U.S. patent number 3,732,919 [Application Number 05/051,650] was granted by the patent office on 1973-05-15 for heat exchanger.
Invention is credited to Joseph R. Wilson.
United States Patent |
3,732,919 |
Wilson |
May 15, 1973 |
HEAT EXCHANGER
Abstract
A heat exchanger has wall means defining an enclosed space, at
least one extending surface heat transfer member defining in
cooperation with the wall means at least two flow channels in the
enclosed space separated by the heat transfer member and contiguous
particles packed in at least one of the channels to rigidly support
the walls of the channel while permitting fluid flow through said
channel.
Inventors: |
Wilson; Joseph R. (Vienna,
OE) |
Family
ID: |
21972567 |
Appl.
No.: |
05/051,650 |
Filed: |
July 1, 1970 |
Current U.S.
Class: |
165/110; 165/166;
165/180; 165/905; 165/907; 261/DIG.72 |
Current CPC
Class: |
F28D
9/0025 (20130101); F16L 9/00 (20130101); F28F
13/003 (20130101); Y10S 261/72 (20130101); Y10S
165/905 (20130101); Y10S 165/907 (20130101) |
Current International
Class: |
F16L
9/00 (20060101); F28D 9/00 (20060101); F28F
13/00 (20060101); F28f 003/00 () |
Field of
Search: |
;165/104,164,165,166,167,150,152,153,110,45,180 ;62/DIG.7 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Davis, Jr.; Albert W.
Claims
I claim:
1. A heat exchanger comprising wall means defining an enclosed
space, at least one thin wall non-pressure carrying extended
surface heat transfer sheet member defining in cooperation with
said wall means at least two flow channels, one of said flow
channels comprising a condenser channel normally operating at a
lower pressure than the pressure in said enclosed space, means
supporting the thin wall sheet member and maintaining the flow
channels including the low pressure condenser channel in rigid
formation, said supporting means comprising contiguous particles
packed in at least the low pressure condenser channel while
permitting fluid flow through the channels.
2. A heat exchanger comprising wall means defining an enclosed
space, at least one thin wall non-pressure carrying extended
surface heat transfer sheet member defining in cooperation with
said wall means at least two flow channels, one of said flow
channels normally operating at a lower pressure than the pressure
in said enclosed space, means supporting the thin wall sheet member
and maintaining the flow channels in rigid formation, said
supporting means comprising contiguous particles packed in at least
the low pressure channel while permitting fluid flow through the
channels.
3. A heat exchanger comprising wall means defining an enclosed
space, at least one thin wall non-pressure carrying extended
surface heat transfer sheet member defining in cooperation with
said wall means at least two flow channels, one of said flow
channels comprising a condenser channel normally operating at a
lower pressure than the pressure in said enclosed space, means
supporting the thin wall sheet member and maintaining the flow
channels including the low pressure condenser channel in rigid
formation, said supporting means comprising contiguous particles
packed in said channels and said enclosed space while permitting
fluid flow through the channels.
4. A heat exchanger as defined in claim 2 comprising a pair of
folded thin wall extended surface heat transfer sheet members in
spaced relation and defining in cooperation with said wall means
two or more flow channels in said space.
5. A heat exchanger as defined in claim 2 wherein more than one
flow channels are operating at the lower pressure than are other
flow channels and each of the flow channels operating under the
lower pressure are packed with the contiguous particles.
6. A heat exchanger as defined in claim 2 wherein the contiguous
particles are generally spheroidal and of uniform size.
7. A heat exchanger as defined in claim 6 wherein the contiguous
particles are generally in a square pitch pack.
8. A heat exchanger as defined in claim 6 wherein the contiguous
particles are generally in a triangular pitch pack.
Description
BACKGROUND OF THE INVENTION
1. Field of the Invention:
The present invention generally appertains to new and novel
improvements in heat exchangers and more particularly relates to
new and novel improvements in the heat transfer surface
construction of heat exchangers.
2. Description of the Prior Art:
Conventional heat exchangers are constructed from shells and tubes
or pipes and such shell and tube exchangers have a long history of
successful operation. They have many advantages, such as ease of
cleaning and repairing, and are in widespread use. However, in
spite of the many advantages and wide acceptance of such shell and
tube exchangers, there are a number of problems associated with
their design, manufacture and use. Some of the most serious of
these problems are:
1. The joints in such exchangers are expensive to make and are not
entirely dependable, since they have a tendency to leak. The
integrity of the joints depends upon the physical properties of the
tube material and upon the skill of the assembler with the range of
useful tube materials being limited and assembly and repairs being
expensive.
2. The tube walls must be at least thick enough to withstand the
pressure, resist corrosion and establish a good tube/sheet joint
which, therefore, sets a minimum wall thickness for various
materials. This adds to the cost of fabrication and repair.
3. The tubular exchanger is basically a cross-flow unit with
baffles being required to redirect the shell-side fluid back and
forth across the bundle in order to achieve counter-flow between
the fluids. As a consequence, there are many mechanical joints
between the tubes and the baffles and such encounter vibration
damage.
4. The range of velocities which can be accommodated is limited,
with many times multi-pass arrangements being necessary to obtain
the desired fluid velocities.
SUMMARY OF THE INVENTION
The present invention envisions the design and construction of heat
exchangers and heat transfer devices from sheet material which is
far less expensive than tubes, pipes and shells. The sheet material
forms the boundaries for flow channels with at least one of the
channels being packed tightly with packing material comprising
particles of generally uniform and preferably spherical size and
shape. The fluid pressure inside such packed but fluid-traversable
channel will be less than the fluid pressure in the adjacent
unpacked and unobstructed channel with the packing supporting the
walls of the flow channel against the external pressure. The
supported sheet material constitutes a heat transfer member that
can be fashioned into a variety of flow channel shapes and
forms.
Of course, the flow path through the packed channel will be
tortuous and the fluid velocities must be kept low to avoid
excessive pressure drop. Therefore, the supported surface exchanger
is particularly useful where the heat transferred from a unit
volume of fluid in the packed channel is high as compared to the
heat transferred to a unit volume of fluid in the unobstructed
channel. Such situations regularly exist where a phase change is
occurring in the packed channel as in condensing or boiling, and
where heat is exchanged between a gas in the unobstructed channel
and a liquid in the packed channel. Condensers, evaporators and
liquid-air type exchangers are typical general applications.
Several applications which have been recognized as being
particularly attractive are multi-stage flash evaporator for
seawater desalting, vertical packed channel evaporator for seawater
desalting, water/air exchangers for ` dry ` cooling towers and
water coolers, corrosive fluid exchangers and fluid
concentrators.
As mentioned above, there is a significant material cost advantage
presented by the sheet material concept of the supported heat
transfer surface, according to this invention. In addition, the
sheet material of the supported heat transfer surface is not a
pressure carrying member but simply transfers pressure to the
supporting and packing particles. In contradistinction, the tube
wall in a tubular exchanger must be sufficiently thick to withstand
the pressure differential, withstand corrosion and have sufficient
material to provide a good joint with the tube sheet. With the
sheet material, there will be no tube sheet joints. While the sheet
material must withstand corrosion, the thickness of the sheet
material can in most cases be much less than the tube wall
thickness of corresponding tubular exchangers. In such tubular
exchangers the tubing material must have sufficient ductility so as
not to crack or split when the tube is rolled into the tube sheet.
It must have a yield strength which can facilitate the rolling-in
process. On the other hand, the supported heat transfer surface
sheet material does not have to meet stringent yield, ductility and
high-strength requirements and a variety of materials which are not
suitable for tubular exchangers can be used as the materials for
the present invention. In fact, plastics or other materials, which
have special qualities such as corrosion resistance or very low
cost, can be used because of their cost and process advantages.
Tube sheet joints are expensive to make and tube sheets, baffles
and tube supports are also expensive. Consequently, the cost per
square foot of a completed tube bundle is almost twice the cost of
the initial tube. With the present invention, the supported heat
transfer surface requires only a minimum of welds, bends and
forming and its fabrication costs are well below that of tube
bundles, which require skilled labor in their layout. With the
supported heat transfer surface simple machinery can be used in the
fabrication, such as sheet metal breaks and automatic welders and
less skilled labor can produce the units in less time than required
in the fabrication of the usual tubular exchangers.
While the particles are primarily intended to serve a structural
function with external pressure being transmitted to the packing
constituted by such particles, it is envisioned that such particles
can contribute to the transfer of heat, and depending upon
conditions, such contribution may be substantial and important.
Generally, however, the material of the particles depends upon
availability. Such materials as coarse sand, smooth gravel or
spherical pellets of concrete, plastic or ceramic may be used,
providing they are unaffected by the heat transfer fluids and are
strong enough to resist crushing and erosion.
Selection of the composition of the heat transfer sheet material
will be based upon the service and operating conditions. Sheet
material thickness should generally be based on pressure
differential, cost, strength, handling ease and corrosion and
erosion requirements. Typical thicknesses of the heat transfer
sheet material may be in the range from about 10 to about 30 mils.
Since strength of the sheet material is less important than is tube
wall strength in conventional tubular exchangers, it may be
economical to use a thinner but more noble material. For example,
it may be desirable to use thin titanium sheets to construct
desalting equipment. In exchangers operating at less severe
temperature and pressure conditions plastic sheet material may be
employed and, for highly corrosive services, materials such as
Teflon sheet may be advisable.
Thus, the primary object of the present invention is to provide a
heat exchanger or heat transfer device wherein the channels for the
flow of fluids therethrough are formed from sheet material with
certain of the channels being packed with particles that permit
flow of fluid therethrough while rigidly supporting the walls of
the channels against external pressure.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a top plan view of a fluid-fluid counterflow heat
exchanger constructed in accordance with the principles of this
invention;
FIG. 2 is a side elevational view of the exchanger of FIG. 1;
FIG. 3 is a transverse vertical sectional view taken on line 3--3
of FIG. 1;
FIG. 4 is an end elevational view of the exchanger of FIG. 1;
FIG. 5 is a transverse vertical sectional view taken on line 5--5
of FIG. 4;
FIG. 6 is a horizontal, cross-sectional view taken on line 6--6 of
FIG. 2;
FIG. 7 is an enlarged perspective showing of the interior sealing
and closure structure of the exchanger shown in FIG. 1;
FIG. 8 is a fragmentary enlarged side view of a portion of the
packed channel showing the packing particles in elevation;
FIG. 9 is a detailed elevational view of the packing particles
arranged in a square pitched pack;
FIG. 10 is a sectional view taken on line 10--10 of FIG. 9;
FIG. 11 is a detailed elevational view of the packing particles
arranged in a triangular pitched pack;
FIG. 12 is a sectional view taken on line 12--12 of FIG. 11;
FIG. 13 is an enlarged detailed perspective view of a fragmentary
portion of the channel structure of the exchanger, showing the
packed and unpacked channels with the latter lying between the
illustrated packed channels;
FIG. 14 is a side elevational view of a condenser formed in
accordance with this invention and embodying the concept of the
packed channels thereof;
FIG. 15 is a transverse vertical sectional view taken on line
15--15 of FIG. 14;
FIG. 16 is a side elevational view of a counterflow heat exchanger
constructed in accordance with the principles of the present
invention and embodying the concept thereof; and
FIG. 17 is a transverse vertical sectional view taken on line
17--17 of FIG. 16.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
Referring now more particularly to the accompanying drawings and
initially to FIGS. 1 to 7, the reference numeral 10 generally
designates a fluid-fluid counterflow heat exchanger embodying the
principles of the present invention. The exchanger 10, as shown
especially in FIG. 3, is formed from sheet material and includes a
bottom wall sheet member 12, a U-shaped cover or container wall
member 14 and a corrugated sheet member 16 which is the heat
transfer member. The bottom plate or wall 12 serves as the bottom
of the exchanger and is provided at opposite ends with transversely
extending trench-like headers 18 and 20 that constitute the inlet
and outlet headers and to which connections 22 of a suitable type
are attached.
The bottom plate 12 has side edge flanges 24 that complement the
laterally outstanding side edge flanges 26 provided on the side
walls 28 of the cover member 14 with such flanges being secured
together by bolt assemblies 30. The intermediate corrugated sheet
member 16 also has outermost side walls 32 and 34 provided with
lateral edge flanges 36 which are positioned between the flanges 24
and 26 and clamped therebetween by the bolt assemblies 30 so as to
mount the sheet member in place.
The sheet member 16 is a thin wall extended surface sheet that is
formed in serpentine fashion with a number of parallel loops or
bends 38 each defined by parallel spaced apart walls 40 and 42
closed at their lower ends 44 by closed integral bight portions or
arcuately closed ends 46 and being open at their upwardly facing
open upper ends 48 which are spacedly confronted by the overlying
top wall 50 of the cover sheet 14. The zig-zag arranged and formed
loops or bends 38 extend spacedly from the top wall 50 of the cover
sheet to the bottom plate 12 and define channels 52 with the cover
member and channels 54 with the bottom plate, as can be appreciated
from FIG. 3. The channels 52 are open to the cover member and
closed to the bottom plate while the channels 54 are open to the
bottom plate and closed to the cover member or sheet 14.
The adjoining front and rear edges of the side by side spaced apart
walls of adjoining bends or loops 38 are seam jointed or welded
together, as at 56 in FIG. 6, so that they cooperate to form the
closed ends of the channels 54 which are only open to the headers
for the flow of for example a condensible gas or condensed liquid
therethrough with warm gas or liquid entering the inlet header 18
and cool liquid leaving the outlet header 20. The condensible
liquid is cooled in its passage between the headers by air flowing
through the channels 52 in a path longitudinally of the exchanger
10. Screens or the like 19 are positioned at the top of the inlet
header 18 and the outlet header 20 to restrict the particles to the
packed channels 54 while permitting fluid to pass freely from the
inlet header 18 to the packed channels 54 and hence to the outlet
header 20.
The condenser channels 54 are packed with particles 58 that support
the sheet 16 on its inside or on the low pressure side thereof with
the packing particles supporting the walls of the flow channels 54
against the external pressure of the air flowing in the channels
52. The fluid pressure in the air flow channels 52 is greater than
the fluid pressure in the adjacent condenser channels 54.
Two supported and adjoining channels 54 are shown in FIG. 13 in
relation with an intermediate unobstructed flow channel 52 with the
particles 58 being packed into the channels 54 so as to support the
thin wall sheet 16 and maintain the rigid formation of the low
pressure channels 54. The particles, as will be more particularly
described, are spherical in shape and may be packed in a particular
formation so as to present a uniform flow path through the channels
54. As shown in FIG. 13, the fluid pressure within the packed
channels 54 of width S is less than the fluid pressure within the
unobstructed channel 52 of width W. Since the packing is tightly
packed within the flow channels 54 of width S, the differential
pressure actually presses the packed channels into very rigid form.
Furthermore, the pressure differential can be substantially greater
than could be supported by a tube of diameter S and tube-wall
thickness T.
The packing material can be of many forms. As illustrated, the
particles 58 are solid ball elements formed from ceramic or
concrete. The particles are preferably generally spherical and of
uniform size. Non-uniform size particles will tend to pack more
solidly and reduce the porosity or flow characteristic of the
channels 54. Glass or plastic beads may be used as well as screened
coarse sand particles and pebbles. The size of the particles is not
critical but, in general, particles of one-tenth to one-half inch
in diameter are preferred.
Various packing arrangements of the spherical packing particles or
elements 58 may be utilized. For example, as shown in FIGS. 9 and
10, the particles or spherical elements 58 are packed in the square
pitched pack 60. In FIGS. 11 and 12, the particles or spherical
elements 58 are arranged tightly in a triangular pitched pack 62.
In either of such arrangements or in any other packed arrangement,
the particles are held tightly against accidental shifting and
rigidly support the thin walled extended surface sheet 16. The
particles primarily serve the function of supporting the extended
surface sheet 16 but may also contribute to the transfer of heat as
a secondary function.
The dimensions of S and W can be varied and adjusted to achieve a
number of desirable characteristics, i.e. different channel flow
areas and hence different velocities, heat transfer coefficients
and pressure drops. Thus, S or W can be varied from point to point
where a wider channel is formed to distribute the fluid more evenly
into the lower flow channels 54. It should also be noted that
various designs, such as fluted surfaces, can be embossed or formed
on the sheet member 16 to enhance the heat transfer properties of
the supported surface sheet 16. The folded sheet member 16 can be
fashioned into a variety of flow channel shapes and many kinds of
heat exchangers can be formed from these shapes.
The dimensions S and W can be varied at any point in the exchanger
provided that their sum is maintained constant. However, if the
outside dimensions of the exchanger are varied appropriately, the
sum of W and S need not be kept constant. Thus, the flow paths or
channels for the two fluids can be varied to suit conditions.
The width of the flow space W, as shown in FIG. 13, between the
packed channels S typically could be about one-half inch although
it may be several times larger or smaller than this value. The
hydraulic radius and hence the heat transfer and hydraulic
characteristics of the flow channel are similar to those of a tube
or pipe with a diameter of twice W.
The width S of the packed spaces, as shown in FIG. 13, between the
sheet material of the heat exchanger should be such that fluid
velocities within these spaces are reasonable. The porosity or
fluid traversability of such spaces will vary between 10 and 40
percent depending upon the nature of the packing and its approach
to perfect spherical shape. Typically, the width of the space S
could also be about one-half inch.
The packing particles should be of uniform size and generally
spherical. Non-uniform size particles will tend to pack more
solidly and reduce the flowability characteristic or porosity of
the packed spaces since the smaller particles, in such case, would
tend to fill the voids between larger particles. Thus would not be
desired in most cases. As shown in FIGS. 9 and 11, the uniform
spheres can be packed in packing arrangements of square pitch pack
and triangular pitch pack, such being illustrative of types of
packing arrangements. Usually three to six layers of particles
would be typical. Thus, for example, when W is one-half inch in
width, the particles would range from about one-fifth inch diameter
(three layers) to one-tenth inch diameter (six layers).
In FIGS. 14 and 15, an alternate arrangement is shown wherein the
condenser 64 has a vapor inlet 66 and a liquid outlet 68 with the
vapor/liquid flowing in the unobstructed tortuous channel 70, the
air flow channels 72 being filled with tightly packed particles
that support the channel defined by a pair of spaced extended
surface sheets. The packed particles are maintained in the desired
location by screen or the like end walls 80 which while maintaining
the particles within the device do not materially restrict the flow
fluid therethrough. In FIGS. 16 and 17, a counterflow heat
exchanger 74 is shown with the same having unobstructed fluid flow
channels 76 and particle air channels 78 defined by the supported
extended surface sheet member 79.
* * * * *