U.S. patent application number 10/443330 was filed with the patent office on 2004-11-25 for adsorber generator for use in sorption heat pump processes.
Invention is credited to Bradley, Steven A., Dunne, Stephen R..
Application Number | 20040231828 10/443330 |
Document ID | / |
Family ID | 33450383 |
Filed Date | 2004-11-25 |
United States Patent
Application |
20040231828 |
Kind Code |
A1 |
Dunne, Stephen R. ; et
al. |
November 25, 2004 |
Adsorber generator for use in sorption heat pump processes
Abstract
This invention provides a compact heat exchanger that has an
effective geometry for heat transfer operations regardless of the
heat conductivity of the material chosen for the fin materials. It
has further been found that the use of adsorbent coated anodized
aluminum for fin materials provides for a very efficient heat
exchanger.
Inventors: |
Dunne, Stephen R.;
(Algonquin, IL) ; Bradley, Steven A.; (Arlington
Heights, IL) |
Correspondence
Address: |
JOHN G TOLOMEI, PATENT DEPARTMENT
UOP LLC
25 EAST ALGONQUIN ROAD
P O BOX 5017
DES PLAINES
IL
60017-5017
US
|
Family ID: |
33450383 |
Appl. No.: |
10/443330 |
Filed: |
May 22, 2003 |
Current U.S.
Class: |
165/104.12 |
Current CPC
Class: |
Y02A 30/276 20180101;
Y02B 30/00 20130101; Y02B 30/64 20130101; Y02A 30/278 20180101;
F28D 9/0031 20130101; F25B 35/04 20130101; Y02A 30/27 20180101 |
Class at
Publication: |
165/104.12 |
International
Class: |
F28D 015/00 |
Claims
1: A sorption heat pump exchanger module comprising: a) a plurality
of metallic plates having a first and a second opposing side and an
adsorbent coating covering essentially the entire surface of said
first opposing side and wherein a first and a second of said
metallic plates are grouped together to form a sub-unit having a
passageway between said two metallic plates for passage of a heat
exchange media and wherein a plurality of said sub-units are spaced
apart in a stacked arrangement that eliminates contact between said
sub-units; b) a plurality of tubes contacting said sub-units
wherein a heat exchange medium flows within said tubes to and from
openings in said tubes to openings in said sub-units, and c) a
passageway between each of said sub-units wherein a refrigerant
flows within said passageway.
2: The sorption heat pump exchanger module of claim 1 wherein the
adsorbent coating comprises a layer of paper comprising said
adsorbent.
3: The sorption heat pump exchanger module of claim 1 wherein said
first opposing side of said first metallic plate faces the first
opposing side of said second metallic plate within each of said
sub-units.
4: The sorption heat pump exchanger module of claim 1 wherein said
second opposing side of said first metallic plate faces said second
opposing side of said second metallic plate within each of said
sub-units.
5: The sorption heat pump exchanger module of claim 1 wherein said
metallic plates have an adsorbent coating covering essentially the
entire surface of said second opposing side.
6: The sorption heat pump exchanger module of claim 1 wherein the
adsorbent coating comprises a layer of paper comprising said
adsorbent.
7: The sorption heat pump exchanger module of claim 1 wherein
within said sub-units, said first metallic plate contacts said
second metallic plate on each of two edges to form a seal to form
said passageway for said heat transfer medium and wherein said
metallic plates are curved to form said passageway.
8: The sorption heat pump exchanger module of claim 1 wherein said
adsorbent coating comprises an adsorbent selected from the group
consisting of zeolite X, Zeolite Y, Zeolite A, silica gel, silicas,
aluminas and mixtures thereof.
9: The sorption heat pump exchanger module of claim 1 wherein said
adsorbent coating comprises a layer comprising zeolite Y selected
from the group consisting of zeolite Y-54, zeolite Y-74, zeolite
Y-84, steam calcined rare earth exchanged Y-54, zeolite Y-85, low
cerium rare earth exchanged Y-84, low cerium rare earth exchanged
zeolite LZ-210 and zeolite DDZ-70.
10: The sorption heat pump exchanger module of claim 1 wherein the
refrigerant and the heat transfer fluid are selected from the group
consisting of water, alcohols, ammonia, light hydrocarbons,
chloro-fluorocarbons, fluorocarbons and mixtures, thereof.
11: The sorption heat pump exchanger module of claim 1 wherein said
substrate comprises anodized aluminum.
12: The sorption heat pump exchanger module of claim 1 wherein said
adsorbent coating covers essentially the entire surface of both
opposing sides of said metallic plates.
13: A sorption heat pump exchanger module comprising a) a plurality
of fin plates, having a first side and a second side opposite said
first side wherein said fin plates are approximately rectangular in
shape, and wherein said fin plates have two long edges and two
short edges; b) an adsorbent coating covering a majority of said
first side and said second side, wherein a gap in said adsorbent
coating extends from one of said long edges to the other of said
long edges c) wherein said fin plates are bent along said gaps to
form a corrugated structure and d) wherein said fin plates contact
a top and a bottom outside surface of a pair of parallel heat
transfer passages.
14: The sorption heat pump exchanger module of claim 13 wherein the
adsorbent coating comprises a layer of paper comprising said
adsorbent.
15: The sorption heat pump exchanger module of claim 1 wherein
within said sub-units, said first metallic plate contacts said
second metallic plate on each of two edges to form a seal to form
said passageway for said heat transfer medium and wherein said
metallic plates are curved to form said passageway.
16: The sorption heat pump exchanger module of claim 13 wherein
said adsorbent coating comprises an adsorbent selected from the
group consisting of zeolite X, Zeolite Y, Zeolite A, silica gel,
silicas, aluminas and mixtures thereof.
17: The sorption heat pump exchanger module of claim 13 wherein
said adsorbent coating comprises a layer comprising zeolite Y
selected from the group consisting of zeolite Y-54, zeolite Y-74,
zeolite Y-84, zeolite Y-85, low cerium rare earth exchanged Y-84,
low cerium rare earth exchanged zeolite LZ-210 and zeolite
DDZ-70.
18: The sorption heat pump exchanger module of claim 13 wherein the
refrigerant and the heat transfer fluid are selected from the group
consisting of water, alcohols, ammonia, light hydrocarbons,
chloro-fluorocarbons, fluorocarbons and mixtures thereof.
19: The sorption heat pump exchanger module of claim 13 wherein
said substrate comprises anodized aluminum.
20-26 (canceled)
Description
BACKGROUND OF THE INVENTION
[0001] The present invention relates to an apparatus for use in
adsorption and desorption based sorption heat pump processes.
[0002] Sorption heat pump processes typically employ some adsorbent
disposed in a metal vessel and on a metal screen or surface which
provides support for the adsorbent and permits the adsorbent to be
placed in contact with the fluid stream containing the adsorbable
component over the range of conditions necessary for the adsorption
and desorption. The metal structures and physical arrangement of
these devices has placed certain process limitations which restrict
the amount of adsorbent which actually comes in contact with the
fluid stream, or is accompanied by heat transfer inefficiencies
inherent in the disposition of the adsorbent.
[0003] In the operation of sorption heat pump systems, generally
there are two or more solid beds containing a solid adsorbent. The
solid adsorbent beds desorb refrigerant when heated and adsorb
refrigerant vapor when cooled. In this manner the beds can be used
to drive the refrigerant around a heat pump system to heat or cool
another fluid such as a process stream or to provide space heating
or cooling. In the heat pump system, commonly referred to as the
heat pump loop, or a sorption refrigeration circuit, the
refrigerant is desorbed from a first bed as it is heated to drive
the refrigerant out of the first bed and the refrigerant vapor is
conveyed to a condenser. In the condenser, the refrigerant vapor is
cooled and condensed. The refrigerant condensate is then expanded
to a lower pressure through an expansion valve and the low pressure
condensate passes to an evaporator where the low pressure
condensate is heat exchanged with the process stream or space to be
conditioned to revaporize the condensate. When further heating no
longer produces desorbed refrigerant from the first bed, the first
bed is isolated and allowed to return to the adsorption conditions.
When the adsorption conditions are established in the first bed,
the refrigerant vapor from the evaporator is reintroduced to the
first bed to complete the cycle. Generally two or more solid
adsorbent beds are employed in a typical cycle wherein one bed is
heated during the desorption stroke and the other bed is cooled
during the adsorption stroke. The time for the completion of a full
cycle of adsorption and desorption is known as the "cycle time."
The upper and lower temperatures will vary depending upon the
selection of the refrigerant fluid and the adsorbent. Some
thermodynamic processes for cooling and heating by adsorption of a
refrigerating fluid on a solid adsorbent use zeolite and other
sorption materials such as activated carbon and silica gel. U.S.
Pat. No. 4,138,850 relates to a system for solar heat utilization
employing a solid zeolite adsorbent mixed with a binder, pressed,
and sintered into divider panels and hermetically sealed in
containers. U.S. Pat. No. 4,637,218 relates to a heat pump system
using zeolites as the solid adsorbent and water as the refrigerant
wherein the zeolite is sliced into bricks or pressed into a desired
configuration to establish a hermetically sealed space and thereby
set up the propagation of a temperature front, or thermal wave
through the adsorbent bed. U.S. Pat. No. 5,477,705 discloses an
apparatus for refrigeration employing a compartmentalized reactor
and alternate circulation of hot and cold fluids to create a
thermal wave which passes through the compartments containing a
solid adsorbent to desorb and adsorb a refrigerant. U.S. Pat. No.
4,548,046 relates to an apparatus for cooling or heating by
adsorption of a refrigerating fluid on a solid adsorbent. The
operations employ a plurality of tubes provided with parallel
radial fins, the spaces between which are filled or covered with
solid adsorbent such as Zeolite 13X located on the outside of the
tubes. U.S. Pat. No. 5,518,977, which is hereby incorporated by
reference, relates to sorption cooling devices which employ
adsorbent coated surfaces to obtain a high cooling coefficient of
performance.
[0004] U.S. Pat. No. 5,585,145 discloses a method for providing an
adsorbent coating on a heat exchanger which comprises applying a
flowable emulsion including a binder agent, water and a solid
adsorbent material to the surface of the heat exchanger. The
disclosure states that the binder can be an adhesive and that the
thickness of the adsorbent coating can be dipped, painted or
sprayed with a drying step comprising heating the layer at
temperatures greater than 150.degree. C. in order to obtain a
durable adsorbent coating structure.
[0005] Many sorption chillers are designed with beads or extrudate
as an adsorbent. In the present invention, as in U.S. Pat. No.
6,102,107, there are no beads or extrudates with their resistance
to heat transfer, but instead there is a compact heat exchanger
module that comprises a laminate of adsorbent, especially zeolite,
in a polymeric or polymeric fiber matrix. This laminate is on a
substrate that can support the laminate and can be employed in the
hot and wet environment of the adsorber/generator.
[0006] U.S. Pat. No. 6,102,107, incorporated herein in its
entirety, teaches the use of a plate-fin-tube arrangement employing
a laminate composed of thin polymeric fiber matrix on a metallic
fin structure. Conventional tubing is laced through the fms by
punching holes in the fin structure and forming collars of the fm
metal that are maintained in intimate thermal contact with the tube
surfaces. While this patent provided for greatly increased heat
transfer and was a significant advance in the design and
performance of adsorber/generators in sorption based heat pumps, it
failed to deal with the problem of maximizing heat transfer when
materials other than high thermal conductivity fin plates are
used.
[0007] In addition to the problem of heat transfer resistance in
some materials, a second potential problem arises when clean,
uncoated aluminum is exposed to water vapor under vacuum
conditions. This is the problem of corrosion of the aluminum
surface and formation of AlOH radicals on the surface. This
reaction liberates hydrogen gas and is a cause for the loss of
vacuum under some conditions that may be present in the
adsorber/generator of a sorption cooler or heat pump. Stainless
steel could be used to solve this deficiency, but the low
conductivity of stainless steel changes the heat transfer
resistance. This makes adsorber/generators made from stainless
steel incapable of transferring the required heat and can result in
structures that are much more costly and only slightly more
efficient than packed bed systems. One feature of the present
invention is to allow for the use of aluminum with its superior
heat transfer properties but without the corrosion problems of the
prior art heat exchangers.
[0008] It is an object of the instant invention to provide an
improved compact heat exchanger with the adsorbent matrix bonded
directly to the plates. It is a further object of the invention to
enable the application of a thin uniform layer of adsorbent
material which is intimately bonded to a heat transfer surface.
Another object of the present invention is to enable a rapid
heating and cooling cycle with the purpose of achieving a high
specific power and a high coefficient of performance for the
sorption cooling cycle. Yet another object of the present invention
is to provide a heat exchanger geometry that is effective
regardless of the heat conductivity of the fin material that is
chosen.
SUMMARY OF THE INVENTION
[0009] The present invention relates to a highly efficient sorption
heat pump module apparatus for use in sorption heat pump processes
which can be used effectively with a rapid cooling and heating
cycle. A sorption heat pump exchanger module is employed comprising
a plurality of metallic plates having a first and a second opposing
side and an adsorbent coating covering essentially the entire
surface of said first opposing side and wherein a first and a
second of said metallic plates are grouped together to form a
sub-unit having a passageway between said two metallic plates for
passage of a heat exchange media and wherein a plurality of said
sub-units are spaced apart in a stacked arrangement that eliminates
contact between said sub-units; a plurality of tubes contacting
said sub-units wherein a heat exchange medium flows within said
tubes to and from openings in said tubes to openings in said
sub-units, and a passageway between each of said sub-units wherein
a refrigerant flows within said passageway.
[0010] In some embodiments of the invention, it has been found that
the use of metallic plates comprising a corrosion resistant
aluminum such as anodized aluminum provides for a highly efficient
heat exchanger that withstands corrosion. More specifically, the
sorption heat pump exchanger module comprises a plurality of
anodized aluminum fin plates having a first and second opposing
sides and an adsorbent coating comprising at least one adsorbent
selected from the group consisting of zeolite X, Zeolite Y, Zeolite
A, silica gel, silicas, aluminas and mixtures thereof. The
adsorbent coating covers essentially the entire surface of each
opposing side to form coated fin plates and the fin plates are
spaced apart in a stacked arrangement that eliminates adsorbent
bridging between all coated surfaces. There are at least 300 coated
fin plates for every meter of the stacked arrangement. A plurality
of tubes extend through openings in the fin plates wherein the
outside of the plurality of tubes directly contacts the periphery
of the openings to form the sorption heat pump exchanger module
defining a first flow path for a heat exchange medium in the
plurality of tubes and a second flow path for a refrigerant between
said coated fin plates.
[0011] In another embodiment of the present invention, a sorption
heat pump exchanger module comprises a plurality of anodized
aluminum fin plates having a first and second opposing sides and an
adsorbent coating covering essentially the entire surface of each
opposing side. There are a plurality of openings defined by the
anodized aluminum fin plates and extending through the anodized
aluminum fin plates and coating. A plurality of tubes that have
uncoated outer walls extend transversely through the anodized
aluminum fin plates and have direct contact with the anodized
aluminum fin plates being spaced apart in a stacked arrangement
that eliminates adsorbent bridging between all coated surfaces and
contain at least 300 anodized aluminum fin plates for every meter
of the stacked arrangement. The plurality of tubes extend through
the openings in the anodized aluminum fin plates wherein the
outside of said plurality of tubes directly contact the periphery
of the openings to form the sorption heat pump exchanger module
defining a first flow path for a heat exchange medium in said
plurality of tubes and a second flow path for a refrigerant between
said coated anodized aluminum fin plates. The adsorbent is selected
from the group consisting of Zeolite X, Zeolite Y, Zeolite A,
silica gel, silicas, aluminas and mixtures thereof.
[0012] In yet other embodiments of the present invention, the
sorption heat pump exchanger module comprises a plurality of fin
plates, having a first side and a second side opposite said first
side wherein said fin plates are approximately rectangular in
shape. The fin plates have two long edges and two short edges. An
adsorbent coating covers a majority of the first side and the
second side, except where there is a gap in the adsorbent coating
extending from one of the long edges to the other of the long
edges. The fm plates are bent along the gaps to form a corrugated
structure and the fin plates contact a top and a bottom outside
surface of a pair of parallel heat transfer passages. This
structure has been found to have highly effective heat transfer
properties.
BRIEF DESCRIPTION OF THE DRAWINGS
[0013] FIG. 1 is a view of a single-sided laminate of a
zeolite-containing matrix bonded to a substrate.
[0014] FIG. 2 is a cross-sectional view of a pair of single-sided
laminates mated together with a heat transfer channel between the
two laminates.
[0015] FIG. 3 shows a view of the heat transfer passageway between
two layers of the laminate of the present invention.
[0016] FIG. 4 shows an assembly of repeating units of the units
shown in FIG. 3.
[0017] FIG. 5 shows a double-sided laminate of a zeolite-containing
matrix bonded to both sides of a substrate.
[0018] FIG. 6 shows an embodiment of the invention having gaps in
the lamination to allow for bonding of a surface to an adjacent
heat transfer passage.
[0019] FIG. 7 shows how the uncoated gaps in the structure shown in
FIG. 6 are mated to the outside of heat transfer surfaces.
[0020] FIG. 8 shows a combination of the heat transfer passage
assembly of FIG. 4 with the addition of fm stock bonded to the
outside surfaces of the heat transfer surfaces.
DETAILED DESCRIPTION OF THE INVENTION
[0021] In the present invention, the adsorption zone is comprises
thin sheets of adsorbent paper layers bonded to a substrate. For
sorption heat pump processes, the adsorption zone comprises a
plurality of such plates disposed on tubes to form a tube and flat
plate heat exchanger. The adsorbent layer comprises an adsorbent
paper layer. An example of the type of adsorbent paper layer for
use in the present invention is disclosed in U.S. Pat. No.
5,650,221 which is hereby incorporated by reference. The adsorbent
paper layer of U.S. Pat. No. 5,650,221 is comprised of an improved
support material, fibrous material, binders, and high levels of
desiccant or adsorbent material. The fibrous materials include
cellulosic fibers, synthetic fibers and mixtures thereof
Fibrillated fibers, that is, fiber shafts which are split at their
ends to form fibrils, i.e., fine fibers or filaments much finer
than the fiber shafts are preferred. Examples of fibrillated,
synthetic organic fibers useful in the adsorbent paper of the
present invention are fibrillated aramid and acrylic fibers. A
particularly preferred example of such a fiber is available from E.
I. du Pont de Nemours & Company under the designation
KEVLAR.RTM.. The desiccant or adsorbent may be incorporated therein
during fabrication of the paper, or the paper may be formed and the
desiccant or adsorbent coated thereon, or a combination of
adsorbent incorporation during paper making and coating with
adsorbent thereafter may be used. As the thickness of the adsorbent
paper increases up to an optimal value, the capacity for heating
will be increased. However, since cost also increases with
increasing thickness, a balance between heating capacity and cost
is necessary. Preferably, the adsorbent paper of the present
invention comprises a thickness of from about 0.13 to about 0.75 mm
and comprises at least 50 wt-% adsorbent. More preferably, the
adsorbent paper comprises from about 0.25 to about 0.6 mm in
thickness and comprises more than about 70 wt-% adsorbent. Most
preferably, the adsorbent paper is about 0.5 mm in thickness and
comprises more than 70 wt-% adsorbent. The adsorbent can be any
material capable of adsorbing an adsorbable component such as a
refrigerant. The adsorbent may comprise powdered solid, crystalline
compounds capable of adsorbing and desorbing the adsorbable
compound. Examples of such adsorbents include silica gels,
activated aluminas, activated carbon, molecular sieves and mixtures
thereof. Molecular sieves include zeolite molecular sieves. Other
materials which can be used as adsorbents include halogenated
compounds such as halogen salts including chloride, bromide, and
fluoride salts as examples. The preferred adsorbents are zeolites.
Preferably, at least 70 wt-% of the adsorbent paper is a zeolite
molecular sieve.
[0022] The pore size of the zeolitic molecular sieves may be varied
by employing different metal cations. For example, sodium zeolite A
has an apparent pore size of about 4 .ANG. units, whereas calcium
zeolite A has an apparent pore size of about 5 .ANG. units. The
term "apparent pore size" as used herein may be defined as the
maximum critical dimension of the molecular sieve in question under
normal conditions. The apparent pore size will always be larger
than the effective pore diameter, which may be defined as the free
diameter of the appropriate silicate ring in the zeolite structure.
Zeolitic molecular sieves in the calcined form may be represented
by the general formula:
Me.sub.2/nO:Al.sub.2O.sub.3:xSiO.sub.2:yH.sub.2O
[0023] where Me is a cation, x has a value from about 2 to
infinity, n is the cation valence and y has a value of from about 2
to 10. The general formula for a molecular sieve composition known
commercially as type 13X is:
1.0.+-.0.2Na.sub.2O:1.00Al.sub.2O.sub.3:2.5.+-.0.5SiO.sub.2
[0024] plus water of hydration. Type 13X has a cubic crystal
structure which is characterized by a three-dimensional network
with mutually connected intracrystalline voids accessible through
pore openings which will admit molecules with critical dimensions
up to 10 .ANG.. The void volume is 51 vol-% of the zeolite and most
adsorption takes place in the crystalline voids. Typical well-known
zeolites which may be used include chabazite, also referred to as
Zeolite D, clinoptilolite, erionite, faujasite, also referred to as
Zeolite X and Zeolite Y, ferrierite, mordenite, Zeolite A, and
Zeolite P. Other zeolites suitable for use according to the present
invention are those having high silica content. The adsorbent can
be selected from the group consisting of DDZ-70, Y-54, Y-74, Y-84,
Y-85, low cerium mixed rare earth exchanged Y-84, calcined rare
earth exchanged LZ-210 at a framework SiO.sub.2/Al.sub.2O.sub.3 mol
equivalent ratio of less than about 7.0 and mixtures thereof.
[0025] The appropriate adsorbent to be selected is dependent upon
the planned operating conditions of the heat pump containing the
sorption heat pump exchangers of the present invention. Among the
factors determining the choice of adsorbent is the source of and
amount of power for the heat pump, the desired regeneration
temperature and the general climatic conditions that occur where
the heat pump will be used. For example, at higher regeneration
temperatures, zeolite (X) (from an Si/Al.sub.2 ratio of 2.3 and up)
or zeolite (Y) (from an Si/Al.sub.2 ratio of 5 and up) are more
effective due to higher heat of adsorption and the resulting
greater ability to obtain high loading at relatively high
adsorption temperatures. When the regeneration temperature and
adsorption temperature are both relatively low, then the preferred
adsorbent type is zeolite DDZ-70 (available from UOP LLC, Des
Plaines, Ill.) due to its low heat of adsorption and consequently
its ability to regenerate at relatively low temperatures.
[0026] For example, when the regeneration temperature and the
condensing and adsorption temperatures are below 40.degree. to
50.degree. C., then the DDZ-70 zeolite is a good choice of
adsorbent. At higher temperatures such as about 150.degree. C.,
regeneration temperature and adsorption temperature above
50.degree. C., NaY zeolite works well.
[0027] A heat transfer fluid, such as a cold fluid to cool the
adsorption zone to adsorption conditions of adsorption temperature,
is introduced at a cold fluid temperature into the heat transfer
zone. A hot heat transfer fluid is introduced to the heat transfer
zone, when required to raise the temperature of the adsorption zone
to desorption conditions such as a desorption temperature. The cold
heat transfer fluid and the hot heat transfer fluid may be selected
from the group consisting of water, alcohols, ammonia, light
hydrocarbons, chloro-fluorocarbons, fluorocarbons, and mixtures
thereof. Water is a preferred heat transfer fluid. Similarly, for
sorption heat pump operations, a refrigerant is selected from the
group consisting of water, alcohols, ammonia, light hydrocarbons,
chloro-fluorocarbons, fluorocarbons, and mixtures thereof. It is
preferred that the heat transfer fluids and the refrigerants not
react with the materials of the heat transfer surface. Additives
and inhibitors such as amines can be added to the heat transfer
fluids to pacify or inhibit such reactions.
[0028] In the operation of the sorption heat pump system of the
present invention, a portion of the adsorbent zones may be in an
adsorption mode, an intermediate mode, or a desorption mode. In the
typical installation, at least one portion of the adsorbent zones
will generally be active in each of the operating modes at any
given time in order to provide a continuous process. The desorption
mode comprises a desorption temperature ranging from about
80.degree. to about 350.degree. C. and a desorption pressure
ranging from about 2 kPa to about 1.5M Pa (220 psia).
[0029] The sorption zone may be operated with a variety of
sorbent/refrigerant combinations or pairs. Examples of pairings of
such sorbent/refrigerant pairs include zeolite/water,
zeolite/ethanol, zeolite/methanol, carbon/ethanol, zeolite/ammonia,
zeolite/propane and silica gel/water. The operating conditions will
vary with the selection of the sorbent/refrigerant pair.
DETAILED DESCRIPTION OF THE DRAWINGS
[0030] FIG. 1 shows a single-sided laminate 10 having at least two
layers including a substrate layer 12 and an adsorbent-containing
layer 14. The adsorbent layer comprises an adsorbent. Preferably,
the adsorbent is selected from the group consisting of zeolite X,
zeolite Y, zeolite A, silica gel, silicas, aluminas, and mixtures
thereof More preferably, the adsorbent is selected from the group
consisting of zeolite Y-54, zeolite Y-74, zeolite Y-84, zeolite
Y-85, steam condensed rare earth exchanged Y-54, low cerium rare
earth exchanged Y-84, low cerium rare earth exchanged zeolite
LZ-210, zeolite DDZ-70 and mixtures thereof. Most preferably, the
adsorbent is selected from the group consisting of zeolite Y having
a trivalent cation in the .beta.-cage of the zeolite structure. The
adsorbent layer may be formed by conventional coating methods such
as slip coatings, dipping, spray coating, curtain coating, and
combinations thereof. One preferred method of forming an adsorbent
layer on the fm plate is by applying a layer of adsorbent paper
such as disclosed herein above wherein the paper contains the
adsorbent in a uniform layer. The adsorbent paper layer may be
laminated to the fin plates by any means such as a heat and
moisture resistant adhesive-like epoxy. By applying the adsorbent
layer to the fm plate prior to assembly of the sorption heat pump
module, the build-up or flooding of adsorbent at the root where the
tube contacts the fin plate is avoided. Typically, the adsorbent
paper layer has a thickness of between about 0.25 and about 0.6 mm.
For layers of this thickness, stacked arrangements of fin plates
having from about 300 to about 800 fin plates per meter of tube
length may be assembled. The arrangements of fin plates in each of
the embodiments of the present invention is optimized for heating
power and cost factors. In particular, the fin thickness, fm
material, and fin spacing as well as the thickness of the adsorbent
layer are optimized to minimize the cost while maximizing the
performance of an adsorption heat pump. Fins that are thicker than
the optimal thickness will not provide the desired heat transfer.
The fms need to be properly spaced for ease of refrigerant flow.
One optimal arrangement consisted of 0.31 mm (0.012 inch) thick
aluminum fms with 0.51 mm (0.02 inch) thick adsorbent media.
[0031] FIG. 2 shows a pair of the single-sided laminates of FIG. 1
oriented so that the substrate layers 12 are facing within each
pair of single-sided laminates. A heat transfer channel 16 is
between each pair of single-sided laminates.
[0032] FIG. 3 shows an alternate embodiment of the invention
wherein two single-sided laminates are corrugated and then mated
together to form flow channels for a refrigerant within a
subassembly 20. The subassembly 20 that is formed is sealed at two
or three of the four edges. Sealed edges 22, 24 are shown. In the
perspective shown in FIG. 3, a heat transfer fluid would flow in
and out of the plane as shown in a heat transfer passage 26. In the
embodiment shown, the uncoated substrate layer 12 is on the
interior of the subassembly 20 and the adsorbent-containing layer
14 is on the outside of the subassembly 20 as shown.
[0033] FIG. 4 shows a view of the subassemblies 20 of FIG. 3
arranged into an assembly 30. The subassembly 20 has been turned so
that the flow path of the heat transfer fluid is now across the
side having the adsorbent layer. Arrows show the direction of flow
of the heat transfer fluid. An inlet header 32 and an outlet header
34 mate and seal to openings at both ends of subassembly 20 and
allow for flow of heat transfer fluid up the headers and across
inside surfaces of subassembly 20. In a heat pump, the entire
assembly displayed in FIG. 3 is placed inside a vacuum vessel and
spaces 36 between the subassemblies 20 contain the refrigerant that
also fills the open portions of the vacuum surrounding the
assembly. The primary surface area for heat transfer is the entire
inside surface of all the subassemblies 20.
[0034] FIG. 5 shows a double-sided laminate 40 that comprises a
single sheet 42 of a base material, such as aluminum and layers 44,
46 of a zeolite matrix bonded to each opposing surface of the base
material.
[0035] FIG. 6 shows a special arrangement of the double-sided
laminate of FIG. 5 where there are gaps 48 in the layers 44, 46 so
as to allow for corrugation that will leave uncoated (nonlaminated)
sections of the base material exposed. The presence of these gaps
allows for bonding of the nonlaminated sections of the laminate to
the outside surface of a heat transfer passage.
[0036] FIG. 7 shows how the gaps 48 are mated to outside surfaces
52, 54 of heat transfer fluid passages in a unit 56. A refrigerant
58 is shown flowing next to the laminate. The double-sided laminate
of FIG. 6 is shown in a corrugated pattern to maximize surface
area.
[0037] FIG. 8 shows how the repeating units of a heat transfer
passage with fin stock bonded to the outside surfaces of the heat
transfer passage as in FIG. 7 are stacked to form an entire heat
exchanger. An inlet header 62 and an outlet header 64 are shown for
flow of the heat exchange fluid to the heat transfer fluid passages
of unit 56. This design combines the advantage of large fm surface
with the compact style heat exchanger that has a large primary
surface area. In one embodiment of FIG. 8, the metal layers are
aluminum plates that have been anodized to prevent any potential
corrosion reactions with water. The anodizing step is carried out
prior to the lamination and assembly of the heat exchanger
core.
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