US3266262A - Vapor recovery method and system - Google Patents

Vapor recovery method and system Download PDF

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Publication number
US3266262A
US3266262A US425481A US42548165A US3266262A US 3266262 A US3266262 A US 3266262A US 425481 A US425481 A US 425481A US 42548165 A US42548165 A US 42548165A US 3266262 A US3266262 A US 3266262A
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United States
Prior art keywords
vapors
column
stage
chilling
water
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Expired - Lifetime
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US425481A
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English (en)
Inventor
Edward L Moragne
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Individual
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Individual
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Publication date
Priority to DENDAT1251233D priority Critical patent/DE1251233B/de
Application filed by Individual filed Critical Individual
Priority to US425481A priority patent/US3266262A/en
Priority to GB49550/65A priority patent/GB1064880A/en
Priority to BE672849D priority patent/BE672849A/xx
Priority to FR39697A priority patent/FR1459464A/fr
Priority to SE441/66A priority patent/SE317954B/xx
Priority to NO161235A priority patent/NO118924B/no
Priority to NL6600427A priority patent/NL6600427A/xx
Application granted granted Critical
Publication of US3266262A publication Critical patent/US3266262A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
    • B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
    • B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
    • B67D7/04—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes for transferring fuels, lubricants or mixed fuels and lubricants
    • B67D7/0476—Vapour recovery systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B01D5/0006—Coils or serpentines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/0081—Feeding the steam or the vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/0093—Removing and treatment of non condensable gases
    • 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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C5/00—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures
    • F17C5/02—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures for filling with liquefied gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/4516—Gas separation or purification devices adapted for specific applications for fuel vapour recovery systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/038—Refrigerants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/061—Level of content in the vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/01—Purifying the fluid
    • F17C2265/015—Purifying the fluid by separating

Definitions

  • This invention relates to a method and system for the recovery of liquefiable components of hydrocarbon vapors, and more particularly to the recovery of gasoline components from vapors expelled from tanks during the filling thereof.
  • the present invention has for its primary object the provision of an improved recovery system which is highly efficient in effecting condensation and recovery of maximum quantities of the liquefiable hydrocarbons.
  • An important object is the provision of a method of recovery which obviates the need for pumps or compressors for collecting and delivering the vapors to the recovery apparatus.
  • a furtther object is the provision of a method which employs multiple-stage cooling to effect condensation of the condensable hydrocarbon components.
  • Another object is the provision of a method employing two stages of cooling of the vapors to successively lower temperatures, the vapors being cooled in the first stage to a temperature just above the freezing point of water in the range from about 33 F. to about 35 F. to initially condense the major proportion of any water vapor present in the vapors to thereby obviate the formation of solid hydrates in the subsequent stage; and the vapors being cooled in the second stage to a temperature in the range from about 20 F. to about 30 F. sufiicient to condense the major proportion of the condensable hydrocarbon components of the vapors.
  • Yet another object is the provision of a method wherein movement of the vapors from the tank being filled is effected by the combination of displacement by liquid entering the tank and reduction in pressure occasioned by reduction in temperature and condensation in the liquid recovery steps of the method.
  • An additional object is the provision of a simple, highly compact and relatively inexpensive apparatus for carrying out the method in accordance with this invention.
  • the character of the fixed gases and their source will be described more fully hereinafter.
  • the vapors initially cooled by the fluid flowing through coil 14 will then enter a vertically disposed column 15, herein termed the liquefier, and will flow upwardly successively through first and second coil-type chillers 16 and 17, respectively, wherein the upflowing vapors will be chilled to successively lower temperatures by a suitable refrigerant fiowing through the coils of the respective chillers.
  • the shell of heat exchanger 13 may be on the side of column 15 to be in open communication therewith.
  • the uncondensed, generally inert gases leaving chillers 16 and 17 will flow out of the upper end of column 15 through a line 20 which leads to the inlet of pre-cooler coil 14, from which the gases will flow through a line 21 to the atmosphere.
  • a generally conventional refrigeration system is employed to produce the necessary chilling temperatures in chillers 16 and 17 and comprises a refrigerant compressor 25 having a suction pipe 26 and a discharge pipe 27 leading into a condenser 28 wherein a suitable and generally conventional refrigerant is liquefied and discharged through a pipe 29 into a receiver 30.
  • a line 31 is connected to the receiver for the delivery of liquefied refrigerant into a header 32 in which are mounted expansion valves 33 and 34 for expanding portions of the refrigerant, respectively, into chillers 16 and 17.
  • a refrigerant return line 35 having a back-pressure valve 36 therein, is connected to the second stage chiller 17 and leads back to suction line 26 going to the refrigerant compressor, thereby completing the refrigerant cycle.
  • Column 15 is provided with a sump or Well 37 fitted with a liquid level controller 38 which is operably connected to a discharge valve 39 mounted in a line 40 lead ing from the bottom of well 37.
  • the lower portion of column 15 above well 37 is equipped with a second liquid level controller 41 operably connected to a control valve 42 mounted in a discharge pipe 43 leading from a point in the bottom of column 15 just above well 37.
  • Pipe 43 is connected to a pump 44 which is controlled by a conventional electrical controller 45 operated by liquid level controller 41.
  • Pump 44 is connected to a discharge line 46 having a valve 47 mounted therein.
  • vapors which include air usually containing some water vapor initially present in the truck tank, together with light hydrocarbons vaporized from the gasoline as it is delivered into the truck tank, will be displaced therefrom into pipe P by the liquid entering the tank, as the filler opening of which will usually be sealed about the filler and vapor outlet pipes.
  • the displaced vapors Will be forced through pipe P and header H into vapor line 10 leading to the recovery system.
  • the displacement of the vapors by the liquid in the truck tank will be assisted by the reduction in pressure occasioned by the reduction in temperature and resulting condensation which takes place in the recovery system to move the vapors to the latter,-
  • the vapors will pass through flash arrestor 11 and thence through the shell of exchanger 13 into the vertically disposed liquefier column 15.
  • the vapors entering the column will be pre-cooled by heat-exchange in exchanger 13 with the cold fixed or inert gases passing out of the top of column 15 through pipe 20 and thence through coil 14 to discharge pipe 21.
  • the entering vapors passing through heat exchanger 13 will thus be partially cooled, generally to a temperature about F. below the ambient atmospheric temperature, and will flow therefrom into column 15 and thence upwardly successively through first stage chiller 16 and second stage chiller 17 wherein the vapors will be cooled to successively lower temperatures sufficient to effect the desired degree of condensation of the liquefiable components.
  • the vapors denuded of the liquefiable components will then flow out of column 15 through pipe 20, as previously noted.
  • First stage chiller 16 will be maintained at a temperature such as to chill the vapors to a suitable dew point temperature for the water vapor present in the vapors.
  • This temperature will ordinarily be in the range of from about 33 F. to 35 F., being carefully maintained to be just above the freezing point of water.
  • substantially all of the water vapor will be condensed and will separate from the uncondensed vapors and will fall to the bottom of column 15, collecting in well 37 to form the body W from which it will be continuously drained from the system through pipe 40 under control of liquid level controller 38.
  • Some of the heavier hydrocarbon components will also condense at the temperature maintained in chiller 16.
  • second stage chiller 17 which will be maintained at a somewhat lower temperature than that in the first stage but sufficiently low to effect substantially complete condensation of the liquefiable hydrocarbons remaining in the vapors.
  • This temperature will be in the range from about F. to about F.
  • the hydrocarbon components condensed in the precooler and the two chilling stages will separate from the fixed or uncondensed gases and will fall to the bottom of column 15 where they will form a layer G on top of the water collected in well 37.
  • the liquefied hydrocarbons will be continuously withdrawn from column 15 by means of pump 44 under the control of liquid level controller 41 and discharged through pipe 46 to storage.
  • the multiple-stage cooling including the pre-cooling stage and the two-stage chilling heretofore described, has been found to be highly effective in recovering a very large proportion of the liquefiable components of the vapors. It is found, however, that the recovery may be additionally increased by passing the vapors in advance of each of the chilling stages through a bed of porous solid materials indicated at 18 and 19, and located in advance of chillers 16 and 17, respectively. These porous solids appear to act as agglomerating agents and their mechanism is not fully understood.
  • the materials may be conventional alumina-silica catalysts commonly employed in many petroleum cracking and other refining process, or may be conventional alumina pellets impregnated with zinc oxide, the proportions of which may be varied in the respective catalyst beds, the proportion of zinc oxide to alumina in the second stage bed 19 being generally greater than in the first stage bed 18.
  • the method and apparatus in accordance with this invention is designed primarily for use when the ambient atmospheric temperatures during loading of the gasoline or other volatile liquid are comparatively high, as under summer conditions, since it will be obvious that under low temperature winter conditions, the volatilization losses will generally be quite low, and sufficiently so that operation of the method and apparatus become unnecessary.
  • the apparatus heretofore described may readily be made very compact and has been constructed to be incorporated in a self-contained unit mounted on a skid, or other mobile platform which can be moved easily from place to place.
  • a self-contained unit mounted on a skid, or other mobile platform which can be moved easily from place to place.
  • Such a unit for example, made about 11 feet in height, 8 feet in length, and 4 feet in width will house an apparatus assembly which is capable of handling about 3500 cubic feet of vapors per minute.
  • a portable unit of even smaller size for connection to ship tanks during loading thereof and having a capacity of about 400 cubic feet per minute has been constructed.
  • the method of recovering liquefiable components from vapors evolved during the filling of tanks with volatile hydrocarbon liquids comprising, cooling the vapors in a first chilling stage to a dew point temperature for water vapor present in the vapors etfective to condense and separate the Water from the vapors, thereafter cooling the water-freed vapors in a second chilling stage to a lower temperature effective to condense and separate therefrom the condensable hydrocarbon components remaining in the vapors, and recovering the condensed hydrocarbons.
  • the method of recovering liquefiable components from vapors evolved during the filling of a tank with volatile hydrocarbon liquids comprising, transferring the evolved vapors to a liquefying zone, pre-cooling said vapors entering the liquefying zone, cooling the precooled vapors in the liquefying zone in a first chilling stage to a dew point temperature for water vapor present in the vapors effective to condense the major proportion of the water vapor, thereafter cooling the water-freed vapors in a second chilling stage to a lower temperature effective to condense the condensable hydrocarbon components remaining in said vapors, separately withdrawing water and the condensed hydrocarbons from the liquefying zone, discharging the finally uncondensed vapors from said zone, and passing said uncondensed vapors into heatexchange relationship with said vapors entering the liquefying zone to effect said pre-cooling.
  • the method of recovering liquefiable components from vapors evolved during the filling of tanks with volatile hydrocarbon liquids comprising, cooling the vapors in a first chilling stage to a dew point temperature for water vapor present in the vapors effective to condense and separate the water from the vapors, thereafter cooling the water-freed vapors in a second chilling stage to a lower temperature effective to condense and separate therefrom the condensable hydrocarbon components remaining in the vapors, passing said vapors in advance of each of said cooling stages through a body of a porous solid material selected from the class consisting of alumina-silica particles and alumina particles impregnated With ZnO and recovering the condensed hydrocarbons.
  • Apparatus for recovering liquefiable components from vapors evolved during the filling of a tank with volatile hydrocarbon liquids comprising, a vertically disposed liquefier column, conduit means for delivering vapors from a tank in which they are evolved to an intermediate portion of said column, first and second vertically spaced chilling coils disposed in said column in the path of upward flow of the vapors through the column, means for circulating a refrigerant through said coils including means for controlling the chilling temperatures in the respective coils, means for withdrawing water from the lower end of said column, means for withdrawing liquefied hydrocarbons from an intermediate portion of the column, and a vent conduit communicating with the upper end of said column for discharging uncondensed vapors therefrom.
  • An apparatus including a body of porous particulate solid material disposed in advance of each of said chilling coils in the path of flow of said vapors therethrough.
  • An apparatus including vapor precooling means, comprising a closed coil connected to said vent conduit and disposed in said conduit means in the path of flow of the entering vapors.
  • Apparatus for recovering liquefiable components from vapors evolved during the filling of a tank with volatile hydrocarbon liquids comprising, a vertically disposed liqucfier column, conduit means for delivering vapors from a tank in which they are evolved to an intermediate portion of said column, first and second vertically spaced chilling coils disposed in said column above the point of entry of said conduit means in the path of upward flow of the vapors through the column, means for circulating a refrigerant through said coils including means for controlling the chilling temperatures in the respective coils, a water-accumulating Well at the lower end of said column, a drain conduit communicating with said well, a first liquid level controller operatively connected to said well and to said drain conduit for controlling the water level in said well, a second conduit connected to the lower portion of said column above said well, a second liquid level controller operatively connected to the lower portion of said column above said well and to said second conduit to control the level of liquefied hydrocarbons accumulating in the column on
  • An apparatus including a body of a porous solid particulate material disposed in advance of each of said chilling coils in the path of flow of the vapors therethrough.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Sampling And Sample Adjustment (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
US425481A 1965-01-14 1965-01-14 Vapor recovery method and system Expired - Lifetime US3266262A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
DENDAT1251233D DE1251233B (en, 2012) 1965-01-14
US425481A US3266262A (en) 1965-01-14 1965-01-14 Vapor recovery method and system
GB49550/65A GB1064880A (en) 1965-01-14 1965-11-22 Vapor recovery method and system
FR39697A FR1459464A (fr) 1965-01-14 1965-11-25 Procédé et appareil pour la récupération de constituants liquéfiables à partir de vapeurs d'hydrocarbures
BE672849D BE672849A (en, 2012) 1965-01-14 1965-11-25
SE441/66A SE317954B (en, 2012) 1965-01-14 1966-01-13
NO161235A NO118924B (en, 2012) 1965-01-14 1966-01-13
NL6600427A NL6600427A (en, 2012) 1965-01-14 1966-01-13

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US425481A US3266262A (en) 1965-01-14 1965-01-14 Vapor recovery method and system

Publications (1)

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US3266262A true US3266262A (en) 1966-08-16

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US425481A Expired - Lifetime US3266262A (en) 1965-01-14 1965-01-14 Vapor recovery method and system

Country Status (8)

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US (1) US3266262A (en, 2012)
BE (1) BE672849A (en, 2012)
DE (1) DE1251233B (en, 2012)
FR (1) FR1459464A (en, 2012)
GB (1) GB1064880A (en, 2012)
NL (1) NL6600427A (en, 2012)
NO (1) NO118924B (en, 2012)
SE (1) SE317954B (en, 2012)

Cited By (40)

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US3541803A (en) * 1968-09-18 1970-11-24 Gulf Central Pipeline Co Cryogenic liquid storage system
US3648436A (en) * 1970-03-26 1972-03-14 Ingersoll Rand Res Inc Gasoline vapor recovery
US3714790A (en) * 1971-04-13 1973-02-06 Fmc Corp Apparatus and method for handling volatile liquids
US3771317A (en) * 1970-12-07 1973-11-13 Parker Hannifin Corp Vapor recovery
US3830074A (en) * 1971-12-06 1974-08-20 Parker Hannifin Corp Vapor recovery system
DE2337055A1 (de) * 1973-07-20 1975-02-06 Linde Ag Verfahren und vorrichtung zur rueckgewinnung des in einem benzin-luft-gemisches enthaltenen benzins
US3972201A (en) * 1975-01-29 1976-08-03 Process Products, Inc. Vapor recovery system
US3981156A (en) * 1975-02-03 1976-09-21 Ecology Control, Inc. Vapor recovery system and method
US4027495A (en) * 1975-07-22 1977-06-07 Edwards Engineering Corporation Vapor recovery system for volatile liquids and vapor condensing apparatus for use therein
US4030899A (en) * 1975-02-24 1977-06-21 U.S. Philips Corporation Cooling device
US4110996A (en) * 1977-05-02 1978-09-05 Phillips Petroleum Company Method and apparatus for recovering vapor
FR2425258A1 (fr) * 1978-05-08 1979-12-07 Elf Union Dispositif pour separer en une fraction liquide et une fraction gazeuse les effluents gazeux provenant d'une installation de traitement d'hydrocarbures
FR2478473A1 (fr) * 1980-03-24 1981-09-25 Buse Kohlensaeure Procede et dispositif pour le detournement de gaz s'echappant d'un reservoir d'entreposage en cas d'incident
US4356699A (en) * 1980-01-02 1982-11-02 Rilett John W Gas condensation
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US4574005A (en) * 1982-03-29 1986-03-04 Nordson Corporation Continuous coater solvent recovery process
US4821524A (en) * 1985-07-30 1989-04-18 Olajipari Fovallalkozo Es Tervezo Vallalat Method and apparatus for reducing evaporation of storage tanks
US5006138A (en) * 1990-05-09 1991-04-09 Hewitt J Paul Vapor recovery system
US5017240A (en) * 1990-02-02 1991-05-21 Brown Earnest D Vapor treatment facilities for petroleum storage tank cleaning
US5076822A (en) * 1990-05-07 1991-12-31 Hewitt J Paul Vapor recovery system
US5144807A (en) * 1990-02-02 1992-09-08 Brown Ernest D Vapor treatment facilities for petroleum storage tank cleaning
US5367882A (en) * 1991-12-09 1994-11-29 Arid Technologies Gasoline vapor recovery
US5426945A (en) * 1994-02-04 1995-06-27 Jordan Holding Company Process and apparatus for recovering vapor
US5540757A (en) * 1995-05-15 1996-07-30 Jordan Holding Company Method for preconditioning adsorbent
WO1996030695A1 (en) * 1995-03-29 1996-10-03 Mmr Technologies, Inc. Self-cleaning low temperature refrigeration system
US5571231A (en) * 1995-10-25 1996-11-05 The Boc Group, Inc. Apparatus for storing a multi-component cryogenic liquid
US5584911A (en) * 1995-06-15 1996-12-17 Jordan Holding Company Vapor recovery system with cyclonic separator
US5591254A (en) * 1995-07-12 1997-01-07 Jordan Holding Company Vapor recovery system with automatic valve control
US5681369A (en) * 1996-05-10 1997-10-28 Jordan Holding Company Apparatus and method for recovering volatile liquid
WO1997040307A1 (en) * 1996-04-25 1997-10-30 Den Norske Stats Oljeselskap A/S Process and system for recovering and storing a light hydrocarbon vapor from crude oil
US5724832A (en) * 1995-03-29 1998-03-10 Mmr Technologies, Inc. Self-cleaning cryogenic refrigeration system
US5871568A (en) * 1996-06-21 1999-02-16 Jordan Technologies, Inc. Return circuit for vapor recovery system
US20080289353A1 (en) * 2007-05-22 2008-11-27 Maruya Richard H Refrigerant service port valve for air conditioners
ITBO20090263A1 (it) * 2009-04-29 2010-10-30 Germano Bregna Impianto per il rifornimento di carburante e procedimento per recuperare vapori in tale impianto.
US20120160218A1 (en) * 2010-12-21 2012-06-28 Audi Ag Fuel system
WO2013181178A2 (en) 2012-05-29 2013-12-05 Jordan Technologies, Llc Carbon safe vapor recovery system
US8979982B2 (en) 2013-05-01 2015-03-17 Jordan Technologies, Llc Negative pressure vapor recovery system
CN105840981A (zh) * 2016-04-14 2016-08-10 新奥科技发展有限公司 甲烷回收系统以及回收方法
WO2018007653A1 (es) * 2016-07-06 2018-01-11 Fuel Management Technologies, S.L. Sistema de recuperación y aprovechamiento de vapores procedentes de combustibles

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DE3903938A1 (de) * 1989-02-10 1990-08-23 Peter Weil Verfahren zur entsorgung der gasrauminhalte von grossvolumigen behaeltern bei umweltbelastenden inhaltstoffen
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CN109562926A (zh) * 2016-07-06 2019-04-02 燃料管理有限公司 燃料蒸气回收和利用系统
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NL6600427A (en, 2012) 1966-07-15
NO118924B (en, 2012) 1970-03-02
DE1251233B (en, 2012)
GB1064880A (en) 1967-04-12
SE317954B (en, 2012) 1969-12-01
BE672849A (en, 2012) 1966-05-25
FR1459464A (fr) 1966-11-18

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