Note : Les descriptions sont présentées dans la langue officielle dans laquelle elles ont été soumises.
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BACKGROUND OF THE INVENTION
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This invention relates to an energy efEicien-t process
and apparatus for desalinizing wa-ter, and more particularly to a
desalinization sys-tem which uses a temperature dif~erential
created wi-thin the con-text of the weather environmen-t in which the
apparatus is located to furnish the heat of vaporization required
to boil salt water and to dissipate heat of condensationr
There are many known methods of desalinizing watex
based on distillation. Considerable effort has been expended
attempting to design a system capable of producing fresh water
at a cost low enough to service a large population or agricultural
area. In general, the approach has been to conserve the heat
; given up when water vapor condenses to vaporize additional
quantities of water, thus reducing the total amo~mt of heat used
per unit mass of fresh water produced.
In designing a desalinization ~ystem, the~e are
essentially two areas of cost which must be considered: initial
capital outlay; and the ongoing operational cost which încludes
the price of the energy consumed and the price of maintenance.
In areas where local natural supplies of fresh water are low, the
capital costs of constructing a laxge desalinization plant will ~ -
often be competitive with the costs o~ a pipeline~ E~owever~
operational expenses are another matter, and as the cost of
energy increases, the possibility that desalinized water can
compete with piped sources of fresh water has become more remote.
Nevertheless, there are areas of the world which ould be
developed to support sizeable populations if provided with fresh
water, yet many of these are located such that no significant
possibility exists for servicing the land with natural fresh
water.
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1 Almost by deEinition, these areas are hot and dry, and
accordingly are characterized by lo~ humidity and days of un-
interrupted direct solar exposure. Uncler these conditions, it is
now possible to produce a sizeable temperature differential
withou-t consuming energy generated from f~ssil or nuclear fuels.
Rather, "hot" and "cold" thermal sinks may be produced by taking
advantage of ambient conditions.
SUMMARY OF THE INVENTION
The instant invention comprises a process ancl apparatus
for desalinizing ~ater which can take advantage of a natural or
artificially created temperature differential to provicle the heat
of vaporization necessary to boil salt water and to dissipate the
heat of condensation produced on formation of pure water. Only
minimal amounts o~ energy are required. Furthermore, the capital
cost is believed to be no greater than that required for a con~
ventional desalinization system. The foregoing characteristics
make the instant invention highly attractive and are directly
: traceable to the novel combination of process steps and components
disclosed herein.
In its broadest overall aspect, the invention lnvolves
moving heat from a "hot" thermal sink of the types disclosed
herein to an evaporation zone which is maintained at subatmos-
pheric pressure, allowing vapor produced on boiling to migrate to
a condensation zone, and moving heat of condensation from the
condensation zone into a "cold" sink. At least one o~ the heat
transfers, either ~rom the hot sink to the evaporation zone or
from the condensation zone to the cool sink, is effected via a
closed system wherein a refrigerant is cyclically condensed and
evaporated (e.g.~ a refrigeration cycle or a "thermal cycle") and
wherein the ratio of energy transferred as heat to energy required
to ef~ect the transfer is at least 15 and preferably 30 or above.
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1 Thus, in the process of the i.nvention, salt water is
fed into an evaporation zone which is maintained at a subatmos-
pheric pressure low enough to cause the water to boil at close to
ambient temperatures. In order to maintain boiling, heat is
transferred to the water in the evaporation zone from a thermal
sink, preferably using a heat pump. To assure that the vacuum is
maintained, the evaporation zone is serv:iced by an evacuation
system for removing non-condensibles and the water vapor produced
is condensed in a condensation zone from which heat is removed
as water is formed by being dissipated into a cold sink. The
cold sink may comprise a naturally oocurring relatively low
temperature sink such as ocean water or an evaporation cooling
apparatus which takes advantage of a low humidity environment.
The thermal sink from which heat is transported to
maintain boiling is not created by burning fuels and is not
normally a high temperature heat source. However, it is contem-
plated that ~aste heat from a nuclear power plant or some other
available source of water such as a naturally occurring hot spring
may be utilized if available. In general, the thermal sink is -
characterized in that heat it gives up to Water in the evapora-
tion zone is made up by heat which would otherwise be discarded
e.g. relatively "low level" heat. Thus, otherwise expendable
heat is dissipated into the thermal sink as makeup heat from, for
example, the sun. Accordingly, the thermal sink may compxise an
artificially created high surface area lake which is fed with
salt water and covered ~ith a transparent sheet to retard
evaporation. It may comprise a mass of material ha~ing a suit-
able melting point which stores up solar heat as heat o fusiQn
such as Glauberls salt. The thermal sink may simply comprise the
3~ surrounding air or an area of the ground exposed to the sun. In
t~is case, a heat: colleoting m~ans will be required~
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1 The heat pump which is used to transport heat comprise5
either a refrigeration cycle or a "thermal cycle!' of the type
hereinafter described. When hot wat~r from geothermal or nuclear
cooling water sources is available, no heat pump whatever need
necessarily be employed. In this case, the heat of vaporization
required to maintain boiling may be provided by direct heat
exchange. To dissipate the heat of condensation, a naturally
occurring sink, such as ocean water, having a temperature lower
than the reduced pressure boiling point or evaporative cooling
may be employed.
EvaporatiVe cooling apparatus is well known in the heat
exchange art and comprises a heat exchanger over which water is
cascaded and air is moved. As the cascading water evaporates,
the outer surfaces of the coils of the exchanger tend to seek
thermal equilibrium with the dew point. Fluid in contact with
inner surfaces of the coils seeks the same equilibrium. Within
certain limits, the temperature may be controlled by ~arying
the amount of air forced through the apparatus. In accordance
~ith the invention, the condensation zone ma~ comprise a portion
~0 of the interior of such an evaporative cooling apparatus, or may
comprise a separate zone serviced by a refrigeration or thermal
cycle ~or transporting heat therefrom to a low temperature sink -
or to evaporative cooling apparatus.
In one important embodiment, the apparatus of the inven-
tion comprises both a refrigeration cycle and a thermal cycle,
arranged in parallel, to transport heat ~rom the ~hermal sink to
the evaporation zone. If a switch is utilized to activate one of
the two cycles at a particular time, in a manner disclosed herein,
it is possible to adapt the desalinization apparatus ~or ~aximum
output at minimum energy as dictated by the varying temperature
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1 di~ferential between the thermal sinks, e.g., in response to
fluctuations in the ambien-t dew point.
~ ccordingly, objects of the invention include the
provision of a method and apparatus for clesalinizing water which
consumes no fossil or nuclear fuels other than that which may
be required to generate the electricity needed to run the electric
motors which service compressors vacuum pumps, or the like.
Another object of the invention is to provide a water
desalinization system which can undergo a change in mode of oper-
ation in response to changes in ambient conditions a5 requiredfor low energy consumption. Still another object is to provide
a water desaliniæa-tion system characterized by a capital outlay
low enough to be competitive with conventional systems. ~nother
object is to provide a desalinization apparatus which desaliniæes
water at close to ambient temperatures and thus reduces or
eliminates the buildup of scale and requires no insulation ~o
prevent heat loss. Yet another object is to provide a water
desalinization apparatus which may be scaled to provide the
fresh water requirements for an ocean going vessel or the like
or for a population center or agricultural area.
Still other objects of the invention are to provide a
water desalinization proceas and apparatus which may be designed
to take advantage of the ambient conditions of a particular
locality to produce fresh water at the lowest practical cost, and
to provide a novel desalinization system and process which employs
; components well known in the heat exchange, refrigeration, and
related arts, and which will accordingly minimize design
engineering problems.
These and other objects and features of the invention
will be apparent *o those skilled in the art from the following
description of some preferred embodiments and from the drawings.
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1 BRIEF DESCRIPTION OF T~ DE~WINGS
Fig. 1 is a schematic diagram illustrating one import-
ant em~odiment of the water desalinization apparatus of the :
invention;
Fig. 2 is a schematic diagram illustrating a secondembodiment of the apparatus of the invention;
Fig. 3 is a phase diagram for refrigerant 11 ~trichloro- :
fluoro methane) useful in illustrating the energy efficiency of
. the process of the invention and showing the thermal character-
: 10 istics and changes oP state which the refrigerant undergoes in
two refrigeration cycles;
Figs. 4, 5, and 6 are diagrammatic illustrations of
other embodiments of the invention; and
Fig. 7 is a diagram illustrating the Plow of heat in
accordance with the invention.
Like reference characters in the respective figures ~:
indicate corresponding partsO All temperatures are in Farenheit
degrees.
DESCRIPTION OF THE PREFERREI) E~BODIMENT
:
;- 20 The energ~ ePficiency of the desalinization process and
apparatus o the invention ultimately depends on the difference
in temperature which is naturally present or can be created within
: the context of the area in which the apparatus is located. The
greater the temperature diPferential, the lower will be the energy :
:~ requirements. Accordingly, it is desirable to design the s~stem
to exploit a naturally occurring temperature diPferential or to :
create and maintain the greatest temperature differential possible
under the circumstances. It is not ~ithin the scope of the :
invention to, for example, create a thermal sink by burning fossil
3~ fuels to heat a boiler. However, in aituations ~here Puels axe
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l already bein~ consumed for other purposes) the otherwise expend-
able waste heat may be absorbed in water or otherwise dissipated
within a mass of material to maintain -the temperature of the
thermal sink. Where such heat sources are not available~ the
thermal sink may comprise a body of sal-t water, either natural
or man made, which is exposed to the sun and includes means for
inhibiting evaporation such as a transparent plastic sheet placed
over its surface. In this circumstance~ the body of water will
thermally equilibrate with its environment and heat removed from
the water will be made up by the sun.
Another useable thermal sink is the air itself. Thus,
in desert areas, the mean air temperature may approach 85 or
more and thus can provide a limitless heat supply. In this
situation, a high surface area heat collecting structure
designed using principles similar to those emplo~ed in construct-
ing heat exchangers will be required. Use o this type of thermal
sink is characterized by significant fluctuations in temperature,
i but in accordance with the principles disclosed hereinaf~er, su~h
fluctuations may be handled simply and automatically.
~0 Another possibility for the thermal sink is an expanse
of hot said~ Thus, heat can be extracted from the earth itself
via coils placed just below the surface. This type of sink would
also undergo daily temperature fluctuations.
Still another possibility for the thermal sin~ is a mass
of material having a high heat of fusion and a melting point suit-
able to allow changes of state at close to ambient temperatures,
e.g., Glauber's salt~ Na2S04 ~ lOH20 (M.P~ = 213). These can be
melted by being exposed to the sun, the sun's energy being stored
as heat fusion, and large quantities of heat may be removed
there~rom~
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1 It is from one of the foregoing types of thermal sinks
or others tha-t may be invisioned that heat is extxacted to pro-
vide the heat of vaporiza-tion which maintains boiling in the
process and apparatus of the invention in a reduced pressure
evaporation zone. To maintain boiling, it: is necessary to assure
that the pressure above the boiling salt water doe~ not build up.
Thus, the build-up o~ noncondensibles is prevented by employing a
vacuum pump. Also, water vapor must be conde~nsed and the heat of
condensation must be removed. If the bolling point is hi~h
enough, condensation may be effected, ~or example, b~ direct heat
exchange with ocean wa~er. However, alternatively, heat o~
condensation may be removed by evaporative cooling.
Evaporative cooling devices are well known in the heat
exchange art and in general may readily be designed on a scale
suitable for any particular application. These devices comprise
heat exchangers which typically contain a fluid from which heat
i5 to be extracted. The exterior surface of the heat exchanger
is contacted with water and a fan blows air across the surface
to cause evaporation. The temperature which can be obtained in
the interior of the apparatus is dependent on the ambient dew
point. At the present state of the art, it is a matter of
mechanical skill to maintain fluid contained within an evapora-
tive cooling apparatus at a temperature substantially equal to
the dew point. Thus, the tsmperature which can be obtained by
evaporative cooling will vary as the dew point varies.
Utilizing the techniques disclosed above, it is possible
to readily create a temperature di~ferential of at least 20,
that is, to obtain a condition wherein the temperature of the
"hot" thermal sink is 20 higher than the temperature o~ a l'cold"
sink or that within an evaporative cooling apparatus. In most
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1 situations, much larger ~emperature differen-tials can be produced.
Also, there are many situations where a natural temperature
differential exists and need only be properly exploited. An
example is the sea, where surface water layers and deep water
layers difEer significantly in temperature.
The invention contemplates boiling water to be desalin-
ized in an evaporation zone, trans~erring heat from the thermal
sink to the evapoxation ~one to provide the heat of vaporization,
and then condensing the vapor by removing heat therefrom and
dissipating it into a lower remperature thermal sink or via
evaporative cooling. To lower the boiling point of the water,
the evaporation zone (and condensation zone) is evacuated to a
pressure less than the vapor pressure of the salt water to be
boiled and is serviced by a vacuum pump for removing non-
condensibles.
Fig. 7 illustrates the broad concept of the invention.
Heat is moved from the "high" temperature sink to the evaporation
zone where it i5 utllized as heat of VapOriZatiQn. Vapor passes
to the condensation zone where it is condensed. The heat of
condensation is transported to the "low" temperatuxe sink. A
vacuum pump removes noncondensibles from the evaporation and
condensation zone and draws fresh water from the evacuated system.
The greater the temperature difference between the sinks, the less
enexgy required to move heat to the evaporation zone and from the
condensation zone, and/or the smaller the heat exchangers required.
The means for moving heat, both to the boiling salt water and
from the condensing fresh water comprises a refrigeration cycle,
a "thermal cycle", or, in an appropriare case a heat exchanger
wherein heat is transferred directly. The energy efficiency of
3~ the system arises because the refxigeration cycle may be run at
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1 very high coefEicients o~ per~ormance, and because the ratio of
energ~ transf~rred as heat to energy re~uired to ef~ect the
transfer in the ~he~mal cycle is ~ery high.
Fig. 1 illustrates an important embodiment of the
apparatus of the invention. Water or other heat carrying fluid
is moved by a high volume~ low pressure pump 9 from a thermal
sink 13 through heat exchanger 10. As illustrated, the heat
exchanger 10 compri~es a jacket 11 which encloses an arra~ of
pipes 12. Water flows through the pipes, loses heat to fluid
located in the interstices therebetween, and exists in the
direction of arrows 15. Heat exchanger 10 is maintained in
thermal communication with an evaporation zone 16 and the heat
exchanger 14 disposed therein by a pair of heat pum~s arranged
in parallel. The first heat pump is a refrigeration cycle
comprising a compressor 18 which circulates a refrigerant, e~g.,
one of the family of fluorocarbons sold under the trademark
Freonr along conduit 20, through the coils of heat exchanger 14,
back through a pump 26, val~e 33, and conduit 22~ through a
float valve 25 (or other means for allowing expansion, such as
20 a restriction), through heat exhanger 10, and back to conduit ~
20. The second heat pump is a "thermal cycle" comprising a ~`
pump 26 which circulates refrigerant through valve 33, conduit
28, heat exchanger 10, conduit 30 and valve 32, and heat exchanger
14. A switch 31 controls valve 32 and three-way valve 33 so that
either the thermal cycle or the refrigeration cycle may be
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activated. When the refrigeration c~cle is activated, refrigerant
~reely passes through the pump 26 or, if necessary, its circu~
lation may be assisted thereby.
Heat exchanger 14 is disposed ~ithin the evaporation
zone 16 ~hich receives water to be desalinized at inlet 36 and
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1 expels a more concentrated brine at waste outle.t 38 with the aid
of a pump (not shown). A subatmospheric pressure is mainta.ined
within e~aporation zone 16 by a vacuum maintaining means 40.
There are several suitable me~hod of removing noncondensibles
from the evaporation zone 16 which do not require large amounts
of energy. Thus, high efficiency two s-tage pumps are commercially
available which are capable of creating and maintaining a vacuum.
Alternatively, a ~mall pump can transport gas from the low vacuum
in evaporation zone 16 to a high subatmospheric pressure zone
(not shown)which itself is maintained at reduced pressure by a
high volume, relatively low efficiency pump. Sti.ll another
alternative is to utilize an ejector to produce a vacuum of a
pressure close to the vapor pressure of the water wh~ch passes
~ through the ejector, and to employ a small vacuum pump to
: transport gas from the evaporation zone into the ejector created
; vacuum. It may be preferable to locate vacuum maintaining means
i 40 in the Condensation zone as illustrated in Fig. 7 to assist
in vapor transport.
. The evaporation zone 16 is in communication with a
~ondensation zone 43, which in this embodiment takes the form of
a portion of the interior of an evaporative cooling apparatus
42. The evaporative cooling apparatus comprises a heat exchanger
: over which salt water 44 is cascaded and air 46 is ~lown ~y a
fan 47. The temperature within the evaporative cooling apparatus
42 may be as low as the ambient dew point, or warmer than t~e . : -
air which is passed over the coils. . :
To illustrate the operation of the apparatus of Fig. 1,
it will first be assumed that on a.given day the dew point is
76 and the temperature of the thermal sink and thus of the coils
. 30 12 is 80. Salt water is fed into evaporation zone .l6 at 36 and
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1 a suba-tmospheric pressure is maintained by vacuum pump 40 to
the degree necessary to initiate boiling of the salt water. As
boiling commences and heat of vaporization is lost, the salt
water begins to cool~ However, the temperature in the evapora-
tion zone is maintained as the boiling ~ater picks up heat Erom
heat exchanger 14~ If the pressure withi:n evaporation zone 16
is maintained.such that the boiling point of the salt water is 86,
: the 86 vapor will condense within the 76 condensation zone 43,
heat of condensation being dissipated by the evaporative cooling
apparatus 42, and fresh water being produced at 48. The 10
temperature differential between the vapor and condensation zone
42 is effective to promote the heat exchange necessary to maintain
the rate of condensation. A small pump 49 removes fresh water
from the reduced pressure environment within condensation zone
43.
In the situtation here hypothesized, the thermal sink ~ :
is at B0 and the water in the evaporation zone 16 boils at 86. ..
Accordingly, the refrigeration cycle must be employed.
With valve 32 closed and valve 33 open to conduit 22,
~ refrigerant vapor taken from heat exchanger 10 through conduit .
20 is compressed by compressor 18, which is designed in accor-
dance with known principles for moving large volumes of ~ :
refrigerant vapor at relatively low pressure differentials. The ~ :
action of the compressor raises the temperature of the vapor to
96 and propels it into the coils of heat exchanger 14 disposed :~
within the evaporation zone 16. In the heat exchanger 14, the
96 vapor condenses, giving up its heat of condensation to the
86 boiling water. The liquid refrigerant next passes through
pump 26, conduit 22, and back into the heat exchanger 10. Float
valve 25 con~rols the flow of refrigerant 50 that a given liquid
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1 refrigerant level is maintained within the heat exchanger. Pump
26 ma~ be activated -to assist the reErige.rclnt flow i~ required.
The water pump 9 forces 80 water from the thermal sink through
the pipe array 12 and as heat is transerred from the water to
the liquid refrigerant, i.t vaporizes and is recycled via conduit
20.
An indication of the energy efficiency of the foregoing
refrigeration cycle can be s.een from Fig. 3 t a graph of latent
heat versus temperature and pressure, which illustrate.s the
changes of state, pressure, and temperatu:re of re~rigerant 11
undergoing the cycle described above. Thus, within heat exchanger
14, 96 refrigerant vapor at point 60, at a pressure o~ 21.97
psi, condenses (65) and gives up its heat of condensation (76.40
BTU~lb~ to the boiling salt water in evaporation zone 16. The
now liquid refrigerant contains 27.43 BTU/lb., and after it
passes into heat exchanger 10, undergoes adiabatic evaporation .
I (62) resulting in 70 liquid containing 22.02 BTU/lb., 5.71
:; BTU/lb. being contained within a small amount of vapor produced
on evaporation. Next, the remaining liquid is vaporized t63~ in ~ -
X0 heat exchange~ 10, taking its heat o~ vapoxi~ation (73.30 BTU/Ib~
from the coils 12. The vapor is now compressed and thereby
heated (64~ by compressor 18 and the c~cle is repeated.
Thus it can be seen that the refrigerant gives up 76.40
BTU of heat to the salt water in evaporation ~one 16 ~or an energy ~:
cost of only 3.10 BTU, that is, the energy required to heat
(compxess) the refrigerant from 70 to 96 (from 13.40 to 21.97.
`~ p.s.i.). The ratio of the energy given to the boiling salt water . :
to the energy consumed by the compressor will hereinafter be :
referred: to as the coefficient of performance. In the situation `~
outlined above, the coefficient of pérformance will thus be
76.~0/3.1a or 2~.6~.
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1 Those skilled in the art will appreciate that the fore-
going calculations are idealized, and that in actual operation
there are mechanical and entropy losses which will lower the
coefficient of performance. It should also be noted that a 10
temperature dif~erence between the refrigerant and ~he thermal
sink and boiling salt water was assumed to be required in the fore-
going cycle for purposes of illustration. In fact, the foregoing
cycle can operate with significantly smaller temperature differ
entials if more efficient or larger heat exchangers are employed.
For purposes of further illustration, it ~ill now be
assumed that the dew point falls rom the 76 level as in the
foregoing cycle to 64. In this situation, the pressure in
evaporation æone 16 is decreased so that the boiling point of the
salt water can be lowered to 74, and the coefficient of perfor-
ma~ce is dramatioally increased. Fig. 3 illustrates the cycle
now in operation.
Thus, within heat exchanger 14, 84 refrigerant vapor
at point 70r at a pressure of 17.60 psi, condenses (75~ and gives
up its heat of condensation (77.48 BTU/lb.) to the boiling salt
water in evaporation zone 16. After the now liquid re~rigerant
passes into heat exchanger 10 (with the assistance of pump 26~ it
undergoes adiabatic evaporation (72~ resulting in 70~ liquid.
Next, the liquid is vaporized (63) in heat exchanger 10, taking
its heat of vaporization from the coils 12. The vapor is next
compressed and thereby,heated (74~, and the cycle is repeated.
This cycle gives up 77.48 BTU of heat to the salt water
... . .
and the compressor consumes only 1 r 68 BTU. Accordlngl~, the
coef~icient of performance is now 77~48/1.68 or 46.11.
Further increases in the coefficient of perEormance are
easily possible if, as sug~ested above, heat exchangers 10 and 14
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1 can be opera-ted at a smaller tempera-ture difEerential. Also,
further decreases in the de~ point or an increase in temperature
of the thermal sink can increase the eEficiency of the apparatus.
Thus, in a situation where the -thermal sink is warmer than the
boiling salt water, it is contemplated that the temperature
differential across the compressor can approach zero. The co-
efficient of performance will accordingly greatly increase as the
denominator of the heat of condensation/heat of compression
ratio is further lowered.
Thus, as the dewpoint falls below 64, the boiling
point of the salt water in evaporation zone 16 is further lowered
and the corresponding lower temperature difference across the
compressor enables more efficient performance. However, at some
point, the pressure differential across the compressor 18 becomes
so small that the compressor may surge, entrain liquid refrig-
erant with vapor refrigerant, and possibly suffer from lubrication
problems. To overcome this problem, the amount of air forced
through the evaporative cooling apparatus 42 by fan 47 is
decreased, and the temperature within the coils 43 is thereby
increased. If the pressure in evaporative zone 16 is now allowed
to increase, the boiling point of the salt water also increases.
This procedure allows the apparatus to be tuned so that the com-
pressor can function at its optimum pressure differential and -
the greatest possible coefficient of performance that is con-
sistent with the mechanical capabilities of the compressor can
be achievea.
In accordance with another aspect of the invention, as
the temperature difEerential between the thermal sink and the
dew point continues to increase, for example, if the dew point
falls to 50, further dramatic increases in energy efficiency
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1 become possible Thus, when the dew point is 50, the boiling
point of the salt water can be lowered to 60, and since the
thermal sink is at a temperature of 80, it can be appreciaked
that the reErigeration cycle need not be employed.
In this situation, switch 31 opens ~alve 33 to conduit
28 and opens valve 32; the compressor 18 i9 shut down; and the
thermal cycle comes into operation. Accordingly, 80 refrigerant
vapor migrates through conduit 30 and valve 32 to the coils of
heat exchanger 14, where it condenses, giv:ing up its heat of
condensation to the 60 boiling salt water. As the refrigerant
continues to condense, liquid refrigerant builds up in heat
e~changer 14 However, pump 26 moves the liquid refrigerant
through the valve 33 and conduit 28 back into the relatively hot
heat exchanger 10, where it again vaporizes and is rec~cled. As
will be appreciated, this cycle is capable of moving extremely ~-
large quantities of heat at very lo~ energ~ costs, since the
only energy required is that used o drive the pump 26O
In view of the foregoing, it can be seen that the
system may be adapted to suit the particular requirements of the
environment in which the process of the invention is practiced,
and can easily be controlled to responcl to seasonal or daily
fluctuations in ambient conditions. Thus~ for a system utilizing
a thermal sink of a substantially constant ~emperature, the higher
the dew point, the less efficient the system becomes, that is,
the greater energy required per pound of fresh water produced and
the lower is the coefficient of performance. As the dew point
falls, the pressure in the evaporation æone 16 is decreased so
that the boiling point of the water is lowered. This either
decreas~s the size of the temperature differential between the
boiling water and the thermal sink, thereby increasing the
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1 coefficient of performance, or lo~ers the boiling temperature
below that of the thermal sink so that the ef~icient thermal
cycle can take over. On a humid day, the temperature of the
evaporative cooling apparatus will necessarily rise. The boiling
point must therefore also rise, generally to at least about lO
degrees higher so that condensation continues with good heat
exchange. The more the boiling temperature exceeds the tempera-
ture of the thermal sink, the lower will be the coeEficient of
performance, i..e., the greater will be the energy required to
pump the heat from the relatively cooler thermal sink. The rate
at which fresh water is produced depends on the size of the
overall apparatus and on the efficiency (size) of the heat ~;
exchangers employed.
In situations where the temperature of the thermal sink
fluctuates, e.g., where the sink comprises the air at ambient
temperature or a sand mass exposed to the sun, it will be appre-
ciated that even at constant de~oint the coe~ficient of perform-
ance will increase and decrease and~or the system ~ill switch
from the refrigeration cycle mode to the thermal cycle mode as
required by variations in the temperatuXe differential. It should
also be noted that in situations where a substantially constant
temperature thermal sink is available and where a constant cool
temperature is maintainable, e.g., where the dewpoint does not
fluctùate dramatically, or where constant temperature cooling
water is available, the foregoing apparatus need not employ both
a refrigeration cycle and a thermal cycle, as~ depending on the
temperature differential involved, only one of the t~o types of
heat pumps is necessary.
Fig. 2 illustrates a second embodiment of the apparatus ~;
o~ the invention which differs from the embodiment of Fig. l in
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1 that the thermal cycle for transferring heat to the evaporation
zone is omitted and a second refrigeration cycle is employed to
remove the heat of condensation from a condensation zone 66 to
the evapora-tive cooling apparatus 42. The additional refrigera-
tion cycle comprises a compressor 68 interposed between heat
exchanger 72 which is disposed within the condensation zone 66,
and evaporative cooling apparatus 42.
As an example of the operation of thls system, it will
be assumed that the dewpoint is 75 and that water is being
1 a condensed at 65 within condensation zone 66. In this situation,
liquid refrigerant vaporizes within heat exchanger 72 as fresh
water condenses, the heat of condensation of the water being
absorbed as heat of vaporization o~ the refrigerant. The vapor
then exits the heat exchanger via conduit 74, is compressed by
compressor 68 such that its temperature is increased to, ~or
example, 85, and is transported into evaporative cooling
apparatus 42. There, the relatively hot vapor condenses on the
75 coils, its heat of condensation being dissipated by evapor- ~
ative cooling~ Next the liquid refxigerant passes through conduit ~ ;
77 and float valve 80, and enters heat exchanger 72 where it is
again vaporized.
Aside from the foregoing refrigeration cycle, the
apparatus of Fig. 2 operates in a manner identical to that o~ the
refrigeration cycle mode of the apparatus of Fig. 1. The
apparatus of Fig. 2 has advantages in that the boiling and the
condensation temperature of the water can be adjusted by varying
the vacuum within the evaporation and condensation zones. This
allows the respective refrigeration cycles to be tuned in response
to variations in the temperature o~ the thermal sink and/or
variations in th~ dew point in a manner such that the minimum
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1 total energ~ is employed per pound of wa-ter produced in response
to changes in the overall temperature differential between the
thermal sink and the dew point. Also, this embodiment i.s
aclvantageously employed in areas where a sizeable temperature
differential is difficult -to produce. This embodiment is less
desirable than the embodiment of Fig. 1 in that one extra heat
exchange is required.
Fig. 4 illustrates another embodiment of the invention
wherein a thermal cycle 90 is interpose~ between the thermal sink
13 and evaporation zone 16 and a refrigeration cycle 91 is employed
to extract heat from the condensation zone 66 and to dissipate
the heat within evaporative cooling apparatus 42. This embodiment
may be advantageously employed where, for example, a constant,
relatively high tem~erature thermal sink is available and the
dew point undergoes wide fluctuations. In this and other arrange-
ments wherein a thermal cycle is used alone on one side of the
apparatus, an ammonia refrigerant may be used in place of the
- frequently employed halocarbon type, since ammonia has a high
latent heat. Accordingly, the amount of refrigerant which must
2Q be pumped per BTU of heat given to the evaporation zonel and thus
the energy requirements of the system, are correspondingly
reduced.
Still another embodiment of the invention is illustrated ;
in Figure 5. In this embodiment, both the evaporation zone 16
and condensation zone 66 are serviced by thermal cycles 90a, 90b.
Where a substantially constant temperature thermal sink and a ~`
~- substantially constant low temperature sink 92 are available, it
is possible that the temperature differential may be great enough
to employ this embodiment~ and fresh water can be produced at ~ -
extraordinarily low eneryy costs.
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1 Fig. 6 illustra-tes another embodiment of the invention
wherein a refri~eration cycle provides heat of vaporization and
a thermal cycle dissipates heat of condensation. This embodiment
is suitable, for example r iIl the ocean where the refrigeration
cycle can extract heat from relatively warm surface water layers,
and heat of condensation can be dissipatad via the thermal cycle
in-to deeper cold wa-ter layers~
Those skilled in the art ~ill appreciate that many
modifications will be possible in the foregoing apparatus and
process without departing from the scope of the invention. For
example, the location and nature of the vacuum producing means
and the type of heat exchangers selected form no part o~ the
instant invention. Also, it will be apparent that even though
the invention has been described as featuring a heat pump for
moving heat from the thermal sink, it is possible to transfer
- heat di~ectly into the evaporation zone by means of a heat
exchanger through which hot water flows if a suitable ~ource
of hot water is available. ~rom the foregoing it will also be
apparent that various systems using thermal cycles, refrigeration
cycles 9 and combinations thereof to either supply heat to the
evaporation zone or to remove heat from the condensation zone
are within the scope of the inventionO Furthermore, it will be
a matter of mechanical skill to provide controls for the apparatus
of the invention to enable it to operate automatically, changing
; to alternate modes of operation and/or adjusting the v~cuum in
the evaporation zone in response to dewpoint or temperature changes.
It will also be possible to adapt the process and apparatus of
the invention to desalinize salt water in batches or continuously. ~ `
Accordingly, other embodiments are within the following claims.
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