NOV- 28, 1939.
P. c. KEITH, JR., Er AL
' 2,181,302
CONVERSION 0F HYDRocARBoNS
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V Filed April 29, 1937
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ATTORNEY
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2,181,302
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Patented Nov. 28, 1939
l . UNITED, STATES»
_
APATElSrr oFFIcE
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ooNvEasroN oFnYnnooAanoNs '
Percival C. Keith, Jr., Peapack, N. J., George W. ,
Robinson, Houston, Tex., and George Roberto,
Jr., Montclair, N. J., assignors to The Poly
merization Process Corporation, Jersey City,
N. J., a corporation of Delaware
'
Application Api-u zo, 1937, sei-iai No.1s9ao4
11 claims
(ci. 19e-1c)
'
constituents
of
the
fresh feed is then passed to a
This invention relates to the production of
normally liquid hydrocarbons, including gasoline
separating zone, preferably conjointly with the
constituents. from -normally gaseous hydrocarf
bons,y More‘p'articularly, the invention relatesA
5 to the conversion by polymerization or similar
reactions of normally gaseous hydrocarbons such'
as those comprising natural gas or the Tgases
produced in connection withoil-cracking opera
-tions to produce therefrom normally liquid hy
normallyl gaseous hydrocarbons from the con
version reaction products. In the separating
zone the liquefied hydrocarbons are separated
from the vuncondensed gases andare collected for
use as charging stock to the conversion reaction.
The uncondensed gases are passed successively
drocarbons which include gasoline constituents.
Normally gaseous hydrocarbons, such as nat
through ’two absorption or scrubbing -zones
wherein the gases are intimately contacted with 10
suitable absorption nìedia whereby the remain
ural gas or the gases produced in connection with
ing constituents suitable for conversion are re
oil cracking, may be converted preferably after
the preliminary removal of hydrogen and meth
15 ane and excessive quantities of ethane to nor
covered-as hydrocarbons dissolved in the absorp-'
tion media. To eifect eiiicient scrubbing the
gases are first scrubbed in the primary scrubbing
154
mally liquid hydrocarbons by subjecting them to . zone with absorption medi‘a‘which'is preferably
temperatures of 750° to 1250° F. at pressures in a relatively light oil and may suitably consist of
excess of 400 pounds per square inch, for ex
a mixture of gasoline, gas 'oil and a small pro
ample, to 3000-pounds .per square inch, or at portion of heavier oils, which may be obtained,
.20 higher temperatures »and lower pressures for a forexample, by diverting a portion of the liquids
relatively longer period or at lower temperature produced in the zone wherein the conversion re
and at lower pressures, if desired, in the presence ' action products are separated into normally gas
eous and normally liquid constituents. In the
operation include hydrogen, normally gaseous 'primary scrubbing zone a substantial proportiony hydrocarbons and normally liquid hydrocarbons. of the recoverable convertible constituents of the
In operations> of this character it is customary uncondensed gases are recovered.
to charge a gas fraction directly to av conversion
In the secondary scrubbing zone the absorption
' furnace and after completion of the conversion - media preferably include somewhat heavier oilsv
operation tov fractionate the products and re 4than the absorption media used in the primary
scrubbing zone and may consist suitably of gas
30 cycle the intermediate constituents capable of
further conversion for admixture with the fresh -oil and a small proportion of heavier oils. Such
feed passing to the polymerization or conversion an oil may be obtained by diverting a portion of
furnace.
'
-the liquids remaining after the gasoline is re
This inventioncontemplates improvements in- moved from normally liquid hydrocarbons col
3Gl the preliminary treatment of a stream of normal , lected in the zone wherein the conversion prod 35
ly gaseous hydrocarbons preferablymixed with ucts are separated into normallyliquid and nor
of catalysts. 'I'he products of such a conversion -
unconverted gases from the process to produce
therefrom a hydrocarbon fraction excellently
f suited as fresh feedfor a conversion operation.
It is an object of the present invention to provide
a novel ,cycle- of operations whereby the gaseous
hydrocarbon stream is- eiliciently treated to pro
4
- duce therefrom a charging stock of superior quai
ity for the conversion operation and to recover
45 most efficiently substantially' allthe constituents
of the hydrocarbon stream suitable for conver-sion reactions, and having other novel and ad
vanta-geous characteristics which will be found
'to obtain.
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According to .the present invention a stream of
normally -gaseous _hydrocarbons obtained, for ex
- ample, from natural gas or from gases produced
in connection with oil-cracking operations, such
as -the overheadfrom a high-pressure separator
or reflux medium from a gasoline stabilizer, is
mally -gaseous constituents.
In 4the secondary
the primary scrubbing zone is eliected. Efficient '
absorption in the primary scrubbing zone is pro
moted by the use of -absorption media `containing
gasoline constituents` since these are closely re
lated in boiling point to the hydrocarbons desiredv
»to be recovered. The use of these materials in
the absorption media results inl a portion thereof
' being> entrained in the gases being scrubbed.
These are recovered in the secondary-scrubbing 50
zone, by the use -offabsorption media relatively
-free of 'gasoline constituents, together with addi- _
tional hydrocarbon gases desired for conversion.
The remaining gases stripped of _their- valuable
suitably compressed and coòledvor refrigerated to_ constituents are discharged fromithe secondary
condense'a substantialv ~fraction thereof which‘ vscrubbing zone, and from'the-system, and re
predominates in hydrocarbons -most suitable for
conversion operations, `such as C3 and C4 hydro
60
carbons. The mixture of liqueñed and gaseous
`
scrubbing zone a unal clean-up of constituents
suitable for conversion and'recovery> of gasoline
constituents contained in the‘ gases because of 40
use of absorption media containing gasoline in
:sesv
moved for use elsewheraforexample, as fuel.> '
Preferably', the enriched absorption media from
the secondary scrubbing zone may-be
to
2,181,302”
» 2
the'primary scrubbing zone as part of the absorp
after being further cooled, if necessary, by passage
tion media therefor.
through cooler 8.
In the fractionator 1 conditions of temperature
The liquefied `hydrocarbons collected in the
and pressure are maintained whereby separation
of normally liquid and normally gaseous hydro
separating zone, which predominate in hydro
carbons most suitable for conversion reaction
obtained -from the fresh feed and from the nor
carbons occurs. For example, the fractionator
may be maintained at a pressure` of 400 pounds
per square inch and with top and bottom tempera
mally gaseous hydrocarbons separated in the
zone wherein the products of conversion are sepa
rated into normally liquid and normally gaseous
10 constituents, are passed to a heater of suitable
>tures of 150° F. and 525° F., respectively. `The
normally liquid hydrocarbons collect in the bot 10
construction and heated at appropriate pressure
conditions to eiîect conversion to normally liquid
hydrocarbons. On emerging vfrom the conversion
heater the reaction products are cooled by admix
15 ture therewith of liquid absorption media con
taining normallygaseous hydrocarbons dissolved
therein, which may be obtained from the scrub
bing zones described above. , The mixture of reac
tion products and absorption media is passed in
20 indirect contact with the incoming fresh feed and
is passed to a fractionation zone after being fur
ther cooled, if necessary. In the fractionation
tom of the fractionator 1 and are withdrawn as
desired through line 9. .In order to maintain the
proper temperature in the liquids collected in the
bottom of fractionator 1 a portion of the liquids
may be diverted from line Bvfor passage through
_line I0, which includes a coil suitably placed in the
heater 4, by means of pump I I, the heater liquids
-suitably at a temperature of about 700° 1'". being
returned to the bottom of'fractionator 1. Vapors
and gases in fractionator 1 ascend to the top and
encounter increasingly low temperatures whereby
normally liquid hydrocarbons are condensed
zone the mixture is separated into normallygase therefrom. Suitable cooling means may be pro
vided for maintaining the .proper temperature .
ous and normally liquid hydrocarbons and is con
tacted, if desirable, by a further quantity of conditions in the top-of the fractionator 1, such
absorption media containing dissolved therein as the introduction of reilux‘through line I2 by
normally gaseous hydrocarbons, which may also be obtained ~from the scrubbing zones described '
30
A portion of the liquids separated in the frac
tionation zone may be circulated through a sepa
rate coil located inthe conversion heater in order
to maintain the temperature desired in the liquids
collected in the zone. A portion of these liquids is
35 withdrawn and passed to a gasoline fractionator
wherein gasoline is removed. Another portion
may be diverted for use as absorption medium in
the primary scrubbing zone. A portion of the
liquids remaining after the removal of gasoline in
the _gasoline fractionator may be used as absorp
tion medium in the secondary scrubbing zone.
The normally gaseous hydrocarbons separated
in the zone of fractionation of thev conversion
reaction products are withdrawn from said zone
45 and after partial condensation the liquefied hy
-drocarbons and uncondensed gases are passed, in
admixture or separately, to the separating zone
jointly with the above-described partially con
densed fresh feed.
50
.
Theinvention is illustrated in the accompany
ing drawing wherein the ligure is a diagrammatic
view in elevation of apparatus suitable `for carry
ing out the present invention. It is to be under '
stood, however, that the drawing is for purposes
55 of illustration only, the invention being capable
0f other modifications.
In the drawing _a stream of hydrocarbons pre
dominating in those most suitable for conversion
to normally liquid hydrocarbons, such as Ca and
means of pump I3.
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The uncondensed normally gaseous hydrocar
bons are withdrawn from the top of fractionator
1 through line I4 and are passed to a condenser I5
wherein' a substantial proportion of the constitu
ents suitable for further conversion treatment,
such as C3 and C4 hydrocarbons, is condensed
therefrom. A portion of the thus produced con
densate may be separated and Withdrawn from
condenser I5 through line I2 for use as reflux in
the fractionator 1.
_
Fresh feed is introduced to the system through
line I6 under pressure by means of compressor I'I
and passed through cooler I8 wherein a substan 40
tial proportion of the constituents thereof suit
able for conversion, such as C: and C4 hydrocar
bons, is condensed. The mixture of liquefied nor
mally gaseous hydrocarbons and uncondensed
gases passes from cooler I8 through line I9 and is 45
introduced to the lower portion of an absorber
tower 20, which functions as a separating 'zone
wherein liquefied normally gaseous hydrocarbonsand uncondensed gases are separated. To this
zone also are introduced the remaining overhead 50
gases from the fractionator 1 which have been
partially liquefied in condenser I5. The liquefied
and uncondensed gases may be withdrawn from
condenser I5 through line 2| in admixture and
introduced to the lower portion of absorber tower 55
20 independently of the fresh feed, or they may be
withdrawn from condenser
I5 in admixture
through line 22 and mixed with the fresh feed in .
60 C4 hydrocarbons, is passed through line I by
line I8 prior to introduction to the lower portion
of absorber tower 2_0. ora separation of liquids and ,60
conversion heater 4 wherein the hydrocarbons are
heated under suitable pressure conditions, for
example, to a temperature of approximately 1030°
65 F. under a pressure of approximately 1200 pounds
per square inch whereby conversion to normally
separation of liquefied and uncondensed hydro
carbons is effected. The liquefied hydrocarbons
means of pump 2 through heat exchanger 3 to
liquid hydrocarbons is effected. The conversion
gases in condenser I5 may be effected with the
liquids being withdrawn through line 2I and the
gases through line 22.
In the lower portion of absorber tower 20 the
collect in the bottom of the absorber tower and
reaction products emerge from the heater 4 are withdrawn therefrom through line l as charg
through line 5 having a pressure reduction valve - ing stock for the conversion reaction. The un
5' therein and are contacted with an absorption condensed- gases ascend the absorber tower and 70
medium containing normally gaseous hydrocar
are scrubbed for the removal of convertible con
bons dissolved thereinl which are introduced stituents, as further described below. Additional
through line 6 which connects with line 5. The charging stock may be introduced in line 48.
mixture of reaction products and absorption me
The liquids collected in the bottom of primary '
75 dium is then passed to a primary fractionator 'I
fractionator 1 are withdrawn through lines 9
.
"2,181,802
3 .
and 23, the latter beingprovided with la pres
absorption media are thereupon introduced into
sure reduction valve 23', and are passed to a gaso
said primary scrubbing zone whereby the result
ing combined' absorption media contain substan
tial proportions of gasoline aswell as gas oil.
To provide suitable absorption media for the
secondary scrubbing zone a portion of the bot
toms collected in the gasoline fractionator 25
line- fractionator 25 afterv being further cooled,
if desired, by passage through cooler 26. In the
gasoline fractionator 25 conditions of tempera
_ture and pressure are maintained whereby gaso
line ‘constituents are separated from heavier oils
' as vapors which ascend the fractionator and are
withdrawn from the tcp thereof through line 21.
10 The gasoline vapors in line 21 arepassed through
a cooler 28 wherein they are condensed, and the
condensed gasoline is collected in gasoline re
and withdrawn therefrom through line 33 may
be diverted through line 36 and introduced into
the absorber tower 20 at the top _thereof after 10
being cooled by suitable heat exchange and, if
necessary, by passage through cooler 31. .
ceiver 29. The gasoline thus produced is with- '
drawn from receiver 23 through line 30 lby means
16 of pump 3| and passed for further treatment,
if necessary, elsewhere. A portion of the gaso
'line in line _30 may be diverted through line 32.
for return to the gasoline fractionator 25 as re
flux to maintain proper temperature conditions
inlthe fractionator to eilect eii‘lcient. separation
Additional scrubbing (media _for introduction
into the vprimary 'scrubbing zone in combination
-with the scrubbing media descending from the
secondary scrubbing zone may consist of a por
tion of the bottoms from primary fractionator
1 passing through line 23 which may be diverted Í
through line 38 by means of pump 39and intro
duced into the- absorber tower 20, at the inter
mediate point which separates the said primary
The heavier oils are collected in the bottom ' and secondary scrubbing zones, after being cooled
of gasoline fractionator 25 and are withdrawn - by suitable heat exchange and, if necessary, by
of gasoline from heavier oils.
.
therefromv through line 33 by means of pump 34, . passage through cooler l0.
'I’he absorber tower 20 conveniently is a unitary
The absorber tower 20 is maintained under
suitable pressure and temperature conditions to
structure divided into three zones. y The lower
portion of the absorber tower 2li constitutes the eiîect the operations desired therein.. For ex
zone of separation of the partially liqueiled" ample, the tower maybe maintained under a
streams of normally gaseous hydrocarbons in‘ro- f pressurev of approximately 380 pounds Vper square
duced therein, as described above. This zone is inch. The liquids collected in the bottom there
separated from ~the upper portion of the tower by of, that is, liqueñed >normally gaseous hydro
means of trap-out -tray 35 which serves to prevent carbons may be maintained -at a temperature of
absorption -media from descending into said zone approximately 155° F. Inasmuch as the partially
of separation. 'I'he upper portion of the absorberl liqueiied streams of hydrocarbons are introduced
tower 20 is divided into a primary scrubbing zone through lines 2| andy I3 at a temperature of
located just above the said trap-out tray, and a approximately 100° F. this temperature will pre
secondary scrubbing zone, which constitutes the vail in~ the top of said separating zone, that is,
top of said absorber tower 20.
.
Absorption media aregintroduced into the ab
40 sorber'tower 20 whereby the gases separated from
>just below the trap-out tray 35. The scrubbing
media introduced into the upper portion of ~the
absorber tower 20 are suitably cooledI to a rela
said streams of partially condensed hydrocarbons , tively low temperature to maintain the tem
perature in the scrubbing zones most suitable
' introduced into -said zone of separation ascend
through said primary scrubbing zone in intimate for eiiicient absorption of` convertible constitu
ents from the gases passing through. For ex
contact with descending absorption media con
sisting essentially of substantial proportions of ample, the scrubbing media may be` cooled be- >
gasoline and gas oil together with, if desired, a fore introduction to a temperature 'of approxi
Aminor proportion of oils heavier than gas oil. ' mately 95° F. In order to maintain the desired
low temperature'in the scrubbing~zones coolingv
In this primary scrubbing zone a substantial pro
portion of the convertible constituents remaining means (not shown) may beprovided for cooling
50 in said gaseseis scrubbed therefrom and recovered the descending absorption media to counteract
the effect of the heat of absorption. The scrubbed
by solution in said scrubbing media.
j
The gases ascending in the absorber tower 23 gases emerging from the secondary scrubbing
pass from thë primary scrubbing zone into a vzone comprising principally vhydrogen and meth
secondary scrubbing zone wherein they ascend in ane are withdrawn from the top of the absorber
55 indirect contact with descending scrubbing media. tower 20 through line l4I and fare thereby with u
drawn from the system for use elsewhere, for
which consist essentially of gas oil with.> ii’ de
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sired. a minorI proportion of oils heavier _than example, as fuel.
gas oil. 1n this secondary scrubbing zone a iinal
It will be understood that the functions of
clean-up of convertible constituents in the gases _ the absorber tower may be performed by a plu
60 is effected whereby substantially all recoverable rality of structures which provide, for example,
convertible constituents are scrubbed therefrom ' a separate structure for each of the separating
and recovered by solution inthe absorption me
and scrubbing zones. To simplify theillustra
día. In this zone also gasoline constituents. en
trained in the gases by contact with the gasoline
65 containing absorption media employed in the
primary scrubbing zone, are recovered by absorp
'tion in the relatively gasoline-free absorption
media.v employed' in the secondary scrubbing zone,
as described above. Preferably, the descending
absorption-media containing normally gaseous
hydrocarbons dissolved therein and absorbed
gasoline constituents-pass directly from the sec-l
ondary scrubbing zone into the primary scrub
bing zone and constitute a portion of the ab
76
sorption media introduced therein. Additional
tion of the'operations of this part of the processj ì
a unitary structure is shown.
-l `The trap-out tray 35 collects the scrubbing
media which have passed through the primary
65 .
and secondary scrubbing zones and contain dis
solved therein normally gaseous hydrocarbons
recovered from the gases passing through the
said scrubbing zone'from the -separating zone 70
located below thesaid trap-out tray35.
At least a portion of the enriched absorption
media collected in trap-out tray 35 is withdrawn
therefrom through line l by means of pumpA 42
and introduœd into admixture with'the prod v15
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4
2,181,802
ucts of conversion emerging from the' heater 4
scrubbing zone, introducing into said primary
in line 5. The normally gaseous hydrocarbons
dissolved in the absorption media admixed with
the conversion products are recovered with the
normally gaseous products of conversion> in the
scrubbing zone and into intimate contact with the
gases passing vtherethrough liquid absorbent
f media comprising a substantial proportion of hy- i
drocarbons in the gasoline boiling range to scrub
primary fractionator 1.
from said gases a substantial proportionV of the
An additional portion of the absorption media
collected in trap-out tray 35 and preferably s.
larger portion thereof may be withdrawn there
from through line 43 by means of pump 44 and
introduced-` into a primary fractionator ‘i at an
intermediate point to assist in regulating the
temperature desired therein and to effect re
covery of the normally gaseous hydrocarbons dis-,
solved in the. absorption media so introduced,
which _normally gaseous hydrocarbons are re’
covered in said primary fractionator 1 with the
normally gaseous constituents of the reaction
convertible constituents remaining thereinwhere
by said convertible constituents are dissolvedin
said absorbent media, passing said scrubbed
gases from said primary scrubbing zone through
a lsecondary scrubbing zone, introducing into said
secondary scrubbing zone and into intimate con
tact with the gases passing therethrough liquid
absorbent media consisting essentially of gas oil
and at most a minor proportion of heavier oils to 1,5
scrub from said gases a substantial proportion of
the recoverable convertible constituents’therein
whereby said convertible constituents are dis-~
products.
.
solved in said last-mentioned absorbent media,
This modiñcation is particularly advantageous heating said liquefied portion of said stream to eñect
when the amount of absorption media used in ~ conversion to normally liquid hydrocarbons, con
said scrubbing zones is more, which is usually the tacting the products of conversion with enriched
case, than the amount desired to be mixed with yabsorbent media from said primary and second
the conversion products prior to separation of ary scrubbing zones, fractionating the -resulting
‘liquids and gases. It may be desirable to pass mixture to separate normally gaseous, constitu
the absorption media withdrawn through line ents including the normally gaseous constituents
43 byvindirect heat exchange with the vfresh of said conversion products and the normally
absorption media passing through lines 33 and lgaseous hydrocarbons dissolved in said last-men
38 by means of heat exchangers 45 and 43, 're
tionedA absorbent media from the normally liquid
spectively, whereby said fresh absorption media
constituents including normally liquid conversion Y 80I
are partially cooled.
products and said last-mentioned absorbent
media substantially stripped of dissolved normal
ly gaseous hydrocarbons, and incorporating at
`
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The absorber tower 2li is provided with. suit
able bubble caps, plates or other gas and liquid
‘ contact means to assist in the intimate contact
least a. portion of said last-mentioned normally
liquid constituents including a substantial pro
portion of gasoline constituents in the liquid ab
of the liquids and gases passing therethrough
and eñect eiiicient performance of the function
of the various portions. Suitable heating means
41 may be provided in the bottom of this tower
to maintain the desired temperature therein.
sorbent media.> introduced into said primary
scrubbing zone.
'
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. 2. The method of converting normally gaseous
This may consist _of means for indirect heat ex
hydrocarbons to normally liquid hydrocarbons
change with the fresh absorption media passing
through line 38.
40
which comprises treating a stream of normally
gaseous hydrocarbons to liquefy a portion in
It is to be understood that the functions of ciuding a substantial _proportion of the convert
the 4fractionators 1 and 25`could be performed ible constituents thereof, separating said liqueñed
by a single structure provided with suitable' trap-' portion from the unliquefied gases of said stream, 45
out trays, etc.. but in Aorder to simplify presen
passing said unliquefled gases through a primary
tation oí the subject matter of the invention sep
scrubbing zone, introducing into said primary
arate structures are illustrated. These fractiona
scrubbing zone and into` intimate contact with
tors also are provided with suitable bubble caps. ' the gases passing therethrough liquid absorbent
plates and other gas and liquid contact means to media comprising a substantial proportion of hy
assist in the intimate contact of liquids and gases drocarbons in the gasoline-boiling range to4 scrub
therein whereby condensation, evaporation, ab
from said gases a substantial proportion o! the
sorption, stripping and other operations inciden
convertible constituents remaining therein where
tal to fractionation are assisted._ Heating means by said convertible constituents are dissolved in
4! is provided in the -bottom vof the fractionator
,55 25 to maintain the ‘temperature desired therein. said absorbent media. passing said scrubbed gases
from said primary scrubbing zone through a sec
These means may consist of'means for indirect ondary scrubbing zone, introducing into said sec
heat exchange with the bottoms from fractionator ondary scrubbing zone and into intimate contact
1 passing through line I3.
'
Y This invention has been described with refer
' with the gases passing therethrough liquid ab
ence to specific embodiments illustrated in the
accompanying drawing. >It is to be understood
that the invention is not limited thereby. how
ever, but is capable o! other embodiments which
may be beyond the physical limitations of the
particular apparatus illustrated.
We claim:A
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1. 4The method of converting normally gaseous
hydrocarbons to normally liquid . hydrocarbons
70 which comprises treating a stream of normally
sorbent media consisting essentially -of gasA oil
and at most a minor proportion oi’y heavier` oils
to scrub from said gases a substantial proportion `
o! therecoverable convertible constituents thered
in whereby said convertible constituents are dis
solved in said last-mentioned absorbent media,
heating said liquefied portion of said stream to
eifect conversion to normally liquid hydrocarbons,
contacting the products of conversion with en
riched absorbent media from said primary and
secondary scrubbingv zones, fractionating the re
gaseous hydrocarbons to liquefy a portion -includ
ing a substantial proportion of the convertible- sulting mixture to `separate normal’y gaseous
constituents thereof, separating said liquefied -constituents including the normally gaseous con
portion from the unliqueiled gases of said stream, stituents of said conversion productsand the nor
passing said unliqueñed gases through a primary Y mally gaseous hydrocarbons dissolved in said last
l
s.
mentioned absorbent media from the normally convertible constituents >remaining _therein
liquid constituents including normally liquid'con
whereby said convertible constituents are dis
version products and's’aid last-mentioned absor solved -in said absorbent media, passing said'bent media _substantially stripped of dissolved scrubbed gases from said .'lprimary scrubbing
normally gaseous hydrocarbons, fractionating at zone through a secondary scrubbing zone, intro
least a portion of said last-mentioned normally ducing -into said secondary scrubbing zone and' v liquid constituents to separate therefrom gasoline into. intimateE contact with the gases .passing _
constituents, and including at least a portion of therethrough liquid absorbent media consisting '
the remaining heavier oil impoverished of gaso , essentially of gas -oil and‘ at .most a minor pro
10 line constituents in the liquid absorbent media portion ofA heavier oils-*to scrubfrom vsaid gases 10
introduced into said secondaryscrubbing zone. ' a .substantial proportion of the recoverable con
3. The method of converting normally gaseous vertible constituents therein -whereby said con
hydrocarbons to normally liquid hydrocarbons vertible constituents aredissolved in said last
which comprises treating a stream of normally mentioned absorbent media, heating' said lique
15 gaseous hydrocarbons to liquefy a portion includ
ñed portion of said stream to effect conversion is
- ing a vsubstantial proportion of the convertible to normally liquid hydrocarbons, contacting the
constituents thereof, separating said liquefied products of _conversion with enriched absorbent>
portion from the unliquefled gases of said stream, media from said primary and secondary scrub
passingl said unliqueñed gases‘through a'primary` A bing' zone,'and fractionating the resulting mix
scrubbing zone, introducing into said primary
ture to separate1 normally gaseous constituents
scrubbing zone and into intimate contact with
the gases passing therethrough liquid absorbent
media comprising a substantialv proportion of hy
drocarbons in the gasoline boiling range to scrub
25 from said gases a substantial proportion of the
including the normally gaseous constituents of
convertible
constituents
remaining
therein
whereby said convertible constituents are dis
solved in said absorbent media, passing said
scrubbed gases' from s'aid primary scrubbing zone
30 through a secondary scrubbing zone,`introducing
into said secondary scrubbing zone and‘into in-`
timate contact with the Kgases passing there
through liquid absorbentmedia consisting essen
tially of gas oil and at most a minor proportion of
zo
said conversion products and the normally gas- '
eous hydrocarbons dissolved in said last-men
tioned absorbent media from the normally liquid
constituents including normally liquid conver 25
sion products and said last-mentionedabsorbent
media substantially stripped „of dissolved nor
ma'ny gaseous hydrocarbons.
'
5. The method of converting normally gaseous 30 ’
hydrocarbons to normally liquid >hydrocarbons
which comprises treating a stream of normally
gaseous 'hydrocarbons to liquefy a portion in
cluding aA substantial proportion of the con
vertible constituents thereof, separating said
35 heavier oils to scrub from said gases a substantial ~ liqueiled portion from the unliquefled gases of
proportion of the recoverable convertible constit
uents therein whereby said convertible constitu
ents are dissolved in said last-mentioned absorb
ent media, introducing at least a portion ofthe
40 enriched absorbent media from the said secondary
scrubbing zone into the primary scrubbing zone
as a portion of the liquid absorbent media intro
duced into said primary> scrubbing zone in con
junction with additional absorbent media from
45 another source including a substantial propor
said stream, passing said unliqueñed gases
through a primary scrubbing zone, introducing
into said primary scrubbing zone and into inti- '
mate contact with the gases passing therethrough
liquid absorbent media comprising hydrocarbons 40
in the gasoline boiling range including a sub
stantial proportion-of low boiling constituents
of gasoline to scrub from said gases a substan
tial proportion of the convertible constituents
iled portion of said stream to eñect conversion to
remaining therein whereby said convertible con 45
stituents are dissolved in said absorbent media,
passing said scrubbed gases from said primary
normally liquid hydrocarbons, contacting the
scrubbing zone through a secondary scrubbing
tion o1' gasoline constituents, heating said lique
products lof conversion with enriched absorbent zone, introducing into said secondary scrubbing
50 media from said primary scrubbing zone, and ,zone and into -intimate contact with the- gases
fractionating the resulting mixture to separate passing therethrough liquid absorbent media
normally gaseous constituents including thenor
mally gaseous constituents of said conversion
products and the normally gaseous> hydrocarbons
dissolved in said last-mentioned absorbent media
from the normally liquid constituents including
normally liquid conversion products and said last
consisting essentially of gas oil and at most a s
minor proportion of heavier oils to scrub from
said gasesa substantial proportion of the re
coverable convertible constituents therein where 55
by said convertible constituents are dissolved
in said last-mentioned absorbent media, heat
mentioned absorbent media substantially stripped ì ing said liqueiied portion of said stream to effect
60
of dissolved normally gaseous hydrocarbons.
4. The method of converting normally gaseous
hydrocarbons to normally liquid hydrocarbons
which comprises treating a stream of normally
gaseous hydrocarbons to liquefy a'portion in
cluding a substantial proportion of the concert
conversion to normally liquid hydrocarbons, con
-tacting productsv 'of conversion with enriched
absorbent, media from said primary and second
ary scrubbing zones, and fractionating the re
sulting mixture to separate normally gaseous
constituents including the normally gaseous con
ible constituents thereof, separating said lique
stituents of said conversion products and the 65
iled portion from the unliqueiled gases of said y normally gaseous hydrocarbons dissolved in said
stream, passing said unliqueñed gases through
last-mentioned absorbent mediairom the nor
’ a primary scrubbing zone, introducing into said
mally liquid constituents >including normally
primary scrubbing zone and into intimate con
liquid
conversiony products and last-mentioned 70 tact with the gases passing therethrough liquid absorbent media substantially stripped of dis 70
absorbent media comprising a substantial pro
portion of hydrocarbons in the gasoline boiling . solved normally gaseous hydrocarbons.
6. A process in accordance with claim 5rwh‘ere
’ range and a substantial proportion of hydro
carbons in they gas oil boiling range to scrub in products of conversion are contacted with v>the
75 from said gases a substantial proportion of the enriched absorption media during the separation
65
2,181,302
thereof into normaliyliîìuid and normally gaseous
scrubbing zone, fractionating` at least a. portion of
said normally liquid constituents into a gasoline
7. A process in accordance with claim 5 where ` fraction and a heavier oil fraction impoverished
in products of conversion are contacted with the of gasoline constituents, introducing into said
enriched absorption -media prior to and during primary scrubbing zone and into contact with
' the gases passing therethrough liquid absorbent
the separation thereof.
media comprising a substantial proportion of hy
8. ¿A process in accordance with claim 5 where
in the normally `gaseous hydrocarbons separated drocarbons in the gasoline boiling range to scrub
from the mixture including .the products of con -from said gases a substantial proportion of the
convertible constituents remaining therein
10 version are cooled to liquefy abortion thereof
whereby said convertible constituents are dis
including a substantial proportion of the con
vertible constituents thereof and combined with solved in said absorbent media, passing said
the inst-mentioned stream of normally gaseous scrubbed gases from said primary scrubbing zone
through a secondary scrubbing zone, introducing
hydrocarbons for treatment therewith.
9. The method of converting normally gaseous into said secondary scrubbing zone and into in. 15
15
hydrocarbons to normally liquid hydrocarbons timate contact with the gases passing there
which comprises heating convertible normally through at least a portion of the said heavier »oil
gaseous hydrocarbons to eiîect conversion thereof fraction impoverished of gasoline constituents as
hydrocarbons.
«
'
,
..
to normally liquid hydrocarbons, contacting .the
products of conversion with a cooling medium
consisting of liquid hydrocarbons containing dis
solved therein> normally gaseous hydrocarbons,
fractîonating the resulting mixture to separate
normally gaseous constituents including the nor
mally gaseous constituents of-îaid conversion
products and normally gaseous hydrocarbons dis
` - solved in 'said cooling medium from the normal
ly liquid constituents' including normally liquid
conversion products and the said cooling medium
liquid absorbent media to scrub from said gases a
substantial proportion of the recoverable con
vertible constituents therein whereby said con
vertible constituents are dissolved in said last
mentioned absorbent media, and contactingI the
productsl of conversion as described with a cool
ing medium comprisingenriched` absorbent me
dia from said primary and secondary scrubbing
zones.
'
-
-
A
11. The method of converting'normally gaseous
hydrocarbons to normally liquid hydrocarbons
30 substantially stripped of _dissolved normally gas- ’ which comprises heating convertible normally 30
eous hydrocarbons; passing normally gaseous
constituents thus obtained through a primary
scrubbing zone, introducing into said primary
scrubbing zone and into -intimate contact with
the gases' passing therethrough a portion-of said
normally liquid constituents including a substan
gaseoushydrocarbons to eiîect conversion there
of to normally liquid’hydrocarbons, contacting
the products of conversion with a cooling medium
consisting of liquid hydrocarbons containing dis
solved therein normally gaseous hydrocarbons,
fractionating the resulting mixture to separate,
normally gaseous constituents including the nor
mally gaseous .constituents of said'conversion.
products and the normally gaseous hydrocar
jbons dissolved in said cooling medium from the
tial proportion of hydrocarbons in the gasoline
boiling range as liquid absorbent media to scrub
fromsald gases a substantial proportion of the
-oonvertible constituents remaining therein
.whereby said convertible constituents are dis-. normally liquid constituents including normally
solved in said absorbent media, Apassing said
scrubbed'gases from said primary scrubbing zone-
V45
into a secondary scrubbing zone, introducing in
to said secondary scrubbing zone and into inti
mate contact with the gases passing therethrough
liquid absorbent media consisting essentially of
liquid conversion products and cooling medium
substantially stripped of dissolved normally gas
eous hydrocarbons' passing normally ,gaseous
constituents thus obtained through a primary
scrubbing zone, fractionating a portion of the
said normally liquid constituents into a gasoline
gas oil and at most a minor proportion of heavier
oils to scrub from said gases a substantial pro
portion ot the recoverable convertible constitu
ents therein whereby said convertible constitu
ents are dissolved in said last-mentioned absorb
ent media, and contacting the products of' con
version as described with a cooling medium com
prising enriched absorbent media from said pri
mary and secondary-scrubbing zones.
10. The method of converting normally gaseous
hydrocarbons >to normally liquid hydrocarbons
fraction and a heavier oil fraction impoverished
of ~gasoline constituents, introducing another por
tion of the normally liquid hydrocarbons ob
tained by the ñrst-mentioned fractionation into
the said primary -scrubbing zone and into inti
mate contact with the gases passing therethrough
as liquid absorbent media to scrub from said
gases a substantial proportion of the convertible
constituents remaining therein whereby said
convertible constituents _are dissolved lin said ab
sorbent media, passing said scrubbed gases from
said primary scrubbing zone through av second
Iwhich comprises heating convertible .no‘mally 'ary
scrubbing zone, introducing at least a por-`
gaseous hydrocarbons to eñect conversion there
of to normally liquid hydrocarbons, contacting
the products of conversion with a cooling medium
consisting of liquid hydrocarbons containing dis
solved therein normally gaseous hydrocarbons,
fractionating the resulting mixture to separate
normally l`gaseous constituents including" the
YLnormally gaseous constituents of said conversion
products and the normally gaseous hydrocarbons
dissolved in said cooling medium from the nor
mally liquid constituents including normally liq
70 uid conversion products and the said cooling me
dium substantially stripped of dissolved normally
gaseous hydrocarbons, passing normally gaseous
constituents thus obtained through a primary y
tion of said heavier oil fraction into- said second
ary scrubbing zone and into intimatecontact with
the gases passing therethrough as'liquid absorb
ent media to scrub from said gases a substantial
proportion of the recoverable convertible constit
uents therein whereby said convertible constit
uents are dissolved in said absorbent media,
contacting the products of conversion as
scribed with a cooling medium comprising
riched absorbent media from said> primary
secondary scrubbing zones.
and
de
en
and .lo
„
PERCIVAL C. KEITH, Jn.
_ GEORGE W. ROBINSON.
VGEORGE ROBERTS. Jl.