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Publication numberUSRE16052 E
Publication typeGrant
Publication dateApr 21, 1925
Filing dateApr 9, 1917
Publication numberUS RE16052 E, US RE16052E, US-E-RE16052, USRE16052 E, USRE16052E
InventorsEmil Schill
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
And franz woidich
US RE16052 E
Abstract  available in
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Claims  available in
Description  (OCR text may contain errors)

April 21, 1925,

511...] B 4 Q k282i E. SCHILL ET AL Original F'iled April 9.

PROCESS OF AND APPARATUS FOR EXTRACTING, LIQUEFYING,

AND SEPARATING LIQUEFIABLE CONSTITUENTS OF GASES th uuu 6 jM/QWHtOZ 8 Reissued Apr. 21, 1925.

UNITED STATES PATENT OFFICE- EMIL SCHILL, OF WOODMERE, NEW YORK, AND FRANZ WOIDICH (KNOWN AS FRANCIS I SALES WOIDICH), OF SAPULPA, OKLAHOMA, ASSIGNORS TO CONTINENTAL GAS OOMPRESSING CORPORATION, OF NEW YORK, N. Y., A CORPORATION OF NEW YORK.

PROCESS OF AND APPARATUS FOR EKTRACTING, LIQUEFYING, AND SEPARATING LIQUEFIABLE CONSTITUENTS OF GASES.

.Original No. 1,415,058, dated May 9, 1922, Serial No. 160,642, filed April 9, 1917. Application-m reissue filed May 28, 1924 To all 1071 cm it may concern:

Be it known that we, EMU. SciIILL, a citizen of lVurttemberg, Germany, and resident of \Voodmere, Long Island, New York, and FRANZ IVoImon, known as FRANCIS SALES VVOIDICH, formerly a citizen of Austria and formerly a resident of New York, N. Y., now a citizen of the United States, and a resident of Sapulpa, Oklahoma, have invented certain new and useful Improvements in Processes of andApparatus for Extracting, Liquefying, and Separating Liquefiable Constituents of Gases, of which the following is a specification. I

The invention relates to, the extraction, liquefaction and separation of liquefiable constituents of gases and deals primarily with hydrocarbons, although it is also applicable to gases of many other varieties, and has for its object to provide a simple process whereby this may be efficiently accomplished. The improvement further con-- templates the provision of a simple apparatus whereby said process may be efli- 'ciently' carried out. Other objects of our invention will appear from the description 'and the features of novelty will be pointed out in the appended claims.

In the accompanying drawing we have shown an example of our improve-d apparatus, in diagrannnatic form, for illustrative and descriptive purposes and similarly for illustrative purposes the description will be directed to a gas mixture the components of which are hydrocarbons.

'"The gas mixture containing the hydrocarbons to be separated from each other.

and to be partly liquefied, and comingfrom the source of supply, for instance the head of an oil well, or astorage tank, or a pipe line, after thaving been freedin a scrubbar-fromv impurities such as dust, oil, water and other substances carried along mechanically by the gas, enters the com resser-1 2, through a. pipe 3 and is compressed therein to such a. degree of pressure as the particular gas to be treated demands. The 'compressed gas leaves the compressor through a pipe 4 which commufiicates with Serial No. 716,513.

a system of horizontal tubular condensers 5. The compressed *gas mixture flows through the tubes of the condensersin counter current of the coolingmedium, which fills the shells of the condensers and the spaces between the tubes thereof. passing through the condenser system 5 part of the liquefiable roducts, contained in the original gas, Wil be condensed.

The mixture consisting of partly liquefied and partly gaseous hydrocarbons, leaves condenserisystem 5 at the bottom through a. pipe 6, whichconnects with a separator 7. The liquefied hydrocarbons will leave the separator 7 at the bottom through pipe 8, whereas that part of the original gas, which has not yet been liquefied in the condenser system 5, leaves the separator 7 at the top through pipe 9, which connects with the condenser system 5*. The latter also consists of a number of condensers similar to the condenser system 5. In the condenser system 5 some more of the liquefiable hydrocarbons, contained in the original gas,will.

become liquefied-i The individual condens- T ers forming part of each system 5 and '5 each comprise a .tank (a) closed at its ends and divided into interior end chambers (b) and (c) by means of transverse partitions (d).' The chamber (b) is in turn divided into two separate parts 6 and b by means of a partition I) while a sieve, screen or the like divides the 'cliamber.(0) into two parts 0 and 0". The screen c is-provided with a large numberof relatively minute apertures so that the gases and vaporsfiowing therethrough are evenly divided and do not acquire any tendency to select only certain of the passages provided for their a travel but How uniformly with equal pres? sure and relativel equal content'throu'gh all the passages W ereb the full benefit of temperature transfers rom the oil system to be hereinafter described is uniformly obtained. Tubes (6) extend between the partitions (d) and establish communication be-' tween the portions 6 and c of the chambers (b) and (0) respectively while similar tubes 6 extend between 'said' partitions d and ,establish communication between the portions and b of, the chambers c and b respectively. A branch 4 extends from the pipe 4 tothe portion of the chamber 1) ,6, which connects with a separator 7.

= separator 7 at the bottom through a pipe tween the tubes e and e on opposite sides of the partition f respectively. After hav-. ing gone through the condenser system 5* the mixture consisting of hydrocarbons liquefied in the condenser system '5 and hydrocarbons still in gaseous form, leaves the condenser system 5 through a pipe The liquefied hydrocarbons pass from the 8*, which connects with a condensation trap 10,- with which the pipe 8 coming from the I separator 7tis also connected] Such hydrocarbons as have not yet been liquefied in condenser 5 leave separator 7 at the top through pipe 9 leading to the gas expander 11. a

Should it be found that all the liquefiable products contained in. the originalgas are not liquefied in condenser system 5 and condenser system 5, additional condenser systems can be used, all worklng inthe manner described. 7 v Before following the course of the products li uefied in the condenser systems, we will f0 low the gas, which, as shown above, passes through pipe 9 and finally reaches the expander 11, said gas being still under substantially the same pressure obtained in compressor 1-2.

In the expander 11 consisting as usual, of a cylinder or cylinders oflering resistance or doing work and operating in general like a steam cylinder the pressure of the gas will be operatively utilized and in consequence, according to well-known physical laws, the temperature of the gas will drop far below zero.

7 The expanded cold as leaves the expander 11 through a 'p1pe'12, which connects with the lower part of an oil absorber 13, and will rise in the latter after having assed through a grate plate 14 inorder to ecome finely divided. In the oil absorber 13 the cold gas will come into direct contact with the absorption'medium (oil) entering the upper part of thehoil absorber 13 through a pipe '15. The oil flowing down and meeting the up-coming cold gas, will absorb therefrom any such liquefiable hydroany liquefiable products and can be used for illuminating, heating and other purposes.

The absorbing medium (oil) mentioned above enters the system for instance from an oil storage tank 20 through a pipe 21 connecting with the oil circulating pump 22, which pumps the oil through pipe 15 into the upper part of oil absorber 13, mentioned above. As described above, the oil going through oil absorber 13 absorbsthere, from i the gases entering oil absorber 13 through pipe 12, such liquefiable products which have not been condensed in condenser systems 5 and 5.

The cold oil leaves oil absorber 13 at the The oil, which, asshown above, through heat exchange in oil cooler 17, with the expanded 00 d gases, has obtained a very low temperature, is now used in the condensersystems 5 and 5, as a cooling medium for the condensation of the gas mixture coming from compressor 1, 2. The cold oil passes the condensers between the shells and the coils in counter current fashion and while it acts as cooling medium therein,

naturally takes up part of the heat from the hot gases going through the tubesof the condensers. I a j i The oil leaves the cqndenser System13 through pipe 26 connecting withsepara-- tor 27. d

On account of the higher temperature at which the oil leaves condenser system 5", part of the hydrocarbons, which have been absorbed by the oil' in oil absorber 13, will have evaporated again, and in order to separate the oil from such vapors, separator 27 is provided. The oil leaves the bottom of the separator 27 through pipe f28',; which connects with the lowest condenser of condenser system 5.

While the temperaturevof the oil entering condenser system 5 ishigher than the one at which it entered condenser system 5, the oil is still cold enough to serve as cooling medium in condenser systemv 5. The oil leaves condenser system 5 at the top through pipe 29 connecting with separator 30, which serves the same purpose as separator 27, namely to separate the oil from such hydrocarbons, which had originally been absorbed in the oil absorber 13, and which on account of the higher temperature of the oil in con denser system 5, have evaporated again.

The oil which leaves separator 30 has now, through heat exchange in the condenser system, obtained its highest temperature. ,It leaves separator 30 at the bottom through pipe 31, which connects with the oil heater 32 at the bottom of rectification column 33. The purpose of the oil heater 32 will be explained later on.

The oil leaves oil heater 32 through pipe 34, which connects with the top of the above mentioned oil cooler, 17, where the hot oil,

' through the direct contact with the cold gas entering oil cooler 17 at'the bottom through pipe 16, will be cooled down to such an extent that the oil will be cold enough to serve as cooling medium in the above described manner. The cold oil leaves oil cooler. 17 through pipe 35, which connects with the oil storage tank 20 from where it enters the jsystem again in the above described manner.

The application of the oil in connection with the apparatus, serves the following purposes:

1. The absorption of such liquefiable hydrocarbons contained in the original gas mixture, which neither'bycompression, nor

' by cooling, nor by a combination of both, can

be recovered in liquid form.

2. As carrier of" such hydrocarbons not liquefied in the condensers to a point where such absorbed hydrocarbons will be vaporized and, therefore,-separated again.

3. As cooling medium ii. the condenser system,'where the liquefaction and condensation of the original hot gas, coming from the compressor, takes place. V

4. As heating medium in the rectification column f r the fractional separation of the mixture of liquid hydrocarbons obtained in the whole system. according to their respective boiling point.

Vie now go back to the above mentioned condensation trap 10, where the condensates coming from the condenser system 5, 5", are

collected. ,The condensation trap 10 is built on' the well-known principle of a steam trap and serves the purpose of continuously removing the liquid condensates. The condensatesleaving the condensation trap 10, are still under high enough pressure to be lifted to any height within the hydrostatic limits of the original'pressure. The bottom of the condensation trap 10 through ipe line 36, connects with the upper part of a regu* lating pct, 37.

The liquefied hydrocarbons collect in the regulating.pot-37'until the liquid'reaches the outlet of pipe 38, which connects the regu-o lating pot 37 with the dephlegmator 39 on top of the rectification column 33. The dephlegmator 39'is constructed in the form of a tubular condenser. The liquid hydrocarbons coming from regulating pct 37 are used in dephlegmator 39 as a cooling medium, which flows around the condenser tubes, and leave dephlegmator 39 through pipe40 at a considerable higher ten'iperature than the one at which they entered the dephlegmator 39 through pipe 38. The pipe 40 connects with'a separator 41 which acts in the same manner as described above for separators. 7, 7, etc. The liquid runs down through a pipe 42 into the middle of rectification column 33,, from where it flows down, passing a distributor, in a finely divided form, until it reaches oil -heater32. where a certain-part of the liquid'hydrocarhon mixture will be evaporated, necessary for the separating effect in the rectification column 33.

The evaporated hydrocarbons on the other hand will rise in the rectification column 33, into direct contact with the liquid hydrocarbons, pre-heated in the dephlegmator 39 and passing therefrom through pipe 40 to separator 41 and to the rectification column 33 through pipe 42. Such direct contact of the cold liquid with the warm vapors will have the following results:

1. The heavier constituents of the vapor will become liquefied again and will, therefore, drop down.

2. The lighter constituents of the vapors, however,'will rise in the column without becoming 1i uefied.

3. The lighter constituents of the liquid will evaporate and join the vapors mentioned in No. 2, and will rise together with them in the column.

4. The heavier constituents of the liquid will flow down and join the liquefied con stituents mentioned in No. 1. The resultof the process in the rectification column 33 will be practically quantitative separation of the light liquefiable hydrocarbons from the heavier ones, according to the well-known principles of separation 'and'distillation by means of rectification columns.

Such hydrocarbons which will not evaporate in oil heater 32 will collect at the bottom of rectification column 33 and leave the same through pipe 43, which connects with the coil of the gasoline cooler 24, cooled by the cold oil coming from oil absorb-er 13 through pipe line23. From the gasoline cooler 24 thenow cold gasoline, passes through pipe 44 and enters test on 55. The test cup is equipped with a ydrometer for determining the specific gravity of the liquid,

with a thermometer-for the determination of the temperature of the liquid, and with an automatic flow scale for the measurement of the quantity of the liquid passing lili) llu through test cup 55. From the test cup 55 the gasoline passes through a pipe 56, and flows into the gasoline storage tank 57.

By observing the temperatures and the hydrometer readings and maintaining them at the predetermined points for the product desired by the operation of suitable valves in the pipe lines controlling the. flow of the respective fluids (the lighter or heavier fractions) the product ultimately recovered in the tank 57 or 71) will be uniform in quality notwit standing variations in temperature or pressure or other conditions in the dephlegmator or in the coolingor heating system.' The product desired may be either lighter or heavier and the arrangement is such that whatever fraction is determined upon atthe outset, or at any particular period of operation, may be recovered by merely controlling the valves of the liquid systems 44, (or 68, 69) until the thermonr eter' and hydrometer readings correspond to the indications for the particular product which is desired.

In case the oil heater 32 provided in the lower part of the separating column 33 should not furnish a high enough temperature, particularly in winter, an additional gas heater58 is provided. The necessary heating medium for the gas heater 58 is taken from the exhaust gases coming out of the explosion chamber of the engine, which is used for driving the compressor l2, said combustion gases being conducted to said gas heater 58 through a pipe 59. We now have to go back to the vapors rising up in rectification column 33. Said vapors will finally reach dephlegmator 39, cooled as ,described above, by the cold liquid hydrocarbon mixture coining from regulating pot 37.

The vapors rise through pipe 60 until they, get into the upper chamber 61 of the dephlegmator 39. From there said "apors flow down' the tubes of the dephlegmator 39' in counter current to the cooling medium entering the dephlegmator 39, as explained above, through pipe 36. The result of this operation will be the partial condensation of the vapors. The liquid art will collect in the lower chamber 62 of the dephlegmator 39 and will leave the same through pipe 63, connected with a liquid distributor 64 located in the upper part of the rectification column 33. From said distributor the liquid in a finely divided spray will flow down in the rectification column '33 and so furnish the necessary amount of liquid for carrying out rectification and separation.

The vapors, which have not been condensed in the-tubes of dephlegmator 39 will leave the upper part of the lower chamber 62 through a pipe 65, whichconnects with the upper part'of a cooler- 66. As a cooling medium for cooler 66, part of the expanded cold gas, coming from expander 11 is used by connecting ipe 12 .with cooler 66 through the medium 0 a pipe line 67 The cooling medium leaves cooler 66 at the top through pipe 68, which connects with the bottom of oil absorber 13. The liquefied light hydrocarbons condensed in cooler 66 will leave the cooler at the bottom through pipe 68, leading to test cup 69 constructed in the same manner as described for gasoline test cup 55. Through a pipe 70 the liquid leaves the test cup 69 leading into the storage tank 71, for the light liquefied products.

Such liquefiable hydrocarbons, which have been absorbed by an absorbing medium (oil) in the oil absorber 13, as seen above, have been evaporated again from the absorbing 'medium, while the latter passed through the condenser system 5 and 5*. To separate the vapors from the absorbing medium, we have seen above that separator 27 -is provided when the absorbing medium leaves condenser system 5, and'scparator 30 when the absorbing medium leaves condenser system 5. While the absorbing medium (oil) leaves the separators 27 and 30 at the bottom, the vaporsleave the tops of the separators 27 and 30 respectively through pipes 72 and 7 3 and enter the lower part of rectification column 33, where they join the, vapors coming from oil heater 32. In this way they will participate in the separation and liquefaction, which takes place in the rectification column 33. i

Instead of using the expanded gases for cooling the oil, the latter may be cooled by other means as, for instance, by means of water, ice machine, or the like. Similarly, instead of cooling the absorbing medium by direct contact with the expanded gases, the same result may be accomplished by means of an indirect cooling system.

Absorption in an oil absorber may be accomplished either under atmospheric pres sure, as described, or under the pressure obtained in the con'ipressor. In other words, the gas leaving the condenser system 5" may be piped directly into the oil absorber 13. The improved process may also be operated, though not as ellicicntly, by leaving out the oil absorption entirely. In this case the gas leaving the condenser system 5 would either 0 directly to the expander, or, it cooled by water, the gas would pass out to the atmosphere.

The absorbing system may also be used in connection .with other compressing and carbons according to their boiling point by t means of the rectification column in combination with dephlegmators may also be used to great advantage in any existing gasoline plants where the hydrocarbons are liquefied by compression or cooling or by a combination of both.

vapors and extracting liquefiable products therefrom by reducing the temperature of said compressed gas, expanding the deva-' porized gas 1n a cylinder, imparting the resulting reduced temperature to a circulating liquid and using the thus cooled liquid as the means for reducing the temperature of the compressed gas.

2. The process of extracting and recovering various liquefiable vapors from gases containing the same which consists in employing a liquid circulating medium as a vehicle for both high and low temperatures causing said medium to acquire the requisite temperatures from the gases under treatment by flowing it past such gases in a' compressed state and again after having been expanded in a cylinder.

3. The process of extracting and recovering various liquefiable vapors from gases containing the same which consists in compressing the said gases cooling the compressed gases and extracting the resultant liquid, expanding the remaining compressed gases in a cylinder, circulating a fluid medium in proximity to the compressed and the expanded gases and to the products extracted therefrom, whereby said compressed gases become the sole means of producing both thehigh and low temperatures required ".for the extraction and recovery inliquid fo m of the liquefiable vapors, by reason of th: transmittal from time to time to the flui'd circulating medium of the temperature of said gas when in a hot compressed state and again when in a cold state after having been expanded in a cylinder, the fluid liquid .medium transmitting its various temperatures, thus acquired, at the appropriate places, to the compressed gases and to the products extracted therefrom.

4. The process of extracting and recovering various liquefiable vapors from gases containing the same which consists in compressing thesaid gases, cooling the compressed gases and extracting the resultant liquid, expanding the remaining compressed gases in the cylinder, circulating a fluid medium in heat exchange relation With the compressed and the expanded gases and transmitting temperatures thus acquired to the compressed gases and thc liquid products "extracted therefrom, bringing the fluid circulating medium into contact with the expanded gases, and separating from the said fluid medium liquefiable ingredients carried over from the said contact andett'ecting said separation by heat transmitted to the circulating fluid through its said heat exchange relation with the compressed gases whereby said compressed gases become the sole means-of producing both the high and low temperatures required for the extraction and recovery in liquid form of the liquefiable vapors, by reason of the transmittal from time to time to the fluid circulating medium of the temperature of said gases when in a hot compressed state and again when in a cold state after having been expanded in a cylinder, and the transmission of temperatures, thus acquired, between the liquid medium, the gases and the products extracted therefrom.

5. The cyclic process which consists in compressing a gas containing various liquefiable vapors, extracting part of the liquefiable product out of said compressed gas by subjecting the latter in heat exchange relation to the cooling action of a fluid medium containing such absorbed vapors as are not liquefied by compressing and cooling alone, withdrawing the thus extracted liquefied products from the compressed. gas thus cooled, expanding the remaining gas in a cylinder and thereby greatly lowering its temperature, passing said cold expanded gas through a finely divided fluid medium capable of absorbing uncondensed vapors remaining from said expanded gas, employing said fluid medium with its absorbed vapors cooled by the last named ste as the means for effecting .the extraction rst mentioned, separating from said medium the absorbed vapors released by the heat acquired from the hot compressed gases, liquefying said vapors,-cooling said heated and devaporized medium by means of the cold devfaporized' expanded gas, and circulating tlieliquid medium to absorb uncondensed v'a pors from the expanded cold gas and for the subsequent operations hereinabove described.

6. The cyclic process which consists'in compressing a gas containing various liquefiable vapors, extracting part of the liquefiablc product out of said rmnpressed gas by subjecting the latter in heat exchange relation to the cooling action of a fluid medium. containingsuch absorbed vapors as are not liquefied by compressing and cooling alone. withdrawing the thus extracted liquefied products from the compressed gas thus cooled, expanding the remaining gas in a cylinder and thereby greatly lowerin its temperature. passing said cold expander gas through a finely divided fluid medium capable of absorbing uncondensed vapors re said fluid medium with its absorbed vapors cooled by the last named step as the means for effecting the extraction first mentioned, separating from said medium the absorbed vapors released by the heat acquired from the hot compressed gases, liquefying said vapors, cooling said heated and devaporized medium by means of the cold devaporizcd expanded gas, combining the liquefied products and separating the same into the specific liquid end products desired by rectifying with heat supplied by the said circulating liquid medium, and circulating the liquid medium to absorb uncondensed vapors from the expanded cold gas and for the subsequent operations hereinabove described.

7. The cyclic process which consists in compressing a gas containing various liquefiable vapors, extracting part of the lique fiable product out of said compressed gas by subjecting the latter in heat exchange relation to the cooling action of a fluid medium containing such absorbed vapors as are not liquefied by compressing and: cooling alone, withdrawing the thus extracted liquefied products from the compressed gas thus cooled, expanding the'remaining gas in a cylinder and thereby greatly lowering its temperature, passing said cooled expanded gas through a finely divided fluid medium capable of absorbing uncondensed vapors remaining from said expanded gas, employing said fluid medium with its absorbed vapors cooled by the last named step as the means for effecting the extraction first mentioned, separatin from said medium the absorbed vapors re eased by the heat acquired from the hot compressed gases, liquefying said vapors, cooling said heated and devaporized medium by means of the cold devaporized expanded gas, combining the liquefied products and separating the same into the specific liquid end products desired by rectifying with heat supplied by the said circulating liquid medium and cooling the rectified product by means of said circulating liquid after the same has come from contact with the expanded cold gases, and circulating the liquid medium to absorb uncondensed vapors from the expanded cold gas and for the subscqucntopcrations hereinabove described.

. 8. Apparatus adapted for the recovery of liquefiable products from gases containing various liquefiable vapors consisting of a compressor for the gases, condensers '[or the compressed ases, means connected with said condensers $01 circulating a cold medium therethrough, separators connected with said condensers for removing the liquefied products, an expansion cylinder and a connection between it and the condensers, means for transmitting the cold temperature produced at the expansion cylinderto the circulating medium employed in the condensers, a rectificatlon column, means for conveying the separated liquid to said column, means for heating said column at one portion thereof and means for cooling the vapors at another portion thereof, and means for removing in liquid form the rectified product from said column and means for maintaining the desired grade of rectified product. 4

9. Apparatus adapted for the recovery of liquefiable products from gases containing various liquefiable vapors consisting of a compressor for the gases, condensers for the compressed gases, means connected with said condensers for circulating a cold medium therethrough, separators connected with said condensers for removing the liquefied products, an expansion cylinder and a connection between it and the condensers, means for transmitting the cold temperature produced at the expansion cylinder to the circulating medium employed in the condensers, a passage for the cooling medium communicating with the cold expanded gases and a passage for the said medium communicating between the last of the condensers through which it passes. and the cold expanded gases aforesaid at the point in the passage of the latter after the same have come from the first mentioned meeting with the said medium, a rectification column, means for conveying the separated liquid to said column, means for heating said column at one portion thereof and means for cooling the vapors at another portion thereof, and means for removing in liquid form the rectified product from said column and means =i-or maintaining the desired grade of rectified product.

1.0. An apparatus adapted for the recovery of' liquefiable products from gases containing various liquefiable vapors, said apparatus comprising in combination a compressor for the gases, a pipe for conducting the compressed gases from the compressor, a shell with whiclfsaid pipe communicates, horizontally arranged tubes in said shell to afford a passage for said gases, a partition also in the shell between said tubes to cause the gases'to flow in one direction through a part of said tubes and in the opposite di rection through the remaining part of said tubes, a numerously and minutely apertured member arranged in the path of said gases within that part of the shell where the direction of the gases changes, a chamber within said shell surrounding said tubes for circulating a cooling fluid, an outlet from said shell for the compressed gases and liquid contained therein, a separator and a connection between said outlet and said separator, an outlet upon said separator for withdrawing the uncondensed gases and a second outlet for withdrawing the condensed liquid, :1 rectifying column anda connection between the liquid outlet of the separator and said rectifying column.

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11. An apparatus adapted for the recovery of liquefiable products from gases containng various liquefiable vapors, said apparatus comprising in combination a compressor for the gases, a pipe for conducting the com pressed gases from the compressor, a shell with which said pipe communicates, transverse partitions in said shell forming between them a closed chamber, horizontally disposed tubes supported in and extending through said partitions, a horizontal partition extending between the tubes from one of the said vertical partitions and terminating short of the other of said vertical partitions, a further horizontal partition in the shell outside of said closed chamber in the path of the incoming gases to compel them to flow through a part of the tubes in one direction and through the remaining part of the tubes in the opposite direction, a numerously and minutely apeitured member in the path of the gases where their direc tion changes, an inlet into the closed chamber I for a cooling medium upon one side of the i5 partition therein and an outlet for the cooling medium at a corresponding point at the opposite side of said-1- closed chamber and horizontal par tion to compelsaid cooling medium to flow in directions opposite to that of the gases in the respective tubes wherein the gases flow in reverse directions, an'outlet for said shell for the compressed gases and liquid contained therein, a separator and a connection between said outlet and said separator, an outlet upon said separator for withdrawing the uncondensed gases and a secondoutletfor withdrawing the condensed liquid, a rectifying column. and a connection between the liquid outlet of the separator.

0 and said rectifying column.

12. The process of extracting and recovering gasoline vapors from gases whose liquefiable content consists in substantial i part of normally liquid hydrocarbons, which consists in compressing the gases,'fractionally condensing the vapors under pressure to separate out the lighter and the heavier constituents of said vapors independently and rectifying said constituents at such temperature and pressure as to produce gasoline,

without previously having removed a substantial part of said normally liquid hydr0- carbons from the material entering the process.

13. The process of extracting and recover ing gasoline vapors from gases whose liquefiable content consists in substantial part of normally liquid hydrocarbons, which consists in compressing the gases, fractionally condensing the vapors under pressure to separate out the lighter and the heavier constituents of said vapors independently, introducing said lighter and heavier constituents into a rectification column at appropriate points therein and rectifying them at such temperature and pressure as to produce gasoline, without previously having removed a substantial part of said normally liquid hydrocarbons from the material entering the process.

14. The process of extracting and recovering gasoline vapors from hydrocarbon gases whose liquefiable content consists in substantial part of normally liquid hydrocarbons, which consists in making a rough separation between certain lighter and heavier constituents thereof, which constitu' ents include substantially allot said normally liquid hydrocarbons, independently introducing said lighter and heavier constituents into a rectification column at appropriate points thereinand rectifying them to separate fixed gases therefrom and produce liquid gasoline.

15. The process of extracting and recovering gasoline vapors from hydrocarbon gases whose liquefiable content consists in substantial part of normally liquid hydrocarbons, which consists in subjecting the hydrocarbon gases to compression and fractional condensation to roughly separate between certain lighter and heavier constituents thereof, which constituents include substantially all of said normally liquid hydrocarbons, independently introducing said lighter and heavies constituents into a rectification column at appropriate points therein and rectitying them to separate fixed gases therefrom and produce liquid gasoline. j

16. The process of extracting and recovering gasoline from hydrocarbon gases whose liquefiable' content consists in substantial part of normally liquid hydrocarbons, which consists in compressing the gases, roughly separating out the liquefiable constituents under pressure to divide the lighter from the heavier of the liquefiable constituents and rectifying said constituents by introducing said constituents at appropriate intermediate points into a rectification coluinn while regulating the condition-s in the column to separate said constituents into fixed gases and gasoline, without previously having removed said normally liquid hydrocarbon content from the material entering the process.

17. The process of extracting and reco\-'ering gasoline from hydrocarbon gases, whose liquetiable content consists in substantial part of hydrocarbons which are individlullly stable under atmospheric conditions, comprising compressing the gases, condensing the liquefiable constituents while under pressure without preliminary removal, of. said stable hydrocarbons. separating the uncondensed gases from the resultant liquid and rectifying said liquid to eliminate the fixedgases.

18. The process of treating hydrocarbon gases whose liquefi'able content consists in substantial part of normally liquidliydrocarbons, which consists in' compressing the gases, condensing the liquefiable constituents While under pressure, separating the uncondensed gases from the resultant liquid and rectifying said liquid toproduce a residual liquid 'product containing substantially'all of said normally liquid hydrocarbon content.

19. The process of extracting and recovering gasoline from hydrocarbon gases containing the same which consists in compressingthe gases, condensing the liquefiable constituents while under pressure, separating the uncondeused gases from the resultant liquid and-fliereafter rectifying said liquid to eliminate the fixed gases.

Signed at New York, N. Y., this 2nd day of May, 192 in the presence of two Wit nesses.

EMIL SCHILL. FRANZ WoIDIoH. Now Dn. F. S. WOIDICH.

Witnesses M. HOHMEISTER, S. STERN.