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Патент USA US2122789

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Patented July'5, 1938
Hans Tropsch, Chicago, Ill., assignm- to Univer
sal Oil Products Company, Chicago, 111., a cor
poration of Delaware
N0 Drawing. Application
July 12, 1935,
Serial No. 31,104
10 Claims. (01. 260-170)
This invention relates to the treatment of
para?ln hydrocarbons which are normally gaseous
including ethane, propane and the butanes.
In a more speci?c sense the invention is con
amounts of lead chromate and zinc sulfate will
rarely exceed 5% ‘by weight of the aluminum used
in preparing catalysts for the present process.
cerned with a process for converting these low
.while aluminum oxide alone is a fairly good de
contain two atoms of hydrogen less per molecule
hydrogenating' catalyst in the above sense, the 5'
tendency to selective splitting off of hydrogen on
the one hand has been found to be increased,
while the tendency to carbon splitting on the other
hand has been found to be decreased by the use
boiling members
and consequently have one double bond between
10 carbon
There is a large commercial production of gase
ous paraf?n hydrocarbons. They occur in very
of thetwo compounds mentioned so that the over- 10
all dehydrogenatlng action is rendered more de?
nite and effective.
Aluminum oxide itself prepared by‘ the con
trolled calcination of natural carbonate and hy
drate ores, or by chemical precipitation methods
is in itself a fairly good catalyst for accelerating 15
the rate of dehydrogenation of gaseous paraf?ns
over a considerable temperature range. However,
as well as para?inic hydrocarbons. ‘
an extensive series of experiments has demon
_ The greater part of the para?in gas production.
strated that this catalytic property is greatly im
proved by the addition of promoting substances in
minor amounts, usually of the order of less than
10% by weight of the oxide.
Aluminum oxide to be used as a base material
for the manufacture of catalysts for the process
In one embodiment, the invention comprises the
dehydrogenation of gaseous paraffin hydrocarbons
at elevated temperatures in the presence of cata
lysts comprising essentially aluminum oxide sup
porting lead chromate and zinc sulfate as pro
In the present instance the catalysts which are
referred for selectively dehydrogenating the
lower boiling para?inic hydrocarbons have been
may be obtained from natural oxide minerals or,
ores such as bauxite or carbonates such as daw
sonite by proper calcination or it may be prepared
by precipitation of aluminum hydrate from solu
tions of aluminum sulphate or different alums,
the precipitate of aluminum hydroxide being de 30
hydrated by heat, and usually it is both desirable
and advantageous to ‘further treat it with air or
other gases or by other means to activate it prior
to use.
- Two hydrated
oxides of aluminum occur in 36
nature, to wit; bauxite having the formula
A12O32H2O and Diaspore with the formula
AlzDaJ-IzO. In both of these oxides iron sesqui
oxide may partially replace the aluminum. These 40
The criterion of an acceptible de
‘hydrogenating catalyst is that it shall split off hy
drogen without inducing either carbon separation
or scission of the bonds between carbon atoms.
In the concept oi’ the present invention, catalyst
two minerals or corresponding oxides produced
from precipitated and suitably activated alumi
num hydrate are adaptable for the manufacture
of the present type of catalysts and in some in
stances have given the best results of any of the 45
compounds whose use'is at present contemplated.
The mineral dawsonite having the formula
NaaAl(COa)a.2Al(OH)a is another mineral which
may be used as a source of aluminum oxide.
According to the ‘present invention the preferred 50
composite catalyst comprising aluminum oxide
promoting substances to be used for improving the
catalytic effectiveness of aluminum oxide in selec
tively dehydrogenating gaseous para?ins are lead
with lead chromate and zinc, sulfate deposited
thereon and prepared according to the forego
tion with zinc sulfate, since extensive experiments
ing alternative methods is usedcas a ?ller in a
reaction tube or chamber in the form of particles
of graded size or small pellets and the gas to be
have shown that the combined use of these two
dehydrogenated is passed through the catalyst
chemical compounds exerts a particularly good
after being heated to the proper temperature,
usually within the range of 400 to 750° C. (752 10'
to 1382“ F.) The most commonly used tempera
chromate either alone or, preferably, in combina
promoting effect. The reason for the particular
value of these two compounds is not entirely ex
plainable on the basis of chemical theory any more
- than is the effectiveness of other catalysts which
have been found empirically to promote speci?c
reactions. However, it appears that, when the
two salts are used jointly, the extension of the life
tures are above 550° C. (1022° F.) though in gen
eral a temperature range of from 900 to 1050“ F.
is practical. The catalyst tube may be heated ex
teriorly if desired to maintain the proper reac 15
of the catalyst mass is quite pronounced, since the
presence of the lead chromate'causes increased
activity in the early stages of use and assists the
catalysts to reach its greatest effectiveness in ‘a
shorter time while the kzinc sulfate begins to act
tion temperature. The pressure employed may
be atmospheric or slightly superatmospheric of
the order of from 50 to 100 pounds per square
inch, though any large amount of pressure has
more slowly and makes up for the gradual loss in
efficiency of the other salt. It may be said, there
fore, that the lead chromate acts in’ the early
stages of use and the zinc sulfate in the later
a tendency to depress the dehydrogenation reac
tions disproportionately to the increase in ca
pacity of the plant. The time during which the
gases are exposed to dehydrogenating conditions
in the presence of the preferred catalyst is com- ,
paratively short, always ‘below 20 seconds and 25
The preparation of active alumina as base ma
frequently as low as from 3 to 6 seconds.
The exit gases from. the tube or. chamber may
terial for the present type of composite catalysts be passed through selective absorbents to com
involves generally the controlled calcination of bine with or absorb the- ole?n or ole?n mixture
aluminum hydrate obtained from various pri
produced or the ole?ns may be selectively poly 30
mary sources such as,’for example, natural min
merized by suitable catalysts, caused to alkylate
30 erals or chemical precipitates. The ‘conditions of other hydrocarbons such as aromatics or treated
time and temperature employed in calcining any directly with chemical reagents to produce desir=
particular mineral or precipitated material will able or commercially valuable derivatives. .Fiter'
depend, to a large extent, upon its physical and, the ole?ns have been removed the residual gases
may be recycled for further dehydrogenating 35
to a smaller extent, upon its chemical composi
treatment with or without removal of hydrogen.
35 eral ‘percent of ferric oxide in isomorphous mix
Members of the present group of catalysts are
tures with aluminum oxide and since it may occur selective in removing two hydrogen atoms from a
in nature in harder and more compact varieties para?in molecule to produce the corresponding
than the precipitated materials, it may require ole?n without furthering to any great degree
di?erent conditions of time and temperature to undesirable side reactions, and because of this
reduce substantially allofit to the desired oxide. show an unusually long period of activity in serv==
In preparing the promoted catalysts carefully ice as will be shown in later examples. When,
calcined aluminum oxide is first ground to pro ‘ however, their activity begins to diminish it is
duce granules of relatively small mesh and these readily regenerated by the simple expedient of
are then given the requisite amounts of the oxidizing with/air or other oxidizing gas at a
promoter compounds by successive precipitation
moderately‘ elevated temperature, usually within
and absorption from aqueous solutions of salts.
The aluminum oxide resulting from a regulated
calcination has a high absorptive capacity for
activating materials and readily takes up the re
when they are precipitated
_ quired percentages
the range employed in the dehydrogenating re
actions. This oxidation effectively removes traces
of carbon deposits which contaminate the sure
face of the particles and decrease their e?lciency.
It is characteristic of the present types of cata
from or dissolved in aqueous solutions. To insure
lysts that they may be repeatedly regenerated
complete absorption of salts from the solutions
without loss of porosity or catalyzing e?ciency.
Numerous experimental data could be adduced 55
to indicate the results obtainable by employing
the present type of catalyst to dehydrogenate
and at the same time a uniform distribution
upon the aluminum ordde granules, the latter may
.55 be added to relatively dilute solutions of salts and
these may then be concentrated until. a critical ' para?ins but the following single example is suf
point is reached corresponding to complete re
moval of dissolved material. At this point the
solvent may be removed by ?ltering or pressing
or evaporation by heat. ‘More of the preferred
details of procedure will be explained in a later
example. The exact method of adding the two
ficiently characteristic, though it is not given with 60
the intent of limiting the scope of the inven
tion correspondingly.
In making the. catalyst, one hundred grams of
aluminum oxide was treated with 200
. granular
parts by weight of a 5.0% potassium dichromate
solution at the boiling point for one-half an hour. 65
The liquid was then ?ltered off and the alumina
mode of operation which suggests itself to per base‘was dried at 300° C. (572° F.). After dry
sons conversant withsuch catalyst preparation ing, the alumina-particles were treated with 200
and ordinary chemical processes maybe used. As parts by weight of a 7.5% lead acetate solution at
a rule, however, the best materials are made by. the boiling point for one-half an hour.‘ After 70
successively applying the lead chromate and the ?ltering off the liquid the catalyst was washed
70 zinc sulfate. Reversing the order of deposition thoroughly with distilled water and then dried
upon the aluminum oxide granules produces cata
at 300° C. (572° F.). Seventy-?ve parts by weight
of this preparation was treated with 150 parts by
lysts of inferior value.
‘In practicing the dehydrogenation of para?inic' wéight of a 25% zinc sulfate solution for one= 75
joint promoters to the aluminum oxide is not ‘a
special feature of the present invention and any
gasls according to the present process a'solid
_ half an hour at the boiling point of the solution.
The liquid was then ?ltered oil and the catalyst
was dried for several hours at ‘300° (L'.v (572° F.)
and ?nally at 600° C. (11_12° F.) for one hour. '
This catalyst was used at 600° C. and gave, at
Per cent
Hydrogen ______________________________ __ 36.9
Methane _____ _; _____ __'_ ________________ __ 13.0
Ethane ________________________________ __
Propylene ____________________ A ____ __-____
i-Butylene_____________________________ _- 20.7
n-Butylene _______ __. ____________________ __
Butanesr ___________ _‘_ _________________ __ 12.3
Since an expansion of 2.03‘ was observed at the
time the sample was taken, the following yields
of iso-butylene and other ole?ns were obtained:
sulfate as promoters.
4. A process for the dehydrogenation of nor
mally gaseous para?ln hydrocarbons to‘produce
ole?n hydrocarbons, which comprises subjecting
said para?ln hydrocarbons to the action of a cata
lyst comprising essentially aluminum oxide, a
promoter catalyst comprising essentially lead 15
chromate, and containing deposited thereon zinc
sulfate, at a temperature of from 750 to 1380“ F.
_ and for a time period of from 3 to 20 seconds.
5. A process for producing ole?ns i'rom paraf
?n hydrocarbons which comprises subjecting the 20
para?lns under. dehydrogenating conditions to
the action of an aluminum oxide catalyst con
Percent yield
Percent yield
based on
based on
ing conditions to the action of a catalyst com
successive additions of lead chromate and zinc
by volume
mally gaseous para?in hydrocarbons to‘produce
ole?n hydrocarbons which comprises subjecting
said para?ln hydrocarbons under dehydrogenat
prising essentially aluminum oxide supporting
moter catalyst comprising essentially lead chro- _
3. A process for the dehydrogenationoi' nor
atmospheric pressure with a feed rate 01' 1 part .
by weight of isobutane per 6 parts by weight oi.’
catalyst per hour, a gas having the following
Iso-butylene .................... ._
Other ole?ns .................... .-
41. 4
7. 1
56. 7
9. 4
The foregoing speci?cation and example are
su?icient to show that the invention has intrinsic
value when practiced in the art, but neither is
35 to be construed as imposing limitations upon the
taining lead chromate in minor proportion.
6. A process for producing ole?ns from paraf
?n hydrocarbons which comprises subjecting the
parai?ns under dehydrogenating conditions to the
action of an aluminum oxide catalyst containing
minor proportions of lead chromate and zinc sul
7. A process for producing ole?ns from nor»
mally gaseous para?‘ln hydrocarbons which com
prises subjecting the para?ins under dehydrogen
ating conditions to the action oi’ an aluminum
scope of the invention, ‘as both are givenv for . oxide catalyst containing lead chromate in minor
illustrative purposes only.
I claim as my invention:
1. A process for the dehydrogenation of nor
40 mally gaseous para?in hydrocarbons to produce
ole?n hydrocarbons, which comprises subjecting
' said parai?n hydrocarbons under dehydrogenat
ing conditions to the action oi.’ a catalyst com
prising essentially aluminum oxide and a pro
45 moter catalyst comprising essentially lead chro
mate and containing deposited thereon zinc sul
2. A process for the dehydrogenation of nor
mally gaseous para?ln hydrocarbons to produce
Y .8. A process for producing ole?ns from nor
mally gaseous para?in hydrocarbons which com;
prises subjecting the para?lns under dehydrogen
ating conditions to the action of an' aluminum
oxide catalyst containing minor proportions of 40
lead chromate and zinc sulphate.
9. A catalyst suitable for converting para?lns
' into ole?ns comprising a mixture of a major pro
portion of aluminum oxide and a minor propor
tion of lead chromate.
10. A catalyst suitable for converting para?lns
into ole?ns comprising a
e of a major
ole?n hydrocarbons, which comprises subjecting proportion of aluminum?oxide and
minor pro
said paraffin hydrocarbons under dehydrogenat-l portions of lead chromate and zinc sulphate.
ing conditions to the action 01' a‘catalyst com
prising essentially aluminum oxide and a pro
at i
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