U.S. patent application number 14/988054 was filed with the patent office on 2017-07-06 for power systems and methods implementing and using same.
The applicant listed for this patent is KALEX, LLC. Invention is credited to Alexander I. Kalina.
Application Number | 20170191382 14/988054 |
Document ID | / |
Family ID | 59226184 |
Filed Date | 2017-07-06 |
United States Patent
Application |
20170191382 |
Kind Code |
A1 |
Kalina; Alexander I. |
July 6, 2017 |
POWER SYSTEMS AND METHODS IMPLEMENTING AND USING SAME
Abstract
Power systems and methods including a vaporization subsystem
(VPSS), an energy conversion subsystem (ECSS), and a distillation
condensation subsystem (DCSS), where the DCSS produces a fully
condensed, lean working solution stream (LWSS) and a fully
condensed, rich working solution stream (RWSS) from a multiple
component working fluid using an external coolant stream, the VPSS
vaporizes and superheats the LWSS and RWSS in a multi-stage
vaporization process such that each LWSS remains in a state of
subcooled liquid prior to being mixed with the RWSS or one or more
intermediate solution streams to maximize heat extraction from an
external heat source stream to form a combined working solution
stream (CWSS) and converting a portion of the heat in the CWSS into
a useable from of energy in the ECSS.
Inventors: |
Kalina; Alexander I.;
(Hillsborough, CA) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
KALEX, LLC |
Belmont |
CA |
US |
|
|
Family ID: |
59226184 |
Appl. No.: |
14/988054 |
Filed: |
January 5, 2016 |
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
F01K 25/065 20130101;
F01K 11/02 20130101; F01K 3/262 20130101 |
International
Class: |
F01K 11/02 20060101
F01K011/02; F01K 25/06 20060101 F01K025/06; F01K 3/26 20060101
F01K003/26 |
Claims
1. A system for power generation comprising a distillation
condensation subsystem (DCSS-50), where a spent combined working
solution stream CWFS is fully condensed in a multi-stage
distillation and condensation process using variable composition
streams derived from the CWFS and an external coolant stream CS to
produce a fully condensed rich working solution stream RWFS and a
fully condensed lean working solution stream LWFS and a spent CS, a
vaporization subsystem (VPSS), where heat from an external heat
source stream HSS is used to heat, fully vaporize and superheat the
RWFS and the LWFS in a multi-stage vaporization process such that
each lean working solution stream remains in a state of supercooled
liquid prior to being mixed with the rich working solution stream
or one or more intermediate solution streams to maximize heat
transfer from the HSS to produce a fully vaporized and superheated
CWFS and a spent HSS, and an energy conversion subsystem (ECSS),
where a portion of heat associated with the CWFS is converted into
a useable form of energy producing a spent CWFS which is forwarded
to the DCSS-50 closing the system, where all of the streams are
derived from a single multi-component fluid.
2. The system of claim 1, wherein: the VPSS comprises a single heat
exchange unit having two working solution tubes and at least one
combining valve, where (a) the combining valve combines a heated
lean working solution stream in a state of subcooled liquid and a
vaporized rich working solution stream under conditions where the
lean working solution stream is fully absorbed by the vaporized
rich working solution stream producing a vaporized combined working
solution stream, (b) once formed, the vaporized combined working
solution stream is superheated to form the fully vaporized and
superheated, combined working solution stream, and (c) all heat is
derived from the external heat source stream, the ECSS comprises a
single pressure turbine, and the DCSS-50 comprising at least two
throttle control valves, three heat exchanges units, two
condensers, three pumps, and three separators.
3. The system of claim 1, wherein: the VPSS comprises a single heat
exchange unit having two working solution tubes and two combining
valves and one dividing valve, where (a) the dividing valve divides
a heated lean working solution stream into a heated first lean
working solution substream and a heated second lean working
solution substream, (b) a first combining valve combines the heated
second lean working solution substream in a state of subcooled
liquid and a partially vaporized rich working solution stream under
conditions where the heated second lean working solution substream
is fully absorbed by the partially vaporized rich working solution
stream producing a partially vaporized intermediate solution
stream, (c) a second combining valve combines a further heated
first lean working solution substream in a state of subcooled
liquid and a vaporized intermediate solution stream under
conditions where the further heated first lean working solution
substream is fully absorbed by the vaporized intermediate solution
stream producing a vaporized combined working solution stream, (d)
once formed, the vaporized combined working solution stream is
superheated to form the fully vaporized and superheated, combined
working solution stream, and (e) all heat is derived from the
external heat source stream, the ECSS comprises a single pressure
turbine, and the DCSS-50 comprising three throttle control valves,
three heat exchanges units, two condensers, three pumps, and three
separators.
4. The system of claim 1, wherein: the VPSS comprises a single heat
exchange unit having two working solution tubes and three combining
valves and two dividing valve, where (a) a first dividing valve
divides a heated lean working solution stream into a heated first
lean working solution substream and a heated second lean working
solution substream, (b) a first combining valve combines the heated
second lean working solution substream in a state of subcooled
liquid and a partially vaporized rich working solution stream under
conditions where the second heated lean working solution substream
is fully absorbed by the partially vaporized rich working solution
stream producing a partially vaporized first intermediate solution
stream, (c) a second dividing valve divides a further heated lean
first working solution substream into a further heated third lean
working solution substream and a further heated fourth lean working
solution substream, (d) a second combining valve combines a further
heated third lean working solution substream and a heated partially
vaporized first intermediate solution stream under conditions where
the yet further heated third lean working solution substream is
fully absorbed by the heated partially vaporized first intermediate
solution stream producing a partially vaporized second intermediate
solution stream, (f) a third combining valve combines a yet further
heated fourth lean working solution substream and a vaporized
second intermediate solution stream under conditions where the yet
further heated fourth lean working solution substream is fully
absorbed by the vaporized second intermediate solution stream
producing a vaporized combined working solution stream, (g) once
formed, the vaporized combined working solution stream is
superheated to form the fully vaporized and superheated, combined
working solution stream, and (h) all heat is derived from the
external heat source stream, the ECSS comprises a single pressure
turbine, and the DCSS-50 comprising three throttle control valves,
three heat exchanges units, two condensers, three pumps, and three
separators.
5. The system of claim 1, wherein the single multi-component
working fluid comprises at least one lower boiling point component
and at least one higher boiling point component.
6. The system of claim 5, wherein the components comprises a
mixture of compounds having favorable thermodynamic characteristics
and solubilities.
7. The system of claim 1, wherein the single multi-component fluid
is selected from the group consisting of a ammonia-water mixture, a
mixture of two or more hydrocarbons, a mixture of two or more
freon, a mixture of hydrocarbons and freons, and mixtures
thereof.
8. The system of claim 7, wherein the single multi-component fluid
comprises a mixture of water and ammonia.
9. The system of claim 6, wherein the single multi-component fluid
comprises a mixture of two or more hydrocarbons, a mixture of two
or more freon, or a mixture of hydrocarbons and freons.
10. A method comprising: condensing a spent combined working
solution stream in a distillation condensation subsystem in a
multi-stage distillation and condensation process using variable
composition streams derived from the spent combined working
solution stream and an external coolant stream producing a fully
condensed, intermediate pressure, rich working solution stream and
a fully condensed, intermediate pressure, lean working solution
stream and a spent external coolant stream, concurrently
pressurizing the fully condensed, intermediate pressure, rich
working solution stream and the fully condensed, intermediate
pressure, lean working solution stream in separate feed pumps
producing a fully condensed, higher pressure, rich working solution
stream and a fully condensed, higher pressure, lean working
solution stream, transferring heat from an external heat source
stream in a vaporization subsystem in a multi-stage vaporization
process such that each higher pressure, lean working solution
stream remains in a state of subcooled liquid prior to being mixed
with the rich working solution stream or one or more intermediate
solution streams derived from the rich working solution stream and
the lean working solution stream or one or more lean working
solution substreams to maximize heat transfer from the external
heat source stream producing a fully vaporized and superheated,
higher pressure, combined working solution stream and a spent
external heat source stream, and converting a portion of heat in a
fully vaporized and superheated, higher pressure, combined working
solution stream in an energy extraction subsystem to a useable form
of energy (mechanical and/or electrical) producing the spent
combined working solution stream, where all of the streams are
derived from a single multi-component fluid comprises at least one
lower boiling point component and at least one higher boiling point
component selected from the group consisting of a ammonia-water
mixture, a mixture of two or more hydrocarbons, a mixture of two or
more freon, a mixture of hydrocarbons and freons, and mixtures
thereof.
11. A method comprising: concurrently forwarding: (a) a fully
condensed, rich working solution stream into a fifth pump producing
a higher pressure, fully condensed, rich working solution stream
and (b) a fully condensed, lean working solution stream into a
sixth pump producing a higher pressure, fully condensed, lean
working solution stream, vaporizing and superheating the higher
pressure, fully condensed, rich working solution stream and the
higher pressure, fully condensed, lean working solution stream in a
vaporization subsystem in a multi-stage vaporization process using
heat from an initial external heat source stream so that the higher
pressure, fully condensed, lean working solution stream or a
plurality of higher pressure, lean working solution substreams
is/are in a state of subcooled liquid prior to mixing and being
fully absorbed by a vapor component of a vaporized, higher
pressure, rich working solution stream or a plurality of vaporized,
higher pressure, intermediate solution streams derived from the
higher pressure, rich working solution stream and the higher
pressure, lean working solution stream producing a fully vaporized
and superheated, combined working solution stream and a spent
external heat source stream, converting a portion of heat in the
fully vaporized and superheated, combined working solution stream
in an energy extraction subsystem to a useable form of energy
comprising mechanical and/or electrical energy producing a spent
combined working solution stream, and condensing the spent combined
working solution stream in a multi-stage distillation and
condensation process in a distillation condensation subsystem using
variable composition streams derived from the spent combined
working solution stream and an initial external coolant stream to
produce the fully condensed, rich working solution stream, the
fully condensed, lean working solution stream, and a spent external
coolant stream, where all of the streams are derived from a single
multi-component fluid.
12. The method of claim 11, wherein the multi-stage vaporization
process comprises the steps of: concurrently heating: (a) the
higher pressure, fully condensed, rich working solution stream and
(b) the higher pressure, fully condensed, lean working solution
stream with heat from a first cooled external heat source stream in
a lower portion of the vaporization subsystem producing the spent
external heat source stream, a vaporized, higher pressure, rich
working solution stream, and a heated, higher pressure, lean
working solution stream, which corresponds to a state of subcooled
liquid, combining the vaporized, higher pressure, rich working
solution stream and the heated, higher pressure, lean working
solution stream in the vaporization subsystem under conditions so
that the heated, higher pressure, lean working solution stream is
fully absorbed by a vapor content of the vaporized, higher
pressure, rich working solution stream producing a vaporized,
combined working solution stream, and heating the vaporized,
combined working solution stream with heat from the initial heat
source stream in an upper portion of the vaporization subsystem
producing the fully vaporized and superheated, combined working
solution stream and the first cooled external heat source
stream.
13. The method of claim 11, wherein the multi-stage distillation
and condensation process comprises the steps of: concurrently
heating: (a) the higher pressure, fully condensed, rich working
solution stream and (b) the higher pressure, fully condensed lean
working solution stream with heat from a second cooled external
heat source stream producing the spent external heat source stream,
a partially vaporized, higher pressure, rich working solution
stream, and a heated, higher pressure, lean working solution
stream, which corresponds to a state of subcooled liquid, dividing
the heated, higher pressure, lean working solution stream into a
heated, higher pressure, first lean working solution substream and
a heated, higher pressure, second lean working solution substream,
where both of the heated, higher pressure, lean working solution
substreams correspond to states of subcooled liquid, combining the
partially vaporized, higher pressure, rich working solution stream
and the heated, higher pressure, first lean working solution
substream in the vaporization subsystem under conditions so that
the heated, higher pressure, first lean working solution stream is
fully absorbed by a vapor content of the partially vaporized,
higher pressure, rich working solution stream producing a higher
pressure, first intermediate solution stream, currently heating:
(a) the higher pressure, first intermediate solution stream and the
heated, higher pressure, second lean working solution substream
with heat from a first cooled external heat source stream producing
the second external heat source stream, a partially vaporized,
higher pressure, first intermediate solution stream, and a further
heated, higher pressure, second lean working solution substream,
which corresponds to a state of subcooled liquid, combining the
partially vaporized, higher pressure, first intermediate solution
stream and the further heated, higher pressure, second lean working
solution substream in the vaporization subsystem under conditions
so that the further heated, higher pressure, second lean working
solution substream is fully absorbed by a vapor content of the
partially vaporized, higher pressure, first intermediate solution
stream producing the vaporized, combined working solution stream,
and heating the vaporized, combined working solution stream with
heat from the initial heat source stream in an upper portion of the
vaporization subsystem producing the fully vaporized and
superheated, combined working solution stream and the first cooled
external heat source stream.
14. The method of claim 11, wherein the multi-stage distillation
and condensation process comprises the steps of: currently heating:
(a) the higher pressure, fully condensed, rich working solution
stream and (b) the higher pressure, fully condensed, lean working
solution stream with heat from a third cooled external heat source
stream producing the spent external heat source stream, a partially
vaporized, higher pressure, rich working solution stream, and a
heated, higher pressure, lean working solution stream, which
corresponds to a state of subcooled liquid, dividing the heated,
higher pressure, lean working solution stream into a heated, higher
pressure, first lean working solution substream and a heated,
higher pressure, second lean working solution substream, where both
of the heated, lean working solution substreams correspond to
states of subcooled liquid, combining the partially vaporized,
higher pressure, rich working solution stream and the heated,
higher pressure, first lean working solution substream in the
vaporization subsystem under conditions so that the heated, higher
pressure, first lean working solution substream is fully absorbed
by a vapor content of the partially vaporized, higher pressure,
rich working solution stream producing a higher pressure, first
intermediate solution stream, currently heating: (a) the higher
pressure, first intermediate solution stream and the heated, higher
pressure, second lean working solution substream with heat from a
second cooled external heat source stream producing the third
external heat source stream, a partially vaporized, higher
pressure, first intermediate solution stream, and a further heated,
higher pressure, second lean working solution stream, which
corresponds to a state of subcooled liquid, dividing the further
heated, higher pressure, second lean working solution substream
into a further heated, higher pressure, third lean working solution
substream and a further heated, higher pressure, fourth lean
working solution substream, where both of the further heated,
higher pressure, lean working solution substream correspond to a
state of subcooled liquid, combining the partially vaporized,
higher pressure, first intermediate solution stream and the further
heated, higher pressure, third lean working solution substream in
the vaporization subsystem under conditions so that the further
heated, higher pressure, third lean working solution substream is
fully absorbed by a vapor content of the partially vaporized,
higher pressure, first intermediate solution stream producing a
higher pressure, second intermediate solution stream, currently
heating: (a) the higher pressure, second intermediate solution
stream and the further heated, higher pressure, fourth lean working
solution substream with heat from a first cooled external heat
source stream producing the second external heat source stream, a
vaporized, higher pressure, second intermediate solution stream,
and a yet further heated, higher pressure, fourth lean working
solution stream, which corresponds to a state of subcooled liquid,
combining the vaporized, higher pressure, second intermediate
solution stream and the yet further heated, higher pressure, fourth
lean working solution substream in the vaporization subsystem under
conditions so that the yet further heated, higher pressure, fourth
lean working solution substream is fully absorbed by a vapor
content of the vaporized, higher pressure, second intermediate
solution stream producing the vaporized combined working solution
stream, and heating the vaporized combined working solution stream
with heat from the initial heat source stream in an upper portion
of the vaporization subsystem producing the fully vaporized and
superheated, combined working solution stream and the first cooled
external heat source stream.
15. The method of claim 11, wherein the multi-stage distillation
and condensation process comprises the steps of: if the spent
combined working solution stream is in a state of slightly
superheated vapor, combining the spent combined working solution
stream and a second pressure adjusted, first lean substream
producing a saturated vapor intermediate solution stream,
transferring heat from either the spent combined working solution
stream or the saturated vapor intermediate solution stream in a
third heat exchange unit (HE3) in counterflow to a liquid third
lean stream producing either a partially condensed, spent combined
working solution stream or a partially condensed, intermediate
solution stream corresponding to a state of a liquid-vapor mixture
and a heated third lean stream corresponding to a state of a
liquid-vapor mixture, transferring heat from either the partially
condensed, spent combined working solution stream or the partially
condensed, intermediate solution stream in a second heat exchange
unit (HE2) in counterflow to a second higher pressure, rich basic
solution substream producing a cooled and partially condensed,
spent combined working solution stream or a cooled and partially
condensed, intermediate solution stream corresponding to a state of
a vapor-liquid mixture and a partially vaporized, second higher
pressure, rich basic solution substream corresponding to a state of
a vapor-liquid mixture, combining either the cooled and partially
condensed, spent combined working solution stream or the cooled and
partially condensed, intermediate solution stream and a pressure
adjusted lean working solution substream producing a lean basic
solution stream, where a composition of the lean basic solution
stream is substantially leaner than a composition of the
intermediate solution streams and a composition of the combined
working solution streams, condensing the lean basic solution stream
in a condenser or first exchange unit or heat exchanger (HE1) in
counterflow to a first higher pressure external coolant substream
producing a fully condensed lean basic solution stream and a spent
external coolant substream, pressurizing the fully condensed lean
basic solution stream in a feed or first pump (P1) producing an
intermediate pressure lean basic solution stream corresponding to a
state of subcooled liquid, combining the intermediate pressure lean
basic solution stream and a vapor second rich stream corresponding
to a state of saturated vapor producing an intermediate pressure,
rich basic solution stream corresponding to a state of saturated
liquid, where the intermediate pressure lean basic solution stream
fully absorbs the vapor second rich stream and a composition of the
intermediate pressure, rich basic solution stream is richer than a
composition of the lean basic solution streams, pressurizing the
intermediate pressure, rich basic solution stream in a circulating
or second pump (P2) producing a higher pressure, rich basic
solution stream corresponding to a state of subcooled liquid,
dividing the higher pressure, rich basic solution stream into a
first higher pressure, rich basic solution substream and the second
higher pressure, rich basic solution substream, separating the
partially vaporized, second higher pressure, rich basic solution
substream in a third gravity separator (SP3) producing the liquid
third lean stream and a vapor third rich stream, where a
composition of the third lean stream is leaner than a composition
of the rich basic solution substreams, separating the heated third
lean stream in a first gravity separator (SP1) producing a
saturated vapor first rich stream and a saturated liquid first lean
stream, if the spent combined working solution stream is in a state
of slightly superheated vapor, dividing the saturated liquid first
lean stream into a first saturated liquid first lean substream and
a second saturated liquid first lean substream and pressure
adjusting the second saturated liquid first lean substream in a
second throttle-valve (TV2) producing the second pressure adjusted,
first lean substream, pressure adjusting the first saturated liquid
first lean substream or the saturated liquid first lean stream in a
third throttle valve (TV3) producing an intermediate pressure first
lean substream or an intermediate pressure saturated first lean
stream corresponding to a state of a liquid-vapor mixture,
separating the intermediate pressure first lean substream or the
intermediate pressure saturated first lean stream in a second
gravity separator (SP2) producing the saturated vapor rich stream
and a saturated liquid, intermediate pressure, lean working
solution stream, dividing the saturated liquid, intermediate
pressure, lean working solution stream into a saturated liquid,
intermediate pressure, lean working solution substream and the
saturated liquid lean, intermediate pressure, working solution
stream, pressure adjusting the saturated liquid, intermediate
pressure, lean working solution substream in a fourth throttle
valve (TV4) producing the pressure adjusted lean working solution
substream, combining the saturated vapor first rich stream and the
vapor third rich stream producing a combined vapor rich stream,
transferring heat from the combined vapor rich stream in a sixth
heat exchange unit or heat exchanger (HE6) in counterflow to an
intermediate pressure rich working solution stream producing a
cooled and partially condensed, combined rich stream corresponding
to a state of a vapor-liquid mixture and a heated intermediate
pressure rich working solution stream combining the cooled and
partially condensed, combined rich stream and the first higher
pressure rich basic solution substream producing a rich working
solution stream corresponding to a state of a liquid-vapor mixture,
condensing the rich working solution stream in a condenser or
fourth heat exchange unit or heat exchanger (HE4) in counterflow to
a second higher pressure coolant substream producing a spent
coolant substream and a condensed rich working solution stream
corresponding to a state of saturated liquid, and pressurizing the
condensed rich working solution stream in a booster or third pump
(P3) producing the intermediate pressure rich working solution
stream corresponding to a state of subcooled liquid.
16. The method of claim 15, further comprising: pressurizing an
initial external coolant stream in a circulating pump (CP)
producing a higher pressure external coolant stream, and dividing
the higher pressure external coolant stream into a first higher
pressure external coolant substream and a second higher pressure
external coolant substream.
17. The method of claim 11, wherein the single multi-component
working fluid comprises at least one lower boiling point component
and at least one higher boiling point component.
18. The method of claim 11, wherein the single multi-component
fluid is selected from the group consisting of a ammonia-water
mixture, a mixture of two or more hydrocarbons, a mixture of two or
more freon, a mixture of hydrocarbons and freons, and mixtures
thereof.
19. The method of claim 18, wherein the single multi-component
fluid comprises a mixture of water and ammonia.
20. The system of claim 18, wherein the single multi-component
fluid comprises a mixture of two or more hydrocarbons, a mixture of
two or more freon, or a mixture of hydrocarbons and freons.
Description
BACKGROUND OF THE INVENTION
[0001] 1. Field of the Invention
[0002] Embodiments of the present invention relate to systems and
methods, designated SBC-19 with DCSS-50, intended for the
generation of power utilizing heat from heat sources that have a
wide range of temperatures such as exhausts from a gas turbine, or
other similar exhaust gas heat sources, or alternately, industrial
waste heat sources.
[0003] More particularly, embodiments of the present invention
relate to systems and methods, designated SBC-19 with DCSS-50,
intended for the generation of power utilizing heat from heat
sources that have a wide range of temperatures such as exhausts
from a gas turbine, or other similar exhaust gas heat sources, or
alternately, industrial waste heat sources, where the system
includes a vaporization subsystem, an energy extraction subsystem,
and a distillation condensation subsystem (DCSS-50).
[0004] 2. Description of the Related Art
[0005] When utilizing such sources it is crucial to make maximum
utilization of the heat available; i.e., to cool the heat source
down to the greatest degree possible and make use of the heat thus
obtained.
[0006] To this end, in the prior art, bottoming cycles utilizing
the exhaust from gas turbines use dual and even triple pressure
Rankine cycle systems, with two or three turbines respectively. In
such systems, the high temperature portion of the heat from the
heat source stream is used for high pressure boiling (utilized in a
high pressure turbine), the mid-temperature portion of the heat is
used at moderate pressures (in a mid-pressure turbine,) and the
low-temperature portion of the heat is used at low pressure (in a
low pressure turbine).
[0007] Thus, there is a need in the art for power systems that
utilize a single pressure turbine energy extraction system that
maximizes heat utilization of heat from heat sources that have a
wide range of temperatures such as exhausts from a gas turbine, or
other similar exhaust gas heat sources, or alternately, industrial
waste heat sources.
SUMMARY OF THE INVENTION
[0008] Embodiments of this invention provide a power system (PS)
including a vaporization subsystem (VPSS), an energy conversion
subsystem (ECSS), and a distillation condensation subsystem
(DCSS-50), where the system utilizes a multiple component working
fluid, the DCSS-50 produces a fully condensed lean working solution
stream and a fully condensed working solution stream from the
working fluid using an external coolant stream, and the VPSS
vaporizes and superheats the two working solution streams in a
multi-stage vaporization process such that each lean stream remains
in a state of subcooled liquid prior to being mixed with the rich
working solution stream or intermediate solution stream to maximize
heat extraction from an external heat source stream and converting
a portion of the heat in a combined working solution stream exiting
the VPSS in the ECSS.
[0009] Embodiments of this invention provide a method including
transferring heat from an external heat source stream to a fully
condensed lean working solution stream and a fully condensed
working solution stream derived from a multiple component working
fluid in a multi-stage vaporization process such that each lean
stream remains in a state of subcooled liquid prior to being mixed
with the rich working solution stream or one or more intermediate
solution streams to maximize heat extraction from an external heat
source stream in a vaporization subsystem (VPSS) to form a fully
vaporized and superheated combined working solution stream,
converting a portion of heat in a fully vaporized and superheated
combined working solution stream in the ECSS into a useable form of
energy (mechanical and/or electrical), and condensing a spent
combined working solution stream in a distillation condensation
subsystem (DCSS-50) using an external coolant stream to form a lean
working solution stream and a rich working solution stream.
BRIEF DESCRIPTION OF THE DRAWINGS
[0010] The invention can be better understood with reference to the
following detailed description together with the appended
illustrative drawings in which like elements are numbered the
same:
[0011] FIG. 1 depicts a general embodiment of a system of this
invention including a vaporization subsystem (VPSS), an energy
conversion subsystem (ECSS), and a distillation condensation
subsystem (DCSS-50).
[0012] FIG. 2A depicts a specific embodiment of a system of this
invention.
[0013] FIG. 2B depicts another specific embodiment of a system of
this invention.
[0014] FIG. 2C depicts another specific embodiment of a system of
this invention.
[0015] FIG. 3 depicts an embodiment of the distillation
condensation subsystem (DCSS-50).
DEFINITIONS USED IN THE INVENTION
[0016] The term "substantially" means that the property is within
95% of its desired value. In other embodiments, "substantially"
means that the property is within 97.5% of its desired value. In
other embodiments, "substantially" means that the property is
within 99% of its desired value. In other embodiments,
"substantially" means that the property is within 99.9% of its
desired value. For example, the term "substantially complete" as it
relates to a coating, means that the coating is at least 95%
complete. In other embodiments, the term "substantially complete"
as it relates to a coating, means that the coating is at least
97.5% complete. In other embodiments, the term "substantially
complete" as it relates to a coating, means that the coating is at
least 99% complete. In other embodiments, the term "substantially
complete" as it relates to a coating, means that the coating is at
least 99.9% complete.
[0017] The term "substantially" means that a value is within about
.+-.5% of the indicated value. In certain embodiments, the value is
within about .+-.2.5% of the indicated value. In certain
embodiments, the value is within about .+-.1% of the indicated
value. In certain embodiments, the value is within about .+-.0.5%
of the indicated value. In certain embodiments, the value is within
about .+-.0.1% of the indicated value. In certain embodiments, the
value is within about .+-.0.01% of the indicated value.
[0018] The term "about" means that the value is within about
.+-.10% of the indicated value. In certain embodiments, the value
is within about .+-.5% of the indicated value. In certain
embodiments, the value is within about .+-.2.5% of the indicated
value. In certain embodiments, the value is within about .+-.1% of
the indicated value. In certain embodiments, the value is within
about .+-.0.5% of the indicated value. The term "about" means that
the property is within about .+-.10% of the indicated value. In
certain embodiments, the property is within about .+-.5% of the
indicated value. In certain embodiments, the property is within
about .+-.2.5% of the indicated value. In certain embodiments, the
property is within about .+-.1% of the indicated value. In certain
embodiments, the property is within about .+-.0.5% of the indicated
value.
[0019] The term "mixture" means that two are more components have
been mixed together to form a mixture before use.
[0020] The term "combination" means that two or more components are
used separately and the final composition includes a combination of
material made from single components.
DETAILED DESCRIPTION OF THE INVENTION
[0021] The inventor has found that systems and corresponding
methods can be constructed that permit maximization of generation
of power utilizing heat from heat sources that have a wide range of
temperatures such as exhausts from a gas turbine, or other similar
exhaust gas heat sources, or alternately, industrial waste heat
sources. In the present systems, a multiple component, variable
composition working fluid is used and the maximum possible
utilization of the heat source is attained by using a multi-stage
vaporization process for the working fluid, with different
compositions of working fluid at each stage.
[0022] Embodiments of this invention relate to systems for power
generation including a distillation condensation subsystem
(DCSS-50), where a spent combined working solution stream CWFS is
fully condensed in a multi-stage distillation and condensation
process using variable composition streams derived from the CWFS
and an external coolant stream CS to produce a fully condensed rich
working solution stream RWFS and a fully condensed lean working
solution stream LWFS and a spent CS. The systems further includes a
vaporization subsystem (VPSS), where heat from an external heat
source stream HSS is used to heat, fully vaporize and superheat the
RWFS and the LWFS in a multi-stage vaporization process such that
each lean working solution stream remains in a state of supercooled
liquid prior to being mixed with the rich working solution stream
or one or more intermediate solution streams to maximize heat
transfer from the HSS to produce a fully vaporized and superheated
CWFS and a spent HSS. The systems further includes an energy
conversion subsystem (ECSS), where a portion of heat associated
with the CWFS is converted into a useable form of energy producing
a spent CWFS which is forwarded to the DCSS-50 closing the system.
All of the streams used in the systems are derived from a single
multi-component fluid.
[0023] In certain embodiments, the VPSS includes a single heat
exchange unit having two working solution tubes and at least one
combining valve, where (a) the combining valve combines a heated
lean working solution stream in a state of subcooled liquid and a
vaporized rich working solution stream under conditions where the
lean working solution stream is fully absorbed by the vaporized
rich working solution stream producing a vaporized combined working
solution stream, (b) once formed, the vaporized combined working
solution stream is superheated to form the fully vaporized and
superheated, combined working solution stream, and (c) all heat is
derived from the external heat source stream, the ECSS comprises a
single pressure turbine, and the DCSS-50 comprising at least two
throttle control valves, three heat exchanges units, two
condensers, three pumps, and three separators.
[0024] In other embodiments of the invention, the VPSS comprises a
single heat exchange unit having two working solution tubes and two
combining valves and one dividing valve, where (a) the dividing
valve divides a heated lean working solution stream into a heated
first lean working solution substream and a heated second lean
working solution substream, (b) a first combining valve combines
the heated second lean working solution substream in a state of
subcooled liquid and a partially vaporized rich working solution
stream under conditions where the heated second lean working
solution substream is fully absorbed by the partially vaporized
rich working solution stream producing a partially vaporized
intermediate solution stream, (c) a second combining valve combines
a further heated first lean working solution substream in a state
of subcooled liquid and a vaporized intermediate solution stream
under conditions where the further heated first lean working
solution substream is fully absorbed by the vaporized intermediate
solution stream producing a vaporized combined working solution
stream, (d) once formed, the vaporized combined working solution
stream is superheated to form the fully vaporized and superheated,
combined working solution stream, and (e) all heat is derived from
the external heat source stream, the ECSS comprises a single
pressure turbine, and the DCSS-50 comprising three throttle control
valves, three heat exchanges units, two condensers, three pumps,
and three separators.
[0025] In other embodiments of the invention, the VPSS comprises a
single heat exchange unit having two working solution tubes and
three combining valves and two dividing valve, where (a) a first
dividing valve divides a heated lean working solution stream into a
heated first lean working solution substream and a heated second
lean working solution substream, (b) a first combining valve
combines the heated second lean working solution substream in a
state of subcooled liquid and a partially vaporized rich working
solution stream under conditions where the second heated lean
working solution substream is fully absorbed by the partially
vaporized rich working solution stream producing a partially
vaporized first intermediate solution stream, (c) a second dividing
valve divides a further heated lean first working solution
substream into a further heated third lean working solution
substream and a further heated fourth lean working solution
substream, (d) a second combining valve combines a further heated
third lean working solution substream and a heated partially
vaporized first intermediate solution stream under conditions where
the yet further heated third lean working solution substream is
fully absorbed by the heated partially vaporized first intermediate
solution stream producing a partially vaporized second intermediate
solution stream, (f) a third combining valve combines a yet further
heated fourth lean working solution substream and a vaporized
second intermediate solution stream under conditions where the yet
further heated fourth lean working solution substream is fully
absorbed by the vaporized second intermediate solution stream
producing a vaporized combined working solution stream, (g) once
formed, the vaporized combined working solution stream is
superheated to form the fully vaporized and superheated, combined
working solution stream, and (h) all heat is derived from the
external heat source stream, the ECSS comprises a single pressure
turbine, and the DCSS-50 comprising three throttle control valves,
three heat exchanges units, two condensers, three pumps, and three
separators.
[0026] In other embodiments of the invention, the single
multi-component working fluid comprises at least one lower boiling
point component and at least one higher boiling point component. In
other embodiments, the single multi-component fluid is selected
from the group consisting of a ammonia-water mixture, a mixture of
two or more hydrocarbons, a mixture of two or more freon, a mixture
of hydrocarbons and freons, and mixtures thereof. In other
embodiments, the single multi-component fluid comprises a mixture
of compounds having favorable thermodynamic characteristics and
solubilities. In other embodiments, the single multi-component
fluid comprises a mixture of water and ammonia.
[0027] Embodiments of this invention relate to methods include
condensing a spent combined working solution stream in a
distillation condensation subsystem in a multi-stage distillation
and condensation process using variable composition streams derived
from the spent combined working solution stream and an external
coolant stream producing a fully condensed, intermediate pressure,
rich working solution stream and a fully condensed, intermediate
pressure, lean working solution stream and a spent external coolant
stream. The methods also include concurrently pressurizing the
fully condensed, intermediate pressure, rich working solution
stream and the fully condensed, intermediate pressure, lean working
solution stream in separate feed pumps producing a fully condensed,
higher pressure, rich working solution stream and a fully
condensed, higher pressure, lean working solution stream. The
methods also include transferring heat from an external heat source
stream in a vaporization subsystem in a multi-stage vaporization
process such that each higher pressure, lean working solution
stream remains in a state of subcooled liquid prior to being mixed
with the rich working solution stream or one or more intermediate
solution streams derived from the rich working solution stream and
the lean working solution stream or one or more lean working
solution substreams to maximize heat transfer from the external
heat source stream producing a fully vaporized and superheated,
higher pressure, combined working solution stream and a spent
external heat source stream. The methods also include converting a
portion of heat in a fully vaporized and superheated, higher
pressure, combined working solution stream in an energy extraction
subsystem to a useable form of energy (mechanical and/or
electrical) producing the spent combined working solution stream.
All of the streams used in the methods are derived from a single
multi-component fluid comprises at least one lower boiling point
component and at least one higher boiling point component selected
from the group consisting of a ammonia-water mixture, a mixture of
two or more hydrocarbons, a mixture of two or more freon, a mixture
of hydrocarbons and freons, and mixtures thereof.
[0028] Embodiments of this invention relate to methods including
concurrently forwarding: (a) a fully condensed, rich working
solution stream into a fifth pump producing a higher pressure,
fully condensed, rich working solution stream and (b) a fully
condensed, lean working solution stream into a sixth pump producing
a higher pressure, fully condensed, lean working solution stream.
The methods include vaporizing and superheating the higher
pressure, fully condensed, rich working solution stream and the
higher pressure, fully condensed, lean working solution stream in a
vaporization subsystem in a multi-stage vaporization process using
heat from an initial external heat source stream so that the higher
pressure, fully condensed, lean working solution stream or a
plurality of higher pressure, lean working solution substreams
is/are in a state of subcooled liquid prior to mixing and being
fully absorbed by a vapor component of a vaporized, higher
pressure, rich working solution stream or a plurality of vaporized,
higher pressure, intermediate solution streams derived from the
higher pressure, rich working solution stream and the higher
pressure, lean working solution stream producing a fully vaporized
and superheated, combined working solution stream and a spent
external heat source stream. The methods include converting a
portion of heat in the fully vaporized and superheated, combined
working solution stream in an energy extraction subsystem to a
useable form of energy comprising mechanical and/or electrical
energy producing a spent combined working solution stream. The
methods include condensing the spent combined working solution
stream in a multi-stage distillation and condensation process in a
distillation condensation subsystem using variable composition
streams derived from the spent combined working solution stream and
an initial external coolant stream to produce the fully condensed,
rich working solution stream, the fully condensed, lean working
solution stream, and a spent external coolant stream. All of the
streams using in the methods are derived from a single
multi-component fluid.
[0029] In certain embodiments of the invention, the multi-stage
vaporization process includes concurrently heating: (a) the higher
pressure, fully condensed, rich working solution stream and (b) the
higher pressure, fully condensed, lean working solution stream with
heat from a first cooled external heat source stream in a lower
portion of the vaporization subsystem producing the spent external
heat source stream, a vaporized, higher pressure, rich working
solution stream, and a heated, higher pressure, lean working
solution stream, which corresponds to a state of subcooled liquid.
The multi-stage vaporization process also includes combining the
vaporized, higher pressure, rich working solution stream and the
heated, higher pressure, lean working solution stream in the
vaporization subsystem under conditions so that the heated, higher
pressure, lean working solution stream is fully absorbed by a vapor
content of the vaporized, higher pressure, rich working solution
stream producing a vaporized, combined working solution stream. The
multi-stage vaporization process also includes heating the
vaporized, combined working solution stream with heat from the
initial heat source stream in an upper portion of the vaporization
subsystem producing the fully vaporized and superheated, combined
working solution stream and the first cooled external heat source
stream.
[0030] In other embodiments of the invention, the multi-stage
distillation and condensation process includes concurrently
heating: (a) the higher pressure, fully condensed, rich working
solution stream and (b) the higher pressure, fully condensed lean
working solution stream with heat from a second cooled external
heat source stream producing the spent external heat source stream,
a partially vaporized, higher pressure, rich working solution
stream, and a heated, higher pressure, lean working solution
stream, which corresponds to a state of subcooled liquid. The
multi-stage vaporization process also includes dividing the heated,
higher pressure, lean working solution stream into a heated, higher
pressure, first lean working solution substream and a heated,
higher pressure, second lean working solution substream, where both
of the heated, higher pressure, lean working solution substreams
correspond to states of subcooled liquid. The multi-stage
vaporization process also includes combining the partially
vaporized, higher pressure, rich working solution stream and the
heated, higher pressure, first lean working solution substream in
the vaporization subsystem under conditions so that the heated,
higher pressure, first lean working solution stream is fully
absorbed by a vapor content of the partially vaporized, higher
pressure, rich working solution stream producing a higher pressure,
first intermediate solution stream. The multi-stage vaporization
process also includes currently heating: (a) the higher pressure,
first intermediate solution stream and the heated, higher pressure,
second lean working solution substream with heat from a first
cooled external heat source stream producing the second external
heat source stream, a partially vaporized, higher pressure, first
intermediate solution stream, and a further heated, higher
pressure, second lean working solution substream, which corresponds
to a state of subcooled liquid. The multi-stage vaporization
process also includes combining the partially vaporized, higher
pressure, first intermediate solution stream and the further
heated, higher pressure, second lean working solution substream in
the vaporization subsystem under conditions so that the further
heated, higher pressure, second lean working solution substream is
fully absorbed by a vapor content of the partially vaporized,
higher pressure, first intermediate solution stream producing the
vaporized, combined working solution stream. The multi-stage
vaporization process also includes heating the vaporized, combined
working solution stream with heat from the initial heat source
stream in an upper portion of the vaporization subsystem producing
the fully vaporized and superheated, combined working solution
stream and the first cooled external heat source stream.
[0031] In other embodiments of the invention, the multi-stage
distillation and condensation process includes currently heating
(a) the higher pressure, fully condensed, rich working solution
stream and (b) the higher pressure, fully condensed, lean working
solution stream with heat from a third cooled external heat source
stream producing the spent external heat source stream, a partially
vaporized, higher pressure, rich working solution stream, and a
heated, higher pressure, lean working solution stream, which
corresponds to a state of subcooled liquid. The multi-stage
vaporization process also includes dividing the heated, higher
pressure, lean working solution stream into a heated, higher
pressure, first lean working solution substream and a heated,
higher pressure, second lean working solution substream, where both
of the heated, lean working solution substreams correspond to
states of subcooled liquid. The multi-stage vaporization process
also includes combining the partially vaporized, higher pressure,
rich working solution stream and the heated, higher pressure, first
lean working solution substream in the vaporization subsystem under
conditions so that the heated, higher pressure, first lean working
solution substream is fully absorbed by a vapor content of the
partially vaporized, higher pressure, rich working solution stream
producing a higher pressure, first intermediate solution stream.
The multi-stage vaporization process also includes currently
heating: (a) the higher pressure, first intermediate solution
stream and the heated, higher pressure, second lean working
solution substream with heat from a second cooled external heat
source stream producing the third external heat source stream, a
partially vaporized, higher pressure, first intermediate solution
stream, and a further heated, higher pressure, second lean working
solution stream, which corresponds to a state of subcooled liquid.
The multi-stage vaporization process also includes dividing the
further heated, higher pressure, second lean working solution
substream into a further heated, higher pressure, third lean
working solution substream and a further heated, higher pressure,
fourth lean working solution substream, where both of the further
heated, higher pressure, lean working solution substream correspond
to a state of subcooled liquid. The multi-stage vaporization
process also includes combining the partially vaporized, higher
pressure, first intermediate solution stream and the further
heated, higher pressure, third lean working solution substream in
the vaporization subsystem under conditions so that the further
heated, higher pressure, third lean working solution substream is
fully absorbed by a vapor content of the partially vaporized,
higher pressure, first intermediate solution stream producing a
higher pressure, second intermediate solution stream. The
multi-stage vaporization process also includes currently heating:
(a) the higher pressure, second intermediate solution stream and
the further heated, higher pressure, fourth lean working solution
substream with heat from a first cooled external heat source stream
producing the second external heat source stream, a vaporized,
higher pressure, second intermediate solution stream, and a yet
further heated, higher pressure, fourth lean working solution
stream, which corresponds to a state of subcooled liquid. The
multi-stage vaporization process also includes combining the
vaporized, higher pressure, second intermediate solution stream and
the yet further heated, higher pressure, fourth lean working
solution substream in the vaporization subsystem under conditions
so that the yet further heated, higher pressure, fourth lean
working solution substream is fully absorbed by a vapor content of
the vaporized, higher pressure, second intermediate solution stream
producing the vaporized combined working solution stream. The
multi-stage vaporization process also includes heating the
vaporized combined working solution stream with heat from the
initial heat source stream in an upper portion of the vaporization
subsystem producing the fully vaporized and superheated, combined
working solution stream and the first cooled external heat source
stream.
[0032] In other embodiments of the invention, the multi-stage
distillation and condensation process includes if the spent
combined working solution stream (S118) is in a state of slightly
superheated vapor, combining the spent combined working solution
stream (S118) and a second pressure adjusted, first lean substream
(S71) producing a saturated vapor intermediate solution stream
(S38). The multi-stage vaporization process also includes
transferring heat from either the spent combined working solution
stream (S118) or the saturated vapor intermediate solution stream
(S38) in a third heat exchange unit (HE3) in counterflow to a
liquid third lean stream (S26) producing either a partially
condensed, spent combined working solution stream (S15) or a
partially condensed, intermediate solution stream (S15)
corresponding to a state of a liquid-vapor mixture and a heated
third lean stream (S5) corresponding to a state of a liquid-vapor
mixture. The multi-stage vaporization process also includes
transferring heat from either the partially condensed, spent
combined working solution stream (S15) or the partially condensed,
intermediate solution stream (S15) in a second heat exchange unit
(HE2) in counterflow to a second higher pressure, rich basic
solution substream (S23) producing a cooled and partially
condensed, spent combined working solution stream (S41) or a cooled
and partially condensed, intermediate solution stream (S41)
corresponding to a state of a vapor-liquid mixture and a partially
vaporized, second higher pressure, rich basic solution substream
(S25) corresponding to a state of a vapor-liquid mixture. The
multi-stage vaporization process also includes combining either the
cooled and partially condensed, spent combined working solution
stream (S41) or the cooled and partially condensed, intermediate
solution stream (S41) and a pressure adjusted lean working solution
substream (S13) producing a lean basic solution stream (S42), where
a composition of the lean basic solution stream (S42) is
substantially leaner than a composition of the intermediate
solution streams and a composition of the combined working solution
streams. The multi-stage vaporization process also includes
condensing the lean basic solution stream (S42) in a condenser or
first exchange unit or heat exchanger (HE1) in counterflow to a
first higher pressure external coolant substream (S52) producing a
fully condensed lean basic solution stream (S1) and a spent
external coolant substream (S54). The multi-stage vaporization
process also includes pressurizing the fully condensed lean basic
solution stream (S1) in a feed or first pump (P1) producing an
intermediate pressure lean basic solution stream (S2) corresponding
to a state of subcooled liquid. The multi-stage vaporization
process also includes combining the intermediate pressure lean
basic solution stream (S2) and a vapor second rich stream (S19)
corresponding to a state of saturated vapor producing an
intermediate pressure, rich basic solution stream (S3)
corresponding to a state of saturated liquid, where the
intermediate pressure lean basic solution stream (S2) fully absorbs
the vapor second rich stream (S19) and a composition of the
intermediate pressure, rich basic solution stream (S3) is richer
than a composition of the lean basic solution streams. The
multi-stage vaporization process also includes pressurizing the
intermediate pressure, rich basic solution stream (S3) in a
circulating or second pump (P2) producing a higher pressure, rich
basic solution stream (S4) corresponding to a state of subcooled
liquid. The multi-stage vaporization process also includes dividing
the higher pressure, rich basic solution stream (S4) into a first
higher pressure, rich basic solution substream (S20) and the second
higher pressure, rich basic solution substream (S23). The
multi-stage vaporization process also includes separating the
partially vaporized, second higher pressure, rich basic solution
substream (S25) in a third gravity separator (SP3) producing the
liquid third lean stream (S26) and a vapor third rich stream (S46),
where a composition of the third lean stream (S26) is leaner than a
composition of the rich basic solution substreams. The multi-stage
vaporization process also includes separating the heated third lean
stream (S5) in a first gravity separator (SP1) producing a
saturated vapor first rich stream (S6) and a saturated liquid first
lean stream (S7). The multi-stage vaporization process also
includes if the spent combined working solution stream is in a
state of slightly superheated vapor, dividing the saturated liquid
first lean stream (S7) into a first saturated liquid first lean
substream (S70) and a second saturated liquid first lean substream
(S10) and pressure adjusting the second saturated liquid first lean
substream (S70) in a second throttle-valve (TV2) producing the
second pressure adjusted, first lean substream (S71). The
multi-stage vaporization process also includes pressure adjusting
the first saturated liquid first lean substream (S10) or the
saturated liquid first lean stream (S7) in a third throttle valve
(TV3) producing an intermediate pressure first lean substream (S30)
or an intermediate pressure saturated first lean stream (S30)
corresponding to a state of a liquid-vapor mixture. The multi-stage
vaporization process also includes separating the intermediate
pressure first lean substream (S30) or the intermediate pressure
saturated first lean stream (S30) in a second gravity separator
(SP2) producing the saturated vapor rich stream (S19) and a
saturated liquid, intermediate pressure, lean working solution
stream (S11). The multi-stage vaporization process also includes
dividing the saturated liquid, intermediate pressure, lean working
solution stream (S11) into a saturated liquid, intermediate
pressure, lean working solution substream (S12) and the saturated
liquid lean, intermediate pressure, working solution stream (S49).
The multi-stage vaporization process also includes pressure
adjusting the saturated liquid, intermediate pressure, lean working
solution substream (S12) in a fourth throttle valve (TV4) producing
the pressure adjusted lean working solution substream (S13). The
multi-stage vaporization process also includes combining the
saturated vapor first rich stream (S6) and the vapor third rich
stream (S46) producing a combined vapor rich stream (S45). The
multi-stage vaporization process also includes transferring heat
from the combined vapor rich stream (S45) in a sixth heat exchange
unit or heat exchanger (HE6) in counterflow to an intermediate
pressure rich working solution stream (S28) producing a cooled and
partially condensed, combined rich stream (S44) corresponding to a
state of a vapor-liquid mixture and a heated intermediate pressure
rich working solution stream (S29). The multi-stage vaporization
process also includes combining the cooled and partially condensed,
combined rich stream (S44) and the first higher pressure rich basic
solution substream (S20) producing a rich working solution stream
(S21) corresponding to a state of a liquid-vapor mixture. The
multi-stage vaporization process also includes condensing the rich
working solution stream (S21) in a condenser or fourth heat
exchange unit or heat exchanger (HE4) in counterflow to a second
higher pressure coolant substream (S53) producing a spent coolant
substream (S55) and a condensed rich working solution stream (S27)
corresponding to a state of saturated liquid. The multi-stage
vaporization process also includes pressurizing the condensed rich
working solution stream (S27) in a booster or third pump (P3)
producing the intermediate pressure rich working solution stream
(S28) corresponding to a state of subcooled liquid.
[0033] In certain embodiments of this invention, the methods
further comprise pressurizing an initial external coolant stream
(S50) in a circulating pump (CP) producing a higher pressure
external coolant stream (S51), and dividing the higher pressure
external coolant stream (S51) into a first higher pressure external
coolant substream (S52) and a second higher pressure external
coolant substream (S53).
[0034] In other embodiments of this invention, the streams comprise
a multi-component working fluid. In other embodiments of this
invention, the single multi-component working fluid at least one
lower boiling point component and at least one higher boiling point
component. In other embodiments of this invention, the single
multi-component fluid is selected from the group consisting of a
ammonia-water mixture, a mixture of two or more hydrocarbons, a
mixture of two or more freon, a mixture of hydrocarbons and freons,
and mixtures thereof. In other embodiments of this invention, the
single multi-component fluid comprises a mixture of water and
ammonia.
Suitable Reagents and Equipment
[0035] The working fluid used in the systems of this invention are
multi-component fluids comprising a lower boiling point component
and a higher boiling point component. Suitable multi-components
fluids include, without limitation, ammonia-water mixtures,
mixtures of two or more hydrocarbons, mixtures of two or more
freon, mixtures of hydrocarbons and freons, or mixtures thereof. In
general, the fluid may comprise mixtures of any number of compounds
with favorable thermodynamic characteristics and solubility. In
certain embodiments, the multi-component fluid comprises a mixture
of water and ammonia.
[0036] It should be recognized by an ordinary artisan that at those
points in the systems of this invention were a stream is split into
two or more sub-streams, dividing valves that affect such stream
splitting are well known in the art and may be manually adjustable
or dynamically adjustable so that the splitting achieves the
desired stream flow rates and system efficiencies. Similarly, when
stream are combined, combining valve that affect combining are also
well known in the art and may be manually adjustable or dynamically
adjustable so that the splitting achieves the desired stream flow
rates and system efficiencies. The combining and dividing value may
also include flow controllers and sensors for determining stream
parameters including, without limitation, temperature, pressure,
composition, boiling point, etc.
DETAILED DESCRIPTION OF THE DRAWINGS OF THE INVENTION
General System
[0037] Referring now to FIG. 1, a general embodiment of a power
system of this invention, generally PS, designated SBC-19, is shown
to include a vaporization subsystem (VPSS), an energy conversion
subsystem (ECSS), and a distillation condensation subsystem
(DCSS-50). A fully condensed rich working solution stream RWFS and
a fully condensed lean working solution stream LWSS are produced in
the DCSS-50 and forwarded to the VPSS. Heat from a heat source
stream HSS is used to heat and fully vaporize the RWFS and the LWFS
producing a fully vaporized combined working solution stream CWSS
and a spent heat source stream SHSS. The CWSS then is forwarded to
the ECSS, where a portion of heat associated with the CWSS is
converted into a useable form of energy producing a spent working
fluid stream SCWSS. The SCWSS is then forwarded to the DCSS-50,
where the SCWFS is distilled and condensed using an external
coolant stream (ECS) producing the RWFS and the LWFS and a spent
external coolant stream (SECS), which are then forwarded separately
to the VPSS, closing the system. All of the streams are derived
from a single multi-component fluid. In the DCSS-50, a multi-stage
distillation and condensation process is used to form the RWSS and
the LWSS and the SECS using variable composition streams derived
from the SCWSS and the ECS. In the VPSS, a multi-stage vaporization
process is used to fully vaporize and superheat the RWSS and LWSS
to form the CWSS so that each lean working solution stream remains
in a state of subcooled liquid prior to being mixed with the RWSS
or one or more intermediate solution streams derived from the RWSS
and all or portions of the LWSS to maximize heat transfer from the
HSS producing a fully vaporized and superheated CWFS and the
SHSS.
Specific Embodiment of Complete System
[0038] Referring now to FIG. 2, an intermediate pressure rich
working solution stream S29 having parameters as at a point 29 and
an intermediate pressure lean working solution stream S49 having
parameters as at a point 49 exit the distillation condensation sub
system (DCSS-50). The intermediate pressure rich working solution
stream S29 has a higher concentration of a low-boiling component of
a multi-component working fluid, while the intermediate pressure
lean working solution stream S49 has a lower concentration of the
low-boiling component of the multi-component fluid.
[0039] The streams S29 and S49 are now sent into two feed pumps P5
and P6, respectively, where their pressure is increased producing a
higher pressure rich working solution stream S100 having parameters
as at a point 100 and a higher pressure lean working solution
stream S110 having parameters as at a point 110. For optimized
operation, temperatures of the rich working solution stream S100
and the lean working solution stream S110 must be equal or
substantially equal. Both streams S100 and S110 correspond to a
state of subcooled liquid.
[0040] The streams S100 and S110 now enter into a heat recovery
vapor generator (HRVG) also referred to herein as a seventh heat
exchange unit or exchanger HE7. The rich working solution stream
S100 and the lean working solution stream S110 flow through their
own pipes into the HRVG/HE7, and are not mixed together, but become
mixed in stages prior to exiting the HRVG/HE7.
[0041] Inside the HRVG/HE7, the rich working solution stream S100
and the lean working solution stream S110 are heated in counterflow
with an initial heat source stream S500 having parameters as at a
point 500 in a multi-stage heat exchange process
500-501-502-503-504-505-506 producing a spent heat source stream
S506 having parameters as at a point 506 as described below and a
fully vaporized and superheated combined working solution stream
S116 having parameters as at a point 116.
[0042] At first, in a low-temperature portion 505-506 of the heat
exchange process 500-501-502-503-504-505-506, heat from a fifth
cooled heat source stream S505 having parameters as at parameters
as at a point 505 is used to heat the streams S100 and S110 up to a
temperature producing a heated rich working solution stream S101
having parameters as at a point 101 and a heated lean working
solution stream S111 having parameters as at a point 111. A
temperature of the heated rich working solution stream S101
corresponds to its boiling point, while a temperature of the lean
working solution stream S111 is the same, but still corresponds to
a state of subcooled liquid.
[0043] Thereafter, in another portion 504-505 of the multi-stage
heat exchange process 500-501-502-503-504-505-506, heat from a
fourth cooled heat source stream S504 having parameters as at
parameters as at a point 504 is used to heat the heated streams
S101 and S111 producing a further heated rich working solution
stream S102 having parameters as at a point 102 and a further
heated lean working solution stream S112 having parameters as at a
point 112. The further heated rich working solution stream S102 is
now boiling and is partially vaporized and corresponds to a state
of a vapor-liquid mixture, while the further heated lean working
solution stream S112 still corresponds to a state of subcooled
liquid.
[0044] The stream S112 is now divided into two substreams S113 and
S122 having parameters as at points 113 and 122, respectively. Note
that pressures of the stream S112 and the substreams S113 and S122
are slightly higher than a pressure of the stream S102.
[0045] The substream S122 is now mixed with the stream S102
producing a first intermediate solution stream S103 having
parameters as at a point 103 corresponding to a state of a
vapor-liquid mixture.
[0046] As a result of this mixing, a substantial portion of the
vapor in the stream S102 is absorbed by the substream S122, which
is in a state of subcooled liquid. As a result, a temperature of
the first intermediate solution stream S103 is increased and
becomes equal to a temperature of the substream S113. Temperatures
of the stream S112 and substreams S113 and S122, as well as a flow
rate of the substream S122, are selected in such a way so as to
make a temperature of the stream S103 equal to the temperatures of
the stream S112 and the substream S113.
[0047] Now, in another portion 503-504 of the multi-stage heat
exchange process 500-501-502-503-504-505-506, heat from a third
cooled heat source stream S503 having parameters as at parameters
as at a point 503 is used to heat the first intermediate solution
stream S103 and the lean working solution substream S113 producing
a heated first intermediate solution stream S104 having parameters
as at a point 104 and a heated lean working solution substream S114
having parameters as at a point 114. The stream S104 is partially
vaporized, while the substream S114 is heated to a temperature that
is higher than a temperature of the stream S104. The substream S114
continues to remain in a state of subcooled liquid.
[0048] Thereafter heated lean working solution substream S114 is
then divided into two substreams S115 and S124 having parameters as
at points 115 and 124, respectively.
[0049] The heated lean working solution substream S124
(corresponding to a state of subcooled lean liquid) is now mixed
with the heated first intermediate solution stream S104
(corresponding to a state of a vapor-liquid mixture) producing a
second intermediate solution stream S105 having parameters as at a
point 105, corresponding to a state of a vapor-liquid mixture with
a concentration and is leaner than the first intermediate solution
stream S104.
[0050] As before, as a result of this mixing, a substantial portion
of the vapor in the first intermediate solution stream S104 is
absorbed by the heated lean working solution substream S124, which
is in a state of subcooled liquid. As a result, a temperature of
the second intermediate solution stream S105 is increased and
becomes equal to a temperature at the heat lean working solution
substream S115.
[0051] In another portion 502-503 of the multi-stage heat exchange
process 500-501-502-503-504-505-506, heat from a second cooled heat
source stream S502 having parameters as at parameters as at a point
502 is used to heat the second intermediate solution stream S105
and the lean working solution substream S115 producing a heated
second intermediate solution stream S106 having parameters as at a
point 106 and a further heated lean working solution substream S126
having parameters as at a point 126. This heating causes the stream
S105 to be further partially vaporized forming the stream S106. A
temperature the substream S126 is higher than a temperature the
stream S106, but as before, due to the lean composition of the
substream 126, it remains in a state of subcooled liquid.
[0052] At this point, the further heated lean working solution
substream S126 and the heated second intermediate solution stream
S106 are combined, forming a combined working solution stream S107
having parameters as at a point 107, corresponding to a state of a
liquid-vapor mixture.
[0053] Once more, as a result of this mixing, a substantial portion
of the vapor in the heat second intermediate solution stream S106
is absorbed by the further heated lean working solution stream
S126, which is in a state of subcooled liquid. As a result, a
temperature of the combined working solution stream S107 is
increased and becomes equal to a temperature the further heated
lean working solution stream S126.
[0054] A total flow rate the combined working solution stream S107
is equal a sum of flow rates of the rich working solution stream
S100 and the lean working solution stream S110 as described below.
A composition of the combined working solution stream S107 is
referred to as the combined working solution composition.
[0055] Now, in another portion 501-502 of the multi-stage heat
exchange process 500-501-502-503-504-505-506, heat from a first
cooled heat source stream S501 having parameters as at a point 501
is used to heat the combined working solution stream S107, which
fully vaporizes producing a fully vaporized combined working
solution stream S108 having parameters as at a point 108,
corresponding to a state of saturated vapor.
[0056] Thereafter, in another portion 500-501 of the multi-stage
heat exchange process 500-501-502-503-504-505-506, heat from the
initial heat source stream S500 is used to heat the fully vaporized
combined working solution stream S108, which is superheated
producing a superheated, fully vaporized combined working solution
stream S116 having parameters as at a point 116, corresponding to a
state of superheated vapor.
[0057] This multi-stage process 500-501-502-503-504-505-506 of heat
transfer means that the boiling process begins at point 101,
capturing the low-temperature heat of the heat source and cooling
the heat source to a temperature as at the point 506. The boiling
temperature of the stream S101 is much lower than the boiling point
of the working solution would be, had it not been divided into lean
and rich streams. Thus, if the working fluid had not been so
divided, much less heat could have been absorbed by the divided
lean and rich streams from the heat source stream or transferred
from the heat source stream to the divided lean and rich
streams.
[0058] In the same manner, the further stages of vaporization,
controlled by the mixing of working solution streams inside the
HRVG/HE7, allow for the capture of the mid-temperature and last the
high temperature portions of the heat of the heat source
stream.
[0059] Returning to the system, the superheated, fully vaporized
combined working solution stream S116 is now sent into an admission
throttle-valve TV1, where its pressure may be slightly reduced (in
order to make sure the inlet pressure to the turbine remains
stable) producing a pressure adjusted superheated, fully vaporized
combined working solution stream S117 having parameters as at a
point 117, corresponding to a state of superheated vapor.
[0060] The pressure adjusted superheated, fully vaporized combined
working solution stream S117 is now sent into a turbine Ti, where
it is expanded, producing useable work (mechanical and/or
electrical) producing a spent combined working solution stream S118
having parameters as at a point 118. In most cases, the parameters
of the stream S118 will correspond to a state of slightly
superheated vapor. However, it is possible that the parameters the
stream S118 will correspond instead to a state of saturated
vapor.
[0061] Looking back now to the heat source stream, the initial heat
source stream S500 having the parameters as at the point 500,
enters into the system and into the HRVG/HE7, where it provides
heat for a heat exchange process 108-116, as described above,
producing the first cooled heat source stream S501 having the
parameters as at the point 501. The first cooled heat source stream
S501 now provides heat for a heat exchange process 107-108, as
described above, producing the second cooled heat source stream
S502 having the parameters as at point 502. The second cooled heat
source stream S502 now provides heat for heat source processes
105-106 and 115-126, as described above, producing the third cooled
heat source stream S503 having the parameters as at the point 503.
The third cooled heat source stream S503 now provides heat for heat
exchanges processes 103-104 and 113-114, as described above,
producing the fourth cooled heat source stream S504 having the
parameters as at point 504. The fourth cooled heat source stream
S504 now provides heat for heat exchange processes 101-102 and
111-112, as described above, producing the fifth cooled heat source
stream S505 having the parameters as at point 505. The fifth cooled
heat source stream S505 now provides heat for heat exchange
processes 100-101 and 110-111, as described above, producing the
spent heat source stream S506 having the parameters as at the point
506, exiting the HRVG/HE7 and the system.
[0062] The spent combined working solution stream S118 must now be
condensed and re-divided into the rich working solution stream S29
and the lean working solution stream S49. In order to do this, a
distillation condensation sub system (DCSS-50) is employed.
Specific Embodiment of DCSS-50
[0063] Referring now to FIG. 3, the DCSS-50 is shown operates as
follows.
[0064] The spent combined working solution stream S118
corresponding to a state of saturated or slightly superheated
vapor, enters into the DCSS-50. If the combined working solution
stream S118 is in a state of slightly superheated vapor, it is now
mixed with a pressure adjusted second SP1 lean substream S71 having
parameters as at a point 71, as described below, producing a
saturated vapor intermediate solution stream S38 having parameters
as at a point 38. If on the other hand, the combined working
solution stream S118 is in a state of saturated vapor, then the
pressure adjusted second SP1 lean substream S71 has a flow rate of
zero and the parameters of the intermediate solution stream S38 are
the same as the parameters of the combined working solution stream
S118.
[0065] Either the saturated vapor intermediate solution stream S38
or the combined working solution stream S118 is now sent into a
third heat exchange unit or exchanger HE3, where it is cooled and
partially condensed in counterflow in a heat exchange process 26-5
or 38-15 with a liquid SP3 lean stream S26 having parameters as at
a point 26 producing a cooled and partially condensed intermediate
solution stream S15 having parameters as at a point 15
corresponding to a state of a liquid-vapor mixture and a heated and
partially vaporized SP3 lean stream S5 having parameters as at a
point 5 corresponding to a state of a liquid-vapor mixture.
[0066] The cooled and partially condensed intermediate solution
stream S15 is now sent into a second heat exchange unit or heat
exchanger HE2, where it is further cooled in counterflow with a
second higher pressure rich basic solution substream S23 having
parameters as at a point 23 in a heat exchange process 15-40-41 or
23-24-25 producing a further cooled and partially condensed
intermediate solution stream S41 having parameters as at a point 41
corresponding to a state of a vapor-liquid mixture and a heated
higher pressure rich basic solution substream S25 having parameters
as at a point 25 as described below.
[0067] The further cooled and partially condensed intermediate
solution stream S41 is then mixed with a pressure adjusted SP2 lean
working solution substream S13 having parameters as at point 13, as
described below, producing a lean basic solution stream S42 having
parameters as at a point 42. A composition of the lean basic
solution stream S42 is substantially leaner than a composition of
the intermediate solution streams S38, S15, S40, and S41 and the
combined working solution stream S118. The leaning of the
intermediate solution stream S41 to produce the lean basic solution
stream S42 allows for a full condensation of the lean basic
solution stream S42 at a low pressure using an external coolant
stream as described below.
[0068] The lean basic solution stream S42 is now sent into a
condenser or first exchange unit or heat exchanger HE1, where it is
fully condensed in counterflow with a first higher pressure
external coolant substream S52 having parameters as at a point 52
in a heat exchange process 42-1 or 52-54 producing by a fully
condensed lean basic solution stream S1 having parameters as at a
point 1 and a spent external coolant substream S54 having
parameters as at a point 54 as described below.
[0069] The fully condensed lean basic solution stream S1 is now
pumped to an intermediate pressure by a feed or first pump P1
producing an intermediate pressure lean basic solution stream S2
having parameters as at a point 2 corresponding to a state of
subcooled liquid.
[0070] The intermediate pressure lean basic solution stream S2 is
now mixed with a vapor SP2 rich stream S19 having parameters as at
a point 19 corresponding to a state of rich saturated vapor as
described below producing a rich basic solution stream S3 having
parameters as at a point 3 corresponding to a state of saturated
liquid.
[0071] The intermediate pressure lean basic solution stream S2
corresponding to a state of subcooled liquid fully absorbs the
vapor SP2 rich stream S19 producing the rich basic solution stream
S3. Therefore, a composition of the rich basic solution stream S3
is richer than the composition of the lean basic solution streams
S42, S1, and S2.
[0072] The rich basic solution stream S3 is now sent into a
circulating or second pump P2, where its pressure is increased
producing a higher pressure rich basic solution stream S4 having
parameters as at point 4 corresponding to a state of subcooled
liquid.
[0073] The higher pressure rich basic solution stream S4 is now
divided into a first higher pressure rich basic solution substream
S20 and the second higher pressure rich basic solution substream
S23 having parameters as at points 20 and 23, respectively.
[0074] The second higher pressure rich basic solution substream S23
is now sent into the second heat exchanger HE2 in the heat exchange
process 15-40-41 or 23-24-25 as described above. In the second heat
exchanger HE2, the second higher pressure rich basic solution
substream S23 reaches its boiling point temperature producing a
boiling second higher pressure rich basic solution substream S24 as
at a point 24, which also corresponds to a temperature of the
condensing intermediate solution stream S40 having parameters as at
a point 40, and then as it flows through the remainder of the
second heat exchanger HE2, the second higher pressure rich basic
solution substream S23 is partially vaporized producing a partially
vaporize, higher pressure rich basic solution substream S25 having
parameters as at a point 25 corresponding to a state of a
vapor-liquid mixture.
[0075] The partially vaporized, higher pressure rich basic solution
substream S25 is now sent into a third gravity separator SP3, where
it separated into the saturated liquid SP3 lean stream S26 having
the parameters as at the point 26 and a saturated vapor SP3 rich
stream S46 having parameters as at a point 46. Note, that a
composition of the SP3 lean stream S26 is leaner than a composition
of the rich basic solution substream S25.
[0076] The saturated liquid SP3 lean stream S26 is now sent into
the third heat exchanger HE3, where it is heated and partially
vaporized in counterflow with the intermediate solution stream S38
in the heat exchange process 38-15 or 26-5 as described above
producing the heated SP3 lean stream S5 having the parameters as at
the point 5, corresponding to a state of a liquid-vapor
mixture.
[0077] The heated SP3 lean stream S5 is now sent into a first
gravity separator SP1, where it is separated into a saturated vapor
SP1 rich stream S6 having parameters as at a point 6, and a
saturated liquid SP1 lean stream S7 having parameters as at a point
7.
[0078] The saturated liquid SP1 lean stream S7 is now divided into
a saturated liquid first SP1 lean substream S10 having parameters
as at a point 10 and a saturated liquid second SP1 lean substream
S70 having parameters as at a point 70, if needed as described
above.
[0079] The saturated liquid second SP1 lean substream S70 is now
sent through a second throttle-valve TV2, where its pressure is
reduced to a pressure equal to the pressure of the combined working
solution stream S118 producing the pressure adjusted second SP1
lean substream S71 having the parameters as at the point 71, before
being mixed with the combined working solution stream S118, forming
the intermediate solution stream S38, as described above.
[0080] Meanwhile, the saturated liquid first SP1 lean substream S10
is sent through a third throttle valve TV3, where its pressure is
reduced to an intermediate pressure producing an intermediate
pressure first SP1 lean substream S30 having parameters as at a
point 30, corresponding to a state of a liquid-vapor mixture.
[0081] The intermediate pressure first SP1 lean substream S30 is
now sent into a second gravity separator SP2, where it is separated
into the saturated vapor SP2 rich stream S19 having the parameters
as at the point 19 as described above and a saturated liquid lean
working solution stream S11 having parameters as at a point 11. A
composition of the stream S11 is the same as a composition of the
intermediate pressure lean working solution stream S49 in the main
system as described above and referred to as the lean working
solution.
[0082] Meanwhile, the saturated vapor SP1 rich stream S6 exiting
the first gravity separator SP1 is combined with the vapor SP3 rich
stream S46 as described above producing a combined vapor rich
stream S45 having parameters as at a point 45.
[0083] The combined vapor rich stream S45 is now sent into a sixth
heat exchange unit or heat exchanger HE6, where it is cooled and
partially condensed in counterflow with an intermediate pressure
rich working solution stream S28 having parameters as at a point 28
in a heat exchange process 45-44 or 28-29 producing a cooled and
partially condensed, combined rich stream S44 having parameters as
at a point 44, corresponding to a state of a vapor-liquid
mixture.
[0084] The cooled and partially condensed, combined rich stream S44
is now mixed with the first higher pressure rich basic solution
substream S20 as described above producing a rich working solution
stream S21 having parameters as at a point 21 corresponding to a
state of a liquid-vapor mixture. The rich working solution stream
S21 has a composition that is the same as the composition of the
intermediate pressure rich working solution stream S29 in the main
system as described above and referred to as the rich working
solution.
[0085] The rich working solution stream S21 is now sent into a
condenser or fourth heat exchange unit or heat exchanger HE4, where
it is fully condensed in counterflow with a second higher pressure
coolant substream S53 having parameters as at a point 53 in a heat
exchange process 53-55 or 21-27 producing a spent coolant substream
S55 having a parameter as a point 55 and a condensed rich working
solution stream S27 having parameters as at a point 27
corresponding to a state of saturated liquid.
[0086] The condensed rich working solution stream S27 is now pumped
by a booster or third pump P3 to an increased pressure producing
the intermediate pressure rich working solution stream S28 having
the parameters as at the point 28 corresponding to a state of
subcooled liquid.
[0087] The intermediate pressure rich working solution stream S28
is then sent into the sixth heat exchanger HE6, where it provides
heat for the heat exchange process 45-44 or 28-29 as described
above producing the heated rich working solution S29 having the
parameters as at the point 29, corresponding to a state of a
subcooled liquid, prior to exiting the DCSS-50 and returning to the
main system.
[0088] Meanwhile, the lean working solution stream S11 exiting the
second gravity separator SP2 is divided into the lean working
solution stream S49 having the parameters as at the point 49 and a
lean working solution substream S12 having parameters as at a point
12.
[0089] The intermediate pressure lean working solution stream S49
is then sent out of the DCSS-50 and back into the main system as
described above. A temperature at lean working solution stream S49
determines a desired temperature of the intermediate pressure rich
working solution stream S29 as described above. The two
temperatures should be equal or substantially equal, so as to allow
the temperatures of the rich working solution stream S100 and the
lean working solution stream S110 of the main system to be equal or
substantially equal or as close to equal as possible.
[0090] Meanwhile, the lean working solution substream S12 is sent
through a fourth throttle-valve TV4, where its pressure is reduced
to a pressure equal to a pressure of the intermediate solution
stream S41 producing the pressure adjusted lean working solution
substream S13 having parameters as at the point 13. The pressure
adjusted lean working solution substream S13 is now mixed with the
intermediate solution stream S41 producing the lean basic solution
stream S42 as described above.
[0091] Meanwhile, looking at the initial external coolant stream
S50 having the parameter as at the point 50 comprising cooling
water, is pumped by a circulating pump CP to increase a pressure of
the coolant producing a higher pressure external coolant stream S51
having the parameter as at the point 51. The higher pressure
coolant stream S51 is then divided into the first higher pressure
coolant substream S52 and the second higher pressure coolant
substream S53 having parameters as at points 52 and 53.
[0092] The first higher pressure coolant substream S52 is then sent
into the first heat exchanger HE1, cooling and fully condensing the
lean basic solution stream S42 in the heat exchange process 42-1 or
52-54 as described above producing a spent coolant stream S54
before exiting the system.
[0093] Meanwhile, the second higher pressure coolant substream S53
is sent into the fourth heat exchanger HE4, cooling and fully
condensing the rich working solution stream S27 in the heat
exchange process 21-27 or 53-55 as described above producing the
spent coolant stream S55 having parameters as at the point 55
before exiting the system.
[0094] Note that compositions of the lean basic solution streams
S42, S1 and S2 are leaner than the composition of the spent
combined working solution stream S118, the combined working
solution composition. This leaning of these streams allows a
pressure of the lean basic solution stream S1 (and correspondingly
the spent combined working solution stream S118) to be
substantially lower that it would be if the spent combined working
solution stream S118 were to be condensed directly. This means a
lower back pressure on the turbine T1 and thus an increased power
output from the main system.
TABLE-US-00001 Streams Compositions S118 combined working solution
S38, S15, S40 & S41 intermediate solution S42, S1 & S2 lean
basic solution S26 & S5 SP3 lean S7, S10, S30, S70 & S71
SP1 lean S11, S12, S13 & S49 lean working solution S6 SP1 rich
S19 SP2 rich S46 SP3 rich S45 & S44 combined rich vapor S3, S4,
S20, S23 & S25 rich basic solution S21, S27, S28 & S29 rich
working solution
Computation and Analysis of System
[0095] Computation and analysis of the present system has shown
that, if used as a bottoming cycle for a gas turbine (which means
that the temperature of the initial heat source stream S500 is
quite high), then the present system will be a few percent less
efficient than a triple-pressure Rankine cycle system bottoming
cycle. The present system will, however, substantially out perform
a dual-pressure Rankine cycle system bottoming cycle. However since
the present system uses only a single turbine, it will be
considerably less expensive in terms of capital cost than either a
dual or triple-pressure Rankin cycle system and the cost per
delivered kilowatt for the present system should be substantially
lower than either a dual or triple-pressure Rankine cycle system
bottoming cycle.
[0096] Moreover, the present system out performs both dual and
triple-pressure Rankine cycle system bottoming cycles outright in
cases, where a temperature of the initial heat source stream S500
is somewhat lower, while maintaining its economic advantage.
[0097] Assuming the use of a full exhaust of a GE 9FB gas turbine
as the initial heat source stream S500, a triple-pressure Ranking
cycle system bottoming cycle will deliver 155,080 kW. In
comparison, the present system, with the same heat source stream,
will deliver 151,153 kW. Thus the present system will deliver
approximately 97.5% of the output of the Ranking cycle system
bottoming cycle system, but using only a single turbine to the
Rankine system's three turbines (for an estimated cost that should
be roughly half as much or less of the Rankine system's cost.)
[0098] The present system described above has been shown using
three stages of mixing inside the HRVG/HE7, however, depending on
the parameters (initial temperature and/or the chosen pressure at
the turbine inlet) of the heat source stream S500 used, it is
possible for the system to operate with only two stages of mixing
inside the HRVG/HE7 as shown in FIG. 2B, or even with just a single
stage of mixing inside the HRVG/HE7 and shown in FIG. 2C. In FIG.
2B, the streams S114, S115, S124, S104, and S105 are missing. In
FIG. 2C, the streams S112, S113, S122, S102, S103, S114, S115,
S124, S104, and S105. In both FIG. 2B and FIG. 2C, the exact
location of the mixing stages will depend on the initial heat
source stream used.
[0099] In all cases, however, it is necessary that the lean working
solution stream or streams at the point where it is or they are
mixed be in a state of a subcooled saturated liquid. At the same
time, the rich working solution streams S100 and S101 and the
intermediate streams S103, S104, S105 and S106 must be in a state
of a vapor-liquid mixture, or a saturated vapor.
[0100] One experienced in the art can select the correct number of
mixing stages inside the HRVG/HE7.
[0101] All references cited herein are incorporated by reference.
Although the invention has been disclosed with reference to its
preferred embodiments, from reading this description those of skill
in the art may appreciate changes and modification that may be made
which do not depart from the scope and spirit of the invention as
described above and claimed hereafter.
* * * * *