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Патент USA US2126281

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Aug. 9, 1938.
' 2,126,281
Filed Nov. 19, 1956 '
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PatentedV Aug, A9,1938 l. L
_ ` 2,126,281
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James B. Rose, Edgeworth,
-three-fourths to Michael L.
`Joseph C. _’l'recs, Pittsburgh, Pa.
Application November 19, 193s, seria No. 111,654:
(Cl. ISB-10)
of common knowledge' that the temperatures toy .
This invention-_relates to a >process of extract
ing gasoline from the gases resulting from the which a catalyst must be heated in order to
cracking'of oil in the manufacture ot "gasoline, i insure a suitable reaction and the pressures to
andhas for its general object to ,obtain a maxi
which gases must be subjected in order to pass
5 mum »recovery of gasoline from such gases and to them >through a catalyst will vary with the par
accomplish such recovery inV an economical and ticular catalyst employed.
eilicient manner.
The liquid condensed from the gases and what
The gases resulting from the cracking of oil in
the manufacture of gasoline are known to the
ever gases may have been uncondensed' are con
etc.) and varying in proportions, according to
deliveredin whole or inpart either to the atmos-phere or into the pipe I through the pipe- I l, by
suitable manipulation of the pressure regulating 15
ducted through a pressure-reducing valve- 'i into
10 trade as "still gases”, "receiver gases’f and “sta-f a receiver 8, wherein further non-condensable 10
bilizer gases”, and contain unsaturates varying in o gases will pass out through the top ofthe re
richness (such-as acetylene, propylene, butylene, ceiver into a pipe 9. The gasesin this pipe may be
` the grades or theoils cracked.
For convenience of description, the gases treated
will be referred to in the claims as “still gases”.
Hitherto these gases have been allowed to go to
waste, except as to such relatively small pro
` portions of the same as may have been employed
0 in the heating of the various units in the cracking
" plants. vBy virtue of my invention, I am enabled '
to reconstruct'these gases by the treatment set
forth hereinafter, thereby to produce gasoline
therefrom on a commercial basis; that is, on a
25 basis which will yield a high proportion of gaso
line at low cost.` '
My process will he described in connection with
the drawing, whichv shows . a diagrammatic or
>The mixture of gases resulting from the crach
ing oi the oil, hereinafter designated “still gases”,
is delivered through a suitable pipe l into a gas
holder t, under a pressure'slightly above `that-ol
35 the atmosphere. From this holder, the gases are
conducted to a compressor 3, where they are sub
jected to a pressure ci from 200 lbs. to 1500 lbs.
per square inch and are delivered under this pres
sure into a> suitable heating stove t, >where the
“l temperature is raised from 200° F. to 1500? F.
' The mixture of gases is then conducted, while
still under the pressure noted, through one or
more catalyst chambers 5 and are delivered thence
‘ to a cooler 6, which effects a partial condensation
the gases so treated `into liquid form, this
condensation into liquid form having been fa
cilitated by the two preceding steps which cooper
in the holder 2 for the purpose of being recycled,
together with the incoming waste gases from the
cracking operation. The pressure reducing "valve 20v
1, which is located at the outlet from the cooler,
serves to reduce any pressures which may exist
in the cooler and in the catalyst chambers‘to
approximately ‘150 lbs. per square inch, and this
pressure, being necessary for the stabilization oi 25
the product, is maintained in the subsequent steps
of my process.
Byrecycling'the gases, a further separation is
accomplished as to the unsaturates that _may not
schematic representation ol an apparatus whereby
it may he realized.
valves il and> i i". The gases delivered from the
receiver into the pipes i0 and i will be collected
havebeen reconstructed and condensed in their 30
hrst run through the process.
The liquid (gasoline) inthe bottom of the re
ceiver is delivered hy means ol’ a charging pump
ll and a. pipe it into a stabilizing tower it, lor
thepurpose of stabilizing the product underthe 35
pressure noted and of effecting, by means of a
condenser it, a further condensation of such
gases as may have been separated from the prod
From the condenser what are known as
“dry” gases may be delivered through the pipe 40
it and the automatic regulator valve il to the
stills for use in the heating operations.
By raising the temperature to ‘1000" to 1500” F.,
a considerable quantity of the saturates are
broken down,- as “well astheunsaturates, and are 45
thereafter cooled and condensed and pumped into
the stabilizing tower, as explained hereinbeiore,
ate to .dissociate the unsaturates and recombine where they are reboiled in order to separate the
50 the dissociated constituents thereof into gasoline. heavier from the lighter ends.
'I'he pressures and temperatures vary between»
A 4catalyst which I have found particularly so
the limits stated hereinbefore in accordance with 4eiiicient in the realization of my process is one
the proportions oi heavier unsaturates in the par
made from ground phosphate rock, mixed prefer
ticular gaseous mixture which is to Abe treated ably in equal proportions by weight with what
and in accordance with the character of the cata
is known to the trade as "ñre bond” (a mixture
55 lyst to which they are subjected, it being a matter _ oi silica sand and water glass). This mixture of 56
‘ $126,281
phosphate rock and lire bond is then thoroughly
under a pressure of from 200 lbs. to 1500 lbs. per
mixed with water, and is then dried and broken
square inch; passing the gases thus heated and
into lumps. While the proportions speciñed
while`under the said pressure in contact with a
catalyst comprising a dried mixture in substan
hereinbefore for the >phosphate rock and nre
bond in the catalyst will result in a product
which-has given satisfactory results at tempera
tially equal proportions by weight of phosphate
rock and ñre bond; cooling the gases while under
tures of approximately 800° F., these proportions
the said pressure therehy- to ei'Iect a preliminary
may be varied to accommodate variations in the
separation of condensable products; reducing the
particular unsaturates and mixtures thereof
pressure on the said gases and condensable prod
ucts and delivering them into a receiving cham
10 which are treated.
Having thus described my invention, what I
claim is:
The process ot manufacturing gasoline from
stlllgases which consists in heating said gases
15 to a temperature between 800° and 1500° F. and
ber; recycling gases evolved in said chamber; and
stabilizing the condensable products under super
atmospheric pressure.
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