US3419369A - Manufacturing town gas from liquefied natural gas - Google Patents

Manufacturing town gas from liquefied natural gas Download PDF

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US3419369A
US3419369A US44126165A US3419369A US 3419369 A US3419369 A US 3419369A US 44126165 A US44126165 A US 44126165A US 3419369 A US3419369 A US 3419369A
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gas
natural gas
air
conduit
zone
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Carl S Kelley
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Phillips Petroleum Co
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Phillips Petroleum Co
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases
    • 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F25J3/046—Completely integrated air feed compression, i.e. common MAC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • F25J3/04618—Heat exchange integration with process streams, e.g. from the air gas consuming unit for cooling an air stream fed to the air fractionation unit
    • G—PHYSICS
    • G05—CONTROLLING; REGULATING
    • G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
    • G05D21/00—Control of chemical or physico-chemical variables, e.g. pH value
    • G05D21/02—Control of chemical or physico-chemical variables, e.g. pH value characterised by the use of electric means
    • 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
    • F17C2221/01—Pure fluids
    • F17C2221/011—Oxygen
    • 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
    • F17C2221/031—Air
    • 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
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • 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
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/32—Hydrogen storage

Definitions

  • ABSTRACT OF THE DISCLOSURE The heating value and specific gravity of liquefied natural gas are adjusted for town gas use by vaporizing the liquefied natural gas by indirect heat exchange with air, which is partially liquefied and separated into an oxygenrich stream; passing a portion of the vaporized natural gas and the oxygen-rich stream to a combustion zone wherein they are burned to produce an intermediate gas; and passing the intermediate gas t0 a mixing zone wherein controlled amounts of the remaining vaporized natural gas and air are added to produce a product having predetermined B.t.u. and specific gravity values.
  • This invention relates to a method and apparatus for regulating and controlling the heating value of natural gas.
  • this invention relates t0 a method and apparatus for reducing the heating value of natural gas to render it suitable for household and industrial uses.
  • this invention relates to a method and apparatus for reducing the heating value of natural gas to produce a gas having a desired heating value and specific gravity.
  • the present invention provides a novel method of adjusting the heating value and specific gravity of a natural gas.
  • the invention is especially useful in adjusting the heating value and specific gravity of liquefied methane at its place of use.
  • My invention utilizes three distinct steps for regulating the heating value and specific gravity of natural gas.
  • the liquefied natural gas is vaporized by indirect heat exchange with air.
  • the air is cooled to a temperature wherein it is, at least partially, liquefied and separated into an oxygen-rich stream and a nitrogen-rich stream. Controlled amounts of the vaporized natural gas and the oxygen-rich stream are then passed to a combustion zone.
  • the third step of my process includes the mixing of the intermediate gas, the remaining portion of the vaporized natural gas, and a controlled amount of air.
  • an object of this invention is to provide a method and apparatus for reducing the heating value of liquefied natural gas.
  • Another important object of this invention is to provide a method and apparatus for producing a gaseous product having a controlled heating value and a controlled specific gravity.
  • the features and method of operation of my invention can best be understood by reference to the drawing.
  • the drawing is a diagrammatic representation of one form of equipment which may be used in the process of the invention.
  • liquified natural gas is supplied to gas vaporization and air liquefaction-separation zone 1 through conduit 2.
  • the flow of liquefied gas through conduit 2 is easily controlled by means of flow control valve 3.
  • the liquefied natural gas is vaporized by indirect heat exchange with air which is supplied through conduit 4. Since lar-ge volumes of high pressure air are required in the process, air compressor 5 is utilized to gather air from the atmosphere through line 6 and compress it. Since the liquefied natural gas is at an extremely low temperature, it cools the high pressure air stream in gas vaporization and air liquefaction zone 1 to a point where the air is partially liquefied and separated into two streams.
  • One stream contains a major amount of oxygen and the yother stream is predominantly nitrogen. Air liquefaction and separation processes are -well known in the art and are not explained in detail here.
  • the stream rich in nitrogen is removed through conduit 7. This nitrogen-rich stream can either be recovered for chemical usage, recovered for refrigerant value, vented to the atmosphere, or in some cases it may be bottled ⁇ and sold for industrial uses.
  • the oxygen-rich stream is withdrawn from gas vaporization and air liquefaction zone 1 through conduit 8.
  • the very cold oxygen-rich stream is passed through heat exchanger 9 in indirect heat exchange with the compressed air stream from compressor f5. Since the compressed air stream from compressor 5 is at an elevated temperature, the oxygenrich stream is heated to a point Where it is revaporized.
  • a portion of the oxygen-rich stream then flows through conduit 10 to partial combustion zone 11.
  • the remaining portion of oxygen-rich stream is withdrawn from the system through conduit 10a.
  • the remaining portion of the oxygen-rich stream can either be recovered for chemical use, recovered for refrigerant value, vented to the atmosphere, or bottled and sold for industrial uses.
  • Vaporized natural gas is withdrawn from gas vaporization and air liquefaction Zone 1 through conduit 12.
  • the vaporized natural gas is also passed to heat exchanger 13 wherein it additionally, in indirect heat exchange, cools the cornpressed air stream from air compressor 5.
  • a portion of the vaporized natural gas ows through conduit 1'4 to partial combustion zone 11.
  • the relative amounts of natural gas and oxygen ilowing to partial combustion zone 11 are regulated by means of control valves 1S and 16, respectively.
  • the ratio of natural gas to oxygen for partial combustion can be conveniently calculated. After this ratio is determined, ilow ratio recorder controller 17 can be used to maintain the proper ratio.
  • partial combustion zone 11 the natural gas is partially burned to produce an intermediate gas which is rich in oxygen and carbon monoxide.
  • Such processes are Well known in the art and have been used for many years in the manufacture of town gas. One such process is described in Petroleum Reiiner, vol. 38 (1959), No. ll, p. 294.
  • the intermediate gas from partial cornbustion zone 11 is withdrawn through conduit 18.
  • the intermediate gas is then passed to mixing zone 19.
  • mixing zone 19 the intermediate gas is mixed with controlled amounts of air which are added through conduit 20.
  • the air stream in conduit 20 can be a portion of the compressed air stream from air compressor 5.
  • the remaining portion Iof the vaporized natural gas from conduit 12 is also added to mixing zone 19 through conduit 21.
  • the exact amounts of the intermediate gas, vaporized natural gas and air that are added to mixing zone 19 is very critical. By carefully controlling the various amounts of intermediate gas, vaporized natural gas and air that are added to the mixing zone 19, it is possible to produce a nal gas having a desired heating value and specific gravity.
  • the determination of the proper amounts of the various components to be added to mixing zone 19 is accomplished by continuously sampling a small portion of the mixed gas that is withdrawn from mixing zone 19 through conduit 22. A small amount of the mixed gas is withdrawn through conduit 23 and passed to densitometer 24. In densitometer 24, the density or specic gravity is determined and a signal proportional to the specific gravity is passed to computer 25.
  • the heating value or B.t.u. content of the mixed gas from mixing zone 19 is determined by withdrawing a small portion of the gas through conduit 26 and passing it to a calorimeter 27. A signal proportional to the B.t.u. content of the gas is passed from calorimeter 27 to computer 25.
  • Computer 25 effectively controls the amounts of air and vaporized natural gas that are added to mixing zone 19. Since the various gaseous streams entering mixing zone 19 have different specific gravities or densities, it is easily seen that computer 2S serves to control the specific gravity of the nal gas product in conduit 22. Since the intermediate gas entering mixture zone 19 through conduit 18 is very rich in hydrois easily seen that when the B.t.u.
  • computer 25 sends a signal to flow ratio recorder controller 28 which resets ow control valve 29 and allows more vaporized natural gas (which gas itself has a specific gravity in the range desired for the nal product) to enter mixing zone 19. Since the vaporized natural gas has a higher B.t.u. content than the intermediate gas entering the mixing zone 19, the B.t.u. content of the gas will be increased. Conversely, if the B.t.u. content of the gas rises above the predetermined limits, computer 25 sends a signal to ow ratio recorder controller 28 which resets iiow control valve 29, thus decreasing the amount of vaporized natural gas entering mixing zone 19.
  • the combination of densitometer 24, computer 25 and calorimeter 27 furnish a unique method of controlling both the specific gravity and the B.t.u. content of the linal gas product. By this process, it is possible to adjust the heating value and the specific gravity of the fina] product to maintain the desired values for these properties.
  • Various components that can be used in the apparatus described above are well known in the art and -have not been described in detail here. It is understood that various heat exchangers, gas compressors, etc., not shown in the drawing, may be necessary for actual operation of my invention. Gas flowing through conduit 22 can be added directly to gas distribution ⁇ mains or it can be passed to a suitable storage vessel.
  • EXAMPLE The apparatus shown in the drawing is used to produce a town gas having a gross heating value of 500 B.t.u. per standard cubic foot with a gas specific gravity of 0.55 (air is 1.00).
  • Liquid methane is supplied through conduit 2 at a temperature of 250 F.
  • Partial combustion zone 11 is operated at a temperature of 2100 F. and at a pressure of 450 p.s.i.a.
  • the catalyst utilized in the partial combustion zone is granular magnesite with a 3 percent by weight nickel content.
  • the resulting gas product is passed through a desiccant and then is added directly to the gas distribution lines or to a suitable gas storage vessel.
  • the following table illustrates various stream compositions, B.t.u. content, and specific gravity measurements that are found in the process of this invention.
  • Method for reducing the heating value of a liqueed natural gas comprising:
  • step (g) passing air and at least a portion of the remainder of said vaporized natural gas stream of step (c) to said mixing zone, the amount of air and said vaporized natural gas added to said mixing zone being suiiicient to produce a gaseous mixture having a predetermined specic gravity and a predetermined heating value lower than said liquefied natural gas; and (h) recovering said gaseous mixture.
  • the method according to claim 1 further comprising cooling the air before introduction into said vaporizing zone by passing in indirect heat exchange relationship with said oxygen-rich stream and said vaporized natural gas stream.
  • suicient air and vaporized natural gas are added to said mixing Zone to produce a gaseous mixture having a specific gravity of 0.55 and a gross heating value of 500 B.t.u. per standard cubic foot.
  • a system for reducing the heating value of liquefied natural gas and maintaining the thus-treated product at a predetermined specific gravity comprising, in combination:
  • a system according to claim 5 wherein said means for measuring specic gravity is a densitometer.

Description

C. S. KELLEY Filed March 19. 1965 MANUFACTURING TOWN GAS FROM LIQUEFIED NATURAL GAS Dec. 3l, 1968 United States Patent 3,419,369 MANUFACTURING TOWN GAS FROM LIQUEFIED NATURAL GAS Carl S. Kelley, Bartlesville, Okla., assigner to Phillips Petroleum Company, a corporation of Delaware Filed Mar. 19, 1965, Ser. No. 441,261 7 Claims. (Cl. 48-196) ABSTRACT OF THE DISCLOSURE The heating value and specific gravity of liquefied natural gas are adjusted for town gas use by vaporizing the liquefied natural gas by indirect heat exchange with air, which is partially liquefied and separated into an oxygenrich stream; passing a portion of the vaporized natural gas and the oxygen-rich stream to a combustion zone wherein they are burned to produce an intermediate gas; and passing the intermediate gas t0 a mixing zone wherein controlled amounts of the remaining vaporized natural gas and air are added to produce a product having predetermined B.t.u. and specific gravity values.
This invention relates to a method and apparatus for regulating and controlling the heating value of natural gas. In one of its aspects, this invention relates t0 a method and apparatus for reducing the heating value of natural gas to render it suitable for household and industrial uses. In another aspect, this invention relates to a method and apparatus for reducing the heating value of natural gas to produce a gas having a desired heating value and specific gravity.
Recently there has been a sharp increase in the use of natural gas throughout the world. A considerable amount of interest has developed in the transportation of liquefied natural gases, especially methane, by barge or the like from producing fields to the place of utilization of said liquefied gas. Within the past few years, processes have been developed whereby natural gas is liquefied at or near a natural gas producing field, and then the liquefied gas is transported t0 its place of utilization. At the place of use, the liquefied natural gas must be revaporized before it is used as a fuel. In some localities, natural gas can be revaporized and used directly as a fuel. In other localities, the gas specifications for existing equipment therein are different from the specifications of the revaporized natural gas. This requires the revaporized natural gas to be reformed to a lower heating value and a new specific gravity before use. In localities where the revaporized natural gas is used as a supplement to or a substitute for manufactured gas, many problems arise. Natural gas has a calorific or heating value (B.t.u. content) about double that of certain manufactured gases so that it cannot be substituted for or mixed directly with such manufactured gases. Therefore, in such localities, the B.t.u. content of the revaporized natural gas rnust be adjusted or modified to equal that of the manufactured gas. Many processes have been proposed for adjusting the heating value of the revaporized natural gas, but these processes are undesirable because the specific gravity of the gas is also changed in the process. It is obvious, that there is need for a process and apparatus for controlling both the heating value and the specific gravity of the vaporized natural gas, before it is distributed for use.
The present invention provides a novel method of adjusting the heating value and specific gravity of a natural gas. The invention is especially useful in adjusting the heating value and specific gravity of liquefied methane at its place of use. My invention utilizes three distinct steps for regulating the heating value and specific gravity of natural gas. In the first step, the liquefied natural gas is vaporized by indirect heat exchange with air. In this vaporization step, the air is cooled to a temperature wherein it is, at least partially, liquefied and separated into an oxygen-rich stream and a nitrogen-rich stream. Controlled amounts of the vaporized natural gas and the oxygen-rich stream are then passed to a combustion zone.
In the second step of my process, a portion of the vaporized natural gas and the Oxygen-rich stream are burned in the combustion Zone to produce an intermediate gas which is rich in hydrogen and carbon monoxide. The third step of my process includes the mixing of the intermediate gas, the remaining portion of the vaporized natural gas, and a controlled amount of air. By closely controlling the various amounts of the intermediate gas, the vaporized methane and the air, it is possible to produce a finished gaseous product having a heating value and a specific gravity that is very near that of manufactured town gas.
Therefore, an object of this invention is to provide a method and apparatus for reducing the heating value of liquefied natural gas. Another important object of this invention is to provide a method and apparatus for producing a gaseous product having a controlled heating value and a controlled specific gravity.
Other objects, advantages and aspects of this invention will be evident to those skilled in the art upon examination of the following description, drawing, and claims.
The features and method of operation of my invention can best be understood by reference to the drawing. The drawing is a diagrammatic representation of one form of equipment which may be used in the process of the invention.
In the drawing, liquified natural gas is supplied to gas vaporization and air liquefaction-separation zone 1 through conduit 2. The flow of liquefied gas through conduit 2 is easily controlled by means of flow control valve 3. In gas vaporization and liquefactionseparation zone 1, the liquefied natural gas is vaporized by indirect heat exchange with air which is supplied through conduit 4. Since lar-ge volumes of high pressure air are required in the process, air compressor 5 is utilized to gather air from the atmosphere through line 6 and compress it. Since the liquefied natural gas is at an extremely low temperature, it cools the high pressure air stream in gas vaporization and air liquefaction zone 1 to a point where the air is partially liquefied and separated into two streams. One stream contains a major amount of oxygen and the yother stream is predominantly nitrogen. Air liquefaction and separation processes are -well known in the art and are not explained in detail here. The stream rich in nitrogen is removed through conduit 7. This nitrogen-rich stream can either be recovered for chemical usage, recovered for refrigerant value, vented to the atmosphere, or in some cases it may be bottled `and sold for industrial uses. The oxygen-rich stream is withdrawn from gas vaporization and air liquefaction zone 1 through conduit 8. The very cold oxygen-rich stream is passed through heat exchanger 9 in indirect heat exchange with the compressed air stream from compressor f5. Since the compressed air stream from compressor 5 is at an elevated temperature, the oxygenrich stream is heated to a point Where it is revaporized. A portion of the oxygen-rich stream then flows through conduit 10 to partial combustion zone 11. The remaining portion of oxygen-rich stream is withdrawn from the system through conduit 10a. The remaining portion of the oxygen-rich stream can either be recovered for chemical use, recovered for refrigerant value, vented to the atmosphere, or bottled and sold for industrial uses. Vaporized natural gas is withdrawn from gas vaporization and air liquefaction Zone 1 through conduit 12. The vaporized natural gas is also passed to heat exchanger 13 wherein it additionally, in indirect heat exchange, cools the cornpressed air stream from air compressor 5. A portion of the vaporized natural gas ows through conduit 1'4 to partial combustion zone 11. The relative amounts of natural gas and oxygen ilowing to partial combustion zone 11 are regulated by means of control valves 1S and 16, respectively. By simple stoichiometric calculations the ratio of natural gas to oxygen for partial combustion can be conveniently calculated. After this ratio is determined, ilow ratio recorder controller 17 can be used to maintain the proper ratio. In partial combustion zone 11, the natural gas is partially burned to produce an intermediate gas which is rich in oxygen and carbon monoxide. Such processes are Well known in the art and have been used for many years in the manufacture of town gas. One such process is described in Petroleum Reiiner, vol. 38 (1959), No. ll, p. 294. The intermediate gas from partial cornbustion zone 11 is withdrawn through conduit 18. The intermediate gas is then passed to mixing zone 19. In mixing zone 19, the intermediate gas is mixed with controlled amounts of air which are added through conduit 20. The air stream in conduit 20 can be a portion of the compressed air stream from air compressor 5. The remaining portion Iof the vaporized natural gas from conduit 12 is also added to mixing zone 19 through conduit 21. The exact amounts of the intermediate gas, vaporized natural gas and air that are added to mixing zone 19 is very critical. By carefully controlling the various amounts of intermediate gas, vaporized natural gas and air that are added to the mixing zone 19, it is possible to produce a nal gas having a desired heating value and specific gravity. The determination of the proper amounts of the various components to be added to mixing zone 19 is accomplished by continuously sampling a small portion of the mixed gas that is withdrawn from mixing zone 19 through conduit 22. A small amount of the mixed gas is withdrawn through conduit 23 and passed to densitometer 24. In densitometer 24, the density or specic gravity is determined and a signal proportional to the specific gravity is passed to computer 25. The heating value or B.t.u. content of the mixed gas from mixing zone 19 is determined by withdrawing a small portion of the gas through conduit 26 and passing it to a calorimeter 27. A signal proportional to the B.t.u. content of the gas is passed from calorimeter 27 to computer 25. Computer 25 effectively controls the amounts of air and vaporized natural gas that are added to mixing zone 19. Since the various gaseous streams entering mixing zone 19 have different specific gravities or densities, it is easily seen that computer 2S serves to control the specific gravity of the nal gas product in conduit 22. Since the intermediate gas entering mixture zone 19 through conduit 18 is very rich in hydrois easily seen that when the B.t.u. value of the gas in conduit 22 falls below the desired level, computer 25 sends a signal to flow ratio recorder controller 28 which resets ow control valve 29 and allows more vaporized natural gas (which gas itself has a specific gravity in the range desired for the nal product) to enter mixing zone 19. Since the vaporized natural gas has a higher B.t.u. content than the intermediate gas entering the mixing zone 19, the B.t.u. content of the gas will be increased. Conversely, if the B.t.u. content of the gas rises above the predetermined limits, computer 25 sends a signal to ow ratio recorder controller 28 which resets iiow control valve 29, thus decreasing the amount of vaporized natural gas entering mixing zone 19. Thus, it is seen that the combination of densitometer 24, computer 25 and calorimeter 27 furnish a unique method of controlling both the specific gravity and the B.t.u. content of the linal gas product. By this process, it is possible to adjust the heating value and the specific gravity of the fina] product to maintain the desired values for these properties. Various components that can be used in the apparatus described above are well known in the art and -have not been described in detail here. It is understood that various heat exchangers, gas compressors, etc., not shown in the drawing, may be necessary for actual operation of my invention. Gas flowing through conduit 22 can be added directly to gas distribution `mains or it can be passed to a suitable storage vessel. Thus, it is evident, that by utilizing this process it is possible to operate in a continuous process to produce a gas product having a predetermined heating value and a predetermined specific gravity. The following example is included to show various operating conditions and stream compositions of the process. Also, two or more units of the invention can be used in parallel.
EXAMPLE The apparatus shown in the drawing is used to produce a town gas having a gross heating value of 500 B.t.u. per standard cubic foot with a gas specific gravity of 0.55 (air is 1.00). Liquid methane is supplied through conduit 2 at a temperature of 250 F. Partial combustion zone 11 is operated at a temperature of 2100 F. and at a pressure of 450 p.s.i.a. The catalyst utilized in the partial combustion zone is granular magnesite with a 3 percent by weight nickel content. The resulting gas product is passed through a desiccant and then is added directly to the gas distribution lines or to a suitable gas storage vessel. The following table illustrates various stream compositions, B.t.u. content, and specific gravity measurements that are found in the process of this invention.
B.t.u.:Britsh thermal unit; ser.:standardlcubiclteet gen, it is less dense than the vaporized natural gas or the iinal gas product. Similarly, air entering mixing zone 19 through conduit 20 is more dense than the final gas product in conduit 22. When the density of the gas in conduit 22 is too great, computer 25 sends a signal to ow ratio recorder controller 28 that will decrease the amount of yair 'flowing through conduit 20 by means of flow control valve 30. Conversely, when the density of the gas in conduit 22 decreases below the predetermined limit, computer 25 serves to add more air by means of ilow ratio recorder controller 28 and tlow control valve 30. Also, it
As will be evident to those skilled in the art, many variations and modications of the invention can be practiced in view of the foregoing disclosure. Such variations and modifications are believed to come within the spirit and scope ofthe invention.
I claim:
1. Method for reducing the heating value of a liqueed natural gas comprising:
(a) vaporizing said liqneed natural gas in a vaporizing zone by passing air in indirect heat exchange therewith, said air being liqueed;
(b) separating an oxygen-rich stream from said liquelied air;
(c) removing a vaporized natural gas stream from said vaporizing zone;
(d) passing a portion of said vaporized natural gas stream and at least a portion of said oxygen-rich stream to a combustion zone;
(e) partially combusting the vaporized natural gas in said combustion zone to produce hydrogen and carbon monoxide as an intermediate gas product;
(f) passing said intermediate gas product from said combustion zone to a mixing zone;
(g) passing air and at least a portion of the remainder of said vaporized natural gas stream of step (c) to said mixing zone, the amount of air and said vaporized natural gas added to said mixing zone being suiiicient to produce a gaseous mixture having a predetermined specic gravity and a predetermined heating value lower than said liquefied natural gas; and (h) recovering said gaseous mixture. 2. The method according to claim 1 further comprising cooling the air before introduction into said vaporizing zone by passing in indirect heat exchange relationship with said oxygen-rich stream and said vaporized natural gas stream.
3. The method according to claim 1 wherein suicient air and vaporized natural gas are added to said mixing Zone to produce a gaseous mixture having a specific gravity of 0.55 and a gross heating value of 500 B.t.u. per standard cubic foot.
4. The method according to claim 1 further comprising:
(a) measuring the specilic gravity of said gaseous mixture and producing a rst signal representative thereof;
(b) controlling the addition of air to said mixing zone in response to said rst signal so that, as the specilic gravity of said gaseous mixture increases above a predetermined level, the amount of air added to said mixing zone is decreased and, as the specific gravity of said gaseous mixture decreases below a predetermined level, the amount of air added to said mixing zone is increased;
(c) measuring the B.t.u. value of said gaseous mixture and producing a second signal representative thereof; and
(d) controlling the addition of vaporized natural gas to said mixing zone in response to said second signal so that, as the B.t.u. value of said gaseous mixture increases above a predetermined level, the amount of vaporized natural gas added to said mixing zone is decreased and, as the B.t.u. value of gaseous mixture decreases below a predetermined level, the amount of vaporized natural gas added to said mixing zone is increased.
5. A system for reducing the heating value of liquefied natural gas and maintaining the thus-treated product at a predetermined specific gravity comprising, in combination:
(a) means for vaporizing said liquefied natural gas by passing air in indirect heat exchange relationship therewith so that said air is at least partially liqueed;
(b) means for separating an oxygen-rich stream from said liquefied air;
(c) a combustion means for partially combusting vaporized natural gas in oxygen to produce an intermediate gas product containing hydrogen and carbon monoxide;
(d) first conduit means for passing at least a portion of said oxygen-rich stream to said combustion means;
(e) second conduit means for passing a portion of the vaporized natural gas from said vaporizing means to said combustion means;
(f) a mixing means;
(g) third conduit means for passing said intermediate gas product from said combustion means to said 'mlXllg means;
(h) fourth conduit means having a i'irst control means disposed therein for introducing controlled amounts of air into said mixing means;
(i) fth conduit means having a second control means disposed therein for introducing controlled amounts of a portion of said vaporized gas from said Vaporizing means to said mixing means;
(j) sixth conduit lmeans for withdrawing a gaseous mixture from said mixing means;
(k) means for measuring the specific gravity of said gaseous mixture passing through said sixth conduit means and producing a first signal representative thereof;
(l) means for manipulating said first control means in response to said first signal so that the amount of air added to said -mixing means is suliicient to maintain the specic gravity of said gaseous mixture at a predetermined level;
(rn) means for measuring the B.t.u. level of said gaseous mixture passing through said sixth conduit means and producing a second signal representative thereof; and
(n) means for manipulating said second control means in response to said second signal so that the amount of vaporized natural gas added to said mixing means is suiicient to maintain the B.t.u. value of said gaseous mixture in said sixth conduit at a predetermined level.
6. A system according to claim 5 wherein said means for measuring specic gravity is a densitometer.
7. A system according to claim 5 wherein said means forrneasuring B.t.u. is a calorimeter.
References Cited UNITED STATES PATENTS 2,547,970 4/ 1951 Phillips et al. 2,557,171 6/1951 Bodle et al. 48-196 XR 3,057,706 10/1962 Marshall et al 48-196 3,241,933 3/1966 Ploum et al. 48-196 3,285,719 11/1966 Bodle et al. 48-196 XR MORRIS O. WOLK, Primary Examiner.
R. E. SERWIN, Assistant Examiner.
U.S. Cl. X.R.
US44126165 1965-03-19 1965-03-19 Manufacturing town gas from liquefied natural gas Expired - Lifetime US3419369A (en)

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US3721253A (en) * 1971-09-24 1973-03-20 Phillips Petroleum Co Controlling apparatus and method
US4277254A (en) * 1980-02-15 1981-07-07 Energy Systems, Incorporated Control system and apparatus for producing compatible mixtures of fuel gases
US5232467A (en) * 1992-06-18 1993-08-03 Texaco Inc. Process for producing dry, sulfur-free, CH4 -enriched synthesis or fuel gas
US5394686A (en) * 1992-06-26 1995-03-07 Texaco Inc. Combined power cycle with liquefied natural gas (LNG) and synthesis or fuel gas
US20050126220A1 (en) * 2003-12-15 2005-06-16 Ward Patrick B. Systems and methods for vaporization of liquefied natural gas
US20070151988A1 (en) * 2005-12-14 2007-07-05 Saucedo Victor M Constant pressure delivery vessel and system
EP2282017A1 (en) * 2009-01-26 2011-02-09 Siemens Aktiengesellschaft Synthesis gas combustion system with dual fuel addition and method for operating a synthesis gas combustion system

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US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
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US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US2547970A (en) * 1948-02-28 1951-04-10 Phillips Petroleum Co Controlling heating valve of natural gas
US3057706A (en) * 1958-06-25 1962-10-09 Conch Int Methane Ltd Adjusting the heating value and specific gravity of natural gas
US3241933A (en) * 1961-08-17 1966-03-22 Conch Int Methane Ltd Process for the reforming of natural gas
US3285719A (en) * 1963-05-23 1966-11-15 Ofw xx

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3721253A (en) * 1971-09-24 1973-03-20 Phillips Petroleum Co Controlling apparatus and method
US4277254A (en) * 1980-02-15 1981-07-07 Energy Systems, Incorporated Control system and apparatus for producing compatible mixtures of fuel gases
US5232467A (en) * 1992-06-18 1993-08-03 Texaco Inc. Process for producing dry, sulfur-free, CH4 -enriched synthesis or fuel gas
EP0574633A1 (en) * 1992-06-18 1993-12-22 Texaco Development Corporation Dry, sulfur-free, methane-enriched synthesis or fuel gas
US5394686A (en) * 1992-06-26 1995-03-07 Texaco Inc. Combined power cycle with liquefied natural gas (LNG) and synthesis or fuel gas
US20050126220A1 (en) * 2003-12-15 2005-06-16 Ward Patrick B. Systems and methods for vaporization of liquefied natural gas
US7299655B2 (en) * 2003-12-15 2007-11-27 Bp Corporation North America Inc. Systems and methods for vaporization of liquefied natural gas
CN1894537B (en) * 2003-12-15 2010-06-09 Bp北美公司 Systems and methods for vaporization of liquefied natural gas
US20070151988A1 (en) * 2005-12-14 2007-07-05 Saucedo Victor M Constant pressure delivery vessel and system
EP2282017A1 (en) * 2009-01-26 2011-02-09 Siemens Aktiengesellschaft Synthesis gas combustion system with dual fuel addition and method for operating a synthesis gas combustion system
WO2010084040A3 (en) * 2009-01-26 2011-03-03 Siemens Aktiengesellschaft Synthesis gas-based fuel system including admixture of a second fuel, and method for the operation of a synthesis gas-based fuel system

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