Note: Descriptions are shown in the official language in which they were submitted.
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BACKGROUND OF THE INVENTION
The present invention relates to equipment and
processes for producing packaged beverages and more
particularly equipment and processes for combining two
or more constituent liquids in a desired ratio or
proportion.
Patented prior art relating to the type of
proportioned disclosed herein include the U.S. patents
to WIT et at 3,237,808 issued March 1, 1969, and Nikolai
et at 3,743,141 issued July 3, 1973.
SUMMARY OF TUB INVENTION
According to an aspect of the invention, A
proportioning apparatus for combining at least two
liquids in a determined proportion comprises:
a receiving chamber for each liquid;
a mixing chamber connected to said receiving
chambers,
an orifice interposed between each of said no-
ceiling chambers and said mixing chamber:
tank means connected to said mixing chamber:
first means for introducing gas under pressure
to said tank means:
second means for introducing gas to said receive
in chambers to pressurize the same at equal pressure:
and
pressure adjusting means responsive to pressure
changes in said tank means to alter the pressure in said
receiving chambers to maintain a constant pressure dip-
ferential between said tank means and said receiving
chambers.
According to another aspect of the invention, a
beverage proportioning apparatus for combining at least
two liquids in a selected proportion and intended for
use with an unlimited source of gas pressure; said
apparatus comprises:
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a receiving chamber for each liquid;
a mixing chamber connected to said receiving
chamfers;
an orifice interposed between each of said no-
ceiling chamber and said mixing chamber:
receptacle means connected to said mixing chamber:
and
adjustable gas pressure regulating valve means
connected to said source and to said receiving chambers
for reducing said source pressure to a selected pressure
and applying said selected pressure equally to said no-
ceiling chambers and to maintain a constant pressure
differential between said receiving chambers and said
receptacle means.
According to another aspect of the invention, a
proportioning apparatus for combining a plurality of
liquids, mixing said liquids in a deter- mined
proportion and depositing said mixed liquids in a
vessel at a controlled rate of flow comprises:
a plurality of discrete chambers for receiving the
individual liquids to be mixed;
means Pro introducing said liquids into said
discrete chambers;
a mixing chamber;
means connecting each said discrete chamber to
said mixing chamber whereby liquid may pass from said
discrete chambers to said mixing chamber;
means to receive said mixed liquids from said
mixing chamber;
means connecting said mixing chamber and said
receiving means; and
means for applying substantially equivalent
positive fluid pressure to said liquid in each of said
discrete chambers and for maintaining a controlled pros-
sure differential between said discrete chambers and
said receiving means whereby said liquids are forced
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under pressure from said discrete chambers, into and
through said mixing chamber and into said receiving
means at controlled rates of flow.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 shows the proportioned according to the
present invention connected to a cooler and
carbonating-cooler vessel, and
Figure 2 it an enlarged view of the proportioned.
Figure 3 is a fragment of a chamber containing a
constituent fluid and is a section, taken along the line
3-3 of Figure 4.
Figure 4 illustrates a chamber or receiving the
constituent fluids and a pressure response valve in one
conduit supplying fluid to the chamber, and
Figure 5 is similar to Figure 4 but the valving
element is operated by a linear actuator.
DESCRIPTION OF THE PREFERRED EMBODIMENT
The beverage mixing unit or proportioned
constructed in accordance with the principle of the
present invention is generally
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identified by the numeral 10. While more than two fluids can
be combined in any selected ratio, the operation of the disclosed
proportioned will be described by making reference to two fluids,
water and beverage syrup or concentrate.
Water conditioned for use as a beverage is introduced
in a pricklier and/or decorator tank 12 and by a conduit 14 which
is connected to a conduit 16. A diaphragm valve 18 operated
by a conventional level sensor 20, including a float 22,
controls the level of water in tank 12. Water from the tank 12
is pumped to a chamber 24 by a pump 26 through a conduit 28 which
is connected to a conduit 30. The quantity of water in
the chamber 24 is maintained substantially constant by a
diaphragm valve 32 operated by a level sensor 34 including a
float 74.
In like manner, beverage concentrate or syrup from
a suitable source is directed to a chamber 36 by conduits 38
and 40 and the level of syrup is maintained substantially
constant by a diaphragm valve 42 operated by a level sensor
44 including a float 76.
Each of the chambers 24 and 36 are connected to a
source of inert gas, such as carbon dioxide or nitrogen, by a
line 46 (Fig. 2) supplying the selected gas at approximately
300 pounds per square inch to a pressure reducing and control
valve 48 which in turn has its low pressure output connected
to a manifold or balancing line 50 by a line 52~ Pressure
inert gas admitted to the chambers 24 and 36 establishes liquid
free head spaces 54 and 56 of variable volume but at constant
pressure. As will be explained in greater detail hereinafter,
the constant pressure gas in each head space displaces the
water and beverage concentrate to a mixing chamber or tank 58
at a rate at which the combined liquids are withdrawn by a
filler (not shown). As shown in Fig. 1, the combined liquid is
displaced or pumped from the tank 58 by lines 60 and 62, to a
~carbonator-cooling tank 64 which may be provided with a level
control 66, including a float 68, operating a diaphragm valve 70
that controls the rate at which the mixed liquids are introduced
into the tank 64. The mixed, cooled and carbonated liquid is
connected to a filler (not shown) by a line 72.
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The proportioned according to the present invention
responds to changes in the flow rate of the individual liquids
or the combined liquids by the fact that the pressure differential
automatically changes in response to flow rate changes. Changes
5 in pressure different tat promptly changes or adjusts flow rates.
While the mix ratio is maintained constant, the principal benefit
of automatic pressure differential adjustment establishes
substantially constant levels of flow rate that diminishes
or obviates cycling of the refrigeration system resulting from a
mismatch o, proportioned capacity to filler capacity.
With reference to Figure 2, showing an enlarged
representation of the proportioned 10, it will be observed that
in each chamber 24 and 36 a nominal liquid level LO is
established by liquid level sensors 34 and 44, associated,
respectively with the floats 74 and 76 actuating, in response to
the liquid level, mechanical valves 78 and 80. On decline
of the liquid level and consequent lowering of one or both
floats, the associated valve 78 and/or 80 is actuated to direct
pressure supplied by shop air lines 82 to diaphragm valves 32
and/or 42 increasing the rate of water/beverage syrup to
chamber 29 and/or 36 until the nominal liquid level LO
is reestablished.
The mixing chamber 58 communicates with water
containing chamber 24 by a conduit By and with the syrup
25 containing chamber 36 by a conduit 86. Each conduit 84 and
86 extends into the body of liquid of each chamber and terminates
substantially below the nominal liquid level LO The operating
level of chambers 24 and 36 is held constant at all times during
normal operation.
The chamber 24 and 36 are preferably elongated
cylindrical shells closed at each end by upper and lower convex
walls 88 and 90, respectively. The upper walls 88 are bored
and integrally joined to upwardly extending nipple 92 that
is of greater internal diameter than the diameter of conduits 84
and 86 to define an annular passageway 94 (only one ox which
is illustrated forming an extension of the head spaces 54
and 56. The ends of the line 50, supplied with carbon dioxide
gas, are connected to the nipples 92 and thus permit the
introduction of carbon dioxide to the head spaces 54 and 5Ç. A
suitable seal or packing gland 96 is provided on the upper end
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of each nipple to insure containment of the carbon dioxide
gas in the head spaces 54 and 56.
According to the arrangement thus far described, pumping
of the constituent liquids, water and syrup, from the chambers 24
and I to the mixing chamber 58 is achieved by maintaining
a greater gas pressure in head spaces 54 and 56 than the pressure
of chamber 5B while concurrent replenishment of the constituent
liquids occur at substantially the same rate of withdrawal.
To achieve a selected ratio of the constituent liquids
in the mixing tank 58, orifices 98 and 100 are provided in
conduits 84 and 86, respectively. Orifice 100 has a fixed
cross-sectional flow area selected to fulfill production
requirements while orifice 98 is provided with micrometer screw
adjustment 102 for adjusting the flow area and thus establish
the desired ratio of the two liquids. It is preferable to
place the adjustable orifice 102 in the stream which will have
the higher flow rate. While the ratio of the constituent fluids
introduced in mixing chamber 58 is determined by the flow area
of orifice 98, as set by the adjustment of micrometer screw 102,
and its relation to the flow area of orifice 100, the rate
at which the liquids flow from chamber 24 and 36 to the mixing
chamber 58 is established by the pressure difference between the
chambers and the tank. However the flow rate from the chamber 58
to the tank 64 is regulated by the diaphragm valve 70.
Carbon dioxide (COY) is supplied to the proportioned 10
and to the carbonator-cooling tank 64 by the supply line 46
having a branch line 47 connected to a bias regulator valve 106,
supplying COY at a selected pressure to the signal port of pressure
reducing and control valve 48, and a branch line 49 serving to supply
COY to a pressure reducing and control valve (not shown) which
in turn supplies a pressure regulated supply of gas to tank 64.
For purposes of this disclosure the pressure supplied to the tank
is approximately 50 pounds per square inch gauge.
To establish a nominal flow rate of the blended liquids
from the mixing chamber 58 to the carbonating-cooler tank 64 the
bias regulator valve 106 is adjusted, by hand operated screw 107,
until the reading of a pressure differential gauge 109 indicates
a level of pressure greater than the pressure in line 108 whose
pressure is equal to the actual pressure within tank 64, that is
50 prig. C~2 at supply pressure is introduced to the bias regulator
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valve 106 by the branch line 47. The output pressure in a line
114, connecting valve 106 with the pressure reducing valve 48, is
equal to the pressure in line 108 plus a bias pro sure displayed
by the gauge 109~ For example, one level of bias pressure
may be 5 prig. yielding a total pressure of 55 prig. in line 114.
The differential pressure of 5 prig. will be maintained across
the valve 106 regardless of any incur ayes or decreases in the
pressure line 108. The set pressure differential constitutes
the pressure difference between the head spaces 54 and 56 and
the tank 64 and such a differential will be calculated taking
into consideration the proportion of the individual liquids, for
example viscosity, and the desired flow rate through the orifices
98 and 100. Accordingly, based on the exemplary pressure
mentioned above, the pressure of COY in the head spaces 54 and 56
will under all operating conditions be 5 prig. greater than the
pressure in the carbonator cooler tank So.
Each of chamber 24 and 36 is provided with Hoyle
level probes 116 each of which have a high level probe H and
a low level probe L. The probes operate in a range of fluid
levels beyond the range controlled by the floats 74 and 76.
In the event flow of water or syrup is greater, diminished or
interrupted to an anticipated degree viz., changing of syrup
tanks or failure of sufficient water supply, the high level
probes H will, in the instance of too much liquid in one or both
of the chamber 24 and 36, detect liquid immersion and promptly
close valve 32 or 42, respectively, depending on which chamber
has excess liquid. Should the liquid level fall below the end
of the low level probes L valve 70 will be promptly closed
to stop all forward flow.
Using the float level control 66 or the high-low level
probes 104 in carbonat~r-cooling tank 64 has no effect on the
flow of mixed liquids from the mixing chamber 58 to the tank
64 since both types of controls operate diaphragm valve 70 to
modulate flow to the tank 64. The combined flow rate to tank
64 is constant and is manually adjustable by changing the setting
of the bias relay valve 106, which, in turn, causes regulator
valve 48 to adjust the gas pressure in the head spaces 54 and 56.
Should the level in the tank 64 reach the high probe H then valve
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70 will close causing the flow of combined fluids from chamber 58
to stop. The pressure in line 60 and the chamber 58 will
increase and be equal to the pressure in the head spaces 54 and
56 establishing a zero pressure drop across the orifices 98 and
100. In a similar fashion when the fluid level in tank 64
increases the float 68 (Figure 1) actuates air controls 66
causing valve 70 to reduce the flow rate of fluid through the
conduit 62. Flow rate reduction causes an increase of pressure
in the line 60 and the chamber 58 thus reducing the pressure
differential across the orifices 98 and 100 and accordingly the
flow rate of the constituent fluid proportionally and the flow
rate of the combined fluids.
C2 is supplied through line 46, (Fig. 2) to regulator
valve 48 where it is reduced to a set pressure determined by bias
relay valve 106. This regulated pressure is supplied through line 52,
to line 50 and to the head spaces 54 and 56. Conduit 50 is
of sufficient size to maintain equal pressures between head
spaces 54 and 56. Pressure in the head spaces 54 and 56 force
the liquid in each of the chambers 24 and 36 up the conduits 84
and 86 to the mixing chamber 58. The quantity or flow rate of
the water and syrup is determined by the pressure differential
between head spaces 54 and 56 and mix chamber 58 and also by
the size of orifices 98 and 100 the water and syrup produce a
blended liquid having a fixed proportion of each constituent
liquid. The carbonator-cooler tank 64 is connected by a line 49
to a source of COY provided at a rate and pressures which will
insure proper carbonation of the blended liquids. The float 68
and its associated valve 70 control the rate at which the blended
liquids are admitted to the tank 64 with such rate responding
directly to the rate at which the carbonated, cooled and blended
liquids are conveyed by the line 72 to a container filling
apparatus (not shown).
The described proportioned and the disclosed environment
in which it functions to achieve substantially constant liquid
flow through a system, results in steady state operation of
the refrigeration system, consistently accurate proportioning
of the constituent fluids prompt proportioned response to meet
container filler demands and a consistent carbonation level.
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To further illustrate operation of the proportioned
in the disclosed system the following examples of flow rate,
temperature and pressure are given with reference to selected
lines and conduits of the system which are identified as A in
5 conduit 14, B in conduit I C in conduit 38, D in line 60 and
E in conduit 72. The notation Q, T and P represent gallons
per hour, temperature in degrees Fahrenheit and pounds per
square inch gauge, respectively.
Example 1
10 A. Q = 6000, P = 50, T = 70
B. Q = 6000, P = 70, T = 45
C. Q = 1500, P = 70, T = 70
D. Q = 7500, P = 45, T = 52
E. Q = 7500, P = 40, T = 36
Example 2
A. Q = 4166, P = 50, T = 70
B. Q = 4166, P = 70, T = 45
C. Q = 834, P = 70, T = 70
D. Q = 5000, P = 45, T - 52
20 E. Q = 5000, P = 40, I` = 36
While the fluid proportioning and mixing apparatus
and its mode of operation described above fulfills the objective
of continuous accurate proportioning of fluids during steady
state operations, shut down or a momentary interruption of
flow, such as correcting problems with the container filling apparatus,
can establish conditions whereby one or both individual fluids
or mixed fluids flow in directions causing intermixing during
the transient period of pressure equalization. The potential
for intermixing may be detected where fluids of different
specific gravity are being combined.
In accordance with the present invention means,
illustrated in Figures 3, 4 and 5 are provided for maintaining
the separation of fluids during the creation of transient
conditions arising when normal flow of fluids is interrupted. More
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particularly, during the change from normal flow to no flow
the established pressure differential of approximately 5 prig.
declines to zero and during this transition achieving
equilibrium includes, among other factors, the dissipation
of flow energy which is related to the specific gravity of the
fluids being mixed.
Figure 3 shows a fragment of the upper portion of
the chamber 36 containing syrup or concentrate. The conduit 86
communicates with the mixing chamber 58 by elbows 101 joined
to a straight section of conduit 103 and to the mixing chamber 58
by a short nipple 110 opening into the mixing chamber 58.
By locating the mixing chamber 58 relative to the chamber 36
as shown in Figure 3 a trap 112 is defined to increase the
resistance of flow and mitigate the tendency of uncontrolled
intermixing of the fluid having a higher specific gravity with
the fluid or fluids of lower specific gravity. In addition
to the trap 112 the chamber is provided with a fluid flow
direction responsive check valve 114 which essentially comprises
a buoyant ball 116 constrained by wires or rods 118 to plug
and seal the nipple 110 in the event the direction of flow is
from the chamber 58 to the chamber 36. The valve 114 thus
promptly prevents flow of mixed fluids to flow to the chamber 36
and accordingly dilution of the heavier gravity fluid is prevented.
Where preference or conditions indicate resort to
a power actuated valve, one arrangement which can be used is
shown in Figure 5.
A linear actuator 120, connected to a source of
pressure fluid by lines 122 and 124, has its output rod 126
passing through a bulkhead fitting 128 provided with an appropriate
conventional seal. The end of the rod 126 carries a shallow
conical plug 130 which, when seated in the opening of nipple 110
isolates the mixing chamber 58 from the nipple 110 and the
chamber 36 communicating therewith.
In the absence of a valving element, such as 116 or
130, the fluid of greater specific gravity will reverse flow
direction, from the mixing chamber 58 to the chamber 36, and
in the course thereof induce flow of the mixed liquids into
the chamber 36 when the system is not in forward flow. Transient
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detrimental flow continues until equilibrium is achieved.
Where flow interruptions are infrequent detection of an improper
mix in the carbonator-cooler by conventional monitoring devices
is questionable but frequent flow interruptions are detected
and may be evident to the consumer.
Although the best mode contemplated for carrying
out the present invention has been herein shown and described,
it will be apparent thaw modification and variation may be
made without departing from what is regarded to be the subject.
What is claimed is:
