US3458973A - Method and apparatus for component concentration in the vapor phase - Google Patents

Method and apparatus for component concentration in the vapor phase Download PDF

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US3458973A
US3458973A US600498A US3458973DA US3458973A US 3458973 A US3458973 A US 3458973A US 600498 A US600498 A US 600498A US 3458973D A US3458973D A US 3458973DA US 3458973 A US3458973 A US 3458973A
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gas
conduits
conduit
adsorber
ethane
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John R Spencer
Walton D Greathouse
James H Cheek
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ConocoPhillips Co
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Continental Oil Co
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40003—Methods relating to valve switching
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/403—Further details for adsorption processes and devices using three beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases

Definitions

  • a cyclical method and apparatus for separating intermediate molecular weight hydrocarbon gases (ethane and ethylene) from primarily methane gas are disclosed.
  • the feed stream of methane, ethane and ethylene gas is flowed through a sorbent bed where ethane and ethylene are adsorbed to a point of saturation.
  • the saturated bed is then desorbed of ethane and ethylene by heating it in a closed heating circuit.
  • This invention relates to the separation of intermediate molecular Weight hydrocarbons from a gas stream. More specifically, this invention is concerned with the recovery of ethane from natural gas streams and with the recovery of ethane and ethylene from refinery gas streams.
  • Another object of this invention is to present a method and apparatus for recovering intermediate molecular weight hydrocarbons which require a minimum of refrigeration equipment.
  • Another object of this invention is to present method and apparatus for recovering ethane and ethylene from hydrocarbon gas streams by adsorption at or near atmospheric temperatures.
  • Another object of this invention is to present method and apparatus for separating ethane and ethylene from hydrocarbon gas streams which are etficient and economical.
  • FIGURE 1 presents schematically one embodiment of applying our in- Patented Aug. 5, 1969 ventive method and apparatus.
  • FIGURE 2 presents schematically a second embodiment.
  • our invention provides a cyclical method and apparatus for recovering intermediate molecular weight gases, such as ethane and ethylene, from a gas stream by adsorbing intermediate molecular Weight gases cyclically in one of a plurality of beds of solid sorbent; another spent bed of solid sorbent (saturated with ethane and/or ethylene) is regenerated by circulating through it a heated regeneration gas in a closed heating or regenerating circuit. As this sorbent bed is heated, the ethane and ethylene are desorbed from the sorbent and become part of the circulating regenerating gas, thereby causing the pressure in the closed regeneration circuit to increase.
  • intermediate molecular weight gases such as ethane and ethylene
  • This gas stream removed is a mixture rich in ethane and ethylene and is a desired product of our method and apparatus.
  • the raw gas treated must consist primarily of ethane, ethylene, methane, and other inerts, with only traces of higher molecular weight hydrocarbons such as propane, butane, etc.
  • Sources of such streams are natural gas from subterranean hydrocarbon reservoirs and petroleum refiney processing steams.
  • Raw gas such as natural gas, containing an intermediate molecular weight hydrocarbon (ethane) to be recovered, flows into the system by way of conduit 1 to one of the adsorbers 16, 17, and 18.
  • the adsorbers are filled with a sorbent material, for example, activated carbon, capable of removing the intermediate molecular weight hydrocarbons from the raw gas stream.
  • a sorbent material for example, activated carbon
  • the raw gas, in flowing through adsorber 16 is stripped of ethane.
  • the residual gas flows from adsorber 16 by way of conduit 22 and is removed from the system.
  • conduits 23 and 24 will serve similarly to remove gas from adsorbers 17 and 18, respectively.
  • the adsorption step of the method comprises flowing a raw gas through a sorbent body, thereby removing all or part of the intermediate molecular weight gas, for example ethane, in the gas and flowing the stripped residue gas from the sorbent body.
  • adsorber 18 When the sorbent material in an adsorber becomes spent or saturated with ethane, it must be regenerated by passing through it a heated gas to desorb the adsorbed ethane.
  • adsorber 18 is in the process of being heated and regenerated.
  • a heated gas obtained prior to beginning the heating step, from the residue gas stream flowing from another adsorber in the adsorption step of the method, flows by way of conduits 11, 7, 14, and 4 to adsorber 18.
  • Conduits 11, 5, 12, and 2, and 11, 6, 13, and 3 serve a similar purpose when adsorbers '16 and 17 are regenerated.
  • the heated gas flowing through adsorber 18 heats the sorbent material therein and causes the adsorber ethane to be desorbed.
  • the gas stream flows from adsorber 18 by way of conduits 24, 34, and 27 into conduits leading to the gas heater.
  • Conduits 22, 32, and 25, and 23, 33, and 26 serve a similar purpose when adsorbers 16 and 17 are being heated.
  • the pressure within adsorber 18, heater 19, the interconnecting conduits and other equipment increases substantially.
  • gas in the regeneration circuit is bled off through conduit 36 and valve V19 sufficiently to maintain pressure in adsorber 18 and heater 19 at the predetermined level.
  • the gas thus removed is a concentration of ethane and is a desired product of the method.
  • the regeneration step of the method comprises circulating a heater regeneration fluid through a spent sorbent bed in a closed circuit and removing gas enriched in ethane from the circuit to maintain a predetermined pressure in the circuit.
  • the cooling step of the method comprises diverting a portion of the residue gas stream from the adsorbing step, cooling the diverted stream, and passing it through the bed to be cooled.
  • the heated bed and associated conduits are filled with a gas rich in ethane. It is desirable to retain this gas within the system.
  • another spent sorbent bed must be placed in the regeneration step. To increase the efficiency of our method, therefore, the gas in the hot adsorber is displaced into the cold adsorber that is about to be regenerated by heating. A portion of residue gas from the adsorber in the sorption circuit is diverted and flowed into the hot regenerated bed and the conduits associated therewith. Simultaneously, gas in the cold spent adsorber is displaced back into the residue gas stream.
  • adsorber 17 would be switched into the adsorption step and a portion of the efliuent residue gas from adsorber 17 flowing in conduit 44 would be diverted through conduits 46, 47, 15, 10, 14, and 4 through the hot regenerated bed 18. Since there is direct communication between adsorber 18 and adsorber 16 by way of conduits 24, 34, 27, 31, 35, 45, 43, 40, heater 19, conduits 11, 5, 12, and 2, a certain volume of gas will be displaced from adsorber 16 through conduit 22. This displaced gas is a lean, stripped gas and is discarded in the residue gas line 44.
  • the apparatus comprises a minimum of three circuits, a sorption circuit, a cooling circuit, and a heating or regenerating circuit.
  • the sorption circuit comprises a raw gas inlet manifold coupled with the three sorbent beds which in turn are coupled with an exit residue gas manifold.
  • conduit 1 and conduits 2, 3, and 4 in conjunction with valve V1, V2, and V3, respectively, make up the inlet gas manifold and control the flow of raw gas into the adsorbers 16, 17, and 18.
  • conduits 22, 23, and 24 intersecting with conduit 44 and interrupted by valves V16, V17, and V18, respectively, comprise the residue gas outlet manifold and control the flow of gas from the adsorbers 16, 17, and 18 when each of these is in the sorption circuit.
  • valves V1 and V16 would be open and valves V2, V3, V4, V7, V10, and V13 would be closed so that raw gas may fiow through conduits 1 and 2, adsorber 16, conduits 22 and 44.
  • the heating or regenerating circuit comprises inlet and outlet manifolds coupled with the three sorbent beds, a compressor, optionally a heat exchanger, and a gas heater.
  • conduit 11 and conduit 5, 6, and 7 interrupted by valves V4, V5, and V6 comprise the inlet heating gas manifold, which connects with the gas heater 19 and by conduits 12 and 2, 13 and 3, and 14 and 4, with adsorbers 16, 17, and 18, respectively.
  • Conduits 25, 26, and 27, interrupted by valves V10, V11, and V12, and conduits 31 and 35 make up the exit heating gas manifold.
  • the manifold is connected to the adsorbers 16, 17, and 18 by conduits 32 and 22, 33 and 23, and 34 and 24, respectively, and communicates through conduit 45, compressor 42, conduit 43, heat exchanger 41, and conduit 40 with gas heater 19.
  • valves V6 and V12 will be open and valves V3, V4, V5, V9, V10, V11, V15, and V18 will be closed.
  • Heating gas can then circulate from the gas heater 19 through conduits 11, 7, 14, 4, adsorber 18, conduits 24, 34, 27, 31, 35, 45, compressor 42, conduit 43, heat exchanger 41, conduit 40, and back to gas heater 19.
  • Conduit 36 and valve V19 are also connected into the heating circuit.
  • pressure in the heating circuit will increase. Whne the pressure reaches a predetermined value, gas is bled off through valve V19 and conduit 36 to maintain the predetermined pressure value.
  • the gas removed is enriched in ethane when processing a natural gas stream and is one of the desired products of the apparatus.
  • Valve V19 can be made automatically responsive to the pressure in the heating circuit, opening and closing to maintain the desired pressure.
  • the cooling circuit comprises inlet and outlet cooling gas manifolds coupled with the three sorbent beds, a compressor or blower (if desired), and gas cooler.
  • conduit 15 and conduits 8, 9, and 10 interrupted by valves V7, V8, and V9 make up the cooling gas inlet manifold which connects with cooler 20 and through conduits 12 and 2, 13 and 3, and 14 and 4 with adsorbers 16, 17, and 18, respectively.
  • Conduits 28, 29, and 30 interrupted by valves V13, V14, and V15 and conduit 38 make up the cooling gas outlet manifold which is connected by conduits 32 and 22, 33 and 23, 34 and 24 with adsorbers 16, 17, and 18, respectively, and communicates through heat exchanger 41 and conduit 39 with the residue gas conduit 44.
  • valves V8 and V14 will be open and valves V2, V5, V7, V9, V11, V13, V15, and V17 will be closed. Gas will then fiow from the residue gas line 44 through conduit 46, the blower 21, conduit 47, gas cooler 20, conduits 15, 9, 13, and 3, adsorber '17, conduits 23, 33, 29, and 38, heat exchanger 41, conduit 39, and back to the residue gas line 44.
  • the efiluent gas from the adsorber about to be regenerated can be returned to the residue gas line by Opening the valve in the residue gas outlet manifold from the bed and closing the valve in the cooling gas outlet manifold.
  • valve V16 would be opened and valve V13 would remain closed. This flow path will bypass the heat exchanger 41 and may be advantageous in some cases.
  • each of the sorbent beds has transferred through each circuit and is ready to resume 1ts first function.
  • the switching of each bed from one circuit to another can be controlled by a time cycle mechanism or by temperature sensing mechanisms.
  • the temperature sensing mechanisms are preferred. For example it may be desirable to place a temperature sensing element in the conduits leading from the heating circuit so that when the temperature of a bed in the heating circuit reaches a predetermined value, as indicated by the temperature of heating gas flowing from that bed, a new cycle can be started.
  • Activated carbon is preferred for the sorbent material used in the sorbent beds.
  • valve V20 remains closed and valve V21 open.
  • the step of cooling is conducted by recycling the cooling gas through the bed being cooled in a semi-closed cooling circuit.
  • Conduits 49 and 50 are connected to the cooling circuit to permit additional gas to enter the cooling circuit from the residue gas line as cooling progresses and the gas volume in the cooling circuit shrinks.
  • cooling gas will flow from the compressor 21 through conduits 15, 9, 13, and 3, adsorber 17, conduits 23, 33, 29, and 38, heat exchanger 41, conduit 51, gas cooler 20, conduit 52, valve V21, conduit 53, and back to the blower 21.
  • Conduits 49 and 50 connect the cooling circuit to the residue gas line, and gas flows through these conduits in quantity sutficient to compensate for shrinkage of gas volume in the cooling circuit.
  • This gas may contain traces of heavier hydrocarbons which, if displaced into the cold adsorber about to be regenerated, would tend to accumulate within the system. These heavier hydrocarbons are the last to be desorbed in regenerating the spent sorbent and are the last to be displaced from the sorbent as the purge step proceeds.
  • This secondary purge step is accomplished by opening valve V20 and closing valve V21 and venting the effluent gas from the bed being purged from the system.
  • the flow path of gas will be from conduit 44 through conduit 50 and blower 21, conduit 15, valve V9, conduits 10, 1-4, 4, adsorber 18, conduits 24, 34, 27, valve V12, conduits 31, 35, 45, blower 42, conduits 43, 48, and valve V20.
  • This gas removed can be treated to remove the heavy hydrocarbons if desirable.
  • This secondary purge step is optional and in many cases may not be necessary.
  • a valve program showing the valve positions for the embodiment of FIGURE 2, including the secondary or subpurge step, is presented in Table H.
  • Feed gas in conduit 1 is at about 100 F. and 820 p.s.i.g. in an amount of about 20 MM c.f./day (measured at 60 F. and 14.65 p.s.i.a.)
  • Adsorber vessels 16, 17, and 18 each have a volume, empty, of 592 ft. and operate at a pressure of about 810-830 p.s.i.a.
  • Each adsorber contain about 16,200 lbs. of activated carbon (8-10 mesh).
  • Temperature of the sorbent material is about 110 F. during adsorption, a maximum of about 450 F.
  • Residue gas in an amount of about 18,800 M c.f./day at about 115-125 F. and 800 p.s.i.a. is produced by way of conduit 44.
  • Reactivation gas is circulated in conduit 11 in an amount of about 13,500 M c.f./day at about 450 F. and 812 p.s.i.a.
  • Reactivation gas in conduit 45 is maintained at a predetermined pressure of about 806 p.s.i.a. by bleeding off gas through valve V19 in an amount of about 1,200 M c.f./day.
  • Gas in conuduit 15 has a temperature of about 120 F.
  • conduit 39 has a temperature of about 175 F. and flows through conduit 15 (FIGURE 1) or conduit 49 (FIGURE 2) in an amount of about 20,000 M c.f./day.
  • Heater 19 is designed for a duty of 6,600,000 B.t.u./hr. and 1,000 p.s.i.g.
  • compositions in mole percentages at various points throughout the system are tabulated below:
  • Apparatus for removing sorbable components from a hydrocarbon gas stream comprising:
  • a gas releasing means communicating between a second point of utility and a circuit consisting of said heater (b), at least one of conduits (g), at least one of vessels (a), at least one of conduits (h), gas circulating means (d), and conduit (i);
  • Apparatus for removing sorbable components from a hydrocarbon gas stream comprising:
  • a method of separating ethane and ethylene gas from a gas stream comprising ethane, ethylene, and methane, and containing only traces of higher molecular weight hydrocarbons comprising:
  • step (d) returning the remaining poriton of said heated gas to contacting said solid sorbent body in step (b);
  • step (f) contacting said sorbent body with a cool gas, thereby cooling said sorbent body to a temperature suflicient to repeat step (a).
  • step (c) 14. The method as set forth in claim 12 wherein said portion of heated gas removed from said closed circuit in step (c) is removed at a rate suificient to maintain a predetermined pressure in said closed circuit.
  • step (b) is flowed in heat exchange relationship with the cool gas of step (e).

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  • Oil, Petroleum & Natural Gas (AREA)
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US600498A 1966-12-09 1966-12-09 Method and apparatus for component concentration in the vapor phase Expired - Lifetime US3458973A (en)

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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3713272A (en) * 1971-08-26 1973-01-30 Continental Oil Co Process for recovering condensible components from a gas stream
US3800507A (en) * 1970-06-23 1974-04-02 Us Navy Low pressure air dehydrator
US4436534A (en) 1982-11-08 1984-03-13 Seguy Bernard R Method for reducing desorbent consumption in recovery systems
US4819477A (en) * 1986-02-27 1989-04-11 Mds Health Group Limited Method and apparatus for trace sample collection
US5518527A (en) * 1993-08-26 1996-05-21 Mitsubishi Petrochemical Engineering Co., Ltd. Method for recovering ethylene from vent gas from ethylene oxide plant vent gas
US7799117B1 (en) * 2006-09-27 2010-09-21 Uop Llc Gas treatment process by temperature swing adsorption
US8002877B1 (en) * 2006-12-07 2011-08-23 Lawrence Sadler Method of trapping ethylene
US8535426B2 (en) 2006-12-07 2013-09-17 Lawrence R. Sadler Apparatus, system, and method for removing ethylene from a gaseous environment
WO2015021047A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method for extracting natural gas liquids from natural gas using an adsorbent media comprising a partially pyrolized macroporous polymer
WO2015021046A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method comprising a microwave heating system for regenerating adsorbent media used for extracting natural gas liquids from natural gas
WO2015021049A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method for extracting natural gas liquids from natural gas using an adsorbent media comprising a cross-linked macroporous polymer
WO2015108569A1 (en) 2014-01-17 2015-07-23 Dow Global Technologies Llc Methane-rich natural gas supply for stationary combustion systems
WO2015112199A1 (en) 2014-01-21 2015-07-30 Dow Global Technologies Llc Process for recovering natural gas liquids from natural gas produced in remote locations
WO2015130339A1 (en) 2014-02-25 2015-09-03 Dow Global Technologies Llc Process control method for extracting natural gas liquids from natural gas
WO2015130338A1 (en) 2014-02-27 2015-09-03 Dow Global Technologies Llc Method for regenerating adsorbent media used for extracting natural gas liquids from natural gas
WO2016003484A3 (en) * 2013-11-20 2016-03-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude A rapid temperature swing adsorption (rtsa) method using structured adsorbent for co2 capture from low pressure and low co2 concentration sources
WO2016137925A1 (en) 2015-02-27 2016-09-01 Dow Global Technologies Llc Method to selectively remove hydrogen sulfide from a gas stream using a functionalized cross-linked macroporous polymer
US9908079B2 (en) 2015-01-27 2018-03-06 Dow Global Technologies Llc Separation of hydrocarbons using regenerable macroporous alkylene-bridged adsorbent
WO2018067298A1 (en) 2016-10-06 2018-04-12 Dow Global Technologies Llc Selective removal of hydrogen sulfide from a gas stream using a quarternary ammonium amine functionalized cross-linked macroporous polymer
WO2018085076A1 (en) 2016-11-04 2018-05-11 Dow Global Technologies Llc Psa produced hydrocarbon gas supply for power generation
WO2019032283A1 (en) 2017-08-11 2019-02-14 Dow Global Technologies Llc METHOD FOR REMOVING SOFTENED COMPOUNDS FROM A GASEOUS FLOW
US10661219B2 (en) 2015-01-27 2020-05-26 DDP Specialty Electronic Materials US, Inc. Separation of nitrogen from hydrocarbon gas using pyrolyzed sulfonated macroporous ion exchange resin

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US3266221A (en) * 1964-06-02 1966-08-16 Union Carbide Corp Ethylene recovery from gas mixtures
US3311189A (en) * 1960-10-28 1967-03-28 Walker Mfg Co Ceramic coated muffler with drainage openings
US3324669A (en) * 1964-06-08 1967-06-13 Pittsburgh Activated Carbon Co Lean oil contact with the regenerative medium for adsorbers

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US3186144A (en) * 1959-09-04 1965-06-01 Nat Tank Co Processes and apparatus for recovering hydrocarbons from gas streams
US3080692A (en) * 1960-07-11 1963-03-12 Nat Tank Co Adsorption process and apparatus for gas dehydration and hydrocarbon recovery
US3311189A (en) * 1960-10-28 1967-03-28 Walker Mfg Co Ceramic coated muffler with drainage openings
US3055157A (en) * 1961-01-11 1962-09-25 Nat Tank Co Control system for closed cycle gas dehydration and hydrocarbon recovery system
US3266221A (en) * 1964-06-02 1966-08-16 Union Carbide Corp Ethylene recovery from gas mixtures
US3324669A (en) * 1964-06-08 1967-06-13 Pittsburgh Activated Carbon Co Lean oil contact with the regenerative medium for adsorbers

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3800507A (en) * 1970-06-23 1974-04-02 Us Navy Low pressure air dehydrator
US3713272A (en) * 1971-08-26 1973-01-30 Continental Oil Co Process for recovering condensible components from a gas stream
US4436534A (en) 1982-11-08 1984-03-13 Seguy Bernard R Method for reducing desorbent consumption in recovery systems
US4819477A (en) * 1986-02-27 1989-04-11 Mds Health Group Limited Method and apparatus for trace sample collection
US5518527A (en) * 1993-08-26 1996-05-21 Mitsubishi Petrochemical Engineering Co., Ltd. Method for recovering ethylene from vent gas from ethylene oxide plant vent gas
US7799117B1 (en) * 2006-09-27 2010-09-21 Uop Llc Gas treatment process by temperature swing adsorption
US8002877B1 (en) * 2006-12-07 2011-08-23 Lawrence Sadler Method of trapping ethylene
US8535426B2 (en) 2006-12-07 2013-09-17 Lawrence R. Sadler Apparatus, system, and method for removing ethylene from a gaseous environment
WO2015021047A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method for extracting natural gas liquids from natural gas using an adsorbent media comprising a partially pyrolized macroporous polymer
WO2015021046A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method comprising a microwave heating system for regenerating adsorbent media used for extracting natural gas liquids from natural gas
WO2015021049A1 (en) 2013-08-06 2015-02-12 Dow Global Technologies Llc Method for extracting natural gas liquids from natural gas using an adsorbent media comprising a cross-linked macroporous polymer
WO2016003484A3 (en) * 2013-11-20 2016-03-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude A rapid temperature swing adsorption (rtsa) method using structured adsorbent for co2 capture from low pressure and low co2 concentration sources
US9314731B2 (en) 2013-11-20 2016-04-19 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude RTSA method using adsorbent structure for CO2 capture from low pressure and low concentration sources
WO2015108569A1 (en) 2014-01-17 2015-07-23 Dow Global Technologies Llc Methane-rich natural gas supply for stationary combustion systems
WO2015112199A1 (en) 2014-01-21 2015-07-30 Dow Global Technologies Llc Process for recovering natural gas liquids from natural gas produced in remote locations
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NO123833B (enrdf_load_stackoverflow) 1972-01-24
SE336424B (enrdf_load_stackoverflow) 1971-07-05
NL6713774A (enrdf_load_stackoverflow) 1968-06-10
DE1619858A1 (de) 1971-03-18
GB1183213A (en) 1970-03-04
BE723734A (enrdf_load_stackoverflow) 1969-04-16

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