U.S. patent application number 10/146008 was filed with the patent office on 2003-11-20 for condenser staging and circuiting for a micro combined heat and power system.
Invention is credited to Anson, Donald, Hanna, William T., Osborne, Rodney L..
Application Number | 20030213248 10/146008 |
Document ID | / |
Family ID | 29418721 |
Filed Date | 2003-11-20 |
United States Patent
Application |
20030213248 |
Kind Code |
A1 |
Osborne, Rodney L. ; et
al. |
November 20, 2003 |
Condenser staging and circuiting for a micro combined heat and
power system
Abstract
A micro combined heat and power system includes at least a heat
source, an expander, a pump, a staged, counterflow condenser and a
conduit for transporting a working fluid. The heat source can be,
for example, a burner, while the expander is preferably a scroll
expander. The heat source superheats the working fluid, which is
preferably an organic working fluid. The superheated organic
working fluid passes through the expander, which is coupled to a
generator to produce electricity. After the working fluid is
expanded, its gives up at least a portion of its excess heat first
to the condenser. By placing the condenser in a counterflow
arrangement, the fluid receiving the heat from the condensing
working fluid can be of a higher temperature, thus allowing more
system variation in the heat to power output ratio. The fluid
receiving heat from the condenser may include circulating air,
water or related fluid to provide space heat or domestic hot
water.
Inventors: |
Osborne, Rodney L.; (Hebron,
OH) ; Hanna, William T.; (Gahanna, OH) ;
Anson, Donald; (Worthington, OH) |
Correspondence
Address: |
Killworth, Gottman, Hagan & Schaeff, L.L.P.
Suite 500
One Dayton Centre
Dayton
OH
45402-2023
US
|
Family ID: |
29418721 |
Appl. No.: |
10/146008 |
Filed: |
May 15, 2002 |
Current U.S.
Class: |
60/670 ;
60/671 |
Current CPC
Class: |
F28D 9/00 20130101; F28F
9/0275 20130101; F28B 11/00 20130101; Y02E 20/14 20130101; F01K
17/02 20130101; F28D 7/08 20130101; F28D 7/085 20130101; F28B 1/02
20130101 |
Class at
Publication: |
60/670 ;
60/671 |
International
Class: |
F01K 001/00; F01K
025/00 |
Claims
We claim:
1. A cogeneration system comprising: a heat source; a working fluid
circuit comprising: conduit configured to transport an organic
working fluid through said working fluid circuit, at least a
portion of said conduit disposed adjacent said heat source such
that said organic working fluid disposed in said portion of said
conduit is superheated during operation of said heat source; an
expander in fluid communication with said conduit such that said
organic working fluid received therefrom remains superheated after
expansion in said expander; a condenser in fluid communication with
said expander, said condenser configured such that a circulating
fluid medium passing therethrough is in counterflow relationship to
said organic working fluid; and a pump configured to circulate said
organic working fluid through at least said conduit, expander and
condenser; and at least one energy conversion circuit operatively
responsive to said working fluid circuit such that upon operation
of said cogeneration system, said at least one energy conversion
circuit is configured to provide useable energy.
2. A cogeneration system according to claim 1, wherein said
condenser is a flat plate condenser.
3. A cogeneration system according to claim 1, wherein said
condenser is a shell-and-tube condenser.
4. A cogeneration system according to claim 3, wherein the shell of
said shell-and-tube condenser is in fluid communication with said
working fluid circuit, and the tube is configured to be in fluid
communication with said circulating fluid medium.
5. A cogeneration system according to claim 1, wherein said at
least one energy conversion circuit comprises: a generator coupled
to said expander to produce electricity; and a circulating fluid
medium in thermal communication with said condenser such that at
least a portion of the heat given up by said organic working fluid
in said condenser provides increased thermal content to said
circulating fluid medium.
6. A cogeneration system according to claim 5, wherein said
expander is a scroll expander.
7. A cogeneration system according to claim 5, wherein said
circulating fluid medium is configured to transport a space heating
fluid.
8. A cogeneration system according to claim 7, wherein said space
heating fluid is water.
9. A cogeneration system according to claim 7, wherein said space
heating fluid is forced air.
10. A cogeneration system according to claim 5, wherein said
circulating fluid medium is configured to transport domestic hot
water.
11. A cogeneration system according to claim 1, wherein said heat
source is a burner.
12. A Rankine cycle cogeneration system comprising: an organic
working fluid; an evaporator capable of superheating said organic
working fluid, said evaporator comprising: a burner; and conduit
adjacently spaced relative to said burner such that during burner
operation heat transferred therefrom is sufficient to superheat
said organic working fluid disposed in said conduit; a
substantially closed-loop working fluid circuit in thermal
communication with said burner, said substantially closed-loop
working fluid circuit configured to transport said organic working
fluid therethrough, said substantially closed-loop working fluid
circuit comprising: an expander in fluid communication with said
conduit such that said organic working fluid received therefrom
remains superheated after expansion in said expander; a condenser
in fluid communication with said expander; a pump configured to
circulate said organic working fluid through at least said conduit,
expander and condenser; and at least one energy conversion circuit
comprising: a generator coupled to said expander to produce
electricity; and a circulating fluid medium configured to pass
through said condenser in counterflow thermal communication with
said organic working fluid such that at least a portion of the heat
given up by said organic working fluid in said condenser provides
increased thermal content to said circulating fluid medium.
13. A dwelling configured to provide at least a portion of the heat
and power needs of occupants therein, said dwelling comprising: a
plurality of walls defining at least one room therebetween; a roof
situated above said plurality of walls; at least one ingress/egress
to facilitate passage into and out of said dwelling; and a
cogeneration system in heat and power communication with said at
least one room, said cogeneration system comprising: a heat source;
a working fluid circuit comprising: conduit configured to transport
an organic working fluid through said working fluid circuit, at
least a portion of said conduit disposed adjacent said heat source
such that said organic working fluid disposed in said portion of
said conduit disposed adjacent said heat source is superheated
during operation of said heat source; an expander in fluid
communication with said conduit such that said organic working
fluid received therefrom remains superheated after expansion in
said expander; a condenser in fluid communication with said
expander, said condenser comprising: a first loop configured to
convey said organic working fluid therethrough; and a second loop
in counterflow thermal communication with said first loop; and a
pump configured to circulate said organic working fluid through at
least said conduit, expander and condenser; a generator responsive
to said expander to provide electricity; and a circulating fluid
medium coupled to said second loop, said circulating fluid medium
configured to provide at least space heat or domestic hot water to
said dwelling.
14. A dwelling according to claim 13, further comprising a
controller responsive to occupant input.
15. A dwelling according to claim 14, wherein said controller
responsive to occupant input is a thermostat.
16. A dwelling according to claim 13, wherein said circulating
fluid medium is configured to provide both space heat and domestic
hot water to said dwelling.
17. A micro combined heat and power system comprising: an electric
production subsystem comprising: an organic working fluid; a burner
for superheating said organic working fluid; a scroll expander
configured to receive and expand said organic working fluid in a
superheated state; a generator operatively coupled to said scroll
expander to produce electricity; a condenser in fluid communication
with said scroll expander, said condenser comprising: a first loop
configured to convey said organic working fluid therethrough; and a
second loop in counterflow thermal communication with said first
loop; and a pump to circulate said organic working fluid through
said electricity generating loop; and a heat production subsystem
including a circulating fluid medium coupled to said second loop,
said circulating fluid medium configured to provide at least space
heat or domestic hot water to said dwelling.
18. A method of producing heat and electrical power from a
cogeneration device, the method comprising the steps of: providing
a heat source; configuring a first circuit to transport an organic
working fluid adjacent said heat source; superheating said organic
working fluid; expanding said superheated organic working fluid to
generate electricity; exchanging at least a portion of the excess
heat from said organic working fluid that has passed through said
expander in a condenser with a circulating fluid medium such that
after passing through said condenser, said organic working fluid is
no longer in a superheated state, said condenser comprising a first
loop configured to convey said organic working fluid therethrough,
and a second loop in counterflow thermal communication with said
first loop such that said second loop is in fluid communication
with said circulating fluid medium; and returning said organic
working fluid such that it is adjacent said heat source.
19. A method according to claim 18, wherein said circulating fluid
medium is configured to transport a space heating fluid.
20. A method according to claim 19, wherein said space heating
fluid is water.
21. A method according to claim 18, wherein said space heating
fluid is forced air.
22. A method according to claim 18, wherein said circulating fluid
medium is configured to transport domestic hot water.
23. A method according to claim 18, wherein said circulating fluid
medium is configured to transport both space heat and domestic hot
water.
Description
BACKGROUND OF THE INVENTION
[0001] The present invention generally relates to improvements in
operability of a Rankine cycle cogeneration system using an organic
working fluid, and more particularly to condenser configurations
integrated into such a system to increase system operability via
modulated cogeneration heat-to-power ratio.
[0002] The concept of cogeneration, or combined heat and power
(CHP), has been known for some time as a way to improve overall
efficiency in energy production systems. With a typical CHP system,
heat (usually in the form of hot air or water) and electricity are
the two forms of energy that are generated. In such a system, the
heat produced from a combustion process can drive an electric
generator, as well as heat up water, often turning it into steam
for dwelling or process heat. Traditionally, CHP systems have been
large, centrally-operated facilities under the control of the state
or a large utility company, sized to provide energy for many
thousands of users. If the region being served by the CHP has as
part of its infrastructure adequate heat transporting capability,
the centrally-generated heat and electric power model of the large
CHP system can, within limits, function reasonably efficiently and
reliably. In the absence of adequate heat transport capability,
however, while the region's electric power needs would continue to
be met by the central generating station, the heat needs would need
to be fulfilled separately and remotely from the electricity
production, often near or within the building housing the end-user.
This latter configuration typically includes the presence of one or
more boilers that could generate hot water or steam to provide most
or all of the localized building heating requirements. While either
configuration works well for its intended purpose, inefficiencies
arise. In the former system, much of the heat generated at the
central generating station is, after being transported over long
distances, unavailable for remote use. In the latter system, the
lack of CHP capability necessitates the consumption of additional
energy at the remote location to satisfy heat requirements.
[0003] Recent trends in the deregulation of energy production and
distribution have made viable the concept of distributed
generation. With distributed generation, the large, central
generating station is supplemented with, or replaced by numerous
smaller autonomous or semi-autonomous units. These changes have led
to the development of smaller CHP systems, called micro-CHP, which
are distinguished from traditional CHP by the size of the system.
By way of contrast, the electric output of a generating
station-sized CHP could be in the tens, hundreds or thousands of
megawatts (MW), where the electric output of a micro-CHP is fairly
small, in the low kW.sub.e or even sub-kW.sub.e range. The
inclusion of a distributed system into dwellings that already have
fluid-carrying pipes for heat transport is especially promising, as
little or no disturbance of the existing building structure to
insert new piping is required. Similarly, a micro-CHP system's
inherent multifunction capability can reduce structural redundancy.
Accordingly, the market for localized heat generation capability in
Europe and the United Kingdom (UK), as well as certain parts of the
United States, dictates that a single unit for residential and
small commercial sites provide heat for both space heat (SH), such
as a hydronic system with radiator, and domestic hot water (DHW),
such as a shower head or faucet in a sink or bathtub, via demand
(instantaneous) or storage systems.
[0004] As with all energy production devices that rely on
non-renewable sources, such as natural gas, coal or oil, a more
efficient system consumes lower quantities of fuel to au generate
the same energy output as its less efficient counterpart. A key
factor in keeping micro-CHP system efficiency high over a wide
range of operating conditions is how much thermal output is
required at the heat source, such as a natural gas burner.
Unfortunately, the nature of micro-CHP system operation, where both
electric power and heat are generated from the same combustion
process often under a fixed heat to power (Q/P) ratio, is such that
when thermal output is reduced to minimize fuel consumption, the
electric power production often drops even more quickly. As such,
these systems cannot operate efficiently when climatic changes and
user energy-consumption habits deviate significantly, over the
course of a day or the year, from the rated Q/P. With a fixed Q/P
heat-led system, because the electric power output follows heat
production, a significant turndown in thermal load results in a
concomitant loss in electric output, and because maximizing system
efficiency is typically a corollary to maximizing electric output,
such part power operation severely limits the benefits associated
with cogeneration systems.
[0005] What is needed is a micro-CHP system that can operate at
high efficiencies regardless of the Q/P requirements. The present
inventors have recognized that with modulation, the system
continues to operate over a longer period of time such that its
duty cycle is relatively large and that the variable heat output
need not encroach on maximizing electrical output. They have
further recognized that by modulating the system, Q/P is improved
at all conditions, especially at part power conditions. They have
also recognized that a modulation approach that varies the mass
flow of the working fluid to match the heat load while
simultaneously varying the fuel flow to the heat source in order to
keep the inlet temperature of the working fluid heated by the heat
source at a constant temperature results in a thermal output that
can be closely tailored to a user's needs while keeping electrical
power output at a maximum. They have moreover recognized that the
inclusion of various system componentry, such as staged condensers,
can improve the efficiency of modulating a system by the
aforementioned approach. They have additionally recognized that in
countries where emission requirements are stringent, modulating can
lower burner output at certain system operating conditions more
effectively than by cycling the system such that fuel consumption
to achieve the same amount of energy output is reduced.
BRIEF SUMMARY OF THE INVENTION
[0006] These needs are met by the present invention, where a
micro-CHP system with staged condenser is described. According to a
first aspect of the present invention, a cogeneration system
includes a heat source, a working fluid circuit and at least one
energy conversion circuit operatively responsive to the working
fluid circuit such that upon operation of the cogeneration system,
the energy conversion circuit provides useable energy. In the
present context, the term "useable energy" includes that which a
user can put to practical use, rather than waste or incidental
energy. This is consistent with the concept of cogeneration, which
is frequently considered to be the thermodynamically sequential
production of two or more useful forms of energy from a single
primary energy source. The most notable examples of useable energy
arising out of the operation of a cogeneration system are
electricity (preferably alternating current electricity, derived
from the mechanical turning of a generator), and heat in the form
of SH and DHW. The working fluid circuit is made up of at least
conduit, an expander, condenser and pump. The conduit is configured
to transport an organic working fluid, where at least a portion of
the conduit is disposed adjacent the heat source such that during
heat source operation, the heat transferred to the conduit is
sufficient to superheat the organic working fluid disposed in that
part of the conduit. The expander is in fluid communication with
the conduit such that the organic working fluid remains superheated
after expansion, while the condenser is in fluid communication with
the expander to extract some of the excess heat still extant in the
working fluid after the expansion process. The condenser is
configured as a counterflow unit, in which a primary heat exchange
loop (i.e., the loop carrying the fluid being cooled) thermally
interacts with a secondary heat exchange loop such that the
entrance of the primary loop is adjacent the exit of the secondary
loop, while the exit of the primary loop is adjacent the entrance
of the secondary loop. The counterflow arrangement enables the
highest possible outlet temperature of the circulating fluid
medium, which, as discussed below, could be DHW or hydronic fluid
for SH. The pump is configured to circulate the organic working
fluid through at least the conduit, expander and condenser.
[0007] The thermodynamic properties of some organic working fluids
are ideally suited to the temperature and pressure regimes
encountered in micro-CHP operation. Of particular interest is that
such fluids remain superheated even after giving up a significant
portion of their energy in the expansion process. This is in
contrast to other working fluids, such as water, that typically
condense to a saturated condition after expansion. Furthermore, the
use of organic working fluid rather than water is important where
shipping and even some end uses could subject portions of the
system to freezing temperatures (below 32.degree. Fahrenheit,
0.degree. Celsius). With a water-filled system, damage and
inoperability could ensue after prolonged exposure to sub-freezing
temperatures, whereas an organic working fluid-based system would
be impervious to temperature extremes encountered by dwellings and
related buildings incorporating such a system. In addition, by
using an organic working fluid rather than water, corrosion issues
germane to water in the presence of oxygen are avoided. The organic
working fluid is preferably either a halocarbon refrigerant or a
naturally-occurring hydrocarbon. Examples of the former include the
refrigerant known as R-245fa, while examples of the latter include
some of the alkanes, such as isopentane. Another advantage
associated with organic working fluids is that their high vapor
density and heat transfer properties in the superheated state
ensure that maximum heat and power can be extracted from the fluid
without having to resort to a large expander.
[0008] Optionally, the energy conversion circuit comprises a
generator coupled to the expander to produce electricity and a
circulating fluid medium in thermal communication with the
condenser such that at least a portion of the heat given up by the
organic working fluid in the condenser provides increased thermal
content to the circulating fluid medium. In the present context,
the term "thermal communication" is meant to broadly cover all
instances of thermal interchange brought about as a result of
coupling between system components, whereas the more narrow "heat
exchange communication" is meant to cover the more specific
relationship between direct, adjacent heat exchange components
designed specifically for that purpose. In addition, the expander
is preferably a scroll expander, while the condenser construction
facilitates the aforementioned counterflow arrangement. A flat
plate heat exchanger is one example of a condenser that can be run
in a counterflow arrangement, where each fluid enters a header from
opposite directions and splits into alternately-spaced parallel
streams. Another arrangement that can be run in a counterflow
arrangement is a shell-and-tube heat exchanger, where the working
fluid vapor enters the top of the shell and is directed by baffles
past the circulating fluid, which traverses the condenser through a
series of tubes, entering at or near the shell bottom and exiting
at or near the top in close proximity to the incoming working fluid
vapor.
[0009] A subcooling section in the condenser can be employed such
that if the condensate level of the organic working fluid is
maintained in the lower portion of the shell, the incoming
circulating fluid can cool this condensate below the saturation
temperature, which is necessary for pumping of the condensed
organic working fluid. This helps to keep the condensed working
fluid in liquid form which, if not for the additional subcooling,
could experience enough of a pressure drop in the pump inlet
section to flash back into vapor. This subcooling is also possible
in the previously discussed flat plate heat exchanger. There, the
superheated organic working fluid vapor enters the heat exchanger,
desuperheats, and then condenses as it gives up its heat to the
circulating fluid. As the circulating fluid is flowing counter to
the vapor, it can approach the temperature of the incoming
superheated vapor, which can be substantially higher than the vapor
condensing temperature. Circulating fluid temperatures from this
arrangement can therefore produce potable hot water. By keeping
this water at or above a predetermined temperature, such as
140.degree. F. (60.degree. C.), the risk of growth of various
pathogens, such as legionella, is reduced or eliminated.
[0010] Preferably, the circulating fluid medium is configured to
transport either or both an SH fluid, such as water or forced air,
or DHW. Preferably, the heat source is a burner in thermal
communication with an evaporator such that heat provided by the
burner causes the organic working fluid that flows through the
conduit in the evaporator to become superheated. Also, the burner
can be disposed within a container (of which the evaporator may
form an integral part) which may include an exhaust duct to carry
away combustion products (primarily exhaust gas), an exhaust fan to
further facilitate such product removal, as well as an exhaust gas
heat exchanger disposed adjacent (preferably within) the exhaust
duct so that residual heat present in the exhaust gas can be used
for supplemental heating in other parts of the cogeneration system.
The exhaust gas heat exchanger can further include an exhaust gas
recirculation device to further improve heat transfer from the
exhaust gas.
[0011] The cogeneration system can be configured such that the
organic working fluid is directly-fired or indirectly-fired. In the
former configuration, the relationship between the burner and the
organic working fluid-carrying evaporator is such that the flame
from the combustion process in the burner directly impinges on
either the conduit carrying the fluid or a container (alternately
referred to as a combustion chamber) that houses at least a portion
of the organic working fluid-carrying conduit such that the portion
of the conduit where the organic working fluid becomes superheated
is considered the evaporator. In the latter configuration, the
flame from the combustion process in the burner gives up a portion
of its heat to conduit making up a secondary circuit, which in turn
conveys a heat exchange fluid to an interloop heat exchanger. The
indirectly-fired system is advantageous in terms of system
flexibility, due in part to its ability to minimize temperature
excursions in the evaporator, and maintainability, as
heat-sensitive components (such as the conduit used to carry the
working fluid) are not directly exposed to the combustion process
in the case of a burner for a heat source. The directly-fired
system is advantageous in terms of system cost and simplicity.
[0012] According to still another aspect of the present invention,
a Rankine cycle cogeneration system is disclosed. The system
includes an organic working fluid, an evaporator made up of a
burner and conduit adjacently spaced relative to the burner, a
substantially closed-loop working fluid circuit in thermal
communication with the burner, and at least one energy conversion
circuit. Heat generated during burner operation is sufficient to
superheat the organic working fluid disposed in the adjacent
conduit. The closed-loop working fluid circuit includes an expander
that in operation maintains the organic working fluid in a
superheated state after expansion, a condenser in fluid
communication with the expander, and a pump configured to circulate
the organic working fluid. The energy conversion circuit includes a
generator coupled to the expander to produce electricity, and a
circulating fluid medium in thermal communication with the organic
working fluid in the condenser such that at least a portion of the
heat given up by the organic working fluid provides increased
thermal content to the circulating fluid medium. The condenser is
constructed such that the circulating fluid medium is in
counterflow with the organic working fluid.
[0013] According to another aspect of the present invention, a
dwelling configured to provide at least a portion of the heat and
power needs of occupants therein is disclosed. The dwelling (which
can be, for example, a house, apartment or commercial, industrial
or office building) includes walls, a roof situated above the
walls, at least one ingress/egress (such as a door) to facilitate
passage into and out of the dwelling, and a cogeneration system in
heat and power communication with at least one room formed within
the dwelling. The cogeneration system includes, at a minimum, a
heat source, a working fluid circuit, a generator and a circulating
fluid medium both of which can be responsive to the operation of
the working fluid circuit. The condenser is made up of at least a
first loop to convey the organic working fluid, and a second loop
to carry fluid from the circulating fluid medium. The second loop
is in counterflow thermal communication with the first loop, and
upon transfer of heat from the first to the second loop, the
circulating fluid medium can provide at least SH or DHW to the
dwelling. By way of example, the condenser could be a parallel
plate condenser or a shell-and-tube condenser, as previously
discussed. Optionally, the dwelling further comprises a controller
(such as a thermostat) responsive to occupant input. Additionally,
the condenser is configured such that a circulating fluid in the
circulating fluid medium passes through the condenser in
counterflow relationship to the organic working fluid.
[0014] According to yet another aspect of the present invention, a
micro combined heat and power system is disclosed. The micro
combined heat and power system includes an electric production
subsystem and a heat production subsystem. The electric production
subsystem includes an organic working fluid, a burner for
superheating the organic working fluid, a scroll expander
configured to receive and expand the organic working fluid in a
superheated state, a generator operatively coupled to the scroll
expander to produce electricity, a condenser in fluid communication
with the scroll expander, and a pump to circulate the organic
working fluid through the electricity generating loop. The heat
production subsystem comprises a circulating fluid medium in
thermal communication with the condenser such that DHW or hydronic
SH can be produced from the heat exchanged in the condenser.
[0015] According to still another aspect of the present invention,
a method of producing heat and electrical power from a cogeneration
device is disclosed. A first working fluid circuit with conduit,
expander, counterflow two loop condenser and pump, and an energy
conversion circuit are used in the present method to achieve
cogeneration. Steps in the method include providing a heat source,
configuring the first circuit to transport an organic working fluid
adjacent the heat source, superheating the organic working fluid in
the first circuit, and expanding the superheated organic working
fluid to generate electricity. The organic working fluid in the
first circuit gives up at least a portion of its heat via
counterflow heat exchange relationship with a fluid in the
circulating fluid medium, where a first loop in the condenser
defines the part of the working fluid circuit in the condenser and
a second loop defines the part of the circulating fluid medium in
the condenser. Optionally, the circulating fluid medium is
configured to transport an SH fluid, such as water or forced air.
Similarly, the circulating fluid medium can be configured to
transport DHW.
BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS
[0016] The following detailed description of the preferred
embodiments of the present invention can be best understood when
read in conjunction with the following drawings, where like
structure is indicated with like reference numerals and in
which:
[0017] FIG. 1 shows a schematic diagram of a directly-fired
cogeneration system according to an embodiment of the present
invention having a connection to both SH and DHW capability;
[0018] FIG. 2 shows a schematic diagram of an indirectly-fired
cogeneration system configuration with connections to separate SH
and DHW capability;
[0019] FIG. 3 shows that electrical output is maximized when a
cogeneration system is modulated according variable heat loads as
compared to that of maintaining a constant heat load;
[0020] FIG. 4A shows a shell-and-tube counterflow condenser
according to an embodiment of the present invention; and
[0021] FIG. 4B shows a parallel plate counterflow condenser
according to an embodiment of the present invention.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
[0022] Referring initially to FIG. 1, a micro-CHP system 100
capable of providing electric current and heated fluid is shown.
The system 100 includes a working fluid circuit and an energy
conversion circuit. The working fluid circuit includes an expander
101, a condenser 102, a pump 103 and an evaporator 104. These four
components define the major components that together approximate an
ideal Rankine cycle system, where the evaporator 104 acts as a
constant pressure heat addition, the expander 101 allows efficient,
nearly isentropic expansion of the working fluid, the condenser 102
acts to reject heat at a constant pressure, and the pump 103
provides efficient, nearly isentropic compression. The evaporator
104, details of which will be discussed at length below, functions
as the primary heat generator in micro-CHP system 100. In such a
configuration, heat generated at the heat source (shown in the
figure being produced by a combustion process where a fuel, such as
natural gas, is transported via gas line 152 past a gas valve 153
to a burner 151) in the evaporator 104 is transferred to an organic
working fluid being transported through conduit 110 (alternately
referred to as piping). In the present micro-CHP system 100, the
energy produced by the expansion of the organic working fluid is
converted into electricity and heat as the two useable forms of
energy. An optional fan 158 to pull away heat source byproducts is
shown downstream of the heat source as an induced-draft fan,
although it could also be a forced-draft fan if located upstream
relative to the burner 151 and its ancillary componentry.
[0023] The energy conversion circuit takes the increased energy
imparted to the working fluid in the working fluid circuit and
converts it into useable form. The electrical form of the useable
energy comes from a generator 105 (preferably induction type) that
is coupled to expander 101. The hot fluid form of the useable
energy comes from a circulating fluid medium 140 (shown preferably
as a combined SH and DHW loop) thermally coupled to condenser 102.
Hydronic fluid flowing through circulating fluid medium 140 is
circulated with a conventional pump 141, and can be supplied as
space heat via radiator 148 or related device. As an example,
hydronic fluid could exit the condenser 102 at about 112.degree. F.
(50.degree. C.) and return to it as low as 86.degree. F.
(30.degree. C.). The nature of the heat exchange process is
preferably through either heat exchangers 180 (shown notionally for
the DHW loop, but equally applicable to the SH loop), or through a
conventional hot water storage tank (for a DHW loop). Isolation of
either the SH or DHW loop within circulating fluid medium 140 is
accomplished through valves 107E and 107F. It will be appreciated
by those of ordinary skill in the art that while the embodiments
depicted in the figures show DHW and SH heat exchangers in parallel
(and in some circumstances being supplied from the same heat
exchange device, shown later), it is within the spirit of the
present disclosure that series or sequential heat exchange
configurations could be used. It will also be appreciated that the
heat exchanger 180 depicted in FIG. 1 could be in the form of the
aforementioned hot water storage tank, where the hot fluid
circulating through circulating fluid medium 140 gives up at least
a portion of its heat to incoming domestic cold water coming from
water supply 191A, which is typically from a municipal water
source, well or the like. Once heated in the tank, the domestic
water can then be routed to remote DHW locations, such as a shower,
bath or hot water faucet, through DHW outlet 191B.
[0024] The organic working fluid (such as naturally-occurring
hydrocarbons or halocarbon refrigerants, not shown) circulates
through the loop defined by the fluidly-connected expander 101,
condenser 102, pump 103, evaporator 104, and conduit 110. The
embodiment of the micro-CHP system 100 shown in the figure is
operated as a directly-fired system, where the fluid that passes
adjacent the heat source through conduit 110 is also the working
fluid passing through the expander 101. While the expander 101 can
be any type, it is preferable that it be a scroll device. For
example, the scroll expander 101 can be based on a conventional
single scroll device, as is known in the art. A scroll device
exhibits numerous advantages over other positive-displacement
systems. For example, since they are made in very high production
volume in dedicated modem facilities, its cost is inherently low.
Furthermore, the modification to an existing production line to
convert from making scroll compressors to making scroll expanders
is considerably simpler than to modify an existing reciprocating
compressor production line, as the changes to valves and actuation
are minimized. Additionally, by operating with very few moving
parts, it can go long durations between service or component
failure. Moreover, when operating in expansion mode, once the fixed
volume of working fluid is captured, the nature of the working
fluid-containing chamber is such that the volume of the chamber is
always expanding. This also promotes long component life as it
avoids the possibility of trapping and attempting to compress (such
as upon a return stroke) a working fluid that could, under certain
pressure and temperature regimes, include an incompressible liquid
phase condensate. An optional oil pump 108 may be used to provide
lubricant to the scroll. A generator 105 (preferably induction
type) is coupled to expander 101 such that motion imparted to it by
expander 101 generates electricity. The generator 105 is preferably
an asynchronous device, thereby promoting simple, low-cost
operation of the system 100, and reducing reliance on complex
generator speed controls and related grid interconnections. The
optional recuperator 109 may be placed between expander 101 and
condenser 102 in order to extract additional heat from the working
fluid once the fluid has been expanded. An optional accumulator 111
may be connected intermediate condenser 102 and pump 103, and can
be isolated from the remainder of the organic working fluid circuit
by valve 107D. The accumulator 111 acts as a working fluid storage
device in that during periods of low fluid flow rates (such as
during system startup), it can provide an additional charge of
fluid into the working fluid circuit to minimize, among other
things, cavitation of pump 103. An optional warming device 113 can
be placed adjacent the accumulator 111 to keep it slightly warmer
than the remaining circuit during periods of system inoperation.
Heat for the warming device 113 can be, for example, from an
electric (resistive) supply.
[0025] Referring next to FIG. 3, a comparison between two ways to
mimic the modulation of a boiler to achieve maximum system
efficiency is shown. In many conventional boiler applications,
where the set point of the system 100 is determined by a single
parameter, such as an outdoor temperature, controller 130 (not
presently shown) can be used to provide primary control input to
the evaporator 104 (not presently shown). By operating the
evaporator in a variable-capacity mode, where the gas valve 153 on
the burner 151 (neither of which are presently shown) can be
modulated, the SH or DHW portions of the circulating fluid medium
can be maintained at the desired set point. Such modulation permits
quasi-steady state system operation that is responsive to heat
needs that are keyed to a specified hydronic supply temperature set
point, which is preferably the hydronic temperature coming off the
condenser 102 (not presently shown). For example, the ambient
outdoor temperature is measured and sets the desired hydronic
supply temperature. A single measuring point is used, preferably
positioned on the North side of the building (in the Northern
hemisphere), to avoid the influence of direct sunlight on cold
days. A linear variation of the hydronic set point is used, so that
on very cold days the hydronic set point is at or near its maximum
setting (shown in the figure as 75.degree. C.), while on warm days
the set point is at or near its minimum (shown in the figure as
25.degree. C.). The hydronic pump 141 (not presently shown)
operates continuously so there is always a flow through the
system.
[0026] Similarly, for the micro-CHP, a single measurement of
outdoor ambient temperature can be used to establish the hydronic
supply set point temperature. The working fluid mass flow is then
controlled by the controller to maintain the actual supply
temperature at this set point. Either an inverter drive or a
separate input on the pump 103 would be sufficient to adjust the
displacement of the pump 103 at constant motor speed to vary flow
rate. The gas valve 153 is modulated to maintain the desired set
point for the evaporator 104 outlet temperature of the working
fluid into the expander 101. Properties of the working fluid, as
well as of optional fluids, such as lubricants, may dictate maximum
operating temperatures of the fluid coming out of the evaporator
104. For example, if the working fluid is the refrigerant known as
R-245fa, the temperature set point at the evaporator 104 exit is
about 310.degree. F. (154.degree. C.).
[0027] By operating the system such that the temperature of the
working fluid at the evaporator 104 outlet is at or near its
maximum value, good overall system efficiency results, regardless
of system load. This can include very low thermal loads; for
example, if the thermal load falls much below about 30 to 40% of
full load, it is appropriate to shutdown the system and cease
making both heat and power. Since the hydronic pump is kept running
at all times, even at a low flow rate, the controller 130 can
continuously monitor the error signal between the hydronic actual
and set point values. When this error is large enough, (i.e., the
actual temperature is below the set point by a preselected value)
the controller 130 can start the system for another on-cycle. As
the system 100 operates it may find that even at the minimum system
mass flow, the actual supply temperature begins to exceed the set
point. When this occurs, the system 100 is again shut down. Under
this approach, the system 100 will operate for as many hours as
possible during the colder heating season by running just often
enough to maintain the hydronic supply temperature at the right
value for the nominal heating load. When the system 100 operates at
less than the maximum hydronic supply temperature, more power is
generated than at the maximum temperature, so the controller 130
automatically and passively maximizes the electric power, which can
be produced. Thus, as shown in the figure, the net electrical
output goes up (at the same working fluid mass flow rate) as
hydronic fluid supply temperature requirements goes down, while
variations in working fluid flow rate and can be used in
conjunction to vary electric output under a given thermal load.
This inherent flexibility promotes overall energy (electrical and
heat) system efficiency.
[0028] Referring again to FIG. 1, the generator 105 is preferably
an asynchronous device, thereby promoting simple, low-cost
operation of the system 100, and reducing reliance on complex
generator speed controls and related grid interconnections. An
asynchronous generator always supplies maximum possible power
without controls, as its torque requirement increases rapidly when
generator 105 exceeds system frequency. The generator 105 can be
designed to provide commercial frequency power, for example, 50 or
60 Hz, while staying within close approximation (often 150 or fewer
revolutions per minute (rpm)) of synchronous speed (3000 or 3600
rpm). Block valve 107A and bypass valve 107B are situated in the
organic working fluid flow path defined by conduit 110. These
valves respond to a signal in controller 130 that would indicate if
no load (such as a grid outage) were on the system, or if a high
Q/P were desired, thus allowing the superheated vapor to bypass the
expander, thereby transferring a majority of the excess heat to the
heat exchange loop in the condenser 102 (for high Q/P operation),
as well as additionally avoiding overspeed of expander 101.
[0029] An optional level indicator switch 120 is placed at the
discharge of condenser 102, while controller 130 is used to
regulate system operation. Sensors connected to controller 130
measure key parameters, such as fluid level information taken from
the level indicator switch 120, and organic working fluid
temperatures at various points within the organic working fluid
circuit. Through appropriate program logic, the controller 130 can
be used to vary pump speed, gas flow rate and evaporator output
temperature, as well as to open and close valves. In many
applications, where the set point of the system is determined by a
single parameter, such as an outdoor temperature, the controller
130 can then be used to provide primary control input to the
evaporator 104. By operating the evaporator 104 in a
variable-capacity mode, where the gas valve 153 on the burner 151
can be modulated, optional SH or DHW portions of the circulating
fluid medium 140 can be maintained at the desired set point. The
circulating fluid medium 140 includes a pump 141 and block valves
107E and 107F that selectively permit flow to SH loop heat
exchanger (indicated by radiator 148) or DHW loop (indicated by DHW
heat exchanger 180, which preferably takes cold water from a source
191A and after heating sends it to a DHW destination 191B).
Preferably, the fluid circulating through at least the SH portion
of the circulating fluid medium 140 is a hydronic fluid. By way of
example, hydronic fluid could exit the condenser 102 at about
50.degree. C. (122.degree. F.) and return to it as low as
300.degree. C. (86.degree. F.). Controller 130 may also be used to
manipulate block valves 107A and 107C and bypass valve 107B, which
are situated in the organic working fluid flow path defined by
conduit 110. Valves 107A and 107B respond to a signal in controller
130 that would indicate if no load (such as a grid outage) were on
the system, or if a high Q/P were desired, thus allowing the
superheated vapor to bypass the expander, thereby transferring a
majority of the excess heat to the heat exchange loop in the
condenser 102 (for high Q/P operation), as well as additionally
avoiding overspeed of expander 101. Similarly, when recuperated
operation is desired, optional block valve 107C can be used to help
tailor working fluid preheat needs of the system by selectively
allowing a portion of the working fluid passing from the pump 103
to evaporator 104 to be routed through recuperator 109.
[0030] Referring next to FIG. 2, an indirectly-fired cogeneration
system 200 is shown. A second loop 250 in cogeneration system 200
includes two parallel sub-loops 250A, 250B, while a first loop,
which includes an expander 201 coupled to generator 205, condenser
202B, pump 203, recuperator 209, conduit 210 and accumulator 211
with warming device 213, is configured similarly to, although not
necessarily identical to, the system shown in FIG. 1. The most
significant difference of the first loop over the system of FIG. 1
is that the evaporator 104 of the former system is now replaced
with an interloop heat exchanger 202A, thus acting as a heat source
for the first loop. Controller 230 is similar to that of the
previously described system, but now with enlarged functionality to
additionally control some or all of the operations of the second
loop 250. It will be appreciated that circulating fluid medium 240
is, while notionally depicting only an SH component that includes a
pump 241 and radiator 248, is understood to be similar to that of
FIG. 1. Also as before, valve 207C can be used to bypass the
recuperator 209 in order to achieve variable Q/P, while pump 208 is
used to circulate oil or related lubricant through the
expander.
[0031] Heat to the two parallel sub-loops 250A, 250B is provided by
a burner 251, which is supplied with fuel by a gas train 252 and
variable flow gas valve 253. Piping 260 (alternately referred to as
conduit, and which makes up the parallel sub-loops) passes through
a combustion chamber 254, where the heat from the combustion of
fuel at burner 251 is given up to the heat exchange fluid (not
shown) that flows through piping 260. Piping 260 branches out into
the first parallel sub-loop 250A, which transports the heat
exchange fluid that has been heated in combustion chamber 254 to
interloop heat exchanger 202A in order to give up the heat to
organic working fluid flowing through the first loop, which as
previously described, save the presence of the interloop heat
exchanger 202A in place of the evaporator 104, is similar in
construction to the directly-fired cogeneration system 100 shown in
FIG. 1. Block valves (not shown) could be used to regulate flow
between the sub-loops 250A and 250B; however, by idling the pump of
the inactive sub-loop, significant flow in that sub-loop is
prevented without the need for additional valving. The second
parallel sub-loop 250B transports the heat exchange fluid to DHW
heat exchanger 280 in order to heat up domestic hot water. One side
of DHW heat exchanger 280 (which can be a water storage tank)
includes coil 280A configured to transport the heat exchange fluid,
and another side, the shell 280B, to transport DHW (not shown) from
a cold water inlet 291A, past coil 280A and to DHW outlet 291B. As
with the system shown in FIG. 1, the cold water preferably comes
from either a well or a city/municipal water supply. Similarly,
temperature sensor 271B can detect the temperature of the DHW
coming out of the DHW heat exchanger 280. This sensor can also be
linked to a controller 230 (discussed in more detail below).
[0032] Combustion chamber 254 includes an exhaust duct 255, an
exhaust gas recirculation device 256 with exhaust duct heat
exchanger 257, and fan 258. Temperature sensor 271A is placed at
the combustion chamber 254 outlet for the second loop 250 to
measure the temperature conditions of the heat exchange fluid, in a
manner similar to that of temperature sensor 271B. Second loop
pumps 285A, 285B are used to circulate heat exchange fluid through
the second loop 250, with pump 285B circulating heat exchange fluid
through DHW heater 280 and pump 285A circulating heat exchange
fluid through interloop heat exchanger 204. The exhaust duct heat
exchanger 257 and an EGR device 256 accept hot exhaust gas from the
burner 251 and recirculate it in an internal heat exchange process,
thereby lowering the temperature of the exhaust gas that is pulled
away and vented to the atmosphere by fan 258. The heat given up by
the exhaust gas in the exhaust gas heat exchanger 257 can be used
to provide additional heat to other parts of the system 200. For
example, this additional heat can be used to increase the
temperature of the heat exchange fluid flowing in second loop 250,
or to increase the heat content of the organic working fluid in the
first loop.
[0033] Referring next to FIGS. 4A and 4B, the condensers 102A and
102B are described in conjunction with the directly-fired
cogeneration system 100 of FIG. 1, although they are equally
applicable to the indirect system 200 of FIG. 2. Condensers 102A
and 102B extract excess heat from the organic working fluid after
the fluid has been expanded such that a circulating fluid medium
140 fluidly communicating with the condenser 102 can absorb and
transfer the heat to remote locations. To achieve a Q/P that varies
depending on the heat and electric needs, the burner 151 is capable
of modulation, while either condenser 102A, 102B is simultaneously
responsive to fluctuating thermal content in the working fluid and
capable of transferring enough heat for hydronic SH needs (as well
as DHW needs). Condenser staging is central to providing a balance
between the often diverging requirements of high heat loads in the
circulating fluid medium and the need for burner modulation. One of
the basic approaches to controlling the temperature at the
evaporator outlet is to vary the mass flow out of the expander. By
way of example, when the working fluid is R-245fa, the outlet
temperature can be fixed, or set, to about 310 F. (154.degree. C.).
By selecting a corresponding pump capacity and speed to control the
mass flow of working fluid into the evaporator, coupled with the
ability of the expander to accept a concomitant amount of vapor
flow, the evaporator outlet pressure tends to be typically between
380 and 400 psia (2.62 MPa and 2.76 MPa, respectively), with a
preferred pressure of 392 psia (2.70 MPa). The outlet temperature
of 310.degree. F. (154.degree. C.) leaves about 30.degree. F.
(17.degree. C.) of superheat above the saturation temperature for
the fluid, thereby simplifying the control system and its ability
to adjust the burner firing rate to maintain the set outlet
temperature. Then, as the thermal output capacity to meet lower
loads is reduced, which could be due to cool or warm weather, the
pump flow is reduced and the pressure changes accordingly to a
lesser value. In an alternative approach, the same superheat
temperature (30.degree. F.) (17.degree. C.) can be maintained,
while allowing the evaporator outlet temperature to fluctuate. Of
the two approaches, it is preferable to run the evaporator outlet
at a constant 310.degree. F. (154.degree. C.) from an efficiency
stand point and for simplicity of the controller, as calculating
the proper superheat temperature requires measuring, in some way,
the evaporator outlet pressure.
[0034] Referring with particularity to FIG. 4A, shell-and-tube
condenser 102A is shown. Organic working fluid travels through a
first, or primary, loop that passes through shell 120, while
circulating fluid travels through a second loop defined by tubing
121. The organic working fluid first flows into a desuperheating
section, then through a subcooling section situated below the
desuperheating section. The two sections are separated by partition
123, which includes perforations 123A therein to permit vapor flow
from the subcooling section to waft up into the desuperheating
section. Baffles 122 are located in the desuperheating section of
shell 120, and create a tortuous path through which the incoming
working fluid must flow, thus promoting increased thermal
interchange between the working fluid and the circulating fluid in
the portion of tubing 121 that is disposed in the desuperheating
section. The shell 120 of condenser 102A includes. After passing
from the desuperheating section to the subcooling section through
the partitions 123A, the organic working fluid condenses, and is
defined by a condensate free surface 126 above which the working
fluid exists as a vapor, and below as a liquid. Outlet 125 is
situated at or near the bottom of shell 120 to permit the condensed
working fluid to continue on to the pump 103 (not presently shown)
in the working fluid circuit. The circulating fluid enters through
tubing inlet 127 and exits through tubing outlet 128. In between,
tubing 121 defines multiple passes through the shell 120 to
maximize contact between the tubing 121 and the working fluid
passing through the desuperheating and subcooling sections of shell
120. By the present construction, the organic working fluid passing
through shell 120 and the circulating fluid passing through tubing
121 are in a counterflow relationship to one another.
[0035] Referring with particularity to FIG. 4B, flat plate
condenser 102B is shown. The flow pattern between the organic
working fluid and the circulating fluid is similar, in that working
fluid enters an inlet 124 to a condenser inlet manifold and exits
through an outlet 125 coming from condenser outlet manifold while
circulating fluid enters through tubing inlet 127 and exits through
tubing outlet 128. As with the condenser 102A shown in FIG. 4A, the
two fluids exchange heat in a counterflow pattern, although, unlike
condenser 102A, the heat exchange process takes part without
multiple passes or convoluted flow patterns, relying instead on the
large ratio of surface area to flow volume made possible by the
flat passages. Because of the absence of multiple passes, all of
the working fluid leaving the condenser is in close heat transfer
communication with only the incoming cooling fluid, hence all the
exiting working fluid can more easily and more completely be cooled
to a temperature closer to that of the incoming coolant.
[0036] Having described the invention in detail and by reference to
preferred embodiments thereof, it will be apparent that
modifications and variations are possible without departing from
the scope of the invention defined in the appended claims. More
specifically, although some aspects of the present invention are
identified herein as preferred or particularly advantageous, it is
contemplated that the present invention is not necessarily limited
to these preferred aspects of the invention.
* * * * *