US1324212A

US1324212A - Process for obtaining distilled products from petroleum and other oils.

Info

Publication number: US1324212A
Application number: US20541917A
Authority: US
Inventors: Artie A Stapp
Original assignee: Individual
Current assignee: Individual
Priority date: 1917-12-04
Filing date: 1917-12-04
Publication date: 1919-12-09
Anticipated expiration: 1936-12-09

Description

. Au A. SMP?. PHESS- FOR OBTAINING MSYILLED PWUDUCTS Fi E @MEMS MJD @HIER GHS.

APPLICATIDN FILED DEC. 4. 19H'- 2 SHEETS-SHEET i.

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Al A. STAPP. PROCESS FOR OBTAINING DIS TILLED PRODUCTS FROM PETROLEUM AND OTHER OILS. APPucATloN FILED No.4. 1917. k Lggmg., Patented Dec. 9,1919.

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ARTIE A. STAPP, OF DENVER, COLORADO. i

PROCESS FOR OBTAINING DISTILLED PRODUCTS FROM PETROLEUM AND OTHER OILS.

To all/@hom may concern Be 1t known that I, ARTIE A. STAP?, a

' citizen of the United States of America, re-

siding at the city and county of Denver' and State of Colorado, have invented a new and useful Process for Obtaining Distilled l Products from Petroleum and other Oils, of which the following is a specification.

My invention relates to a new process for obtaining distilled products from petroleum and other oils.

The objects of my process are:``

First: To provide a continuously oil feeding process for obtaining distilled products, particularly gasolene, from petroleum and other oils by first subjecting such oils to a pre-heat suflicient to remove the low-boiling hydrocarbons, particularly the gasolene-fraction, and condensing it and conveying it to t a gasolene container.

Second: To provide a continuously oil feeding process that first removes the gasolene lfraction by a low heat, and then subjects the oils tof heat of sufficient temperature to vaporize the oils, then subjects the vapors to a temperature suiicient to crack the vapor, then condensing the cracked product and separating conveyingthe gasolene fraction t'o a container.

Third :v To provide a continuous oil feed process that first removes the gasolene fraction by a low heat and then subjects the oils to higher temperature suiiicient to vaporize the oils, then subjects the vapors to a temperature suiiicient to crack them, then condenses and separates the cracked product and conveys the'gasolene fraction to' a con-4 tainer, and that passes the gas through va superheaterto a vappri'zer and thence to a cracking chamber to increase the percentage of saturated hydrocarbons, and thus reduces the loss by gas' formation. Also, to provide Specification of Letters Patent.

Patented Dec. 9, i919.

Application filed December 4, 1917. Serial No.4 205,419.

Fig 2 is a vertical, longitudinal, sectional view of one of the gasolene. containers.

Fig. 3 is a vertical, longitudinal, sectional view of the vaporizer, showing a reciprocating carbon scraper therein.

Fig. 4 is a vertical, transverse, sectional View of the vaporizer, showing an end view of the scraper.

Fig. 5 is a horizontal, sectional view on the line 5-5 of Fig. 4.

Fig. 6 is a longitudinal, sectional view, showing a lcylinder and hydraulically, operated piston therein, to which the 'carbon scraper rod is secured; and

Fig. 7 is a side view embodying a slight modication in connection with the gas superheater. Q

Similar letters of reference refer to similar parts throughout the several views.

M process has for its essential object'the obtaining of low boiling hydrocarbons from petroleums and heavy oils in a continuous oil feed apparatus that is arranged to remove the gasolene fraction as well as to extract benzene and other valuable products from oils, and at the same time mechanically eliminate the deleterious carbon and other residue products during the operation of the process, thus enabling me to produce gasolene and other products economically and on a large scale. Inasmuch as the apparatus herein illustrated has been especially designed to effect this process,l a detailed description of the same is given, as follows:

The numeral 1 indicates a petroleum or other oil supply tank, which is connected by a pipe 2, with a suitable pump 3, which is also connected by a pipe 4, with a preheater, which constitutes the first unit Aof the improved apparatus.

This pre-heater consists of a pipe or tube 5, of suitable dimensions, a portion of which is housed within a heater 6, in the form preferably of a brick or other heat resisting chamber, the portion of "the tube 5, outside of the. heating chamber being provided with an asbestos wrapping, this arrangementfefL fecting a gradual heating of the oil after entering the said pre-heater.

I may employ either oil or gas as a heating medium throughout the apparatus, and to this end a fuel pipe 8, projects into the heater beneath the tube 5, the pipe being arranged with suitable burners and being connected with a fuel supply.V The pipe 8, is provided with a valve 9, for regulating cof,

thc fuel supply. The end portion of the pipe 5, within the. heater` has connected therewith a vertical tube or pipe 10, which constitutes a filtering column, and the heater is constructed to inclose this column also. A pipe 11, extends from the column 10, and connects with a condenser coil 12, which is connected by a pipe 13, with a gasolene container 14.

The filtering column is filled with any suitable material such as iron balls or broken clay, which form a condensing medium for the vapors, whereby a closer separation of the vapors at a given temperature is effected.

A pipe 15, connects the inner end of the tube 5. with a cylindrical vaporizer 16, which is inclosed in a suitable heating chamber 17. and beneath the vaporizer is a fuel pipe 18, having suitable burners, the pipe being connected with a fuel supply. The vaporizer has a vertical depending outlet pipe 19, at each end and these pipes connect with a conveyer tube 20, in which is mounted a spiral conveyer 21. The carbon which adheres to the wall and ends of the vaporizer is removed in a manner to be here` inafter described, and passes down through the pipes 19, to the tube 20, whence it is carried forward by the spiral conveyer and deposited in a container 22, which is connected to the tube 20, by a valved pipe 23. The container has a draw-off valve 24, for removing the carbon, during which operation the valve in the pipe 23, is closed.

The heater 17, has a floor 25, beneath which the conveyer tube runs, and inner end walls 2,6, which are spaced from the main or outer..;en-d walls. In the space between these walls arelocated the pipes 19, which are thus shielded from the heat generated in the heating chamber. The heaters (i and 17 are provided with outlet pipes or chimneys 27. 1

From one end of the vaporizer extends a vertical pipe 28, which constitutes a cracking chamber' and this pipe is preferably tapered from its lower or inlet end to its upper or outlet end. The cracking tube 28, is surrounded throughout its length by a stack 29, having an outlet pipe or chimney at its upper end, and which is spaced all around from the cracking tube. The stack is formed at regular intervals with suitably arranged openings 30, in which arey introduced burners 31, which are connected to fuel pipes 32 leading to the fuel supply.

The burners 31', are adapted to raise the temperature in the cracking tube to 450 degrees C. or above, in order to break up the heavier hydrocarbons in hydrocarbons of lighter gravity. A pipe 34, extends from the upper end of the cracking tube and forms an outlet for the vapors in said tube. This tube connects with a `condenser 35,

which in turn is connected by a pipe 3G, with a separator 37, which is preferably cylindrical in form and is housed within a heater 38. The separator has a filtering column 39,

at one end, similar to the filtering column 10, of the pre-heater and supplied with the same character of condensing or separating material as the column 10, and a pipe 4() extends from the column 39 to a condenser 41, which in turn connects with a gasolene container 42. A fuel burner 37A, extends beneath the separator and connects with the main fuel supply pipe.

The condensers 12 and 41 are connected by a gas conveying pipe 43, which is connected by a pipe 44 with a pipe 45, which connects with the upper ends of the containers 14 and 42. rllhe pipe 45, extends from the containers 14 and 42 to a suitable gas pump 46, to which is also connected one end of a pipe 47, which connects at its other end with a pipe 48, that forms a connection between the conveyer tube 20 and a residue container 49.

The end of the separator 37, opposite that which receivesthe pipe 3G, is provided with a pipe 50, which connects with the pipe 15 leading from the pre-heater. The pipes 15 and 50 are formed with traps 51 and 52, respectively, which collect any carbon passing from the pre-heater and separator respectively. The pipes 15 and 50 are also connected by a gas conveying pipe 53, which in turn is connected by a branch pipe 54, with the gas pipe 47, and the pipe 47 has a branch 100 pipe 55, which leads to one end of a superheater 56, the other end of which is connected by a pipe 57, with the vaporizer 1G.

A fuel burner 58, extends beneath the superheater 56, and is connected with the fuel supply. rlhe gases passino through the pipe 47 enter' the superheater through the branch pipe 55, and are there subjected to a high temperature by contact with incandescent carbon in the said heater after which they pass through the pipe 57 into the vaporizer, when they mix with the vapors therein and pass into the cracking tube, where the presence of such gas revents the formation of gas of the same clihracter, thus maintaining a state of equilibrium in the action of the cracking tube, the reaction tending toward the formation of low boiling hydrocarbons instead of gas.

The gas which is released in the separator passes through pipes 40, 43 and 44, to the upper ends of both gasolene containers, whence it is drawn away by the pump 46, and forced through the superheater 56 to the vaporizer, where it mixes with the vapors therein, which then ascends in the cracking tube, increasing the percentage of saturated hydrocarbons as above stated. The vapors and gas pass up through the cracking tube and thence through the condenser 35 to the 130 separator, the pipes 53 and 54 acting to 'equalize the pressure on the opposite sides of the traps 15 and 52. Thus a continuous circulation of the gas through the apparatus is effected by the pump 46, and a constant pressure of above one atmosphere is maintained by a pressure release valve 59, which permits escape of the gas under excessive pressure.

The oil pipe 4, leading from the oil pump 3, to the pre-heater is also provided with a pressure release valve 60, which is connected by a pipe 61, with the pipe 2, leading to the o1l supply tank, or if desired, the pipe 61, may connect directly with the supply tank.

The gasolene containers 14 and 42 are each constructed as shown in Fig. 2, and are provided at their lower ends with draw-oft` valves-62, by which the carbon which settles to the rbottoms of the containers can be withdrawn. These containers are also provided with spigots 63, which are connected to the outer ends of threaded nipples 64, on the inner ends of which are screwed elbows 65, each of which is provided with a diaphragm having a conical aperture 66, which is adapted to be opened. or closed by a needle valve 67, which extends slidably through` an axial hole-in a cap 68, which is screwed upon the upper end of the elbow. The upper end of the valve is pivotally connected to the lower end of a link 69, the upper end of which is pivotally connected to a lug on the bottom of a float 70, which is upheld by the body of gasolene in the container. The valve 67 has secured thereon a stop collar 71, which yengages the cap 68 and thus limits the upward movement of the valve. The vertical portion of the elbow above the diaphragm, is provided with apertures 72, through which the oil flows to the'conical aperture in the diaphragm, and thence out through the spigot. When the flow of oil into the container is continuous, the float is elevated and the needle valve is raised and permits: the oil to run out through the spigot, but when th. oil in the tank drops below a certain level, the oat descends and the needle valve closes the outlet, and prevents dripping at the spigot.

In all apparatus'for the treatment of petroleum to produce low boiling hydrocarbons, the problem of the removal of carbon, wherever it settles and adheres, must be met, in order to insure efciency, and in the present apparatus I have devised the following mechanism for removing carbon from the vaporizer, and also from the vapor pipe 34, leading fromA the cracking tube, the mechanisms beingthe same in both places.

In Fig. 3 is illustrated an enlarged view, in section` of the vaporizer, showing the reciprocating Scrapers, and in Fig. 6 is illustrated mechanism ,for reciprocating the Scrapers. The scraping devices are mounted on a rod 73, which passes through a packing box 74, on one end of the vaporizer. Upon the end of the rod which extends into the vaporizer is secured a hub 75, having oppositely extended wing portions 76, Which are provided with dove-tailed recesses, and in each of these recesses is slid the shank portion of a scraper 77the edges of the shank being beveled lto fit the recess, as clearly shown in Fig. 5.

, The shanks of the Scrapers are slotted as shown in Fig. 4, and bolts 78 are passed through the said slots, and through holes in the wings, and receive clamping nuts 79.

tial rotation bein'g suflicient to, rotate the scra'pers 77, a distance equal to the length of their cutting edges, and an angle plate form of scraper 81 is secured to the face of the i blade 80, as shown in Fig. 4, which is adapted to contact with the end plate or head of the vaporizer, and scrape a Vportion oi' the carbon therefrom on each alternate stroke of the rod.

, A hub 82 similarto the hub 75 but facing in the opposite direction, is secured upon the rod 73, at a distance fromV the first hub, slightly less than halt1 the length of the vaporizer, and this hub is provided with. Scrapers similar to those carried by the hub 75, with the exception that the blade corresponding to the blade is apertured to receive the rod `73, while the end scraper corresponding to the scraper 81 is formed in two parts which lie on opposite sides of the rod 73, as shown.

The rod 73 is adapted to have a stroke slightly greaterthan the distance between the two scraping devices, in order that each scraping device may overlap the path of the other at the center portion of the ,vaporizer, and thus keep the entire surface of the same free from carbon.

The outer extension of the rod 73, passes through a cylinder 83, which is provided with a packing box at each end, and upon that portion of the rod within the cylinder is rigidly mounted a piston 84 having projecting hubs on each side of the same, which engagethe heads of the cylinder, to define a space between each cylinder head,'and the adjacent face of the piston. Pipes 85 are screwed into threaded apertures inthe cyll The slots permit'adjustment of the Scrapers inder adjoining their ends, and the inner ends of these pipes are screwed into a circular valve casing 86, at diametrically opposite points. This casing is also provided with an inlet pipe 87, and an outlet pipe 88, at diametrically opposite points, and a valve 89 is pivotally'mounted in the casing. This valve is a four-Way valve, and permits the entrance of water into one end of the cylinder back of the piston, and the exit of water from the other end of the cylinde-r simultaneously. A rock arm 90 is secured to the stem of the valve, and a rod 91 is connected to the rock arm, and any suitable mechanism for operating the rod to oscillate the valve may be employed. Any suitable means may also be employed to partially rotate the rod 73, at the limit of each stroke, andas one Way of accomplishing this, 1 may form the rod 73 square, for a portion of its length, and have the squared portion slide through an intermittently operated ratchet wheel 92 as shown, this feature forming no part of the present invention. By giving to the scrapers a continuous `reciprocating movement, together with a partial rotation at the end of each stroke, the Whole interior surface of the vaporzer is kept free from carbon deposit, and the carbon thus removed passes down through the pipes 19, and into the conveyer pipe 20, where it is carried by the conveyor 21 to the container 22. The residue, which is a tarry substance, passes from the conveyor pipe up through the pipe 48, and into a container, whence it may be drawn oii' from time to time. n

In Fig. 7, the superheater and vaporizer are shown connected by a pipe 57A, a part of which is in the form of a condenser' 57B, for the condensation of any liquids formed in the superheater.

The first operative step of my process consists of automatically feeding petroleum oils to a heater which I term a pre-heater, Where the temperature is only sufficient to release from the oil the low boiling hydrocarbons, particularly the gasolene fraction.

The second step comprises means herein described for passing the liberated gasolene product to a condenser 12, and then to a gasolene container 14.

The third step consists of means including a pump for drawing the gas from the con denser and gasolene container and forcing the same into and through a gas superheater to a vaporizer, or from the superheater through a condenser and thence to the vaporizer, depending upon liquid formation in the superheater.

This gas superheater and the pump and piping form a coperating part of a second condenser 41 and gasolene container 42, which Will be particularly referred to hereinafter.

The fourth step of my process is to then convey the oil from a pre-heater, horizontally arranged, to a vaporizer 16, that is provided with a cracking chamber 28.

The vaporizer is surrounded by a heater 17 and the cracking chamber is surrounded by a stack 29, and both the stack and the heater are provided with gas heating apparatus for securing and maintaining the required temperature.

The vapors arising in the cracking tube are converted by the cracking process into a mixture of gases and low and high boiling hydrocarbons, which pass from the cracking tube, through the condenser 35, and into the separator 37, Where the temperature is such that a separation of the hydrocarbons takes place, the low boiling product passing through the filtering column 39, pipe 40, and condenser 41, to the container 42, While the high boiling product is returned to a vaporizer for further treatment, the uncondensed gases being conveyed to the superheater, and thence to the vaporizer.

The next step is then to convey the oil products from the separator to the vaporizer 1G or to one heated to a diiierent temperature, which is done through a pipe 50, which connects 'with the pipe 15 that leads from the pre-heater. The gas in the containers 14 and 42, is thus drawn through the pipe 45 by the pump 4G, and is forced through the pipes 47 and 55 to the superheater 56.

The vaporizer 16, as Well as the pipe leading from the cracking chamber to the condenser 35, is provided with suitable carbon loosening and ejecting apparatus.

The next step is then to superheat the gas in the superheater 56, Which is done by a suitable gas burner 58, and to then convey this superheated gas directly into the vaporizer 16, or rst pass it through a condenser as before mentioned, and then to the vaporizer. The superheater is also connected to the residue receptacle 49, and with the conveyertube 20, through the pipe 48.

The superheated gas from the pre-heater and the separator is forced by the pump 46, into the vaporizer, Where it miXesWith the vapors therein, thereby subsequently increasing the percentage of saturated hydrocarbons, and these mixed gases and vapors pass up through the cracking tube under a continuously increasing temperature, andv thence through the condenser 35 to the separator, and from it to the condenser 41, and to the gesolene container 42.

A pressure release valve 59 is placed in the gas circulating system, that permits the pump to maintain a constant pressure of about one or more atmospheres.

My process provides a simple, easily and economically operated process for the treatment of petroleum oils to produce loW boiling hydrocarbons such as gasolene and other products therefrom, as set forth in the treatment embodying theessential steps of my process.

I do not, however, wish to be limited in them or to the exact operation of them as described, as changes might be made without departing from my invention.

Having described my process, what I claim as new and desire to secure. by Letters Patent, is z' The herein described process of continuously producing low boiling hydrocarbons, as kerosene, benzin and gasolene from petroleum oils, which consists of first treating the oil to a temperature suiiicient only to release the gasolene fraction, then condensing the gasolene in said fraction and separating the same from the uncondensed gas which is subjected to further treatment as set forth below, then vaporizing the heavy oil, and cracking and condensing and sepa rating the low and high boiling hydrocarbons, condensing the gasolene fraction, then superheating the separated gas together with that previously mentioned, and mixing the same with the vapors undergoing the cracking treatment.

In testimony whereof I atlix my signature in presence of two witnesses.

ARTIE A. STAPP.

Witnesses:

G. SARGENT ELLIOTT, ELIZABETH SMITH.