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, .Fam ZG, 1948.
2,434,672
E. Q. PATTEE
METHOD OF CONCENTHATING DISTILLERY STILL SLOP
Filed 0G12. l5, 1945
um.
wm,
MM
mh.
T1
‘\ INVENTOR.
Patented Jan. 20, 1948
' 2,434,672
OFFICE
UNITED STATES
2,434,872
METHOD 0F CONCENTRATING DISERY
STILL SLOP
Ellis C. Pattee, Cincinnati, Ohio, assigner to
National Distillers Products Corporation, a cor
poration of Virginia
Application October 15, 1943, Serial No. 506,317
l
4 Claims. (Cl. 15in-47)
This invention is a new and useful process for
concentrating distillery slop. The invention will
be understood from the following description read
in conjunction with the drawing, the single figure
' of which is a diagrammatic showing in side ele
trolled by valve 23, and so introduced into the unit
2 l, in which it passes in indirect heat exchanging
relationship to the liquid introduced through pipe
I9. All or part of the steam is condensed ln unit
2l, the condensate being withdrawn through the
pipe 2l. Evaporation of the material introduced
through pipe I8 takes place in the unit 2i. the
vation with parts in section of apparatus in which
the invention may be carried out.
In the manufacture of distilled liquors and of
steam so produced passing oil’ through pipe 25
alcohol by the fermentation of cereals, the cereal
into
the next succeeding evaporator unit 28. The
is first mashed and then fermented and then dis 10 partly
concentrated distillery slop passes out of
tilled. The residue remaining in the still is known
unit 2l through pipe 2l into the unit 26. In this
as distillery slop and contains soluble materials in
unit the steam from pipe 25 is passed in indirect
solution and insoluble materials in suspension.
heat exchanging relationship to the partly con
In accordance with my invention the distillery
centrated distillery slop so introduced, with the
slop from any suitable source is introduced
result that all or part of the steam is condensed
through pipe I to screen 2. The screen surface 3
in this unit, the condensate passing of! through
of screen 2 may range from 20 to 100 mesh (Tyler
the pipe it. Further evaporation of the water
specifications) and is preferably of about 60 mesh.
content of the distillery slop occurs in unit 26, the
Preferably the screen is of the oscillating or shak
ing type embodying means for moving the mate 20 steam so produced passing of! through pipe 29
into the next succeeding unit 3i. The more
rial retained on top oi' the screen progressively
nearly concentrated distillery slop passes out of
forward so that this material is discharged con
unit 2B through pipe 32 into unit 2i. In this unit
tinuously from the lower end 4 of the screen sur
the
steam from pipe t9 passes ‘in indirect heat ex
face and diverted from the system by means of
chute 5. The material passing through the screen 25 changing relationship to the distillery slop so in
troduced, with the result that all or part of the
includes all the soluble solids and includes also
steam
is condensed, the condensate passing out
the liner or smaller insoluble solids. This mate
of the unit through pipe 33. In consequence` of
rial ñows downwardly within the trough 8 into
this evaporation of the water content of the dis»
pipe 1. The larger insoluble solids in chute 5 may,
tillery slop so introduced occurs, the steam so pro
if desired, be pressed and the expressed liquor‘
duced passing ou through pipe 34 into the baro
combined with the liquid in pipe 1. The liquidV in
metric
condenser l5 by which it is condensed
pipe 1 is moved continuously’by means of» pump
and removed.
8 through pipe 9 into the pipe still il. The pipe
It will, of course, be understood that the lowest
still il includes the continuous tubular heater l2
absolute pressure is maintained on the slop in
mounted in the refractory setting I3 and heated
unit 3|. that a slightly higher absolute pressure
is maintained on the slop in unit 26, that a still
cient heat is introduced into the liquid in its
higher absolute pressure is maintained on the
passage through heater i2 to raise it to the boil
slop in unit 2i, and ythat a still higher absolute
ing point and in addition to vaporize a part of
pressure is maintained on the slop in the drum
the water content therein. The amount of water 40 l l, to the end that the necessary temperature dif
so vaporized may range from 10 to 40% of the
i’erential for eiiicient evaporation may exist in
entire Water content and preferably is about 25%
each auch receptacle.
`
of the entire water content when three subsequent
The
concentrated
distillery
slop passes out of
evaporative effects are employed. If desired,
unit
3i
through
pipe
38
into
pump
3l’. At this
some pressure in excess of atmospheric may be 45
stage
the
moisture
content
will
range
between 20
maintained on the material in heater i2 by means
and 40% of the whole, and is preferably ap“
of the pressure reduction valve l5. The material
proximately 30%. This material is pumped con
so heated is then discharged through pipe I8 into
tinuously
throughpipe il' into the distributor 38.
the drum il in which separation between the
products of combustion produced by burner
liquor and vapor takes place. The liquid portion 50 it The
after passing in indirect heat exchanging rela
accumulates in the cone bottom i8 of drum I ‘l
tionship through the material passing through
passing ofi.’ continuously through pipe i9 con
heater i2 move out ci' refractory setting il
trolled by valve 20 into the iirst unit 2l of a bat
through the stack El by which they are dis
tery of evaporators. The steam is conducted
charged into the lower part of the spray drying
away from the drum l'l through pipe tt, con
tower 42. These products of combustion move
« by any suitable means, such as burner I4. Sulli
2,434,672 '
syrup into direct contact with the said gaseous
upwardly within the tower 4,2, passing therein in
direct heat exchanging relationship to the con
centrated distillery slop introduced into the up
per part of the tower in finely divided form by the
distributor 38. After so passing the products of
combustion move out of the system through the
stack 43.
In moving downwardly within the tower 42, the
distillery s1op is converted into ñnely divided solid
products of combustion thereby producing dried
concentrated slop.
stable. It is high in proteins, especially the water
soluble'proteins, and in vitamin content and is a
valuable feed stock.
The foregoing description is for purposes of
illustration and not of limitation and itis there 20
products of combustion, discharging the stream
3. Method of concentrating distillery still slop
which comprises screening the same thereby re
moving coarse suspended solids therefrom and
thereafter forcing such slop as a continuous
stream through a tubular zone in which it is
indirectly heated to a temperature above 100°
form, in which the moisture content may range 10 C. by passing it in said tubular zone in indirect
heat exchanging relationship with gaseous prod
between 2 and 12% of the whole and is prefer
ucts of combustion, and vaporizing not in excess
ably approximately 8%. This material is contin
of 10-40% of the water content of said s1op in
. uously collected and withdrawn by means of the
said zone at a temperature in excess of 100° C.
sloping bottom 44 and the chute 45.
The product so obtained is firm and chemically 15 thereafter conducting away the said gaseous
fore my intention that the invention be limited
only by the following claims or their equivalent
so heated into a separating zone, continuously re
moving steam and concentrated slop as inde
pendent streams from said separating zone, con
ducting the steam so Withdrawn into indirect
e heat exchanging relationship to the concentrated
slop so withdrawn while maintaining a pressure
on said slop below that obtaining in said separat
ing zone thereby producing a syrup, subdividing
25 the said syrup and passing the subdivided syrup
I claim:
_
_
in direct contact with the said gaseous products
1. Method of concentrating distillery still slop
of combustion thereby producing dried concen
which comprises screening the same thereby re
-trated
distillery s1op.
moving coarse suspended solids therefrom and
4. In the concentrating of distillery still slop
thereafter forcing such slop as a continuous
wherein I have endeavored to claim broadly all
inherent novelty.
stream through a tubular Zone in which it is in 30 the improvement which comprises screening said
slop, thereby removing coarse suspended solids
directly heated to a temperature above 100° C.,
therefrom, thereafter forcing such slop as a con
and vaporizing not in excess of 10-40% of the
tinuous stream through a tubular zone, indirectly
water content of said slop in said zone at a tem
heating said slop contained in said tubular zone
perature in excess of 100° C., discharging the
with gaseous products ci’ combustion and lvapor
35
stream so heated into a separating zone and con
izing not in excess of substantially l0-40% of
duct’ng the steam so withdrawn into indirect
the water content of said slop in said zone at a
heat exchanging relationship to the concentrated
temperature in excess of 100° C., in order to avoid
s1op so withdrawn while maintaining a pressure
decomposition of the slop discharging the partly
on said slop below that obtaining in said sepa
40 vaporized stream of slop so heated into a sepa
rating zone.
rating zone, continuously removing concentrated
2. Method of concentrating distillery still slop
slop as an independent stream from said separat
which comprises screening the same thereby re
ing zone, and continuously removing steam as an
_noving coarse suspended solids therefrom and
independent stream from said separating zone
thereafter forcing such slop as a continuous
45 to thereby create a readily available source of in
stream through a tubular zone in which it is in
ì direct heat.
directly heated to a temperature above 100° C.
ELLIS C. PATTEE.
by passing it in said tubular zone in indirect heat
exchanging relationship with gaseous products of
combustion, and vaporizing not in excess of 10
40% of the water content of said slop in said
50
REFERENCES ClTED
The following references are of record in the
`file of this patent:
after conducting away the said gaseous products
UNITED STATES PATENTS
of combustion, discharging the stream so heated
Number
Name
Date
into a separating zone, continuously removing
Christensen ______ __ Dec. 17, 1940
steam and concentrated slops as independent 55 2,225,428
2,037,006
Clayton __________ __ Apr. 14, 1936
streams from said separating zone, conducting
zone at a temperature in excess of 100° C. there- '
the steam so withdrawn into indirect heat ex
changing relationship to the concentrated slop so
withdrawn while maintaining a pressure on said
s1op below that obtaining in said separating zone 60
thereby producing a syrup and conducting said
1,016,160
2,193,786
2,263,608
1,033,558
Kestner __________ __ Jan.
Thurman ________ __ Mar.
Brown ___________ __ Nov.
Dunn ____________ __ July
30,
12,
25,
23,
1912
1940
1941
1912
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