US1766246A - Process of cracking oil - Google Patents

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vJune 24, IQKLv l, .J. pEpATTRE-SEGUY PROCESS 0F CRACKING OIL Originalv Fi1ed June 28, 1926 g l i l I I l I i f l l Patented June 24, 1930 UNITED STATES PATENT OFFICE JEAN DELATTBE-SEGUY, OF CHICAGO, ILLINOIS, ASSIGNOR TO UNIVERSAL OIL PRODUCTS COIIPIANY, OF CHICAGO, ILLINOIS, A CORPORATION OF SOUTH DAKOTA PROCESS OF CRACKING OIL application med :une as, 1926.

This invention relates to im rovements in process of cracking oil, and re ers more articularly to the cracking of petroleum oil to produce therefrom lighter hydrocarbons which crude petroleum or topped crude contains more or less objectionable extraneous matter such as salt, saline compounds, earthy materials or the like.

It has been found in practice that in cracking crude petroleums of this character in the typ'e of crackin plant now used, in which the oil is passed thrugh a cracking coil mounted in a furnace, that there is a tendency for the salt to deposit out and clog or choke up the tubes.

The object ofthe present invention is to remove the salt or like compounds from the petroleum before they reach the primary cracking coil as part of a continuous process.

' In the drawing, the single figure shows a somewhat diagrammatic view of an apparatus suitable for carrying out the present invention.

Referring to the drawings, 1 designates a bottom fired furnace as shown. In the coolest part of the furnace is mounted the primar cracking coil 2, While in the hottest part of tliie furnace is mounted the cracking secondary coil 3. The coil 2 connects by transfer line 4 having throttle valve 5 to an enlarged expansion chamber 6 preferably located outside of the fire zone. The expansion chamber 6 may be provided with the residue drawof lines 7 controlled by the valves 8, manholes 9 and the vapor outlet pipe 10 controlled by the valve 11. This pipe 10 leads ,to the side of a dephlegmator 12, which 'dephlegmator is provided. with the reflux drawoif pipe -13 connected to pum 14,/ and thence by pipe 15 to the inlet of t e coil 2. The top of the dephlegmator is provided with vapor outlet pipe 16 having throttle valve 17 leading to water condenser pipe 18, thence to the receiver 19. The receiver 19 may be rovided with gas outlet pipe 2O controlled by the valve 21 and liqui drawo pipe 22 controlled by the valve23. The dephle mator 12, may be cooled b liquid drawn off rom 5 the receiver 19 throug the pipe 24 and pump Serial No. 118,979.

25 or by any other suitable cooling means, not shown.

, The crude petroleum or topped crude containin the extraneous constituents referred to, is ed fromany suitable sou'rce of supply to the heating coil 3 by means of the feed line 26 and pump 27. The oil passes from the coil 3 through the transfer line 28 having throttle valve 29 to the lower side of the eX- pansion chamber 6, as shown. A pump 30 may be interposed in the line 28.

In carrying out the process, the coils and more or less of the expansion chamber are lled with oil, and raisedto initial conditions of heat and pressure. 'The petroleum containing the objectionable extraneous matter is then fed intothe coil 3 Where it is heated under substantially atmospheric pressure to a transfer temperature of say 950 I". more or less, at which temperature it enters the expansion chamber 6. The oil in the primary heating coil 2 is heated to a transfer tempera` ture of say 850 F., and the primary heating coil 2, expansion chamber and dephlegmator maintained under a substantially uniform pressure of say 150 pounds. In order therefore, to get the oil from the coil 3 into the expansion chamber, it will be necessary to use the pump 30 to force the oil into the expansion chamber against the operating pressure contained therein.

As the oil from the coil 3 enters the expansion chamber, it will be more or less completely vaporized, and the salt or other extraneous matter deposited out and drawn out with the residuum and coke. -The vapors from the oil in the coil 3, as Well as the vapors from the oil in the coil 2 will pass out of the expansion chamber into the dephlegmator where the insufficiently cracked portio ns will be condensed and returned through lines 13 and 15,1and pump 14 to the inlet of the primary coi 2.

The coil 3 is preferably of smaller diameter and shorter len h than the coil 2, and the velocity of the oil 1s such as to more readily sweep out of the coil the salt or the like, into the ex ansion chamber 6 than would be the case w ere it passed through the larger and longer cracking coil 2.

I claim as my invention: 1. A process for cracking hydrocarbon oil containing salt and other deleterious solid constituents comprising maintaining a bulk.

supply of oil constituents in an enlarged reaction z`one, taking oli vapors from said reaction zone, subjecting such vapors to reflux y thouh condensation, delivering hydrocarbon oil constituents containing salt or other deleterions compounds to a heating coil wherein such hydrocarbon oil is subjected to a high temperature While under a relatively low pressure, increasing the pressure on said hydrocarbon o il and delivering the same to said enlarged reaction zone wherein the salt and solid constituents separate from the oil, continuously passing reliux condensate separated from the vapors subjected to reflux condensation through an independent heating coil wherein it is subjected to a cracking temperature While maintained under a super-atmospheric pressure, deliverin the heated reflux condensate to said enlarge reaction zone and maintaining said enlarged reaction zone under substantially the same pressure as that maintaine on the reflux condensate passing said independent heating coil.

rocess for cracking hydrocarbon oil containing deleterious solid constituents comprising maintainin a supply of oil constituents in an enlarge zone, subjecting vapors separated in said'zoneto reflux condensation, initially heating the h drocarbon oil containing deleterious soli to high temperature while under a relatively 10W pressure, increasing the pressure on said hydrocarbon oil, introducing the same at said elevated pressure into said zone, continuously subjecting reinx condensate separated from the vapors subjected to reflux condensation to a cracking temperature under a relatively high superatmospheric pressure, introducing the heated reflux condensate to said zone and I maintaining said zone under a superatmospheric pressure substantially above the pressure maintained on the hydrocarbon oil containing the deleterious solids during the initial heat treatment thereof.

JEAN DELATTRE-SEGUY.

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