US3254496A - Natural gas liquefaction process - Google Patents

Natural gas liquefaction process Download PDF

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Publication number
US3254496A
US3254496A US270109A US27010963A US3254496A US 3254496 A US3254496 A US 3254496A US 270109 A US270109 A US 270109A US 27010963 A US27010963 A US 27010963A US 3254496 A US3254496 A US 3254496A
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natural gas
gas
liquid
cycle
refrigeration cycle
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Roche Yves Marie Bernard
D Avray Ville
Perret Jean Charles Armand
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D'ETUDE DU TRANSPORT ET de la VALORISATION DES GAZ NATURELS DU SAHARA Ste
TRANSP ET de la VALORISATION D
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TRANSP ET de la VALORISATION D
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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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0085—Ethane; Ethylene
    • 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
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    • 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
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    • 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"
    • F25J1/0045—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 vaporising a liquid return stream
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    • 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
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    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • this gas which contains the ma or part of' the more volatile neutral gases present 1n the natural gas, is employed as combustible gas after the sensible heat of the latter has been recovered if desired.
  • the object of the present invent-ion is to provide a process for liquefying natural gases containing more or less large amounts of more volatile neutral gases of the cascade type comprising a plurality of successive refrigeration cycles, said process comprising adding to said cascade an additional refrigeration cycle of the natural gas in which there is utilized as refrigerating fluid, in an open circuit, the combustible gas containing the major part of the more volatile neutral gases separated from the natural gas current in the course of the preceding liquefaction operations of this cascade.
  • More volatile neutral gases is intended to mean gases such as nitrogen, helium, argon etc. contained in the natural gas. In order to simplify the disclosure, they will be designated hereinafter by the simplified expression of neutral gases it being understood that carbon dioxide is not included therein since it is less volatile than the natural gas obtained at the end of the process.
  • FIG. 1 is a diagram of a plant for carrying out the process of the invention when the amount of neutral gas ice which remains in the liquefied natural gas at the outlet is not limited;
  • FIGS. 2 and 3 are plant diagrams of utility when the amount of neutral gas in the liquefied natural gas is limited to a given value
  • FIG. 4 is a diagram of a plant identical to that shown in FIG. 3 but including the separation of the neutral gas;
  • FIGS. 5 and 6 are plant diagrams for carrying out the invention comprising a stage for eliminating CO in the course of liquefaction;
  • FIG. 7 is a diagram of a plant for carrying out the process of the invention comprising a stage regulating the amount of nitrogen contained in the liquefied natural gas, and
  • FIGS. 8, 9, 10 and 11 represent diagrammatically a plant for storing the liquefied natural gas.
  • the current of natural gas under pressure is previously cooled, then condensed at a temperature in the neighbourhood of C. by conventional cascade or other processes, the pressure of the current of natural gas being determined so as to obtain the latter in the liquid state in the neighbourhood of this temperature. It enters the plant shown in FIGS. 1-4 and 6 at 1.
  • FIGS. 1, 2 and 3 Depending on the amount of more volatile neutral gas contained in the current of natural gas and that it is desired to maintain in the liquefied natural gas obtained by the process, one or the other of the plants shown in FIGS. 1, 2 and 3 is used.
  • the current of natural gas under pressure in theliquid state arriving at 1 is cooled in an exchanger E, which is the high pressure stage of the methane cycle for example of the aforementioned conventional cascade cycle, and passes through a point 2 before being expanded in a flash flask B
  • the expansion occurs between the pressure of point 2 and a presssure between 15 and 20 'kg./sq.cm.
  • This pressure is determined by the amount of neutral gas contained in the current of natural gas and by the amount of neutral gas maintained in the liquid natural gas.
  • the liquid part (issuing at 3) of the flask B is cooled in exchangers E and E which are the medium and low pressure stages of the same refrigerating cycle as the preceding one.
  • exchangers E and E which are the medium and low pressure stages of the same refrigerating cycle as the preceding one.
  • the natural gas is at a pressure of the same order of magnitude as that prevailing in the flash flask B and at a temperature in the neighbourhood of, but higher than, that of the methane boiling at the pressure of the exchanger E
  • the natural gas then passes through an exchanger E in shell 41: constituting an expansion zone and is obtained, at the outlet of this exchanger at 5, at a pressure in the neighbourhood of that prevailing in the flask flash B 15-20 kg.) and at a temperature equal to, or lower than, the boiling temperature of this same natural gas at atmospheric pressure.
  • the gaseous part of the flash leaving the flask B at 6 and which will be subsequently used as combustible gas passes through the exchanger E and the exchanger or liquefier E which are the medium and low pressure stages of the selected refrigeration cycle, and is partially or completely condensed at a point 7.
  • the gas-liquid mixture obtained at point 7 in a more or less large proportion passes through an exchanger E in shell or expansion zone 4a at the outlet of which at 8 the gas is already completely condensed and subcooled at the pressure substantially corresponding to that of the flash flask B
  • the liquid obtained is then expanded in the exchangers E and E to atmospheric pressure or a pressure slightly higher, depending on the amount of neutral gas containedin the combustible gas and the temperature conditions that are desired of the liquid natural gas issuing from the plant at 5.
  • the boiling temperature of this expanded liquid will vary continually in accordance with the liquid-vapour states 'of equilibrium obtained in the exchangers E and E
  • These exchangers are consequently of the vapour recycling and counter-current type. They are divided into successive compartments, the number of compartments being selected in accordance with the minimum approach speeds to be maintained between the current of liquid natural gas and the boiling liquid.
  • the vapours are mixed with the liquid overflowing from the compartment so that the gasliquid mixture feeding the following compartment is in a liquid-vapour equilibrium state.
  • the combustible gas in gaseous phase is conducted by a pipe 9 to the point of its use as fuel.
  • FIGS. 2 and 3 are practically identical, to within a few details, to the high pressure stage of the refrigeration cycle, for example the methane cycle, of the conventional cascade.
  • the current of natural gas under pressure in the liquid state arriving at 1 is cooled in the exchanger E, for example the high pressure stage of the methane cycle, then expanded in a denitrogenizing column V The expansion occurs between the pressure of point 2 and a pressure between 15 and 20 kg./sq.cm. This pressure is determined by the amount of neutral gas maintained in the liquid natural gas.
  • the liquid part of the bottom of the column V issuing at 3 is cooled in the exchangers E and E which are the medium pressure and low pressure stages of the same refrigeration cycle, for example methane cycle.
  • the natural gas is at a pressure of the same order of magnitude as that prevailing in the de-nitrogenizing column V and at a temperature in the neighbourhood of, but higher than, that of the methane boiling at the pressure of the exchanger E 1
  • the natural gas then passes through the exchanger E and is obtained at the outlet of this exchanger at 5 at a pressure in the neighbourhood of that prevailing in the de-nitrogenizing column V and at a temperature equal to or lower than the boiling temperature of this natural gas at atmospheric pressure.
  • the reflux from the column V issuing at 6, and which will subsequently be used as combustible gas, passes through the exchanger E and the exchanger or liquefier E which are the medium and low pressure stages of the selected refrigeration cycle.
  • the combustible gas is partially or entirely condensed at point 7, it is liquid and subcooled in the exchanger E
  • the entirely liquid combustible gas is expanded in the exchangers E and E, which are constituted in a manner similar to that previously described.
  • the plant shown in FIG. 3 differs from that shown in FIG.
  • the de-nitrogenizing column V by the operation of the de-nitrogenizing column V the latter being so calculated that the amount of neutral gas remaining in the bottom of the column and issuing at 3 is substantially nil, the totality of neutral gas being contained in the gaseous phase issuing at 6.
  • the high-pressure stage of the methane cycle is replaced for the natural gas by the redistillers of the denitrogenizing column V a flash flask B is used to obtain i the cooling of the methane of the refrigeration cycle for its utilization at the medium pressure stage.
  • the three plants (FIGS. 1, 2 and 3) just described permit obtaining by means of the process of the invention the natural gas liquefied under pressure and at a temperature which is equal to, or lower than, the boiling temperature of this natural gas at atmospheric pressure.
  • the advantage of the process is to increase the operational pressures of the low pressure and medium pressure stages of the refrigeration cycle preceding the cycle of the process.
  • the pressure of the liquefied natural gas permits transferring the liquid current from the works to the storage plant.
  • the subcooling of this liquid permits, by variation of its sensible heat, compensating the exterior supplies of heat, on one hand, in the transfer line and, on the other, in the storage plants, as will be explained hereinafter.
  • FIG. 4 shows a plant for carrying out the process of the invention which permits separating the neutral gases contained in the natural gas current and, if desired, increasing the helium content in the neutral gas so as to facilitate the subsequent separation thereof.
  • This plant is partly identical to that shown in FIG. 3, but the new elements could just as well [be combined with the plan-ts shown in FIG. 1 or FIG. 2.
  • the combustible gas extracted from the de-nitrogenizing column, at point 6 is partially recondensed in the exchanger E .fed by the low pressure stage of the refrigeration circuit, for example a methane circuit.
  • the liquid-vapour current is treated in a column V where the combustible gas is separated from the major part of the neutral gases it contains.
  • the Ibottom of the column V issuing at 10 passes through the exchanger or liquefier E which is the low pressure stage of the methane refrigeration circuit, and, in passing through the point 7, passes through the exchanger E7 of FIGS. 1-3 which is in this case constituted by two elements E and E
  • the liquid obtained at the outlet of the element Eq at 8 is separated into two currents, one of which supplies the head condenser of the column V through the point 11, Whereas the other directly supplies the exchangers E and Eq as well as E.,.
  • vapours of the neutral gases available at the outlet of this process are at the pressure chosen for the fractionation of the natural gas ⁇ current of the combustible gas (pressure of column contemplated concentration and temperature.
  • the process of the invention also permits eliminating by filtration in the course of liquefaction the CO present in the natural gas entering the plant.
  • the current of natural gas under pressure contains, in addition to the more volatile neutral gases, more or less large amounts of CO
  • this CO is eliminated from the natural gas current before liquefaction by washing with sodium hydroxide or ethanolamine.
  • the utilization of such processes for eliminating CO apart from their cost price, increases the working costs of the liquefaction of the natural gas.
  • the natural gas current is saturated with water at a temperature exceeding the surrounding temperature; therefore the plants for dehydrating the gas are considerably increased.
  • the process of the invention does not concern the formation of this precipitate but its elimination from the liquid current. It comprises eliminating by filtration the.
  • precipitate obtained by expansion of preferably the liquid in a flash flask.
  • the formation of the precipitate is continuous from the point of formation of the first crystal when the temperature of the liquid continues to drop.
  • the precipitate formed has a tendency to agglomerate into a mass which is compact but, however, fragile owing to the presence in the precipitate of heavier hydrocarbons,
  • the liquid obtained upon expansion in the flash flask contains a large amount of CO in the liquid state. This precipitate only decants when the speeds are substantially nil and it is filtered by passing it through a pad of glass wool, a plate of sintered metal or any other filtering material which resists the contemplated temperature conditions and stresses.
  • FIG. 5 shows a detail of the plant
  • Operation of the valves 17, 17a, 20, 28, 2-2, 25,27, 29, 26, 35 permits the alternative operation of the flash flask B or E
  • the flask B regenerating: the valve 17 is open, 17a closed, the liquid expanded in B is cooled and separates into a liquid fraction and a gaseous fraction.
  • all the CO precipitates, the CO being retained inside a filter 1-8 placed at the lower part of the flash flask.
  • the liquid natural gas is recovered toward the second expansion stage through the collector 19 through the medium of a valve '20 :which is open.
  • the gaseous phase issuing from flask B at 21 is conducted through an open valve 22 to a condenser 23.
  • the recondensed vapours issuing at 24 from the condenser 2-3 are re-injected into the expanding means 1'6 feeding the flask flask B through the valve 17.
  • valves .17, 20 and 22 are open
  • valves 25, 26, 27 and 28 being closed.
  • the flask B being in the regenerating condition, the regeneration is effected .by a supply of combustible gas heated to around 50 C. coming from the pipe 8 and passing, through an open valve 29, the filter of the flash flask B at counter-current.
  • the hot gas sublimates the CO deposited on the filter; the mixture gas-combustible+CO being sent toward the point of utilization through the pipe 31, a valve 35 being open, the end of the regeneration of the filter is '5 effected when the temperature at 34 tends to reach C.
  • FIG. 6 With reference to FIG. 6, there is shown a complete plant comprising the filtration of the carbon dioxide in two successive expansions.
  • Each expansion flaskor filter B and B provided with filters is diagrammatically represented by a single flask, whereas the device shown in FIG. 5 is adapted to one and the other.
  • the filtered liquid part is evacuated through the pipe 36 to the flash flask B and through the expansion orifice 37, the latter is expanded.
  • the filtered liquid issuing at 38 is the liquefied natural gas.
  • the vapour part of the flash flask B issuing at 39 passes through the exchanger E then E issues at 40 and a flask B permits the separation of non-condensed gas if desired, the liquid of the flask being sent into the flash flask B through a pipe 41 directly into the expanding means 16.
  • the flash vapour produced in the flask B is recondensed through a pipe 42 in theexchanger E reintroduced through a pipe 43 directly into the expanding means 37.
  • the whole of the diagram, apart from this additional element, is in conformity with that of the plant shown inFIG. 4.
  • the expansion can be effected in one or a plurality of stages depending on the amount of CO contained in the entering gas, the available heat in the refrigerating cycles and the temperatures at which these calories are available, thus fixing the vapour condensation pressures and the value of the expansion in the flash flask.
  • the condensation of the vapours of the flash is for its part a direct function of the percentage of nitrogen contained in the current of the entering natural gas.
  • the more these vapours are charged with neutral gas the more the recondensation of the vapours will require a refrigerating liquid having a low boiling point; now, the low boiling points are a direct function of the amountof neutral gases remaining in the combustible gas.
  • percentages of neutral gases in the entering natural gas of the order of 7% in mole the amount in the liquid gas cannot exceed 0.5%.
  • the reinjection of the condensed vapours through an injection nozzle placed at the expansion of the liquid to be cooled and filtered has for purpose to avoid the formation of solid deposits at the expansion orifice and consequently stopping up and to instantaneously reestablish the liquid-vapour equilibriumin the flask and thereby decrease to the maximum extent the neutral gas content of the formed vapour, which thus facilitates the recondensation of the latter.
  • the combustible gas which is entirely liquid at Point 8 is no longer expanded in the exchanger Eq but in a flash flask B the vapour part of the flash being conducted through a pipe 44 into the exchanger Eq
  • the liquid part is divided into three currents, one feeding through the pipe 11 the head condenser of the column V the second feeding the exchanger Eq the third mixed with the liquid coming from the flash flask B in a pipe 45 through a valve 46 being evacuated from the process through the pipe line 38.
  • a part of the liquid of the flash flask is thus mixed with the liquid issuing from the last filtration stage so that, by the mixture of these two liquids, the neutral gas content in the liquefied natural gas is increased.
  • a precise regulation of the amount of neutral gas mixed with the liquefied natural gas can thus be obtained, and this permits reducing by more than 50% the natural gas losses when storing.
  • FIGS. 8-11 show diagrammatically liquefied natural gas storage plants.
  • the liquefied natural gas feeds a storage reservoir from below at 51.
  • a buffer or layer of neutral gas such as that produced by the fractionating column V of the preceding plants.
  • This neutral gas, arriving at 52, is stored in a buifer reservoir constituted by a normal gasometer 53 connected to the liquid reservoir 51 at the upper end of the reservoir where an overpressure valve 54 permits moreover sending to the torch through 55 the over-pressure of neutral gas due to the filling or the overpressure of natural gas when the storage reservoir 51 is full; at this moment, the heat losses are no longer compensated by the sensible heat provided by the subcooled liquefied natural gas.
  • the collector 60 is connected to a gasometer 61 (FIG. 10) which receives neutral gases, such as those obtained by the process of the invention, the pressure excess in this gasometer 61 being sent to the torch through a pipe '62.
  • a gasometer 61 FIG. 10
  • Such a device is applicable to plants provided with a single storage reservoir or with a plurality of storage reservoirs fed in parallel.
  • a device of the type shown in FIG. 11 comprising a common collector 63 which connects the points 60 of the reservoir 51, 51 the gasometer 61.
  • the first reservoir is completely full, it is no longer possible to compensate the evaporations by the supply of sensible heat of the subcooled liquid natural gas.
  • the vapours produced in the course of the heating of the storage are therefore $61.11 9 the common collector whence they are drawn off in major part by the reservoir which is in course of being filled and reliquefied by the subcooled liquid natural gas inside this same reservoir.
  • This process of liquefaction of the vapours produced is applicable in the course of lodging a methane transporting ship.
  • the vaporations are in this case directed to the common collector of the storage reservoirs, the liquid natural gas produced by the works being then cooled at such temperature that these vapours can be in large part reliquefied in the storage reservoirs during the loading of a ship. Apart from the emanation at the start of loading, almost all the vapours can thus be reliquefied.
  • the liquefaction process of the invention thus permits materially improving the liquefaction, the refining, and the storage of natural gases.

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US3331213A (en) * 1964-06-17 1967-07-18 Conch Int Methane Ltd Process for the separation of gaseous mixtures employing a product as refrigerant
US3340699A (en) * 1965-06-11 1967-09-12 Little Inc A Cryogenic condenser with liquid level sensing and control
US3377812A (en) * 1964-03-10 1968-04-16 British Oxygen Co Ltd Rearrangement of flow-thru serial adsorbers to remove gaseous constituents
US3407614A (en) * 1966-12-19 1968-10-29 Phillips Petroleum Co Helium purification
US3596472A (en) * 1967-12-20 1971-08-03 Messer Griesheim Gmbh Process for liquefying natural gas containing nitrogen
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US4824732A (en) * 1983-05-11 1989-04-25 Cinpres Limited Process and apparatus for injection moulding and mouldings produced thereby
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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
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US3377812A (en) * 1964-03-10 1968-04-16 British Oxygen Co Ltd Rearrangement of flow-thru serial adsorbers to remove gaseous constituents
US3331213A (en) * 1964-06-17 1967-07-18 Conch Int Methane Ltd Process for the separation of gaseous mixtures employing a product as refrigerant
US3340699A (en) * 1965-06-11 1967-09-12 Little Inc A Cryogenic condenser with liquid level sensing and control
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US3653220A (en) * 1969-05-09 1972-04-04 Airco Boc Cryogenic Plants Cor Process for helium recovery and purification
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LU43449A1 (zh) 1963-05-29
BE630256A (zh)
FR1331960A (fr) 1963-07-12
DE1267236B (de) 1968-05-02
NL291145A (zh)
GB996929A (en) 1965-06-30

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