U.S. patent number 3,724,523 [Application Number 05/050,752] was granted by the patent office on 1973-04-03 for tubular structure for film evaporators.
This patent grant is currently assigned to Metallgesellschaft Aktiengesellschaft. Invention is credited to Konrad Mattern.
United States Patent |
3,724,523 |
Mattern |
April 3, 1973 |
TUBULAR STRUCTURE FOR FILM EVAPORATORS
Abstract
A tube-bundle evaporator through the interior of the tubes of
which the liquid to be evaporated is passed. The tubes are deformed
so that the flow cross-section increases longitudinally in the
direction of flow of the vapor while the perimeter or peripheral
extent of the tube and, preferably, the diameter of the smallest
circumscribing circle remains constant over the entire length of
the tube.
Inventors: |
Mattern; Konrad (Bad Homburg,
DT) |
Assignee: |
Metallgesellschaft
Aktiengesellschaft (Frankfurt am Main, DT)
|
Family
ID: |
21967201 |
Appl.
No.: |
05/050,752 |
Filed: |
June 29, 1970 |
Current U.S.
Class: |
159/13.2;
159/28.1; 165/177; 159/14; 165/147 |
Current CPC
Class: |
F28F
1/06 (20130101); B01D 1/22 (20130101); F28F
13/08 (20130101) |
Current International
Class: |
B01D
1/22 (20060101); B01d 001/22 (); B01d 001/00 ();
F28f 013/08 (); F28f 001/00 () |
Field of
Search: |
;159/13A,13B,28,28VH
;165/146,147,172,177 ;138/177 ;202/236 ;203/89 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
|
|
|
|
|
|
|
1,159,879 |
|
Oct 1956 |
|
FR |
|
1,159,878 |
|
Feb 1958 |
|
FR |
|
Primary Examiner: Yudkoff; Norman
Assistant Examiner: Sofer; J.
Claims
I claim:
1. A tube structure for an evaporator, comprising at least one tube
traversed internally by a vaporizable liquid and heated by a fluid
in contact with the exterior of said tube, said tube being formed
internally having equal-diameter cylindrical end portions and
between said end portions with a plurality of rectilinear,
angularly equispaced troughs deformed from the tube wall extending
along the tube and defining a flow cross-section of the tube
increasing substantially linearly over the distance between said
end portions and defining a direction of flow of fluid from the
small to the large cross-section whereby the flow velocity through
the tube is maintained substantially constant, said troughs having
arcuate floors lying on a circle of the same diameter as said end
portions whereby said tube is circumscribed by a circular cylinder
of substantially constant diameter over its entire length, said
troughs flooring from said small cross-section to said large
cross-section.
2. The tube structure defined in claim 1 wherein at least three
angularly equispaced troughs are provided about said axis.
3. The tube structure defined in claim 1 wherein said troughs in
cross-section each have a pair of parallel sides and the sides of
neighboring troughs include angles of substantially
(360.degree./N), where N equals the number of troughs.
4. The tube structure defined in claim 1, further comprising a pair
of tube sheets at opposite ends of said tube and secured to said
end portions.
5. The tube structure defined in claim 1 wherein four such troughs
are provided at the vertices of a star centered on the axis of the
tube.
6. The tube structure defined in claim 1 wherein three such troughs
are provided at the vertices of a star centered on the axis of said
tube.
Description
1. FIELD OF THE INVENTION
My present invention relates to evaporators and, more particularly,
to heat-exchange devices for the evaporation of liquids.
2. BACKGROUND OF THE INVENTION
A large number of evaporators, refluxers, boilers and vaporizers
have been provided heretofore in accordance with fluid-fluid
heat-exchange principles whereby a liquid to be evaporated is
brought into contact with one surface of the heat exchanger while a
heating liquid is brought into contact with another heat exchange
surface in heat-exchange relationship with the first.
The device, therefore, may be an indirect heat exchanger having
passages for the heating fluid and for the vaporizable liquid,
separated by a thermally conductive wall through which the heat
exchange is effected. Such heat exchangers are used for a wide
variety of purposes and, for example, in low-temperature systems,
they may be used for vaporizing a liquefied gas or a refrigerant,
while in chemical technology generally, they may be used for
concentration of liquids, drying of slurries, production of vapors
or the like.
The present invention is concerned with tube-bundle evaporators
which, while operating in accordance with the above-described
principles, generally define the passages traversed by the
vaporizable liquid by tubes extending parallel to one another and
constituting a tube bundle. An evaporator of the latter type can
comprise, therefore, a plurality of generally parallel tubes fixed
at their ends in a pair of tube sheets, the latter being welded or
clamped in a housing which includes a pair of end domes or closures
defining manifold chambers communicating with the respective ends
of the tubes at the point at which the tubes terminate in the
respective tubing sheets. The casing or housing surrounding the
tubes by the sheets defines a compartment traversed by the heating
fluid which, therefore, passes through the interstices between the
tubes. A structure of this type can have a wide variety of
configurations and will be referred to hereinafter as a tube-bundle
heat exchanger.
It is important at this point to note that evaporators are also
classified by the orientation of the tubes and the manner in which
the liquid to be evaporated is fed to the tube bundle. For example,
the tubes may be oriented in either vertical of horizontal
direction and, while it will be apparent hereinafter that the
orientation is not critical for the purposes of the present
invention, it nevertheless is preferred to apply the invention to
vertical-tube evaporators. The liquid-feed direction is significant
as well and, I may observe, the invention is applicable to both
falling-film or climbing-film evaporators. In a falling-film
evaporator, the liquid to be vaporized falls downwardly along the
surface of the tube and is supplied to the tube bundle from above.
Conversely, the liquid of a climbing-film evaporator moves upwardly
along the tube wall from below.
In conventional evaporator tubes, i.e., the tubes of tube-bundle
evaporators of the falling-film or climbing-film and vertical-tube
types, the interior of the tube has a constant diameter and
cross-section and, since the vapor is formed only after the liquid
has been heated to the boiling point, the velocity of the vapor at
the liquid-inlet is initially zero but rises to a maximum at the
exit end of the tube. In tubes which are supplied with liquid at
their lower ends, the increasing formation of vapor as the liquid
rises produces vapor bubbles which frequently block the rise of
liquid beyond a certain point. As a result, the laminar flow of
liquid along the tube wall, i.e., the existance of a liquid film,
is possible only in the lower portions of the tubes and,
consequently, the heat-exchange characteristics between the heating
fluid and the liquid vary along the tube length. The increase in
heating beyond the stable liquid film gives rise to concentrated
evaporation and, therefore, encrustation of the heat-exchange
surfaces within the tube with solids deposited as a consequence of
the non-uniform evaporation.
In falling-film evaporators, i.e., vertical tube evaporators in
which the tubes receive liquid from above, it is desirable that the
film of vaporizable liquid descend along the inner walls of the
tubes in a uniform fashion. At the upper or inlet ends of the
tubes, the vapor velocity is, of course, zero and the vapor
velocity increases to a maximum at the outlet or lower ends of the
tubes. However, even this system has significant disadvantages.
Firstly, the formation of vapor bubbles near the inlet end of the
tube tends to create vapor layer in laminar flow along the heat
exchange surface, the vapor layer, deflecting the incoming liquid
away from the walls of the tube and forming a strand of the liquid
through the center of the tube. This coherent liquid filament,
thread or strand may remain out of contact with tube wall over
virtually its entire period of passage through the tube. Hence this
strand of liquid is not subjected to evaporation, while residual
liquid films along the surface of the tube are overheated and have
a tendency to vaporize without concentration of solids within the
body of the remaining liquid, thereby promoting encrustation and
contamination of the tube surface. Furthermore, since the laminar
gas flow is not a problem in regions at which turbulence occurs to
break up this cushion, the heat exchange through the tube walls is
irregular and often unpredictable. In fact, only at those tube
portions at which turbulent flow occurs is the liquid to be
evaporated permitted to contact the heating surface of the tube and
is the formation of crusts and the like reduced.
These disadvantages have long plagued the evaporator art and
numerous suggestions have been made to eliminate them. For example,
it has been proposed to provide deflectors, agitators and other
means for generating turbulence or providing centrifugal force to
return the vaporizable liquid to a heating surface. Such means
have, however, proved to be of limited suitability, not only
because of their high initial and operating costs, but also because
they have found to be ineffective for many types of evaporation. It
has also been proposed to provide tubular inserts within the heat
exchange tubes, thereby increasing the velocity of the liquid or
gas traversing the tubes and promoting turbulence in accordance
with the Reynold's effect. However, even this represents a cost
increase and provides a large surface which is ineffective in the
heat exchange so that a great deal of the liquid traversing the
tube is used to wet the surface of the insert and the concentration
of the remaining liquid, i.e., the liquid in contact with the
heating surface is proportionally increased. This represents a
greater danger of soiling and encrustation.
3. OBJECTS OF THE INVENTION
It is, therefore, the principal object of the present invention to
provide an improved tube construction for a tube-bundle evaporator
of the character described.
Another object of this invention is to provide a tube-bundle heat
exchanger of the falling-film or climbing-film type which is free
from the disadvantages of earlier heat exchangers using uniform
cross-section tubes and yet can be made at low cost.
It is also an object of the invention to provide an efficient
evaporator tube structure which eliminates the need for centrifugal
and other turbulence-inducing devices and yet is capable of
eliminating the disadvantages of climbing-film or falling-film
evaporators of prior-art constructions.
4. SUMMARY OF THE INVENTION
These objects and others which will become apparent hereinafter are
achieved, in accordance with the present invention, with a tube
construction for a tube-bundle evaporator, preferably of the
falling-film or climbing-film type, in which the tube over the
major part of its length spanning the tube sheets is formed
unitarily (be deformation) with a plurality of troughs radiating
from the center of the tube and of a flow cross-section which
increases longitudinally in the direction of flow of the vapor, the
peripheral extent of the tubes remaining constant over the tube's
length. The term "peripheral extent" is used here to describe the
perimeter of the tube in a cross-sectional plan perpendicular to
the tube axis. The troughs or grooves, which should be at least
three in number, collectively open into the interior of the tube at
which flow remains unobstructed. As a result, the cross-section of
the tube viewed from the liquid-inlet end is at a minimum, but
increases progressively and preferably linearly with the distance
from the liquid inlet end to the liquid outlet end at which the
flow cross-section corresponds to the cross-section A = .pi.R.sup.2
where R is the radius of the interior of the cylinder tube. The
perimeter of the tube, regardless of the flow cross-section is
given by P = 2.pi.(R + .DELTA.R) where .DELTA.R is the thickness of
the tube. At the liquid-inlet end of the tube, the flow
cross-section may approach zero but is preferably a small fraction
of the maximum cross-section of the tube, i.e., (A/20) to
(A/3).
According to an important feature of the present invention, the
walls of the troughs or grooves are parallel to one another, i.e.,
each trough in cross-section is defined between a pair of parallel
sides lying on these walls, these sides being parallel to an axial
plane passing centrally through the representative trough and lying
midway between these walls. Furthermore, the walls of adjacent
troughs include angles of about (360.degree./N), where N is the
number of angularly equispaced troughs (preferably N = 3 or 4). I
have found it to be desirable to provide free-end portions of the
tubes which are of cylindrical configuration and free from the
troughs to enable the tubes to be fitted or joined to the tube
sheets at the liquid-inlet and outlet ends of the tubes and to
deform the troughs from the walls of a cylindrical tube by spinning
or drawing. As a result, it is possible to create a tube
construction in which the circle of smallest diameter which can
circumscribe the tube at any of its star-shaped cross-sections will
correspond to the outer diameter of the original tube. The
cross-section of the tube is preferably selected so that the vapor
formed in the tube flows at a uniform velocity throughout its
length.
If the tubes are formed by spinning with troughs having sidewalls
which diverge at an angle, say, of 120.degree., it is possible
theoretically to collapse the shell of the tube so that the inside
surfaces of the inwardly deformed generally segmental portions
contact one another and eliminate a free cross-section between
them. The system of the present invention is operative even where
the free cross-section of the troughs initially is zero, the fluid
thus passing through the central opening in the initial stages. In
all of the preferred constructions, the tube will be of star-shaped
profile with the vertices of the outermost points lying on the
circumference of the original tube, i.e., on the circumscribing
circle or a circle centered on the tube and of a circumference
equal to the perimeter of the tube. The peripheral extent or
perimeter of the tube, however, remains constant over its entire
length. In practice, the tube is collapsed at its inlet end so that
a star-shaped free cross-section is left in the tube and the tube
walls have a clearance from one another of 1 to 3 mm. The liquid to
be evaporated thus can enter the tube band be immediately subjected
to turbulent flow.
5. DESCRIPTION OF THE DRAWING
The above and other objects, features and advantages of the present
invention will become more readily apparent from the following
description, reference being made to the accompanying drawing in
which:
FIG. 1 is a vertical elevational view of a tube structure (and the
associated tube sheets) of a tube-bundle evaporator embodying the
invention and operating in accordance with falling-film
principles;
FIG. 2 is a cross-sectional view taken along the line II -- II of
FIG. 1;
FIG. 3 is a section taken along the line III -- III of FIG. 1 and
showing that portion of the tube having the smallest
cross-section;
FIGS. 4 - 7 are cross-sectional views taken along the lines IV --
IV to VII -- VII, respectively; and
FIG. 8 is a cross-sectional view along the line VIII -- VIII of
FIG. 1 illustrating the region in which the tube is of maximum flow
cross-section;
FIG. 9 is a vertical elevational view of a tube according to the
invention operating under the principles of a climbing-film
evaporator;
FIGS. 10 - 16 are sections taken generally along the lines X -- X
to XVI -- XVI, respectively; and
FIG. 17 is a section through a tube according to another embodiment
of the invention.
6. SPECIFIC DESCRIPTION
In FIG. 1, I show a falling-film evaporator in which the heating
and evaporating tube 3 is anchored in the tube sheets 1 and 2 of
the evaporator, the tube sheets being only fragmentarily
illustrated in this drawing. Above the tube sheet 1, therefore, the
usual housing (not shown) may define an inlet chamber A to which
the liquid is supplied, the liquid being distributed to the upper
ends of the tubes 3 of the tube bundle. Around the tubes 3, between
the tube sheets 1 and 2, the housing defines a chamber B provided
with the usual conduits for supplying a heating fluid to the
interstices between the tubes of the tube bundle. Below the tube
sheet 2, the housing defines a chamber C to which concentrated
liquid is removed.
The circular top ends of the tubes 3 are rolled into the upper tube
sheet 1 and the tubes are formed by spinning with three troughs 7,
8 and 9 which lie in radial planes of the tubes and angularly
equispaced about the axis 10. The walls 11 and 12 defining each of
the troughs 7 - 9 lie generally parallel to one another and to a
radial plane P through the respective trough and midway between the
sides 11 and 12 thereof. According to the principles of the present
invention, the sides 12 and 13 of adjoining troughs intersect at an
angle .alpha. = (360.degree./N) or 120.degree. where N = 3 as
shown. The radial extend r of each trough wall is slightly less
than R + .DELTA. R, where R is the internal diameter of the tube
(see FIG. 8) and .DELTA.R is the wall thickness thereof. The
circumferential width t of the trough initially is about 2 mm.
Furthermore, at each cross-section taken perpendicular to the axis
10, several of which are illustrated in FIGS. 2 - 7, the perimeter
of the tube is equal to the circumference of the cylindrical tube
(FIG. 8). Hence, the lengths of the sides 12 and 13 must be equal
to the arc length L between the two troughs.
In FIG. 2, I have shown a section in which the trough formations
are viewed from an end while FIG. 3 represents the initial
horizontal section. The troughs 7 - 9 progressively decrease in
depth so that a section taken at about one-fourth of the length of
the tube shows in FIG. 4 a corresponding increase of the flow
cross-section to about one-fourth of the circular section of the
tube as seen in FIG. 8. As the depth of the troughs is reduced, the
flow cross-section increases (preferably linearly) so that midway
along the tube the flow cross-section is about half of maximum
(FIG. 5) about three-fourths of the way along the tube, the flow
cross-section is about three-fourths of maximum (FIG. 6) and close
to the end of the tube (FIG. 7 the flow cross-section is
approximately equal to the maximum. The cylindrical end portions 14
and 15 of the tubes, of course, are free from the troughs and serve
to anchor the tube in the sheets 1 and 2.
In FIG. 17, I have shown a four-trough structure which is otherwise
similar to the embodiments previously described. Here, however, the
walls 17 and 18 of adjacent troughs include an angle .beta. =
(360.degree./N) where N = 4 and .beta. = 90.degree.. The walls 17
and 19 defining each of the troughs lie parallel to one another and
the troughs have their apices lying along a circle 20 corresponding
to the original tube circumference.
FIG. 9 shows a climbing-film evaporator, where a heating and
evaporating tube 3 is disposed between partly shown tube plates 1
and 2. The tube 3 is heated by steam, which is supplied to the
chamber defined by the tube plates 1, 2 and a shell, which is not
shown. The circular lower end of the tube is rolled into the lower
tube plate 2. By spinning, the tube has been formed with three
troughs so that the cross-section of the tube behind the rolled-in
portion is reduced to a fraction of the original cross-section of
the tube while gaps having a width of about 2 millimeters are left.
FIG. 16 illustrates a view taken into the tube. The periphery of
the three-pronged figure has the same peripheral extent as the
original tube. FIG. 15 is a horizontal transverse sectional view
taken through the tube 3 along line XV -- XV. FIG. 14 is a
sectional view taken through the tube along line XIV -- XIV at
about one-fourth of the length of the tube, where the cross-section
of the tube is about one-fourth of the original cross-section of
the tube. The cross-section increases continuously as the troughs
decrease in depth. FIG. 13 is a sectional view taken through the
tube along line XIII -- XIII at one-half of the length of the tube.
The cross-section of the tube is one-half of the cross-section of
the original circular tube. FIG. 12 is a transverse sectional view
taken through the tube along line XII -- XII at three-fourths of
the length of the tube, where the cross-section of the tube is
about three-fourths of the original cross-section of the tube. FIG.
11 is a sectional view taken along line XI -- XI shortly before the
termination of the troughs. FIG. 10 is a sectional view taken on
line X -- X through that portion of the tube which is rolled in the
tube plate 1 and has again the original circular cross-section.
7. SPECIFIC EXAMPLES
Example 1
The falling-film evaporator shown in FIG. 1 was used, which was
provided with heating and evaporating tubes having a length of 4
meters. The tubes had an inside diameter of 32 millimeters before
they were formed with the troughs and at various points of their
length, measured from top to bottom, had approximately the
following cross-sections in square millimeters:
Tube cross-section at one-fourth of tube length 200 Tube
cross-section at one-half of tube length 400 Tube cross-section at
three-fourths of tube length 600 Tube cross-section at the exit end
of the tube 800
Liquid containing 20 percent solids was fed into the tube 3 from
above at a rate of 36.7 kilograms per hour. The evaporating
temperature was 60.degree.C and the heating steam had a temperature
of 75.degree.C. After a single pass through the tubes of the
evaporator, the liquid had been evaporated to a solids content of
50 percent.
The heat transfer rate was about 2,000 kilocalories per square
meter/hour/.degree.C.
When water was evaporated at a total rate of 22 kilograms per hour,
the vapor velocity was uniform in all parts of the tube and
amounted to 58 meters per second.
Example 2
The climbing-film evaporator shown in FIG. 9 was used, which was
provided with heating and evaporating tubes 3 meters long. Before
the tubes were formed with the troughs, they had a diameter of 32
millimeters. At various points of their length, measured from
bottom to top, the tubes had the following cross-sections in square
millimeters:
At one-fourth of tube length 200 At one-half of tube length 400 At
three-fourths of tube length 600 At the exit end of the tube
800
Liquid having a solids content of 30 percent was fed into the tubes
at the boiling temperature at a rate of 40 kilograms per hour. The
tube was heated on the outside with steam. Water at a rate of 20
kilograms per hour was evaporated in the tube when the evaporating
temperature inside the tube was 60.degree.C and the heating steam
had a temperature of 75.degree.C on the outside surface of the
tube. The vapor produced in the tube forced the liquid to be
evaporated upwardly through the tube and had a virtually constant
velocity of 67 meters per second.
A single pass through the heating and evaporating tube produced
liquid at a rate of 20 kilograms per hour and water vapor at a rate
of 20 kilograms per hour. The resulting liquid had a solids content
of 60 percent.
* * * * *