[0001] This invention relates to the generation of energy by means of a working fluid, and
to the regeneration of a working fluid. More particularly, this invention relates
to a method of and to apparatus for generating energy by means of a working fluid
and for regenerating such a working fluid.
[0002] In the generation of energy by expansion of a working fluid, the energy which can
be produced by expansion of the working fluid is limited by the temperatures at which
heating and cooling mediums can economically be provided for regeneration of the working
fluid. The result is, therefore, that such a working fluid is expanded from a high
pressure charged level to a low pressure spent level, with the high pressure charged
level being governed by the maximum pressure at which the working fluid can be evaporated
with the available heating medium, and with the spent low pressure level being governed
by the minimum pressure at which the working fluid can be condensed with the available
cooling medium.
[0003] In practice, therefore, expansion of the working fluid is controlled to provide a
spent low pressure level at which the condensation temperature of the working fluid
is greater than the temperature of the cooling medium, to permit condensation of the
working fluid.
[0004] In addition, in practice, regeneration is based on condensation of working fluid
in a condenser wherein the working fluid is arranged to flow in heat exchange relationship
with an available cooling medium. Because of the desire to achieve maximum expansion
of the working fluid, regeneration of working fluid is often effected where the temperature
difference between the condensation temperature of the spent working fluid at the
spent level and the temperature of the available cooling medium is marginal-often
as low as 1°C. This of necessity imposes a requirement for a large condenser with
an extensive heat exchange surface, and for a large supply of cooling medium, thereby
substantially adding to the operating costs.
[0005] This is particularly significant where severe restraints are imposed by the temperatures
of available heating and cooling mediums as in the case of ocean thermal energy conversion
systems.
[0006] In accordance with one aspect of the invention, there is provided a method of generating
energy, which comprises expanding a gaseous working fluid from a charged high pressure
level to a spent low pressure level to release energy, and regenerating the spent
working fluid by, in at least one regeneration stage:
(a) condensing the working fluid in an absorption stage by dissolving it in a solvent
solution while cooling with a cooling medium, the solvent solution comprising a solvent
having an initial working fluid concentration which is sufficient to provide a solvent
solution boiling range suitable for absorption of the working fluid;
(b) increasing the pressure of the solvent solution containing the dissolved working
fluid and evaporating the working fluid being regenerated by heating in an evaporation
stage;
(c) withdrawing the evaporated working fluid for re-expansion to release energy; and
(d) recycling the balance of the solvent solution remaining after evaporation of the
working fluid, to constitute the solvent solution for the absorption stage of that
regeneration stage.
[0007] In accordance with a further aspect of the invention there is provided a method of
optimizing, within limits imposed by available sources of cooling and heating mediums,
the energy supply capability of a gaseous working fluid which is expanded from a charged
high pressure level to a spent low pressure level to provide available energy, the
method comprising expanding the gaseous working fluid to a spent low pressure level,
and regenerating the spent working fluid by, in at least one regeneration stage:
(a) condensing the working fluid being regenerated in an absorption stage by dissolving
it in a solvent solution while cooling with the cooling medium, the solvent solution
comprising a solvent having an initial working fluid concentration which is sufficient
to provide a solvent solution boiling range suitable for absorption of the working
fluid;
(b) increasing the pressure of the solvent solution containing the dissolved working
fluid, and evaporating the working fluid being regenerated by heating in an evaporation
stage with the available heating medium;
(c) withdrawing the evaporated working fluid to constitute a charged working fluid;
and
(d) recycling the balance of the solvent solution remaining after evaporation of the
working fluid being regenerated, to constitute the solvent solution for the absorption
stage of that regeneration stage.
[0008] In an embodiment of the invention the spent working fluid may be regenerated in a
plurality of successive regeneration stages by increasing the pressure in each stage
until the working fluid has been regenerated to its charged state in the final regeneration
stage.
[0009] The spent working fluid may thus be regenerated by feeding it to a first regeneration
stage, feeding the evaporated working fluid from each regeneration stage to a succeeding
regeneration stage for further regeneration, and recycling within each regeneration
stage the solvent solution remaining after evaporation of the working fluid in the
evaporation stage of that regeneration stage for the recycled solvent solution to
constitute the solvent the solvent solution for the absorption stage of that regeneration
stage.
[0010] The working fluid may be expanded to a spent low pressure level where the condensation
temperature of the gaseous working fluid is below the minimum temperature of the cooling
medium in the absorption stage.
[0011] Further in accordance with the invention, there is provided a method of optimizing,
within limits imposed by available sources of cooling and heating mediums, the energy
supply capability of a gaseous working fluid which is expanded from a charged high
pressure level to a spent low pressure level to provide available energy, the method
comprising expanding the gaseous working fluid to a spent low pressure level, and
regenerating the spent working fluid by, in a plurality of successive regeneration
stages, condensing the working fluid and then evaporating the working fluid at an
increased pressure, the working fluid being condensed in each regeneration stage by
absorbing or dissolving it in a solvent solution while cooling with the cooling medium,
the solvent solution comprising a solvent having, in each stage, an initial working
fluid concentration which is sufficient to provide a solvent solution boiling range
suitable for absorption of the working fluid, and the working fluid being evaporated
in each stage by increasing the pressure to a level where the working fluid being
regenerated can be evaporated with the available heating medium, and then evaporating
the working fluid.
[0012] The invention further extends to apparatus for generating energy, the apparatus comprising
expansion means for expanding a gaseous working fluid from a charged high pressure
level to a spent low pressure level to release energy, and a plurality of successive
regeneration stages for regenerating such a spent working fluid, each regeneration
stage comprising:
(a) an absorber for receiving both a spent working fluid and a solvent solution for
dissolving or absorbing the spent working fluid, the absorber having cirulation means
for circulating a cooling medium through it to cool it;
(b) a pump for pumping a resultant solvent solution from the absorber to increase
its pressure;
(c) an evaporator for receiving a resultant solvent solution from the pump, the evaporator
having circulation means for circulating a heating medium through it to heat it to
evaporate such a working fluid to be regenerated;
(d) a separator for separating such an evaporated working fluid being regenerated,
from such a solvent solution;
(e) feed means to feed such an evaporated working fluid to the absorber of a succeeding
regeneration stage;
(f) recycle means for recycling a solvent solution from the separator to the condenser;
[0013] and a feed conduit for feeding a regenerated working fluid from the separator of
a final regeneration stage to the expansion means.
[0014] Since the solvent solution in each regeneration stage is recycled, the solvent solution
constitutes a closed loop in that stage, and is separate from the solvent solution
in each other regeneration stage. Furthermore, in each regeneration stage, the quantity
of working fluid being regenerated is dissolved in the solvent solution of that stage,
and the equivalent quantity of working fluid being regenerated is evaporated from
the solvent solution in the evaporation stage of each regeneration stage.
[0015] It will be appreciated that the quantity of solvent solution, and the initial concentration
of working fluid in the solvent solution in each regeneration stage will be separately
adjusted as may be required for specific operating conditions, and as may be required
for variations in the minimum temperature level of an available cooling medium.
[0016] The solvent of the solvent solution may be any suitable solvent which is a solvent
for the working fluid, which has a boiling point above the maximum temperature which
will be attained in any evaporation stage, and which will provide a solvent solution
when working fluid is dissolved therein, which has a boiling point which decreases
as the concentration of working fluid increases.
[0017] While the solvent solution is preferably a binary solution, it will be appreciated
that it may be a solution of a plurality of liquids.
[0018] A number of working fluids which would be suitable, are known to those skilled in
the art. Any of such working fluids may be employed in this invention.
[0019] In one embodiment of the invention, the working fluid and solvent may be in the form
of hydrocarbons having appropr.iate boiling points. Thus, for example, the solvent
may be in the form of butane or pentane while the working fluid may be in the form
of propane. In an alternative example, the working fluid may be an appropriate freon
compound, with the solvent being an appropriate solvent for that compound.
[0020] In a preferred embodiment of the invention, the working fluid is in the form of ammonia
and the solvent is in the form of water. In this embodiment of the invention, at a
pressure of one atmosphere the boiling point of water is 100°C whereas the boiling
point of pure ammonia is -33°C. As the concentration of ammonia in water increases,
the boiling point of the aqueous ammonia solution will decrease. From binary phase
diagrams of water and ammonia solutions, the appropriate initial concentration of
ammonia in the solvent solution for each regeneration stage, can readily be determined
for this invention from the pressure and temperature which will prevail in each condensation
stage.
[0021] In a preferred embodiment of the invention, the initial concentration of working
fluid in the solvent solution in each regeneration stage, and the proportion of solvent
solution to working fluid to be regenerated will be selected so that after complete
absorption of the working fluid being regenerated in the absorption stage of that
regeneration stage, the solvent solution will have a boiling point marginally above
the minimum temperature attained in that absorption stage during use.
[0022] In practice, therefore, the minimum quantity of solvent solution will be employed
which will satisfy this requirement thereby reducing cooling medium requirements to
the minimum, and thereby further reducing heating medium requirements to the minimum.
[0023] It will be appreciated that since the pressure is increased between the absorption
stage and evaporation stage of each regeneration stage, there will be a step-wise
or incremental increase in pressure between each preceeding regeneration stage and
each succeeding regeneration stage. It follows, therefore, that the initial concentration
of working fluid in the solvent solution for each successive regeneration stage will
be correspondingly higher to provide a boiling range for the solvent solution in each
stage which is suitable for dissolving or absorbing the working fluid at the pressure
prevailing in that stage.
[0024] In a preferred embodiment of the invention, the pressure is increased between the
absorption and evaporation stages of each regeneration stage, to the maximum pressure
at which the working fluid being regenerated can be evaporated effectively in the
evaporation stage by the, or by a heating medium, available for heating the evaporation
stage.
[0025] The pressure is, therefore, preferably increased in each regeneration stage to the
maximum level where the solvent solution in each evaporation stage will, after evaporation
of the working fluid in that stage, have a boiling point marginally below the maximum
temperature attainable in that evaporation stage.
[0026] By appropriate control of the pressure, evaporation of the required quantity of working
fluid being regenerated can be readily effected in each evaporation stage. Control
valve means may, however, be provided to control the quantity of evaporated working
fluid which is fed from each regeneration stage to each succeeding regeneration stage.
Thus, if a greater quantity of working fluid than that required for regeneration has
been evaporated in an evaporator stage, only the required quantity will pass to the
succeeding regeneration stage. The balance will be recycled with the solvent solution.
[0027] The method of this invention may preferably include the step of, in each regeneration
stage, feeding the solvent solution and evaporated working fluid from the evaporation
stage to a separation stage for separating the working fluid being regenerated.
[0028] The separator stage may be provided by a separator of any conventional suitable type
known to those skilled in the art.
[0029] The solvent solution which is recycled to the absorption stage in each regeneration
stage, is conveniently expanded to reduce its pressure to a pressure corresponding
with or approaching that of the pressure of the working fluid being regenerated in
that absorption stage.
[0030] In a preferred embodiment of the invention, in each regeneration stage, the solvent
solution which is recycled, is recycled in heat exchange relationship with the evaporation
stage to thereby reduce the heating medium requirements for the evaporation stage.
[0031] The solvent solution which is recycled in each regeneration stage, may be recycled
at least partially in heat exchange relationship with the absorption stage.
[0032] Where the recycled solvent solution is recycled in heat exchange relationship with
an absorption stage, the cooling medium requirement will decrease because the quantity
of heat to be removed will remain constant, but the capacity of the absorption stage
will have to be increased. Conversely, if the recycled solvent solution is not recycled
in heat exchange relationship with the absorption stage, the capacity of the absorption
stage will decrease while the requirement of cooling medium will increase.
[0033] In practice, therefore, depending upon the source and availability of the cooling
medium, on the basis of economic considerations, the reduced cost of supplying lesser
quantities of cooling medium can be balanced against the capital costs of increasing
the capacity of the absorption stages to determine whether the recycled solvent solution
should be recycled in heat exchange relationship, or at least partially in heat exchange
relationship with the absorption stages, or not at all.
[0034] In an embodiment of the invention, all of the absorption stages of the regeneration
stages may be carried out separately in a single composite absorption stage which
is cooled by means of cooling medium from a common source. Furthermore, all of the
evaporation stages may be carried out separately in a single composite evaporation
stage which is heated by means of a heating medium from a common source.
[0035] The apparatus of this invention may, therefore, include a single composite absorption
unit and a single composite evaporation unit, with all the absorbers of the various
regeneration stages being incorporated in the absorption unit, and all the evaporators
of the various regeneration stages being incorporated in the evaporated unit.
[0036] While this invention may have various applications, and while various types of cooling
and heating means known to those skilled in the art, may be employed, this invention
can have particular application in regard to the utilization of readily and economically
available cooling and heating mediums for the generation of energy.
[0037] The invention can, therefore, have specific application where low temperature differential
heating and cooling mediums are employed.
[0038] A preferred application of the invention would, therefore, be in the field of thermal
energy conversion using cool water withdrawn from a body of water as the cooling medium,
and using, as heating medium, hot water from a body of water, water heated by solar
heating, hot water heated additionally by solar heating means, or water or heating
fluid in the form of waste heat fluids from industrial plants.
[0039] A preferred application of the invention would, therefore, be in the field of ocean
thermal energy conversion [OTEC] where ocean surface water is used as the heating
medium and ocean water withdrawn from a sufficient depth from an ocean is used as
the cooling medium, thereby resulting in a low temperature differential between the
heating and cooling mediums.
[0040] Normally, ocean water would be withdrawn from a depth of about 200 feet to provide
the most economical cooling medium at the lowest temperature. The temperature does
not tend to decrease significantly beyond a depth of about 200 feet.
[0041] A further preferred application of the invention would be in regard to solar ponds
for supplying the heating medium, and also the cooling medium if desired.
[0042] The invention further extends to a method of increasing the pressure of a gaseous
working fluid from an initial low pressure level to a high pressure level utilizing
an available heating medium and utilizing an available cooling medium, which comprises
incrementally increasing the pressure of the working fluid by, in a plurality of successive
incremental regeneration stages:
(a) absorbing the working fluid being regenerated in an absorption stage by dissolving
it in a solvent solution while cooling with such an available cooling medium; the
solvent solution comprising a solvent having an initial working fluid concentration
which is sufficient to provide a solvent solution boiling range suitable for absorption
of the working fluid;
(b) increasing the pressure of the solvent solution containing the dissolved working
fluid, and evaporating the working fluid being regenerated in an evaporation stage
by heating with such an available heating medium;
(c) feeding the evaporated working fluid which is at an increased pressure level,
to a succeeding regeneration stage for absorption;
(d) recycling the balance of the solvent solution remaining after evaporation of the
working fluid being regenerated, to constitute the solvent solution for the absorption
stage of that regeneration stage; and
(e) withdrawing regenerated working fluid from a final regeneration stage.
[0043] The expansion of the working fluid from a charged high pressure level to a spent
low pressure level to release energy may be effected by any suitable conventional
means known to those skilled in the art, and the energy so released may be stored
or utilized in accordance with any of a number of conventional methods known to those
skilled in the art.
[0044] In a preferred embodiment of the invention, the working fluid may be expanded to
drive a turbine of conventional type.
[0045] In an embodiment of the invention, where the mass ratio between the solvent solution
being recycled through an absorption stage and the working fluid being regenerated
is sufficient, the pressure of the solvent solution leaving the evaporation stage
may be utilized to increase the pressure of the working fluid being regenerated which
is introduced into the absorption stage with the recycled solvent solution.
[0046] In this embodiment of the invention, instead of expanding the solvent solution which
is recycled to reduce its pressure to a pressure corresponding with or approaching
that of the pressure of the working fluid being regenerated in an absorption stage,
the solvent solution may be injected into the absorption stage in such a manner as
to entrain the working fluid and draw the working fluid into the absorption stage.
[0047] Various injection systems are known to those skilled in the art which could be used
for this purpose. As an example, an injection system such as an injection nozzle having
a restricted zone to create a zone of low pressure may be used. With such an injection
nozzle, the working fluid will be introduced into the proximity of the restricted
zone so that the reduced pressure created will permit the working fluid to be introduced
into the absorption stage.
[0048] It will be appreciated that, depending upon relative flow rates and pressures, it
may still be necessary to control the pressure of the recycled solvent solution by
expanding it to provide an appropriate pressure.
[0049] By utilizing the pressure, or at least part of the pressure, of the solvent solution
which is recycled, this will contribute to an increase in pressure in the absorption
stage. This can provide the advantage of improving absorption in the absorption stage,
or can be utilized to permit expansion of the working fluid to an even lower spent
level. In this event, the initial increase in pressure provided by the solvent solution
may be utilized to increase the pressure in the absorption stage, to a level where
absorption can be effectively achieved in accordance with this invention.
[0050] Applicant believes that this application of the pressure of the solvent solution
will tend to be valuable in the first stage, and probably the first and second stages
of a multi-stage regeneration system while, in a single stage system or a system employing
only two stages it will tend to be less valuable. This will primarily be due to the
fact that the mass ratio between the recycled solvent solution and the working fluid
will not be sufficient.
[0051] Preferred embodiments of the invention are now described by way of example with reference
to the accompany drawings.
[0052] In the drawings: -
Figure 1 shows a schematic representation of one embodiment of the method and apparatus
of this invention;
Figure 2 shows a fragmentary schematic representation of the method and apparatus
of Figure 1 incorporating a modification to the expansion stage;
Figure 3 shows a fragmentary schematic representation of a further embodiment of the
invention in which injection means is utilized to inject the working fluid being regenerated;
Figure 4 shows a schematic representation of a further embodiment of the method and
apparatus of this invention.
[0053] With reference to Figure 1 of the drawings, numeral 50 refers generally to apparatus
for use in generating energy by the expansion of a gaseous working fluid from a charged
high pressure level to a spent low pressure level to release energy, and for regenerating
the spent working fluid.
[0054] The apparatus 50 includes expansion means in the form of a turbine 52 in which a
gaseous working fluid is expanded from a charged high pressure level to a spent low
pressure level to released energy to drive the turbine 52. The gaseous working fluid
at the high pressure level is fed to the turbine 52 along charged line 54 and is discharged
from the turbine 52 along spent line 56.
[0055] The apparatus 50 further includes regeneration means for regenerating the spent gaseous
fluid. The regeneration means comprises four successive incremental regeneration stages.
[0056] For ease of reference the components of each regeneration stage have been identified
by a letter followed by a suffix in arabic numerals indicating the particular regeneration
stage. In addition, the flow lines for each regeneration stage have been identified
by reference numerals having a prefix corresponding to that of the particular regeneration
stage.
[0057] The first regeneration stage comprises an absorber A1 for condensing the gaseous
working fluid by dissolving it in a solvent solution, a pump P1 for pumping the solvent
solution containing the dissolved working fluid to increase the pressure, evaporator
E1 for evaporating the working fluid, and a separator S1 for separating the evaporated
working fluid from the solvent solution.
[0058] The first regeneration stage includes an influent line 1-1 into which the spent gaseous
working fluid from the spent line 56 and solvent solution from a solvent solution
recycle line 1-13 are fed into the first stage and through the absorber A1.
[0059] The resultant solvent solution from the absorber A1 is fed along line 1-2 to the
inlet of the pump P1. The solution is discharged from the pump P1 at an increased
pressure along line 1-3 and through the evaporator El. The solvent solution and evaporated
working fluid are fed from the evaporator E1 along line 1-4 to the separator S1. The
separated evaporated working fluid is fed from the separator S1 along line 1-5 to
the influent line 2-1 of the second stage. The solvent solution from the separator
S1 is recycled along solvent solution recycle line 1-13 to the influent line 1-1.
[0060] The second, third and fourth regeneration stages correspond exactly with the first
regeneration stage except that the evaporated, separated working fluid from the separator
S4 is withdrawn along line 4-5 and fed into the charged line 54 to repeat the cycle.
[0061] In the preferred embodiment of the invention, the gaseous working fluid is ammonia,
whereas the solvent is water. In addition, in the preferred embodiment of the invention,
the apparatus 50 is an apparatus for use in producing energy by ocean thermal energy
conversion.
[0062] The apparatus 50 is, therefore, conveniently installed on the seashore or on a floating
platform. In addition, the apparatus 50 includes pump means [not shown] for pumping
surface water from the surface of an ocean to the evaporators of the apparatus to
constitute the heating medium for the apparatus, and includes pump means [not shown]
for pumping cold water from a sufficient depth of such an ocean for constituting the
cooling medium for cooling the absorbers of the apparatus 50.
[0063] Thus, the absorber A1 includes circulation means having an inlet 1-9 and an outlet
1-10 for circulating deep ocean water through the absorber A1. Similarly, the evaporator
E1 includes an inlet 1-11 and an outlet 1-12 for circulating ocean surface water through
the evaporator for heating the evaporator El.
[0064] Further, in each regeneration stage, the recycle line 1-13, 2-13, 3-13 and 4-13 has
an evaporator heat exchange line 1-15, 2-15, 3-15 and 4-15, respectively, passing
in heat exchange relationship through the evaporator E.
[0065] In addition, in each of the regeneration stages, the solvent solution recycle line
-13 may have a condenser heat exchange line 1-16, 2-16, 3-16 and 4-16, respectively,
extending in heat exchange relationship through the absorber A or, alternatively,
may completely bypass the absorber A as indicated by chain-dotted lines 1-18, 2-18,
3-18 and 4-18.
[0066] Where the recycled solvent solution passes in heat exchange relationship through
the absorber of each-regeneration stage, it will assist in cooling the absorber and
will thus reduce the quantity of cooling water required to effect the required cooling
in that absorber since the quantity of heat to be transferred will remain constant.
It will, however, necessitate an increase in the absorber capacity and thus, in the
absorber size.
[0067] In practice, therefore, the capital cost of an increase in absorber size can be balanced
against the cost of the additional quantity of cooling medium to decide, on the basis
of pure economics, as to whether the recycle line should pass through the absorbers,
should completely bypass the absorbers, or should pass partially through the absorbers.
[0068] In the preferred embodiment of the invention, the recycle lines will bypass the absorbers.
[0069] In the preferred embodiment of the invention, the gaseous working fluid is ammonia,
whereas the solvent solution is a solution of ammonia in water.
[0070] The use of the apparatus 50, and thus the process of this invention, is now described
with reference to a preferred ocean thermal energy conversion system typically employing,
as heating medium, surface water at a temperature of 27°C, and employing as cooling
medium, deep ocean water [typically at a depth of not less than about 200 feet] having
a temperature of about 4°C.
[0071] Since the boiling point of pure ammonia is -33°C at a pressure of one atmosphere,
and since the minimum temperature of the cold water cooling medium is 4°C, it would
normally not be possible to regenerate ammonia at a pressure of one atmosphere by
using such a cooling medium. In other words, regeneration would only be possible if
the ammonia working fluid were at a pressure where the boiling point of ammonia is
above 4°C.
[0072] In other words, regeneration of the gaseous working fluid would only be possible
if the working fluid is expanded across the turbine 52 to a pressure at which it is
capable of regeneration with the available cooling medium. This imposes a direct and
severe limitation on the energy which can be generated since the maximum pressure
to which the ammonia working fluid can be regenerated is also limited by the evaporation
capacity of the hot water heating medium at 27°C.
[0073] In practice, utilizing surface water at a temperature of about 27°C, evaporation
of ammonia in the final evaporator E4 can only be achieved in an effective manner
at a maximum pressure of about nine atmospheres.
[0074] It will be appreciated, therefore, that if the working fluid can be expanded from
a charged level of nine atmospheres to a spent level pressure of one atmosphere, as
opposed to a spent level pressure of say only four atmospheres, the quantity of energy
released will be increased substantially.
[0075] In the preferred process as illustrated in Figure 1, the gaseous ammonia working
fluid is indeed allowed to expand across the turbine 52 from a pressure of about nine
atmospheres to a pressure of about one atmosphere.
[0076] A specific quantity of gaseous working fluid to be regenerated, at a spent pressure
level of one atmosphere is, therefore fed to the first stage along influent line 1-1.
[0077] This quantity of gaseous working fluid is condensed in the absorber A1 by dissolving
it in a solvent solution which is fed along solvent solution recycle line 1-13 into
the influent line 1-1 at the same pressure of one atmosphere.
[0078] In the preferred embodiment of the invention, the solvent solutions will not be passed
in heat exchange relationship through the absorbers. Thus, the spent gaseous ammonia,
which may contain about 10% by weight of liquid ammonia, will be at a temperature
of about -33°C, whereas the corresponding solvent solution will be at a temperature
of about 8°C.
[0079] The solvent solution comprises water having an initial ammonia concentration which
is sufficient to provide a binary solution which at the pressure of one atmosphere,
has a boiling point within the temperature range which will prevail in the absorber
A1. Further, the proportion of solvent solution to the quantity of working fluid to
be regenerated is such that after the solvent solution has dissolved the quantity
of working fluid to be regenerated in the absorber A1, the resultant binary solution
will have a concentration which will provide, at the pressure of one atmosphere, a
boiling point marginally above the minimum temperature of the cooling medium. The
boiling point of the solvent solution will thus be in the region of about 6°C where
the minimum temperature of the cold water is about 4°C.
[0080] In this way it will be insured that the total quantity of working fluid to be regenerated
will dissolve in the solvent solution, and that the minimum quantity of solvent solution
to dissolve that quantity of gaseous ammonia will be employed thereby reducing the
cold water requirements and the capacity of the absorber A1 to the practical minimum.
[0081] The solvent solution containing the dissolved working fluid being regenerated, will
leave the absorber A1 at a temperature of about 6°C and at a pressure of one atmosphere,
and is pumped by the pump P1 to the evaporator E1.
[0082] The pump P1 is controlled to increase the pressure of the solvent solution to the
maximum pressure at which the dissolved ammonia working fluid can be effectively evaporated
in the evaporator El by means of the surface water heating medium at a maximum temperature
of 27°C.
[0083] Preferably, the pressure increase is controlled so that after evaporation of the
quantity of working fluid being regenerated, the solvent solution in the evaporator
El will have a boiling point marginally below 27°C, such as about 25°C.
[0084] This pressure can readily be determined from a binary water/ammonia phase diagram
in relation to the prevailing ammonia concentration and temperature range in the evaporator
El.
[0085] It will naturally be appreciated that the initial concentration of ammonia in water
for the solvent solution, as also the required quantity of solvent solution; which
is fed to the absorber Al, can also readily be determined from such a phase diagram
on the basis of the known pressure and temperature range.
[0086] The evaporated working fluid and solvent solution are fed along line 1-4 to the separator
S1, where they are allowed to separate.
[0087] From the separator S1, the solvent solution, at a temperature of about 25°C will
be recycled along the solvent solution recycle line 1-13 to constitute the solvent
solution for the first stage. The separated, evaporated ammonia working fluid at about
25°C is fed from the separator S1 to the second regeneration stage along influent
line 2-1. As in the case of the first regeneration stage, the quantity of working
fluid being regenerated, is mixed with a solvent solution recycled from a separator
S2 of the second regeneration stage along the solvent solution recycle line 2-13 for
dissolving the working fluid in the absorber A2.
[0088] Since the pressure in the absorber A2 will be greater than the pressure in the absorber
A1, it follows that the initial concetration of ammonia in the solvent solution for
the second stage will be correspondingly higher to insure that an appropriate boiling
point is again provided for effectively dissolving or absorbing the working fluid
being regenerated in the absorber A2.
[0089] It will be appreciated that the solvent solution which is recycled from the separator
S to the absorber A in each stage leaves the separator S at a higher pressure than
the pressure of the influent working fluid. Each solvent solution recycle line 1-13,
2-13, 3-13 and 4-13, therefore, includes a pressure-reducing valve V1, V2, V3 and
V4, respectively, for reducing the pressure of the recycled solvent solution to the
same pressure as that of the influent working fluid being regenerated.
[0090] For each successive regeneration stage, therefore, the initial concentration of ammonia
in the solvent solution will increase step-wise in correspondence with the step-wise
increase in pressure provided by the pump means in each stage.
[0091] It will be appreciated that the apparatus will include an appropriate number of regeneration
stages until the quantity of working fluid being regenerated, has been regenerated
to the appropriate charged high pressure level in a final regeneration stage such
as the fourth regeneration stage shown in the drawing. It will further be appreciated
that the spent pressure level to which the working fluid is expanded, will likewise
determine the number of regeneration stages required. Thus if the working fluid is
expanded to only say 3 atmospheres, only two or three regeneration stages may be required.
[0092] In the embodiment illustrated in the drawing, the pump means P4 will increase the
pressure of the solvent solution to about nine atmospheres thereby yielding a charged
regenerated working fluid at a pressure of about nine atmospheres which is withdrawn
from the separator S4 and fed along the charged line 54 to the turbine 52.
[0093] It will be appreciated that in the preferred embodiment of the invention, the process
will be carried out as a continuous process in which a constant quantity of working
fluid by unit time is continuously being expanded across the turbine 52 and is then
continuously being regenerated in the regeneration means.
[0094] To further illustrate the use of the invention in the preferred embodiment as illustrated
in Figure 1, typical parameters of the process are now indicated with reference to
specific theoretical calculations performed on the basis of 1 kilogram of gaseous
ammonia working fluid, and on the basis of deep ocean water at a minimum temperature
of 4°C as cooling medium, and surface ocean water at a maximum temperature of 27°C
as heating medium.
[0095] These parameters as calculated are set out in Tables I, II, III and IV below for
the first, second, third and fourth regeneration stages, respectively.
[0096] In each table, the particular point at which the parameter has been calculated, is
indicated by the appropriate reference numeral in the drawing. These points are listed
in the first column of each table.
[0097] The columns in the tables are as follows:
(a) First column - reference numerals (RN);
(b) Second column - temperature (t) in °C;
(c) Third column - pressure (p) in atmospheres;
(d) Fourth column - ratio by weight of total ammonia (dissolved and undissolved) to
water plus total ammonia (RATIO);
(e) Fifth column - weight (w) in kilograms; and
(f) Sixth column - Enthalpy (E) in kcal/g.
[0098] From the above theoretical calculations, the total heat supplied to the four evaporator
stages amounted to 1258.35 kcals, while the total heat removed from the four absorption
stages amounted to 1200.8 kcals.
[0099] The difference of 57.55 is the work put in per kilogram of working fluid regenerated
and thus the theoretical amount of work which is available.
[0100] The energy required to operate the pumps was calculated to be 2.08 kcals/kg of working
fluid regenerated.
[0101] The theoretical amount of work available is therefore 55.47 kcal/kg of working fluid.
[0102] If it is assumed that the efficiency of the turbine is 85%, the theoretical thermal
efficiency will be 4.408%.
[0103] The theoretical thermal efficiency of an ideal Carnot cycle system operating with
a cooling medium at a constant temperature of 4°C and with a heating medium at a constant
temperature of 27°C, would be 7.04%. However, considering that the temperature of
the heating and cooling mediums must change in such a process, the efficiency of the
theoretical ideal thermodynamical cycle will be only about 4.9%.
[0104] Therefore, the ratio of the efficiency of a system in accordance with this invention
on the basis of the theoretical calculations, would be:
(a) 62.55% in relation to an ideal Carnot cycle system;
(b) about 82% in relation to an ideal thermodynamical cycle under corresponding conditions.
[0105] It is an advantage of the embodiment of the invention as illustrated with reference
to the drawing, that an effective system can be provided for generating energy by
using the relatively low temperature differential between surface ocean water as heating
medium and deep ocean water as cooling medium.
[0106] It is a further advantage of this embodiment that a system can be provided for regeneration
of spent gaseous ammonia at a relatively low level of about one atmosphere or less.
[0107] It is a further advantage of the embodiment of the invention as illustrated, that
because the regeneration range of the gaseous working fluid has been increased, the
gaseous working fluid can be expanded from a high pressure level of about nine atmospheres,
to a low pressure level of about one atmosphere or less. Thus, the quantity of energy
available for release is substantially greater than would be the case if the working
fluid were expanded from a pressure of about nine atmospheres to a pressure of only
about four or five atmospheres.
[0108] The embodiment of the invention as illustrated in the drawing can provide a further
advantage arising from the fact that the cold water requirements need only be sufficient
to provide a final temperature in each absorber of about 6°C. The temperature of the
cold water cooling medium can thus increase across each absorber as indicated in the
above tables. Thus, the cooling medium requirements will be substantially less than
would be the case if it were necessary to supply a sufficient quantity of cooling
water at a sufficient rate to approach the Carnot cycle ideal where the cooling medium
would remain at the constant minimum temperature. The same considerations apply to
the heating medium, where the hot water is allowed to cool from about 27°C to the
temperature indicated in the above tables across each evaporator stage thereby again
providing a substantially reduced heating water requirement over that required by
the ideal Carnot cycle operation.
[0109] It will be appreciated that since, in each absorber, the cooling range for the solvent
solution and working fluid is substantially the same, and the temperature range for
the cooling medium is substantially the same, the absorbers of the four regeneration
stages can conveniently be combined into-a single composite absorber through which
the lines 1-1, 2-1, 3-1 and 4-1 pass separately for cooling by means of a single circulating
supply of cold water. In the same way, all the evaporators can be combined in a single
composite evaporator heated by means of the circulating hot water from a single source.
[0110] It will further be appreciated that, theoretically, the quantity of solvent solution
in each regeneration stage should remain constant, and that the initial concentration
of ammonia in water to constitute the solvent solution, should also remain constant
for constant minimum cooling water temperatures and constant maximum heating water
temperatures.
[0111] In practice, however, the quantity of solvent solution will have to be adjusted during
use to compensate for varying conditions and for losses. In addition, the concentration
of ammonia in water in each regeneration stage, will have to be adjusted periodically
in relation to seasonal variations in the minimum temperature of cold water and maximum
temperature of hot water.
[0112] It will also be appreciated that where heating of the hot water can economically
be achieved, such as by solar heating or the like, the effectiveness of the process
of this invention can be improved. Such supplemental heating will, therefore, be employed
under appropriate conditions if dictated by economic considerations.
[0113] With reference to Figure 2 of the drawings, numeral 150 refers generally to an alternative
embodiment of the method and apparatus of this invention to the embodiment illustrated
in Figure 1.
[0114] The apparatus 150 corresponds substantially with the apparatus 50 and corresponding
parts are indicated by corresponding reference numerals.
[0115] In the apparatus 150, in place of the single turbine 52 of the apparatus 50, a two-stage
turbine system is employed comprising a first turbine 152 and a second turbine 153.
[0116] The charged working fluid is partially expanded across the first turbine 152 into
a heat exchange vessel 170.
[0117] From the heat exchange vessel 170 the partially expanded working fluid is led along
separate conduits 171 and 172 through the absorber A2 and through the absorber A1
respectively in heat exchange relationship with the cooling water.
[0118] Thereafter the partially spent working fluid is further expanded across the second
turbine 153 to its final spent level. It is then fed, as before, along the spent line
56 to the influent line 1-1.
[0119] Applicant believes that by utilizing a two-stage turbine system with heat exchange
of the partially expanded working fluid, the effectiveness of the system can be improved
particularly where the system includes a number of regeneration stages. Applicant
believes that it will tend to be less significant where fewer stages are employed.
[0120] With reference to Figure 3 of the drawings, the drawing shows, to an enlarged scale,
the apparatus of Figure 1 which has been adapted in the first and second regeneration
stages for the pressure of the recycled solvent solution to be utilized in increasing
the pressure of the influent spent working fluid into the absorption stage A1 and
the absorption stage A2 respectively.
[0121] As indicated in Figure 3, the absorption stage A1 incorporates an injection system
for injecting the recycled solvent solution at a pressure substantially higher than
the pressure of the spent working fluid into the absorber A1.
[0122] The injection system is in the form of an injection nozzle 180 having an intermediate
restricted zone to generate a zone of low pressure.
[0123] The spent line 56 joins the nozzle 180 at the restricted zone and, as is known those
skilled in the art, in an attitude where the reduced pressure generated at the restricted
zone by the solvent solution being injected through the nozzle 180 into the absorber
A1, will draw the spent working fluid into the nozzle 180 and thus into the absorber
A1.
[0124] It will be appreciated that the effectiveness of this system will depend upon the
mass ratio between the solvent solution being recycled and the working fluid being
regenerated.
[0125] If the ratio is to low, it will not be possible to introduce the total quantity of
working fluid being regenerated by means of the flow of the solvent solution being
recycled.
[0126] In practice therefore, depending upon conditions, it may be necessary to partially
reduce the pressure of the solvent solution being recycled before entry into the nozzle
180, or it may be necessary to introduce some of the working fluid being regenerated
through the nozzle 180, and the remainder directly into the absorber A1.
[0127] While the absorber A2 has not been illustrated in Figure 3, it will be appreciated
that the working fluid being regenerated in the second regeneration stage will be
introduced into the absorber A2 by means of an injection system corresponding to that
of the absorber A1.
[0128] The embodiment of the invention as illustrated in Figure 3 of the drawings, can provide
the advantage that the pressure of the solvent solution being recycled in the first
and second stages respectively can be at least partially utilized to introduce the
working fluid being regenerated, and to increase the pressure in the first and second
absorbers A1 and A2.
[0129] This affect can be utilized to improve the effectiveness of absorption in the first
and second absorbers A1 and A2. Alternatively, or in addition, this feature can be
utilized to permit expansion of the charged working fluid to a yet lower pressure
across the turbine 52, with reliance being placed on the pressure contribution of
the solvent solution being recycled to raise the pressure in the absorber A1 to a
level where effective absorption of the working fluid being regenerated can be effected.
Similarly, if employed in relation to the second regeneration stage, the same considerations
will apply where the working fluid introduced into the absorber A2 can be at a lower
pressure, and reliance is placed on the pressure of the solvent solution being recycled
into the absorber A2, to increase the pressure to a level for effective absorption
in the absorber A2.
[0130] Applicant believes that the injection system can be advantageous in the apparatus
50 particularly in the first and second stages, but would tend to have lesser value
in subsequent stages.
[0131] With reference to Figure 4 of the drawings, reference numeral 450 refers generally
to yet a further alternative embodiment of the method and apparatus of this invention.
[0132] The system 450 as illustrated in Figure 4, is designed for use where the charged
working fluid is expanded to a relatively higher level than the level described with
reference to Figures 1 to 3, but regeneration of the spent working fluid is effected
in accordance with this invention to provide an economical system with high efficiency.
[0133] The apparatus 450 includes a turbine 452, and absorber A, a pump P, a regenerator
R, an evaporator E and a separator S.
[0134] The spent working fluid expanded across the turbine 452 is fed along spent line 456
to influent line 464. Solvent solution which is recycled from the separator S along
solvent solution recycle line 465 is fed through a pressure reducing valve V to reduce
the pressure of the solvent solution to that of the spent working fluid, and then
into the absorber A through the influent line 464.
[0135] As described with reference to Figure 1, cooling medium in the form of cold deep
ocean water is circulated in heat exchange relationship through the absorber A by
means of conduit 461, while heating surface water is circulated through evaporator
E in heat exchange relationship therewith, along conduit 463.
[0136] The spent working fluid is absorbed by the solvent solution in the absorber A whereafter
the solvent solution containing the absorbed working fluid has its pressure increased
by the pump P.
[0137] The solvent solution containing the absorbed working fluid is fed from the pump P
along line 466 through the regenerator R and then to the evaporator E for evaporation
of the dissolved working fluid being regenerated.
[0138] The solvent solution being recycled along the line 465, is passed in heat exchange
relationship with the solvent solution passed through the regenerator R to -effect
heat exchange.
[0139] From the evaporator E, the evaporated fluid being regenerated and the solvent solution
passes to the separator S for separation, whereafter the separated charged working
fluid is fed along charged line 454 to the turbine 452.
[0140] To illustrate this embodiment of the invention, typical parameters of the process
of the system of Figure 4, are now indicated with reference to specific theoretical
calculations performed on the basis of 1 kilogram of gaseous ammonia working fluid,
and on the basis of deep ocean water at a minimum temperature of 4°C as cooling medium,
and surface ocean water at a maximum temperature of 27°C as heating medium.
[0141] These parameters as calculated are set out in Table V below. The particular point
at which the parameter has been calculated, has been indicated by the appropriate
reference numeral in Figure 4. These points are listed in the first column of Table
V.
[0142] It will be noted from Table V that the working fluid is expanded from a charged level
of 9 atmospheres to a spent level of 5.5 atmospheres. It will further be noted that
the spent working fluid and solvent solution enter the absorber A at a temperature
of 12°C, and that the solvent solution containing the absorbed working fluid being
regenerated, leaves the absorber A at a temperature of about 8°C.
[0143] By using an absorber A for absorbing the spent ammonia working fluid, and by having
an appropriate initial concentration of ammonia in water for the solvent solution
being recycled, absorption of the ammonia working fluid can commence in the absorber
A at a temperature of 12°C or slightly higher, and complete absorption will have occurred
by the time the temperature has been reduced to about 8°C by the cooling medium at
4°C.
[0144] There is therefore a significant temperature difference between the temperature of
the cooling medium and the minimum temperature required for complete absorption of
the working fluid being regenerated.
[0145] In contrast with a system employing a conventional condensation stage for the condensation
of a working fluid such as ammonia, condensation of gaseous ammonia at 5.5 atmospheres
would only commence at a temperature of about 5°C resulting in a marginal difference
of 1°C between the temperature of condensation and the temperature of the available
cooling medium, which is at 4°C.
[0146] Thus, before condensation can occur in a condensation stage, the temperature of the
working fluid would have to be reduced to about 5°C by the cooling medium at 4°C.
It will be appreciated that because of the marginal temperature difference, the requirements
of cooling water will be substantial and a substantial heat transfer surface will
be required.
[0147] In contrast therewith, by utilizing an absorber in accordance with this invention,
while both the working fluid being regenerated and the solvent solution being recycled
will have to be cooled, because absorption of working fluid can commence at a temperature
substantially above the temperature of the cooling medium, and can be completed at
a temperature substantially above the temperature of the cooling medium, the amount
of cooling water required can be reduced substantially and/or the heat transfer surface
requirement can be reduced substantially.
[0148] In practice, on the basis of economics, the cooling water requirements, the heat
transfer surface area, and the temperature difference between the temperature of the
cooling water and the temperature required for complete absorption of the spent working
fluid, can be balanced to achieve the most economical system in the light of the operating
parameters and capital costs.
[0149] Because the solvent solution containing the working fluid being regenerated would
leave the absorber A at a temperature higher than the temperature of a condensed working
fluid leaving a condenser, evaporation in the evaporator E will be facilitated. By
additionally circulating the solvent solution being recycled and the solvent solution
containing the absorbed working fluid in heat exchange relationship through the regenerator
R, both absorption in the absorber A and evaporation in the evaporator E will be improved.
[0150] The system 450 therefore provides the advantage of an increased enthalpy drop across
the turbine 452 and provides a system of increased efficiency and economy.
[0151] To illustrate the advantages of the system in accordance with this invention, calculations
have been performed to compare the system illustrated in Figure 4 with a conventional
OTEC system utilizing a conventional Rankine cycle under the same operating parameters
imposed by the temperatures of the heating and cooling mediums. The parameters for
the Rankine cycle system were obtained from the publication entitled "OTEC Pilot Plan
Heat Engine" by D. Richards and L. L. Perini, John Hopkins University, OTC 3592, 1979.
[0152] This comparison is set out in Table VI below.
[0153] The significant advantages of the system of Figure 4 in relation to the conventional
Rankine cycle system are clearly apparent from Table VI above. It is clear that the
system in accordance with this invention can provide significant imporvements in efficiency
and economy. This is particularly significant in OTEC systems and related systems
where the severe restraints imposed by the temperatures of the available heating and
cooling mediums have heretofore presented a serious barrier to commercial utilization
of OTEC systems.