pipe (ODP), and the return pipe (RP) all
extend into an atmospherically vented oil tank (3) situated near
the bases of oil-filled towers (1). Through these pipes, oil is
drained into and pumped from vented oil tank (3). Oil pump (2) is
attached to oil feeder pipe (OFP) to facilitate the pumping of oil
from vented oil tank (3) to oil-filled towers (1). Oil pump (2)
could be instead a submersible pump situated within vented oil tank
(3). Since oil feeder pipe (OFP) attaches to both oil-filled towers
(1), it has two first ends. Each first end is connected to the
lower portion of each oil-filled tower (1) by oil fill valves (4).
Oil feeder pipe (OFP) has also a second end which end extends
within vented oil tank (3). Oil pump (2) is located between the
first ends and the second end of oil feeder pipe (OFP) and above
and outside of vented oil tank (3).
Oil pump (2) is used to transfer the oil from the vented oil tank
(3) to the oil-filled towers (1) until a level sensor within each
oil tank (not shown) indicates that an oil-filled tower (1) is
filled completely with oil. When one of the tower sensors indicates
that its respective oil-filled tower (1) is filled, an automated
tower vent valve (5), located at the top of each oil-filled tower
(1) and connected to return pipe (RP), allows excess oil to flow
through return pipe (RP) to vented oil tank (3).
Below each tower oil fill valve (4) on each oil-filled tower (1) is
a tower oil drain valve (8). Tower oil drain valve (8) is connected
to oil drain pipe (ODP) and enables oil to drain by means of
gravity from each oil-filled tower (1) through oil drain pipe (ODP)
back into vented oil tank (3).
At the top of each oil-filled tower (1) and near tower vent valve
(5), is tower vacuum valve (6) connecting oil-filled tower (1) to
vacuum piping (9). Tower vent valve (5), tower vacuum valve (6),
tower oil fill valve (4), and tower oil drain valve (8) are
automated control valves. They and the level sensor in each tower
(1), regulate the activity of oil-filled towers (1) such that tower
oil valve (8) at the bottom of the oil-filled tower (1) opens to
allow oil to drain to the vented oil tank (3) while valves (4) (5)
(6) are closed. This draining of oil creates a substantial vacuum
within oil-filled tower (1). This vacuum is transmitted to the rest
of the system when tower vacuum valve (6) opens and allows the
vacuum to be transmitted through vacuum regulating valve (7) and
vacuum piping (9). Vacuum regulating valve (7) is located in vacuum
piping (9) to regulate the flow of vacuum through vacuum piping
(9). The oil inside oil-filled towers (1) does not vaporize under
the extreme vacuum conditions because the oil is at ambient
temperature. The vacuum regulating valve (7) has a capillary
bleed-off (not shown) to control the vacuum level transmitted
through vacuum piping (9) to the rest of the system at the level
specified by a computer control system associated with the system
of FIG. 1. Such computer control systems are well known to those
skilled in the art.
In use, oil-filled towers (1) alternately fill with oil and drain.
In towers 42 to 50 feet in height, the towers may drain to
approximately the 35 foot level. The level corresponds to the
effect of one atmosphere. This alternating action results in a
continuous vacuum being supplied to the system through vacuum
regulating valve (7) and vacuum piping (9). Oil pump (2) is cycled
on and off by the computer as required to fill oil-filled towers
(1).
The interrelationship of oil-filled towers (1) in their draining
and filling of oil can be likened to the actions of pistons in an
engine. Vacuum Generating Section (100) could be replaced by other
known vacuum devices, but preferably a water seal vacuum pump with
air ejectors.
Liquid Cleansing Area(200)
The Liquid Cleansing Area (200) is seen in FIG. 1 as composed of
reference numerals (15) through (29). At the heart of this area is
insulated evaporator chamber (21) which is somewhat rounded in
shape although its height is greater than its width. Insulated
evaporator chamber (21) is connected to insulated vapor condensing
tower (20) which is tubular in shape and has a diameter that is
less than that of insulated evaporator chamber (21). Insulated
evaporator chamber (21) and insulated vapor condensing tower (20)
as combined, are preferably 42 to 50 feet in overall height.
Insulated vapor condensing tower (20) itself can vary in height.
Insulated evaporator chamber (21) is preferably 8 to 15 feet in
height. Depending upon end goals, these heights may differ
significantly as would be appreciated by those skilled in the
art.
Insulated vapor condensing tower (20) extends into insulated
evaporator chamber (21) and has an open end that is spaced from the
top inside portion of insulated evaporator chamber (21). The base
of insulated vapor condensing tower (20) opens into insulated
distillate water trap (27) such that it is in fluid communication
therewith. Insulated distillate water trap (27) is a U in shape
with the leg of the U which connects to the base of insulated vapor
condensing tower (20) being wider than its opposing leg and base.
Insulated distillate water trap (27) is a typical trap that is
readily available in the market. Its opposing leg connects to and
is integral with vacuum piping (9) so that the vacuum pressure
created in Vacuum Generating Section (100) is communicated to
Liquid Cleansing Area (200) through vacuum piping (9) and insulated
distillate water trap (27). The vacuum is transmitted through
insulated distillate water trap (27) to insulated vapor condensing
tower (20) in vapor expansion area (26). Vapor expansion area (26)
is the longitudinal extension of insulated evaporator chamber (21)
within insulated vapor condensing tower (20) and the upper half of
insulated evaporator chamber (21).
Extending within insulated vapor condensing tower (20) is open tube
bundle heat exchanger (19) comprised of heat exchanger tubes. The
top end of open tube bundle heat exchanger (19) is connected to a
liquid transfer pipe (LTP). Liquid transfer pipe (LTP) initially
extends transversely from and into insulated vapor condensing tower
(20) and below the base of insulated evaporator chamber (21). It
then angles downwardly generally parallel to insulated vapor
condensing tower (20) to interconnect with seawater supply pump and
filter strainer (15) and descend into the liquid (16) that is to be
purified. This liquid (16) may be seawater or other contaminated
water. It is usually at 50 to 70 degrees fahrenheit, although
hotter or colder temperatures are within the operating ranges of
the device. Seawater supply pump and filter strainer (15) pumps
this liquid through liquid transfer piping (LTP) to open tube
bundle heat exchanger (19).
Seawater and brine discharge piping (28) is connected to the bottom
end of open tube bundle heat exchanger (19). It extends
transversely from within insulated vapor condensing tower (20) to
the outside of condenser tower (20) and then angles downwardly to
empty into the body of liquid, such as seawater (16). In use,
liquid (16) passes by means of pump (15) into liquid transfer pipe
(LTP) and to open tube bundle heat exchanger (19). Here, the liquid
enters open tube bundle heat exchanger (19) and flows through the
heat exchanger tubes, absorbing heat from the water vapors which
surround the outside of the tubes as discussed below. The liquid
which has passed through the open tube bundle heat exchanger (19),
is then discharged through seawater and brine discharge piping (28)
back to its area of origin, only slightly warmer than the
temperature at which it was originally supplied by seawater supply
pump and filter strainer (15). The water that is returned to (16)
through discharge piping (28) is usually not more than 5 to 10
degrees warmer than when it was originally supplied.
Thus just as the oil from vented oil tank (3) is carried in a full
circle from vented oil tank (3) back to vented oil tank (3), so is
the liquid from point (16) carded from its point of origin and
back.
Extending from the portion of liquid transfer pipe (LTP) which is
situated transverse to the longitudinal axis of insulated vapor
condensing tower (20) and lies outside thereof, is a branch pipe of
smaller diameter than that of the liquid transfer pipe (LTP). This
smaller branch pipe extends generally parallel to the upper portion
of the liquid transfer pipe (LTP) and into the base of insulated
evaporator chamber (21). A make-up water regulating valve (17)
affects the communication between the branch pipe and the liquid
transfer pipe (LTP). When the make-up water regulating valve (17)
is open, the liquid passing through liquid transfer pipe (LTP)
enters the insulated evaporator chamber (21) through make-up water
regulating valve (17). This design and the opening and closing of
make-up water regulating valve (17) enable the system to maintain
the proper water level inside insulated evaporator chamber (21).
That level is a level just below demister pad(s) (22) and covering
open tube bundle heat exchanger (25) both of which are discussed
below. In certain installations in which the entering liquid such
as seawater (16) has a high concentration of oxygen and gasses, a
degassification chamber, such as described in the second embodiment
herein, would be added between make-up water regulating valve (17)
and insulated evaporator chamber (21). This degassification chamber
enables the removal of a majority of these gasses from the
liquid.
Extending within insulated evaporator chamber (21), around its
inside sides and in its lower half, is an open tube bundle heat
exchanger (25). This open tube bundle heat exchanger (25) heats the
seawater contained in the lower half of insulated evaporator
chamber (21). The top half of insulated vapor condensing tower (20)
is surrounded by open tube bundle heat exchanger (25). As seen in
FIG. 1, open tube bundle heat exchanger (25) is fed by heating
source supply piping (23) that extends outside of insulated
evaporator chamber (21). Through supply piping (23) is passed a
heated medium which then enters open bundle heat exchanger (25).
The medium then exits from open bundle heat exchanger (25) by means
of heating source return piping (24) which extends from open bundle
heat exchanger (25) to outside of insulated evaporator changer
(21). Situated between and communicating with both heating source
supply piping (23) and heating source return piping (24) is flow
regulating/bypass valve (29) which enables communication between
both sections if desired. Operation of a heat exchanger such as
shown at (23), (24), (25), and (29) as well known in the art.
There are different configurations of heat exchangers that can
perform the same function as that just described with respect to
open tube bundle heat exchanger (25). Further, the location of the
heat exchanger inside insulated evaporator chamber (21) can be
varied from U-shaped to circular although in all instances the heat
exchanger must heat the liquid in the lower half of insulated
evaporator chamber (21). It must not however, be inside the chamber
nor must it follow the inside configuration of the insulated
evaporator chamber (21). For instance, it may be wrapped around the
lower outside half of the evaporator chamber (21). It must be
located only to heat the liquid below the demister pad (22) that is
discussed below. Sources of heat for open tube bundle heat
exchanger (25) are well known in the art, but some examples of
these am now listed.
a. 80 to 100 degree fahrenheit cooling tower water from industrial
-process or a commercial HVAC system.
b. Heat reclaimed from an internal combustion engine coolant and
exhaust manifold.
c. Low pressure steam.
d. Solar, geothermal, or other free heat.
e. Hot water or steam discharge(s) from utility or electrical
generating plants.
Extending parallel to and above open tube bundle heat exchanger
(25) and generally centrally of insulated evaporator chamber (21),
is a demister or demister pads (22). This pad extends fully across
the inside diameter of insulated evaporator chamber (21 ) creating
a layer that is interrupted only by the top of insulated vapor
condensing tower (20) which passes through demister pad or demister
pads (22). The demister pad is vapor permeable and corresponds in
shape to that of insulated evaporator chamber in horizontal cross
section. Thus the diameter and circumference of demister pad or the
combination of demister pads (22) is generally equal to that of the
inside central area of insulated evaporator chamber (21). Demister
pad or demister pads (22) may be made of separation mesh or similar
materials, stainless steel or PVC or other material generally
impervious to corrosion.
The liquid such as seawater which enters insulated evaporator
chamber (21) by means of the branch pipe and make-up water
regulating valve (17), is heated to approximately 10 degrees
fahrenheit above its original temperature by the heat source
flowing through open tube bundle heat exchanger (25). (Prior to
introducing a heat source into open tube bundle heat exchanger (25)
within insulated evaporator chamber (21), a computer control system
ensures that certain conditions are met. These are that insulated
evaporator chamber (21) is filled with seawater from (16) to a
correct water level, and that the system vacuum level is
established through vacuum piping (9) to insulated evaporator
chamber (21) at latent heat of vaporization point under vacuum
conditions which corresponds to a set relationship with respect to
the temperature of the seawater within insulated evaporator chamber
(21). Introduction of heat to the open tube bundle heat exchanger
(25) may then begin.)
Since insulated evaporator chamber (21) is under vacuum pressure
(due to its ultimate connection to vacuum piping (9) by way of
insulated vapor condensing tower (20) and insulated distillate
water trap (27)), vigorous vaporization of the liquid, likely
seawater, contained in insulated evaporator chamber (21) occurs as
the liquid warms. As this vaporization occurs, demister or demister
pads (22) serves to limit any carryover of particles such as salt
when seawater is involved, into the resulting vapor stream. As the
liquid, here presumably seawater, vaporizes, salts and other
contaminants are separated and settle toward the bottom of
insulated evaporator chamber (21). The vapor meanwhile passes
through the demister or demister pads (22) and ultimately into
vapor expansion area (26).
Extending outside of and from the base of insulated evaporator
chamber (21) is discharge pipe (DP). Discharge pipe (DP) is
situated generally parallel to and alongside of insulated vapor
condensing tower (20). Discharge pipe (DP) is connected by means of
brine discharge regulating valve (18) to seawater and brine
discharge piping (28). This connection allows the concentrated
residue such as salts resulting from the vaporization in the
insulated evaporator chamber (21) to be discharged from the base
insulated evaporator chamber (21) through discharge pipe (DP) into
brine discharge piping (28) and emptied with the fluid from open
tube bundle heat exchanger (19) into the main source of liquid such
as seawater (16). Alternately, the discharge at (28) may be used
with known hydraulic recovery technology (not shown) to reduce
pumping requirements or electrical power requirements. This is
accomplished by utilizing the power from the discharge at (28)
prior to allowing the liquid and residue to return to (16). The
discharge at brine discharge regulating valve (18) can also be
diverted separately from brine discharge piping (28) to allow
collection of contaminants and salts in a suitable container or
evaporation pond.
Returning to the vaporization in the insulated evaporator chamber
(21), as the seawater or other liquid vaporizes and passes through
the demister or demister pads (22), the vapors expand in the
insulated evaporator chamber (21). Here they are pulled into
insulated vapor condensing tower (20) through vapor expansion area
(26). This is due to the vacuum which is transmitted from vacuum
piping (9) through insulated distillate water trap (27). The vapors
condense on the cooler open tube bundle heat exchanger tubes (19)
and then fall as droplets (30) and collect in insulated distillate
water trap (27) located at the base of insulated vapor condensing
tower (20). As soon as insulated distillate water trap (27) fills
completely with liquid, a pressure differential develops between
the vapor in insulated evaporator chamber (21) and the vacuum in
vacuum piping (9), This pressure differential causes the liquid in
insulated distillate water trap (27) to flow in the piping to the
insulated distillate water collection tanks (10). These tanks are
discussed in greater detail with respect to End Collection Zone
(300). The trap feature is unique in that once the insulated
distillate water trap (27) is filled with liquid, the vacuum
requirement for the system diminishes. As the liquid exits the trap
(27), it does not simply revaporize because the vacuum level from
vacuum piping (9) is computer controlled to a latent heat of
vaporization point under vacuum pressure which corresponds to a
temperature greater than the temperature of the water condensing in
the insulated distillate water trap (27).
End Collection Zone (300)
End Collection Zone (300) is composed of reference numerals (10)
through (14) in FIG. 1.
Located below the joinder of vacuum piping (9) and insulated
distillate water trap (27) are at least two insulated and closed
distillate water collection tanks (10). Each insulated distillate
water collection tank (10) has on its topmost portion a water inlet
control valve (13) which connects it via a pipe to vacuum piping
(9). At the opposite, bottom end of each insulated distillate water
collection tank (10) is a collection tank drain valve (11) which
connects each insulated water collection tank (10) to a pipe which
empties the distilled liquid from insulated water collection tanks
(10) into a desired location for potable water. Vent and vacuum
control valves (14) are connected to the tops of insulated
distillate water tanks (10) and in part to each other. They vent
each insulated distillate water collection tank (10) to atmosphere
or seal the insulated distillate water collection tanks (10) within
the vacuum system.
In use, the water from insulated distillate water trap (27) flows
toward the two or more insulated distillate water collection tanks
(10) due to the vacuum pressure transmitted through vacuum piping
(9). The insulated distillate water collection tanks (10) are
exposed to the vacuum pressure in vacuum piping (9) when water
inlet valve (13) is open and collection tank drain valve (11) and
vacuum and vent control valves (14) are closed. The water
collection tanks are at the same vacuum level as the vacuum
transmitted through vacuum piping (9). Thus with water inlet
control valve (13) open, the distilled water flowing from the
insulated distillate water trap (27) flows into the first insulated
distillate water collection tank (10), filling it with water. When
the first insulated distillate water collection tank (10) is
filled, water inlet control valve (13) for that insulated
distillate water collection tank (10) closes and collection tank
drain valve (11) for that insulated distillate water collection
tank (1 0) opens. The vent control valve at (14) for that insulated
distillate water collection tank (10) also opens at that time so
that the water inside the insulated distillate water collection
tank (10) will drain into the potable water discharge piping (12).
As soon as the insulated distillate water collection tank (10) just
drained is empty of water, vent control valve at (14) closes, water
inlet control valve (13) remains closed, collection tank drain
valve (11) closes, and vacuum control valve at (14) opens to
evacuate all air from the insulated distillate water collection
tank (10). Vacuum valve at (14) closes as soon as the tank is
evacuated of such air, and water inlet control valve (13) is
reopened to receive once again the distilled water from insulated
distillate water trap (27). Known sensors controlled by a computer
system are used in End Collection Zone (300) to facilitate the
appropriate opening and dosing of the valves.
The insulated distillate water collection tanks (10) alternately
drain and fill with water so that a continuous flow of water from
water trap (27)to one of tanks (10) occurs. The insulated
distillate water collection tanks (10) are insulated to isolate
them from ambient temperatures, and the piping from the insulated
distillate water trap (27) to the insulated distillate water
collection tanks (10) is also insulated.
The elements described in End Collection Zone (300) could be
replaced by a known rotating vane device or a peristaltic pump and
tank assembly. This is true with respect to the End Collection Zone
(300) in all embodiments.
Vacuum level inside the invention is computer maintained to
correspond to a temperature for vaporization of liquid under vacuum
that is warmer than the incoming liquid being supplied to the
invention. This vacuum and temperature relationship serve to allow
the cooler distillate liquid to not simply revaporize when it exits
trap (27). Further, trap (27) and its collection tanks are
insulated to avoid ambient temperatures from affecting the process,
and the venting and draining of the collection tanks are such that
they do not diminish the vacuum levels inside the desalination
device.
This invention can operate at a broad range of incoming liquid
temperatures and vacuum levels, but one example would be 60 degrees
fahrenheit incoming seawater to the device with a system vacuum
level initially established at 29.25 inches Hg, approximately 70
degrees fahrenheit temperature of heated water in chamber (21), and
water collecting at trap (27) at 60 to 61 degrees fahrenheit. The
test is that the incoming heat source at (23) must be adequate to
elevate the temperature of liquid in boiler chamber (21) so the
liquid will vaporize under vacuum conditions.
The liquid is able to fill and drain from evaporator (21) under
vacuum conditions because of the height of the tower (20) and
evaporator chamber (21) above the barometric level of one
atmosphere (approximately 33 feet). As the brine concentrates are
allowed to exit through valve (18), computer controlled water
regulating valves maintain the proper liquid level in the device by
opening and closing slightly when level sensors in the evaporator
chamber (21) indicate there is a need for liquid to be added.
As stated above, evaporator chamber (21 ) is provided with vacuum
transmitted through the vapor collection pipes, and the heating
elements within insulated evaporator chamber (21) are
thermostatically controlled to elevate the liquid within insulated
evaporator chamber (21) approximately 10 degrees fahrenheit above
the incoming liquid temperature. At vacuum levels of operation,
approximately 1100 btu/lb-m is required to vaporize water within
the evaporator chamber (21). If the incoming feed water is 60
degrees fahrenheit, the boiler chamber will be typically at 70
degrees fahrenheit and the vacuum level will typically be set for
29.25 inches Hg.
The relationship and interconnection of vacuum generating section
(100) to cleansing area (200) am of particular interest in that the
manner in which cleansing section (200) operates to condense vapors
and utilize trap (27) effectively stops substantially any moisture
vapor migration and accumulation of such moisture in oil-filled
towers (1). This feature is significant and has not been addressed
in other similar inventions using oil-filled towers to create
vacuum.
This device recovers low levels of processed heat normally
discarded in other systems. It muses this heat for the process of
creating dean liquid from contaminated liquid. The device purifies
and distills a contaminated liquid (such as seawater to potable
water) and in doing so removes heat from an outside source
processed liquid and feeds it into the system. Here this is through
open tube bundle heat exchanger (25) which then returns the outside
source processed liquid at a lower temperature for reuse in the
external system, Prior art inventions do not make use of low level
processed heat from outside sources. Thus the present invention
replaces or supplements the function of the cooling tower or its
equivalent since it recovers at least a preponderance of the heat
of rejection. This latter aspect is not captured by other
inventions known to the inventor.
This device and process are expandable modularly such that more
than one device are served by the same set of vacuum towers or heat
sources and pumping sources. The attached drawings, which are not
to scale, represent only the schematic relational flow of the
process. There are different configurations for the condenser
tower, boiler chamber, and vapor collection piping. The vacuum
towers, boiler chamber and condenser tower can be partially located
below ground level to minimize height problems. Heat for the
process can be supplied from a number of different sources
including solar, geothermal, steam, hot water, or internal
combustion engine. As an example, the invention could be located
adjacent an oceanside nuclear power generating facility and make
use of the cooling water which is usually returned to the ocean at
substantially elevated temperatures.
Turning now to FIG. 2 and the second embodiment of this invention a
liquid purifying/distilling invention is disclosed.
FIG. 2, may be divided again into three major areas: a Vacuum
Generating Section (1000); a Liquid Cleansing Area (2000); and an
End Collection Zone (3000).
Vacuum Generating Section (1000)
This first area is composed of reference numerals (1') through (3')
in FIG. 2. As in FIG. 1, vacuum pressure is used throughout the
system. In this embodiment, the vacuum pressure is created by the
use of a water seal vacuum pump equipped with air ejectors (1') and
self contained cooling feature. This water seal vacuum pump with
air ejectors (1') transmits vacuum through vacuum regulating valve
(2') located above water seal vacuum pump with air ejectors (1')
and connected thereto by vacuum piping (3'). When vacuum regulating
valve (2') is open, the vacuum pressure created by water seal
vacuum pump with air ejectors (1') is transmitted throughout vacuum
piping (3') and the entire system of the second embodiment of this
invention as seen in FIG. 2.
The vacuum regulating valve (2') has a capillary bleed-off to
control the vacuum level transmitted through vacuum piping (3') to
the rest of the system at the level specified by a computer control
system known to those skilled in the art. On larger applications of
this invention, this section can be substituted in its entirety by
the Vacuum Generating Section (100) described in FIG. 1 which
utilizes oil-filled towers to produce the same vacuum effect. In
certain smaller applications, a standard vacuum pump, usually two
stage with an in-line desiccant or moisture vapor trap of some
type, may be substituted for the water seal vacuum pump.
Liquid Cleansing Area (200)
This second area is composed of reference numerals (4') through
(23') in FIG. 2. An insulated evaporator chamber (4') is flanked on
one side by an insulated and refrigerated heat exchanger (cold)
(17') and on the other side by an insulated degassification chamber
(22'). Insulated evaporator chamber (4'), shown as capsular in
shape, is in fluid communication with both as disclosed below.
Insulated vapor collection piping (16') extends between the tops of
insulated evaporator chamber (4') and insulated and refrigerated
heat exchanger (cold) (17'). Piping extends between the base of
insulated degassification chamber (22') and the lower portion of
insulated evaporator chamber (4'). Valve (23') controls the flow in
that piping and is situated on that piping.
Insulated degassification chamber (22') is capsular in shape.
Refrigerated heat exchanger (cold) (17') is tubular in shape and is
surrounded by refrigeration coils whose sole purpose is to exchange
heat. The coils may as well be placed in the walls of or inside of
the body of heat exchanger (cold) (17'). The base of insulated and
refrigerated heat exchanger (cold) (17') is connected through a
U-shaped trap known in the art and more accurately described herein
as an insulated distillate liquid trap (19'), to vacuum piping
(3'). Insulated liquid trap (19') is essentially the same as the
trap of the previous embodiment and of the embodiment that follows.
Insulated degassification chamber (22') is in direct communication
through a vacuum control valve and piping with vacuum piping (3')
emanating from the top of insulated degassification chamber (22')
and connecting to the Vacuum Generating Section (1000) in order to
provide initial degassification of dissolved gasses from the glycol
solution contained within insulated degassification chamber (22')
as discussed below.
Refrigerant condenser coils (hot) (9') are located in the base area
of insulated evaporator chamber (4') in FIG. 2, but could as well
be wrapped around the outside of the lower portion of insulated
evaporator chamber (4') to transfer the same heat effect to the
liquid that is to be contained therein. Refrigerant condenser coils
(hot) (9') are connected by tubing at one end to a supplemental
refrigerant heat exchanger (8') with fan or other cooling means and
a refrigeration heat pump (7') the latter two of which are located
outside of insulated evaporator chamber (4'). Although supplemental
refrigerant heat exchanger (8') is shown generally below insulated
and refrigerated heat exchanger (cold) (17'), it does not need to
be in that location.
Refrigeration heat pump (7') is connected by tubing to the top of
the refrigeration coils that make up a part of refrigerated heat
exchanger (cold) (17'). At an opposite end, the refrigeration coils
that make up a part of insulated and refrigerated heat exchanger
(cold) (17') are connected through refrigeration expansion valve
(18') to refrigerant condenser coils (hot) (9'). In this way, the
typical closed cycle of a heat/coolant system is used to advantage
to produce heat in insulated evaporator chamber (4') and to remove
heat in insulated and refrigerated heat exchanger (cold) (17').
That is, the heated medium passing through the refrigeration coils
of insulated and refrigerated heat exchanger (cold) (17') passes
through refrigerant condenser coils (hot) (9') to heat liquid in
the base of insulated evaporator chamber (4'). The heated medium
then passes into refrigerant heat exchanger (8') where it is cooled
and recycled back into the top of the refrigeration coils of
refrigerated heat exchanger (cold) (17').
Above the connection between insulated degassification chamber
(22') and insulated evaporator chamber (4') and extending
transversely across the inside of insulated evaporator chamber (4')
generally at its mid point, is demister pad or demister pads (5').
These pads or this pad (5') is generally identical to that
described in the first embodiment herein. Demister pad or demister
pads (5') is vapor permeable and has the same circumference and
diameter as the inside mid section of insulated evaporator chamber
(4'). Thus at the mid section of insulated evaporator chamber (4'),
demister pad or demister pads (5') form a vapor permeable layer
inside insulated evaporator chamber (4') above refrigerant
condenser coils (hot) (9'). Below demister pads or demister pad
(5') but above refrigerant condenser coils (hot) (9') is a
supplemental heating electrode (6'). Supplemental heating electrode
(6') facilitates and supplements the more exact control of the
fluid temperature in the lower portion of insulated evaporator
chamber (4').
Supplemental heating electrode (6') extends from the inside of
insulated evaporator chamber (4') to its outside and rests within a
well in the insulated evaporator chamber (4') that is not
shown.
Solution make-up regulating valve (23') placed between the
connection of degassification chamber (22') and insulated
evaporator chamber (4'), regulates the flow of solution from
degassification chamber (22') to insulated evaporator chamber (4').
In so doing, it maintains a proper solution level in insulated
evaporator chamber (4'). That level is just below demister pad or
demister pads (5') and covering refrigerant condenser coils (hot)
(9') and heating electrode (6').
Below insulated evaporator chamber (4') is a closed insulated fluid
collection tank (10'). The top of this insulated fluid collection
tank (10') is fluidly connected through collection tank inlet valve
(13') to the base of insulated evaporator chamber (4'). Through
another connection at its top, insulated fluid collection tank
(10') is connected by a vent valve at (14') to the atmosphere and
by a vacuum valve at (14') to vacuum piping (3'). At the base of
insulated fluid collection tank (10') is collection tank drain
valve (11'). The base of insulated fluid collection tank (10') may
be opened by collection tank drain valve (11') to drain out the
contents in the insulated fluid collection tank (10') through
discharge piping (12') when the vent valve at (14') opens as
described in greater detail below.
Glycol and water solution from a glycol and water solution tank
(GH.sub.2 O) is transmitted to the upper portion of insulated
degassification chamber (22') by solution feed pump with inlet
filter/strainer (20'). Solution feed pump with inlet
filter/strainer (20') transfers the glycol and water solution
through piping extending from the glycol and water solution tank
(GH.sub.2 O) to the top area of insulated degassification chamber
(22') by means of solution regulating valve (21'). Solution
regulating valve (21') opens to allow a proper solution level to be
maintained in insulated degassification chamber (22'). The proper
solution level is approximately 75 percent full so that them is
only a small area at the top for degassification which is caused by
the vacuum connection of insulated degassification chamber (22') to
vacuum piping (3').
The solution passing through insulated degassification chamber
(22') enters at a rate controlled by valve (23') into insulated
evaporator chamber (4'). The fluid enters below demister pad or
demister pads (5') but above supplemental electrode (6') and
refrigerant condenser coils (hot) (9'). Here, it is heated by means
of refrigerant condenser coils (hot) (9') and supplemental heating
electrode (6'). Through this heating, the water in the solution
vaporizes and separates from the glycol, the glycol being left in
liquid form. The water vapor passes through demister pad or
demister pads (5') while the glycol concentrates and drops into
insulated fluid collection tank (10') by means of collection tank
inlet valve (13'). When a specific gravity or specific conductance
sensor (not shown) associated with insulated fluid collection tank
(10') indicates to a computer hooked to the system of FIG. 2 but
not shown, that the concentration in insulated fluid collection
tank (10') is proper the following occurs. Collection tank inlet
valve (13') closes, the vacuum valve at (14') remains closed,
collection tank drain valve (11') opens and the vent valve at (14')
opens to the atmosphere to allow the glycol to drain into glycol
discharge piping (12'). When all of the glycol has drained from
tank (10'), collection tank drain valve (11') closes, collection
tank inlet valve (13') remains closed, the vent valve at (14')
closes, and the vacuum valve at (14') opens to evacuate insulated
fluid collection tank (10') of air. When insulated fluid collection
tank (10') has returned to a vacuum pressure, the vacuum valve at
(14') closes, and collection tank inlet valve (13') slowly opens
and allows the liquid at the lower portion of insulated evaporator
chamber (4') to enter insulated fluid collection tank (10'). This
liquid will again be displaced by concentrated glycol and the
process repeats itself. The entire collection area can be replaced
by a peristaltic pump and tank assembly in which the computer
control system operates the peristaltic pump to empty the tank
whenever the proper specific gravity or specific conductance level
for glycol is reached.
The vaporized water in insulated evaporator chamber (4') passes
through the demister pad or demister pads (5') and fills vapor
expansion area (15') in the top half of insulated evaporator
chamber (4'). From here it is pulled toward the insulated and
refrigerated heat exchanger (cold) (17') due to the vacuum pressure
and cooler condensing temperatures therein. In the insulated and
refrigerated heat exchanger (cold) (17') the vapor gives up its
heat and condenses into a liquid and collects in the insulated
distillate liquid trap (19') below the insulated and refrigerated
heat exchanger (cold) (17').
Different configurations of this embodiment are possible and
particularly in large applications the following possibility
amongst many might be considered. Insulated and refrigerated heat
exchanger (cold) (17') could be situated below insulated evaporator
chamber (4'). This would be similar to that shown in FIG. 1 with
connections to the upper and lower portion of evaporator chamber
(4') being modified to match that shown in FIG. 1 with respect to
insulated evaporator chamber (21). Further other heating and
cooling sources and means can be used in lieu of the heat pump to
accomplish the same purposes.
End Collection Zone (3000)
This area to FIG. 2 is composed of reference numerals (24') through
(28') and is located between the Vacuum Generation Zone (1000) and
the Liquid Cleansing Zone (2000). Its design and operation is
essentially the same as that described with respect to the previous
embodiment. Again, end collection zone (3000) is comprised of at
least two closed insulated distillate collection tanks (26'). These
tanks are each in fluid communication through a water inlet control
valve (24') at their top ends with vacuum piping (3') and insulated
distillate liquid trap (19'). Also at their top ends they are
connected by vacuum and vent control valves at (25') either to the
atmosphere or to vacuum piping (3'). The base of each insulated
distillate collection tank (26') is connected by means of one
collection tank drain valve (27') to discharge piping (28').
The water from insulated distillate liquid trap (19') flows through
the piping connecting it to vacuum piping (3') and insulated
distillate collection tanks (26'). From here it flows toward the
two or more insulated distillate collection tanks (26'). This is
due to the vacuum transmitted through vacuum piping (3'). The water
exiting insulated distillate liquid trap (19') does not revaporize
because the computer control system selects the vacuum level at
vacuum piping (3') which corresponds to the latent heat of
vaporization point for water which corresponds to a higher
temperature than the temperature of water exiting insulated
distillate liquid trap (19'). The insulated distillate collection
tanks (26') are subjected to vacuum from vacuum piping (3') when
water inlet valve (24') is open, collection tank drain valve (27')
is closed, and vacuum and vent valves at (25') are closed. The
insulated distillate collection tanks (26') are at the same vacuum
level as that of vacuum piping (3').
Water flows from the insulated distillate liquid trap (19') into
the first insulated distillate collection tank (26') through open
water inlet control valve (24'). When the first of the insulated
distillate collection tanks (26') is filled with water, water inlet
control valve (24') to that insulated distillate collection tank
(26') closes, collection tank drain valve (27') to that tank opens,
vacuum valve at (25') to that tank remains closed, and vent valve
at (25') for that tank opens and the distillate inside the tank
drains to the discharge piping (28'). As soon as that insulated
distillate collection tank (26') is empty of fluid, the vent valve
at (25') closes, water inlet control valve (24') remains closed,
collection tank drain valve (27') closes, and the vacuum valve at
(25') opens to evacuate all air from the freshly emptied insulated
distillate collection tank (26'). Once the insulated distillate
collection tank (26') is evacuated, the vacuum valve at (25')
closes, and water inlet control valve (24') is opened to allow the
distillate to be once again collected in the insulated distillate
collection tank (26').
The insulated distillate collection tanks (26') alternately drain
and fill so that a continuous flow of water through the insulated
distillate liquid trap (19') occurs. The insulated distillate
collection tanks (26') are insulated to isolate them from ambient
temperatures, and the piping from the insulated distillate liquid
trap (19') to the insulated distillate collection tanks (26') is
also insulated.
The elements described in this area could be replaced by a known
rotating vane device or peristaltic pump and tank as described in
the previous embodiment.
The discussion with respect to the second embodiment herein has
been directed to the separation of water from glycol. Again, it is
to be understood that other liquids, fluids or solutions are
contemplated including human and animal bodily fluids. If one is to
use the second embodiment in the treatment or cleansing of blood
such as plasma pheresis, certain modifications are understood to be
made. Solution feed pump with inlet filter/strainer (20') may be
replaced by intravenous tubing connected at solution regulating
valve (21') and then to a donor or typical blood collection
container or used in conjunction with other blood processing
equipment which separates out red blood cells from plasma. Blood
distillates collected at insulated distillate collection tank (26')
would not be exposed to atmosphere at the vent valve at (25') nor
would they be discharged into piping as shown at (28'). Instead,
blood distillates would be collected at insulated distillate
collection tank (26') in a suitable detachable container approved
for medical purposes which would allow the distillate to remain
sterile and under a vacuum condition. This vacuum distillate in the
detached container (26') could be tested, supplemented, and
reinjected into a donor or stored for future use. Blood
concentrates (salts, residues,etc. ) collected at tank (10') may be
stored for later recombination with the distillate or otherwise,
may be reused, may be tested and screened, or may be disposed of
all as desired by the user.
Tank (10') may also be replaced by a rotating vane device or
peristaltic pump and tank assembly. The computer control system
which controls the emptying of tank (10') can respond to either
specific conductance or specific gravity.
The purpose of this embodiment is to separate certain specific
fluids in solution using low temperatures and vacuum. Examples for
its use are the separation of water from glycol solutions, ethylene
and propylene glycol from glycol/sludge/additives solutions, and
metals finishing industry solutions which require separation of one
fluid from a solution, or purification of a certain fluid by
separation of solids in solution with it. The computer control
system used would allow the selection of various fluids based upon
their specific gravity and vaporization points under vacuum
conditions. Such systems are known in the art. The vacuum pressure
used in this embodiment is selected to correspond to the
vaporization point of the particular fluid which will be removed
first from the process.
FIG. 3 is the third embodiment of this invention. It too is
comprised of three areas of study, the Vacuum Generating Section
(100), the Liquid Cleansing Area (20,000), and the End Collection
Zone (300). The Vacuum Generating Section (100) and the End
Collection Zone (300) are identical to that shown in FIG. 1 and
therefore no further discussion of these areas is made. Again
Vacuum Generating Section (100) may be replaced by a known vacuum
system and the End Collection Zone (300) may be replaced by a known
peristaltic pump and tank assembly or by a rotating vane device.
The first embodiment herein is most closely related with this last
third embodiment and both operate very similarly. Reference to the
operation of the first embodiment will be of use in understanding
this third embodiment.
Liquid Cleansing Area (20,000)
The liquid cleansing area of this embodiment is comprised of
reference numerals (12") through (17") and reference numerals (21")
through (27").
Liquid, seawater, contaminated water, or water from a large body of
water (17") is transported by means of pump (16") through water
line (WL). Pump (16") is connected to waterline (WL). Water line
(WL) extends from (17") to a first branch (WLB1) and a second
branch (WLB2). Water line branch one (WLB1) extends into an
insulated heat exchanger (13"). Water line branch two (WLB2)
extends into an insulated degassification tank (24") which is
discussed more fully in later paragraphs. Insulated heat exchanger
(13") is capsular in shape. Extending around the internal middle
and lower portion of insulated heat exchanger (13") are a plurality
of tubes which communicate with each other and water line branch
one (WLB1) in a traditional heat exchanger configuration well known
to those skilled in the art. Liquid from (17") is pumped by means
of pump (16") through water line (WL) and water line branch one
(WLB1) into and through the tubes in insulated heat exchanger
(13").
The bottom of insulated heat exchanger (13") opens into an
insulated pipe which leads into a U shaped trap (27"). Trap (27")
is also insulated and continues into an insulated pipe that leads
into End Collection Zone (300). Trap (27") and its immediate
connections are identical to those disclosed in FIG. 1.
The liquid in water line branch one (WLB1) passes into and through
the tubes in insulated heat exchanger (13") and exits insulated
heat exchanger (13") at a water line branch three (WLB3). Water
line branch three (WLB3) is surrounded by insulation and has two
ends and one valved branch connection, water line branch four
(WLB4). One of the two ends connects to the top side of the tubes
in insulated heat exchanger (13"). This connection is opposite to
and above the connection of water line branch one (WLB1) with the
tubes in heat exchanger (13"). The other of the two ends connects
at the lower half of an insulated boiler chamber (12") to heat
reclaim coils (23") both to be discussed in the following
paragraphs. This connection of water line branch three (WLB3)
causes the first end of water line branch three (WLB3) to be
located at a higher level than the second end of water line branch
three (WLB3). Water line branch four (WLB4) is a bypass pipe and
valve which is computer controlled according to the temperature of
the fluid in water line branch three (WLB3). It is connected
between water line branch three (WLB3) and exit pipe (EP) which is
also discussed in the following paragraphs.
Situated near insulated heat exchanger (13") and of similar shape,
is insulated boiler chamber (12"). Boiler chamber (12") is
connected at its top end by means of insulated vapor collection
piping (14") to the top end of insulated heat exchanger (13").
Situated around the lower mid section of insulated boiler chamber
(12") are heat reclaim coils (23") which connect at their top side
to water line branch three (WLB3). Above heat reclaim coils (23")
and within insulated boiler chamber (12") is heating electrode
(26") which heats the liquid contained in insulated boiler chamber
(12"). Heating electrode (26") is typically powered by an external
electrical power source, or may be a supplemental hot water
exchanger supplied with heat from a cooling tower or similar source
as described in the first embodiment. The purpose of the electrode
or heat source (26") is simply to heat and maintain the water in
the boiler chamber (12") at the correct temperatures, and this heat
may come from a variety of sources. As noted in the first
embodiment, the vacuum level is first established at the proper
level prior to introduction of heat. In certain installations (not
shown) in which the boiler chamber (12") and heat exchanger (13")
are relocated to 42 to 50 feet in overall height in similar fashion
as described below, the heating electrode may be supplementally
powered by electrical power hydraulically recovered from the water
exiting at exit pipe (EP). Such hydraulic recovery is well known to
those skilled in the art.
Demister pads (28") are located in the top upper portion of
insulated boiler chamber (12") above heat electrode (26"). They are
dimensioned and perform the function as described in previous
embodiments.
Liquid exiting water line branch three (WLB3) enters and flows
through heat reclaim coils (23"). Connected to the lower portion of
heat reclaim coils (23") at that side opposite water line branch
three (WLB3) is water regulating valve (15") and exit piping (EP).
Exit piping (EP) connects with bypass water line (WLB4) below valve
(15") and then extends into the original body of liquid, which may
be seawater (17"). The liquid passing through heat reclaim coils
(23") exits through computer controlled water regulating valve
(15") into exit piping (EP) and is returned to the original body of
liquid which may be seawater (17"). In certain installations,
hydraulic recovery of the pumping forces supplied by pump (16") and
exiting through exit pipe (EP) will be achieved by relocating (not
shown) the height of boiler chamber (12"), degassification chamber
(24"), cross duct or vapor collection piping (14"), and insulated
heat exchanger (13") to a position 42 to 50 feet above ground. This
is done by lengthening connecting piping water line (WL), exit pipe
(EP) and piping leading to trap (27") and tank (21 "). The purpose
will be to recover the forces from the liquid exiting at exit pipe
(EP) before that liquid returns to the original body of liquid and
to use this recovered hydraulic power to reduce pumping or
electrical requirements in the same fashion as in the first
embodiment described herein.
As noted earlier, a portion of the seawater or unfit liquid brought
from body (17") is diverted into water line branch two (WLB2). This
branch circumvents insulated heat exchanger (13") and passes into
insulated capsular degassification chamber (24"). Water line branch
two (WLB2) could as well branch from water line branch three (WLB3)
or exit pipe (EP). The purpose of water line branch two (WLB2) is
to provide make-up liquid to degassification chamber (24").
Degassification chamber (24") is in fluid communication with
insulated boiler chamber (12") by means of insulated piping and
valve (25") and it is located to the side of insulated boiler
chamber (12") near exit pipe (EP). The connection of
degassification chamber (24") to insulated boiler chamber (12") is
above the connection to exit pipe (EP) and water regulating valve
(15") and below demister pad (28") but above heat reclaim coils
(23") and heating electrode (26"). At its top end, degassification
chamber (24") is in direct fluid communication with vacuum line
(VL) having its origins in Vacuum Generating Section (100). In use,
seawater or unfit liquid passing through water line branch two
(WLB2) into degassification chamber (24") is subject to vacuum
pressure to remove dissolved gasses.
The seawater or unfit liquid passes through degassification chamber
(24") and regulating valve (25") into boiler chamber (12") and
there is exposed to electrode (26") and heat reclaim coils (23").
Valve (25") serves to regulate makeup fluid level within boiler
chamber (12") and to maintain that fluid level at the proper
operating level below demister pad (28") and covering electrode
(26") and heat reclaim coil (23"). In view of this exposure, at
least a portion of the liquid boils. The vapor from the boiling
liquid passes through demister pad or pads (28") into vapor
collection piping (14") and from there into insulated heat
exchanger (13"). Meanwhile, residue in the liquid brought into
insulated boiler chamber (12") from degassification chamber (24")
is separated by means of the boiling action in boiler chamber (12")
and falls to the bottom of insulated boiler chamber (12").
The base of insulated boiler chamber (12") is connected by means of
a closable valve to a closed brine tank (21"). Brine tank (21") is
in turn connected at its base through a valve to an open brine
collection tank (22"). Insulated boiler chamber (12") and brine
collection tanks (21") and (22") are connected together in series
with insulated boiler chamber (12") being above and in line with
brine tank and brine collection tank (21"and 22"). Although brine
tank (21") is a closed unit, through its top it is in valved fluid
communication with vacuum line (VL) as well as boiler chamber
(12"). The vacuum connection facilitates the collection of brine
from insulted boiler tank (12").
In view of the connection of insulated boiler chamber (12") to
brine tank (21"), the salt residues and other contaminants from the
seawater (17") that settle in the bottom of boiler chamber (12"),
pass into brine tank (21"). These residues are allowed to settle as
a concentrated brine solution and displace the seawater contained
in brine tank (21") until the outside computer controls note that a
total dissolved solids, specific gravity, or conductivity level is
reached. At this time, the brine is drained into tank (22"). The
valve between insulated boiler chamber (12") and brine tank (21")
closes off to maintain vacuum in the chamber (12") while the brine
is drained from brine tank (21") to brine collection tank (22").
The drain between the two tanks (21", 22") then closes and the
vacuum valve opens momentarily to evacuate air from brine tank
(21"). This valve then closes and the valve between brine tank
(21") and insulated boiler chamber (12") slowly reopens to allow
brine to once again collect in brine tank (21"). Valve (25")
operates to allow water from the insulated degassification tank
(24") to enter insulated boiler chamber (12") to compensate for the
refilling of brine collection tank (22"). Degassification chamber
(24") is sized to be of larger capacity than brine collection tank
(22"). Tanks (21" and 22") may be replaced by a rotating vane
device or a peristaltic pump and tank assembly. The computer
control which controls the emptying of the tank (21") can respond
to either specific conductance or specific gravity.
The vapor passing through piping (14") enters insulated heat
exchanger (13") and passes over the tubes therein carrying liquid
from water line branch one (WLB1). The vapor is thereby cooled and
condenses as it passes over the tubes in insulated heat exchanger
(13"). Simultaneously, the liquid passing through the tubes in
insulated heat exchanger (13") is heated by the vapor passing over
the tubes. Once the vapor condenses, it drains out of the base of
insulated heat exchanger (13") into trap (27). From there it
proceeds to End Collection Zone (300) as described in the preceding
figures.
Vacuum level inside the invention is computer maintained to
correspond to a temperature for vaporization of liquid under vacuum
that is warmer than the incoming liquid being supplied to it. As
one example, 60 degrees fahrenheit seawater to the device will
require boiler chamber (12") to be at a temperature of
approximately 70 degrees fahrenheit in order to maintain full
process capabilities. The vacuum level will have been initially
established at 29.25 inches Hg so that the water exiting trap (27")
does not revaporize. This device can operate under a broad range of
temperatures for the seawater or other liquid being supplied to it.
The test is that the incoming heat source (26") in conjunction with
the heat recovery source at (23") must adequately elevate the
liquid in boiler chamber (12") to vapor under vacuum
conditions.
As stated above, the boiler chamber (12") is provided with vacuum
transmitted through vapor collection pipes (14"). The heating
element or heating source (23") is thermostatically controlled to
provide enough heat to elevate the liquid within the boiler chamber
(12") to vapor. At vacuum levels of operation, approximately 1100
btu/lb-m is required to vaporize water.
The foregoing description is only one example of the manner of
accomplishing the invention. Obvious modifications are within the
contemplation to the inventor. One modification is changing the
floating head heat exchanger for a direct heat exchanger, or
changing the configurations of the boiler chamber, evaporator, heat
exchanger, and location of heat reclaim coils.
Another modification might involve the heat reclaim coils (23"). In
some instances, the heat reclaim coils (23") will be located on the
(WL) or located in or around the insulated degassification tank
(24"). It is understood that when the insulated degassification
tank (24") has heat reclaim coils (23") located around or in it,
that the vacuum level of the system will be adjusted by computer so
that water vaporization in the degassification tank (24") does not
occur.
This sort of modification could be made in the first or third
embodiments herein.
In this embodiment and the previous embodiments, fluids, heat, and
energy are by means of closed exchange systems continuously
recycled to maximize efficiency, reduce costs in construction and
usage, and diminish impact on the environment.
* * * * *