US1698811A - Process of refining oil - Google Patents

Description

Jan. I5, 1929.

C. B. FORWARD PROCESS 0F REFINING OIL Original Filed Aug. 19, 1919 tlf.

- Smurf @Humm/toc C2 B. FDRWARD.

WNUJODO Alrw nunk Patented Jan. v15, 1929.

UNITED STATES 11,698,811 PATENT OFFICE."

CHAUNCEY vB. FORWARD, OF URBANA, OHIO. i

PROCESS OF BEFINING OIL.

Application led August 19, 1919, Serial No. 318,484. Renewed lMarch 1927.

My invention relates to a process of refining oil which is an improvement in the methods heretofore practiced and patented `by me, and theV present process is particularly distinguished in the steps taken to superheat the yaporized or volatilized product preliminary to clarifying or condensing such product. In general, my object is to Subject a continually flowing stream of oil to superheated steam until it is highly vola tilized and the 1i uid residue and volatilized product separate and then to superheat the hot lvolatilizedproduct by assing it through coils of small pipe whic are exposed to superheated steam at high temperature, whereby free carbon from the volatile product is eliminated, a large percentage of and a better quality of volatile oil is secured, and the use of extremely high temperatures is permitted in an economical way without destroying the qualities orvalues contained in the liquid residue.

In the accompanying drawing, I show a diagram of a system or apparatus adapted to practice my method. As shown,'water is v forced by a pump 2 into a reservoir 3 where a uniform pressure is maintained to con# stantly supply water under valve and meter control to a flash boiler 4 comprising coils of heating pipes wherein thewater is con verted into a flowing stream of superheated steam which is carrled forward under high pressure at a temperature of a proximateljr 1000 to 1200o F. This s uperiieated steam is 'utilized to heat a body of flowing crude oil in its liquid 'state and also to super-heat the volatile products derived therefrom. Thus the crude oil is pumped from a given source of supply by a pump 5 through relatively small pipesarranged in-coils 7 and 8 within separate preheaters 9 and 10 respecl tively'. The oil flowing through these coils is raised to a high temperature and Volatiln ized to a large extent by subjecting coil 8 to superheated steam introduced into heater 10 through pipe 11 at a temperature of 1000 to 1200 F. After such use the steam 4is lowered in' temperature and is conveyed from heater 10 by pipe 12 into heater 9 to heat t-he oil in its linltia'l flow through coil 7 to coil 8. Thus a higher temperature 1s maintained constantly in,heater 10 than 1r. the initial heater 9, because the flow of steam is inverse to the low of oil.

lVhen the steam is discharged from heater 9 it is conveyed in the form of a live steam,

.also be under valve control.

The treated oil flows under high pressure through pipe 16 from coil 8 into a closed vessel l5, together with superheated steam obtained from pipe 17, and a nozzle 13 is preferably employed to atolnize the unvaporized Oil as it is injected together with the vapor and steam into vessel 15, hereinafter referred to as a separator. Inasmuch as such atomization is effected under high temperature in a closed vessel an additional portion of the oil is volatilized." Independent 011t-A let pipes 18 and 19`are provided for the volatile and unvolatilized separations, and a high pressure is maintained ,const-antlvin the separator by valves adapted to regulate the pressure. and control the outfiow of the sepy arations through said pipes. Outlet ipe 19 at the bottom of the separator trans ers the liquid residue to a tank 20, which may be locatedv at any\ desired distance from the plant because the pressure within separator 15 is sufficient, to .force the residue any reasonable dist-ance.

The volatilized product in separator 15, together with superbe-ated steam, passes through pipe 18 into and through one or more heating 'coils -21` 22 and 23 located in separate insulated (cylinders 2.4, 25 and 26, respectively; and a. temperature ot about 70() to 900o F.,.or higher is maintained in cach cylinder by superheated steam derived from boiler 4. The used steam is discharged at a very high temperature from heaters 25 and 26 through connected pipes 27 into preheater 9, and I also utilize a portion of this steam in effecting separations in separator 15 as indicated by pipe 17'hereinbef0re described. The used steam in vapor heater 24 may also be discharged to drum 14, or this used steam may be discharged into preheater 9 before being discharged to drum 14. The steam from heaters 25 and 26 is delivered to preheater 9 at a very much higher temperature than the steam delivered from reheater 10, and the e'eet of this is decidedly advantageous in constantly maintaining a high temperature in initial heater 9.

F rom the foregoing it will be seen that a large portion ofthe oil will be volatilized or reduced to a vapor, and the volatilized product separated from the unvolatilized product in the separator. This heated volatilized product is then heated to a higher temperature, or superheat'ed, thereby converting it into va more volatile product so that when subsequent condensation occurs a very high percentage of gasoline or motor fuel content can be separated therefrom. There are other advantages derived by superheating the vapors, among which is the selferemoval of the free carbon from the vapors, and which content is trapped in a clean-out receptacle 29 through. which the volatile product must pass by way of pipes 30 before discharging into the lower end of a condensing cylinder 31.v A second cleanout receptacle 32 has a valved pipe-connection 33 with the bottom of receptacle 29 and the contents of these receptacles can be drained into'a storage tank 34 without interrupting operations. In this connection it should be understood that there is no localization of direct flame or fire to the heating coils and therefore no coking or carbonization of the oil due to so-called local heat spots; that the rapidity with which the vapors are forced through the relatively small pipes in the coils does not permit the carbon which is freed to adhere to the inner side of the coils or coke and foul the pipes; and that because the residue from separator l5 isnot subjected to the high temperatures used in and for the vapor heaters, the residue is in better condition' for further refining than it can possibly be gotten where a similar quantity of volatile separations have been effected by distillation by direct heat from a fire, or by other steps known to me.

The volatile product from clean-out receptacle 29 passes upward through conlensing cylinder 31 in which a constant spray of water is delivered through pipe 35, and the volatilized product which is not condensed is carried under the sustained pressure in the system through pipe 36 into a worm condenser 37. lThe water spray reduces the temperature of the vapors and by regulating the amount of water the heavier end of the resultant gasoline or motor fuel oil may be cut out by condensation, and the gravity or end point by distillation controlled to suit the operator. The product coming from the worm condenser is a waterwhite motor fuel oil or gasoline which is discharged with thefcondensed steam into a separator 38 from whence the oil overflows into a receiver 39 before it is discharged at intervals into a storage tank 40 by the automatic operation of a pump 4l controlled by.

afloat42. in receiver 39. rlhe gasoline or motor fuel is at this point ready for the market without further treatment.

'Ihe heavier fractional separation in cylinder 3l passes out of the bottom thereof into a well 43 with the water which is sprayed into said cylinder, and a valved pipe 44 connects this well with a cooling coil 45 which is adapted to discharge the mixed liquid into a separator-46 having an overflow connection with a receiver 47. `When a predetermined lquantity of the oil fractions are trapped in receiver 47 it is automatically conveyed therefrom by a pump 48 to a distant point where it can be either stored or used as needed.

In operating this process I do not wish to be limited to the use of steam in spraying the oil into separator l5, but the commingling or injection of steam at this point helps maintain the pressure and temperature in the separator and thus forces the vapors more rapidly through the subsequent heating coils. Steam so introduced also washes the vapors so that the gasoline or motor-fuel product is sweeter, purer and better than it is when steam is not so used.

In using at different times both large and small coils and separators I have found that the most economical sized apparatus or unit for commercial use will refine approximately 150 barrels of oil per day, and where a series of say five or more such units are used the superheated steam may be reheated by a coil in a small furnace and used again in successive units repeatedly. I-Iowever, by the use of a flash boiler as herein disclosed and as I have constructed it, very little if any additional re is required to create the steam as well as superheat it to the desired temperature. Thus in order to superheat the steam to the desired temperature it is necessary to have the superheating or final pipe sections of the coil in close relationship with the fire, and the temperature in the furnace above the portion of the coil in which the superheating is done is sufficient to create the necessary amount of steam desired. This effects a great economy in the operation of my process and in an installation involving a series of units I would include a reserve flash boiler which could be used whenever it was found necessary to re-' va matter of fact I have demonstrated on a commercial scale that the lower pipes of the superheater for the steam are practically the `only places at which there is any wear and tear, and these pipes can be quickly replaced at a nominal cost. The remainder of the apparatus is not subjected to direct tire, nor

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affected materially by constant u`se in practicing the process.- Viewing the invention broadly, I donotV necessarily limit myself tothe use of a flash boiler for the supply of superheated steam, as I have. practiced this process with steam created and superheated in a re ular Water tube boiler, nor do I desire to limit myself to the use of hand-operated valves for regulating the ow of steam,'oil or vapors, because an automatic control may be employed if desired, although in actual practice very little attention is required to set or regulate hand. valves.

That I claim is:

1. A process of refining oil, consisting,r in conveying a stream of oil through heating coils exposed to superheated steam and ateniizing the heated product together with ay compressible fluid in a closed vessel, in forcing the volatilized and atomized product from the closed vessel through heating coils exposed to superheated steam 0f approximately 1000 F. or above until highly heated, and finally liquefying the highly volatilized product and separating the liquids so de. rived.

2. A process of refining oil, consisting in forcing a stream of oil through heating coils into a separator while heating said coils with superheated steam introduced at approximately 1000 F., in forcing the heated volatilized product of the foregoing step through heating coils exposed to su erheated steam at a temperature higher t an I700 F. until such product is superheated, in removing the carbonaceous material freed from said superheated volatilized product, in spraying said volatilized product with a liquid, and 1n condensing said product lsubsequent to such treatment. l

3. A process of refining oil, consisting in passing a stream ofoil through heaters exposed 'to s uperheated steam, separating the volatile and liquid constituents under pressure subsequent to such heat treatment, in`

passing the heated volatile product through heaters exposed to superheated steam, in subjecting the highly-heated volatilized product to the washing and cooling action of water in a closed eylinder under the pressure sustained in effecting separations, in conveying the volatilized and liquid contents of said. cylinder separately therefrom, in li uefying said treated volatilized roduct, an in Vseparating the different liquids derived by said steps.

4. A process of refining oil, consisting in subjecting a flowing bodyof oil to superheated steam at a temperature of ap roximately 1000 F. and volatilizing an separating its volatile and liquid constituents under the pressures arisin from the use of such high temperature, t en superheating the volatilized separations, then passing said' superheated volatilized product under pressure @through -a Washing and cooling liquid in -a closed cylinder, then condenslng the'- saidvolatilized product and separating the differentliquids derived by said steps. i0`

5. A- process of refiningoil, consisting in i' forcing a stream of oil through heating coils exposed to superheated steam and discharging the heated product together with steam under pressure into a closed vessel having separate channels of exit for volatilized and liquid products, then conveying the volatilized product together with the steam through heating coils exposed to su'perheatcdsteam until such product and steam` is heated to high temperatures, then subjecting the highly heated product to the Washing and cooling action of a fiuid in a closed cylinder open to the pressure maintained in effecting separations, then liquefying thevolatilized product and finally separating the different liquids derived by said steps.

6. A process of refininer oil, consisting in forcing a stream of oil t irough heaters ex'- posed to superheated steam 'introduced at about a temperature of1000 F., in Hseparating the volat'i-lizedrand liquid constituents of the heated oil, in lreheating the volatilized' product with superheated steam in a heater 4maintained at a temperature -of 700 F. or higher,in vutilizing the used steam of said last step ata lower temperature to heatthe oil in-its initial flow to the, oilheaters, and in liquefying the volatilized product and separating the liquids resulting from the aforesaid steps.

7, A process of refining oil, consisting in forcing a stream fof oil through a plural number of heaters in which superheated steam is causedto fiow inverselyv to the fiow 105 of oil, in discharging the heated oil together with steam into a closed vessel to effeet a high degree of separation of the volatile and liquid constitutents of the heated oil, in conveying thevolatilized product with 110 steam under pressure through a plural number of heaters exposed to superheated steam, in transferring the used steam from the heaters used in the last step to the heaters used in the first step, in removing the mixed 115 li uids deposited in the closed vessel, and in su jecting the volatilized product within a second closed vesselto the washing and cooling action of water.'

8. A processwof refining oil, comprising 120 steps which consists in assing a stream of water constantly throng a fiash boiler and `instantaneously convrtin the flowing water into superheated steam w lich is dschar,f vedv continuously at a tem rature of approxi- 125 mately 1000 F. or big 1er while contemporane'ously forcing. a stream of' mineral oil continuousl through a heater vin which the superheatedY steam 1s introduced at said temperature and allowed to accumulate in vol- 13 through said heater in indirect heat exchange' ume as rapidly as created in said flash boiler.

9. A process of refining oil, consisting in forcing a stream of mineral loil constantly through a series of coils of small pipe, while .contemporaneously forcing a stream of water through other coils of pipe in a flash boiler and converting the flowing water into a flowing stream of superheated steam at a temperature of approximately 1000o F. or higher; in discharging the superheated steam immediately into contact with the oil-conveying coils of pipe, and in discharging the oil and vapor and steam together into a vapor and liquid separator under the pressure derived from such high temperature.

10. A process of refining oil, consisting in separately forcing a stream of oil through a series of heating coils and a stream of water through a flash boiler and in maintaining a constant discharge of superheated steam at a temperature of 1000 F. or higher while applying the same'vto a part of said series of coils at graduated temperatures inversely to the flow of oil until a hot vapor product is produced; inpassing said hot vapor product through other parts of said series of heating coils While applying the same superheated steam thereto to create a more volatile prod-1, uct; and in finally condensing the volatil'fj ized product. A

11. In a process of refining oil the improvement comprising passing a rapid flow of vapors of oil boiling substantially below 900o F. and free from hydrocarbon constituents in the liquid state in a stream of restricted cross-section in a series of successive passes through a heater and superheating the oil vapors during their passage therethrough to a temperature in excess of 900o F.

by flowing a. superheated compressible fluid relations with said oil vapors, maintaining a temperature differential of less than about 500 F. between the maximum temperature of the superheated oil vapors and said superheated compressible fluid contacting with the heating-surfaces and maintaining the pres sure under which said superheated compressible fluid is supplied to said heater substantially in excess of the pressure at .which it is discharged therefrom,`whereby a rapid forced flow of the said'superheated compressible fluid is maintained through said heater and over the heat transferring surface therein.

12. In a process of refining oil'the improvement comprising passing a' rapid flow of vapors ofoil boiling substantially below 900 degrees F. andA free 4from hydrocarbon constituents in theliquid state in a stream of restricted cross section in a series' of .successive passes through a heater and superheating the oil vapors during their passage therethrough to a temperature in excess of 900 degrees F. by maintaining a rapid forced flow of superheated steam through said heaterin indirect heat exchanging relation with said oil vapors and maintaining a temperature differential of less than about 500 degrees F. between the said superheated steam and the hot oil vapors.

13. In a process of refining oil the improvement comprising passing a rapid flow of vapors of oil boiling substantially below 900 degrees F. and free from hydrocarbon constituents in the liquid state in a stream of restricted cross section in a series of successive passes through a heater and superheating the oil vapors during their passage therethrough to a temperature in excess ot 900 degrees F. by maintaining a rapid forced flowof a superheated gaseous substance through said heater in indirect heat exchanging relation with said oil vapors and maintaining a temperature differential of less than about 500 degrees F. between the said superheated gaseous substance and the hot p oil vapors.

14. In a pro.ess of refining oil the improvement comprising passing a'rapid flow of vapors of oil boiling substantiallyvbelow I900 degrees F. and free from hydrocarbon constituents in the liquid state-in a stream 0frestricted cross section in a series of successive passes througha heater and superheating the oil vapors during their passage therethrough to a temperature in excess of 900 degrees F. by maintainingv a rapid forced flow of a superheated gaseous substance under superatmospheric pressure through said heater in indirect heat exchanging relation with said oil vapors and maintaining a temperature differential of less than about 500 degrees F. between the said superheated gaseous substance and the hot oil vapors.

- 15. In a process of refining oil the improvement comprising passing a rapid flow of vapors of oil boiling substantially below 900 degrees F. and free from hydrocarbon constituents in the liquid state admixed with steam in a stream of restricted cross-section in a series of successive passes through a heater and superheating the steam and oil vapor mixture during its passage therethrough to a temperature in excessof 900 degrees F. by maintaining a.` rapid forced' flow of a superheated gaseous substance through said heater in indirect heat exchanging relation with the said steam and oil vapor mixture and maintaining a temperature dierential of less than Iabout 500 degrees F. between the said superheated gaseous substance and the hot steam oil' vapor mixture.

Signed at Cleveland, in the county of Cuyahoga, and State of Ohio, this 23rd day of'May7 1919.

lCI-IAUNCEY B. FORWARD?"

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