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Патент USA US2375142

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May 1,-1945.
A. L SKLAR
WAX PRODUCTION
Filed Oct. 2, 1942
2,375,142
Patented May 1_, 1945
; 2,375,142
‘Fries
“UNITED STATES‘ PATENT
2,875,142
_
wax rnonnc'rron'
_
new Lee Sklar, Washington. D. c.
- ‘Application October 2, 1942, Serial No. mates
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6 Claims. (c1. ecu-412.8) i
valves so ‘that liquid can be passe'd-inseri'es
This invention relates to the production of wax
and is particularly directed to an improved methe
od for the e?icient and economical separation of
a useful wax from sugar-cane. ,
I
through any desired set of the extractors similar
to the well-known- arrangement of diifuser bat
teries for the extraction of sugar values from I
a
It has long been known that sugar cane con
tains a waxy substance, largely localized upon
, sugar beets. The extractors are ?tted with a false -
bottom for supporting the wax-containing mate
a the outer rind of the cane, and a“ number of pro
posals have_bee_n made for isolating this wax, '
rial to be extracted.
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.
Liquid ‘sulfur dioxide may be supplied to any
of the extractors from reservoir l0 through pipe,
which-is commonly known as “sugar cane wax.”
It has been found thata substantial proportion 10 I l ._ Steam is supplied to the heaters through pipe .
of the wax content of the sugarcane is carried
l2. Liquid may be passed ‘from any selector ex
along with the juice obtained in. the usual crush
tractor through any selected group of the re
maining extractors. Returnpipe l3 and the in
ing and expressing operations, and that this wax '
is eventually found in the ‘?lter cake resulting > dividual feed pipes connecting pipe , H with the
from the defecating and clarifying operations and 15 extractors make it possible to start or- end the '
known in theindustry as ‘.‘mud."
extraction cycle at any of the extractors, and by
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means of pipe' l4 liquid may be ‘transferred from‘
any of the extractors to any of the crystallizers
C1, C2~—Cn, which need not correspond in num-_
obtained in the defecationof ‘the-‘cane juice, by. 20 ber'with the number of extractors. In normal
extracting the materials with liquid sulfur _di-' "operation one of the extractors is being unloaded
and reloaded with a fresh'charge of wax-contain
ing material while the“ material in the other ex- , The extraction is preferably carried out under
I pressure at a temperature above normal. The
tractors is undergoing the counter-current ex—
wax is obtained in solid form from the extracting ' 25 traction.
The sulfur dioxide recoverysystem includes a
liquid by evaporating, off the sulfur dioxide or
I have ‘now found'that the sugar cane wax can '
beveryemciently separated from materials con
taining the same, such as the ?lter cake or mud
om‘de._
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preferablyby cooling the extracting liquidand
still [5, a compressor l6 and a condenser l'l. .
decanting or ?ltering the liquid portion from the
., In the operation of the apparatus, a charge
wax which separates out ‘on cooling.
of dry wax-containing material, such as the
,
‘ In-order to provide an economical extraction
80 _ “mud” described above, is placed in one of the ex
tractors in place of an exhausted charge,‘ nearly
saturated liquid from the'extraotor with the most
recently changed material is. then passed into the
terial to a series of extractions ‘on the counter
freshly charged extractor, and soy on, in series,
current principle beginning the treatment of
fresh material with liquid sulfur dioxide. which 35 while a fresh batch of liquid sulfur dioxide'is
_ of substantially the entire wax content of the a
- material, it is advantageous to subject the .ma
is already nearly saturated with wax byv contact ' L fed from. the reservoir intothe extractor con- ’
with previously extracted material and finally
treating the nearly exhausted material with fresh : ,
liquid sulfur dioxide.
The number of extractions necessary and the
relative volumes of liquid sulfur dioxide required
will largely depend onlthe temperature at which '
taining the most nearly exhausted charge. '_ The
contents of the reactors are maintained at. a suit-v
able temperature, for example, about 75° 0., by
adjusting the vsteam supply to< the external heat
_ ers. The liquid coming from the‘last charged ex
tractor, now substantially saturated with wax, is
now passed to one of the crystallizers C1, Ca-_-Cn,
extractions are carried out which will be governed 46. and a new extraction cycle is started.
by the pressure which the available apparatus will
.The'solution in the crystallizer is cooled to
approximately --10° C. by pumping'o? sulfur
An illustrative method of operation, embody
dioxide vapor through ‘compressor l?and con
‘ing the principles of the invention will be more
denser l'l until the pressure in the crystallizer is 5
particularly described with reference ‘to the ac
approximately atmospheric. Due to the cooling,
companying drawing which is a diagrammatic 60 the major portion of the wax content of the
representation of apparatus suitable for practic-'
solution crystallizes out. The liquid remaining
s
and.
-
ing the invention.
<
1
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vIn the drawing A1, A2—An are a plurality
extractors having external heaters B1, B2—Bn and
?tted with suitable pipe interconnections and
in the crystalli'zer is then drawn off through pipe l8 to the liquid sulfur dioxide reservoir.
In order to avoid an undue accumulation of
impurities in the liquid sulfur dioxide, a portion
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y
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a
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2,375,142
of the liquid from the crystallizers is continuously
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temperature'substantialiy above normal to pro- '
duce a solution‘ of the wax in liquid sulfur dioxide,
separating the solution from the extracted ma
‘terial, and thereafter separating the wax from
The material remaining in» the crystaliizers 5 the solution by cooling the solution.
4. A method of producing sugar cane wax‘
. after withdrawal of the mother liquor is a light
or intermittently Ied to still 15 where it is vapor
ized and the vapors returned to the system
through compressor i6 and condenser 11.
colored, ?u?y material which readily decom
‘ ‘which comprises extracting material containing .
sugar cane wax with liquid sulfur dioxide at a
poses on heating-to form a brownish wax, typi
temperature substantially above normal to pro
‘ cally haying‘a melting point of 75° C., an iodine
number of 36 and a saponi?cation number of 116. 10 duce a solution of the wax in liquid sulfur dioxide,
separating the solution from the extracted ma
This wax is very hard and is capable of producing
terial, and thereafter cooling the solution by
a brilliant gloss. A typical dry sugar cane “mud”
partial evaporation of the sulfur dioxide and .
will yield about 10% by weight of the wax.
k ‘separating the residual liquid from the solid ma
1. A method of producing sugar cane wax 15 terial formed on cooling.
5. A method of producing sugar cane wax
which comprises extracting material containing
which comprises extracting sugar cane mud with
sugar cane wax with liquid sulfur dioxide to pro
liquid sulfur dioxide at a temperature substam
duce a solution of the wax in liquid sulfur dioxide,
tially above normal, separating the solution of
Separating the solution from the extracted ma
terial, and thereafter separating the wax from 20 wax thereby obtained from the residual mud, and
thereafter separating the wax from the solution.
the solution.
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6. A method of producing sugar cane wax
2. A method of producing sugar cane wax
which comprises passing a series of batches of
which comprises extracting‘ material containing
liquid sulfur dioxide succemvely into contact
sugar cane wax with liquid sulfur dioxide at a‘
temperature substantially above normal to pro 25 with a series of batches of sugar cane mud of
progressively increasing wax content at a tem
duce a solution of the wax in liquid sulfur dioxide,
. separating the solution from the extracted ma
terial, and thereafter separating the wax from
perature substantially above normal until the
liquid sulfur dioxide is substantially saturated
with ‘wax and the mud is substantially free of
‘
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3. A method of producing sugar cane wax 30 wax, and separating the wax from the solution.
the solution.
which comprises extracting material containing
sugar cane wax with liquid sulfur dioxide at a .
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