US3243967A - Carbon dioxide liquification plant and process - Google Patents

Carbon dioxide liquification plant and process Download PDF

Info

Publication number
US3243967A
US3243967A US325113A US32511363A US3243967A US 3243967 A US3243967 A US 3243967A US 325113 A US325113 A US 325113A US 32511363 A US32511363 A US 32511363A US 3243967 A US3243967 A US 3243967A
Authority
US
United States
Prior art keywords
gas
accumulator
pressure
stream
liquid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US325113A
Inventor
Jr Theodore R Blevins
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ConocoPhillips Co
Original Assignee
Continental Oil Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Continental Oil Co filed Critical Continental Oil Co
Priority to US325113A priority Critical patent/US3243967A/en
Application granted granted Critical
Publication of US3243967A publication Critical patent/US3243967A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0027—Oxides of carbon, e.g. CO2
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/80—Carbon dioxide
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/04—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pressure accumulator
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • An object of the invention is a process for liquefying gas, especially carbon dioxide, without the need for elaborate refrigeration means.
  • Another object of the invention is apparatus for liquefying gas, especially carbon dioxide, which does not involve elaborate refrigeration means.
  • a particular object of the invention is an apparatus for liquefying gas, especially carbon dioxide, wherein liquefied gas can be automatically transferred from an accumulator to a storage tank without the use of a pump.
  • Another particular object of the invention is apparatus which permits liquefying gas, particularly carbon dioxide, and transfer of liquefied gas periodically from an accumulator to a storage tank without the use of a pump or operator control.
  • the single figure shows the essential items of apparatus and of process flow for the practice of the invention by a preferred embodiment thereof.
  • the process of the invention comprises: passing an expanding gaseous stream in indirect heat exchange with a second gaseous stream which second gaseous ream is maintained at substantially constant elevated pressure while the heat exchange is being controlled to liquefy at least a substantial proportion of the second gaseous stream to produce a product stream containing at least a substantial proportion of liquefied gas; this product stream is withdrawn from the heat exchange zone at substantially the same pressure as maintained therein.
  • An additional amount of liquefied gas can be obtained by expanding the product s eam from the withdrawal pressure to a lower pressure.
  • a gaseous stream of carbon dioxide, at a predetermined elevated pressure, is passed from source 11 by way of valved conduit 12 into heat exchanger 13.
  • Another gaseous carbon dioxide stream from source 15 is passed, at a predetermined elevated pressure, by way of valved line 16 into heat exchanger 13 separately from the gaseous stream introduced by way of line 12.
  • the carbon dioxide streams here may be obtained from any source. They are particularly easily obtainable from the waste gas of natural gas purification plants.
  • the carbon dioxide streams are dehydrated to a dew point where condensation of water vapor will not interfere with operation of the process.
  • the streams may be available "ice at elevated pressures or brought to the desired elevated pressure by compressors, not shown.
  • the carbon dioxide may be pure or it may contain moderate amounts of natural gas hydrocarbons.
  • Heat exchanger 13 is adapted for indirect heat exchange contact between two gaseous streams.
  • heat exchanger 13 is a shell and tube exchanger.
  • the dimensions of the heat exchanger will be dependent upon the heat duty required to liquefy at least a substantial proportion of the gaseous stream from source 15.
  • the cooling heat exchanger duty is afforded by expanding the gaseous stream from line 12 through heat exchanger 13 down to the necessary lower pressure.
  • the expanded gas is vented to the atmosphere by way of valved line 18.
  • the main expansion of the gas stream from source 11 is carried out before the stream enters exchanger 13. Additional ex pansion is taken within exchanger 13.
  • the gaseous stream from source is cooled in heat exchanger 13 at substantially constant pressure which pressure generally is about the same pressure as that existing on the gas stream delivered from source 15, except for line pressure drops.
  • a gas liquid product stream is produced in heat exchanger 13 by the substantial constant pressure cooling; this product stream is withdrawn from heat exchanger 13 by way of line 20.
  • Pressure regulator 22 maintains the withdrawn product stream and the gas from source 15 at the substantially constant desired elevated pressure.
  • the heat exchange within exchanger 13 is carried out in such a manner that at least a substantial proportion of the gaseous stream is liquefied. With a carbon dioxide gaseous stream it is convenient to liquefy 20-50% of the gas introduced by way of line 16 into exchanger 13.
  • an additional amount of liquid carbon dioxide is produced by expansion cooling of the product stream beyond regulator 22.
  • the stream of gas and liquid is passed from regulator 22 and expands through conduit 24 to the pressure maintained within gas-liquid separator vessel (accumulator) 30.
  • Accumulator 3% may be any vessel which affords separation of a gas-liquid stream and permits accumulating a body of liquid and the withdrawal overhead of gas.
  • Gas is taken overhead from accumulator 33 by way of conduits 34, 35 and 36.
  • the desired substantially constant elevated pressure is maintained within accumulator by pressure regulator 38 positioned in conduit 36.
  • Conduits 34, 35 and 36 permit passing the elevated pressure gas from accumulator 30 to join the gas stream from conduit 12 near the entrance of heat exchanger 13. This return gas provides additional expansion cooling.
  • Accumulator 30 is provided with a liquid level sensing and control means 49.
  • LLC 40 may be any form of conventional means responsing to the liquid level.
  • the sensing element here is a simple float.
  • Conduit 44 permits transfer of liquid carbon dioxide from accumulator 39 to storage tank 46.
  • An important feature of the process of the invention is that the liquid from accumulator 3th is transferred by way of line 44 to storage tank 46 without the use of a pump.
  • tank 46 is maintahe at subsantially the same pressure as acumulator 3%).
  • gas produced in tank 46 is used for expansion cooling in heat exchanger 13 by providing conduit Eli and conduit 52 which joins conduit 36.
  • Conduit 52 is provided with a check valve, not numbered.
  • pressure regulator 38 normally maintains .and 4% of natural gas hydrocarbons.
  • an important feature of this invention is “that liquid is periodically, automatically, transferred from accumulator to tank 46 without wasting the expansion cooling capacity possessed by gas from tank 46.
  • a bypass conduit means 60 is provided for passing gas from conduit 50 around pressure regulator 38 to conduit 36.
  • Conduit 69 includes control valve 62 which is activated by LLC 40 by way of control line 64. When the float reaches the desired liquid level in accumulator 30, the liquid level controller 40 activates the valve opening mechanism of value 62 causing it to open. Gas from tank 46 is then passed through conduit 50 and conduit 62 into line 36 which is at a much lower pressure than accumulator 30. Thus the necessary pressure differential between accumulator 3t and storage tank 46 is created and liquid is forced from accumulator until LLC 40 causes valve 62 to close.
  • the stream emerging from exchanger 13 by way of line 20 contains about 50% of liquid carbon dioxide.
  • valve 62 When the liquid level in accumulator 30 reaches the desired point, valve 62 is opened, pressure drops in tank 46 and the pressure differential between accumulator 30 and tank 46 automatically transfers liquid to tank 46. Valve 62 is closed by LLC 40 and the cycle of accumulation of liquid in accumulator 3%) begins again.
  • Means not shown are provided in accumulator 30 which automatically close-in the operation should the liquid level in accumulator 30 reach a danger point.
  • the invention provides a very simple answer to producing liquids gas when gas is available at high pressure in amounts greater than that needed in the form of a liquid; the extra gas is used to provide the cooling needed to produce the desired amount of liquid gas.
  • the apparatus and process of this invention provide an operation that functions automatically without the need for intervention by an operator except for maintenance.
  • product is available at a pressure of 820 p.s.i.g. and 60.
  • a process for liquefying gas and transferring said liquid to a storage tank which process comprises:
  • An apparatus for liquefying a gas which apparatus comprises, in combination:
  • heat exchanger means for indirect contact of two gaseous streams
  • a second conduit means for introducing a second gaseous streams, at a predetermined elevated .pressure, into said heat exchanger and means for maintaining said second stream at substantially constant pressure while in said heat exchanger;

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Description

APril 1966 T. R. BLEVINS, JR 3,243,967
CARBON DIOXIDE LIQUIFICATION PLANT AND PROCESS Filed Nov. 20, 1963 Theodore E. 5/6 v/ns, Jr
A TTORNEY United States Patent 3,243,967 CARBQN DIOXEDE LIQUIFICATION PLANT AND PRGCESS Theodore R. Blevins, J12, Arvada, C010,, assignor to Continental Gil Company, Ponca City, Okla, a corporaion of Gklahoma Filed Nov. 20, 1963, Ser. No. 325,113 3 Clmms. (Cl. 629) This invention relates to a process and apparatus for liquefying gas and particularly for liquefying carbon dioxide.
An object of the invention is a process for liquefying gas, especially carbon dioxide, without the need for elaborate refrigeration means. Another object of the invention is apparatus for liquefying gas, especially carbon dioxide, which does not involve elaborate refrigeration means. A particular object of the invention is an apparatus for liquefying gas, especially carbon dioxide, wherein liquefied gas can be automatically transferred from an accumulator to a storage tank without the use of a pump. Another particular object of the invention is apparatus which permits liquefying gas, particularly carbon dioxide, and transfer of liquefied gas periodically from an accumulator to a storage tank without the use of a pump or operator control. Other objects of the invention will become apparent in the course of the detailed description thereof.
The single figure shows the essential items of apparatus and of process flow for the practice of the invention by a preferred embodiment thereof.
Briefly, the process of the invention comprises: passing an expanding gaseous stream in indirect heat exchange with a second gaseous stream which second gaseous ream is maintained at substantially constant elevated pressure while the heat exchange is being controlled to liquefy at least a substantial proportion of the second gaseous stream to produce a product stream containing at least a substantial proportion of liquefied gas; this product stream is withdrawn from the heat exchange zone at substantially the same pressure as maintained therein. An additional amount of liquefied gas can be obtained by expanding the product s eam from the withdrawal pressure to a lower pressure.
The above and other features of the invention are described in connection with the single figure which forms a part of the specification. It is to be understood that the figure sets forth only those items of apparatus and those process features needed for the practice of the invention, to be taken in conjunction with features which can be readily added by those of ordinary skill in this art.
The invention is described in connection with liquefication of carbon dioxide; however, it is to be understood that the process and apparatus may be used for liquefying any gas whose phase diagram permits a substantial amount of liquid to be produced under the process conditions of the invention.
A gaseous stream of carbon dioxide, at a predetermined elevated pressure, is passed from source 11 by way of valved conduit 12 into heat exchanger 13. Another gaseous carbon dioxide stream from source 15 is passed, at a predetermined elevated pressure, by way of valved line 16 into heat exchanger 13 separately from the gaseous stream introduced by way of line 12.
The carbon dioxide streams here may be obtained from any source. They are particularly easily obtainable from the waste gas of natural gas purification plants. The carbon dioxide streams are dehydrated to a dew point where condensation of water vapor will not interfere with operation of the process. The streams may be available "ice at elevated pressures or brought to the desired elevated pressure by compressors, not shown. The carbon dioxide may be pure or it may contain moderate amounts of natural gas hydrocarbons.
Heat exchanger 13 is adapted for indirect heat exchange contact between two gaseous streams. Preferably heat exchanger 13 is a shell and tube exchanger. The dimensions of the heat exchanger will be dependent upon the heat duty required to liquefy at least a substantial proportion of the gaseous stream from source 15.
The cooling heat exchanger duty is afforded by expanding the gaseous stream from line 12 through heat exchanger 13 down to the necessary lower pressure. In this embodiment the expanded gas is vented to the atmosphere by way of valved line 18. In general, the main expansion of the gas stream from source 11 is carried out before the stream enters exchanger 13. Additional ex pansion is taken within exchanger 13. The gaseous stream from source is cooled in heat exchanger 13 at substantially constant pressure which pressure generally is about the same pressure as that existing on the gas stream delivered from source 15, except for line pressure drops.
A gas liquid product stream is produced in heat exchanger 13 by the substantial constant pressure cooling; this product stream is withdrawn from heat exchanger 13 by way of line 20. Pressure regulator 22 maintains the withdrawn product stream and the gas from source 15 at the substantially constant desired elevated pressure. The heat exchange within exchanger 13 is carried out in such a manner that at least a substantial proportion of the gaseous stream is liquefied. With a carbon dioxide gaseous stream it is convenient to liquefy 20-50% of the gas introduced by way of line 16 into exchanger 13.
In a preferred form of the invention, an additional amount of liquid carbon dioxide is produced by expansion cooling of the product stream beyond regulator 22. The stream of gas and liquid is passed from regulator 22 and expands through conduit 24 to the pressure maintained within gas-liquid separator vessel (accumulator) 30. Accumulator 3% may be any vessel which affords separation of a gas-liquid stream and permits accumulating a body of liquid and the withdrawal overhead of gas. Gas is taken overhead from accumulator 33 by way of conduits 34, 35 and 36. The desired substantially constant elevated pressure is maintained within accumulator by pressure regulator 38 positioned in conduit 36. Conduits 34, 35 and 36 permit passing the elevated pressure gas from accumulator 30 to join the gas stream from conduit 12 near the entrance of heat exchanger 13. This return gas provides additional expansion cooling.
Accumulator 30 is provided with a liquid level sensing and control means 49. LLC 40 may be any form of conventional means responsing to the liquid level. The sensing element here is a simple float.
Conduit 44 permits transfer of liquid carbon dioxide from accumulator 39 to storage tank 46. An important feature of the process of the invention is that the liquid from accumulator 3th is transferred by way of line 44 to storage tank 46 without the use of a pump.
Normally accumulator 3%, storage tank 46 and all of the lines and vessels are insulated; for convenience no insulation is shown.
Preferably tank 46 is maintahe at subsantially the same pressure as acumulator 3%). In this embodiment gas produced in tank 46 is used for expansion cooling in heat exchanger 13 by providing conduit Eli and conduit 52 which joins conduit 36. Conduit 52 is provided with a check valve, not numbered. In the embodiment of the figure pressure regulator 38 normally maintains .and 4% of natural gas hydrocarbons.
additional expansion takes place.
,from exchanger 13 at 50 F.
tank 46 and acumulator 30 at substantially the same pressure.
When a sufficient body of liquid is present in accumulator 30, it is transferred by way of conduit 44 to tank 46 by the creation of a pressure difierential between accumulator 30 and tank 46. The pressure in tank 46 i's'lowered below the pressure of accumulator 3t) and this pressure dilferential forces liquid from accumulator 30 into tank 46. This pressure differential may be created by providing a simple relief valve at tank 46 and venting the gas to the atmosphere.
However, an important feature of this invention is "that liquid is periodically, automatically, transferred from accumulator to tank 46 without wasting the expansion cooling capacity possessed by gas from tank 46. In this embodiment a bypass conduit means 60 is provided for passing gas from conduit 50 around pressure regulator 38 to conduit 36. Conduit 69 includes control valve 62 which is activated by LLC 40 by way of control line 64. When the float reaches the desired liquid level in accumulator 30, the liquid level controller 40 activates the valve opening mechanism of value 62 causing it to open. Gas from tank 46 is then passed through conduit 50 and conduit 62 into line 36 which is at a much lower pressure than accumulator 30. Thus the necessary pressure differential between accumulator 3t and storage tank 46 is created and liquid is forced from accumulator until LLC 40 causes valve 62 to close.
The process of the invention is described in connection with FIG. 1 in a specific embodiment wherein essential- 1y pure liquid carbon dioxide is produced from a gaseous stream consisting of 92% carbon dioxide, 4% nitrogen, A natural gas purification plant provides 4 million standard cubic feet per day of this gas. This stream is dehydrated to a dew point lower than 50 F.; the dry gas stream is at 600 p.s.i.g. and 64 F. This 600 p.s.i.g. stream is expanded and is introduced into heat exchanger 13 where The stream emerging from heat exchanger 13 is at about F. and about p.s.i.g.
- The stream which provides the liquid carbon dioxide F. temperature. 1.4 million s.c.f. per day of this gas are introduced at 60 F. and 820 p.s.i.g. into exchange 13 where it is indirectly cooled; a product stream emerges This gas stream is maintained in exchanger 13 at 810 p.s.i.g. by controller 22.
The stream emerging from exchanger 13 by way of line 20 contains about 50% of liquid carbon dioxide.
About 15% more of the gaseous carbon dioxide present in the product stream is liquefied by expansion cooling down to 300 p.s.i.g., which pressure is maintained at accumulator 30 by regulator 38. Tank 46 is maintained at 300 p.s.i.g. and a tempertaure of 10 F.
When the liquid level in accumulator 30 reaches the desired point, valve 62 is opened, pressure drops in tank 46 and the pressure differential between accumulator 30 and tank 46 automatically transfers liquid to tank 46. Valve 62 is closed by LLC 40 and the cycle of accumulation of liquid in accumulator 3%) begins again.
Means not shown are provided in accumulator 30 which automatically close-in the operation should the liquid level in accumulator 30 reach a danger point.
It can be seen from the above description that the invention provides a very simple answer to producing liquids gas when gas is available at high pressure in amounts greater than that needed in the form of a liquid; the extra gas is used to provide the cooling needed to produce the desired amount of liquid gas. In natural gas purification plants where it is customary to operate with a minimum labor force, the apparatus and process of this invention provide an operation that functions automatically without the need for intervention by an operator except for maintenance.
product is available at a pressure of 820 p.s.i.g. and 60.
Thus having described the invention what is claime 1. A process for liquefying gas and transferring said liquid to a storage tank which process comprises:
indirectly heat exchanging a gaseous stream, maintained at substantially constant pressure by a first pressure regulator means, and another gaseous stream under conditions Wherein'expansion of said other stream provides suflicient cooling-to liquefy at least a substantial proportion of said constant pressure stream;
passing a liquid-vapor product stream, at substantially the aforesaid constant pressure, from said heat exchange to a gas-liquid accumulator adapted to accumulate liquefied gas while maintaining said ac cumulator at a substantially constant pressure, lower than the aforesaid pressure;
expansion cooling said product stream through said first regulator means during said passage to liquefy additional gas;
passing gas from said accumulator and gas from a storage tank containing liquefied gas, transferred from said accumulator, at said accumulator constant pressure, through another pressure regulator means to said indirect heat exchange as a part of said other gaseous stream; and periodically transferring liquid from said accumulator to said tank, by having an accumulator liquid level controller means activate a gas control valve means, in communication with the gas space in said tank, thereby afiording a pressure differential between said accumulator and said tank. 4
2. The process of claim 1 wherein both said streams are carbon dioxide.
3. An apparatus for liquefying a gas which apparatus comprises, in combination:
heat exchanger means for indirect contact of two gaseous streams;
a first conduit means for passing a first gaseous stream at predetermined elevated pressure into said heat exchanger means and means permitting expansion cooling of said first stream to provide cooling duty in said exchanger;
a second conduit means for introducing a second gaseous streams, at a predetermined elevated .pressure, into said heat exchanger and means for maintaining said second stream at substantially constant pressure while in said heat exchanger;
a gas-liquid separator-accumulator and means for maintaining said vessel at a predetermined elevated pressure; j
a third conduit means for passing a gas-liquid stream, product of said heat exchanged second stream, into said accumulator;
a storage tank for liquefied gas;
a fourth conduit means for passing liquefied gas from said accumulator to said tank;
a fifth conduit means for passing gas from said accumulator to said heat exchanger means for indirect contact with said second stream in said exchanger;
a sixth conduit means for passing gas from said tank to join gas from said accumulator, at the predetermined elevated pressure maintained in said accumulator; and I a bypass conduit means, including valve means responsive to liquid level within said accumulator, for passing gas from said tank to said heat exchanger for indirect contact with said second stream in said exchanger, said bypass conduit means providing a pressure drop between said accumulator and said tank, whereby liquefied gas can be automatically forced from said accumulator to said tank.
(References on following page) References Cited by the Examiner UNITED FOREIGN PATENTS STATES PATENTS 579,624 6/ 1933 Germany. Ragatz 202-460 XR 1,145,197 3/1963 Germany. Eastman 62-11 5 301,741 12/1929 Great Britain. BronsonL 62--10 Gantt 202160 NORMAN YUDKOFF, Primary Examiner.

Claims (1)

1. A PROCESS FOR LIQUEFYING GAS AND TRANSFERRING SAID LIQUID TO A STORAGE TANK WHICH PROCESS COMPRISES: INDIRECTLY HEAT EXCHANGING A GASEOUS STREAM, MAINTAINED AT SUBSTANTIALLY CONSTANT PRESSURE BY A FIRST PRESSURE REGULATOR MEANS, AND ANOTHER GASEOUS STREAM UNDER CONDITIONS WHEREIN EXPANSION OF SAID OTHER STREAM PROVIDES SUFFICIENT COOLING TO LIQUEFY AT LEAST A SUBSTANTIAL PROPORTION OF SAID CONSTANT PRESSURE STREAM; PASSING A LIQUID-VAPOR PRODUCT STREAM, AT SUBSTANTIALLY THE AFORESAID CONSTANT PRESSURE, FROM SAID HEAT EXCHANGE TO A GAS-LIQUID ACCUMULATOR ADAPTED TO ACCUMULATE LIQUEFIED GAS WHILE MAINTAINING SAID ACCUMULATOR AT A SUBSTANTIALLY CONSTANT PRESSURE, LOWER THAN THE AFORESAID PRESSURE; EXPANSION COOLING SAID PRODUCT STREAM THROUGH SAID FIRST REGULATOR MEANS DURING SAID PASSAGE TO LIQUEFY ADDITIONAL GAS; PASSING GAS FROM SAID ACCUMULATOR AND GAS FROM A STORAGE TANK CONTAINING LIQUEFIED GAS, TRANSFERRED FROM SAID ACCUMULATOR, AT SAID ACCUMULATOR CONSTANT PRESSURE, THROUGH ANOTHER PRESSURE REGULATOR MEANS TO SAID INDIRECT HEAT EXCHANGE AS A PART OF SAID OTHER GASEOUS STREAM; AND PERIODICALLY TRANSFERRING LIQUID FROM SAID ACCUMULATOR TO SAID TANK, BY HAVING AN ACCUMULATOR LIQUID LEVEL CONTROLLER MEANS ACTIVATE A GAS CONTROL VALVE MEANS, IN COMMUNICATION WITH THE GAS SPACE IN SAID TANK, THEREBY AFFORDING A PRESSURE DIFFERENTIAL BETWEEN SAID ACCUMULATOR AND SAID TANK.
US325113A 1963-11-20 1963-11-20 Carbon dioxide liquification plant and process Expired - Lifetime US3243967A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US325113A US3243967A (en) 1963-11-20 1963-11-20 Carbon dioxide liquification plant and process

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US325113A US3243967A (en) 1963-11-20 1963-11-20 Carbon dioxide liquification plant and process
NL6516809A NL6516809A (en) 1965-12-23 1965-12-23

Publications (1)

Publication Number Publication Date
US3243967A true US3243967A (en) 1966-04-05

Family

ID=19795013

Family Applications (1)

Application Number Title Priority Date Filing Date
US325113A Expired - Lifetime US3243967A (en) 1963-11-20 1963-11-20 Carbon dioxide liquification plant and process

Country Status (4)

Country Link
US (1) US3243967A (en)
FR (1) FR1463349A (en)
GB (1) GB1064552A (en)
NL (1) NL6516809A (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3962881A (en) * 1974-02-19 1976-06-15 Airco, Inc. Liquefaction of a vapor utilizing refrigeration of LNG
FR2990749A1 (en) * 2012-05-15 2013-11-22 Air Liquide METHOD AND APPARATUS FOR BREATHING A CO2-RICH FLUID
WO2022199072A1 (en) * 2021-03-24 2022-09-29 惠州凯美特气体有限公司 Liquid carbon dioxide production device and system
EP4390280A1 (en) * 2022-12-12 2024-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for separating a carbon dioxide-containing gas mixture

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB301741A (en) * 1927-12-02 1929-12-12 Linde Eismasch Ag Method of solidifying gases
DE579624C (en) * 1929-11-30 1933-07-01 I G Farbenindustrie Akt Ges Production of solid carbonic acid
US2276089A (en) * 1937-06-26 1942-03-10 Union Oil Co Recovery of solvents from oils
US2632316A (en) * 1950-11-04 1953-03-24 Texas Co Separation of carbon dioxide from gaseous mixtures
US2738658A (en) * 1952-12-24 1956-03-20 Air Reduction Separation of gas by solidification
US2813594A (en) * 1956-02-23 1957-11-19 Universal Oil Prod Co Fractionator condensing assembly
DE1145197B (en) * 1961-07-17 1963-03-14 Steinkohlengas Ag Process for the production of medium-pressure carbonic acid which can be filled in the liquid state with less than 0.2 volume percent foreign gas content from high-pressure carbonic acid with a higher foreign gas content

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB301741A (en) * 1927-12-02 1929-12-12 Linde Eismasch Ag Method of solidifying gases
DE579624C (en) * 1929-11-30 1933-07-01 I G Farbenindustrie Akt Ges Production of solid carbonic acid
US2276089A (en) * 1937-06-26 1942-03-10 Union Oil Co Recovery of solvents from oils
US2632316A (en) * 1950-11-04 1953-03-24 Texas Co Separation of carbon dioxide from gaseous mixtures
US2738658A (en) * 1952-12-24 1956-03-20 Air Reduction Separation of gas by solidification
US2813594A (en) * 1956-02-23 1957-11-19 Universal Oil Prod Co Fractionator condensing assembly
DE1145197B (en) * 1961-07-17 1963-03-14 Steinkohlengas Ag Process for the production of medium-pressure carbonic acid which can be filled in the liquid state with less than 0.2 volume percent foreign gas content from high-pressure carbonic acid with a higher foreign gas content

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3962881A (en) * 1974-02-19 1976-06-15 Airco, Inc. Liquefaction of a vapor utilizing refrigeration of LNG
FR2990749A1 (en) * 2012-05-15 2013-11-22 Air Liquide METHOD AND APPARATUS FOR BREATHING A CO2-RICH FLUID
WO2013171421A3 (en) * 2012-05-15 2015-11-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for venting a co2‑rich fluid
WO2022199072A1 (en) * 2021-03-24 2022-09-29 惠州凯美特气体有限公司 Liquid carbon dioxide production device and system
EP4390280A1 (en) * 2022-12-12 2024-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for separating a carbon dioxide-containing gas mixture

Also Published As

Publication number Publication date
FR1463349A (en) 1966-06-03
GB1064552A (en) 1967-04-05
NL6516809A (en) 1967-06-26

Similar Documents

Publication Publication Date Title
US2082189A (en) Method of liquefying and storing fuel gases
US3413817A (en) Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3218816A (en) Process for cooling a gas mixture to a low temperature
US4609390A (en) Process and apparatus for separating hydrocarbon gas into a residue gas fraction and a product fraction
US3292380A (en) Method and equipment for treating hydrocarbon gases for pressure reduction and condensate recovery
US3347055A (en) Method for recuperating refrigeration
US4901533A (en) Process and apparatus for the liquefaction of a natural gas stream utilizing a single mixed refrigerant
US3312073A (en) Process for liquefying natural gas
US2535148A (en) Method of storing natural gas
US4012212A (en) Process and apparatus for liquefying natural gas
US2209534A (en) Method for producing gas wells
CA1253818A (en) Purification of carbon dioxide for use in brewing
US2959020A (en) Process for the liquefaction and reliquefaction of natural gas
US2880591A (en) Low-temperature gas absorption
US3478529A (en) Purification of refrigerant
US2716332A (en) Systems for separating nitrogen from natural gas
US2090163A (en) Method of liquefying and storing fuel gases
US2541569A (en) Liquefying and regasifying natural gases
US3754405A (en) Method of controlling the hydrocarbon dew point of a gas stream
US1905971A (en) Process and apparatus for refrigeration with liquefied fuel gas
US3413816A (en) Liquefaction of natural gas
US2729291A (en) Separating co2-petroleum mixtures
US3160489A (en) Nitrogen removal from natural gas
US3581510A (en) Gas liquefaction by refrigeration with parallel expansion of the refrigerant
US3056268A (en) Method for stabilizing the operation of a plant for the low temperature rectification of gaseous mixtures