US2245625A

US2245625A - Apparatus for production of low boiling point hydrocarbons

Info

Publication number: US2245625A
Application number: US141961A
Authority: US
Inventors: Trotter Joseph Wilson
Original assignee: Individual
Current assignee: Individual
Priority date: 1937-05-11
Filing date: 1937-05-11
Publication date: 1941-06-17
Anticipated expiration: 1958-06-17

Description

June 17, 1941. 1 w, TRQTTER 2,245,625 APP-ARATUS FOR PRODUCTION OF LOW BOILING POINT HYDROCARBONS,

Filed May 11, 1957 4 Sheets-Sheet l Lm m June 17, 1941. J, W. TROTTER 2,245,625

APPARATUS FOR PRODUCTION OF LOW BOILING POINT HYDROCARBONS Filed May ll, 1957 4 Sheets-Sheet 2 June 17, 1941.

J. w. TROTTER 2,245,625 APPARTUS FOR PRODUCTION OF LOW BOILING POINT HYDROCARBONS Filed May l1, l193'? 4 Sheets-Sheet 5 June 17, 194,1. v 1, W, TRQTTER 2,245,625 APPARATUS FOR PRODUCTION 'OF Low BOILING POINT HYDROOARBONS Filed May 11, 1937 4 Sheets-Sheet 4 f fi . f f [m/ef//ar' Joselb iff/Waffen y 4 N. 7 s I Patented June 17, 1941 joseph Wilsonfrotter, Toronto,.0ntario,ilanadaj I ApplicationMay I1, 1937, SerialiNd 1413961' v9 caims.V (o1. 19e-'406) The principal objects of the inventionV are to produce a gasoline, ether orlotheriliquid'hydrocarbon of high quality bo'th 'in respect to puri-ty and octane rating, which will produce extram'dinarily high results in powervalues when used in internal combustion engines:

A furtherand 'important object is to produce a hydrogenated product free from sulphur' and otheriagents which will deleteriously .affectymetal parts with Whichit may comelinr contact When in use.l 'Q1 'o i y. n

A still further object is to devise a Yprc'icesfs which may be' effectively controlled to eliminate losses and` to produce thedesired resultsoinan economical manner.

The .principal features ofthe inventionconsist in the novel steps of treatment of hydro-carbon oils of the paraffin series. of approximately 45 to 47 Baume in the presence of superheated steam whereby increasing temperatures and :decreasing pressures are applied in non#corrosivelir lined apparatus,'and in the provision ofan arrangement of .apparatusl to enablethe effective treatment of the different boiling points in the oil constituent stepby'step and "from which the heavier products 'can be removed'in the various puriers and separators provided, as will appear from the following detailed description of the apparatus and the successive steps of treatment of the hydro-carbons` therein.

yIn the accompanying drawings,

Figure 1 is a diagrammatic plan of the ar.- rangement of the various units comprising la complete plant for exercising the improved process of producing Various products from vhydro-- carbon oils.

Figure 2 is an enlarged plan view showing the arrangement of the feed tankreceiving its supply from the oil preheaters and the accumulator and high pressure reaction chambers connected therewith. v

Figure 3 is a `longitudinal sectional elevation of one of the reaction chambers.

Figure 4 isa longitudinal part sectional elevation of one of the vaporizers shown connected to the reaction chambers.

Figure 5 is a longitudinal part sectional elevation of one of the converters. c

Figure 6 is a plan section of the converter on the line 6--6 of Figure 5.

Figure 7 is an enlarged diagrammatic plan of the heater of the converter.

Figure 8 is a longitudinal sectional `View of one of the digesters.

Figure' 9 'is' a cross sectional view through' the dges'te'r on th 1ine9'-`9`of Figure '8.

Figure 'l0l is a 'longitudinal part sectional elevation of one yofltlfiepuriflers i Vllit'gure 11 is'an enlarged ydiagrammatic plan ofL the -batteryvof converters and digesters connected Withthe vaporizers.

Referring tothe drawings, a Vstorage tank I of suitable capacity 4for containing a supply of topped crude hydro-carbon is arranged in a desirable location. "Thhydro-cabon Sis conducted from the tarikll through a Valve-controlled pipe 2 to a battery of high pressure pumps 3 which feed at f. a pressure up .to 10.00 lbs. per square' inch to an .15.. .Y A s accumulator 4I l A reservoir '6isfpi'ped 'to connect with the pipe [leading to 'thepunps 31and is also connected by a l'ipe Zto the 'lead from the storage tank l,

..Aboth .pipes ben'g controlled by suitable valves.

, topped vcrude hydro-carbo-ns and 'fed by said pumpsrinto-itheaccumulator "4 in a Vpreheated condition.

'Ihe'hydro-carbons pumped to the accumulator 4 are Yconducted therefrom by vpipe* I3 to Voneor morefabattery of preheater furnaces |14 in which lit is --heatedto Ia rtemperature of approximately 750. F. vand from rthe furnaces it is conducted 4by avalved pipe l5 to the feed tank I6 where it is unified before passing onthrough pipe l1 to an accumulator I8 Vfrom which it ows through valve-,controlled branches to the Vhigh pressure molecular reaction tanks I9 which are arranged-'ina battery ywithin an enclosed heatretaining chamber 20 and are adapted to break upthe mass'by 'bruising-and separating the molecules.

19, .aswmay lbe required, which are approximately 36 diameter by 35 feet in length, through trans- The pipe 23 conducts the vapour, which has? been held in passage through the tanks. |9 for ay period of approximately ftee'n minutes lat al temperature sustained by the walls of the chamber at a pressure of approximatelylOOO` lbs.

per square inch, to a tank 24 arrangedtransversely of the battery of reaction tanks I9 and' in which the product is unied. Fromthe tank 24' it is conducted through Valved pipes 24" to a group of vertical vaporizers 25 (Figure 4)v into which it is sprayed through a perforated coil' 25" into a body of oil, which is fed tothe vaporizers from a feed tank 251, at a temperature of about 750 F., thereby imparting heat to thebody ofA oil which is carried to a series of purifiers` as hereinafter described. i l L The vapours rising in the vaporizers 25', which are approximately 8 feet in diameter and 60'feet high, are conducted to a batteryof twelve converters 26, shown in detail in Figure 12, by a conduit 21, which is connected by 21 to each converter.

The vapor enters each converter through the tubular column 28, (see the detail.' Figure 5) which discharges from the lower end against an electrically heated hot plate 29 (Fig. 7) arrangedv immediately below a perforated plate arranged in the end of the column (Fig, 6). VScreens of a decreasing mesh are arranged between the several sections of the column 28. A perforated tube ring 30 is arranged belowa balile 3| in each converter to act as a blow-out to clean out the bottom of the converters througha valved cleanout 32, steam being conducted thereto' from'the steam line S through valved branch pipes 's..

The vapours are discharged from eachcon-y verter through a perforated rose 33 to thel outlet 34, The discharge of the vapoursV againstthe hot plates in the converters raises the temperal ture, which has been reduced in the vaporZers,

to approximately l000 F. at a pressureof aboutv 250 lbs., and the resultant reaction is to produce in the converters a vapour which willproduce a gasoline of from 60 to 68 Baum in accordance l with the number of converters it is passed valved Vleadsl through. VGasoline of approximately *Baume and 10 octane may be produced by passing ,thel

vapours through converters a to d, 64 Baum by passing through eight converters. a to and 68 Baume by passing through the twelve verters to m.

The battery of converters is preferably arranged in groups' of six, a to f', each converter.

taken off by the conduit A, but suitably valved by-pass pipes-gare arranged so. that the dis-l charge from the lrst'group of 'threeconverters a toy c or any. additional'number may bef-takenare coupledhto `a "7o, to each of the converters of this group of six and Y in series through the remainder of said group of six.

'Ihe discharge from the first group of six is conducted through conduit A to the inlet of the end converter h of the second group h to m and the discharge from h and the succeeding tanks of the group may be carried in series by the valved by-pass pipes n or the discharge may be conducted by a common conduit B to a conduit C, which is connected to the inlets 35 of the battery.4 of digesters 35, which are approximately 4 feet in diameter and 60 feet high.

,The vapour flows into each digester through against an electric hot plate 36 as shown in Fig- [ure 8, and steam. at about 1000 Fl is injected through the coil 31 fed thereto through the con- Iduit 31' leading from the steam line S. The

steam striking the hot plate, being convergently directed by the baille 39 causes a separation of the 4hydra'genwhich mixes with the vaporized oil whichis maintained at a temperature of about 1000 and .apressure'of 250,1bs. Perforated screen 39X are arranged in` spaced relation throughout the height of the tank' to effect a thorough unification of the oil and hydrogen molecules and a thorough saturation of the hydro-carbons.`

A perforatedrose 40 is arranged at theinner i end lof the outlet conduit 4| of each digester.

A perforated coil 3 8 is arranged in each digester and is` connectedby a conduit 38' to a high pressure air-line to enable the cleaning of the digesters.

4Valved by-pass conduits 4|' connect theoutletsof each digester with`.the `inletsli' to enable the `vapours being passed in series through the' digesters or such vapours'may be carried to the digestersl in multiple and a common conduit 4|X isconnected to all outlets. Petroleum ether may be producedfi'n passing the vapours Vthrough the entirejbattery of converters and digesters at predetermined"temperatures and pressures and thejregulation of time `treatment by the control of the various valves in'the system.

The outlet conduit `4|x from vthe digesters conveys-the producedyv'apour to a battery of restv chambers-42 which are in the'form of vertical cylinders'approximately Sfeet in diameter and 60 feet high, in which the vapour may be held at a temperature of Vapproximately 1000F: and a pressure of aboutl 250 lbs. for a period of about thirtyseconds more orless in accordance with the-.particularcharacteristic of the product desired. Fromjghey stills 42 the vapours are conducted to an accumulator header 43, which is aboutS feet in diameter and 25 feet long and Whichovercomesany surge. v .l

.The outlet.44 from.the header 43 is connected by pipe 45 ,with the superheated-'steam line S.

An oil separator 46 is arranged in the outlet 44 and said outlet leads throughxa'conduit 41 in the form of av verticaluloopgarranged in an expzinsiontovvertii,V which is externallyheat insulated to maintain temperatures: Thisloop extends from the top of the Ytower to a .point adjacent to the bottom; `where it Adischarges its vapours'against a heater plate E4 9, l'I 'lie tower 48 .whichis about l2 feet diameter and; 115 feet lhigh is" provided with spaced Yscreens 50 ranging from about 40 mesh yat the bottom to 80 mesh at the too-which furtherensu'res lthe thorough admixture -and .treatment Vof* the hydro-carbon gases.' These screens are of silver Wire which assist in raising the hydrogen Vcontent of the hydrocarlcmn vapours.

Any oil condensed in the accumulator 43, the oil separator 46 or the tower 4,6 is conducted by a pipe line l to the preparatory tank Il.

The Oil heated in the vaporizers 2.5 and anycondensates from Athe converters 26 and digesters 35 is conducted to a battery of purifiers 52 which are here shown in the form of a series of tanks of about 8 feet diameter and gradually decreasing height from 80 feet to 50 feet. The oil is fed into perforated tube rings 53 arranged near the bottom thereof which project the oil upwardly in ne jets into a body of distilled water, supplied by a pump 56 connected with the supply tank 51. Any suitable means may be provided for maintaining the water at a desired level in each purier. The oil rising to the top of each of. the purifiers is conducted from the top of one purifier to the bottom of the adjacent one, and in its passage through the series is divested of its sulphur and other objectionable constituents.

The nal oil product of the purifiers is fed into a perforated tubular conduit 58 extending longitudinally of the preparatory tank Il approximately l0 feet diameter and 40 feet long to treat the crude oil to bring it to the desired gravity.

A pipe 59 leads from the tank Il to a blowdown tank 60 and connections 6l lead from the bottom of. each of the puriers to said blowdown.

The vapour rising from the tower 48 is carried through pipe 62 to the vapour condenser 63 of any suitable form.

The vapour or partly condensed produce is then directed from the condenser 63 to the surface condenser 66 or to the water condenser 61 which is arranged in a suitable by-pass circuit.

A vacuum pump 6'8 conducts the condensate to the settling tank 69.

Electric energy from a suitable source is supplied for motorized valves which are used throughout and for the heaters and lighting etc.

`It is an important feature of this process that all the tanks, such as the accumnlators, preheaters, preparatory chamber, reaction tanks, vaporizers, converters, digesters, stills, etc. (and all connecting piping) are made of such dimensions as to carry the high pressures and temperatures required and all such tanks are preferably monel metal lined which prevents corrosion and assists in the hydrogenation of the petroleum which is treated throughout in the presence of. steam.

What I claim as my invention is:

l. An apparatus for treating hydro-carbons comprising in combination high pressure pumping means, means for introducing hydro-carbons in predetermined proportions to said pumping means, heating coils receiving the discharge from said pumping means, means for heating said coils, a series of reaction tanks, conduit means receiving the heated product from said heating coils and connected in multiple with one end of each of said reaction tanks to supply said product thereto, means for selectively and variably controlling the iiow through said reaction tanks yto retain the product under pressure for a predetermined time, vaporizers, means maintaining liquid bodies of hydro-carbon in said vaporizers, means connected with said reaction tanks for receiving and conducting the said heated product therefrom to said vaporizers, means in said vaporizers connected with the latter means for receiving the said product therefrom and projecting the same upwardly upper end of said Vaporizers for receiving and conducting the resultant vapour product therefrom, a battery of converters, means for variably directing said resultant vapour from said latterv conduit means to said converters in accordance with the characteristics required of the' iinal product, heaters in said converters, and means for condensing the resultant vapour produc-t.

2. An apparatus as claimed in claim 1 in which the converters comprise tanks with heaters therein to rst heat the incoming vapours from the vaporizers and being provided with means for feeding steam into the ow of heated vapours as they are released from said heaters into the tanks.

3. An apparatus as claimed in claim 1 in which the vapour from the vaporizers is fed through a common conduit and individual valved branches to each converter, and each converter is provided with a valved outlet connected to a common conduit, and valved by-pass conduits are arranged between said individual inlets and outlets to conduct the vapours from the vaporizers in series through the converters or in multiple in accordance with the characteristics required of the product to be produced.

4. An apparatus as claimed in claim 1 in which each of said converters is formed with a downwardly extending inlet, a hot plate arranged opposite to the discharge end of the inlet, means for convergently distributing steam into the vapours discharged from said inlet, an outlet, and valved means for controlling the flow of vapours to the inlets and from said outlets.

5. An apparatus as claimed in claim 1 in which digesters are provided with downwardly extending inlets and conduit means to receive the vapours emanating from said converters and conduct same to said downwardly extending inlets, a series of screens being disposed in surrounding relation to the inlet, means being provided for raising the temperature of the incoming vapours, and means for introducing steam into the digesters. l

6. An apparatus as claimed in claim 1 having digesters connected with and receiving the vapours from said converters, valved conduit means for selectively directing the vapours through said digesters in series or in multiple, rest chambers receiving the vapours from the digesters, an expansion tower, conduit means directing the Vapours from said rest chambers into the lower end of said tower, said tower having a plurality of screens disposed in the path of ow of the vapours, a condenser connected with the top of said expansion tower, and means for separating the condensates.

7. An apparatus as claimed in claim 1 having digesters connected with and receiving the vapours from said converters, rest chambers having valved inlets and outlets, means for variably connecting said digesters to said valved inlets, a header tank, conduits connecting said rest chambers with said header tank, means for adding steam to the vapours at the header tank, an expansion tower, a conduit connecting the header with the expansion tower, an oil separator in said latter conduit, and condensers connected to the expansion tower,

8. An apparatus as claimed in claim 1 in which the reaction tanks comprise a multiple of tanks connected in parallel in the flow circuit and having valved inlets and outlets at the respective ends, said inlets and outlets being screened,`

tilled water and having means in the bottom for l0 spraying fluid hydro-carbon upwardly therein, means for supplying uid hydro-carbon to said latter means, means for conducting the liquid hydrocarbon in series from the top of each purifier to the spraying means in'the bottomV of the next, a preparatory tank connected to the nal discharge ofsaid purifiers, and means for feeding the contents fromY said preparatory tank to the inlet of said pumping means.

' JOSEPH WILSON TROTTER.