US3312073A - Process for liquefying natural gas - Google Patents

Process for liquefying natural gas Download PDF

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US3312073A
US3312073A US415723A US41572364A US3312073A US 3312073 A US3312073 A US 3312073A US 415723 A US415723 A US 415723A US 41572364 A US41572364 A US 41572364A US 3312073 A US3312073 A US 3312073A
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gas
stream
natural gas
well head
vessel
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Jackson Robert Glover
Harmens Alexander
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Conch International Methane Ltd
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Conch International Methane Ltd
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    • 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
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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"
    • F25J1/0035—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 gas expansion with extraction of work
    • 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"
    • F25J1/0035—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 gas expansion with extraction of work
    • F25J1/0037—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 gas expansion with extraction of work of a return stream
    • 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
    • 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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/70—Heating the adsorption vessel
    • 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
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/32—Compression of the product stream
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons

Definitions

  • This invention relates to a process for producing a supply of liquefied natural gas at a lower pressure than that at which the natural gas is available while delivering a second supply of natural gas into a distribution pipeline at an intermediate pressure.
  • US. Patent No. 1,747,761 describes a process in which one stream of high pressure natural gas from the Wells is expanded in an expansion machine to cool the gas which is then heat exchanged with a second stream of high pressure gas from the wells and then delivered to the distribution pipeline, and the cooled second stream is itself expanded in an expansion machine to liquefy part of it, the remainder going to storage or to a distribution pipeline.
  • German Patent No. 951,751 describes a similar process with the added refinement that the gas separated at the liquefaction stage (hereinafter called flash gas) is used to cool further the already cooled second stream prior to its expansion.
  • the present invention provides a process for producing a supply of liquefied natural gas at a lower pressure than that at which the natural gas is available while delivering a second supply of natural gas into a distribution pipeline at an intermediate pressure which comprises the following steps:
  • step (f) isenthalpically expanding the second stream from step (e) to produce liquefied natural gas and flash gas
  • step (g) passing the flash gas firstly to step (e) and then to step (c) to effect the cooling in those steps and finally compressing it to the intermediate pressure and passing it into the distribution pipeline.
  • Step (g) Work produced in the isentropic expansions, which may take place in any suitable type of expansion machine, may be used to provide some of the compression energy required in step (g). Generally some additional comp-ression energy will have to be provided but the amount will depend upon a number of factors, such as the pressure at which the natural gas is available, the required intermediate pressure and the proportion of natural gas which is required in liquid form.
  • isentropic expansion is used to mean expansion with external work although, of course, it is appreciated that theoretically expansion with external work is only isentropic if the expansion machine used is efiicient.
  • step (a) the isentropic expansion and resulting cooling in step (a) will normally cause methane hydrates to form in the natural gas and these may be separated, decomposed and the Water removed from the system before step (b) with the result that the first stream of natural gas goes into the distribution pipeline substantially dryer than it was originally.
  • the second stream of natural gas is intended for partial liquefaction, it is necessary to remove all of the Water before the temperature becomes so low that hydrates or ice would form.
  • This can be achieved by passing the second stream through a dehydrating bed before it is cooled by the expanded first stream.
  • Dehydration may be achieved by activated alumina, silica gel, activated carbon, or other suitable molecular sieves.
  • Any carbon dioxide or hydrogen sulphide in the natural gas can be removed prior to the carrying out of the process of the present invention by any of the well-known absorption processes in, for example, alkali metal carbonate solutions, alkali metal hydroxide solutions or alkanolamine solutions. If, however, these contaminants are present only in small proportions they need not be removed prior to the process, but any solid carbon dioxide or hydrogen sulphide forming in the liquefied natural gas product can be separated, e.g. filtered or centrifuged, off.
  • FIG. I is a flow sheet illustrating the invention
  • FIG. II is a flow sheet illustrating a modified form of the invention.
  • the raw natural gas in the examples described with reference to FIG. I contained 95.2% methane, 3% ethane, 1% propane, butane and higher hydrocarbons, and 0.8% carbon dioxide on a dry basis.
  • the raw natural gas was saturated with water at F.
  • the raw natural gas in the example described with reference to FIG. 11 contained 90.2% methane, 3% ethane, 1% propane, butane and higher hydrocarbons, 5% nitrogen and 0.8%
  • the raw natural gas enters the installation from the wells via pipe 1 at 3,750 p.s.i.a. and 140 F. It is cooled to 90 F. in water cooler 2 and then passed to the water separator 3. Since the raw gas is originally saturated with water, some of this water will condense upon cooling in cooler 2 and will separate in vessel 3 and can be removed by way of pressure reduction valve 4.
  • a small proportion (0.007 mol percent) of solid methane hydrate is formed in this expansion step and is carried along with the gas through pipe 10 to the hydrate separator 11.
  • This hydrate separator contains a warming coil 12 heated by a small stream of gas flowing through pipe 13 and drawn off the main stream in pipe 5.
  • the quantity of warn gas passing through pipe 13 is controlled by control valve 6.
  • the relatively warm gas in coil 12 after melting the methane hydrates in vessel 11 is returned to the main gas stream via pipe 14
  • the water formed on decomposition of the hydrate is removed from the system via pressure reduction valve 15.
  • the second natural gas stream in pipe 9 which comprises 44.2% of the natural gas stream before division is passed through a bed of 2 0r 3 Angstrom molecular sieve in adsorber 19. This molecular sieve retains all the water in the gas stream.
  • the dry gas leaves the adsorber through pipe 20 at 100 F., is cooled to 75 F. in water cooler 21 and is then (in FIG. I) cooled to -36 F. in heat exchanger 17 giving up its heat to the expanded gas of the first stream.
  • Valve 45 is assumed to be closed.
  • the dried, cooled second stream leaves heat exchanger 17 through pipe 22 and passes through heat exchanger 23 in which it gives up heat to returning flash gas, as will be described in more detail below, and from which it emerges at 60 F. in pipe 24.
  • the gas at -60 F. from pipe 24 is passed through expansion machine 25 in which its pressure is reduced to 675 p.s.i.a. and its temperature to -117 F.
  • the gas emerging from the expansion machine 25 passes through pipe 26 to heat exchanger 27 in which it is cooled again against flash gas and from which it emerges in pipe 28 at a temperature of 135 F. It is then isenthalpically expanded through throttle valve 29 to a pressure of p.s.i.a. into flash vessel 30.
  • 44.8% of the gas stream passing through valve 29 condenses and the carbon dioxide in the stream solidifies to form a slurry in the condensate. 55.2% of the stream leaves the flash vessel 30 as cold flash gas at 257 P. which is virtually pure methane.
  • the slurry of solid carbon dioxide in the liquefied natural gas collecting in flash vessel 30 is pumped by pump 31 through a separator 32 in which the solid carbon dioxide is separated, e.g. in a cyclone separator.
  • the flash gas leaves the flash vessel 30 by pipe 40 and is fed into heat exchanger 27 to cool the second stream, as described above. If the flash gas was used in heat exchanger 27 at a temperature of 25'7 F. it would cause freezing of carbon dioxide on the heat exchange tubes, To avoid this, it is mixed with an approximately equal volume of warmer gas from blower 50 prior to entering the heat exchanger. The mixture of gases fed to the heat exchanger in pipe 51 is at -l91 F., which temperature will not cause freezing of carbon dioxide on the heat exchanger tubes.
  • the flash gases leave the heat exchanger by pipe 34 at 124 F. and are divided into two streams at point 35, approximately half flowing to blower 50 and the other half flowing to heat exchanger 23 in which it is further heated to 46 F. in cooling the second stream as described above.
  • the flash gas stream leaves heat exchanger 23 by pipe as and passes to compressor 37
  • the compressor is shown in the accompanying drawings as a single stage compressor in the interest of simplicity, in practice it will have a plurality of stages, say 5 with 4 intercoolers.
  • the gas emerges from the fifth stage at 1,030 p.s.i.a. and F. and is fed through pipe 38 to distribution pipeline 18.
  • gas may be taken 01f between suitable stages of compressor 37 for the purpose of reconditioning the molecular sieve in adsorber 19a.
  • adsorber 19 and adsorber 19:: are alternately switched into the system for gas purification purposes and out of the system for reconditioning.
  • a suitable arrangement for the reconditioning step is to withdraw about 3% of the gas after the first stage of compression when the gas is at 74 p.s.i.a. and 187 F.
  • This gas is taken ofl through pipe 39 and is heated to 450 F. by means of waste heat in heater 40. The hot gas then passes through pipe 41 into spent adsorber 19a for reconditioning the same.
  • the adsorber effluent leaving through pipe 42 may be used as fuel gas.
  • the reconditioning of the adsorbers may be carried out as follows.
  • adsorber 19 When adsorber 19 is spent it is taken out of the gas purification system and replaced in that system by reconditioned adsorber 19a.
  • the pressure in adsorber 19 which, when in operation, is 3,750 p.s.i.a. is let down to atmospheric pressure which releases part of the adsorbed water to the atmosphere,
  • the contamin' ants left behind on the molecular sieve are desorbed by the stream of hot natural gas from pipe 41 described above.
  • adsorber 19 After reconditioning, adsorber 19 has to be cooled down to ambient temperature before reinsertion into the gas purification system. This is achieved by passing a stream of cooled purified natural gas through the adsorber.
  • the expansion machines 44 and 25 do not produce enough power under the conditions of the above example to drive the compressor 37.
  • the additional power required is provided by a suitable engine 43.
  • the pressure required in the distribution pipeline 18 were less than the 1,030 p.s.i.a. referred to above then it may well be possible to operate the above described process without the use of external power.
  • step (c) of process (1) above may be heat exchanged against part of the second stream in parallel with the heat exchange of the remainder of the second stream with the expanded first stream in step (b).
  • step (b) By controlling the relative proportion of the said part of the second stream it is possible to vary the proportion of the incoming natural gas which will finish up in the liquid form.
  • heat exchanger 48 is interposed in the flash gas stream just upstream of the compressor.
  • the relative flows through heat exchangers 17 and 48 are controlled by valves 45, 46 and 47.
  • valve 47 When valve 47 is fully closed, valves 45 and 46 will be adjusted so that 44% of the second stream passes through heat exchanger 48 and 56% of the second stream passes through heat exchanger 17.
  • an input of 395 x 10 st. cu. ft./day of natural gas will produce 290 x 10 st. cu. ft./day partially purified pipeline gas for distribution at 1,030 p.s.i.a., 100 x 10 st. cu.
  • Expander 44 will generate 5,000 horsepower and compressor 37 consume 34,500 horsepower. Thus the power to be fed into the system by engine 43 will increase to 25,000 horsepower. Any intermediate condition can, of course, be attained by suitable adjustments of valves 45, 46 and 47.
  • the plant is adapted to apply the process of the present invention to a liquefied natural gas when it is desired to remove nitrogen from the gas.
  • the treatment of the natural gas before division into two streams is the same as in FIG. I.
  • the treatment of the first stream taken ofl through pipe 8 is also the same as in FIG. I.
  • the treatment of the second stream taken olf through pipe 9 is the same as in FIG. I up to pipe 26 carrying the gas emerging from expander 25, except that in the present case the beds 19 and 19a are designed so as to remove most of the carbon dioxide as well as the water.
  • pipe 26 leads directly to heat exchanger 27.
  • valve 26a (used to provide the previously described operation) is closed and valve 26b (previously closed) is opened.
  • the cold expanded natural gas in pipe 26 passes first to heat exchanger 52 and then through pipe 53 to the nitrogen adsorption unit 54. Before it enters the nitrogen adsorption unit, the natural gas is mixed with a controlled amount of liquefied natural gas from pipe 55 to lower its temperature sufficiently for efficient operation of the adsor tion unit.
  • the nitrogen adsorption unit 54 which, in the interest of simplicity, is not shown in detail is of the type described in British patent specification 12,480/63. It comprises at least two alternating adsorption columns containing a molecular sieve (3 Angstroms) which are alternately adsorbing nitrogen and being regenerated and a small column containing a heat accumulating bed in ac cordance with British patent specification 12,480/ 63 and which is operated in the manner described in that specifi- 6 cation to ensure that the gas emerging from the adsorption unit is at a substantially constant temperature.
  • a molecular sieve 3 Angstroms
  • the purified natural gas leaves adsorption unit 54 via pipe 56, then passes through heat exchanger 52 in which it is cooled by the gas leaving expander 25 and then passes through heat exchanger 27 in which it is further cooled by flash gas. It leaves heat exchanger 27 by pipe 28 and is then isenthalpically expanded through throttle valve 29 into flash vessel 30 when a considerable proportion of the gas liquefies.
  • the liquefied natural gas in flash vessel 30 is pumped by pump 31 to storage vessel 33 through pipe 57 and control valve 62.
  • Pipe 55 branches off from pipe 57 and some of the liquefied natural gas is directed to pipe 53 as has already been described.
  • the proportion of liquefied natural gas flowing through pipe 55 is controlled by control valve 58.
  • the flash gas leaves vessel 30 by pipe 49 and hence is passed through heat exchangers 27 and 23 and is thereafter treated as in FIG. I.
  • Warm gas for regeneration of the adsorption beds in the nitrogen adsorption unit 54 is supplied by pipe 60 branching off from pipe 39 and leaves the adsorption unit together with the desorbed nitrogen by pipe 61. If the natural gas contains helium as well as nitrogen, helium can be separated from the efiluent from pipe 61.
  • a process for producing from natural gas at high pressure a supply of liquefied natural gas at a lower pres sure than the high pressure at which the natural gas is available while delivering a second supply of natural gas into a distribution pipeline at an intermediate pressure which comprises (a) isentropically expanding a first stream of the natural gas from the high pressure at which it is available to the intermediate pressure and so cooling it,
  • step (f) isenthalpically expanding the second stream from step (e) to produce liquefied natural gas and flash gas
  • step (g) passing the flash gas firstly to setp (e) and then to step (c) to effect the cooling in those steps and finally compressing it to the intermediate pressure and passing it into the distribution pipeline.
  • step (a) methane hydrates formed in step (a) are separated and decomposed and the resulting water removed from the system before step (b).
  • step (g) A process as claimed in claim 4 in which warm purified natural gas produced in the compression operation referred to in step (g) is used to recondition the dehydration bed.
  • step (f) A process as claimed in claim 1 in which the flash gas from step (f) is mixed with warm flash gas before being passed to step (e).
  • step (c) A process as claimed in claim 1 in which the flash gas, after effecting the cooling in step (c), is heat exchanged against part of the second stream in parallel with the heat exchange of the remainder of the second stream with the expanded first stream in step (b).

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  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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US415723A 1964-01-23 1964-12-03 Process for liquefying natural gas Expired - Lifetime US3312073A (en)

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US3360944A (en) * 1966-04-05 1968-01-02 American Messer Corp Gas liquefaction with work expansion of major feed portion
US3376709A (en) * 1965-07-14 1968-04-09 Frank H. Dickey Separation of acid gases from natural gas by solidification
US3398544A (en) * 1966-07-27 1968-08-27 Continental Oil Co Solidification of acidic components in natural gas
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3503220A (en) * 1967-07-27 1970-03-31 Chicago Bridge & Iron Co Expander cycle for natural gas liquefication with split feed stream
US3657898A (en) * 1968-08-15 1972-04-25 Air Prod & Chem Method and apparatus for producing refrigeration
US3696637A (en) * 1968-08-15 1972-10-10 Air Prod & Chem Method and apparatus for producing refrigeration
US3724225A (en) * 1970-02-25 1973-04-03 Exxon Research Engineering Co Separation of carbon dioxide from a natural gas stream
US3735600A (en) * 1970-05-11 1973-05-29 Gulf Research Development Co Apparatus and process for liquefaction of natural gases
US3792590A (en) * 1970-12-21 1974-02-19 Airco Inc Liquefaction of natural gas
US3886756A (en) * 1972-05-10 1975-06-03 Air Prod & Chem Separation of gases
US3894856A (en) * 1969-07-22 1975-07-15 Airco Inc Liquefaction of natural gas with product used as adsorber
US3905201A (en) * 1969-08-12 1975-09-16 Union Carbide Corp Air separation with work expansion to high and low pressure rectification stages
US4004430A (en) * 1974-09-30 1977-01-25 The Lummus Company Process and apparatus for treating natural gas
US4822393A (en) * 1988-06-30 1989-04-18 Kryos Energy Inc. Natural gas pretreatment prior to liquefaction
USRE33408E (en) * 1983-09-29 1990-10-30 Exxon Production Research Company Process for LPG recovery
US20040055329A1 (en) * 2002-08-15 2004-03-25 Mathias James A. Process for cooling a product in a heat exchanger employing microchannels
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US20070017250A1 (en) * 2001-05-04 2007-01-25 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20070056317A1 (en) * 2003-02-07 2007-03-15 Robert Amin Removing contaminants from natural gas
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
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US20080282612A1 (en) * 2005-08-17 2008-11-20 Mathieu Andre De Bas Process and Apparatus for the Purification of Methane Rich Gas Streams
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US20110094263A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US20110094262A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US20150033792A1 (en) * 2013-07-31 2015-02-05 General Electric Company System and integrated process for liquid natural gas production
US20150107297A1 (en) * 2012-03-21 2015-04-23 1304338 Alberta Ltd. Temperature controlled method to liquefy gas and a production plant using the method
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
RU2671665C1 (ru) * 2017-12-20 2018-11-06 Андрей Владиславович Курочкин Установка сжижения природного газа и способ ее работы (варианты)
RU2673972C1 (ru) * 2017-12-26 2018-12-03 Андрей Владиславович Курочкин Комплекс для редуцирования, сжижения и компримирования природного газа (варианты)
US10254041B2 (en) * 2015-02-03 2019-04-09 Ilng B.V. System and method for processing a hydrocarbon-comprising fluid
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path
FR3142104A1 (fr) * 2022-11-21 2024-05-24 Engie Procédé et dispositif d’épuration en phase liquide de traces d’impuretés
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Cited By (59)

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Publication number Priority date Publication date Assignee Title
US3376709A (en) * 1965-07-14 1968-04-09 Frank H. Dickey Separation of acid gases from natural gas by solidification
US3360944A (en) * 1966-04-05 1968-01-02 American Messer Corp Gas liquefaction with work expansion of major feed portion
US3398544A (en) * 1966-07-27 1968-08-27 Continental Oil Co Solidification of acidic components in natural gas
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3503220A (en) * 1967-07-27 1970-03-31 Chicago Bridge & Iron Co Expander cycle for natural gas liquefication with split feed stream
US3657898A (en) * 1968-08-15 1972-04-25 Air Prod & Chem Method and apparatus for producing refrigeration
US3696637A (en) * 1968-08-15 1972-10-10 Air Prod & Chem Method and apparatus for producing refrigeration
US3894856A (en) * 1969-07-22 1975-07-15 Airco Inc Liquefaction of natural gas with product used as adsorber
US3905201A (en) * 1969-08-12 1975-09-16 Union Carbide Corp Air separation with work expansion to high and low pressure rectification stages
US3724225A (en) * 1970-02-25 1973-04-03 Exxon Research Engineering Co Separation of carbon dioxide from a natural gas stream
US3735600A (en) * 1970-05-11 1973-05-29 Gulf Research Development Co Apparatus and process for liquefaction of natural gases
US3792590A (en) * 1970-12-21 1974-02-19 Airco Inc Liquefaction of natural gas
US3886756A (en) * 1972-05-10 1975-06-03 Air Prod & Chem Separation of gases
US4004430A (en) * 1974-09-30 1977-01-25 The Lummus Company Process and apparatus for treating natural gas
USRE33408E (en) * 1983-09-29 1990-10-30 Exxon Production Research Company Process for LPG recovery
US4822393A (en) * 1988-06-30 1989-04-18 Kryos Energy Inc. Natural gas pretreatment prior to liquefaction
US7594414B2 (en) 2001-05-04 2009-09-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US7591150B2 (en) 2001-05-04 2009-09-22 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20060213223A1 (en) * 2001-05-04 2006-09-28 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20070017250A1 (en) * 2001-05-04 2007-01-25 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20100186446A1 (en) * 2001-05-04 2010-07-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
US20070137246A1 (en) * 2001-05-04 2007-06-21 Battelle Energy Alliance, Llc Systems and methods for delivering hydrogen and separation of hydrogen from a carrier medium
US7637122B2 (en) 2001-05-04 2009-12-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
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EP1478874A4 (en) * 2002-02-27 2007-09-12 Bechtel Bwxt Idaho Llc NATURAL GAS LIQUEFACTION APPARATUS AND ASSOCIATED METHODS
US20040055329A1 (en) * 2002-08-15 2004-03-25 Mathias James A. Process for cooling a product in a heat exchanger employing microchannels
US7000427B2 (en) * 2002-08-15 2006-02-21 Velocys, Inc. Process for cooling a product in a heat exchanger employing microchannels
US20100024472A1 (en) * 2003-02-07 2010-02-04 Woodside Energy Limited Removing Contaminants from Natural Gas
US20070056317A1 (en) * 2003-02-07 2007-03-15 Robert Amin Removing contaminants from natural gas
US20080282612A1 (en) * 2005-08-17 2008-11-20 Mathieu Andre De Bas Process and Apparatus for the Purification of Methane Rich Gas Streams
US8673056B2 (en) * 2005-08-17 2014-03-18 Gastreatment Services B.V. Process and apparatus for the purification of methane rich gas streams
WO2008064038A3 (en) * 2006-11-16 2008-08-28 Battelle Energy Alliance Llc Apparatus for the liquefaction of gas and methods relating to same
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US20090071634A1 (en) * 2007-09-13 2009-03-19 Battelle Energy Alliance, Llc Heat exchanger and associated methods
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
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US20110094262A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US8899074B2 (en) 2009-10-22 2014-12-02 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US10571187B2 (en) * 2012-03-21 2020-02-25 1304338 Alberta Ltd Temperature controlled method to liquefy gas and a production plant using the method
US20150107297A1 (en) * 2012-03-21 2015-04-23 1304338 Alberta Ltd. Temperature controlled method to liquefy gas and a production plant using the method
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path
JP2020003203A (ja) * 2013-07-31 2020-01-09 ゼネラル・エレクトリック・カンパニイ 液化天然ガス生成のためのシステム及び組み込みプロセス
US20150033792A1 (en) * 2013-07-31 2015-02-05 General Electric Company System and integrated process for liquid natural gas production
CN105408713B (zh) * 2013-07-31 2018-06-26 通用电气公司 用于液体天然气生产的系统和集成方法
WO2015017293A3 (en) * 2013-07-31 2015-08-27 General Electric Company System and integrated process for liquid natural gas production
JP2016532846A (ja) * 2013-07-31 2016-10-20 ゼネラル・エレクトリック・カンパニイ 液化天然ガス生成のためのシステム及び組み込みプロセス
CN105408713A (zh) * 2013-07-31 2016-03-16 通用电气公司 用于液体天然气生产的系统和集成方法
US10254041B2 (en) * 2015-02-03 2019-04-09 Ilng B.V. System and method for processing a hydrocarbon-comprising fluid
RU2671665C1 (ru) * 2017-12-20 2018-11-06 Андрей Владиславович Курочкин Установка сжижения природного газа и способ ее работы (варианты)
RU2673972C1 (ru) * 2017-12-26 2018-12-03 Андрей Владиславович Курочкин Комплекс для редуцирования, сжижения и компримирования природного газа (варианты)
US12234713B2 (en) 2022-06-29 2025-02-25 Cnx Resources Corporation Systems and method for efficient transport of fluid separators
FR3142104A1 (fr) * 2022-11-21 2024-05-24 Engie Procédé et dispositif d’épuration en phase liquide de traces d’impuretés
WO2024110449A1 (fr) 2022-11-21 2024-05-30 Engie Procédé et dispositif d'épuration en phase liquide de traces d'impuretés

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NL6500885A (cs) 1965-07-26

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