US1900113A - Treatment of hydrocarbons - Google Patents

Description

March 7, 1933. w. R. HOWARD TREATMENT OF HYDROCARBONS K Original Filed Feb. 2l, 1927 111m ww. -I Nw uw In... HH- @N .uh w A l- K \w\ fr 1 1 n N1 i im N rf top of the deph egmator line 10,

Patented Mar. 7, 19,33

UNITED s'ijATEs PATENT Aori-ICE WILLIAM R. HKDWAXD, .OF WASHINGTON, DISTRICT F COLUMBIA, ASSIGNOR TO UNI- vEnsAL oLYPRoDUc'rs COMPANY, soU'rH DAKOTA TREATMENT 0F HYDROCARBONS Application led Februaryf21, 1927, Serial No. 169,774. Renewed February 4, 1931'.

The present invention relates to improvements in the art of conversion of heavier hydrocarbons into lighter hydrocarbons', but more particularly to a process wherein the heavier ends or residue are so processed as to remain in a liquid form and yet yield a greater amount of lighter hydrocarbons, such as asoline and the like. i'

n the cracking of hydrocarbon oils of the present time, it has been experienced that a crude oil of 209'Bauni gravity may be converted into (i-75% more or less, of light distillates, such as gasoline, and theremainder into solid coke,qex'cept for a small percentage of gas. It has also beenexperienced that this same crude may be converted into 'I5-85% more or less, of a similar light distillate, 5-10,`/(, more orless, into heavyr residual oil, and the' balance into solid coke, with the exception of the same small percentage of gas.

`One of the objects of thepresent invention -is to convert substantially the entire crude into liquid products wherein the overhead light distillates comprisesthe greater percent, and the remaining residuumwis a liquid product having commercalvalue as fuel oil free from coke.` j y Other objects and advantages will more completely `apparent froin vthe .following description.

in the drawing, ai@ Si'ngieiigure is a Side elevationall view showing diagrammatically apparatus for carrying out the invention.

Referring more in-detail to the drawing, 1 represents a feed pump for forcing vthe ch'arg ing stock through line 2 controlled by valve 2' into cracking tube'3 mounted in furnace 4. Line' 5 is a transfer line'from-the cracking tube controlled byvalve 5", into expansion chamber'G;v Erom the top of expansion chamber 6, a vapor line 7,.provided with valve 8, leadsto the de hlegmator 9 andv from the rovided with valve 11, ,leads to vwater coo ed.'con denser 12, continuing through rundown line 13, controlled by Avalve 14, int0 receiver 15. Receiver ma he provided with a gasontlet at the top. in theform of-pipe 16, controlled by valve 17, and near the bottom thereof pipe 18, controlled by valve 19,- for the vwithdrawal lof the condenser liquids'. Line 20, controlled by valve 21, is za bottom drawof for receiver 15.

From the side of expansion chamber 6 at different levels are outlet .pipes 22, 23 'and 24, controlled by valves 25, 2G and 27, respectively, running to a common line 28, which continues into mixing chamber 29. At the bottom of expansion chamber 6 an additional residuum drawofi' 30 may be provided, which enters line 28 through valve 31; this drawoff 30 also has an outlet 92, controlled by valve l33, for withdrawing,rcsiduuni from the system toa supply tankl (not shown).

To the bottom of dephlegmator 9 maybe connected the reflux leg 34 which may com 0F CHICAGO, ILLINOIS, A CORPORATION OF I munic'ate with mixing'chainber 29. Mixing Y chamber 29 may be providedwith a stirring mechanism 35-and means for revolving same i at 36. vF rom the top of mixing chamber 29 a livered through-line 41, through heat ex-v changer 42, here shown 'located in the top of dephlegmator 9 and on into mixing chamber 29. This charging line 4l may be provided with valves 43 and 44 and by-pass line 45 so that the charging stock may be fed directly into the top of dephlegniator 9 through nozzle 4G and reach mixing Achamber 29 through icliux leg 34.-

It isv z. well known fact today that-in the lcracking of. petroleum oils certain disadvantagesa'aI .experiencedin -piissin'gfoil to `be cracked once through the crackinghzone with:2 out the return ofthe reflux condensate in that when ani' substantial 'crackingis produced the crackingtubes quicklyr till up with a heavy` carbon-like sulistanceland coke and even if the charging stock is continuously supplied with a rrtlnx condensate and'passcd through the cracking zonein order to obtain a large yield of lighter distillates, this coke or cokelike material is necessarily deposited in the expansion chamber.

and is picked up by pump 1, and through line 2 is sent through cracking tubes 3 where it is heated to the desired cracking temperature, which, in this process, need vnot be as high as 850 or 900 F., but wherein atemperature of 750 or 809 F. will produce the desired results. The heated charging stock is then discharged into expansion chamber 6 where a separation or reaction takes place, the lighter vapors `going throughv vapor line 7 into dephlegmator 9 and the heavier portion going out through line 30 with valve 33 closed, and into line 28, and then into mixing chamber 29. `As the vapors from the vapor line reach dephlegmator 9 they are separated into lighter vapors which pass out through vapor line 10 and on into receiver 15, after being condensed in condenser 12, and into heavier f1 actions which drop tothe bottom as redux condensate, being withdrawn through line 34 and passed to mixing chamber 29.

As the process continues the residuum from expansion chamber 6, the redux from dephlegmator 9, and the charging stock passed through line 41 all come together in mixing chamber 29 where the'y may or maynot be given mechanical agitation by. means of stirrer 35. As pump 11 continues to pick up thisvmaterial and circulate it through cracking tubes 3, the temperature dually increases and it is so treatedun'ti vapors having a desired end boiling point are coming from the' top of dephlegmator 9. l As the process progresses' and the liquid level in the expansion chamber 6 rises, the residuum may be drawn od and into .mixing chamber 29 through either of valves 25', 26 or 27 and into mixing chamber by vmeans o'f line 28.

If this process continues as so far described, certain results may be obtained, but in a much shorter period of time the cracking tubes 3 ,may clog up with c oke and the accumulation of coke 1n expansion chamber'6 may prevent the withdrawal of residuum and constitute the end of a run. To overcome this objection, pump 39 is started anda portion of the oil in the mixing chamber 29, which is at a tem perature far below that of the oil in the transfer line 5 is fed into expansion chamber 6 and comes in contact with the residuum or heavier ends resulting from the separation oftheoil in the expansion chamber and so retgulates the nature, viscosity, and character o this resid uum as to keep it in liquid form and continually allow same or a portion of same to dow 5 back to mixing chamber 29 whereV it is mixed with redux and charging stock for further cracking in coil 3.

As this residuum becomes heavier a portion of same may be withdrawn through line 30 at the bottom of expansion chamber 6 and by regulating valves 31 and 33 may-be drawn otf through line 32 into a fuel oil storage tank (not shown).

By operating the process as above described, the oil to be treated can be subjected an increased number of times to milder cracking conditions as it passes through cracking tubes 3 and to a' greater agitation in the ring or cycle, which .prevents the accumulation of undesirable coke and also allows a greater yield of lighter distillates or gasoline without forming any substantial amount of coke and forming a residuum salable as commercial fuel oil. A

The process may be operated with predetermined superatmospheric pressures from three to several hundred pounds on the cracking tube 3, expansion chamber 6, dephlegmator 9, and receiver 15 by the manipulation of valves 11, 14 and 17, or differential pressures may be maintained.

I claim as my inventi'on:

1. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of temperature and superatmospheric pressure in a heating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separat-l ing the vapors, subjecting the vapors to tedux condensation, separately condensing and collecting the uncondensed vapors subsequent to redux condensation, removing from the vapor separating zone regulated portions of non-vaporized residue and passing same to an enlarged mixing zone wherein a substantial body accumulates, removing from the redux condensing zone regulated portions of redux condensate and passing same to said mixing zone wherein a substantial body thereof accumulates and mixes with said substantial body of non-vaporized residue, and removing from said mixing zone regulated portions of said mixture and directing same directly and without passage through said heating zone to said 'vapor separating zone where said mixture mixes with the non-vaporized residue accumulated in said vapor separating zone.

2. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of temperature and'superatmospheric pressure in a heating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting the vapors to rcdux condensation, separately condensing and collecting the uncondensed vapors subsequent to redux condensation, removing from the vapor separating zone regulated portions of` non-vaporized residue and passing same to a mixing zone, removing from the' reflux condensin g zone regulated portions of reflux condensate and passing same to said mixing zone Where it mixes with said non-vaporized residue, and removing from said mixing zone regulated portions of said mixture and passing same directly and without passage through said heating zone to said vapor separating zone at a point removed from the heated oil introduction where said mixture mixes with the non-vaporized residue accumulated in said vapor separating zone and continuously withdrawing from said vapor separating zone regulated portions of the heavy non-vaporized residue and isolating same from the system.

8. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of temperature and superatmospheric pressure in a heating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting same to reflux condensation, separately condensing and collecting the uncondensed vapor subsequent to reflux condensation, removing from the vapor separating zone regulated portions of non-vaporized residue and passing same to a mixing zone, removing from the reflux condensing zone regulated portions of reflux condensate and passing same to said mixing zone Where it mixes with said iion-vaporized residue, removing fiom said mixing zone regulated portions of said mixture and directing same to the heating Zone for retreatiiient, removing additional portions of said mixture from said mixing zone and directing the same directly and without application of additional heat into said separating zone prior to admixture with the heated oil supplied thereto.

4. A process of hydrocarbon o'il conversion comprising subjecting oil to cracking conditions of temperature and superatmospheric pressure in a heating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting the vapors to reflux condensation, separately condensing and collecting the uncondensed vapors subseguent to reiiux condensation, removing rom the vapor separating zone regulated portions of non-vaporized residue and passing same to a mixing zone, `removing from the refiux condensing zone regulated portions of reflux condensate and passing same tol said mixing zone where it mixes with said nonvaporized residue, and removing from said mixing zone re lated portions of said mixture and directing same to said vapor separating zone where said mixture mixes with the non-vaporized residue accumulated in said vapor separating zone, in simultaneously and separately removing from said mixing zone controlled quantities of said mixture and directing same to said heating zone.

5. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of tem erature and superatmospheric pressure in a 'eating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting the vapors to reflux condensation, separately condensing and collecti the uncondensed vapors subsequent to re ux condensation, removing from the vapor separating zone regulated portions of nonvaporized residue and assing same to a mixing zone, removing rom the reiux condensing zone regulated portions of reflux condensate and assing same to said mixing zone where it mixes with said non-vaporized residue, and removing from said mixing zone regulated portions of said mixture and directing same to said vapor separating zone where said mixture mixes with the nonvaporized residue accumulated in said vapor separating zone, in simultaneously and separately removing from said mixing zone controlled quantities of said mixture and directing same to said heating zone, and mixing with the latter controlled quantities of fresh charging stock.

6. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of temperature and superatmospheric pressure in a heating zone to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting the vapors to reflux condensation, separately condensing and collectingi-l the uncondensed vapors subsequent to reflux condensation, removing from the vapor separating zone regulated portions of non-vaporized residue and passing same to a mixing zone, removing from the reflux condensing zone regulated portions of reflux condensate and passing same to said mixing zone where it mixes with said non-vaporized residue, and removing from said mixing zone regulated portions of said mixture and directing same to said vapor separating zone where ysaid mixture mixes with the nonvaporized residue accumulated in said vapor separating zone, the portions of said mixture from the mixing zone being introduced to the vapor separating zone at a lower tem` perature than the temperature of the hydrocarbons within the vapor separating zone.

7. A process of hydrocarbon oil conversion comprising subjecting oil to cracking conditions of temperature and superatmospheric pressure in a heating zone -to cause substantial vaporization, passing the heated oil to a vapor separating zone and there separating the vapors, subjecting same to reux condensation, separately condensing and collecting the uncondensed vapors subsequent to reux condensation, removing from the vapor separating zone regulated portions of non-vaporized residue and passing same to a mixing zone, removing from the reflux condensing zone regulated portions of reflux condensate and passing same to said mixing zone where it mixes with said non-vaporized residue, and removing from said mixing zone regulated portions of said mixture and directing same to said vapor separating zone where said mixture mixes with the non-vaporized residue accumulated in said vapor se arating zone returning other portions o said mixture to said heating zone, simultaneously removing from the mixing zone any released vapors and passing same to said dephlegmating zone and maintaining a lower pressure in said mixing zone than is maintained in said separating zone.

8. A process of hydrocarbon oilconversion which consists in passing the oil through a heating coil wherein it is heated to a cracking temperature under superatmospheric pressure, discharging the heated oilk into an enlarged zone of reaction wherein vapors are evolved and separate from unvaporized oil, taking olf the vapors and subjecting them to dephlegmation, passing the refiux condensate to a mixing zone, passing unvaporized oil from said zone of reaction to said mixing zone, returning vapors from said mixing zone to the dephlegmation step, removing regulated portions of said mixture from said mixing zone and introducing said portions to said zone of reaction apart from the discharge of heated oil thereinto.

9. `A process of hydrocarbon oil conversion which consists in passing the oil throuvh a heating coil wherein it is heated to a craclliing temperature under superatinospheric pressure, discharging the heated oil into an enlarged zone of reaction wherein vapors are evolved and separate from unvaporized oil, taking oi the vapors and subjecting them to dephlegmation, passing the reflux condensate to a mixing zone, passing unvaporized oil from said zone of reaction to said mixing zone, passing charging oil for the process in heat interchange with the vapors undergoing dephlegmation and then passing such char g oil to the mixing zone, removing regu ated portions of said mixture from said mixing zone and introducing said portions to said zone of reaction apart fromthe discharge of heated oil thereinto.

10. A rocess of hydrocarbon oil conversion which consists in passing the oil throu h a heating coil wherein it is heated to a crac ing temperature under superatmospheric pressure, discharging the heated oil into an enlarged zone of reaction wherein vapors are evolved and separate from unvaporized oil, takin oi the vaporsand subjecting them to dep legmation, passing the reflux condensate to a zone, passing the unvaporized oil from said zone of reaction to said mixing zone, subjecting the contents of said mixing zone to agitation, removing regulated portions of said mixture from said mixing zone and introducing said portions to said zone of reaction apart from the discharge of heated oil thereinto.

11. A process for cracking hydrocarbon oil comprising passing the oil through a heating coil and thence to the first of serially connected enlar ed chambers, delivering liquid oil fromthe to the second enlarged chamber, taking off vapors from the second enlarged chamber, paing said vapors to a reflux condenser, introducing charging oil for the process and reflux condensate from said reflux condenser to said second enlarged chamber, maintaining a local cyclic circulation through said enlarged chambers by withdrawing oil from the second chamber and returning it directly to the first chamber and maintaining a second cyclic circulation through said heating coil and chambers by withdrawing additional oil from said second chamber and supplying the same to said heating coil.

12. A process for cracking hydrocarbon oil comprising passing the oil through a heating coil and thence to the first of serially connected enlarged chambers, taking off vapors therefrom, delivering liquid oil from the first to the second enlarged chamber, taking olf vapors from the second enlarged chamber, passing said vapors from both chambers to a. reflux condenser, introducing chargin oil for the process and reflux condensate rom said reflux condenser to said second enlarged chamber, maintaining a local cyclic circulation through said enlarged chambers by withdrawing oil from the second chamber and returning it directly to the first chamber and maintaining a second cyclic circulation through said heating coil and chambers by Withdrawin additional oil from said second chamber an supplying the same to said heating coil.

WILLIAM R. HOWARD.

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