US2582148A - Method of recovering desirable liquefiable hydrocarbons - Google Patents

Method of recovering desirable liquefiable hydrocarbons Download PDF

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US2582148A
US2582148A US748358A US74835847A US2582148A US 2582148 A US2582148 A US 2582148A US 748358 A US748358 A US 748358A US 74835847 A US74835847 A US 74835847A US 2582148 A US2582148 A US 2582148A
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pressure
formation
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stripped
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Jr Henry Meredith Nelly
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JF Pritchard and Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0645—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 3 carbon atoms or more

Definitions

  • Fracfiormfa- Separafor l rjecflon Well Producing Remover /3 Pressure Separafar 3nnentor Harry M. may J/: W 1 WM.
  • This invention relates to a method of recovering desirable liquefiable hydrocarbons from a fiow' of high pressure natural gas such as the flow from a highpressure well and particularly where the residue gas is to be used for pressuring producing formations.
  • the principal objects of the present invention are to provide a method for recovering desirable liquefiable hydrocarbons from high pressure natural gas, and to provide an inexpensive method for injecting the residue gas into a producing formation at the required pressure
  • the single figure is a diagrammatic view of my improved apparatus for removing desirable liquefiable hydrocarbons and raising the pressure of the residue gas to the desired injection pressure.
  • I designates a well drilled into a natural gas producing formation and wherethrough the formation liquid is discharged in a gaseous fiow containing desirable liquefiable hydrocarbon fractions, the flow being discharged from the well through a tubing 2 to which is connected a fiow pipe 3 leading from the well to the gas processing apparatus embodying the features of the present invention.
  • 4 designates a repressuring well having an intalge pipe 5 through which residue gas is returned to a producin formation which may be the formation into which the producing well is drilled or another formation which is to be repressured with the residue gas produced from the well I.
  • Gaseous hydrocarbons from the well I are directed through the pipe 3- at substantially full well head pressure and temperature which, by way of an example, may be 3100 p. s. i. g. and 180 F. to a precooler 6 wherein the flow of gas 2 is reduced to as low a temperature as possible without the formation of hydrates.
  • the temp-erature' may be reduced by the use of water to F. and the gas is delivered into a high pressure separator 7 which is connected with the precooler 6 by a pipe 8.
  • the gas constituent raises to the top of the separator and is discharged through a pipe II to a carbon dioxide and hydrogen sulfide removal unit l2, after which the-vapor is discharged through a pipe I3 to a dehydrator unit l4 wherein thedew point of the vapor is reduced, the vapor being discharged through a pipe 15.
  • the hydrogen sulfide and carbon dioxide removal unit I2 may be omitted and the vapors passed directly to the dehydrator.
  • the flow of vapors in the pipe Is is diverted for flow through pipes l6 and ll leading to heat exchangers l8 and I9 wherein the heat exchange mediums are the residue gas and the recovered liquefied hydrocarbons respectively, the purpose being to recover the refrigeration of the fluids before they are discharged for injection purposes and to the fractionating apparatus H].
  • the cooled vapor passing from the heat exchanger I8 is discharged at a low temperature of, for example, 15 F. through a pipe 20 to a refrigerating unit 2
  • the vapor is discharged from the refrigerating unit through a pipe 24 at a temperature, for example, -10 F.
  • the flow through the heat exchanger I9 is discharged through a pipe 25 at, for example, a 20 temperature, the pipe 25 being connected with the pipe 24 so that the respective flows are reunited and discharged through a pipe 26 into aseparator 21.
  • the vapor being discharged from the heat exchanger through a pipe 32 is throttled through a valve 33 to a pressure at which complete condensation of the vapor may be effected with a minimum extraction of latent heat.
  • the vapors may be expanded to a pressure slightly below the critical pressure of the mixture, thus setting the temperature of condensation slightly below the critical temperature where the latent heat is zero, the proximity of the operating temperature to the critical temperature depending upon the ability to control the condensing temperature and pressure,
  • the vapor upon being throttled through the valve 33 is further cooled due to the Joule-Thomson effect.
  • the expanded vapor at a temperature of -35 F. and at a pressure of 680 p. s. i. g. is discharged through a refrigerating unit 34 where the temperature is reduced to a temperature of 95 F. by contact with ethane, which ethane is delivered from a suitable refrigeration apparatus (not shown) through a pipe 35 and returned through a pipe 36.
  • ethane which ethane is delivered from a suitable refrigeration apparatus (not shown) through a pipe 35 and returned through a pipe 36.
  • the temperature is brought to a 95 F.
  • the major portion of the vapor is liquefied as a 4 result of the reduced temperature and lower pressure.
  • the liquid gravitates to the bottom of the surge drum and is discharged through a pipe 39 to the inlet of a pump M] which raises the pressure of the liquid to that necessary for return of the liquefied vapor to the formation to be repressured. Any vapor remaining is vented from the top of the surge drum through a pipe 4 I.
  • the liquid under the pressure necessary for return to the formation is discharged from the pump through a pipe 42 which leads through the heat exchanger [8.
  • a part of the flow is diverted for flow through the heat exchanger 3 I through a pipe 43 and flow from the heat exchanger is conducted through-a pipe 44 back to the pipe 42, the flow being diverted by a valve 45 that is inserted in the pipe 42 between the connections of the pipes 43 and 44 therewith,
  • the pressure is readily re-established by a simple pump apparatus while the residue gas is in liquid form and capable of being raised to the desired pressure with a minimum of power.
  • the method of obtaining desirable liquefiable petroleum hydrocarbons from a producing formation including flowing the gas under pressure from the formation to the surface of the ground, precooling the gas at substantially the pressure of the flow from said formation to effect stripping of the gas of the desirable liquefiable hydrocarbons, expanding the stripped gas to a substantially lower pressure, refrigerating the stripped gas to effect substantial condensation at the expanded pressure, pumping the liquefied stripped gas to the formation at a pressure higher than the pressure of said petroleum hydrocarbons in the formation, and passing the liquefied stripped gas in heat exchange relation with the gas fiow prior to extraction of the desirable liquefiable hydrocarbons for the precooling of the gas fiow.
  • the method of obtaining desirable liquefiable hydrocarbons from a producing formation including flowing the gas under pressure from the formation to the surface of the ground, p'recooling the gas at substantially the pressure of the fiow from said formation to effect stripping of the gas of the desirable ,liquefiable hydrocarbons, expanding the stripped gas to a substantially lower pressure, refrigerating the expanded gas to effect substantial liquefaction of said gas at the expanded pressure, pumping the liquefied stripped gas to the formation at a pressure above the pressure of the formation for returning the liquefied stripped gas to the formation, and passing the stripped liquefied gas in heat exchange relation with a part of gas flow prior to extraction of the desirable liquefiable hydrocarbons for said precooling of the gas flow, and passin the desirable liquefied hydrocarbons into heat exchange relation with the remainder of the gas flow.
  • the method of obtaining desirable liquefiable petroleum hydrocarbons from a producing formation including flowing the gas under pressure from the formation, cooling the gas at substantially the pressure of the flow from said formation to strip the gas by condensation of the desirable liquefiable hydrocarbons, removing the condensate from the stripped gas, expanding the stripped gasto a substantially lower pressure, refrigerating the stripped gas to effect liquefaction of the stripped gas and pumping the stripped liquefiedgas to the formation at a pressure higher than the pressure of said petroleum hydrocarbons in the formation.

Description

Jan. 8, 1952 H. M. NELLY, JR
METHOD OF RECOVERING DESIRABLE LIQUEFIABLE HYDROCARBONS Filed May 15, 1947 Ju/ye drum Pump
Fracfiormfa- Separafor l rjecflon Well Producing Remover /3 Pressure Separafar 3nnentor Harry M. may J/: W 1 WM.
attorney:
Patented jan. 8, 1952 METHOD OF RECOVEBING DESIRABLE LIQUEFIABLE HYDROCARBON S Henry Meredith Nelly, J r., Houston, Tex, assignor' to J. F. Pritchard & 00., Kansas City, Mo., a
corporation of Missouri I Application May 15, 1947, semi No.- 748,358
3 Claims. (01. 1cc21) This invention relates to a method of recovering desirable liquefiable hydrocarbons from a fiow' of high pressure natural gas such as the flow from a highpressure well and particularly where the residue gas is to be used for pressuring producing formations.
It is well known that high pressure natural gas contains profitable quantities of desirable liquefiable hydrocarbons but such hydrocarbons, for practical purposes, must be recovered at substantially lower pressure than the pressure of the formation in which the residue gas is to be used. Consequently, the pressure of the residue gas must be raised to a pressure above the pressure of the formation in which it is to be used.
Heretofore this has required expensive compressor equipment and much horsepower to raise the pressure of the residue gas to the required injection pressure. Consequently, recovery of such hydrocarbons may not be profitable where it is necessary and desirable to use the residue gas for pressurin high pressure formations.
Therefore, the principal objects of the present invention are to provide a method for recovering desirable liquefiable hydrocarbons from high pressure natural gas, and to provide an inexpensive method for injecting the residue gas into a producing formation at the required pressure In accomplishing these and other objects of the invention hereinafter pointed out, I have provided improved structure and method of operation illustrated in the accompanying drawing wherein:
The single figure is a diagrammatic view of my improved apparatus for removing desirable liquefiable hydrocarbons and raising the pressure of the residue gas to the desired injection pressure.
Referring more in detail to the drawings:
I designates a well drilled into a natural gas producing formation and wherethrough the formation liquid is discharged in a gaseous fiow containing desirable liquefiable hydrocarbon fractions, the flow being discharged from the well through a tubing 2 to which is connected a fiow pipe 3 leading from the well to the gas processing apparatus embodying the features of the present invention. 4 designates a repressuring well having an intalge pipe 5 through which residue gas is returned to a producin formation which may be the formation into which the producing well is drilled or another formation which is to be repressured with the residue gas produced from the well I.
Gaseous hydrocarbons from the well I are directed through the pipe 3- at substantially full well head pressure and temperature which, by way of an example, may be 3100 p. s. i. g. and 180 F. to a precooler 6 wherein the flow of gas 2 is reduced to as low a temperature as possible without the formation of hydrates. By way of illustration, the temp-erature'may be reduced by the use of water to F. and the gas is delivered into a high pressure separator 7 which is connected with the precooler 6 by a pipe 8. Upon being dischargedto the high pressure separator, any liquids contained in the gas flow or resulting incidental to reduction in temperature, mainly heavy distillate material, settle to the bottom of the separator and are discharged through a pipe 9 leading to a fractionating apparatus which is indicated at Ill. The gas constituent raises to the top of the separator and is discharged through a pipe II to a carbon dioxide and hydrogen sulfide removal unit l2, after which the-vapor is discharged through a pipe I3 to a dehydrator unit l4 wherein thedew point of the vapor is reduced, the vapor being discharged through a pipe 15.
If hydrogen sulfide and carbon dioxide are not present in the gas or if the composition of the vapor is such that its boiling point is higher than the solidification point of carbon dioxide and hydrogen sulfide, the hydrogen sulfide and carbon dioxide removal unit I2 may be omitted and the vapors passed directly to the dehydrator.
The flow of vapors in the pipe Isis diverted for flow through pipes l6 and ll leading to heat exchangers l8 and I9 wherein the heat exchange mediums are the residue gas and the recovered liquefied hydrocarbons respectively, the purpose being to recover the refrigeration of the fluids before they are discharged for injection purposes and to the fractionating apparatus H]. The cooled vapor passing from the heat exchanger I8 is discharged at a low temperature of, for example, 15 F. through a pipe 20 to a refrigerating unit 2| where the temperature of the vapor is reduced by contact with a refrigerating medium such as ethane admitted through the refrigeration unit through a pipe 22 and discharged through a pipe 23, which pipes are connected with suitable refrigerating machinery (not shown). The vapor is discharged from the refrigerating unit through a pipe 24 at a temperature, for example, -10 F. The flow through the heat exchanger I9 is discharged through a pipe 25 at, for example, a 20 temperature, the pipe 25 being connected with the pipe 24 so that the respective flows are reunited and discharged through a pipe 26 into aseparator 21.
Since the vapor has been cooled to the point for the recovery of the natural gasoline, butane and propane constituents, such constituents gravitate as liquids tothe bottom of the separator 21 and are discharged through a pipe 28 for flow through the heat exchanger l9 and discharged through a pipe 29 that is connected with the pipe 9 so that the desirable liquefied hydrocarbons resulting in'the separator 2? are conducted along with those from the separator 7 to the fractionating apparatus ill for the production of the desired materials such as distillate, natural gasoline, butane and propane. The vapor from the separator 21 is discharged through a pipe 33 that is connected with a heat exchanger 3i wherein the vapor is reduced to a lower temperature, for example, 45 F. through extraction of the refrigeration from the repressure fluid. The vapor being discharged from the heat exchanger through a pipe 32 is throttled through a valve 33 to a pressure at which complete condensation of the vapor may be effected with a minimum extraction of latent heat. For example, the vapors may be expanded to a pressure slightly below the critical pressure of the mixture, thus setting the temperature of condensation slightly below the critical temperature where the latent heat is zero, the proximity of the operating temperature to the critical temperature depending upon the ability to control the condensing temperature and pressure,
The vapor upon being throttled through the valve 33 is further cooled due to the Joule-Thomson effect. The expanded vapor at a temperature of -35 F. and at a pressure of 680 p. s. i. g. is discharged through a refrigerating unit 34 where the temperature is reduced to a temperature of 95 F. by contact with ethane, which ethane is delivered from a suitable refrigeration apparatus (not shown) through a pipe 35 and returned through a pipe 36. In the refrigerating unit the temperature is brought to a 95 F.
temperature and the flow is discharged at a pressure of substantially 670p. s. i. g. through a pipe 31 that is connected with a surge drum 38.
The major portion of the vapor is liquefied as a 4 result of the reduced temperature and lower pressure. The liquid gravitates to the bottom of the surge drum and is discharged through a pipe 39 to the inlet of a pump M] which raises the pressure of the liquid to that necessary for return of the liquefied vapor to the formation to be repressured. Any vapor remaining is vented from the top of the surge drum through a pipe 4 I.
The liquid under the pressure necessary for return to the formation, is discharged from the pump through a pipe 42 which leads through the heat exchanger [8. A part of the flow is diverted for flow through the heat exchanger 3 I through a pipe 43 and flow from the heat exchanger is conducted through-a pipe 44 back to the pipe 42, the flow being diverted by a valve 45 that is inserted in the pipe 42 between the connections of the pipes 43 and 44 therewith,
By lique'fying the residue gas and raising the pressure of the liquefied gas to the pressure necessary for repressure injection; for example, in the illustrated instance to 3800 p. s. i. g., I am enabled to treat a high pressured gas flow to recover the desirable liquefiable constituents and economically return the residue gas for injection purposes since expensive compressors and power necessary to raise the liquid gas to the required pressure are not required.'
With the present invention the pressure is readily re-established by a simple pump apparatus while the residue gas is in liquid form and capable of being raised to the desired pressure with a minimum of power.
It is to be understood that the pressures and temperatures are given for examples and that the temperatures and pressure may be varied to meet the conditions under which the apparatus may be operated to obtain the desired results.
What I claim and desire to secure by Letters Patent is:
1. The method of obtaining desirable liquefiable petroleum hydrocarbons from a producing formation including flowing the gas under pressure from the formation to the surface of the ground, precooling the gas at substantially the pressure of the flow from said formation to effect stripping of the gas of the desirable liquefiable hydrocarbons, expanding the stripped gas to a substantially lower pressure, refrigerating the stripped gas to effect substantial condensation at the expanded pressure, pumping the liquefied stripped gas to the formation at a pressure higher than the pressure of said petroleum hydrocarbons in the formation, and passing the liquefied stripped gas in heat exchange relation with the gas fiow prior to extraction of the desirable liquefiable hydrocarbons for the precooling of the gas fiow.
2. The method of obtaining desirable liquefiable hydrocarbons from a producing formation including flowing the gas under pressure from the formation to the surface of the ground, p'recooling the gas at substantially the pressure of the fiow from said formation to effect stripping of the gas of the desirable ,liquefiable hydrocarbons, expanding the stripped gas to a substantially lower pressure, refrigerating the expanded gas to effect substantial liquefaction of said gas at the expanded pressure, pumping the liquefied stripped gas to the formation at a pressure above the pressure of the formation for returning the liquefied stripped gas to the formation, and passing the stripped liquefied gas in heat exchange relation with a part of gas flow prior to extraction of the desirable liquefiable hydrocarbons for said precooling of the gas flow, and passin the desirable liquefied hydrocarbons into heat exchange relation with the remainder of the gas flow.
3. The method of obtaining desirable liquefiable petroleum hydrocarbons from a producing formation including flowing the gas under pressure from the formation, cooling the gas at substantially the pressure of the flow from said formation to strip the gas by condensation of the desirable liquefiable hydrocarbons, removing the condensate from the stripped gas, expanding the stripped gasto a substantially lower pressure, refrigerating the stripped gas to effect liquefaction of the stripped gas and pumping the stripped liquefiedgas to the formation at a pressure higher than the pressure of said petroleum hydrocarbons in the formation.
HENRY MEREDITH NELLY, JR.
REFERENCES CITED The following references are of record in the file of this patent:
UNITED STATES PATENTS Number Name Date 2,258,015 Keith et a1. Oct. 7, 1941 2,297,832 Hudson Oct. 6, I942 2,361,012 Cole et a1. Oct. 24, 1944 2,374,104 Kirkbride Apr. 17, 1945

Claims (1)

  1. 3. THE METHOD OF OBTAINING DESIRABLE LIQUEFIABLE PETROLEUM HYDROCARBON FROM A PRODUCING FORMATION INCLUDING FLOWING THE GAS UNDER PRESSURE FROM THE FORMATION, COOLING THE GASE AT SUBSTANTIALLY THE PRESSURE OF THE FLOW FROM SAID FORMATION TO STRIP THE GAS BY CONDENSATION OF THE DESIRABLE LIQUEFLABLE HYDROCARBONS, REMOVING THE CONDENSATE FROM THE STRIPPED GAS, EXPANDING THE STRIPPED GAS TO A SUBSTANTIALLY LOWER PRESSURE, REFRIGERATING THE STRIPPED GAS TO EFFECT LIQUEFACTION OF THE STRIPPED GAS AND PUMPING THE STRIPPED LIQUEFIED GAS TO THE FORMATION AT A PRESSURE HIGHER
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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2718262A (en) * 1952-01-29 1955-09-20 Exxon Research Engineering Co Secondary oil recovery by selfpropelled solvent extraction
US2720265A (en) * 1954-03-31 1955-10-11 Gulf Research Development Co Adjusting the retrograde condensation pressure of hydrocarbon compositions
US2832416A (en) * 1955-07-26 1958-04-29 Texas Co Oil well treatment
US2842941A (en) * 1956-03-29 1958-07-15 J F Pritchard & Company Method for purification of carbon dioxide
US2875830A (en) * 1954-02-04 1959-03-03 Oil Recovery Corp Method of recovery of oil by injection of hydrocarbon solution of carbon dioxide into oil structure
US2951347A (en) * 1956-04-04 1960-09-06 Black Sivalls & Bryson Inc Method of processing gas
US3110155A (en) * 1960-04-11 1963-11-12 British Oxygen Co Ltd Improved process for the separation of air to produce a desired separation product in the gaseous phase under pressure
US3116136A (en) * 1960-11-01 1963-12-31 American Mach & Foundry Gas drying and separation
US3162519A (en) * 1958-06-30 1964-12-22 Conch Int Methane Ltd Liquefaction of natural gas
US3195316A (en) * 1963-08-02 1965-07-20 Chicago & Bridge & Iron Compan Methane liquefaction system
US3224211A (en) * 1961-11-20 1965-12-21 Phillips Petroleum Co Processing low b.t.u. gas from natural gas
US3242681A (en) * 1963-01-31 1966-03-29 Philips Corp Natural gas liquefaction and storage
US3254496A (en) * 1962-04-05 1966-06-07 Transp Et De La Valorisation D Natural gas liquefaction process
US3256933A (en) * 1950-07-13 1966-06-21 Exxon Production Research Co Methods of recovery of oil
US3282060A (en) * 1965-11-09 1966-11-01 Phillips Petroleum Co Separation of natural gases
US3360945A (en) * 1965-02-25 1968-01-02 Lummus Co Repressurized natural gas addition to main gas stream to maintain well head pressure
US3846993A (en) * 1971-02-01 1974-11-12 Phillips Petroleum Co Cryogenic extraction process for natural gas liquids
US4147525A (en) * 1976-06-08 1979-04-03 Bradley Robert A Process for liquefaction of natural gas
US4195979A (en) * 1978-05-12 1980-04-01 Phillips Petroleum Company Liquefaction of high pressure gas
US4310049A (en) * 1979-04-17 1982-01-12 California Institute Of Technology Crude oil desulfurization
US4664190A (en) * 1985-12-18 1987-05-12 Shell Western E&P Inc. Process for recovering natural gas liquids
US5520249A (en) * 1993-12-23 1996-05-28 Institut Francais Du Petrole Process for the pretreatment of a natural gas containing hydrogen sulphide

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2258015A (en) * 1939-05-23 1941-10-07 Kellogg M W Co Separating hydrocarbon fluids
US2297832A (en) * 1940-11-05 1942-10-06 Cities Service Oil Co Extraction and treatment of volatile liquid hydrocarbons
US2361012A (en) * 1942-09-12 1944-10-24 Texas Co Method of storing oils
US2374104A (en) * 1940-07-05 1945-04-17 Pan American Refining Corp Recovery of liquid hydrocarbons from high pressure wells

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2258015A (en) * 1939-05-23 1941-10-07 Kellogg M W Co Separating hydrocarbon fluids
US2374104A (en) * 1940-07-05 1945-04-17 Pan American Refining Corp Recovery of liquid hydrocarbons from high pressure wells
US2297832A (en) * 1940-11-05 1942-10-06 Cities Service Oil Co Extraction and treatment of volatile liquid hydrocarbons
US2361012A (en) * 1942-09-12 1944-10-24 Texas Co Method of storing oils

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3256933A (en) * 1950-07-13 1966-06-21 Exxon Production Research Co Methods of recovery of oil
US2718262A (en) * 1952-01-29 1955-09-20 Exxon Research Engineering Co Secondary oil recovery by selfpropelled solvent extraction
US2875830A (en) * 1954-02-04 1959-03-03 Oil Recovery Corp Method of recovery of oil by injection of hydrocarbon solution of carbon dioxide into oil structure
US2720265A (en) * 1954-03-31 1955-10-11 Gulf Research Development Co Adjusting the retrograde condensation pressure of hydrocarbon compositions
US2832416A (en) * 1955-07-26 1958-04-29 Texas Co Oil well treatment
US2842941A (en) * 1956-03-29 1958-07-15 J F Pritchard & Company Method for purification of carbon dioxide
US2951347A (en) * 1956-04-04 1960-09-06 Black Sivalls & Bryson Inc Method of processing gas
US3162519A (en) * 1958-06-30 1964-12-22 Conch Int Methane Ltd Liquefaction of natural gas
US3110155A (en) * 1960-04-11 1963-11-12 British Oxygen Co Ltd Improved process for the separation of air to produce a desired separation product in the gaseous phase under pressure
US3116136A (en) * 1960-11-01 1963-12-31 American Mach & Foundry Gas drying and separation
US3224211A (en) * 1961-11-20 1965-12-21 Phillips Petroleum Co Processing low b.t.u. gas from natural gas
US3254496A (en) * 1962-04-05 1966-06-07 Transp Et De La Valorisation D Natural gas liquefaction process
US3242681A (en) * 1963-01-31 1966-03-29 Philips Corp Natural gas liquefaction and storage
US3195316A (en) * 1963-08-02 1965-07-20 Chicago & Bridge & Iron Compan Methane liquefaction system
US3360945A (en) * 1965-02-25 1968-01-02 Lummus Co Repressurized natural gas addition to main gas stream to maintain well head pressure
US3282060A (en) * 1965-11-09 1966-11-01 Phillips Petroleum Co Separation of natural gases
US3846993A (en) * 1971-02-01 1974-11-12 Phillips Petroleum Co Cryogenic extraction process for natural gas liquids
US4147525A (en) * 1976-06-08 1979-04-03 Bradley Robert A Process for liquefaction of natural gas
US4195979A (en) * 1978-05-12 1980-04-01 Phillips Petroleum Company Liquefaction of high pressure gas
US4310049A (en) * 1979-04-17 1982-01-12 California Institute Of Technology Crude oil desulfurization
US4664190A (en) * 1985-12-18 1987-05-12 Shell Western E&P Inc. Process for recovering natural gas liquids
US5520249A (en) * 1993-12-23 1996-05-28 Institut Francais Du Petrole Process for the pretreatment of a natural gas containing hydrogen sulphide

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