US3243967A - Carbon dioxide liquification plant and process - Google Patents

Carbon dioxide liquification plant and process Download PDF

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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
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United States
Prior art keywords
gas
accumulator
pressure
stream
liquid
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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
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English (en)
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
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Continental Oil Co
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Filing date
Publication date
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Priority to US325113A priority Critical patent/US3243967A/en
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Publication of US3243967A publication Critical patent/US3243967A/en
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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;

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  • 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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)
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 (enrdf_load_html_response) 1965-12-23 1965-12-23

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FR (1) FR1463349A (enrdf_load_html_response)
GB (1) GB1064552A (enrdf_load_html_response)
NL (1) NL6516809A (enrdf_load_html_response)

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 (fr) * 2012-05-15 2013-11-22 Air Liquide Procede et appareil de mise a l'air d'un fluide riche en co2
WO2022199072A1 (zh) * 2021-03-24 2022-09-29 惠州凯美特气体有限公司 液态二氧化碳生产设备及系统
EP4390280A1 (fr) * 2022-12-12 2024-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'un mélange gazeux contenant du dioxyde de carbone

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 (de) * 1929-11-30 1933-07-01 I G Farbenindustrie Akt Ges Herstellung fester Kohlensaeure
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 (de) * 1961-07-17 1963-03-14 Steinkohlengas Ag Verfahren zur Herstellung von in fluessigem Zustand umfuellbarer Mitteldruck-Kohlensaeure mit weniger als 0,2 Volumprozent Fremdgas-gehalt aus Hochdruck-Kohlensaeure mithoeherem Fremdgasgehalt

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 (de) * 1929-11-30 1933-07-01 I G Farbenindustrie Akt Ges Herstellung fester Kohlensaeure
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 (de) * 1961-07-17 1963-03-14 Steinkohlengas Ag Verfahren zur Herstellung von in fluessigem Zustand umfuellbarer Mitteldruck-Kohlensaeure mit weniger als 0,2 Volumprozent Fremdgas-gehalt aus Hochdruck-Kohlensaeure mithoeherem Fremdgasgehalt

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 (fr) * 2012-05-15 2013-11-22 Air Liquide Procede et appareil de mise a l'air d'un fluide riche en co2
WO2013171421A3 (fr) * 2012-05-15 2015-11-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de mise à l'air d'un fluide riche en co2
WO2022199072A1 (zh) * 2021-03-24 2022-09-29 惠州凯美特气体有限公司 液态二氧化碳生产设备及系统
EP4390280A1 (fr) * 2022-12-12 2024-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'un mélange gazeux contenant du dioxyde de carbone

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

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