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2,459,451
Patented Jan. 18, 1949
UNITED iSTATES PATENT -~oI-‘i'nce
BUTADIENE Ex'raAc'rIoN
John W. Packle, Green Village, and Edwin M;
Glazier, Elizabeth, N. J., asslgnors to Standard
Oil Development Company, ‘a corporation of
Delaware
Application February 2,' 1945, Serial No. 575,817
s claims.
(Cl. 260-6815)
l
This invention relates to improvements in the
extraction of hydrocarbons and relates particu
larly to the extraction of dioleñns from mixtures
of hydrocarbons consisting of saturated and un
saturated hydrocarbons and other low boiling
compounds.
In the extraction of hydrocarbons,` for example '
in the separation of unsaturated hydrocarbons ‘
from mixtures of saturated and unsaturated hy
drocarbons together with other low boiling com
pounds, various solvents can be used as extract
ants but it has always been diiïicult to remove
all of the desired constituents from the mixture
of hydrocarbons and also to obtain a pure ex
tract containing only the desired constituents and
not an extract containing a major portion of
the desired constituent and a substantial por
tion of the undesirable constituents that were
2
od of operating the several mixers to obtain
intimate contact between the hydrocarbon and
solvent phases while minimizing the detrimental
effect of entrained hydrocarbon with the solvent.
In a typical train of mixer-settlers used to ex
tract butadiene from a C». stream, the hydrocar
bon feed is charged at an intermediate point and
flows countercurrent to the solvent through the
absorption stages and the hydrocarbon from the
last settler is withdrawn as the final raffinate.
The cold lean solvent is charged to the rafiinate
stage and by successive contacts with the hydro
carbon phase in the several absorption stages,
essentially all of the butadiene is absorbed by
the solvent and the final rafiinate contains prac
tically none of this material. The solvent from
the feed stage contains approximately all of the
, butadiene entering the system in the fresh feed,
present in the original hydrocarbon mixture.
plus additional butadiene which is rejected from
It is an object of this invention to provide im
provements in the method of extracting from a
mixture of hydrocarbons an unsaturated hydro
_carbon in a substantially pure form.
through the stripping stages. This rejected
butadiene selectively strips from solution the
Another object of this invention is to provide
a method in which substantially all of the desired
constituents are removed >from the mixture of
hydrocarbons and recovered in a substantially
pure form.
These and other objects of the invention will
be understood on reading the following descrip
tion with reference to the drawing illustrating
diagrammatically the flow of materials.
For example, the separation of butadiene from
the solvent inthe last stage by the addition of
heat and flowscountercurrently to the solvent
materials other than butadiene which are con
tained in the solvent from the feed stage in rel
atively small quantities, until the hydrocarbon
dissolved in the solvent consists of butadiene of
the desired purity. The quantity of hydrocarbon
remaining in the solvent leaving the last stage
is slightly less than the quantity of butadiene
entering the system with the fresh feed due to
the fact that a small quantity of butadiene is
contained in the iinal raflinate stream.
Referring to the drawing, the mixture of hydro
carbons is passed through pipe I into a turbinetype agitator 2, together with the solvent for ex
tracting butadiene which is introduced into pipe
I by means of pipe 3. Into this pipe l is also
introduced, through pipe 4, hydrocarbons that `
vention to the separation and segregation of buta
Idiene alone or the use of this particular solvent 40 have been removed~ from the solvent extract as
will be hereafter described.v This mixture of sol
alone or to the use of a turbine-type agitator, as
vent extract and hydrocarbons is intimately
the method may likewise be used for the sep
mixed in turbine-type agitator 2. The intimately
aration of other compounds such as isoprene,
liquid mixtures of hydrocarbons containing 4
carbon atoms to the molecule using an ammonia
cal cuprous acetate solution as the solvent and
a turbine-type mixer as the agitator will be de
scribed, but it is not intended to limit this in
ethylene, styrene, etc., using other preferential
solvents, such as cuprous ammonium chloride
lsolutions and may be accomplished with other
types of agitators._
In the extraction of butadiene from a C4 stream
with copper ammonium acetate solution by coun
tercurrently contacting the solvent and hydro
carbon in a series of mixers followed by drum
settlers, a portion of the hydrocarbon is not
settled from the solvent and is thus carried along
countercurrently to the normal flow of hydro
carbon. The present invention provides a meth
mixed mixture is then passed through pipe 5
into the settling chamber. B_by means of a plu
' ’rality of pipes 1, 8, 9, and Ill.
This settling ,
chamber is maintained at a temperature of about
18° F. and at a pressure of about 5-18 lbs. per
square inch gauge. Cooling means may be pro
50 vided by an outside jacket, not shown.
The mixture, in this settling chamber, sepa
rates into two phases, one a hydrocarbon phase
and the other an extract phase containing _the
solvent with the butadiene` dissolved therein.
55 This solvent with butadiene and some undesired
3
2,459,451
`
hydrocarbons dissolved therein is removed
through pipe II and passed to turbine-type agi
4
.
.
lower part of the desorber 48. The temperature
here maintained is about 170° F. 'l'.'he solvent
tator I2. The undissoived hydrocarbons are re
substantially i'r'ee of dissolved hydrocarbons, is
withdrawn from- the bottom portion of desorber
48 by means of pipe 42 and passed by-means of
moved from settler 8 by means of pipe I3 and
passed by means of pump I4 into pipe I8 through
which is passed the solvent extract solution.
pump 43 through chiller 44 to reduce the- tem
The mixture of hydrocarbons and the solvent
perature to about 8° F. and through pipe 22 into
extract is then passed into turbine-type agitator
turbine-type _agitator 23. Substantially pure
Il where they are intimately contacted ancir then
butadiene with some ammonia vapor is recov
passed through pipe Il and a plurality of pipes 10 ered from the upper part of the desorber 4U and
I8 into settler I3 where a separation takes place.
passed through pipe 45 upward through the buta
the lower layer containing the solvent'extract
diene scrubber 48 wherein water, provided at the
being passed through pipe 3 into pipe lI and the
upper part by means of pipe 41, removes sub
upper layer of unabsorbed hydrocarbons being
stantially all of the ammonia fromthe butadiene.
passed through pipe 28 by means of pump 2l 15 The wash water is removed from the lower part
into line 22, through which a solvent substan
of the scrubber by means of pipe 48 while pure
tially free of hydrocarbons is being passed to
butadiene is removed from the upper part by
turbine-type agitator 23. The mixture of hydro
carbons and solvent is intimately contacted by
means of pipe 48 and is then liqueñed as the de
sired product.
means of this turbine-type agitator 23. ‘ This 20
mixture then passes through pipe 24 and, by
means of a plurality of pipesv 25, into settler 26
where layer separation takes place and the upper
layer substantially free of butadiene is removed
through pipe 21 from the system. the lower layer
of v`solvent with butadiene in solution passing
timïugn pipe ls to the turbine-type agitator is.
.
. holdup time therein, while the sharpness of sepa
ration in the settlers varies inversely with the
mixer speeds and directly with the holdup time
in the settlers. The holdup times in the mixers
These threeabsorption steps as carried out in
turbine-type agitators 2, I8 and 23, in combina
tion with settlers l, I3 and 28, are maintained
at temperatures below room temperature, that
is 18°, 14°, and lll"- F. and pressures of 18, 21,
and 24 lbs. per square inch gauge.; It is obvious
that lower temperatures and somewhat higher
temperatures may be used and also that the
pressure may be varied within the limits set‘by
the freezing point of the particular solution and
the vapor pressure of the hydrocarbon liquid.
'I'he solvent containing substantially all of the
butadiene and some of the other hydrocarbons
that were present in the charge hydrocarbon mix
ture leaves settler 6 and passes through pipe II.
In turbine-type agitator I2. it is intimately con
tacted with hydrocarbons, principally butadiene,
'I'he speeds of the turbo-mixers used to con
tact the solvent and hydrocarbon are adjustable.
The intimacy of contact and thus the approach
to equilibrium between the two phases varies di~
rectly with the speed of the mixers and the
so
and settlers are constant for any given rate of
iiow of hydrocarbon and solvent through the
system, thus leaving the speeds of the turbo
mixer as the controllable variable.
In order to operate the turbo-mixers at high
speeds to obtain a close approach to equilibrium
_ but not to severely penalize the system by excessive
entrainment of hydrocarbon with the solvent, it
is necessary to operate the mixers at diiiferent
speeds depending upon their relative positions in
the train of mixer-settler stages. This procedure
is necessary because the eifect of hydrocarbon en
trainment on _the overall operation of the system
varies depending on the concentration of the en
trained hydrocarbon and on the relative quantities
voi* hydrocarbon recycle from these stages or, in
other words, on the position in the system. It is
necessary to minimize the hydrocarbon entrain
ment from the feed stage into the stripping stage
due to the fact that the quantity of hydrocarbon
that have been rejected from settler 28 and
passed through cooler 23 by means of pipe~ 30.
In this agitator I2 the butadiene is preferen
tially dissolved in the hydrocarbon phase and
undesired hydrocarbons are preferentially re
- flowing in the stripping section is only about'15%
jected from the solvent phase. The mixture of 50 of that in the absorption section, and the differ
hydrocarbon and solvent phases is passed
ential in concentration of butadiene in Ithe hy
through pipe 3| and a plurality of pipes 32 and
drocarbon phases for the feed stage and the
is separated in settler 33. The temperature
stripping stage is appreciably greater than the dii'
maintained in settler 33 is about 25° F. and the
ferential existing between any other successive
pressure is about 15 lbs. per square inch gauge. - stages in the system. These two factors mean that
'I'he hydrocarbon phase is passed through pipe.
entrainment at this point has a magnified eiïect
4, provided with pump 34, into pipe I. The sol
on the concentration of butadiene throughout the '
vent layer, operated in settler 33 is passed
stripping section and it is, therefore, of prime im
through pipe 35 by means of pump 38 through
portance to keep the entrainment of hydrocarbon
heater 3l and by a plurality of pipes 38 to settler 60 from the feed stage to a minimum by reducing
28 where a temperature of about 90° F. and a
the speed of the agitator in the feed stage. Ex
pressure of 50 lbs. per square inch gauge is main
cessive entrainment of hydrocarbon into the iinal
tained. The elevated temperature maintained
or hot rejection stage is also to be avoided at all
in settler 28 rejects substantially all of the rest
costs, since the hydrocarbon dissolved in the sol
of the undesired hydrocarbons from the solvent, 65 vent at this latter point is the ñnal product and
together with some butadiene. This hydrocar
the quantity of stripping recycle required to pro
bon phase is passed through pipe 30 into line II
duce
the desired productV purity increases very
and the solvent containing substantially all of
rapidly with relatively small increases in the
the butadiene that was present in the charge
amount of impurities carried into this stage. '
hydrocarbon mixture is removed through pipe
However,
entrainment in the stripping stage is not
38 and passed to the upper part of desorber 4I).
as much a problem as it is in the feed stage and
Pipe 39 is provided with a reducing valve' 39'
the absorption stages. Hence, the stripping stage
to lower the’pressure to about 10 lbs. per square
inch gauge. Steam is supplied to the lower part
can be operated at a fairly high speed which may
be more or less constant in each stage. Based on
of the desorber by means of steam coil 4_i in the '15. these factors, it has been found that the lowest
2,459,451.
possible speed must be maintained in the feed
stage with the speed increasing in each succeed
ing absorption stage in the direction in which the
hydrocarbon flows. In practice it will be found
desirable to maintain the agitator speeds in the
final absorption stage and in ythe stripping stage
substantially the same.
p
Since it is desirable to utilize settlers that are
as small as possible to minimize the cost of the
installation, while reducing the entrainment of
hydrocarbon with the solvent as much as possible,
particularly at the positions where it is most
and settling chamber of the last stage and (9') the
olefin is expelled from the said solvent phase,
from which substantially all of the hydrocarbon
except the desired olefin was expelled, by heating
to a suillciently highl temperature to vaporize the
olefin, the improvement which comprisesincreas
ing the speed of agitation in each turbine-type “
agitator succeeding the feed stage in the direction
of hydrocarbon flow and maintaining the speed of
the agitation in each turbine-type agitator suc
ceeding the feed stage in the direction of solvent
flow at substantially the same rate as that in the
final stage following the feed stage in the direc
-tion ofhydrocarbon flow.
~
»
imum recovery and product purity, the following
critical conditions have been found essential for 15 2. In the liquid phase solvent extraction of a
diolelin from a mixture of' dioleflns, oleflnsI and
_ optimum operation ofthe process:Y
harmful so as to give maximum capacity and max
_ saturated hydrocarbons in a plurality of stages,
4 Settling rate ...... „in/min. (maximum)__ 1.5
, Residence time in mixersnmin. (minimum) ..._ 1.6
‘
‘_ each stage comprising a turbine type agitator
and a settling chamber in which (1) the solvent
Temperatures--_-___‘__ .... -.._..... __“ F__ 8 to -100
passesy through the stages in progressively in
/20
Pressures __________________ _'__lbs./sq. in-- 5-50‘
creasing concentration of the diolefln content
Cuprous copper concentration insolvent-- 3-__|-0.2N
andthe hydrocarbon mixture‘passes through‘the
04H: in C4 phase ...... „___„per cent__0.2 to 98
Peripheral'A speed of .turbo mixers:
'
- stages in progressively decreasing content-of the
diolefln, (2) fresh hydrocarbon is intimately con'
Raflinate stage.v ________ -lt/min-- 4570-540
tacted with al preferential solvent -for a diolefin
_Absorption stage _______ „fia/min-- 390-450 25 ‘inra feed stage, v(3) the mixture of hydrocarbon
vFeed stage_______ -_‘.-e-__-‘ft./min-_ 24U-330
Strippingdstargea-_„î_a__;.ft./min;_ "45u-540
AlthoughV thee-present inventionhas been de
and solvent is first passed tothe turbine type
agitator ofthe feed stage and then to the set
tling chamber of the feed stage to' form 'a solvent
phase and a hydrocarbon phase, (4) the solventl
'jphaseafter being separated is contacted with a
hydrocarbon phase, having a higher diolefin. _con
merous changes in the details of the flow plan and _ a centration than the hydrocarbon phase from
which it was separated,l (5) the hydrocarbon
other featuresof the -processumay be resorted >to
without departing from the spirit'andscope VofA 35., phaseafter. being separted is contacted with a
" solvent phase, havinga lower‘diolefln content"
the invention as hereinafter claimed. For ex
ample, while only one stripping stage and _two ’ ‘ than the Vone from which it was separated, (6) the
solvent phase after passing through the turbine
absorption stages have been shown, any desired
type agitator and settling chamber of the last _f
number of stages can be used. o
The nature and objects of the present invention 40 stage is heated and passed to a settling chamber
to expel in the liquid phase substantially all hy
having thus been set forth and a specific illus
drocarbons except the desired dioleiin, (7) the
tration of the samegiven, what is claimed as new
expelled hydrocarbons are separated from the
and useful and desired to be secured by Letters
solvent phase in the said settling chamber, (8)
1. In the liquid phase solvent extraction of an 45 the separated hydrocarbons are recycled to the
solvent phase passing to the turbine type agi
oleñn from a mixture of oleflns and saturated
tator and settling chamber of the last stage and
hydrocarbons in a plurality of stages each stage
(9) the diolefin is expelled from the said solvent
comprising a turbine-type agitator and a settling
chamber in which (1) the solvent passes through ‘ phase from which substantiauy au of the hydro
the stages in progressively increasing concentra 50 carbon except the desired dioleñn was expelled by
heating to a sufficiently high temperature to
tion of the olefin content and the hydrocarbon
vaporize the dioleiin, the improvement which
mixture passes through the stagesin progres
comprises increasing the speed of agitation in
sively decreasing content of the olefln,_ (2) fresh
each turbine-type agitator succeeding the feed
hydrocarbon is intimately contacted with a pref
erential solvent for an olefin in a feed stage, (3) 55 stage in the direction of `hydrocarbon flow and
maintaining the speed of the agitation in each
the mixture of hydrocarbonr and solvent is first
turbine type agitator succeeding the feed stage in
passed to the turbine type agitator of the feed
the direction of solvent flow at substantially the
stage and lthen to the settling chamber of the feed
same rate as that in the final stage following the
stage to form a solvent phase and a hydrocarbon
phase, (4) the solvent phase after being separated 60 feed stage in the direction of hydrocarbon flow.
3. In the liquid phase extraction of a dioleñn
is contacted with a hydrocarbon phase, having a
With a cuprous salt solution from a mixture of
higher oleñn concentration than the hydrocarbon
hydrocarbons containing a diolefln in a plurality
phase from which it was separated, (5) the hydro
01E-stages, each stage comprising a turbine-type ‘
carbon phase after being separated is contacted
agitator and a settling chamber in which (l) the
with a solvent phase, having a lower olefin con
cuprous salt solution passes through the stages
tent than the one from which it was separated,
in progressively increasing concentration of the
(6) the solvent phase after passing through the
dioleiin content and the hydrocarbon mixture
turbine type agitator and settling chamber of the
passes through the stages in progressively de
last stage is heated and passed to a settling cham- '
creasing content of the diolefln, (2) fresh hydro
ber to expel in the liquid phase substantially all
carbon is intimately contacted with a cuprous salt
hydrocarbons except the desired olefin, (7) the
solution in a feed stage, (3) the mixture of hydro
expelled hydrocarbons are separated from the
carbon and cuprous salt solution is first passed
solvent phase in the said settling chamber, (8)
to the turbine type agitator of the feed stage
the separated hydrocarbons are recycled to the
solvent phase passing to the turbine type agitator 75 and then to the settling chamber of the feed. stage
scribed with a certain degree of >particularity, it
is >to be understood that the present disclosure has
been made only by way of4 example fand that nu
Patent is:
'
'
`
-
2,459,451
to form a solvent phase land a hydrocarbon
in the direction of solvent flow at substantially
the same rate as that in the final stage following
phase, (4) the solvent phase after being separated
is contacted with a hydrocarbon phase, having a i
the feed stage in the direction of hydrocarbon
higher diolefin concentration than the hydro
flow.
carbon phase from which it 'was separated, (5)
5. In thev liquid phase extraction of butadiene
the hydrocarbon, phase after beingseparated is
with a cuprous sait solution from a mixture of
contacted with a solvent phase, having` a lower
dioleñn content than the one from which it was
hydrocarbons containing butadiene in a plurality
of stages, each stage comprising a turbine type
separated, (6) the solvent phase after passing
through the turbine type agitator and settling
chamber of the last >stage is heated and passed
' agitator and a settling chamber in which (1)
the cuprous salt solution passes through the -
stages in progressively increasing concentration
of the butadiene content and the» hydrocarbon
„ to a settling chamber to expel in the liquid phase
' substantially-all hydrocarbons except the desired
dioleñns, (7) the expelled hydrocarbons are'sepa- _
mixture passes through the stages in progressive
ly decreasing contento! the butadiene, (2) fresh
rated from the solvent phase in the said settling
hydrocarbon is v intimately contacted with _a
' chamber, _(8) the separated hydrocarbons are
cuprous salt solution for butadiene in a feed
recycled to the solvent phase passing to the tur- v ` stage, (3) the mixture of hydrocarbon ' and
bine type agitator and settling chamber of the,
cuprous sait solution is first passed to the turbine
last stage and (9) the diolefin is expelled fromtype agitator of the feed stage and then to the
the said solvent phase from which substantially v20 settling chamber of the feed stage to form a
- all of the hydrocarbon except the desired dioleiln
solvent phase and a hydrocarbon phase,v (4) the .
was expelled by heating- to a Vsumciently high
temperature to vaporize the dioleiln, the im
solvent phase after being separated is contacted
with a hydrocarbon phase, having a higher buta
provement which comprises increasing the speed
ciene concentration than the hydrocarbon phase
of agitation in each turbine type' agitator suc 25 from which it was separated, (5) the hydrocarbon
ceeding the feed stage in the direction of hydro
phase after being separated is contacted with a.
carbon iiow and maintaining the speed of the
solvent phase, having a lower butadiene content
agitation in each turbine type agitator succeed
than the one from which it was separated, (6)
ing the feed stage in the direction of the ñow of
the _solvent phase after -passing through the '
,the cuprous salt solution at substantially the same 30 turbine type agitator and settling chamber of
rate as that in the final stage following the feed
the last stage is heated and passed to a settling
' stage in the direction of- hydrocarbon flow.
chamber to expel in the liquid phase substan- '
vtially all hydrocarbons exceptthe desired buta
^ 4. In the liquid phase solvent extraction of
diene, (7) the expelled hydrocarbons are separated
butadiene from a mixture of butadiene, oleiins
and saturated hydrocarbons in a plurality of 35 from the solvent phase in the said settling cham
stages, each stage comprising a turbine type agi
ber, (8) the separated hydrocarbons are recycled
to the solvent phase passing to the turbine type
tator and a settling chamber in which (1) the
solvent passes through thestages in progressively
agitator and settling chamber of the last _stage
increasing concentration'of the butadiene con
and (9) `the butadiene is expelled from the said
tent and the hydrocarbon mixture passes through 40 solvent phase from which substantially all of the
the stages in progressively decreasing content of
hydrocarbon except the desired butadiene was
the butadiene, (2) fresh hydrocarbon is intimately ' expelled by heating to a sumciently high tem
contacted with a preferential solvent for buta
- perature. to >vaporize the butadiene, the improve
diene in a feed stage, (3) the mixture of hydro
inent >which comprises increasing the> speed of
carbon and solvent is first 'passed to the turbine 45 agitation in each turbine-type agitator .succeed
type agitator of the feed stage and then _to the
ing the feed stage in the direction of hydrocarbon
settling chamber .of the feed stage to form a sol
flow and maintaining _the speed of the agitation in
vent phase and a hydrocarbon phase, (4) the
each turbine type agitator succeeding the feed
solvent phase after being separated is contactedf
' stagev in the direction of the flow ofthe cuprous
with a hydrocarbon phase, having a higher buta
50 salt solution at substantially the same rate as that
diene concentration than the hydrocarbon phase
-~ in ther?lnal stage following the feed stage in the
from which it was separated, (5) the hydrocar
direction of hydrocarbon flow;
bon phase after being separated is contacted with
a solvent phase, having a lower butadiene content
than the one from which it was separated, (6) the,
6. In the'liquid phase extraction of butadeine v
with an ammoniacal cuprous acetate solution
from a mixture of hydrocarbons containing buta
solvent phase after passing through the turbine
type agitator and settling chamber of the last
diene ina plurality of stages, each stagecompris
ing- a turbine type agitator and a. settling chamber
' stage is heated and passed to a settling chamber
to expel in the liquid phase substantially all hy- '
drocarbons except the desired butadiene, (7) the
expelled hydrocarbons are separated from the
solvent phase in the saidsettling chamber, (8)
the separated hydrocarbons are recycled to lthe ‘
solvent phase passing to the turbine type agi»
tator and settling chamber of the last stage and.
(9) the butadiene is expelled from the said solvent
phase from which substantiallyall of the hydro
carbon except the desired butadiene was expelled
by heating to a sufficiently high temperature to
' vaporize the butadiene, the improvement which
comprises increasing the speed of agitation. in
each turbine type agitator succeeding the feedI
stage in the direction of hydrocarbon now and
maintaining the speed of the agitation in each`
turbine type agitator succeeding the feed stage
in which (l) the ammoniacal cuprous acetate
solution passes through the stages in progressive
ly increasing concentration of the butadiene con
tent and the hydrocarbon mixture passes- through
the stages in progressively' decreasing contentvof
the butadiene, ( 2) fresh hydrocarbon is intimate
ly contacted with an ammoniacal cuprous acetate
solution for butadeine in a feed stage, (3).the
mixture of hydrocarbon and an ammoniacal
cuprous acetate solution is ñrst 'passed‘to- the
turbine ~type agitator of the feed stage and then
to the settling chamber ofthe ,feed stage to form
,10
a solvent phase and a hydrocarbon phase, (4)
the solvent phase after being separated is con
tacted with a> hydrocarbon phase, having a higher
butadiene concentration than the hydrocarbon
phase from which it was separated, (5) the
hydrocarbon phase after being separated is con
9,459,451
_
tacted with a solvent phase, having a lower buta
10
diene content than the one from which it was
rotor speeds ofthe agitator in the feed stage is
of such value as to give a peripheral speed be
separated, (6) -the solvent phase after passing
through the turbine type agitator and settling
tween 240 and >330 feet per minute therein.
chamber of the last stage is heated and passed
rotor speed of the agitator inthe feed stage is of
such value as to give a peripheral speed of 240
to 330 feet per minute therein and the rotor speed
in the final absorption and desorption stages are
' to a settling chamhber to expel in the liquid phase
8. Process according to, claim 6 in which the I
substantially all hydrocarbons except the desired
butadiene, (7) the expelled hydrocarbons are
separated from the solvent phase in the said
of such values as t0 give a peripheral speed of »
settling chamber, (8) the separated hydrocarbons 10 450 to 540 feet per minute therein.
are recycled to the solvent phase passing to the
JOHN W. PACKIE.
turbine type agitator and settling chamber of the
EDWIN M. GLAZIER.
last stage and (9) the butadiene is expelled from
the said solvent phase from which substantially
REFERENCES CITED
all of the hydrocarbon except the desired buta 15
The following references are of record-in the
diene had been expelled by heating to a suñicient
fìie of this patent:
.
ly high temperature to vaporize the butadiene,
the improvement which comprises increasing the
UNITED STATES PATENTS
speed of agitation‘in each turbine-type agitator 1 Number
Name
Date
__
succeeding the feed stage in the direction of hy
1,651,328
Edeleanu _________ -_ Nov. 29, 1927
drocarbon ilow and maintaining the speed of the
Brown ............ _'. Mar. 7, 1939
2,149,574
agitation in each turbine type agitator succeeding
2,154,676
Haueber et al. _'._____ Apr.. 18, 1939
thev feed stage in the direction of ilow o1' the am
2,216,602
Regatz _____ _1_ .... -_ Oct. 1, 1940
moniacal cuprous acetate solution at substantial
2,369,559
Gilliland v....~.-__--____- Feb. 13, 1945
ly the sanie rate as that in the ñnal Stage follow
2,383,784
Fleer -_.... ________ _- Aug. 28, 1945
:Lthe feed stage in the direction oi.' hydrocarbon
2,388,913
Hall _____________ __ Nov. 13, 1945 .
'L'Proœss »wording to «claim e in which the
2,420,906
Packie et al. ....... _- M88' 20, 1947
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